CN215234224U - Kneading and stirring rotor for kneading reactor - Google Patents

Abstract

The utility model discloses a kneading stirring rotor for kneading reactor, this kneading stirring rotor include two stirring rotor (5) of parallel arrangement in pairs, are provided with impeller (6) that are the heliciform and distribute according to preface staggered arrangement on stirring rotor (5), and adjacent impeller (6) dislocation set on two stirring rotor (5) for E type scraper on the adjacent impeller (6) on two stirring rotor (5) can intermeshing. The E-shaped scrapers of the utility model are meshed with each other and scraped with each other in the rotating process, so that the high viscous fluid adhered on the E-shaped scrapers, the rotor wall and the inner wall of the reaction chamber can be quickly cleaned, the full reaction area inside the reaction chamber is scraped without dead zones, the shearing distribution is more uniform, the mixing efficiency is higher, and the reaction energy consumption is low; the kneading and stirring rotor can enhance the axial flow of materials, has strong self-cleaning effect, reduces the heat-sensitive loss, improves the heat transfer efficiency and reduces the waste discharge, and is particularly suitable for large-scale industrial devices.

Description

Kneading and stirring rotor for kneading reactor

Technical Field

The utility model belongs to the technical field of the stirring, especially, relate to stirring rotor with impel and self-cleaning function, specifically speaking is a kneading stirring rotor for kneading reactor.

Background

For the high-viscosity polymerization reaction process, the viscosity of the system at the later stage of the reaction is continuously increased along with the progress of the reaction, and the viscosity of the system at the later stage of the reaction can finally even reach hundreds of thousands of millipascal seconds, at this time, the flowing of the materials becomes extremely difficult, and for high-boiling-point materials, especially heavy tar or phenol tar, coal tar, high polymer and the like which have the characteristics of high viscosity, high freezing point and high heat sensitivity, foaming or swelling at high temperature usually occurs, and some phenomena even rheological solidification occur. For a conventional stirring reactor, due to the fact that the viscosity of materials is high, the temperature is high, the fluidity is poor, the materials are prone to caking in a reactor body, dead zones are formed, carbonization or expansion is caused, the local reaction temperature is too high, the molecular weight of a polymer is out of control, and operation cannot be carried out normally. Meanwhile, at high viscosity, the polymerization product often wraps the monomer and the catalyst, so that the interface in the system cannot be updated. Conventional stirred reactors have not been suitable for the final polycondensation process of polycondensation.

The kettle type stirring equipment has no effect on the technical process, and the main problems are that: along with the reduction of volatile components, the viscosity of the material is rapidly increased by hundreds of times or even thousands of times at a certain stage, the kettle type stirring equipment cannot exceed the limit, and finally, the vehicle is overloaded and stopped; the sticky materials are agglomerated or wrapped on the stirrer and the stirring rotor, the surface cannot be updated, and the evaporation area is reduced; the material is adhered to the inner wall of the kettle, and the heat transfer capacity is greatly reduced.

Likewise, twin screw extruders are commonly used for high viscosity polymer processing. In which the product is pressed against the wall of the container and friction is generated there. At this time, the screw side pushes the product, which is hindered by wall friction, in the conveying direction of the screw. However, the disadvantage is that the residence time is short and is not suitable for reactions with a slow reaction rate, while the feed rate increases quadratically with the increase in the screw diameter. If larger cartridges are to be constructed, a very small pitch is required to set a high degree of filling. This results in a rotor that is bulky and heavy, which severely limits the practical industrial application of the twin-screw extruder.

Therefore, it is necessary to develop a reactor which can well prevent high-viscosity materials from adhering to the reactor and the kettle body, prevent dead zones from occurring, and control residence time, and the stirring rotor used in the reactor and the impeller structure used in the reactor become difficult points of research and development.

SUMMERY OF THE UTILITY MODEL

The utility model aims at the problem that prior art exists, provide a rotor to propulsion performance good, can carry out high-efficient the mixing and can realize the clear kneading stirring rotor who is used for kneading the reactor of oneself to the result.

The utility model aims at solving through the following technical scheme:

a kneading stirring rotor for a kneading reactor, characterized in that: this mediate stirring rotor includes two stirring rotor of parallel arrangement in pairs, is provided with according to the preface staggered arrangement impeller that is the heliciform and distributes on stirring rotor, and the adjacent impeller dislocation set on two stirring rotor for E type scraper on the adjacent impeller on two stirring rotor can intermeshing.

