KR910005676B1 - Stirring device and stirred tower polymerization reactor - Google Patents

Abstract

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Description

Stirring device and stirred tower polymerization reactor

1 is a longitudinal sectional view of the first embodiment of the present invention.

2 is a cross-sectional view taken along the line I-I of FIG.

3 is a schematic explanatory diagram showing a flow form of a first embodiment of the present invention.

4 and 5 are schematic explanatory diagrams showing the flow patterns at the circumferential adjacent portions and the inner portions of the container as viewed from the A-A plane of FIG. 3, respectively.

6 is a front view of a second embodiment of the present invention.

7 is a plan view of FIG.

8 is a front view of a third embodiment of the present invention.

9 is a plan view of FIG.

10 is a front view of a fourth embodiment of the present invention.

11 is a plan view of FIG.

12 is a longitudinal cross-sectional view of one embodiment of a reactor of the present invention.

13 is a cross-sectional view taken along the line III-III of FIG.

14 is a longitudinal sectional view of another embodiment of a reactor of the present invention.

15 is a cross-sectional view taken along the line IV-IV of FIG.

16 is a longitudinal sectional view of another embodiment of a reactor of the present invention.

FIG. 17 is a cross-sectional view taken along the line VI-VI of FIG. 16. FIG.

18 is a graph showing the experimental results of the residence time distribution obtained in Comparative Examples B1 and B2 and Experimental Examples B1 to B3 of the present invention.

* Explanation of symbols for main parts of the drawings

1, 24: container 2, 25: rotating shaft

3, 29: flat 4, 30: inclined wings

5, 50: center line 6, 51: inner wall of the container

7 fluid surface 21 fluid supply port

22: fluid outlet 23: jacket

26 sealing means 27 blocking plate

28: stirring chamber 40: tube fixed plate

41: outlying body 42: tube

The present invention relates to a stirring apparatus used as a reaction apparatus, for example, in which a reaction of a highly viscous substance such as a viscous solution or slurry is performed by stirring to obtain a uniform product.

The present invention also relates to a polymerization reactor having excellent performance in continuously producing a polymer compound. In particular, the present invention relates to a continuous polymerization reactor used for solution polymerization and bulk polymerization in a high viscosity homogeneous system.

As described in Shinji Nagada's book, Mixing Principles and Applications (1976, published by High Yarn), agitators for highly viscous materials have significantly larger paddle-shaped wings, anchor wings, spiral ribbon wings and spirals. Screwed vanes have been used. The large flat wing and the anchor wing were simple in structure and easy to manufacture and clean, but were unable to stir the highly viscous material effectively.

In particular, if the Reynolds number, Re (= ρnd / μ, where ρ is density, n is rotational speed, d is the radius of the blade, μ is the viscosity) is equal to or less than ten units or more, It was very bad.

On the other hand, spiral ribbon blades and spiral screw blades fixed to the vertical tube have excellent performances for agitating high-viscosity materials and excellent performance even when the Reynolds number is low, but the structure is complicated. Difficulty and cost of production was also high and there was a difficulty in cleaning.

In addition, although a solution and a bulk polymerization reaction have been widely used as a polymerization reaction for preparing a polymer compound, when the polymer is dissolved in monomers and solvents in this solution and the bulk polymerization method, the polymerization process proceeds to homogeneity and It becomes a high viscosity.

For example, the polymerization reaction can be exemplified as follows.

Mass polymerization of polymethyl methacrylate, mass polymerization of solution and acrylonitrile-styrene resin, solution polymerization of acrylonitrile-butadiene-styrene resin, solution polymerization of polybutadiene, solution polymerization of styrene-butadiene rubber, ε-capro Polycondensation of nylon 6 using lactam as a raw material (particularly the initial step), polycondensation of nylon 66 using adipic acid and hexamethylenediamine as a raw material (particularly an intermediate step) and solution polymerization of polyvinyl acetate And the like. General requirements for the continuous polymerization of highly viscous reaction fluids are described in detail in the 1976 Basics and Analysis of Murugami Yasuhiro Rogers, published by Bifugan.

