Radial stirring paddle and stirring reaction kettle device

Abstract

The invention belongs to the technical field of stirring equipment, and discloses a radial stirring paddle and a stirring reaction kettle device. The radial stirring paddle comprises a rotating shaft, a disc, a plurality of radial flow blades and a plurality of radial auxiliary blades. The rotating shaft can be driven by the driving output end to rotate and is perpendicularly installed in the center of the disc. The radial flow blades are distributed at intervals, each radial flow blade is perpendicularly fixed to the disc and extends in the radial direction of the disc, the side, close to the outer edge of the disc, of each radial flow blade exceeds the edge of the disc, and the radial flow blades are asymmetric about the disc face of the disc. A gap is reserved between each radial flow blade and the rotating shaft, the radial auxiliary blades are perpendicular to the disc, each radial auxiliary blade is located in one gap, and the radial auxiliary blades abut against the side walls of the radial flow blades and the outer wall of the rotating shaft respectively along the two radial ends of the disc. The radial stirring paddle can improve the stirring uniformity of materials, and is good in stirring effect and low in energy consumption.

Description

Technical Field

[0001] The invention relates to the technical field of stirring equipment, and in particular to a radial stirring paddle and a stirring reactor device. Background Art

[0002] Stirred reactors are widely used in industrial production as stirring containers for mixing materials. The stirring paddle is the core component of the stirred reactor. The stirring paddle can be divided into radial flow paddles and axial flow paddles according to the flow pattern it generates in the stirred reactor. In the process of the radial flow paddle, the paddle pumps the fluid out from the center of the paddle in a radial outward direction, and is divided into two main circulation flows, upper and lower, when it encounters the wall of the stirred reactor; in the process of the rotation of the axial flow paddle, according to the inclination angle of the paddle and the direction of rotation, the fluid is pumped downward or upward toward the bottom or liquid surface of the stirred reactor, and circulates when it encounters the bottom or liquid surface of the stirred reactor, forming a main circulation in the stirred reactor.

[0003] For immiscible solution systems, there is usually a density difference between the dispersed phase and the continuous phase, and the greater the density difference between the two phases, the higher the requirements for mixing and dispersion in the stirred reactor. If there is a weak mixing zone or dead zone in the reactor, not only will the diameter of the dispersed phase droplets be large, but the two phases will also be easily stratified; in addition, when the stirred reactor is operated continuously, the dispersed phase or continuous phase that continuously enters the reactor is prone to short-circuiting, causing the volume ratio of the two phases in the reactor and at the outlet to seriously deviate from the volume ratio of the two phases in the process design, thereby causing the reactor to operate unstable. Since the shear capacity of radial flow impellers is significantly higher than that of axial flow impellers, radial flow impellers are widely used in the stirring and dispersion of immiscible solution systems. For example, the most commonly used radial flow impellers are Rushton impellers, such as Figure 1As shown, the Rushton paddle includes a rotating shaft 100' and a disc 200', the rotating shaft 100' is vertically installed at the center of the disc 200', and the rectangular blades 300' are evenly distributed on the edge of the disc 200', so that the Rushton paddle has a strong shearing ability. However, since the torque of the radial flow stirring paddle in the prior art is mainly generated at the end away from the stirring shaft, such as the rectangular blades 300' of the Rushton paddle are only distributed on the edge of the disc 200', and in the area close to the rotating shaft 100', the rectangular blades 300' and the disc 200' are not closed, the main flow is not conducive to increasing the radial circulation volume of the radial flow stirring paddle, which leads to uneven stirring and insufficient stirring effect. Specifically, when the density difference between the dispersed phase and the continuous phase increases, the shear and circulation provided by the Rushton paddle in the kettle cannot meet the sufficient liquid-liquid dispersion, resulting in excessive droplet diameter and the outlet dispersed phase / continuous phase volume ratio far deviating from the process setting value during continuous operation. Although increasing the stirring speed is a way to enhance the mixing in the kettle, the circulation volume in the kettle is limited, and increasing the stirring speed may cause the turbulent energy dissipation rate in the strong shear zone to continue to increase, while the turbulent energy dissipation rate in the weak shear zone changes little, resulting in no significant dispersion enhancement of the immiscible solution in the kettle. Therefore, it is urgent to propose a radial stirring paddle and a stirred reactor device to solve the above problems. Summary of the invention

[0004] The first object of the present invention is to provide a radial stirring paddle, which can improve the stirring uniformity of materials, has a good stirring effect and low energy consumption.

