Polymerization reaction kettle and application thereof

Abstract

The invention provides a polymerization reaction kettle. The polymerization reaction kettle comprises a polymerization kettle body, a bottom stirring shaft and a top extension stirring shaft, a bottom stirring paddle is arranged on the bottom stirring shaft; a helical ribbon paddle is arranged on the bottom stirring paddle; a frame type paddle is arranged on the helical ribbon paddle; a top extending stirring shaft is arranged in the polymerization kettle body, an axial flow stirring paddle is arranged on the top extending stirring shaft, a detachable jacket is lined in the polymerization kettle body, a ventilation pipeline is arranged on the jacket, and gas hole channels are dispersed in the jacket and are communicated with the ventilation pipeline. The polymerization reaction kettle provided by the invention can adapt to the characteristics of large viscosity change, complex phase change, high requirement on material mixing uniformity and the like in the polyolefin production process, and meanwhile, liquid nitrogen or a carbon monoxide killing agent can be introduced into the polymerization reaction kettle through the ventilation pipeline on the jacket; and the gas is fully mixed with a liquid-phase reaction medium in the polymerization reaction kettle through a gas hole channel on the jacket, so that the polymerization reaction kettle is timely cooled and the reaction is quickly terminated.

Description

TECHNICAL FIELD

[0001] The present application relates to a reaction device, in particular to a reaction kettle for producing high-viscosity polymerization system. BACKGROUND

[0002] The stirring type polymerization reaction device is one of the most widely used reactor forms in the current chemical polymerization process. The reactants, catalysts, solvents and other materials can realize strong momentum, heat and mass transfer performance in the stirring type polymerization reaction device, and flexible operation and enhanced mixing effect can be realized.

[0003] In the process of synthesizing polyolefin resin by solution method, the monomers, catalysts, polymers and other materials involved will change in many phases as the reaction proceeds. For example, in the early stage of polymerization, the concentration of polymerization product is low at this time, and the system mainly contains polymerization monomers, and the apparent viscosity of the system is low. As the polymerization degree increases, the concentration of monomers gradually decreases, the concentration of polymers gradually increases, and the apparent viscosity of the system increases. In the later stage of polymerization reaction, the concentration difference between the polymer and the monomer is large, which leads to the melting state of the system, and the polymer even has swelling phenomenon. At this time, the system presents strong non-Newtonian property, and the difficulty of reaction heat removal and mixing increases significantly. Therefore, the polymerization reaction kettle used in the solution method olefin polymerization process should meet the following requirements: first, the rapid mixing of catalysts, monomers and other materials in the initial state, which ensures that the catalyst is not accumulated in a local place, causing the polymerization explosion in the later stage of reaction; second, the heat transfer capacity of the reaction device decreases after the viscosity increases significantly in the later stage of reaction, and the operation and structure of the stirrer are adjusted to ensure that the stirrer is always in a state of high heat transfer capacity.

[0004] In the later stage of polymerization reaction, due to the continuous increase of the viscosity of the polymerization system, the polyolefin swells and sticks in the olefin monomer or the reaction solvent, and the viscosity of the system can reach 10 6 -10 7 cp, the mass transfer of the system is greatly affected, and the catalyst is also affected by the limited mass transfer, which causes uneven concentration distribution of the catalyst in the polymerization kettle, aggregation of the catalyst, polymerization explosion, temperature overrun of the reaction kettle, and rapid heat removal of the polymerization kettle. The traditional kettle type reactor cannot meet the needs of industrial rapid heat removal, and the external circulation heat removal is easy to cause the blockage of the external circulation pipeline due to the too large viscosity of the system. The new type of flash evaporation heat removal will cause large changes in the pressure of the polymerization system due to the need to reduce the pressure of the system, and thus it is difficult to maintain the steady state of the polymerization system. Therefore, it is necessary to seek a reaction device and method suitable for rapid heat removal of the super high viscosity polymerization system.

[0005] When the reaction system is run away, the reaction temperature exceeds the upper limit, and the reaction system needs to be terminated in time, mainly by adding carbon monoxide and other gaseous killing agents, but the gaseous killing agent is not fully dissolved and uniformly dispersed in the solution polymerization process, which causes the termination of the polymerization system to be invalid, therefore, it is necessary to seek a feeding method that can quickly and uniformly mix the gaseous termination agent with the solution polymerization system.

[0006] Chinese patent CN104941557A discloses a polymerization reactor, the stirring paddle is provided with a liquid guide plate, which can make the material move in the plane layer, solve the problem that the material is stuck on the stirring shaft, and the cleaning after shutdown is difficult, the bottom of the reactor is set as a 45° inclined conical bottom, which can make the impurities generated in the reaction pass through the discharge port and out of the bottom, the discharge port is provided with a material collecting pit, and a screen is arranged between the cylinder and the bottom plate, the material collecting pit and the screen can separate the material and impurities at the discharge port, and improve the self-pollution removal capacity of the polymerization reactor, thereby saving the cost of manual or mechanical cleaning of the polymerization reactor, the polymerization reactor has the advantages of good energy-saving effect and good pollution removal effect, and has a wide market prospect. Although the stirring paddle with the liquid guide plate can make the material move in the plane layer and reduce the residue of the material on the stirring shaft, it is difficult to realize the up-down mixing of the high-viscosity material in the reactor and the overall circulation of the material, and the mixing is insufficient.

[0007] Chinese patent CN104941557A discloses a polypropylene polymerization reactor, which comprises a reactor body composed of a first part, a second part and a third part from top to bottom, the first part and the third part are both hemispherical, the second part is cylindrical, a first opening is arranged on the inner side wall of the upper part of the second part along the circumferential direction thereof; a stirring device comprising a rotating shaft, a plurality of stirring blades, at least one cross bar, the cross bar being fixedly connected to one end of the rotating shaft and penetrating through the first opening, two baffles, one of the baffles being arranged in the hollow part between the inner side wall and the outer side wall of the second part, and the other baffle being arranged in the second part, and a plurality of brush rods arranged in the hollow part between the inner side wall and the outer side wall of the second part. The invention is suitable for low-viscosity systems of propylene polymerization, but for high-viscosity materials, due to the large viscosity of the system, the shear force is too large during stirring, and the stirring paddle in the reactor can only realize parallel stirring of the material, and up-down circulating stirring is difficult to realize.

