Reaction device for producing high-viscosity poly-alpha-olefin

Abstract

The utility model provides a reaction device for producing high-viscosity poly-alpha-olefin. The reaction device comprises a horizontal reaction kettle, at least two overflow partition plates are arranged at the bottom of an inner cavity of the horizontal reaction kettle, the overflow partition plates are perpendicular to the bottom of the inner cavity and divide the inner cavity into at least three cavities, and the upper portions of every two adjacent cavities are communicated. In the material flowing direction, the volume of the cavity is gradually reduced, and the height of the overflow partition plate is gradually reduced; a stirring paddle and a heat exchange coil pipe arranged around the stirring paddle in a surrounding manner are arranged in the cavity; a baffle is arranged on the inner side wall of the cavity. When the reaction device is used for producing high-viscosity poly-alpha-olefin, the pipeline can be effectively prevented from being blocked by materials.

Description

Technical Field

[0001] The utility model relates to a reaction device for producing high-viscosity poly-alpha-olefin, belonging to the field of poly-alpha-olefin production. Background Art

[0002] Poly-alpha-olefin (PAO) is an important chemical product. Its raw material monomer is linear alpha-olefin (commonly 1-decene), that is, a straight-chain olefin with more than 4 carbon atoms and a double bond at the end of the molecule. As the most important synthetic lubricating oil, poly-alpha-olefin has excellent viscosity-temperature performance, low-temperature fluidity, high oxidation stability, low evaporation loss and other advantages.

[0003] High-viscosity PAO generally refers to poly-alpha-olefin oil with a kinematic viscosity greater than 40 mm 2 / s at 100 °C. High-viscosity PAO can significantly reduce the friction and wear between the contact surfaces of relative motion, improve the durability of mechanical equipment, the durability of gaskets and the emission interval period, and at the same time can also improve the reliability of equipment. It is often used in gear oil, engine oil, compressor oil, etc. Moreover, the characteristics of poly-alpha-olefin such as renewable, easy to degrade and low toxicity have led to a rapid growth in its demand in the global lubricating oil market.

[0004] At present, the catalyst systems used for the synthesis of poly-alpha-olefin mainly include: AlCl3, BF3, Ziegler-Natta and metallocene catalysts, etc. The selection of catalysts has a direct impact on the product synthesis process and technology. Metallocene is an organometallic coordination compound formed by the connection of a transition metal and cyclopentadiene. In fact, it is a new type of Ziegler-Natta catalyst. Metallocene catalysts have the characteristic of a single active site, which can effectively prevent the problem that the molecular weight distribution of the oligomerization product is difficult to control due to different olefin growth rates at different sites of the catalyst, so they have received more and more attention.

[0005] In the field of poly-α-olefin production with metallocene catalyst systems, the batch polymerization device is one of the commonly used polymerization devices, and its advantages mainly include: being applicable to gas-liquid-solid mixing within a wide viscosity range, having high heat transfer efficiency, flexible variation in the input amount of stirring energy, and high operation flexibility. For example, CN218167040U provides a poly-α-olefin lubricating oil reaction device, which includes: a reactor for carrying out polymerization reactions; a stirring mechanism including stirring paddles arranged in the reactor cavity, and the stirring paddles are used to stir the reaction materials; a heat exchange system including cooling coils and a refrigerator, the cooling coils are arranged around the stirring paddles, the water inlet of the cooling coils is communicated with the water supply port of the refrigerator, the water outlet of the cooling coils is communicated with the water return port of the refrigerator, and the cooling coils are used to cool the fluid in the reactor cavity; a heating system including a heating jacket and a heater, the heating jacket is arranged outside the reactor and forms a heating cavity with the outer side wall of the reactor, the water inlet of the heating cavity is communicated with the water supply port of the heater, the water outlet of the heating cavity is communicated with the water return port of the heater, and the heating cavity is used to heat the reaction materials in the reactor cavity.

[0006] However, the batch polymerization device has the characteristics of a continuous stirred-tank reactor, and the residence time distribution of the materials in the batch polymerization device is not concentrated. At the same time, this device has problems such as easy blockage of pipelines by materials and difficulty in controlling the reaction temperature during the production of high-viscosity poly-α-olefins.