The requirements extracted from the booklet may be listed as follows.

(1) The residence time distribution should be sharp, ie the characteristics of the extrusion flow are required.

(2) The stirring efficiency should be high so that the temperature and concentration distribution in all parts of the flow direction are uniform.

(3) There should be no spaces in the reactor, which are obstructed by flow, in other places.

(4) Less power required for stirring.

(5) Heat transfer surface and heat transfer coefficient should be large to remove reaction heat rapidly.

(6) The structure of the device should be simple and easy to clean.

Although a number of polymerization apparatuses have already been proposed due to research efforts to satisfy the above requirements, no sufficiently satisfactory apparatus has yet been proposed.

As an example of the proposed continuous polymerization apparatus, there is an apparatus of the association such as Japanese Patent Application No. 127489/1979, which has a drawback such as high power required for stirring, narrow heat transfer area, and complexity of structure. Japanese Patent Laid-Open Publication No. 99290/1978 was also a reactor having problems with extrusion flow characteristics.

In addition, Japanese Patent Laid-Open No. 202720/1985 has a problem in that the structure becomes complicated due to two rotation shafts.

As in the above example, the already proposed continuous polymerization apparatus had several problems.

An object of the present invention is to solve the above problems of the stirring device, and to provide a new stirring device having a simple structure with high stirring performance for a high viscosity material.

Another object of the present invention is to provide a sharp residence time distribution (i.e. extrusion flow characteristics) to solve the problems of the polymerization reactions described above, mixing of all stirrability on the stirring surface, high heat transfer coefficient, simple It is an object of the present invention to provide a stirred tower polymerization apparatus having no obstacle in structure and flow surface and having low power for stirring.

The present invention provides a stirring device comprising a vessel, a rotary shaft inserted into the vessel and installed vertically, and a flat blade having an area of at least 60% of the cross-sectional area formed by the axis of rotation axis, the inner wall of the vessel and the surface of the agitated material in the vessel. Will be provided.

The flat blade is fixed parallel to the axis of rotation.

The stirring device of the present invention has the following effects and effects by the rotation of the large flat blade and the inclined blade inside the container.

(1) The large flat blades produce two types of flows: fast on the outside and slow on the inside.

(2) Two types of flow Another upward and downward flow is generated by inclined vanes arranged on one side or both sides.

(3) As the effects of (1) and (2), the circulation is excellent in all parts of the container, whereby the stirring can be carried out efficiently and rapidly.

By using the principle of the stirring device as described above, the present invention provides a cylindrical container having a fluid supply port and a fluid discharge port; A rotating shaft inserted into the container in a concentric manner and vertically installed; A plurality of flat blades mounted on the rotary shaft and a plurality of inclined blades mounted on the rotary shaft at a predetermined angle from the center line in a pair so as to have a surface essentially parallel to the center line of the rotary shaft. Stirring means consisting of; It is to provide a stirred tower polymerization reactor composed of partition means for partitioning the vessel in the longitudinal direction between the stirring means.

In the reactor of the above structure, the fluid is supplied into the vessel through the fluid supply port and is introduced into the stirring zone partitioned by the partition means in the longitudinal direction. In this stirring zone, flat blades and inclined blades, which function as stirring means as in the stirring device described above, are mounted on a rotating shaft, which rotates upwards, downwards, and horizontally as a combined effect of the two types of wings. Circulating flow such as

This fed fluid is agitated and sufficiently mixed to be transferred to one stirring zone for further mixing and discharged out of the device through the fluid outlet of the vessel.

Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. Several embodiments of the stirring device of the present invention will first be described with reference to FIGS. 1 to 11.

Next, three examples of the apparatus used for the polymerization reaction of the present invention will be described with reference to FIGS.