[0008] Chinese patent CN220238291U discloses a stirring device for polymerization reaction, comprising a stirring tank, a stirring shaft and a stirring paddle, the stirring paddle is composed of a support rod, a double helical paddle, a turbine paddle and an anchor paddle, the stirring shaft is provided with a plurality of support rods in parallel from top to bottom, the end of the support rod is connected with the double helical paddle, and the ends of the lowermost support rod are also connected with the anchor paddle; the turbine paddle is arranged on the support rod body and / or the stirring shaft, and the paddle blade of the turbine paddle is an inclined blade. Although this technology can be used for uniform dispersion and mixing of materials in the polymerization process, it cannot realize effective and rapid mass transfer and heat removal of high-viscosity materials and timely termination of reaction.

[0009] Chinese patent CN209020351U discloses an automatic stirring type autoclave, comprising a kettle body, a top cover, support legs, a feeding pipe, a discharging pipe, a motor located above the top cover and a stirring shaft driven by the motor, a flowmeter is arranged on the feeding pipe, a pressure gauge is connected with a pressure sensor, the motor is connected with a speed reducer, the speed reducer is connected with the stirring shaft located in the kettle body through a transmission shaft, one side of the transmission shaft is connected with a liquid guide pipe, one end of the liquid guide pipe is provided with a liquid pump, a double helical-frame paddle is arranged on the stirring shaft, the transmission shaft, the stirring shaft and the double helical-frame paddle are hollow structures, liquid outlets are arranged on the stirring shaft and the double helical-frame paddle, electromagnetic heating coils and cooling pipes are arranged at intervals on both sides of the kettle body, a discharging pipe is arranged at the center position below the kettle body, and support legs are arranged below the kettle body. However, this technology cannot realize forced mass transfer and rapid heat removal of high-viscosity polymer materials. SUMMARY

[0010] In order to ensure rapid mixing and uniform dispersion of catalyst, monomer and other materials in the initial state of polymerization reaction, thereby reducing the phenomenon of polymerization explosion in the later stage of reaction, and to solve the problem of heat transfer capacity decline caused by significant increase in viscosity of the system in the later stage of polymerization reaction, the stirrer is adjusted in operation and structure to ensure that the stirrer is always in a condition of high heat transfer capacity, and to effectively solve the problem of reaction temperature overrun caused by polymerization explosion in the later stage of the reaction kettle, ensure rapid heat removal of the reaction kettle and rapid termination of the reaction. The present application provides a polymerization reactor suitable for high-viscosity fluid or solid-like material. The polymerization reactor provided by the present application can adapt to the characteristics of large viscosity change, complex phase change, high mixing uniformity requirement and the like in the production process of polyolefins, and the polymerization reactor can pass liquid nitrogen or carbon monoxide killing agent through the gas pipeline on the jacket, mix with the liquid phase reaction medium in the polymerization reactor through the gas hole on the jacket, and ensure timely heat removal and rapid termination of the reaction of the polymerization reactor.

[0011] In order to meet the needs of sufficient mixing of materials, efficient mass transfer and heat transfer, and quick heat removal and timely termination of reaction when the reaction is out of limit in the process of olefin polymerization, the present application provides a polymerization reactor, which comprises a polymerization reactor body, a bottom stirring shaft and a top stretching stirring shaft, the bottom stirring shaft is provided with a bottom stirring paddle, the bottom stirring paddle is provided with a ribbon paddle, the ribbon paddle is provided with a frame paddle, the top stretching stirring shaft is provided with an axial flow stirring paddle, the inside of the polymerization reactor body is lined with a detachable jacket, the jacket is provided with a vent line, the inside of the jacket is dispersed with gas channels, and the gas channels are communicated with the vent line.

[0012] In an embodiment, the diameter of the jacket is 0.85-0.95 times the diameter of the polymerization reactor.

[0013] In an embodiment, the bottom stirring shaft vertically extends into the polymerization reactor from the bottom of the polymerization reactor.

[0014] In an embodiment, the diameter of the bottom stirring paddle is 0.85-0.95 times the diameter of the polymerization reactor body.

[0015] In an embodiment, the ribbon paddle is located above the bottom stirring paddle to promote the flow and mixing of materials in the polymerization reactor.

[0016] In an embodiment, the ribbon paddle has two blades, the generatrix of each blade presents a spiral line, and the two blades are centrally symmetric about the axis of the bottom stirring shaft.

[0017] In an embodiment, the maximum diameter of the projection of the ribbon paddle in the vertical direction is the same as the diameter of the bottom stirring paddle, and is 0.85-0.95 times the diameter of the polymerization reactor body, and the pitch of the spiral generatrix of each blade is 0.5 times the diameter of the ribbon paddle to 1 times the diameter of the ribbon paddle.

[0018] In an embodiment, the cross-sectional shape of the frame paddle is cylindrical or rectangular, which is fixed on the blade of the ribbon paddle by welding or other methods, and plays the role of mixing materials and fixing support, and its size depends on the size of the ribbon paddle and the bottom stirring paddle. The bottom stirring shaft, the bottom stirring paddle, the ribbon paddle and the frame paddle together constitute the bottom stirrer of the polymerization reactor; the top stretching stirring shaft and the axial flow stirring paddle arranged on the top stretching stirring shaft together constitute the top stirrer of the polymerization reactor.

[0019] In an embodiment, the rotation directions of the bottom stirrer and the top stirrer can be the same or opposite.

[0020] In an embodiment, the ratio of the rotation speeds of the bottom stirrer and the top stirrer is 0.3-1.

[0021] In an embodiment, the top-stretching stirring shaft is vertically stretched into the polymerization reactor from the top of the polymerization reactor.

[0022] In an embodiment, the number of the axial-flow stirring paddles is 2-6, and the axial-flow stirring paddles are arranged from top to bottom on the top-stretching stirring shaft.

[0023] In an embodiment, when the number of the axial-flow stirring paddles is multiple, the diameters of the axial-flow stirring paddles are equal, the diameter of the axial-flow stirring paddle is 0.3-0.7 times of the diameter of the polymerization reactor, the number of the blades on each axial-flow stirring paddle is 2-4, and each blade is uniformly distributed about the axis of the top-stretching stirring shaft; the ratio of the distance between the bottom axial-flow stirring paddle and the bottom of the polymerization reactor to the diameter of the polymerization reactor is 0.15-0.3; and the ratio of the distance between two adjacent axial-flow stirring paddles to the diameter of the axial-flow stirring paddle is 0.3-1.5.

[0024] In an embodiment, the gas channels of the jacket are uniformly distributed on the inner walls of the front, rear, left and right of the jacket, and the number of the gas channels on each inner wall is 10-20, and the diameter of the gas channel is 3-5 mm.

[0025] In an embodiment, the gas channels are each provided with a cap, and the cap is in a closed state in the case of no gas passing, so as to prevent the material from entering the gas channel and causing blockage.

[0026] The application also provides a method for olefin polymerization reaction, which uses the above polymerization reactor.