[0007] The batch polymerization device has the characteristics of a continuous stirred-tank reactor, and the residence time distribution of the materials in the batch polymerization device is not concentrated. Therefore, those skilled in the art also commonly use the method of connecting multiple reactors in series to reduce the degree of backmixing in the entire reaction system. For example, CN208921166U provides a multi-reactor series mixing performance measurement experimental device, which includes a water supply system, a large reaction kettle, and at least two small reaction kettles. The small reaction kettles are connected in series through pipelines. The water supply system supplies water to the large reaction kettle and the small reaction kettle at one end of the series pipeline respectively. Stirring mechanisms are respectively arranged inside the large reaction kettle and each small reaction kettle. This multi-reactor series mixing performance measurement experimental device can measure the backmixing situation of the materials in the batch liquid-phase reactor. However, this process still has the following disadvantages: for the production of high-viscosity poly-α-olefins, high-viscosity materials are prone to blockage in the pipes; multiple sets of independent heat exchange systems increase the operation difficulty, etc.

[0008] Therefore, it is necessary to provide a new horizontal multi-stage reaction device for the production of high-viscosity poly-α-olefins to solve problems such as easy blockage of pipelines by materials existing in the existing devices during the production of high-viscosity poly-α-olefins. Utility Model Content

[0009] In order to solve the above technical problems, the purpose of the present utility model is to provide a reaction device for producing high-viscosity poly-α-olefin. When using this reaction device to produce high-viscosity poly-α-olefin, material blockage in the pipeline can be effectively avoided.

[0010] To achieve the above purpose, the present utility model provides a reaction device for producing high-viscosity poly-α-olefin, which includes a horizontal reaction kettle; at least two overflow partitions are arranged at the bottom of the inner cavity of the horizontal reaction kettle. The overflow partitions are perpendicular to the bottom of the inner cavity and divide the inner cavity into at least three chambers. The upper parts of adjacent two chambers are connected; along the direction of material flow, the volume of the chambers decreases, and the height of the overflow partitions decreases; a stirring paddle and a heat exchange coil (the heat exchange coil is not limited to the position at the same height as the stirring paddle and can extend upward or downward) surrounding the stirring paddle are arranged inside the chambers; baffles are arranged on the inner side walls of the chambers (the baffles are arranged closely against the inner side walls of the chambers and the arc is conformable to the inner side walls of the chambers).

[0011] The horizontal reaction kettle is used to carry out a polymerization reaction on raw materials to obtain high-viscosity poly-α-olefin. Among them, using overflow partitions with decreasing height to divide the horizontal reaction kettle into multiple multi-stage series chambers with decreasing volume and connected upper parts can, on the one hand, improve the concentration of the molecular weight of the poly-α-olefin product; on the other hand, it can prevent blockage problems when high-viscosity poly-α-olefin flows between reaction chambers and avoid material backmixing between chambers.

[0012] At the same time, the arrangement of the stirring paddle in the chamber can further improve the uniformity of material distribution and prevent local explosive polymerization. A heat exchange coil is arranged around the stirring paddle (by introducing a cold medium or a hot medium, it plays a role in cooling or heating). On the basis of achieving efficient heat exchange, the heat exchange area in each chamber of the device can be designed in zones, so as to effectively control the polymerization reaction temperature and reduce the operation difficulty of the reaction device.

[0013] In addition, baffles are arranged on the inner side walls of the chambers, which can also effectively reduce the flow dead zone and improve the material mixing efficiency.

[0014] In an optional implementation manner, a cold medium or a hot medium can be introduced into the heat exchange coil by means of an external heat exchange system to play a role in cooling or heating. The temperature of the cold medium can be 0 - 20°C, and the temperature of the hot medium can be 0 - 250°C. Each chamber can share a set of heat exchange systems. This can be achieved by those skilled in the art according to the prior art and will not be elaborated here.

[0015] In an alternative embodiment, along the direction of material flow, the volume of the next-stage chamber is 0.05 to 0.95 times that of the previous-stage chamber. Further, along the direction of material flow, the height of the next-stage partition is 0.05 to 0.95 times that of the previous-stage partition. The distances between two adjacent overflow plates arranged adjacent to each other can be equally spaced or unequally spaced. The height of the overflow plates and the distances between adjacent overflow plates vary correspondingly according to the volumes of the respective chambers, which can be adjusted by those skilled in the art and will not be elaborated herein.

