Reaction kettle and reaction system

Abstract

The utility model provides a reaction kettle and a reaction system. The reaction kettle comprises a reaction kettle main body, wherein the reaction kettle main body is provided with an upper feed port and a lower discharge port; a heat exchange assembly and a flow guide assembly are sequentially arranged at the upper part in the reaction kettle main body from top to bottom, and the heat exchange assembly is positioned below the upper feed port; the flow guide assembly is arranged to be capable of circumferentially rotating relative to the axial direction of the reaction kettle main body, so that condensate condensed by the heat exchange assembly can be guided to the inner wall of the reaction kettle. When the reaction kettle runs, condensate obtained by condensation of the cooling disc can be guided to flow down along the wall of the reaction kettle through rotation of the flow guide assembly, so that a small amount of reaction liquid or viscous or solid polymers sputtered to the wall of the kettle is scoured, an interface near the reaction liquid level is effectively cooled, the material caking working condition at the reaction interface is reduced, and the reaction efficiency is improved. And the product quality is improved.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of chemical equipment, concretely relates to a reaction kettle and reaction system. BACKGROUND

[0002] In chemical production, many important polymerization, condensation and other chemical reaction processes are accompanied by strong exothermic effect, and have the characteristics of fast reaction rate and concentrated heat release, which puts forward very high requirements for instantaneous heat removal and accurate temperature control of the reaction system.

[0003] The traditional jacketed reaction kettle widely used in industry mainly relies on the cooling medium in the jacket for heat removal. However, the inventors of the utility model have found that in response to such rapid and strong exothermic reactions, the traditional reaction kettle has an inherent defect: the heat transfer efficiency of the area near the reaction liquid surface (i.e. the "gas-liquid-solid" three-phase interface composed of gas phase, liquid phase and possibly existing solid catalyst or product particles) is much lower than that of the main liquid phase area in the kettle body. This is because the fluid disturbance at the liquid surface is weakened, and the cooling effect of the jacket cannot directly and efficiently cover this area, resulting in a local heat accumulation zone with a higher temperature than the main liquid phase temperature in the reaction kettle.

[0004] The existence of the heat accumulation zone near the reaction liquid surface area can cause a series of problems: for example, the local heat accumulation can cause the reactants at the interface to undergo secondary reactions, such as excessive polymerization, crosslinking, degradation, etc., generating viscous or solid polymers; these viscous or solid polymers can adhere to the kettle wall, baffle, thermometer sleeve, and the surface of all internal components above the liquid level, forming hard coking; and these coking under the action of mechanical stirring, fluid scouring, etc. in the reaction system, will fall off from the inner wall, break and mix into the final product in the form of impurity particles or fine powder. Process practice has confirmed that the generation of these coking and fine powder seriously affects the product quality (such as purity, particle size distribution), reduces the product yield, increases the burden and cost of subsequent separation and purification, and greatly reduces the production efficiency and continuity of the equipment due to the need for frequent shutdown for cleaning. SUMMARY

[0005] In view of the deficiencies in the prior art, the utility model discloses a reaction kettle and reaction system, which solves the problem of high proportion of caked and fine powder products caused by the existence of the heat accumulation zone near the reaction liquid surface area in the prior art, improves the yield of qualified products, and improves the absorption performance of the products.

[0006] In order to achieve the above technical purposes, on the one hand, the utility model provides a reaction kettle, which comprises:

[0007] A reaction kettle body, which is provided with an upper feed inlet and a lower discharge outlet;

[0008] A heat exchange assembly and a flow guide assembly are sequentially arranged from top to bottom in the upper portion of the reaction kettle body, and the heat exchange assembly is located below the upper feed inlet; wherein the flow guide assembly is arranged to rotate relative to the axial direction of the reaction kettle body, thereby guiding the condensed liquid condensed by the heat exchange assembly to the inner wall of the reaction kettle.