[0027] The olefin includes, but is not limited to, at least one of butene-1, hexene-1 and octene-1.

[0028] The polymerization reactor of the application comprises a polymerization reactor body, a bottom stirring shaft, a top-stretching stirring shaft, a bottom stirring paddle arranged on the bottom stirring shaft, a ribbon paddle arranged on the bottom stirring paddle, a frame paddle arranged on the ribbon paddle, an axial-flow stirring paddle arranged on the top-stretching stirring shaft, a detachable jacket and a gas channel arranged on the jacket. The stirring device arranged in the polymerization reactor of the application is a special stirring form designed for the change of fluid characteristics in the production process of polyolefin, which can adapt to the requirements of high mixing uniformity, large viscosity change and complex phase change in the production process of polyolefin, and the detachable jacket and the gas channel arranged on the jacket can be used to pass in liquid nitrogen or carbon monoxide killing agent from the gas channel of the jacket when rapid heat removal or rapid termination of reaction is required, so as to realize rapid heat removal and timely termination of reaction.

[0029] Compared with the prior art, the application has at least the following beneficial effects:

[0030] (1) The axial flow stirring paddle and frame paddle used in the polymerization reactor provided by the present application can realize sufficient mixing of high-viscosity materials in the radial direction, and the screw paddle and bottom stirring paddle can realize sufficient mixing of the materials in the axial direction, thereby realizing the overall circulation of the materials in the polymerization reactor and making the materials uniformly mixed.

[0031] (2) The polymerization reactor provided by the present application can realize sufficient mixing of high-viscosity materials in the polymerization reactor, effectively realize mass transfer and heat transfer in the reaction process, thereby improving the polymerization reaction efficiency and ensuring the performance stability of the polymerization product.

[0032] (3) The detachable jacket of the present application is provided with a gas channel, and the detachable jacket has a ventilation function, which can realize rapid heat removal of the high-viscosity solution polymerization reaction system and timely termination of the reaction, thereby ensuring the stability of the industrial operation device. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1 The figure is a structural schematic diagram of the polymerization reactor of an embodiment of the present application.

[0034] Figure 2 The figure is a flow path schematic diagram of the materials in the polymerization reactor of the present application.

[0035] In the figure, the reference signs are as follows:

[0036] Polymerization reactor body 1

[0037] Bottom stirring shaft 2

[0038] Bottom stirring paddle 3

[0039] Screw paddle 4

[0040] Frame paddle 5

[0041] Top extension stirring shaft 6

[0042] Axial flow stirring paddle 7

[0043] Gas channel 8

[0044] Jacket 9

[0045] Ventilation pipeline 10 DETAILED DESCRIPTION

[0046] In order to have a clearer understanding of the technical features, objects and beneficial effects of the present application, the technical solutions of the present application are described in detail as follows, but it cannot be understood as a limitation on the implementable scope of the present application.

[0047] The polymerization reactor of the present application comprises a polymerization reactor body 1, a bottom stirring shaft 2 and a top stretching stirring shaft 6; the bottom stirring shaft 2 is provided with a bottom stirring paddle 3; the bottom stirring paddle 3 is provided with a screw belt paddle 4; the screw belt paddle 4 is provided with a frame paddle 5; the top stretching stirring shaft 6 is provided with an axial flow stirring paddle 7; the inside of the polymerization reactor body 1 is lined with a detachable jacket 9; the jacket 9 is provided with a gas pipeline 10; the inside of the jacket 9 is dispersed with gas channels 8; the gas channels 8 are communicated with the gas pipeline 10.

[0048] In an embodiment, the jacket 9 is kept a certain distance from the polymerization reactor body 1; the upper part of the jacket 9 and the polymerization reactor body 1 are pressed together by a reactor cover; the position where the jacket 9 and the reactor cover are pressed together is provided with a gas pipeline; the diameter of the jacket 9 is 0.85-0.95 times the diameter of the polymerization reactor.

[0049] In an embodiment, the bottom stirring shaft 2 vertically extends into the polymerization reactor from the bottom of the polymerization reactor.

[0050] In an embodiment, the bottom stirring paddle 3 is in the form of an anchor paddle or the like, has the feature of following the shape of the inner surface of the bottom head of the polymerization reactor, and keeps a constant distance from the inner surface of the bottom head of the polymerization reactor body 1; the bottom stirring paddle 3 is fixed on the bottom stirring shaft 2 by welding or the like, and rotates in the same direction as the bottom stirring shaft 2.

[0051] In an embodiment, the diameter of the bottom stirring paddle 3 is 0.85-0.95 times the diameter of the polymerization reactor body 1.

[0052] In an embodiment, the screw belt paddle 4 is located above the bottom stirring paddle 3, and is used to promote the flow and mixing of the materials in the polymerization reactor.

[0053] In an embodiment, the screw belt paddle 4 has two blades; the generatrix of each blade presents a spiral line; and the two blades are centrally symmetrical about the axis of the bottom stirring shaft 2.

[0054] In an embodiment, the maximum diameter of the projection of the screw belt paddle 4 in the vertical direction is the same as the diameter of the bottom stirring paddle 3, and is 0.85-0.95 times the diameter of the polymerization reactor body 1; the pitch of the spiral generatrix of each blade is 0.5 times the diameter of the screw belt paddle 4 to 1 times the diameter of the screw belt paddle 4.

[0055] In an embodiment, the cross-sectional shape of the frame paddle 5 is cylindrical or rectangular, and is fixed on the blades of the screw belt paddle 4 by welding or the like, and simultaneously plays the role of mixing materials and fixed support, and its size depends on the size of the screw belt paddle 4 and the bottom stirring paddle 3. The bottom stirring shaft 2, the bottom stirring paddle 3, the screw belt paddle 4 and the frame paddle 5 together constitute the bottom stirrer of the polymerization reactor; the top stretching stirring shaft 6 and the axial flow stirring paddle 7 provided on the top stretching stirring shaft 6 together constitute the top stirrer of the polymerization reactor.

[0056] In an embodiment, the rotation directions of the bottom stirrer and the top stirrer can be the same or opposite.

[0057] In an embodiment, the ratio of the rotation speeds of the bottom stirrer and the top stirrer is 0.3 to 1.

[0058] In an embodiment, the top extension stirring shaft 6 extends vertically into the polymerization reactor from the top of the polymerization reactor.

[0059] In an embodiment, the number of the axial flow stirring paddles 7 is 2 to 6, and arranged sequentially from top to bottom on the top extension stirring shaft 6.