[0016] In a preferred embodiment, the number of overflow partitions is 3 to 10.

[0017] In a preferred embodiment, the length-to-diameter ratio of the horizontal reaction kettle is 3 to 10:1.

[0018] Further, the diameter of the stirring paddle is greater than or equal to 0.2 times and less than 1.0 times the diameter of the chamber. In some alternative embodiments, the stirring paddle can be a radial flow paddle or an axial flow paddle, etc. On the basis of adapting to the volume of the reaction kettle, the stirring paddle can also adopt a form of multi-blade combination.

[0019] In a preferred embodiment, the heat exchange coil is a spiral heat exchange coil. The heat exchange area can be controlled by adjusting the number of spiral turns, so as to realize the controllability of the reaction temperature.

[0020] Further, the number of spiral turns of the spiral heat exchange coil is 5 to 50 turns, and the spiral diameter is 0.2 to 0.8 times the diameter of the chamber. The spiral heat exchange coil can be distributed throughout the chamber, and is not limited to the position at the same height as the stirring paddle.

[0021] Further, the width of the baffle is 0.02 to 0.2 times the diameter of the chamber.

[0022] In a preferred embodiment, a temperature sensor and a pressure sensor are further arranged inside the chamber, so as to achieve the beneficial effect of segmentally monitoring the reaction temperature and the reaction pressure.

[0023] Further, the shape of the top of the overflow partition is planar or serrated.

[0024] In a preferred embodiment, the reaction device for producing high-viscosity poly-α-olefin further includes a variable-frequency motor and a motor output shaft; the variable-frequency motor and the stirring paddle are connected through the motor output shaft. The variable-frequency stirring motor can effectively control the input stirring power and prevent energy waste. The rotational speed of the variable-frequency motor is 50 to 1200 r / min. The variable-frequency motor and the stirring paddle are connected through the motor output shaft, and can also be connected through a speed reducer and a coupling.

[0025] In an alternative embodiment, in a horizontal reactor, 1-decene can be used as a raw material and subjected to a polymerization reaction under the action of a metallocene catalyst to obtain a high-viscosity polyalpha-olefin. The conditions for the polymerization reaction are as follows: the initial reaction temperature is 20 to 100 °C; the reaction time is 1 to 9 h; the reaction pressure is 0.1 to 0.7 MPa; and the operation mode is continuous polymerization reaction. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 Schematically shows a structural diagram of a reaction device for producing a high-viscosity polyalpha-olefin in an embodiment of the present invention.

[0027] Among them, 10 - horizontal reactor; 11 - overflow baffle; 12 - stirring paddle; 13 - heat exchange coil; 14 - baffle; 20 - variable-frequency motor; 30 - motor output shaft. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0028] In order to have a clearer understanding of the technical features, objectives, and beneficial effects of the present invention, the technical solutions of the present invention will be described in detail below, but it should not be construed as a limitation on the scope of implementation of the present invention.

[0029] It should be noted that the terms "first", "second", etc. in the specification and claims of the present invention are used to distinguish similar objects and do not necessarily need to describe a specific order or sequence. It should be understood that such data can be interchanged under appropriate circumstances for the embodiments of the present application described herein. In addition, the terms "comprising" and "having" and any variations thereof are intended to cover non-exclusive inclusion. For example, a process, method, system, product, or device that includes a series of steps or units does not necessarily have to be limited to those steps or units clearly listed, but may include other steps or units not clearly listed or inherent to these processes, methods, products, or devices.

[0030] Example 1

[0031] This example provides a reaction device for producing a high-viscosity polyalpha-olefin, as Figure 1 shown, which includes a horizontal reactor 10 (the length-to-diameter ratio is 4:1); among them,

[0032] The horizontal reactor 10 is provided with a material inlet and a material outlet on two relatively parallel short side walls. One of the side walls has a catalyst inlet (the metallocene catalyst enters the reaction device through this port) and a reaction raw material inlet (raw material 1-decene enters the reaction device through this port), and the positions of these two inlets are both near the blades of the stirring paddle. The other relatively parallel side wall has a poly-α-olefin outlet (the poly-α-olefin product flows out of the reaction device through this port). The horizontal reactor 10 is used to carry out a polymerization reaction on the reaction raw materials under the action of a catalyst to obtain the product poly-α-olefin.