1 and 2 show one embodiment of the stirring device of the present invention.

The rotating shaft 2 is vertically installed inside the container 1, and the flat plate reaction 3 and the inclined blade 4 are fixed to the rotating shaft 2. The flat blade 3 is installed in essentially parallel with the center line 5 of the rotation shaft 2, the area of the flat blade 3 is the center line 5 of the rotation shaft 2, the inner wall 6 of the container and 60% or more of the cross-sectional area formed by the fluid surface 7 cannot be obtained when the stirring area is 60% or less, and the reason will be described later. The inclined vanes 4 are also fixed to the rotation axis 2 at a predetermined angle with respect to the centerline 5. FIG. 3 flows due to the planar cross-section of vessel 1 (cross section III-III in FIG. 1) upon stirring the highly viscous material using the vanes 3 and 4 shown in FIGS. It shows the form of. When the flat blade 3 moves at a predetermined speed (indicated by arrow 10), the outer portion of the fluid is pushed by the flat blade 3 to move in the same direction as the blade 3.

However, due to the effect of the viscous resistance between the wing 3 and the inner wall 6, it is different from the volume of the fluid adjacent to the circumference. This difference is adjacent to the flat blade 3, causing radial flow as indicated by the radial flow rate (indicated by arrow 12).

When the radial flow toward the center reaches the center, the flow direction is changed to become a flow circulating inward as the inner flow velocity (indicated by arrow 13).

Thus, the inner circulation flow generated in this manner becomes strong, so that the inner flow velocity 13 is larger than the velocity at the surface of the rotating shaft 2 (indicated by arrow 14) and the velocity at its inner side of the inclined blade 4. do.

On the other hand, the velocity 11 of the fluid adjacent to the circumference becomes considerably smaller than the velocity (indicated by arrow 16) at its outer side of the inclined blade 4.

4 shows the shape of the flow adjacent to the circumference viewed from the A-A plane in the direction indicated. Since the velocity 11 in the fluid adjacent to the circumference is small compared to the velocity (indicated by arrow 16) of the inclined vanes 4, the fluid is moved downwards as indicated by arrow 17.

5 shows the shape of the flow in the inner part seen from the A-A plane.

The apparatus of the present invention is completely different in this area from the case where it is adjacent to the circumference shown in FIG. 4, and the inner flow speed 13 is larger than the speed of the inclined blade 4 (indicated by arrow 15). As indicated by the arrow 18, it moves to white.

Since the flat blade 3 is enlarged to generate the flow of the two associations described above, the size of the blade 3 is subject to certain limitations. In FIG. 3, since the fluid is displaced by the movement of the flat blade 3, the static pressure is generated at the front surface of the flat blade 3, and the space generated by the movement of the flat blade 3 is divided into the fluid. It is filled by the inner circulation flow of the negative pressure is generated on the back of the flat blade (3). This pressure difference causes a short flow to occur in the space between the side end of the flat blade 3 and the inner wall 6 of the container 1.

As the short flow increases, the inner circulation flow decreases, so the short flow must be minimized.

The inventors of the present invention have conducted various experiments, and the area formed by the center line 2 of the rotating shaft 2 and the outline of the flat blade 3 has a center line 5, a fluid surface 7, and a container inner wall 6 It has been found that at least 60%, preferably at least 80% of the area formed by).

In addition, the angle of the inclined vanes 4 is rather freely selectable.

In FIGS. 1 to 3, upward flow and downward in the inner portion occur in adjacent portions of the circumference, and reverse flow may occur if the upper angle is changed.

One embodiment of the present invention has been described in terms of structure, operation and effects, and the present invention is not limited to the above-described stirring device, but rather includes the embodiments described below.

FIG. 6 is a front view of a second embodiment of the present invention, and FIG. 7 is a plan view of the stirring device shown in FIG. 6, and this embodiment shows two flat blades 3a and 3b and two inclined blades 4a. 4b), the stirring device of the present invention is not limited to the number of flat and inclined blades.