The impeller comprises a blade disc, a plurality of v-shaped 21274is uniformly distributed on the peripheral side of the blade disc, the scraper blade is obliquely arranged relative to the blade disc and forms an E-shaped scraper together with the blade disc in the thickness direction.

The scraper blades are distributed on corresponding disc corners of the blade disc, the outer edges of the disc corners are arc surfaces, and the number of the disc corners is not less than three.

The outer bottom surface of the scraper blade is an arc surface matched with the outer edge of the disk corner along the circumferential direction of the blade disk.

Any two adjacent disc corners are connected through a first convex connecting cambered surface, a short plane, a concave middle cambered surface, a long plane and a second convex connecting cambered surface which are connected in sequence, and the included angle between the short plane and the long plane is 90-135 ℃.

The degree of the central angle corresponding to the short plane is 6-15 degrees, and the degree of the central angle corresponding to the long plane is 30-80 degrees; and the ratio of the central angle degree corresponding to the long plane to the central angle degree corresponding to the short plane is inversely proportional to the number of disc angles.

The ratio of the length of the short plane to the length of the long plane is 1: 1.4-2.0.

The included angle between the vertical edge of the scraper blade and the central axis of the blade disc is 3-8 degrees; the included angle between the projection line of any one of the two transverse edges of the scraper blade on the blade disc and the corresponding radial line on the blade disc is 6-10 degrees.

The ratio of the thickness of the scraper blade to the thickness of the blade disc is 1: 1-1.2; the scraper blade has a shape of 21274, and the ratio of the width of the transverse edge to the thickness of the blade disc is 1: 1-1.2.

The dislocation angle between arbitrary adjacent impeller on same stirring rotor is 3 ~ 10, the utility model discloses the dislocation angle that the circumference 360 of cutting apart the impeller and go out refers to.

The gaps between the adjacent surfaces of the mutually meshed E-shaped scrapers are 3-8 mm; the clearance between the outer edge of the E-shaped scraper of the impeller on one stirring rotor and the outer wall of the other stirring rotor is 3-8 mm; the clearance between the outer edge of the E-shaped scraper and the inner wall of the reaction cavity of the kneading and stirring area of the reactor is 3-8 mm.

The two stirring rotors rotate in the same direction at a differential speed, and the common speed ratio is 4: 5.

Compared with the prior art, the utility model has the following advantages:

the utility model discloses an E type scraper on kneading and stirring rotor meshes each other, scrapes each other in the rotation process for the high viscous fluid that adheres on E type scraper, on the rotor wall and on the reaction chamber inner wall can be cleared up fast, can be fine avoid high viscous material to adhere on kneading and stirring rotor and reaction chamber inner wall, improved mixing efficiency, avoided the appearance of dead zone to a certain extent, simultaneously, reaction space also improves greatly; compared with a traditional horizontal double-rotor reactor and a double-screw extruder, the full-reaction zone in the reaction cavity can be scraped and swept, no dead zone exists, the shearing distribution is more uniform, the mixing efficiency is higher, the reaction energy consumption is low, and the device is particularly suitable for large industrial devices.

The utility model discloses a mediate stirring rotor can strengthen the material axial flow, and have very strong automatically cleaning effect, reduce the temperature sensing loss, improve heat transfer efficiency and mixing efficiency, reduce the energy consumption, reduce the wastes material and discharge, use the continuous stable safe operation that can guarantee the system on horizontal birotor automatically cleaning reactor.

The utility model discloses a slope sets up the scraper blade on the leaf disc, and the axial upset of scraper blade relative leaf disc, radial torsion for the impeller structure that has E type scraper possesses the characteristics of flexible mediate, low shearing force, can make the material mix evenly when effectively preventing the material decomposition; and the shape of the blade disc is processed, so that the surface updating efficiency of an impeller structure formed by matching the shape of the blade disc with the E-shaped scraper is high, the separation of volatile components such as solvents, monomers and the like from high-viscosity polymers is facilitated, and the polymerization, drying and devolatilization effects are improved.