[0033] Along the direction of material flow, three overflow partitions 11 are sequentially arranged at the bottom of the inner cavity of the horizontal reactor 10, which are successively denoted as the first overflow partition, the second overflow partition, and the third overflow partition. The shapes of the tops of the first overflow partition, the second overflow partition, and the third overflow partition are all serrated.

[0034] Along the direction of material flow, the overflow partitions are perpendicular to the bottom of the inner cavity and sequentially divide the inner cavity into four chambers, which are successively denoted as the first chamber, the second chamber, the third chamber, and the fourth chamber, and the upper parts of the first chamber, the second chamber, the third chamber, and the fourth chamber are interconnected. The volume ratios of the first chamber, the second chamber, the third chamber, and the fourth chamber are 10:6:3:1; among them, the distance between the side wall and the first overflow plate = the distance between the first overflow partition and the second overflow partition = the distance between the second overflow partition and the third overflow partition = the distance between the third overflow partition and the other side wall; the height ratios of the first overflow partition, the second overflow partition, and the third overflow partition are 10:6:3.

[0035] Stirring paddles are arranged inside the first chamber, the second chamber, the third chamber, and the fourth chamber, and spiral heat exchange coils are arranged around the stirring paddles (the heat exchange coils are not limited to the positions at the same height as the stirring paddles and can extend upward and downward). The number of spiral turns of the spiral heat exchange coil in the first chamber is 50 turns, the number of spiral turns of the spiral heat exchange coil in the second chamber is 30 turns, the number of spiral turns of the spiral heat exchange coil in the third chamber is 15 turns, and the number of spiral turns of the spiral heat exchange coil in the fourth chamber is 5 turns. The diameters of the heat exchange coils in the first chamber, the second chamber, the third chamber, and the fourth chamber are 20m, and the spiral diameter is 0.6 times the diameter of the chamber.

[0036] Baffles 14 are arranged on the inner side walls of each chamber, and the number of baffles is 4 (one baffle is distributed on each of the front, back, left, and right wall surfaces of the chamber, Figure 1 and only 2 baffles arranged on the left side wall and the right side wall are shown).

[0037] The variable-frequency motor 20 and the stirring paddle 12 are connected by the motor output shaft 30. The variable-frequency motor 20 can drive the motor output shaft 30 and the stirring paddle 12 to rotate, thereby realizing the input of the stirring power. The motor output shaft 30 is connected to the variable-frequency motor 20 and the stirring paddle 12, and is responsible for the output of torque and the positioning of the stirring paddle 12. The stirring paddle 12 adopts a single-layer turbine paddle. The rotation speed of the variable-frequency motor 20 is 600 r / min, and no speed reducer is used.

[0038] All the equipment materials in the reaction device that come into contact with the reaction materials are made of stainless steel, and the stainless steel material has the advantages of corrosion resistance, high strength, and high temperature oxidation resistance.

[0039] This embodiment also provides a reaction method for producing high-viscosity poly-α-olefin, which includes:

[0040] Before the polymerization reaction starts, inject the raw material 1-decene into the reaction device through the reactant feed port, and make it overflow section by section until the working liquid level is reached in the tail section chamber. Turn on the variable-frequency motor 20, set the rotation speed of each motor according to the stirring requirements in each chamber until the flow is stable. Adjust the temperature of the heat medium in the heat exchange coil 13 until the temperature in each chamber reaches the reaction requirements. Pass the metallocene catalyst into the reaction device through the catalyst feed port to initiate the reaction. After the reaction is initiated, switch the medium in the heat exchange coil 13 to the cold medium to cool the materials in each chamber to prevent explosive polymerization. Gradually adjust the stirring speed until the reaction device reaches a stable state to continuously produce poly-α-olefin.

[0041] Among them, the conditions of the polymerization reaction include an initial reaction temperature of 30 °C, a reaction time of 3 h, and a reaction pressure of 0.12 MPa.

[0042] Example 2

[0043] This embodiment provides a reaction device for producing high-viscosity poly-α-olefin, as Figure 1 shown, which includes a horizontal reaction kettle 10 (the ratio of length to diameter is 10:1); among them,

[0044] On two relatively parallel short side walls of the horizontal reaction kettle 10, a material inlet and a material outlet are provided. One of the side walls has a catalyst feed port (the metallocene catalyst enters the reaction device through this port) and a reactant feed port (the raw material 1-decene enters the reaction device through this port), and the positions of these two feed ports are both near the paddle blades of the stirring paddle. The other relatively parallel side wall has a product discharge port (the poly-α-olefin product flows out of the reaction device through this port). The horizontal reaction kettle 10 is used to carry out a polymerization reaction on the reactants under the action of a catalyst to obtain the product poly-α-olefin.