[0060] In an embodiment, when the number of the axial flow stirring paddles 7 is multiple, the diameters of the multiple axial flow stirring paddles 7 are equal, and the diameter of the axial flow stirring paddle 7 is 0.3 to 0.7 times the diameter of the polymerization reactor body 1, the number of the blades on each axial flow stirring paddle 7 is 2 to 4, and each blade is uniformly distributed about the axis of the top extension stirring shaft 6; the ratio of the distance between the bottommost axial flow stirring paddle 7 and the bottom of the polymerization reactor and the diameter of the polymerization reactor is 0.15 to 0.3; and the ratio of the distance between two adjacent axial flow stirring paddles 7 and the diameter of the axial flow stirring paddle 7 is 0.3 to 1.5.

[0061] In an embodiment, the gas channels 8 of the jacket 9 are uniformly distributed on the inner walls of the front, rear, left and right of the jacket 9, the number of the gas channels 8 on each inner wall is 10-20, and the diameter of the gas channels 8 is 3-5 mm.

[0062] In an embodiment, the gas channels 8 are each provided with a cap, and the cap is in a closed state in the case of no gas passing, preventing the material from entering the gas channels 8 and causing blockage.

[0063] The application also provides a method for olefin polymerization reaction, which uses the above polymerization reactor.

[0064] The olefin includes, but is not limited to, at least one of butene-1, hexene-1 and octene-1.

[0065] In order to better understand the application, preferred embodiments will be described, and it should be noted that these embodiments are not intended to limit the application.

[0066] Example 1

[0067] The polymerization reactor of the embodiment comprises a polymerization kettle body 1, a bottom stirring shaft 2, an anchor stirring paddle 3, a ribbon paddle 4, a frame paddle 5, a top extension stirring shaft 6, an axial flow stirring paddle 7, gas holes 8, a detachable jacket 9, and a vent line 10 at the upper end of the jacket 9. The bottom stirring shaft 2 extends vertically into the polymerization kettle body 1 from directly below the polymerization kettle body 1. The anchor stirring paddle 3 is fixed on the bottom stirring shaft 2 and rotates at the same speed in the same direction as the bottom stirring shaft 2. The ribbon paddle 4 is located above the anchor stirring paddle 3 and is connected to the anchor stirring paddle 3, and is fixed by the frame paddle 5 to promote the flow and mixing of materials in the polymerization reactor. The top extension stirring shaft 6 extends vertically into the polymerization kettle body 1 from above the top of the polymerization reactor. The axial flow stirring paddle 7 is fixed on the top extension stirring shaft 6 by welding in the form of a hub. The inside of the polymerization kettle body 1 is lined with a detachable jacket 9. The jacket 9 is spaced apart from the polymerization kettle body 1 by a certain distance. The upper part of the jacket 9 and the polymerization kettle body 1 are pressed together by a kettle cover. The jacket 9 and the kettle cover are provided with a vent line 10 at the pressing position. The jacket 9 is provided with gas holes 8.

[0068] The anchor stirring paddle 3 has a diameter of 0.95 times the diameter of the polymerization kettle body 1, a width of 0.05 times the diameter of the anchor stirring paddle, and a constant distance between the anchor stirring paddle and the inner surface of the polymerization kettle body 1 of 0.025 times the diameter of the polymerization kettle body 1. The ribbon paddle 4 has two blades, each blade has a helical line as its generatrix, and the two blades are symmetric about the axis of the bottom stirring shaft 2. The maximum diameter of the projection of the ribbon paddle 4 in the vertical direction is the same as the diameter of the anchor stirring paddle 3, and is 0.95 times the diameter of the polymerization kettle body 1. The pitch of the helical generatrix of each blade is the same as the diameter of the ribbon paddle 4, and the total height is 1.1 times the diameter. To reduce the flow resistance, the frame paddle 5 has a cylindrical cross-section. The bottom stirring shaft 2, the anchor stirring paddle 3, the ribbon paddle 4, and the frame paddle 5 together form the bottom stirrer of the polymerization reactor. The axial flow stirring paddle 7 has a diameter of 0.4 times the diameter of the polymerization kettle body 1. Each axial flow stirring paddle 7 has 3 blades, and the number of axial flow stirring paddles 7 is 4. The distance between adjacent two layers of axial flow stirring paddles is the same as the diameter of the axial flow stirring paddle 7. The distance between the bottommost axial flow stirring paddle 7 and the kettle bottom is 0.25 times the diameter of the polymerization reactor. The axial flow stirring paddle 7 makes the surrounding material move downward along the axial direction during rotation. The axial flow stirring paddle 7 and the top extension stirring shaft 6 on which it is located form the top stirrer of the polymerization reactor. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 0.3.

[0069] The diameter of the jacket 9 is 0.90 times the diameter of the polymerization reactor, the gas channels 8 are evenly distributed on the inner walls of the jacket 9 in the front, rear, left and right directions, the number of gas channels 8 on each inner wall is 15, the diameter of the gas channels 8 is 4mm, and the gas channels 8 in each direction are connected with the gas pipeline 10, and the gas channels 8 are provided with caps, which are in a closed state in the case of no gas to prevent the material from entering the gas channels 8 and causing blockage.

[0070] Example 2

[0071] The polymerization reactor of the embodiment comprises a polymerization kettle body 1, a bottom stirring shaft 2, a bottom stirring paddle 3, a spiral ribbon paddle 4, a frame paddle 5, a top extension stirring shaft 6, an axial flow stirring paddle 7, a gas channel 8, a detachable jacket 9 and a gas pipeline 10 at the upper end of the jacket 9. The bottom stirring shaft 2 vertically extends into the polymerization kettle body 1 from the bottom of the polymerization kettle body 1; the bottom stirring paddle 3 is an anchor paddle, which is fixed on the bottom stirring shaft 2 and rotates at the same speed in the same direction as the bottom stirring shaft 2; the spiral ribbon paddle 4 is located above the bottom stirring paddle 3 and is connected with the bottom stirring paddle 3 and fixed by the frame paddle 5, which is used to promote the flow and mixing of the material in the polymerization reactor; the top extension stirring shaft 6 vertically extends into the polymerization kettle body 1 from above the top of the polymerization reactor, the axial flow stirring paddle 7 is fixed on the top extension stirring shaft 6 by welding in the form of a hub, the inside of the polymerization kettle is lined with a detachable jacket 9, which is spaced apart from the polymerization kettle body 1, the upper part of the jacket 9 and the polymerization kettle body 1 are pressed together by the kettle cover, and the jacket and the kettle cover are provided with a gas pipeline 10, and the inside of the jacket 9 is provided with gas channels 8.