[0005] To achieve this object, the present invention adopts the following technical solutions:

[0006] Radial impeller, including:

[0007] A rotating shaft, which can be driven to rotate by the driving output end;

[0008] A disc, wherein the rotating shaft is vertically mounted at the center of the disc;

[0009] A plurality of radial flow blades, the plurality of radial flow blades are spaced and distributed along the outer circumference of the disk, each of the radial flow blades is vertically fixed to the disk and extends radially along the disk, each of the radial flow blades is radially close to the outer edge of the disk and exceeds the edge of the disk, and the radial flow blades are asymmetric with respect to the disk surface, and a gap is left between each of the radial flow blades and the rotating shaft;

[0010] A plurality of radial auxiliary blades are perpendicular to the disc, each of the radial auxiliary blades is located in one of the gaps, and the radial auxiliary blades are respectively in contact with the radial flow blade side wall and the outer wall of the rotating shaft along the radial ends of the disc.

[0011] As an optional technical solution for the radial stirring impeller, the radial flow blade is provided with a notch on a side close to the rotating shaft, and the disc is clamped in the notch.

[0012] As an optional technical solution for the radial stirring impeller, the number of the radial auxiliary blades is equal to the number of the radial flow blades and corresponds one to one.

[0013] As an optional technical solution for the radial stirring impeller, the radial auxiliary blades are located on a side of the disc close to the drive output end.

[0014] As an optional technical solution for the radial stirring impeller, the radial auxiliary blades are located on the side of the disc away from the drive output end.

[0015] As an optional technical solution for a radial agitator, the radial flow blade is a rectangle, and the radial auxiliary blade is a right triangle. One of the right-angled sides of the right triangle abuts against the surface of the disc, and the other right-angled side of the right triangle abuts against the radial flow blade and is flush with the side of the radial flow blade close to the drive output end.

[0016] As an optional technical solution for a radial agitator, the radial flow blade is a rectangle, and the radial auxiliary blade is a hypotenuse right-angled trapezoid. The short base of the hypotenuse right-angled trapezoid abuts against the outer wall of the rotating shaft, the long base of the hypotenuse right-angled trapezoid abuts against the radial flow blade and is flush with the side of the radial flow blade close to the drive output end, and the right-angled side of the hypotenuse right-angled trapezoid abuts against the disc.

[0017] As an optional technical solution for the radial stirring impeller, the radial flow blades and the radial auxiliary blades are both rectangular, and the side of the radial flow blade close to the drive output end is flush with the side of the radial auxiliary blade close to the drive output end.

[0018] As an optional technical solution for a radial agitator, the radial flow blade is a rectangle, and the radial auxiliary blade is a curved right-angled trapezoid. The long base of the curved right-angled trapezoid abuts against the outer wall of the rotating shaft, the short base of the curved right-angled trapezoid abuts against the radial flow blade and is flush with the side of the radial flow blade close to the drive output end, the right-angled side of the curved right-angled trapezoid abuts against the disc, and the curved side of the curved right-angled trapezoid bends toward the disc.

[0019] The second object of the present invention is to provide a stirred reactor device, which can improve the stirring uniformity of materials, has a good stirring effect and low energy consumption.

[0020] To achieve this object, the present invention adopts the following technical solutions:

[0021] The stirred reactor device comprises a reactor body and the radial stirring paddle, wherein the radial stirring paddle is vertically arranged in the reactor body.

[0022] Beneficial effects of the present invention:

[0023] The radial stirring paddle provided by the present invention comprises a rotating shaft, a disc, a plurality of radial flow blades and a plurality of radial auxiliary blades. The rotating shaft is vertically mounted at the center of the disc, and a plurality of radial flow blades are spaced and distributed along the outer circumference of the disc, and each radial flow blade is radially close to the outer edge of the disc and exceeds the edge of the disc, and the radial flow blade is asymmetric about the disc surface, thereby increasing the shearing of the radial flow blade on the material, and thus improving the stirring effect of the radial stirring paddle. A gap is left between each radial flow blade and the rotating shaft, and the radial auxiliary blade is located in one of the gaps, and the two ends of the radial auxiliary blade are respectively abutted against the side wall of the radial flow blade and the outer wall of the rotating shaft, so that the radial auxiliary blade and the disc are in a closed state in the area close to the rotating shaft (i.e., the gap), increasing the radial velocity component of the fluid in the area close to the rotating shaft, inducing more materials to enter the upper circulation flow or the lower circulation flow, thereby improving the radial displacement of the radial stirring paddle. Therefore, without significantly increasing the stirring power consumption, the radial stirring paddle can strengthen the material circulation, stir the material more evenly, and have a good stirring effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 It is a structural schematic diagram of a traditional Rushton paddle in the prior art;