[0009] In further examples of the present application, the flow guide assembly comprises: a central through hole for sleeving the flow guide assembly on the stirring device of the reaction kettle; a frame surrounding the central through hole and providing a steam passage; a plurality of flow guide vanes movably connected to the periphery of the frame by connecting members; wherein the flow guide vanes are configured to gradually lift from the stowed state to the working angle under the action of centrifugal force generated by the rotation of the flow guide assembly, so as to guide the condensed liquid condensed by the heat exchange assembly to the inner wall of the reaction kettle.

[0010] In further examples of the present application, the projections of the adjacent two flow guide vanes in the vertical direction at least partially overlap and the overlapping parts are at different horizontal heights to form a passage for steam to pass through in the overlapping area, wherein the vertical direction refers to the direction perpendicular to the bottom of the reaction kettle.

[0011] In further examples of the present application, the connecting members are hinge connecting members, so that the flow guide vanes are rotatably connected to the frame.

[0012] In further examples of the present application, N reaction zones are sequentially arranged in the reaction kettle body along the axial direction from bottom to top, N≥2, and each reaction zone is provided with an independent temperature control unit, so as to independently control the temperature of the reaction materials at different liquid levels.

[0013] In further examples of the present application, the independent temperature control unit is a jacket or an inner coil.

[0014] In further examples of the present application, the independent temperature control unit is provided with a reaction zone temperature sensor group for monitoring the control temperature of the corresponding polymerization reaction zone.

[0015] In further examples of the present application, the reaction kettle top space is provided with a gas phase temperature sensor for monitoring the gas phase temperature in the kettle.

[0016] In further examples of the present application, the reaction kettle lower portion is provided with a liquid phase temperature sensor for monitoring the temperature of the reaction system.

[0017] In further examples of the present application, the ratio of the height of at least one of the second to Nth reaction zones to the height of the first reaction zone is 0.4-0.9.

[0018] In further examples of the present application, the stirring device is a frame stirring paddle, and the diameter of the frame stirring paddle is 0.6-0.95 times the diameter of the reactor body.

[0019] In further examples of the present application, the height of the stirring paddle is 0.3-0.8 times the total height of the reaction zone inside the reactor.

[0020] In further examples of the present application, the stirring paddle is a frame stirring paddle, and the diameter of the frame stirring paddle is 0.6-0.95 times the diameter of the reactor body.

[0021] Compared with the prior art, the present application has the beneficial effects that: the reactor of the present application can guide the condensate obtained by the cooling disc to flow down along the reactor wall by rotating the flow guide assembly during the operation of the reactor, so as to flush the reaction liquid or the viscous or solid polymer splashed to the wall, effectively cool the interface near the reaction liquid surface, and reduce the material caking condition at the gas-liquid-solid three-phase interface, thereby improving the quality of the product.

[0022] The reaction system comprising the above-mentioned reactor can realize batch feeding and post-treatment operations such as dehydration and drying after reaction, improve production efficiency, and obtain products with excellent performance. BRIEF DESCRIPTION OF DRAWINGS

[0023] The accompanying drawings, which form a part of this application, are included to provide a further understanding of the application, and are incorporated in and constitute a part of this application. The embodiments illustrated in the drawings, and their description, serve to explain embodiments of the present application and do not limit the present application in any manner. In the drawings:

[0024] Figure 1 FIG. 1 shows a structure schematic view of a segmented temperature control reactor for preparing a water-absorbing resin according to the present application.

[0025] Figure 2 FIG. 5 shows a top view structure schematic view of a flow guide assembly.

[0026] Figure 3 FIG. 6 shows a side view structure schematic view of a flow guide assembly.

[0027] Figure 4 FIG. 7 shows a structure schematic view of a flow guide assembly in a folded structure.

[0028] Wherein, the above-mentioned drawings include the following reference signs:

[0029] 1-reactor main body, 21-upper feeding port, 22-lower discharging port, 3-jacket, 4-heat exchange component, 5-flow guide component, 51-center through hole, 52-connecting shaft, 53-frame, 54-connector, 55-flow guide fan blade, 6-stirring paddle, 71-first temperature sensor, 72-second temperature sensor, 73-third temperature sensor, 74-fourth temperature sensor, 75-gas phase temperature sensor, 76-liquid phase temperature sensor. DETAILED DESCRIPTION

[0030] In order to facilitate the understanding of the present application, the present application will be described more fully below, and the preferred embodiments of the present application are given. But it should be understood that these embodiments are only used for more detailed description, and should not be understood as limiting the present application in any form, that is, not intended to limit the scope of protection of the present application.