[0072] The bottom stirring paddle 3 is an anchor paddle, the diameter of which is 0.90 times the diameter of the polymerization kettle body 1, the width of which is 0.05 times the diameter of the anchor paddle, and the constant distance between the anchor paddle and the inner surface of the polymerization kettle body 1 is 0.025 times the diameter of the polymerization kettle body 1. The screw paddle 4 has two blades, the generatrix of each blade presents a spiral line, and the two blades are centrally symmetrical about the axis of the bottom stirring shaft 2; the maximum diameter of the projection of the screw paddle 4 in the vertical direction is the same as the diameter of the bottom stirring paddle 3, and is 0.90 times the diameter of the polymerization kettle body 1, the pitch of the spiral generatrix of each blade is 0.5 times the diameter of the screw paddle 4, and the total height is 1.1 times the diameter. In order to reduce the flow resistance, the cross section of the frame paddle 5 is cylindrical. The bottom stirring shaft 2, the bottom stirring paddle 3, the screw paddle 4 and the frame paddle 5 together constitute the bottom stirrer of the polymerization reactor of the application. The diameter of the axial flow stirring paddle 7 is 0.3 times the diameter of the polymerization kettle body 1, there are 4 blades on each axial flow stirring paddle 7, the number of axial flow stirring paddles 7 is 3, the distance between adjacent two layers of axial flow stirring paddles 7 is the same as the diameter, and the distance between the bottommost axial flow stirring paddle 7 and the kettle bottom of the polymerization reactor is 0.3 times the diameter of the polymerization reactor. The axial flow stirring paddle moves the surrounding material downward in the axial direction during rotation. The above-mentioned axial flow stirring paddle 7 and the top stretching stirring shaft 6 where it is located constitute the top stirrer of the polymerization reactor of the application. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 0.5.

[0073] The diameter of the jacket 9 is 0.95 times the diameter of the polymerization reactor, the inside of the jacket 9 is uniformly distributed with gas channels 8 on the inner walls in the front, rear, left and right four directions, the number of gas channels 8 on each inner wall is 10, and the diameter of the gas channels 8 is 5mm; each direction of the gas channel 8 is connected with the gas pipeline 10, and at the same time, the gas channel 8 is provided with a cap, which is in a closed state in the case of no gas, preventing the material from entering the gas channel 8 and causing blockage.

[0074] Example 3

[0075] The polymerization reactor of the embodiment comprises a polymerization kettle body 1, a bottom stirring shaft 2, an anchor stirring paddle 3, a ribbon paddle 4, a frame paddle 5, a top stirring shaft 6, an axial flow stirring paddle 7, gas holes 8, a detachable jacket 9, and a vent line 10 at the upper end of the jacket 9. The bottom stirring shaft 2 extends vertically into the polymerization kettle body 1 from directly below the polymerization kettle body 1. The anchor stirring paddle 3 is fixed on the bottom stirring shaft 2 and rotates at the same speed in the same direction as the bottom stirring shaft 2. The ribbon paddle 4 is located above the anchor stirring paddle 3 and is connected to the anchor stirring paddle 3 and fixed by the frame paddle 5, which is used to promote the flow and mixing of materials in the polymerization reactor. The top stirring shaft 6 extends vertically into the polymerization kettle body 1 from above the polymerization reactor. The axial flow stirring paddle 7 is fixed on the top stirring shaft 6 by welding in the form of a hub. The inside of the polymerization kettle body is lined with a detachable jacket 9. The jacket 9 is spaced apart from the polymerization kettle body 1 by a certain distance. The upper part of the jacket 9 and the kettle body 2 are pressed together by a kettle cover. The jacket 9 is provided with a vent line 10 at the pressing part of the kettle cover. The jacket 9 is provided with gas holes 8.

[0076] The anchor stirring paddle 3 has a diameter of 0.95 times the diameter of the polymerization kettle body 1, a width of 0.05 times the diameter of the anchor stirring paddle, and a constant distance between the anchor stirring paddle and the inner surface of the polymerization kettle body 1 of 0.025 times the diameter of the polymerization kettle body 1. The ribbon paddle 4 has two blades, each with a helical wire. The two blades are symmetric about the axis of the bottom stirring shaft 2. The maximum diameter of the projection of the ribbon paddle 4 in the vertical direction is the same as the diameter of the anchor stirring paddle 3, which is 0.95 times the diameter of the polymerization kettle body 1. The pitch of the helical wire of each blade is 0.5 times the diameter of the ribbon paddle 4, and the total height is 1.1 times the diameter. To reduce flow resistance, the frame paddle 5 has a cylindrical cross-section. The bottom stirring shaft 2, the anchor stirring paddle 3, the ribbon paddle 4, and the frame paddle 5 together form the bottom stirrer of the polymerization reactor. The diameter of the axial flow stirring paddle 7 is 0.3 times the diameter of the polymerization kettle body 1. Each axial flow stirring paddle 7 has 4 blades, and the number of axial flow stirring paddles 7 is 6. The distance between adjacent two layers of axial flow stirring paddles 7 is 0.5 times the diameter of the axial flow stirring paddle 7. The distance between the bottommost axial flow stirring paddle 7 and the kettle bottom is 0.15 times the diameter of the polymerization reactor. During rotation, the axial flow stirring paddle 7 causes the surrounding material to move downward along the axial direction. The axial flow stirring paddle 7 and the top stirring shaft 6 on which it is located form the top stirrer of the polymerization reactor. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 1.

[0077] The diameter of the jacket 9 is 0.85 times the diameter of the polymerization reactor, the inside of the jacket 9 is uniformly distributed with gas channels 8 on the inner walls in the front, rear, left and right directions, the number of gas channels 8 on each inner wall is 20, the diameter of the gas channel 8 is 3mm; the gas channels 8 in each direction are connected with the gas pipeline 10, and there is a cap on the gas channel 8, which is in a closed state in the case of no gas, preventing the material from entering the gas channel 8 and causing blockage.

[0078] Example 4

[0079] The polymerization reactor of the embodiment includes a polymerization kettle body 1, a bottom stirring shaft 2, a bottom stirring paddle 3, a spiral ribbon paddle 4, a frame paddle 5, a top stirring shaft 6, an axial flow stirring paddle 7, a gas channel 8, a detachable jacket 9 and a gas pipeline 10 on the upper end of the jacket 9. The bottom stirring shaft 2 extends vertically from the bottom of the polymerization kettle body 1 into the polymerization kettle body 1; the bottom stirring paddle 3 is an anchor paddle, which is fixed on the bottom stirring shaft 2 and rotates at the same speed as the bottom stirring shaft 2; the spiral ribbon paddle 4 is located above the bottom stirring paddle 3 and is connected with the bottom stirring paddle 3, and is fixed by the frame paddle 5, which is used to promote the flow and mixing of the material in the polymerization reactor; the top stirring shaft 6 extends vertically from above the top of the polymerization reactor into the polymerization kettle body 1, the axial flow stirring paddle 7 is fixed on the top stirring shaft 6 by the form of hub, the inside of the polymerization kettle is lined with a detachable jacket 9, the jacket 9 is left a certain distance from the polymerization kettle body 1, the upper part of the jacket 9 and the polymerization kettle body 1 is pressed together by the kettle cover, and the jacket 9 and the kettle cover are provided with a gas pipeline 10, and the inside of the jacket 9 is distributed with gas channels 8.