[0025] Figure 2 This is a schematic diagram of the first structure of the radial stirring paddle provided in the first embodiment of the present invention;

[0026] Figure 3 is a schematic diagram of a second structure of a radial stirring paddle provided in the first embodiment of the present invention;

[0027] Figure 4 This is a schematic diagram of the first structure of the radial stirring paddle provided in the second embodiment of the present invention;

[0028] Figure 5 is a schematic diagram of a second structure of a radial stirring paddle provided in the second embodiment of the present invention;

[0029] Figure 6 This is a schematic diagram of the first structure of the radial stirring paddle provided in the third embodiment of the present invention;

[0030] Figure 7 This is a schematic diagram of the second structure of the radial stirring paddle provided in the third embodiment of the present invention;

[0031] Figure 8This is a schematic diagram of the first structure of the radial stirring paddle provided in the fourth embodiment of the present invention;

[0032] Fig. 9 This is a second structural schematic diagram of the radial agitator provided in the fourth embodiment of the present invention.

[0033] In the figure:

[0034] 100', rotating shaft; 200', disc; 300', rectangular blade;

[0035] 100, rotating shaft; 200, disk; 300, radial flow blade; 400, radial auxiliary blade. DETAILED DESCRIPTION

[0036] The present invention will be further described in detail below in conjunction with the accompanying drawings and embodiments. It is to be understood that the specific embodiments described herein are only used to explain the present invention, rather than to limit the present invention. It should also be noted that, for ease of description, only parts related to the present invention, rather than all structures, are shown in the accompanying drawings.

[0037] In the description of the present invention, unless otherwise clearly specified and limited, the terms "connected", "connected", and "fixed" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0038] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may include that the first and second features are in direct contact, or may include that the first and second features are not in direct contact but are in contact through another feature between them. Moreover, a first feature being "above", "above" and "above" a second feature includes that the first feature is directly above and obliquely above the second feature, or simply indicates that the first feature is higher in level than the second feature. A first feature being "below", "below" and "below" a second feature includes that the first feature is directly below and obliquely below the second feature, or simply indicates that the first feature is lower in level than the second feature.

[0039] In the description of this embodiment, the terms "upper", "lower", "right", etc., directions or positional relationships are based on the directions or positional relationships shown in the drawings, and are only for the convenience of description and simplification of operation, rather than indicating or implying that the device or element referred to must have a specific direction, be constructed and operated in a specific direction, and therefore cannot be understood as limiting the present invention. In addition, the terms "first" and "second" are only used to distinguish in the description and have no special meaning.

[0040] Embodiment 1

[0041] The radial stirring paddle provided in this embodiment can improve the stirring uniformity of the material, has a good stirring effect and low energy consumption.

[0042] Specifically, Figure 2 As shown, the radial impeller includes a rotating shaft 100, a disc 200, a plurality of radial flow blades 300 and a plurality of radial auxiliary blades 400. The rotating shaft 100 can be driven to rotate by the drive output end, and the rotating shaft 100 is vertically installed at the center of the disc 200. The plurality of radial flow blades 300 are spaced apart along the outer circumference of the disc 200. For example, the radial flow blades 300 can be two, three, four or six. Each radial flow blade 300 is vertically fixed to the disc 200 and extends radially along the disc 200. Each radial flow blade 300 is radially close to the outer edge of the disc 200 and exceeds the edge of the disc 200, and the radial flow blade 300 is asymmetric about the disc surface of the disc 200. A gap is left between each radial flow blade 300 and the rotating shaft 100, and the radial auxiliary blade 400 is perpendicular to the disc 200, and each radial auxiliary blade 400 is located in one of the gaps. In addition, the radial auxiliary blades 400 are respectively in contact with the side walls of the radial flow blades 300 and the outer wall of the rotating shaft 100 along the radial ends of the disk 200 .