[0031] Unless otherwise defined, the technical terms used in the following examples have the same meaning as generally understood by those skilled in the art to which the present application belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods, unless otherwise specified, are all conventional methods. In the description of the present application, unless otherwise explicitly specified and limited, the terms "connected", "connected", "fixed" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the internal communication of two elements or the interaction relationship between two elements. For ordinary skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0032] In the present application, unless otherwise explicitly specified and limited, the "upper" or "lower" of the first feature to the second feature can include the direct contact of the first and second features, or can include the contact of the first and second features through another feature between them. Moreover, the "above" and "above" of the first feature to the second feature includes the vertical and oblique above of the first feature to the second feature, or only indicates that the horizontal height of the first feature is higher than that of the second feature. The "below" and "below" of the first feature to the second feature includes the vertical and oblique below of the first feature to the second feature, or only indicates that the horizontal height of the first feature is less than that of the second feature.

[0033] In the description of this embodiment, terms such as "upper," "lower," and "right" are based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of description and simplification of operation, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model.

[0034] Example 1

[0035] A type of reaction vessel, such as Figure 1 As shown, the reactor includes: a reactor body 1, which has an upper feed inlet 21 and a lower discharge outlet 22; in the upper part of the reactor body 1, a heat exchange component 4 and a flow guiding component 5 are arranged sequentially from top to bottom, and the heat exchange component 4 is located below the upper feed inlet 21; wherein, the flow guiding component 5 is configured to be able to rotate circumferentially relative to the axial direction of the reactor body 1, thereby guiding the condensate condensed by the heat exchange component 4 to the inner wall of the reactor.

[0036] In this embodiment, during operation, the reaction heat in the upper space can be removed and condensed by the heat exchange component 4 to obtain condensate. The flow guiding component 5 is located below the condensate's falling path and is connected to it. When rotating, the flow guiding component 5 uses centrifugal force to spray and distribute the received condensate onto the inner wall of the reactor, forming a continuous condensate flow that washes over and cools the heat accumulation zone near the reaction liquid surface, thus suppressing coking and deposition near the reaction liquid surface on the inner wall of the reactor.

[0037] It should be noted that the specific structure of the flow guiding component 5 is not limited in this utility model. Any equipment or facility that can rotate circumferentially along the main body 1 of the reactor and guide the condensate condensed from the upper heat exchange component 4 to the inner wall of the reactor is acceptable. For example, the flow guiding component 5 can be a flow guiding channel group. The condensate condensed from the heat exchange component 4 drips onto the flow guiding channel group, and then, under the action of centrifugal force, the condenser in the flow guiding channel group is thrown towards the inner wall of the reactor, thereby washing away the solids accumulated on the inner wall of the reactor near the surface of the reaction liquid. The heat exchange component 4 is used to condense the steam in the upper gas phase space of the reactor. Optionally, the specific structure of the heat exchange component 4 is not limited in this embodiment. For example, the heat exchange component 4 can be a tubular heat exchanger or a plate heat exchanger. Any equipment that can achieve heat exchange with the whole system is acceptable. In an optional example of this embodiment, the heat exchange component 4 is a tubular cooling coil.

[0038] Optionally, the inner wall of the reactor body 1 and / or the surface of the heat exchange component 4 and / or the surface of the flow guiding component 5 are coated with a hydrophobic coating, which is a fluoropolymer material coating. Further optionally, the hydrophobic coating has a thickness ranging from 0.1 to 0.3 mm and a surface contact angle greater than 120°, which can effectively reduce material adhesion and improve the absorption performance of the product.