FIG. 8 is a front view of the third embodiment of the present invention, and FIG. 9 is a plan view of the stirring device shown in FIG. 8, which has one flat blade 3 and one screwed inclined blade 4 , The stirring device of the present invention is not limited to the blade type or inclined type.

FIG. 10 is a front view of a fourth embodiment of the present invention, and FIG. 11 is a plan view, in which the present embodiment shows one flat vane 3 and three inclined vanes mounted at different angles from the flat vane 3 Consists of (4a) (4b) (4c), indicating that the device of the present invention is not limited by the number of inclined vanes 4 and the direction in which it is mounted.

In the second or third embodiment described above, the same effects and results as those described in the first embodiment and the flat blade can be achieved, and the flow is generated in all parts of the vessel so that quick and efficient agitation can be obtained. .

In addition, in the above embodiment, the inclined vanes are arranged in a slow flow adjacent to the circumference and a fast inward circulation at the inner region so that the inclined vanes generate an upward and a downward flow in only one of the two types of flows described above. It could be.

The following is an experimental result showing the effect compared to the stirring device of the present invention and the conventional stirring device.

Comparative Example A1

A solution having a viscosity of 200 poise was obtained by dissolving I ₂ and Na ₂ SO ₃ in a starch syrup solution in a transparent container made of acrylic resin having an inner diameter and a height of 200 mm and an anchor wing having a diameter of 190 mm, respectively. Ready.

Each of these two solutions was injected into the vessel and the blades were rotated at a rotation speed of n = 15 (rmp).

Accordingly, the time t (min) required for the dark brown color of I ₂ to disappear due to the effect of Na ₂ SO ₃ was measured, and the required rotation speed N was calculated as the formula N = n · t.

As a result, even when the value of N was 200 or more, the color of I ₂ remained on the top and the center of the container.

Comparative Example A2

A spiral ribbon wing having a diameter of 190 mm was installed in the same vessel used in Comparative Example A1, and t (min) was measured by the same analysis described above, and the value of N was calculated as N = n · t.

As a result, it was N = 35 when in all the areas, except for the vicinity of the rotational axis do not have the color of I _2. And when N = 60, the color disappeared from all parts of the container.

Experimental Example A1-A4

In the same container used in Comparative Example A1, a flat blade having a diameter of 190 mm was installed, and correspondingly, four sets of new wings of the present invention were prepared and sequentially installed, respectively, and in the same manner as in Comparative Example A1. Measure the time t (min) at which the color of I ₂ disappears at all points, using the formula N = n

The results of obtaining N are shown in Table 1 below.

TABLE 1

It can be seen from Table 1 that the stirring device of the present invention is superior to the spiral ribbon wing despite the simple structure, allowing high viscosity fluids to be mixed in a short time.

The present invention comprises a large flat blade having an area of at least 60% of the cross-sectional area formed by the center line of the rotating shaft, the inner wall of the container and the surface of the supply fluid, and the large flat blade configured by mounting the large flat blade essentially parallel to the rotating shaft. will be.

Therefore, due to the rotation of the flat blade, a slow flow near the circumference and a fast inner circulation flow occur inside. In addition, in order to achieve a complete flow in all parts of the container and to increase the stirring efficiency, the inclined blades are mounted on the rotating shaft at a predetermined angle with respect to the center line of the rotating shaft and rotated, so as to increase or improve both of the two types of flows. It is to generate a flow up and down only by the amount of flow.

Accordingly, the present invention achieves rapid and efficient agitation performance in treating high viscosity solutions or slurries by rapidly forming complete flow forms over the entire portion of the vessel.

Next, an embodiment of a stirred tower polymerization reactor to which the present invention is applied will be described in detail with reference to FIGS. 12 to 18.