[0045] Along the direction of material flow, five overflow partitions are successively arranged at the bottom of the inner cavity of the horizontal reactor 10, which are successively recorded as the first overflow partition, the second overflow partition, the third overflow partition, the fourth overflow partition and the fifth overflow partition. The shapes of the tops of the first overflow partition, the second overflow partition and the third overflow partition are all flat plates.

[0046] Along the direction of material flow, the overflow partition 11 is perpendicular to the bottom of the inner cavity and successively divides the inner cavity into six chambers, which are successively recorded as the first chamber, the second chamber, the third chamber, the fourth chamber, the fifth chamber and the sixth chamber. The upper parts of the first chamber, the second chamber, the third chamber, the fourth chamber, the fifth chamber and the sixth chamber are interconnected. The volume ratio of the first chamber, the second chamber, the third chamber, the fourth chamber, the fifth chamber and the sixth chamber is 100:45:16:7:6:5; among them, the distances from the side wall to the first overflow partition, from the first overflow partition to the second overflow partition, from the second overflow partition to the third overflow partition, from the third overflow partition to the fourth overflow partition, from the fourth overflow partition to the fifth overflow partition and from the fifth overflow partition to the other side wall are not equidistant, and the distance ratios are successively 10:5:2:1:1:1; the height differences between the first overflow partition, the second overflow partition, the third overflow partition, the fourth overflow partition and the fifth overflow partition are equi-gradient.

[0047] Stirring paddles are arranged inside the first chamber, the second chamber, the third chamber and the fourth chamber, and spiral heat exchange coils are arranged around the stirring paddles (the heat exchange coils are not limited to the positions at the same height as the stirring paddles and can extend upward and downward). The number of spiral turns of the spiral heat exchange coil in the first chamber is 50 turns, the number of spiral turns of the spiral heat exchange coil in the second chamber is 45 turns, the number of spiral turns of the spiral heat exchange coil in the third chamber is 40 turns, the number of spiral turns of the spiral heat exchange coil in the fourth chamber is 35 turns, the number of spiral turns of the spiral heat exchange coil in the fifth chamber is 30 turns, and the number of spiral turns of the spiral heat exchange coil in the sixth chamber is 25 turns. The diameters of the heat exchange coils in the first chamber, the second chamber, the third chamber, the fourth chamber, the fifth chamber and the sixth chamber are 40m, and the spiral diameter is 0.8 times the diameter of the chamber.

[0048] Baffles 14 are arranged on the inner side walls of each chamber, and the number of baffles is 4 (one baffle is distributed on each of the front, back, left and right walls of the chamber, Figure 1 and only 2 baffles arranged on the left side wall and the right side wall are shown).

[0049] The variable-frequency motor 20 and the stirring paddle 12 are connected by the motor output shaft 30. The variable-frequency motor 20 can drive the motor output shaft 30 and the stirring paddle 12 to rotate, thereby realizing the input of the stirring power; the motor output shaft 30 is connected to the variable-frequency motor 20 and the stirring paddle 12, and is responsible for the output of torque and the positioning of the stirring paddle 12; the stirring paddle 12 adopts a single-layer turbine paddle; the rotation speed of the variable-frequency motor 20 is 600 r / min, and no speed reducer is used.

[0050] All the equipment materials in the reaction device that come into contact with the reaction materials are made of stainless steel, and the stainless steel material has the advantages of corrosion resistance, high strength, and high temperature oxidation resistance.

[0051] This embodiment also provides a reaction method for producing high-viscosity poly-α-olefin, which includes:

[0052] Before the polymerization reaction starts, inject raw material 1-decene into the reaction device through the reactant feed port, and make it overflow section by section until the working liquid level is reached in the tail section chamber; turn on the variable-frequency motor 20, set the rotation speed of each motor according to the stirring requirements in each chamber until the flow is stable; adjust the temperature of the heat medium in the heat exchange coil 13 until the temperature in each chamber reaches the reaction requirements; introduce metallocene catalyst into the reaction device through the catalyst feed port to initiate the reaction; after the reaction is successfully initiated, switch the medium in the heat exchange coil 13 to a cold medium to cool the materials in each chamber and prevent explosive polymerization; gradually adjust the stirring speed until the reaction device reaches a stable state to continuously produce poly-α-olefin.