[0039] Optionally, there is no gap or a gap between the heat exchange assembly 4 and the flow guide assembly 5. When there is a gap, the height of the gap is not more than 10 cm, which provides an operating buffer zone between the heat exchange assembly 4 and the flow guide assembly 5, so as to facilitate the condensate to fall more smoothly into the flow guide disc.

[0040] Embodiment 2

[0041] Based on the reaction kettle shown in Embodiment 1, the structure of the flow guide assembly 5 is optimized in this embodiment.

[0042] Optionally, as shown in Figure 2 the flow guide assembly 5 includes a central through hole 51 for sleeving the flow guide assembly 5 on the stirring device of the reaction kettle, a frame 53 surrounding the central through hole 51 to provide a steam passage, and a plurality of flow guide vanes 55 movably connected to the periphery of the frame 53 through a connecting piece 54. The flow guide vanes 55 are configured to gradually lift from a retracted state to a working angle under the action of centrifugal force generated by the rotation of the flow guide assembly 5, so as to guide the condensate condensed by the heat exchange assembly 4 to the inner wall of the reaction kettle.

[0043] Optionally, the flow guide assembly 5 of this embodiment can be connected to a separate driving device or fixed to the stirring device of the reaction kettle and rotate coaxially with the stirring device. When the driving device is started, i.e. the flow guide assembly 5 is in a working state, the flow guide vanes 55 can gradually lift from a retracted state to a working angle under the action of centrifugal force generated by rotation, so as to guide the steam condensate to the inner wall of the reaction kettle. It should be noted that the rotation angle of the flow guide vanes 55 can be adjusted according to the driving rate of the driving device. Figure 3 A side view structure of one operating state of the flow guide assembly 5 is shown.

[0044] Optionally, the projections of two adjacent flow guide vanes 55 in the vertical direction at least partially overlap and the overlapping parts are at different horizontal heights, so as to form a passage for steam to pass through in the overlapping area. The central through hole 51 of the flow guide assembly 5 of this embodiment can be used for steam passage or for stirring shaft or other axial equipment to pass through, which improves the operation flexibility of the reaction kettle. In addition, the frame 53 can also provide a passage for the steam to rise to the heat exchange assembly 4. Moreover, the projections of two adjacent flow guide vanes 55 in the vertical direction at least partially overlap (such as the dashed line part formed by the two adjacent flow guide vanes 55 in Figure 2 the vertical direction) and the overlapping parts are not in the same horizontal plane (axial height is staggered), which not only ensures that the liquid condensed by the heat exchange assembly 4 falls as much as possible on the flow guide vanes, but also forms an air passage, so that the steam evaporated in the reaction kettle can be transmitted to the heat exchange assembly 4, thereby improving the heat exchange efficiency and meeting the heat exchange demand in the reaction kettle.

[0045] Optionally, the flow guide assembly 5 further comprises a connecting shaft 52 for connecting the driving device, and a frame 53 connected to the connecting shaft 52. By providing the connecting shaft 52, the flow guide assembly 5 can rotate independently of the stirring shaft, and under the action of centrifugal force, the condensed material can be thrown to the inner wall of the reactor.

[0046] Optionally, the connecting member 54 is a hinge connecting member, so that the flow guide fan blade 55 is rotatably connected to the frame 53. In this way, when the driving device of the flow guide assembly 5 is not working, the hinge and the flow guide fan blade 55 are in a folded state (as shown in Figure 4 ), which is convenient for feeding operation to avoid the newly added material in the reactor falling on the flow guide fan blade 55. It should be noted that when the material is added to the reactor, the flow guide assembly 5 is in a non-working state, i.e. in a folded state, so that the material added from the upper feeding port 21 can smoothly enter the reactor, avoiding the material falling on the flow guide assembly 5.

[0047] Embodiment 3

[0048] Based on the reactor shown in Embodiment 1, the reactor body 1 in this embodiment is provided with a stirring device, which is a frame stirring paddle 6. Through rotational movement, the material in the reactor is fully mixed, ensuring uniform temperature distribution and improving reaction efficiency.