Drawings

FIG. 1 is a schematic perspective view of a kneading and stirring rotor according to the present invention;

FIG. 2 is a schematic plane structure diagram of the kneading and stirring rotor of the present invention;

FIG. 3 is a schematic cross-sectional structure view of the kneading and stirring rotor of the present invention;

FIG. 4 is a schematic structural view of a quadrangular bladed disk of the present invention;

FIG. 5 is a schematic view of the structure of the quadrangular impeller of the present invention;

fig. 6 is a schematic structural view of the scraper blade of the present invention;

FIG. 7 is a schematic structural view of a pentagonal bladed disk of the present invention;

FIG. 8 is a perspective view of a pentagonal impeller structure of the present invention;

FIG. 9 is a plan view of a pentagonal impeller structure of the present invention;

FIG. 10 is a schematic structural view of a kneading reactor barrel with a 8-shaped cross section, in which the kneading stirring rotor of the present invention is used;

FIG. 11 is a schematic structural view of a kneading reactor barrel with a "heart" shaped cross section with a kneading stirring rotor according to the present invention.

Wherein: 1-leaf disc; 2-a doctor blade; 3-disc angle; 31-first connecting arc surface; 32-short plane; 33-middle arc; 34-long plane; 35-a second connecting cambered surface; 4, mounting a groove; 5-a stirring rotor; 6-impeller.

Detailed Description

The present invention will be further described with reference to the accompanying drawings and examples.

As shown in fig. 1-9: a kneading and stirring rotor for a kneading reactor comprises two stirring rotors 5 which are arranged in parallel in pairs, impellers 6 which are arranged in a staggered manner in sequence and distributed spirally are arranged on the stirring rotors 5, the dislocation angle between any adjacent impellers 6 on the same stirring rotor 5 is 3-10 degrees, and the adjacent impellers 6 on the two stirring rotors 5 are also arranged in a staggered manner (the dislocation angle between the impeller 6 of one stirring rotor 5 and the two adjacent impellers 6 on the other stirring rotor 5 is 1.5-5 degrees), so that E-shaped scrapers on the adjacent impellers 6 on the two stirring rotors 5 can be meshed with each other; the impeller 6 comprises a blade disc 1, a plurality of disc corners 3 which are uniformly distributed are arranged on the blade disc 1, the outer edges of the disc corners 3 are arc surfaces, the outer edges of the disc corners 3 are connected to form a circle, a mounting groove 4 is correspondingly arranged on any disc corner 3, a v-21274is fixedly mounted on each mounting groove 4, a plurality of v-21274-shaped scraper blades 2 are uniformly distributed on the peripheral side of the blade disc 1, the scraper blades 2 are obliquely arranged relative to the blade disc 1 and form an E-shaped scraper together with the blade disc 1 in the thickness direction, and the v-21274-shaped scraper blades 2 are arranged on the peripheral side of the blade disc 1.

As shown in fig. 5, 8 and 9, in addition, in the impeller 6 of the present invention, the scraper blade 2 may be directly embedded in the mounting groove 4, or may be welded as needed.

In the above structure, as shown in fig. 4-9, the number of the plate corners 3 is not less than three, and any two adjacent plate corners 3 are connected by the convex first connecting arc surface 31, the short plane 32, the concave middle arc surface 33, the long plane 34 and the convex second connecting arc surface 35 which are connected in sequence. In the structure, in order to improve the surface renewal efficiency of the impeller structure, facilitate the removal of volatile components such as solvent, monomer and the like from a high-viscosity polymer and increase the effects of polymerization, drying and devolatilization, the ratio of the length of the short plane 32 to the length of the long plane 34 is set to be 1: 1.4-2.0; the degree of the central angle corresponding to the short plane 32 is 6-15 degrees, the degree of the central angle corresponding to the long plane 34 is 30-80 degrees, and the ratio of the degree of the central angle corresponding to the long plane 34 to the degree of the central angle corresponding to the short plane 32 is inversely proportional to the number of the disc angles 3; the included angle between the short plane 32 and the long plane 34 is 90-135 ℃.

As shown in fig. 5, 8, and 9, in the above-described structure, the outer bottom surface of the doctor blade 2 is an arc surface conforming to the outer edge of the disk corner 3 in the circumferential direction of the disk 1, and may be a flat surface as necessary. The included angle between the vertical edge of the scraper blade 2 and the central axis of the blade disc 1 is 3-8 degrees, namely the scraper blade 2 is twisted by 3-8 degrees by taking the radial line of the blade disc 1 as an axis; the projection line of any one of the two transverse edges of the scraper blade 2 on the blade disc 1 and the corresponding radial line on the blade disc 1 form an included angle of 6-10 degrees, namely the scraper blade 2 turns over by 6-10 degrees by taking the central axis of the blade disc 1 as an axis.