[0043] Based on the above design, the rotating shaft 100 can rotate, and the rotating shaft 100 is vertically installed at the center of the disc 200 to realize the rotation of the radial stirring paddle. A plurality of radial flow blades 300 are spaced and distributed along the outer circumference of the disc 200, and each radial flow blade 300 is vertically fixed to the disc 200 and extends radially along the disc 200, so as to realize radial stirring of the material and each radial flow blade 300 is subjected to uniform force. Each radial flow blade 300 extends beyond the edge of the disc 200 on one side close to the outer edge of the disc 200 along the radial direction of the disc 200, and the radial flow blade 300 is asymmetric with respect to the disc surface of the disc 200, that is, the disc 200 divides the radial flow blade 300 into two parts, and the sizes of the two parts are different, so as to increase the shearing of the material by the radial flow blade 300, thereby improving the stirring effect of the radial stirring paddle. There is a gap between each radial flow blade 300 and the rotating shaft 100, and the radial auxiliary blade 400 is located in one of the gaps, and the two ends of the radial auxiliary blade 400 are respectively in contact with the side wall of the radial flow blade 300 and the outer wall of the rotating shaft 100, so that the area near the rotating shaft 100 (i.e., the gap) between the radial auxiliary blade 400 and the disc 200 is in a closed state, which increases the radial velocity component of the fluid in the area near the rotating shaft 100, induces more materials to enter the upper circulation flow or the lower circulation flow, thereby increasing the radial displacement of the radial stirring paddle. Therefore, without significantly increasing the stirring power consumption, the radial stirring paddle can strengthen the material circulation, thereby stirring the materials more evenly and achieving a good stirring effect.

[0044] Optionally, a notch is provided on one side of the radial flow blade 300 close to the rotating shaft 100 , and the disc 200 is clamped in the notch, which facilitates the installation of the radial flow blade 300 and increases the connection strength between the radial flow blade 300 and the disc 200 .

[0045] Optionally, the number of radial auxiliary blades 400 is equal to the number of radial flow blades 300 and corresponds one to one, that is, a radial auxiliary blade 400 is provided at each gap to improve the stirring effect of the radial stirring paddle.

[0046] In this embodiment, the radial flow blade 300 is a rectangle, and the radial auxiliary blade 400 is a right triangle. One of the right-angled sides of the right triangle abuts against the surface of the disk 200, and the other right-angled side of the right triangle abuts against the radial flow blade 300 and is flush with the side of the radial flow blade 300 close to the drive output end.

[0047] Furthermore, the triangular radial auxiliary blades 400 can be located on both sides of the disk 200, forming the first structure of the radial stirring paddle and the second structure of the radial stirring paddle in this embodiment. Figure 2 As shown, the triangular radial auxiliary blade 400 is located on the side of the disk 200 close to the drive output end (i.e., the upper surface of the disk 200). Figure 3 As shown, the triangular radial auxiliary blades 400 may also be located on the side of the disk 200 away from the drive output end (ie, the lower surface of the disk 200).

[0048] It should be noted that Figure 3 Only one set of radial flow blades 300 and radial auxiliary blades 400 are shown.

[0049] This embodiment also provides a stirring reactor device, which has a good stirring effect on materials.

[0050] Specifically, the stirred reactor device comprises a reactor body and the radial stirring paddle, wherein the radial stirring paddle is vertically arranged in the reactor body. Due to the radial stirring paddle, the stirred reactor device can stir the materials more evenly and achieve a good stirring effect.

[0051] Four groups of comparative experiments were conducted on the radial stirring impeller provided in this embodiment (Experimental Examples 1 to Experimental Examples 4) and the traditional Rushton impeller in the prior art (Comparative Examples 1 to Comparative Examples 4), namely, Experimental Example 1 and Comparative Example 1 in the first group of experiments; Experimental Example 2 and Comparative Example 2 in the second group of experiments; Experimental Example 3 and Comparative Example 3 in the third group of experiments; Experimental Example 4 and Comparative Example 4 in the fourth group of experiments. The reactor body used in each group of experiments is the same, and the specific experimental parameters and experimental results are as follows:

[0052] The first set of experiments:

[0053] Experimental Example 1: The inner diameter of the reactor body is T=200mm; the height is 280mm, of which the height of the elliptical bottom head is 50mm and the height of the straight section is 230mm; four baffles are installed close to the inner wall of the reactor, and the width of each baffle is T / 10. A radial flow stirring paddle is installed on the stirring shaft, and the height from the bottom of the reactor is T / 3. The diameter of the stirring shaft is 10mm, the diameter of the entire radial flow stirring paddle is 67mm, and the diameter of the disk 200 is 50mm; there are six radial flow blades 300, the width of the radial flow blade 300 (i.e., the width perpendicular to the radial direction of the disk 200) is 14mm, and the length of the radial flow blade 300 (i.e., the length along the radial direction of the disk 200) is 17mm; there are six radial auxiliary blades 400 on the side of the disk 200 close to the drive output end, and the shape is triangular. The dispersed phase is n-hexane with a density of 600kg / m3; the continuous phase is water with a density of 1000kg / m3; the reactor body is in continuous operation, the dispersed phase feed rate is 25mL / min, and the continuous phase feed rate is 275mL / min; both the dispersed phase and the continuous phase are added from the side wall of the reactor body, where the dispersed phase feed position is 60mm from the bottom and the continuous phase feed position is 12mm from the bottom. The reactor body has an overflow outlet, 200mm from the bottom of the reactor, and the theoretical outlet dispersed phase volume ratio is 0.083. The stirring speed is 450rpm, the power is measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation is stable is measured by the sampling method.

[0054] Comparative Example 1: Only the radial flow impeller in Experimental Example 1 was replaced with a conventional Rushton impeller of the prior art. The diameter of the conventional Rushton impeller was still 67 mm, the diameter of the disk 200 was still 50 mm, the number of rectangular blades was still six, the width was still 14 mm, and the length was still 17 mm. The stirring speed was still 450 rpm, and the power was measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation was stable was measured by the sampling method.

[0055] Experimental Example 1 and Comparative Example 1 were carried out under the same stirring speed and operating medium properties. The experimental results show that the radial flow impeller in Experimental Example 1 has the same power consumption as the traditional Rushton impeller in Comparative Example 1. However, in Experimental Example 1, the volume ratio of the dispersed phase at the outlet of the reactor body under continuous stirring is 0.084, which is only 1.2% different from the theoretical value of 0.083; while in Comparative Example 1, the volume ratio of the dispersed phase at the outlet of the reactor body under continuous stirring is 0.103, which is as high as 24.1% different from the theoretical value of 0.083. Therefore, this group of experiments shows that the radial flow impeller provided in this embodiment can significantly promote the continuous stirring and mixing of immiscible solutions in the reactor body without increasing power consumption, can strengthen the dispersion of the dispersed phase, reduce its short circuit, make the fluid in the reactor close to the fully mixed flow, and the volume ratio of the dispersed phase at the outlet is close to the theoretical value.

[0056] The second set of experiments:

[0057] Experimental Example 2: Based on Experimental Example 1 of the first group of experiments, the diameter distribution of the dispersed phase droplets in the kettle was photographed using a telecentric photography multiphase measuring instrument to obtain the Sauter mean diameter D 32 .

[0058] Comparative Example 2: Based on the comparative example 1 of the first group of experiments, the diameter distribution of the dispersed phase droplets in the kettle was photographed using a telecentric photography multiphase measuring instrument to obtain the Sauter mean diameter d 32 .

[0059] The experimental results show that the radial flow impeller measurement D obtained in Experimental Example 2 32 =120 μm, the conventional Rushton paddle measurement in Comparative Example 2 obtained d 32 =150 μm. That is, the radial flow impeller provided in Experimental Example 2 significantly reduces the diameter of the dispersed phase droplets in the kettle by 20% compared with the traditional Rushton impeller in Comparative Example 2. Therefore, this group of experiments shows that the radial flow impeller provided in this embodiment can enhance the breakup of the dispersed phase droplets in the immiscible solution system and reduce the diameter of the dispersed phase droplets.

[0060] The third set of experiments:

[0061] Experimental Example 3: Based on Experimental Example 1 of the first group of experiments, only the feeding position of the dispersed phase and the continuous phase was adjusted from the side wall of the reactor body to the feeding from above the liquid surface. The stirring speed was still 450 rpm, the power was measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation was stable was measured by the sampling method.

[0062] Comparative Example 3: Based on Comparative Example 1 of the first group of experiments, only the feeding position of the dispersed phase and the continuous phase was adjusted from the side wall of the reactor body to the upper liquid surface. The stirring speed was still 450 rpm, the power was measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation was stable was measured by the sampling method.