[0053] Among them, the conditions of the polymerization reaction include an initial reaction temperature of 70 °C; a reaction time of 1 h; a reaction pressure of 0.2 MPa.

[0054] Comparative Example 1

[0055] This comparative example provides a reaction device for producing high-viscosity poly-α-olefin, which includes three vertical kettle-type stirring reactors connected in series (connected by pipelines) in sequence.

[0056] Among them, along the material flow direction, the volume ratio of the reactors is 10:6:3; the total volume of the three reactors is the same as the volume of the horizontal reaction kettle in Example 1. Along the material flow direction, the heat exchange area ratio of the heat exchange coils in each reactor is 10:6:3.

[0057] The reaction conditions of the polymerization reaction are the same as those in Example 1.

[0058] The reaction apparatuses in Example 1, Example 2 and Comparative Example 1 were respectively used to continuously carry out polymerization reactions, and the liquid levels of the polymerization reactors were accurately monitored. When the pipeline was blocked by materials, the liquid levels in the first chamber of the reactor in Example 1 and Example 2 or the liquid level in the first reactor in Comparative Example 1 would show a continuous rising phenomenon. The time when the liquid level control became unstable corresponding to Example 1, Example 2 and Comparative Example 1 is shown in Table 1.

[0059] Table 1

[0060] Raw material flow rate 5 kg / h 10 kg / h 30 kg / h Example 1 >200h >200h >200h Example 2 >400h >400h >400h Comparative Example 1 20h 16h 10h

[0061] It can be found from Table 1 that after 200 h of operation in Example 1, the liquid level rose slightly but remained at a stable value; after 400 h of operation in Example 2, the liquid level did not show obvious changes; while after 20 h of operation in Comparative Example 1, the liquid level showed a rising phenomenon. The reaction apparatus and technical solution provided by the present utility model can effectively reduce the degree of material blockage in the reactor, and the overflow type of material flow mode can reduce the conveying difficulty of high-viscosity fluids between reaction chambers and effectively ensure the control of the material liquid level.

Claims

1. A reaction device for producing high-viscosity poly-α-olefin, characterized in that: It comprises a horizontal reactor (10); at least two overflow baffles (11) are arranged at the bottom of the inner cavity of the horizontal reactor (10); the overflow baffles (11) are perpendicular to the bottom of the inner cavity and divide the inner cavity into at least three chambers, and the upper parts of two adjacent chambers are connected; Along the direction of material flow, the volume of the chamber decreases and the height of the overflow baffle (11) decreases; The chamber is provided with a stirring paddle (12) and a heat exchange coil (13) surrounding the stirring paddle (12); A baffle (14) is arranged on the inner wall of the chamber.

2. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: Along the direction of material flow, the volume of the next chamber is 0.05 to 0.95 times the volume of the previous chamber.

3. The reaction device for producing high-viscosity poly-α-olefin according to claim 2, characterized in that: Along the direction of material flow, the height of the next-level partition is 0.05 to 0.95 times the height of the previous-level partition.

4. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: The number of the overflow baffles (11) is 3 to 10.

5. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: The aspect ratio of the horizontal reactor (10) is 3 to 10:

1.

6. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: The diameter of the stirring paddle (12) is greater than or equal to 0.2 times the diameter of the chamber and less than 1.0 times the diameter of the chamber.

7. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: The heat exchange coil (13) is a spiral heat exchange coil.

8. The reaction device for producing high-viscosity poly-α-olefin according to claim 7, characterized in that: The number of spiral turns of the spiral heat exchange coil is 5 to 50, and the spiral diameter is 0.2 to 0.8 times the diameter of the chamber.

9. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: The width of the baffle (14) is 0.02 to 0.2 times the diameter of the chamber.

10. The reaction device for producing high-viscosity poly-α-olefin according to claim 1, characterized in that: It also includes a variable frequency motor (20) and a motor output shaft (30); the variable frequency motor (20) and the stirring paddle (12) are connected via the motor output shaft (30).

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