[0049] Optionally, the diameter of the stirring paddle 6 is 0.6-0.95 times the diameter of the reactor body 1, so as to facilitate the radial stirring action of the stirring device to fully disperse the material.

[0050] Optionally, the height of the stirring paddle 6 is 0.3-0.8 times the total height of the reaction zone inside the reactor, so as to promote the mass transfer contact of the material in the reaction zone from the axial angle of the reactor.

[0051] Optionally, the stirring paddle 6 is a frame stirring paddle comprising at least a pair of vertical rods, which can increase the dispersion efficiency, make the particle dispersion more uniform, avoid excessive adhesion between particles, and also increase the strength of the stirring paddle 6 to some extent.

[0052] Embodiment 4

[0053] Based on the reactor shown in Embodiment 1, a heat exchange device such as a jacket 3 can be optionally provided outside the reactor body 1 to timely remove the reaction heat. The device for heat exchange of the reactor in this embodiment is optimized.

[0054] Optionally, the reactor body 1 is sequentially provided with N reaction zones in the axial direction from bottom to top, N≥2, and each reaction zone is provided with an independent temperature control unit, so that the reaction materials at different liquid levels are independently controlled in sections. Thus, by adjusting the temperature near the reaction liquid surface, heat accumulation can be further prevented. In combination with the technical feature of the flow guide assembly 5 for guiding the condensed liquid to the inner wall of the reactor, the temperature at the reaction liquid surface is adjusted to an appropriate range, which ensures efficient reaction while avoiding the generation of viscous or solid polymers due to high temperature.

[0055] The specific structure of the temperature control unit of each reaction zone in this embodiment is not limited, and any device that can achieve independent temperature control of different reaction zones in the reactor can be used, such as a jacket 3, an inner coil, or other devices that can achieve heat exchange. Those skilled in the art can choose as needed. Optionally, the independent temperature control unit is a jacket 3 or an inner coil.

[0056] In this embodiment, a plurality of temperature monitoring devices are also provided.

[0057] Optionally, the independent temperature control unit is provided with a reaction zone temperature sensor group for monitoring the control temperature of the corresponding reaction zone. The reaction zone temperature sensor group is arranged in the temperature control unit of different reaction zones, so as to monitor the temperature control of different reactions in real time and improve the operation accuracy of the reactor. Figure 1 The first temperature sensor 71, the second temperature sensor 72, the third temperature sensor 73, and the fourth temperature sensor 74 are shown for monitoring the temperature of the heat transfer medium in the jacket 3 of the first to fourth reaction zones, respectively.

[0058] Optionally, the gas phase temperature sensor 75 is arranged at the top space of the reactor for monitoring the gas phase temperature in the reactor.

[0059] Optionally, the liquid phase temperature sensor 76 is arranged at the lower part of the reactor for monitoring the temperature of the reaction system when the reactor is running.

[0060] Optionally, these temperature sensors are electrically connected with the display panel, and can display the temperature data of the heat transfer medium of the temperature control unit, the gas phase space, and the liquid phase space (reaction system) in real time. In actual operation, the operator can intuitively understand the temperature distribution in the reactor through the display panel, and adjust the flow or temperature setting value of the independent temperature control unit as needed, so as to realize precise temperature control.

[0061] It should be noted that the relative height of each reaction zone is not limited, and the skilled person in the art can set multiple reaction zones with appropriate relative height according to the needs of batch feeding materials. In the optional example of the present application, the ratio of the height of at least one reaction zone in the second reaction zone to the Nth reaction zone to the height of the first reaction zone is 0.4-0.9, preferably 0.65-0.75, more preferably 0.68-0.72, and even more preferably 0.65, thereby facilitating the improvement of product performance and the regulation of particle size distribution.

[0062] It should be noted that the present application is not limited to the specific value of N, and the number of reaction zones that need to be independently temperature-controlled in the reaction kettle can be adjusted according to actual needs. Figure 1 An example of a segmented temperature control reaction kettle comprising four reaction zones from bottom to top is shown, and the independent temperature control unit in the figure is a jacket 3; the height of the first reaction zone in the reaction kettle is twice the height of the second to fourth reaction zones.