As shown in fig. 5, 6, 8, and 9, since the doctor blade 2 has high working strength, the doctor blade 2 of the present invention is made of 304 steel, 304L steel, or 316L steel, and in special cases, HC276 (hastelloy) is used; in addition, the thickness of the doctor blade 2 cannot be too low, the ratio of the thickness of the doctor blade 2 to the thickness of the vane wheel 1 is 1:1-1.2, the ratio of the width of the transverse edge in the shape of the doctor blade 2 to the thickness of the vane wheel 1 is 1: 1-1.2; the overall width or the length of the transverse edges of the doctor blade 2 is furthermore determined according to the particular application.

It should be noted that, according to actual need, the utility model discloses a bladed disk 1 can adopt hollow structure's disc, needs design bladed disk 1's disc thickness and corresponding size according to the temperature of medium, pressure, heat transfer area this moment.

As shown in fig. 4 and 5, the blisk 1 adopts a disc with four disc angles 3, the degree of the central angle corresponding to the short plane 32 is 11 degrees, the degree of the central angle corresponding to the long plane 34 is 55 degrees, and the included angle between the short plane 32 and the long plane 34 is 125 degrees; the mounting grooves 4 are arranged on the disk corners 3, one' -21274is fixedly mounted on each mounting groove 4, and the scraper blade 2 is overturned by 10 degrees by taking the central axis of the blade disk 1 as an axis and is overturned by 5 degrees by taking the radial line of the blade disk 1 as an axis in a mode of being perpendicular to the blade disk 1 along the radial direction of the blade disk 1. As shown in fig. 7, 8 and 9, the blisk 1 is a disc with five disc angles 3, the number of central angles corresponding to the short planes 32 is 8 degrees, the number of central angles corresponding to the long planes 34 is 40 degrees, and the included angle between the short planes 32 and the long planes 34 is 110 ℃; the mounting grooves 4 are arranged on the disk corners 3, one' -21274is fixedly mounted on each mounting groove 4, and the scraper blade 2 is overturned by 7 degrees by taking the central axis of the blade disk 1 as an axis and is overturned by 3 degrees by taking the radial line of the blade disk 1 as an axis in a mode of being perpendicular to the blade disk 1 along the radial direction of the blade disk 1.

Taking the impeller 6 shown in fig. 5 or fig. 8 as an example, when the impeller 6 is installed on the stirring rotor 5, the whole impeller 6 has a helical angle along the axis, which can effectively make the material have a forward moving plug flow, and because the disk angle 3 of two adjacent bladed disks 1 is equivalent to a barrier weir plate, the residence time of the material can be effectively controlled by changing the speed of the stirring rotor 5.

The utility model discloses a cross-sectional structure when kneading agitator rotor is used for the kneading reactor barrel of "8" font cross-section is shown as figure 10, cross-sectional structure when being used for the kneading reactor barrel of "heart" font cross-section is shown as figure 11, in kneading reactor's barrel, the clearance between each looks proximal surface between the E type scraper of intermeshing is 3mm ~ 8mm, the clearance between the outer fringe of the E type scraper of impeller 6 on an agitator rotor 5 and another agitator rotor 5's outer wall is 3mm ~ 8mm, the clearance between the outer fringe of E type scraper and the reactor kneading stirring region's reaction intracavity wall is 3mm ~ 8 mm. When the self-cleaning device is used, the E-shaped scrapers on the two stirring rotors 5 are meshed with each other, the two rotors rotate in the same direction and at a different speed, the common speed ratio is 4:5, the E-shaped scraper on one stirring rotor 5 can scrape the inner wall of a cylinder body to clean and clean the E-shaped scraper on the other stirring rotor 5 at the same time, and the dynamic contour lines generated in the rotating process of the two rotors ensure that no dead angle exists in the device, namely the self-cleaning effect is realized. In order to provide strong mixing and simultaneously push materials (including high-viscosity materials) to gradually move forwards to form a macroscopic plug flow reactor, the E-shaped scrapers on the stirring rotor 5 are arranged in a spiral shape, the arrangement mode provides driving force for the axial conveying of the high-viscosity materials and can prevent the back mixing of the materials, the flow of the materials in the equipment is close to plug flow, and narrow residence time distribution can be obtained; when the method is used for polycondensation, the product quality can be improved; when used for devolatilization, the devolatilization effect can be improved.

The kneading reactor barrel of the "heart" shaped cross-section shown in FIG. 11, because of its larger effective volume and gas phase free space, is typically used in high solvent content devolatilization, while still maintaining good devolatilization and greater throughput.