12 is a longitudinal sectional view of one embodiment of a reactor of the present invention.

As shown in FIG. 12 and FIG. 13, the rotating shaft 25 is inserted into the container 24 which provided the fluid supply port 21, the fluid discharge port 22, and the jacket 23, and is installed vertically.

The rotary shaft 25 is sealed with a rotating material by the shaft sealing means 26 at the upper end portion.

The container 24 is partitioned by the number of blocking plates 27 serving as partitioning means, the extrusion flow characteristics in the flow direction, a plurality of holes perforated with a predetermined opening ratio blocking plate It can be used as (27).

In the stirring chamber 28 partitioned by the said blocking plate 27, the stirring means is attached to the rotating shaft 25. As shown in FIG.

Stirring means in each of the stirring chamber 28 is a flat blade 29, parallel to the center line 50 of the rotating shaft 25, and the flat blade (29) inclined blades forming a pair ( 30a, 30b, 30c.

The three inclined vanes 30a, 30b and 30c having a shape close to the square plate are mounted on the rotating shaft 25 by 90 degrees apart from the flat vane 29, and the other inclined vanes are also shown in FIG. As shown, they are symmetrically provided on the rotation axis 25 in the same inclination angle and the same direction with respect to the centerline 50, and they are mutually mutually arranged in the vertical position.

FIG. 13 is a sectional view taken along line III-III of FIG. 12. When the rotating shaft 25 rotates, the flat blade 29 rotates in the direction of the arrow 31, and the fluid displaced by the rotating motion is indicated by the arrow 32. Likewise a large circulating flow is formed in the inner region.

Since the velocity of the circulating flow is greater than that of the inclined vanes 30a, 30b and 30c, the flow exceeds the vanes 30a, 30b and 30c, and thus the circulating fluid is circulated. It is raised upward by 30) and flows upward.

On the other hand, the liquid proximate to the inner wall of the container 24 is subjected to viscous resistance from the inner wall and downwards by the inclined vanes 30 because the liquid flows slowly in the direction indicated by the arrow 33 as shown in FIG. It is pressed down and flows downward.

Therefore, the upstream and the downflow occur at the portion close to the inner wall above the center, thereby forming the overall up and down circulation flow.

In addition, when the inclined wing is mounted inclined in the opposite direction as shown in the figure, downward flow on the central portion and upward flow on the inner wall portion occur.

As described above, the circulating flow in both the horizontal and the up-down direction is simultaneously generated in the stirring chamber 28, thereby achieving efficient mixing.

In addition, since the stirring effect of the flat blade is made in all parts of the container, there is no part of the “square space”.

In the case of the stirring blade of the in-phase, the flow is insufficient near the rotating shaft, and gel-like substances tend to adhere to the rotating shaft. However, in the reaction apparatus of the present embodiment, a strong circulating flow is formed around the rotating shaft 25. Attachment of the material is prevented.

As described above, the large flat blade 29 plays a role of generating a horizontal circulating flow, so that a certain restriction is imposed on its size.

In FIG. 13, a positive pressure is generated at the front of the flat blade 29 in the rotational direction, and a negative pressure is generated at the rear due to a space generated by the rotation of the flat blade. The fluid is filled by the circulation flow.

Thus, there is an input difference between the front and rear of the flat blade so that short flow occurs in the gap between the inner wall 51 of the vessel and the side edge of the flat blade 29.

As the short flow increases, the overall circulation flow decreases, so the short flow must be minimized.

The inventor of the present invention has an area formed by the center line 50 of the rotating shaft 25 and the outer edges of the flat blade 29 and the area formed by the center line 50 and the inner wall 51 and the blocking plate 27 of the container. It has been found from the results of aberration that it should be more than 60%, preferably more than 80%.

In addition, the power required for agitation in the present invention is almost the same as the power required in the conventional large paddle-shaped blade is to fall into the category of low power requirements as a stirring blade for high viscosity fluid.