[0063] Example 5

[0064] This embodiment shows the process of preparing a water-absorbing resin using an exemplary reaction system of the present application. It should be noted that this embodiment is only a better display and does not limit the scope of protection of the present application.

[0065] It should be noted that when any material is added to the reaction kettle in this embodiment, the flow guide assembly 5 is in a retracted state to avoid material dripping onto the flow guide assembly 5.

[0066] Specifically: this embodiment uses Figure 1 the reaction kettle shown to prepare a water-absorbing resin, and the process includes two batches of reaction material feeding processes. Specifically:

[0067] (1) Preparation stage: add 1000 mL of hydrocarbon dispersion medium (n-hexane) and 4.0 g of emulsifier (sucrose fatty acid ester) to the reaction kettle; the control temperature of the first polymerization reaction zone in this stage is 65°C, the control temperature of the second polymerization reaction zone is 65°C, and the control temperature of the third and fourth polymerization reaction zones is 50°C.

[0068] (2) First batch polymerization stage: a first batch of reactants was added to the reactor, 800 g of 35% monomer aqueous solution (75% neutralization degree of acrylic acid), 0.3 g of initiator (sodium persulfate), 0.1 g of crosslinking agent (ethylene glycol), and 0.4 g of thickening agent (methyl cellulose) were added for polymerization. After adding the first batch of reactants, the liquid level of the reaction system was about 50% of the height of the second polymerization zone. During the polymerization process, the temperature sensor was used to monitor: al) the main polymerization stage in which the exothermic peak appeared in the reaction system and fell to the reference temperature 1 °C before the peak, the control temperature of the first polymerization zone was 75 °C, the control temperature of the second polymerization zone was 65 °C, and the control temperature of the third and fourth polymerization zones was 50 °C. b1) Then the control temperature of the first polymerization zone was set to 95 °C, the control temperature of the second polymerization zone was set to 65 °C, and the control temperature of the third and fourth polymerization zones was set to 50 °C to promote the reaction system to continue the holding reaction for about 60 min, and the first batch of polymerization product was obtained.

[0069] (3) Second batch polymerization stage: 800 g of 35% monomer aqueous solution, 0.3 g of initiator, 0.1 g of crosslinking agent, and 0.4 g of thickening agent were added to the reactor, so that the reaction system was located at about 50% of the height of the third polymerization zone. During the polymerization process, the temperature sensor was used to monitor: a2) the main polymerization stage in which the exothermic peak appeared in the reaction system and fell to the reference temperature 1 °C before the peak, the control temperature of the first and second polymerization zones was 75 °C, the control temperature of the third polymerization zone was 65 °C, and the control temperature of the fourth polymerization zone was 50 °C. b2) Then the control temperature of the first and second polymerization zones was set to 95 °C, the control temperature of the third polymerization zone was set to 65 °C, and the control temperature of the fourth polymerization zone was set to 50 °C to promote the reaction system to continue the holding reaction for about 60 min; after the reaction was completed, dehydration and drying were performed to obtain the water-absorbing resin product.

[0070] The water-absorbing resin has a particle size ratio of 93% in the range of 100-800um, a free absorption (g / g) of 66, and a pressurized absorption (g / g) of 37. The water-absorbing resin prepared by using the reaction kettle comprising a flow guide assembly and an independent temperature control unit has a very high qualified particle size ratio and excellent absorption performance. Specifically, the particle size ratio of the product in the range of 100-800um is as high as 93%, which reflects that the particle growth is uniform and the fine powder is very little during the reaction process, and the particle size distribution is highly concentrated. The free absorption is 66 g / g, and the pressurized absorption is 37 g / g, which indicates that the resin particles have a complete porous structure and high strength, and there is no obvious hardening agglomeration inside. It is confirmed that the temperature is uniform and stable during the reaction process of the embodiment, and there is no local overheating condition. The free absorption and pressurized absorption testing method is as follows: 0.9% sodium chloride aqueous solution is used as simulated urine according to the testing method specified in GB / T 22875-2018, and the physiological saline absorption (g / g) and pressurized absorption (g / g) of the product are measured, wherein the pressurized absorption of the water-absorbing resin is measured by using a load of 4.14kPa.