[0063] Experimental Example 3 and Comparative Example 3 were conducted under the same stirring speed and operating medium properties. The experimental results show that changing the feed position of the dispersed phase and the continuous phase will not affect the stirring power consumption. However, in this group of experiments, since the feed position is located above the liquid surface and closer to the overflow outlet, the volume ratio of the dispersed phase at the outlet of Experimental Example 3 is increased by 15.5% compared with that of Experimental Example 1; the volume ratio of the dispersed phase at the outlet of Comparative Example 3 is also increased by 19.4% compared with that of Comparative Example 1. In addition, the volume ratio of the dispersed phase at the outlet of the reactor body in Experimental Example 3 deviates from the theoretical value of 0.083 by 16.9%; while in Comparative Example 3, the volume ratio of the dispersed phase at the outlet of the reactor body deviates from the theoretical value of 0.083 by as much as 48.2%. Therefore, this group of experiments fully demonstrates that the radial flow agitator provided in this embodiment can induce more fluid to enter the upper circulation flow in the kettle through the radial auxiliary blades 400, thereby increasing the radial displacement of the radial flow agitator, which can significantly promote the continuous stirring and mixing in the immiscible solution reactor body, strengthen the dispersion of the dispersed phase, reduce its short circuit, and make the volume ratio of the dispersed phase at the outlet of the kettle close to the theoretical value.

[0064] The fourth set of experiments:

[0065] Experimental Example 4: Based on Experimental Example 1 of the first group of experiments, only the feed flow rates of the dispersed phase and the continuous phase were adjusted, the dispersed phase feed flow rate was 150 mL / min, the continuous phase feed flow rate was 150 mL / min, and the theoretical outlet dispersed phase volume ratio was 0.5. The stirring speed was still 450 rpm, the power was measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation was stable was measured by the sampling method.

[0066] Comparative Example 4: Based on Comparative Example 1 of the first group of experiments, only the feed flow rates of the dispersed phase and the continuous phase were adjusted, the dispersed phase feed flow rate was 150 mL / min, the continuous phase feed flow rate was 150 mL / min, and the theoretical outlet dispersed phase volume ratio was 0.5. The stirring speed was still 450 rpm, the power was measured by the shaft torque method, and the outlet dispersed phase volume ratio after the continuous operation was stable was measured by the sampling method.

[0067] Experiment 4 and Comparative Example 4 were conducted under the same stirring speed and operating medium properties. The experimental results show that the radial flow impeller provided in Experimental Example 4 has comparable power consumption compared to the traditional Rushton impeller in Comparative Example 4. However, the dispersed phase volume ratio at the outlet of the reactor body in Experimental Example 4 is 0.513, which is only 2.6% different from the theoretical value of 0.5; while the dispersed phase volume ratio at the outlet of the reactor body in Comparative Example 4 is 0.582, which is as high as 16.4% different from the theoretical value of 0.5. Therefore, this group of experiments shows that the radial flow impeller provided in this embodiment can significantly promote the continuous stirring and mixing of immiscible solutions in the reactor body without increasing power consumption, can strengthen the dispersion of the dispersed phase, reduce its short circuit, make the fluid in the reactor close to the fully mixed flow, and the dispersed phase volume ratio at the outlet is closer to the theoretical value.

[0068] In summary, the radial stirring impeller provided in this embodiment can, on the one hand, significantly promote the mixing of immiscible solutions, strengthen the dispersion of the dispersed phase, reduce its short circuit, make the fluid in the kettle close to a fully mixed flow, and the volume ratio of the dispersed phase at the outlet is close to the theoretical value; on the other hand, it can strengthen the breakup of the dispersed phase droplets of the immiscible solution system and reduce the diameter of the dispersed phase droplets.

[0069] Embodiment 2

[0070] The similarities between this embodiment and the first embodiment are not described in detail. Only the differences between this embodiment and the first embodiment are described below:

[0071] In this embodiment, Figure 4 and Figure 5 As shown, the radial flow blade 300 is a rectangle, and the radial auxiliary blade 400 is a right-angle trapezoid with a beveled side. The short bottom side of the right-angle trapezoid with a beveled side abuts against the outer wall of the rotating shaft 100, the long bottom side of the right-angle trapezoid with a beveled side abuts against the radial flow blade 300 and is flush with the side of the radial flow blade 300 close to the drive output end, and the right-angled side of the right-angle trapezoid with a beveled side abuts against the disc 200. In the radial stirring paddle provided in this embodiment, the radial auxiliary blade 400 with a beveled side right-angle trapezoid is simply arranged, which can increase the sealing of the radial flow blade 300 and the disc 200, and improve the stirring effect of the radial stirring paddle.