Adopt the utility model provides a kneading reactor of kneading stirring rotor, kneading reactor can operate under the condition of charge coefficient 60% ~ 70%, and industrialization device volume is from 100L ~ 10000L, and the heating area that corresponds is from 4m²～150m². When the device is used for experiments, the specification of the device is 10L-200L.

The utility model has compact and beautiful structure, large heat transfer volume per unit volume and high heat efficiency; the impeller 6 has special structure, good surface heat transfer self-cleaning effect and high heat transfer coefficient; the operation mode is multiple, and normal pressure operation and vacuum operation can be performed; the application range is wide, and the material is suitable for organic matters, inorganic matters, heat-sensitive materials, high-humidity and low-humidity granular materials or viscous materials.

The above embodiments are only for explaining the technical idea of the present invention, and the protection scope of the present invention cannot be limited thereby, and any modification made on the basis of the technical scheme according to the technical idea provided by the present invention all fall within the protection scope of the present invention; the technology not related to the utility model can be realized by the prior art.

Claims (10)

1. A kneading stirring rotor for a kneading reactor, characterized in that: this kneading mixing rotor includes two mixing rotor (5) of parallel arrangement in pairs, is provided with impeller (6) that are the heliciform and distribute according to the preface staggered arrangement on mixing rotor (5), and adjacent impeller (6) staggered arrangement on two mixing rotor (5) for E type scraper on the adjacent impeller (6) on two mixing rotor (5) can intermeshing.

2. Kneading stirring rotor for a kneading reactor according to claim 1, characterized in that: the impeller (6) comprises a blade disc (1), a plurality of v-21274-shaped scraper blades (2) are uniformly distributed on the peripheral side of the blade disc (1), the scraper blades (2) are obliquely arranged relative to the blade disc (1), and the v-21274-shaped scraper blades (2) and the blade disc (1) in the thickness direction form an E-shaped scraper.

3. The kneading stirring rotor for a kneading reactor according to claim 2, characterized in that: the scraper blades (2) are distributed on corresponding disc corners (3) of the blade disc (1), and the outer edges of the disc corners (3) are arc surfaces, and the number of the disc corners (3) is not less than three.

4. The kneading stirring rotor for a kneading reactor according to claim 3, characterized in that: any two adjacent disc corners (3) are connected with each other through a convex first connecting arc surface (31), a short plane (32), a concave middle arc surface (33), a long plane (34) and a convex second connecting arc surface (35) which are connected in sequence, and the included angle between the short plane (32) and the long plane (34) is 90-135 ℃.

5. The kneading stirring rotor for a kneading reactor according to claim 4, characterized in that: the degree of the central angle corresponding to the short plane (32) is 6-15 degrees, and the degree of the central angle corresponding to the long plane (34) is 30-80 degrees; and the ratio of the central angle degree corresponding to the long plane (34) to the central angle degree corresponding to the short plane (32) is inversely proportional to the number of the disc angles (3).

6. The kneading stirring rotor for a kneading reactor according to claim 4, characterized in that: the ratio of the length of the short plane (32) to the length of the long plane (34) is 1: 1.4-2.0.

7. The kneading stirring rotor for a kneading reactor according to claim 2, characterized in that: the included angle between the vertical edge of the scraper blade (2) and the central axis of the blade disc (1) is 3-8 degrees; the projection line of any one of the two transverse edges of the scraper blade (2) on the blade disc (1) and the corresponding radial line on the blade disc (1) form an included angle of 6-10 degrees.

8. The kneading stirring rotor for a kneading reactor according to claim 2 or 7, characterized in that: the ratio of the thickness of the scraper blade (2) to the thickness of the blade disc (1) is 1: 1-1.2; the scraper blade (2) has a shape such that the ratio of the width of the transverse edge to the thickness of the leaf disc (1) is 1:1 to 1.2.

9. The kneading stirring rotor for a kneading reactor according to claim 1 or 2, characterized in that: the dislocation angle between any adjacent impellers (6) on the same stirring rotor (5) is 3-10 degrees.

10. The kneading stirring rotor for a kneading reactor according to claim 1 or 2, characterized in that: the gaps between the adjacent surfaces of the mutually meshed E-shaped scrapers are 3-8 mm; the clearance between the outer edge of the E-shaped scraper of the impeller (6) on one stirring rotor (5) and the outer wall of the other stirring rotor (5) is 3-8 mm; the clearance between the outer edge of the E-shaped scraper and the inner wall of the reaction cavity of the kneading and stirring area of the reactor is 3-8 mm.

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