The heat transfer coefficient of the vessel wall is also superior to the conventional stirring vanes in stirring the highly viscous material. This is because the large flat blade of the present embodiment changes the position of the fluid by the effect of scratching the inner wall and the up and down circulation flow.

In addition, the structure of the present invention is very simple as paddle type and anchor type blades; It is simpler than the spiral ribbon wings used in the highly viscous fluids and the stirring blades of the aforementioned patent application.

As described above, this embodiment of the present invention satisfies all the above-mentioned requirements as a reactor for continuous polymerization.

In addition, in this embodiment, a blocking plate is used as an example, and the structure and shape of an annular ring body or another form can also be used.

FIG. 14 is a longitudinal sectional view of another embodiment of the reactor of the present invention, and FIG. 15 is a sectional view taken along the line IV-IV of FIG.

In the present embodiment, the two flat blades 29a and 29b are mounted on the rotating shaft 25 by being spaced 180 degrees apart from each other in a manner parallel to the centerline 50 of the rotating shaft 25.

Four inclined vanes 30a, 30b, 30c and 30d together with the flat vanes 29a and 29b are spaced 90 degrees from the flat vanes so that two are respectively rotated at the bottom and two at the bottom. It is attached to (25).

The inclined vanes are mounted inclined with respect to the centerline 50 of the rotating shaft 25 at the angle and direction as shown in the figure.

In this embodiment, it is shown that no limit is imposed on the number of flat and inclined vanes as the reactor of the present invention.

In addition, a heat exchanger is used as the partitioning means, and the heat exchanger arranges the tube fixing plate 40, the outer body 41, and the tube 42 between the stirring chambers, and a high viscosity fluid passes through the tube 42. It is to be cooled or heated by a thermally conductive oil filled between the outside of the sike tube (42) and the inside of the outer body (41), and the tubyu (42) simultaneously functions as a blocking plate and a function of a heat exchanger. It will be done.

FIG. 16 is a longitudinal sectional view of yet another embodiment of the reactor of the present invention, and FIG. 17 is a sectional view taken along the line VI-VI of FIG.

In this embodiment, the stirring means consists of a combination of one flat blade 29 and the spiral inclined blade 30.

This example shows that the reactor of the present invention is not limited to flat and inclined vanes.

In addition, the coil tubing 42 is inserted between the stirring chambers 28 as a partitioning means, and cooling or heating is performed by thermally conductive oil or the like flowing through the tubing 42 when a high-viscosity fluid passes through this portion. It is configured to receive the coiled tubing 42 serves as a partition means.

Next, the experimental result of the residence time distribution of the reaction apparatus of this invention and the conventional type of reaction apparatus is demonstrated.

In this experiment, the test apparatus used a long cylindrical transparent acrylic vessel having an internal diameter of 200 mm, which was partitioned into 28 stirring chambers and had 27 heat exchangers.

The experiment was carried out by attaching the stirring blade described above to this test apparatus sequentially.

The height of the stirring chamber was 100mm, four acrylic tubs having an inner diameter of 23mm were disposed on a 100mm heat exchanger.

The configuration of the test apparatus as described above is almost the same as the apparatus shown in FIG.

A starch syrup having a viscosity of 200 poise was used to feed it from the bottom of the vessel by a gear pump.

While supplying the starch syrup continuously, the red ink was intermittently injected and the flow was visually observed to determine the residence time distribution by continuously measuring the lightness of the color in the axle shaft.

Table 2 summarizes the observations of flow and the wings used.

The comparative example in this Table 2 is the case of the conventional reactor, and the experimental example is the case using the above-mentioned thing.

TABLE 2

From Table 2 the following becomes clear:

(1) Inadequate flow zones exist even with large paddle blades and spiral ribbon blades in conventional agitation.

(2) In Experimental Examples B1-B3, it was observed that there was no insufficient region at all as a result of using the wing shape of the present invention.