[0080] The anchor paddle 3 has a diameter of 0.85 times the diameter of the polymerization kettle body 1, a width of 0.05 times the diameter of the anchor paddle, and a constant distance between the anchor paddle and the inner surface of the polymerization kettle body 1 of 0.025 times the diameter of the polymerization kettle body 1. The ribbon paddle 4 has two blades, each blade has a helical wire, and the two blades are symmetric about the axis of the bottom stirring shaft 2; the maximum diameter of the projection of the ribbon paddle 4 in the vertical direction is the same as the diameter of the anchor paddle 3, and is 0.85 times the diameter of the polymerization kettle body 1; the pitch of the helical wire of each blade is 0.8 times the diameter of the ribbon paddle 4, and the total height is 1.1 times the diameter. In order to reduce the flow resistance, the cross section of the frame paddle 5 is cylindrical. The bottom stirring shaft 2, the anchor paddle 3, the ribbon paddle 4 and the frame paddle 5 together form the bottom stirrer of the polymerization reactor of the present application. The diameter of the axial flow stirring paddle 7 is 0.7 times the diameter of the polymerization kettle body 1, each axial flow stirring paddle 7 has 2 blades, and the number of axial flow stirring paddles 7 is 2. The distance between the adjacent two layers of axial flow stirring paddles is 1.5 times the diameter, and the distance between the bottommost axial flow stirring paddle 7 and the kettle bottom is 0.2 times the diameter of the polymerization reactor. The axial flow stirring paddle 7 makes the surrounding material move downward along the axial direction during rotation. The above-mentioned axial flow stirring paddle 7 and the top stretching stirring shaft 6 where it is located constitute the top stirrer of the polymerization reactor of the present application. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 0.7.

[0081] The diameter of the jacket 9 is 0.85 times the diameter of the polymerization reactor, the inside of the jacket 9 is uniformly distributed with gas channels 8 on the inner walls in the front, rear, left and right directions, the number of gas channels 8 on each inner wall is 10, and the diameter of the gas channels 8 is 4 mm; each direction of the gas channel 8 is connected with the gas pipeline 10, and at the same time, the gas channel 8 has a cap, which is in a closed state in the case of no gas, preventing the material from entering the gas pipeline 10 and causing blockage.

[0082] Example 5

[0083] The polymerization reactor of the embodiment comprises a polymerization kettle body 1, a bottom stirring shaft 2, an anchor stirring paddle 3, a ribbon paddle 4, a frame paddle 5, a top stirring shaft 6, an axial flow stirring paddle 7, gas holes 8, a detachable jacket 9, and a vent line 10 at the upper end of the jacket 9. The bottom stirring shaft 2 extends vertically into the polymerization kettle body 1 from directly below the polymerization kettle body 1. The anchor stirring paddle 3 is fixed on the bottom stirring shaft 2 and rotates at the same speed in the same direction as the bottom stirring shaft 2. The ribbon paddle 4 is located above the anchor stirring paddle 3 and is connected to the anchor stirring paddle 3 and fixed by the frame paddle 5, which is used to promote the flow and mixing of materials in the polymerization reactor. The top stirring shaft 6 extends vertically into the polymerization kettle body 1 from above the top of the polymerization reactor. The axial flow stirring paddle 7 is fixed on the top stirring shaft 6 by welding in the form of a hub. The inside of the polymerization kettle body 1 is lined with a detachable jacket 9. There is a certain distance between the jacket 9 and the polymerization kettle body 1. The upper part of the jacket 9 and the polymerization kettle body 1 are pressed together by a kettle cover. The jacket 9 and the kettle cover are provided with a vent line 10 at the pressing position. The inside of the jacket 9 is provided with gas holes 8.

[0084] The anchor stirring paddle 3 has a diameter of 0.92 times the diameter of the polymerization kettle body 1, a width of 0.05 times the diameter of the anchor stirring paddle, and a constant distance between the anchor stirring paddle and the inner surface of the polymerization kettle body 1 of 0.025 times the diameter of the polymerization kettle body 1. The ribbon paddle 4 has two blades, each with a helical wire. The two blades are symmetric about the axis of the bottom stirring shaft 2. The maximum diameter of the projection of the ribbon paddle 4 in the vertical direction is the same as the diameter of the anchor stirring paddle 3, which is 0.92 times the diameter of the polymerization kettle body 1. The pitch of the helical wire of each blade is 0.6 times the diameter of the ribbon paddle 4, and the total height is 1.1 times the diameter. To reduce the flow resistance, the frame paddle 5 has a cylindrical cross-section. The bottom stirring shaft 2, the anchor stirring paddle 3, the ribbon paddle 4, and the frame paddle 5 together form the bottom stirrer of the polymerization reactor. The diameter of the axial flow stirring paddle 7 is 0.5 times the diameter of the polymerization kettle body 1. Each axial flow stirring paddle 7 has 3 blades, and the number of axial flow stirring paddles 7 is 5. The distance between adjacent two layers of axial flow stirring paddles is 1.1 times the diameter, and the distance between the bottommost axial flow stirring paddle 7 and the kettle bottom is 0.3 times the diameter of the polymerization reactor. The axial flow stirring paddle makes the surrounding material move downward along the axial direction during rotation. The axial flow stirring paddle 7 and the top stirring shaft 6 on which it is located constitute the top stirrer of the polymerization reactor. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 0.9.

[0085] The diameter of the jacket 9 is 0.90 times the diameter of the polymerization reactor, the gas channels 8 are evenly distributed on the inner walls of the jacket 9 in the front, rear, left and right directions, the number of gas channels 8 on each inner wall is 15, the diameter of the gas channels 8 is 3mm, and the gas channels 8 in each direction are connected with the gas pipeline 10, and the gas channels 8 are provided with caps, which are in a closed state in the case of no gas to prevent the material from entering the gas channels 8 and causing blockage.