[0072] Furthermore, the radial auxiliary blades 400 of right-angle trapezoidal shape with oblique sides can be located on both sides of the disk 200, forming the first structure of the radial stirring paddle and the second structure of the radial stirring paddle in this embodiment. Figure 4 As shown, the radial auxiliary blade 400 of the right-angle trapezoidal shape with a hypotenuse is located on the side of the disk 200 close to the drive output end (i.e., the upper surface of the disk 200). Figure 5 As shown, the radial auxiliary blades 400 of a right-angle trapezoidal shape with a hypotenuse may also be located on the side of the disk 200 away from the drive output end (ie, the lower surface of the disk 200).

[0073] It should be noted that Figure 4 and Figure 5 Only one set of radial flow blades 300 and radial auxiliary blades 400 are shown.

[0074] Embodiment 3

[0075] The similarities between this embodiment and the first embodiment are not described in detail. Only the differences between this embodiment and the first embodiment are described below:

[0076] In this embodiment, Figure 6 and Figure 7 As shown, the radial flow blades 300 and the radial auxiliary blades 400 are both rectangular, and the side of the radial flow blades 300 close to the drive output end is flush with the side of the radial auxiliary blades 400 close to the drive output end. In the radial agitator provided in this embodiment, since the radial flow blades 300 and the radial auxiliary blades 400 are both rectangular, they can be processed and used at the same time, which is simple to process and saves costs. Furthermore, the rectangular radial auxiliary blades 400 can be located on both sides of the disc 200, forming the first structure of the radial agitator in this embodiment and the second structure of the radial agitator. Specifically, continue as Figure 6 As shown, the rectangular radial auxiliary blade 400 is located on the side of the disk 200 close to the drive output end (i.e., the upper surface of the disk 200). Figure 7 As shown, the rectangular radial auxiliary blades 400 may also be located on the side of the disk 200 away from the drive output end (ie, the lower surface of the disk 200).

[0077] It should be noted that Figure 6 and Figure 7 Only one set of radial flow blades 300 and radial auxiliary blades 400 are shown.

[0078] Embodiment 4

[0079] The similarities between this embodiment and the first embodiment are not described in detail. Only the differences between this embodiment and the first embodiment are described below:

[0080] In this embodiment, Figure 8 and Fig. 9As shown, the radial flow blade 300 is a rectangle, and the radial auxiliary blade 400 is a curved right-angle trapezoid. The long bottom side of the curved right-angle trapezoid abuts against the outer wall of the rotating shaft 100, the short bottom side of the curved right-angle trapezoid abuts against the radial flow blade 300 and is flush with the side of the radial flow blade 300 close to the drive output end, the right-angle side of the curved right-angle trapezoid abuts against the disc 200, and the curved side of the curved right-angle trapezoid bends toward the disc 200. Compared with the radial stirring paddles provided in the first, second and third embodiments, the radial auxiliary blade 400 of the curved right-angle trapezoid provided in this embodiment increases the closure of the radial flow blade 300 and the disc 200, and the curved side is arranged to facilitate the flow of materials, so that the stirring effect is better.

[0081] Furthermore, the radial auxiliary blades 400 of curved right-angle trapezoidal shape can be located on both sides of the disk 200, forming the first structure of the radial stirring paddle and the second structure of the radial stirring paddle in this embodiment. Figure 8 As shown, the radial auxiliary blade 400 of a curved right-angle trapezoid is located on the side of the disk 200 close to the drive output end (i.e., the upper surface of the disk 200). Fig. 9 As shown, the radial auxiliary blades 400 of a curved right-angle trapezoidal shape may also be located on the side of the disk 200 away from the drive output end (ie, the lower surface of the disk 200).

[0082] It should be noted that Figure 8 and Fig. 9 Only one set of radial flow blades 300 and radial auxiliary blades 400 are shown.

[0083] Of course, the radial auxiliary blades 400 may also be in other shapes, and are not limited to the shapes in the first, second, third and fourth embodiments. The specific shape may be set as required.