18 shows the results of measuring the residence time distribution of starch syrup in the cylindrical containers used in Comparative Examples B1 and B2 and Experimental Examples B1 to B3. In Fig. 18, E (ψ) of the ordinate indicates the residence time distribution as a function of the dimensionless time ψ of the abscissa.

In the case of the comparative example B1, the height and position of the highest value are shifted considerably from the arrangement | positioning form of a perfect mixing chamber, and it is not a desirable situation because the retention amount of fluid is very large for a long time.

In the case of Comparative Example B2, the height of the highest value is low, but in the form of a perfect mixing chamber, the number of corresponding mixing chambers is too small, which is inconsistent with the compression flow in this case.

For this reason, the upward and downward circulating flow is so powerful that part of the flow tends to bypass the outlet directly.

Experimental examples B1 to B3 are very desired because they approach the arrangement of the perfect mixing chamber.

The reaction apparatus of the present invention is to provide the desired effect as follows to provide a stirred tower polymerization reactor which is very useful industrially in the present invention.

(1) In the reactor of the present invention, since the partition means are arranged between the stirring zones, the extrusion flow characteristics are achieved, and the temperature of each stirring zone can be independently controlled in the polymerization reaction process with excellent mixing effect. will be.

In addition, by inserting the heat exchange tubing in the partition means it is possible to more easily independently control the temperature in each stirring zone.

(2) In the reaction apparatus of the present invention, two types of agitated blades, which are inclined and flat, are mounted on a rotating shaft, so that upward, downward, and horizontal circulating flows are formed so that a high viscosity solution or slurry-type material becomes a barrier to flow. High mixing efficiency can be obtained because there is no mixing area.

(3) In the conventional reactor, the flow around the rotating shaft is insufficient, so that the gel is attached to the rotating shaft. However, in the reaction apparatus of the present invention, the gel-like substance does not adhere to the rotating shaft because of the high mixing performance around the rotating shaft. Will be.

(4) The reactor of the present invention has two types of blades, inclined and flat, so that it requires less power than stirring with only one type of flat blade.

(5) In the reactor of the present invention, the up and down flows are generated, thereby improving the heat transfer coefficient due to the scratching effect of the flat blade and the exchange of fluid, thereby resulting in excellent thermal conductivity.

(6) The reactor of the present invention is characterized in that its structure is simplified.

Claims (8)

A container, an axis of rotation inserted into the container, an area of at least 60% of the cross-sectional area formed by the center line of the axis of rotation and the inner wall of the container and the surface of the agitated material in the container, and at the center line of the axis of rotation Stirring device comprising a flat blade mounted on the side of the rotary shaft in a precise parallel manner, and a slanted blade mounted on the side of the rotary shaft at a predetermined angle with respect to the center line of the rotary shaft. The stirring device according to claim 1, wherein at least one of the flat blades and a plurality of the inclined blades are attached to the rotating shaft. The stirring device according to claim 1, wherein the inclined vanes are configured in a screw shape. A cylindrical container having a fluid supply port and a fluid outlet port, a rotating shaft inserted into the container in a same manner, and a plurality of flat blades mounted on the side of the rotating shaft in a manner parallel to the center line of the rotating shaft, Stirring means having a plurality of inclined blades mounted on the side of the rotating shaft inclined with respect to the center line to form a pair with a flat wing, and partition means disposed between the stirring means and partitioning the container in the longitudinal direction. Stirred tower polymerization reactor, characterized in that configured. The stirring tower polymerization reactor according to claim 4, wherein the partition means comprises a porous plate. The stirring tower polymerization reactor according to claim 4, wherein the partition means comprises a tub, a tubing fixing plate, and an outer body. 5. The stirring tower polymerization reactor according to claim 4, wherein the partition means comprises a coil tub. The stirring tower polymerization reactor according to any one of claims 4 to 7, wherein the inclined vanes are configured in a screw shape.

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