[0086] Example 6

[0087] The polymerization reactor of the embodiment comprises a polymerization kettle body 1, a bottom stirring shaft 2, a bottom stirring paddle 3, a spiral ribbon paddle 4, a frame paddle 5, a top stirring shaft 6, an axial flow stirring paddle 7, a gas channel 8, a detachable jacket 9 and a gas pipeline 10 at the upper end of the jacket 9. The bottom stirring shaft 2 vertically extends into the polymerization kettle body 1 from the front bottom of the polymerization kettle body 1; the bottom stirring paddle 3 is an anchor paddle, which is fixed on the bottom stirring shaft 2 and rotates at the same speed in the same direction as the bottom stirring shaft 2; the spiral ribbon paddle 4 is located above the bottom stirring paddle 3 and is connected with the bottom stirring paddle 3 and fixed by the frame paddle 5, which is used to promote the flow and mixing of the material in the polymerization reactor; the top stirring shaft 6 vertically extends into the polymerization kettle body 1 from above the top of the polymerization reactor, the axial flow stirring paddle 7 is fixed on the top stirring shaft 6 by welding in the form of a hub, the polymerization kettle body 1 is lined with a detachable jacket 9, a certain distance is left between the jacket 9 and the polymerization kettle body 1, the upper part of the jacket 9 and the polymerization kettle body 1 is pressed together by a kettle cover, a gas pipeline 10 is provided at the pressing part of the jacket 9 and the kettle cover, and the jacket 9 is internally distributed with gas channels 8.

[0088] The bottom stirring paddle 3 is an anchor paddle, the diameter of which is 0.88 times the diameter of the polymerization kettle body 1, the width of which is 0.05 times the diameter of the anchor paddle, and the constant distance between the anchor paddle and the inner surface of the polymerization kettle body 1 is 0.025 times the diameter of the polymerization kettle body 1. The screw paddle 4 has two blades, the generatrix of each blade presents a spiral line, and the two blades are centrally symmetrical about the axis of the bottom stirring shaft 2; the maximum diameter of the projection of the screw paddle 4 in the vertical direction is the same as the diameter of the bottom stirring paddle 3, and is 0.88 times the diameter of the polymerization kettle body 1; the pitch of the spiral generatrix of each blade is 0.8 times the diameter of the screw paddle 4, and the total height is 1.1 times the diameter thereof. In order to reduce the flow resistance, the cross section of the frame paddle 5 is rectangular. The bottom stirring shaft 2, the bottom stirring paddle 3, the screw paddle 4 and the frame paddle 5 together constitute the bottom stirrer of the polymerization reactor of the present application. The diameter of the axial flow stirring paddle 7 is 0.6 times the diameter of the polymerization kettle body, each axial flow stirring paddle 7 has 3 blades, the number of axial flow stirring paddles 7 is 4, the distance between adjacent two layers of axial flow stirring paddles is 1.3 times the diameter thereof, and the distance between the bottommost axial flow stirring paddle 7 and the kettle bottom of the polymerization reactor is 0.15 times the diameter of the polymerization reactor. During the rotation of the axial flow stirring paddle 7, the surrounding material moves downward along the axial direction. The above-mentioned axial flow stirring paddle 7 and the top extension stirring shaft 6 where it is located constitute the top stirrer of the polymerization reactor of the present application. The bottom stirrer and the top stirrer rotate in the same direction, and the speed ratio is 0.4.

[0089] As shown in Figure 2 The flow path diagram of the material in the polymerization reactor when the material is in the high viscosity stage with a viscosity of 20000 cP is shown in the figure. As can be seen from the figure, under the action of the bottom stirrer, the material near the bottom of the polymerization reactor gradually rises to the vicinity of the liquid surface with the rotation of the bottom stirrer. At the same time, the material near the center of the polymerization reactor gradually moves downward under the action of the top stirrer, and finally returns to the head at the bottom of the polymerization reactor, thereby forming an overall circulation and realizing the overall mixing of the material.

[0090] The diameter of the jacket 9 is 0.90 times the diameter of the polymerization reactor, the inside of the jacket 9 is uniformly distributed with gas channels 8 on the inner walls in the front, rear, left and right directions, the number of gas channels 8 on each inner wall is 20, and the diameter of the gas channels 8 is 5 mm; the gas channels 8 in each direction are connected with the gas pipeline 10, and at the same time, there are caps on the gas channels 8, which are in a closed state in the case of no gas, preventing the material from entering the gas channels 8 and causing blockage.

[0091] Comparative Example 1

[0092] The difference between Example 1 and Comparative Example 1 is that the jacket 9 is not provided with gas channels 8, and the gas pipeline 10 is not provided, but the outside of the polymerization reactor is lined with a jacket, and a coolant is introduced into the jacket to remove heat, and the others are the same as Example 1.

[0093] Test Example 1

[0094] This embodiment provides a method for rapid heat removal in the industrial production of polybutene-1. The method uses the polymerization reactor of Example 1 to conduct polymerization and heat removal tests. The specific steps are as follows:

[0095] A raw material comprising a liquid phase mixture of butene-1 monomer and polyalpha-olefin is introduced into the polymerization reactor. The raw material comprises butene-1 monomer, polyethylene, and polypropylene, wherein the concentration of butene-1 monomer is 75 wt%. The polymerization temperature is 70°C, and the reaction pressure is 1.3 MPa. Under the action of the catalyst, the polymerization reaction is carried out for 2 h, and the viscosity of the polybutene slurry reaches 5 x 10 6 cp, the reactor is warmed to 90°C, and then liquid nitrogen is introduced into the polymerization reactor through the gas line. After 80 s, the temperature of the polymerization reactor drops to 50°C.

[0096] Test Example 2

[0097] This embodiment provides a method for rapid heat removal in the industrial production of polybutene-1. The method uses the polymerization reactor of Example 2 to conduct polymerization and heat removal tests. The specific steps are as follows:

[0098] A raw material comprising a liquid phase mixture of butene-1 monomer and polyalpha-olefin is introduced into the polymerization reactor. The raw material comprises butene-1 monomer, polyethylene, and polypropylene, wherein the concentration of butene-1 monomer is 75 wt%. The polymerization temperature is 70°C, and the reaction pressure is 1.3 MPa. Under the action of the catalyst, the polymerization reaction is carried out for 2 h, and the viscosity of the polybutene slurry reaches 5 x 10 6 cp, the reactor is warmed to 90°C, and then liquid nitrogen is introduced into the polymerization reactor through the gas line. After 96 s, the temperature of the polymerization reactor drops to 50°C.