[0071] It should be noted that the above is a further detailed description of the present application in combination with specific embodiments, and cannot be considered as limiting the specific implementation of the present application to these descriptions. The size data of the embodiment does not limit the technical solution, but only shows one specific working condition. For ordinary skilled persons in the technical field to which the present application belongs, some simple improvements and decorations can be made without departing from the concept of the present application, and all of them should be considered as belonging to the protection scope of the present application.

Claims

1. A reaction vessel, characterized by, The application relates to a reaction kettle, which comprises the following: a reaction kettle body (1) provided with an upper feeding port (21) and a lower discharging port (22); a heat exchange assembly (4) and a flow guide assembly (5) are sequentially arranged in the upper portion of the reaction kettle body (1) from top to bottom, and the heat exchange assembly (4) is arranged below the upper feeding port (21); wherein the flow guide assembly (5) is arranged to be rotatable relative to the circumferential direction of the reaction kettle body (1), so as to guide the condensed liquid condensed by the heat exchange assembly (4) to the inner wall of the reaction kettle.

2. The reactor of claim 1, wherein The flow guide assembly (5) comprises: a central through hole (51) for sleeving the flow guide assembly (5) on the stirring device of the reaction kettle; a frame (53) surrounding the central through hole (51) and providing a steam passage; a plurality of flow guide vanes (55) movably connected to the periphery of the frame (53) through connecting pieces (54); wherein the flow guide vanes (55) are configured to gradually lift from a retracted state to a working angle under the action of centrifugal force generated by the rotation of the flow guide assembly (5), so as to guide the condensed liquid condensed by the heat exchange assembly (4) to the inner wall of the reaction kettle.

3. The reactor of claim 2, wherein The projections of the adjacent two flow guide vanes (55) in the vertical direction at least partially overlap and the overlapping parts are at different horizontal heights, so as to form a passage for steam passing through in the overlapping area.

4. The reactor of claim 2 or 3, wherein The connecting piece (54) is a hinge connecting piece, so that the flow guide vane (55) is rotatably connected to the frame (53).

5. The reactor of claim 1, wherein N reaction zones are sequentially arranged in the reaction kettle body (1) along the axial direction from bottom to top, N>=2, and each reaction zone is provided with an independent temperature control unit, so that the reaction materials at different liquid levels are independently controlled in sections.

6. The reactor of claim 5, wherein The independent temperature control unit is a jacket or an inner coil; and / or, the independent temperature control unit is provided with a reaction zone temperature sensor group for monitoring the control temperature of the corresponding polymerization reaction zone; and / or, the reaction kettle top space is provided with a gas phase temperature sensor (75) for monitoring the gas phase temperature in the kettle; and / or, the reaction kettle lower portion is provided with a liquid phase temperature sensor (76) for monitoring the temperature of the reaction system.

7. The reactor of claim 5 or 6, wherein The height ratio of at least one of the second to Nth reaction zones to the first reaction zone is 0.4-0.

9.

8. The reactor of claim 1, wherein The reaction kettle body (1) is provided with a stirring device, and the stirring device is a frame type stirring paddle (6); the diameter of the stirring paddle (6) is 0.6-0.95 times the diameter of the reaction kettle body (1).

9. The reactor of claim 8, wherein, The height of the stirring paddle (6) is 0.3-0.8 times the total height of the reaction zones in the reaction kettle.

10. A reaction system characterized by, The application further relates to a reaction kettle, a feeding device and a dehydration drying device according to any one of claims 1-9; wherein the feeding device is connected with the upper feeding port (21) of the reaction kettle and is used for adding reaction materials into the reaction kettle body (1) in batches; and the dehydration drying device is connected with the lower discharging port (22) of the reaction kettle and is used for receiving reaction products and performing post-treatment on the reaction products.

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