[0084] It should also be noted that the comparative experimental setting method of the radial stirring paddle and the traditional Rushton paddle in Example 2, Example 3 and Example 4 is the same as that in Example 1, and the same conclusion can be drawn, which will not be repeated here. In short, the radial stirring paddle provided by the present invention can significantly promote the mixing of immiscible solutions, strengthen the dispersion of the dispersed phase, reduce its short circuit, make the fluid in the kettle close to the fully mixed flow, and the outlet dispersed phase volume ratio is close to the theoretical value; on the other hand, it can strengthen the fragmentation of the dispersed phase droplets of the immiscible solution system and reduce the diameter of the dispersed phase droplets. Obviously, the above embodiments of the present invention are only examples made to clearly illustrate the present invention, and are not limitations on the embodiments of the present invention. For ordinary technicians in the field, various obvious changes, readjustments and substitutions can be made without departing from the scope of protection of the present invention. It is not necessary and impossible to enumerate all the embodiments here. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the scope of protection of the claims of the present invention.

Claims

1. Radial stirring blade, characterized in that: include: A rotating shaft (100), wherein the rotating shaft (100) can be driven to rotate by a driving output end; A disk (200), wherein the rotating shaft (100) is vertically mounted at the center of the disk (200); A plurality of radial flow blades (300), wherein the plurality of radial flow blades (300) are spaced and distributed along the outer circumference of the disk (200), each of the radial flow blades (300) is vertically fixed to the disk (200) and extends radially along the disk (200), each of the radial flow blades (300) is radially close to the outer edge of the disk (200) and exceeds the edge of the disk (200), and the radial flow blades (300) are asymmetric with respect to the disk surface of the disk (200), and a gap is left between each of the radial flow blades (300) and the rotating shaft (100); A plurality of radial auxiliary blades (400), wherein the radial auxiliary blades (400) are perpendicular to the disc (200), each of the radial auxiliary blades (400) is located in one of the gaps, and the radial auxiliary blades (400) are respectively in contact with the side wall of the radial flow blade (300) and the outer wall of the rotating shaft (100) along the radial ends of the disc (200).

2. The radial stirring impeller according to claim 1, characterized in that: The radial flow blade (300) is provided with a notch on one side close to the rotating shaft (100), and the disc (200) is clamped in the notch.

3. The radial stirring impeller according to claim 1, characterized in that: The number of the radial auxiliary blades (400) is equal to the number of the radial flow blades (300), and they correspond one to one.

4. The radial stirring impeller according to claim 1, characterized in that: The radial auxiliary blade (400) is located on a side of the disc (200) close to the drive output end.

5. The radial stirring impeller according to claim 1, characterized in that: The radial auxiliary blade (400) is located on a side of the disc (200) away from the drive output end.

6. The radial stirring impeller according to any one of claims 1 to 5, characterized in that: The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a right triangle, one of the right-angled sides of the right triangle abuts against the surface of the disk (200), and the other right-angled side of the right triangle abuts against the radial flow blade (300) and is flush with a side of the radial flow blade (300) close to the drive output end.

7. The radial stirring impeller according to any one of claims 1 to 5, characterized in that: The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a hypotenuse right-angled trapezoid. The short base of the hypotenuse right-angled trapezoid abuts against the outer wall of the rotating shaft (100), the long base of the hypotenuse right-angled trapezoid abuts against the radial flow blade (300) and is flush with a side of the radial flow blade (300) close to the drive output end, and the right-angled side of the hypotenuse right-angled trapezoid abuts against the disc (200).

8. The radial stirring impeller according to any one of claims 1 to 5, characterized in that: The radial flow blade (300) and the radial auxiliary blade (400) are both rectangular, and a side of the radial flow blade (300) close to the drive output end and a side of the radial auxiliary blade (400) close to the drive output end are flush.

9. The radial stirring impeller according to any one of claims 1 to 5, characterized in that: The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a curved right-angle trapezoid. The long bottom side of the curved right-angle trapezoid abuts against the outer wall of the rotating shaft (100), the short bottom side of the curved right-angle trapezoid abuts against the radial flow blade (300) and is flush with a side of the radial flow blade (300) close to the drive output end, the right-angle side of the curved right-angle trapezoid abuts against the disc (200), and the curved side of the curved right-angle trapezoid is bent toward the disc (200).

10. A stirred reactor device, characterized in that: It comprises a reactor body and the radial stirring paddle according to any one of claims 1 to 9, wherein the radial stirring paddle is vertically arranged in the reactor body.

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