[0099] Test Example 3

[0100] This embodiment provides a method for rapid heat removal in the industrial production of polybutene-1. The method uses the polymerization reactor of Example 3 to conduct polymerization and heat removal tests. The specific steps are as follows:

[0101] A raw material comprising a liquid phase mixture of butene-1 monomer and polyalpha-olefin is introduced into the polymerization reactor. The raw material comprises butene-1 monomer, polyethylene, and polypropylene, wherein the concentration of butene-1 monomer is 75 wt%. The polymerization temperature is 70°C, and the reaction pressure is 1.3 MPa. Under the action of the catalyst, the polymerization reaction is carried out for 2 h, and the viscosity of the polybutene slurry reaches 5 x 10 6 cp, the reactor is warmed to 90°C, and then liquid nitrogen is introduced into the polymerization reactor through the gas line. After 112 s, the temperature of the polymerization reactor drops to 50°C.

[0102] Test Example 4

[0103] The present embodiment provides a method for rapid heat removal in the industrial production of polyhexene-1 elastomer. The method uses the polymerization reactor of Example 1 to perform polymerization and heat removal tests. The specific steps are as follows:

[0104] Add hexene-1 monomer and reaction solvent toluene into the polymerization reactor, wherein the concentration of hexene-1 monomer is 65%, then add alkyl aluminum cocatalyst and catalyst to start the polymerization reaction. The polymerization temperature is 60℃, the reaction pressure is 1.0 MPa, the polymerization reaction time is 2h, and the viscosity of the polyhexene slurry reaches 2x10 5 cp, then increase the temperature of the polymerization reactor to 90℃, and immediately introduce liquid nitrogen into the polymerization reactor through the gas line. After 55s, the temperature of the polymerization reactor drops to 50℃.

[0105] Comparative Test Example 1

[0106] The difference between the present embodiment and Comparative Example 1 is that the polymerization reactor of Comparative Example 1 is used, and the other steps are the same as those of Test Example 1. The specific steps are as follows:

[0107] Introduce raw materials containing butene-1 monomer and polyalpha-olefin into the polymerization reactor, wherein the raw materials contain butene-1 monomer, polyethylene and polypropylene, and the concentration of butene-1 monomer is 75wt%. The polymerization temperature is 70℃, the reaction pressure is 1.3 MPa, and the polymerization reaction is carried out under the action of the catalyst for 2h. The viscosity of the polybutene slurry reaches 5x10 6 cp, then increase the temperature of the polymerization reactor to 90℃, stop the oil bath circulation heating, and introduce liquid nitrogen into the jacket outside the polymerization reactor. After 2550s, the temperature of the reactor drops to 50℃.

[0108] Of course, the present application can have other various embodiments. Those skilled in the art can make various corresponding changes and modifications to the present application without departing from the spirit and essence of the present application. These corresponding changes and modifications should all fall within the protection scope of the claims of the present application.

Claims

1. A polymerization reactor, characterized in that, include: The polymerization reactor body, bottom stirring shaft, and top stirring shaft; The bottom stirring shaft is equipped with a bottom stirring paddle; the bottom stirring paddle is equipped with a ribbon paddle; the ribbon paddle is equipped with a frame paddle; the top stirring shaft is equipped with an axial flow stirring paddle; the polymerization reactor body is lined with a removable jacket; the jacket is equipped with a venting line; the jacket has dispersed gas channels inside; the gas channels are connected to the venting line.

2. The polymerization reactor according to claim 1, characterized in that, The diameter of the jacket is 0.85-0.95 times the diameter of the polymerization reactor.

3. The polymerization reactor according to claim 1, characterized in that, The bottom stirring shaft extends vertically into the polymerization reactor from the bottom of the reactor.

4. The polymerization reactor according to claim 1, characterized in that, The distance between the bottom stirring paddle and the inner surface of the bottom end cap of the polymerization reactor remains constant; the bottom stirring paddle is fixed on the bottom stirring shaft and rotates in the same direction as the bottom stirring shaft; The diameter of the bottom agitator is 0.85 to 0.95 times the diameter of the polymerization reactor.

5. The polymerization reactor according to claim 1, characterized in that, The ribbon impeller is located above the bottom agitator and is used to promote the flow and mixing of materials in the polymerization reactor.

6. The polymerization reactor according to claim 1, characterized in that, The ribbon propeller has two blades, each blade has a helical generatrix, and the two blades are symmetrical about the axis of the bottom stirring shaft.

7. The polymerization reactor according to claim 6, characterized in that, The maximum diameter of the projection formed by the spiral impeller in the vertical direction is the same as the diameter of the bottom stirring impeller, and is 0.85 to 0.95 times the diameter of the polymerization reactor. The pitch of the helical generatrix of each blade is 0.5 to 1 times the diameter of the spiral impeller.

8. The polymerization reactor according to claim 1, characterized in that, The cross-sectional shape of the frame-type propeller is cylindrical or rectangular.

9. The polymerization reactor according to claim 1, characterized in that, The bottom stirring shaft, bottom stirring paddle, ribbon paddle, and frame paddle together constitute the bottom stirrer of the polymerization reactor; the top stirring shaft and the axial flow stirring paddle installed on the top stirring shaft together constitute the top stirrer of the polymerization reactor. The bottom stirrer and the top stirrer can rotate in the same or opposite directions; The ratio of the rotational speeds of the bottom agitator and the top agitator is 0.3 to 1.

10. The polymerization reactor according to claim 1, characterized in that, The top-extending stirring shaft extends vertically into the polymerization reactor from the top.

11. The polymerization reactor according to claim 1, characterized in that, The number of axial flow agitators is 2 to 6, and they are arranged sequentially from top to bottom on the top extension agitator shaft.

12. The polymerization reactor according to claim 1, characterized in that, When there are multiple axial flow agitators, the diameters of the multiple axial flow agitators are equal, and the diameter of the axial flow agitator is 0.3 to 0.7 times the diameter of the polymerization reactor. Each axial flow agitator has 2 to 4 blades, and each blade is evenly distributed about the axis of the top agitator shaft. The ratio of the distance between the bottommost axial flow agitator and the bottom of the polymerization reactor to the diameter of the polymerization reactor is 0.15 to 0.

3. The ratio of the distance between two adjacent axial flow agitators to the diameter of the axial flow agitator is 0.3 to 1.

5.

13. The polymerization reactor according to claim 1, characterized in that, The gas channels of the jacket are evenly distributed on the inner walls of the jacket in the front, back, left and right directions. There are 10-20 gas channels on each inner wall, and the diameter of the gas channels is 3-5 mm.

14. The polymerization reactor according to any one of claims 1-13, characterized in that, Each gas channel is equipped with a cap, which is closed when no gas is being supplied.

15. A method for olefin polymerization, characterized in that, The olefin polymerization reaction is carried out in the polymerization reactor described in any one of claims 1-14.

Images