Radial impeller and stirred tank reactor arrangement
By designing a radial stirring impeller with asymmetrically distributed radial flow blades and auxiliary blades, the problems of uneven mixing and increased energy consumption in the prior art are solved, achieving efficient mixing effect and low-energy mixing uniformity.
Patent Information
- Application Number
- CN202411767139.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Patents(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-04
- Publication Date
- 2025-11-18
- Estimated Expiration
- 2044-12-04
AI Technical Summary
Existing radial flow impellers suffer from uneven mixing and insufficient shearing capacity in immiscible solution systems, resulting in large dispersed phase droplet diameters and deviations of the outlet two-phase volume ratio from the process design value during continuous operation. Furthermore, increasing the stirring speed only results in a limited increase in energy consumption.
Design a radial stirring impeller, including a rotating shaft, a disk, multiple radial flow blades and radial auxiliary blades. The blades are asymmetrically distributed and form a closed state near the rotating shaft, which increases the radial velocity component of the fluid and improves the stirring effect.
Without increasing energy consumption, it significantly improves stirring uniformity and stirring effect, reduces the diameter of dispersed phase droplets, approaches a fully mixed fluid state, and the outlet two-phase volume ratio is close to the theoretical value.
Smart Images
Figure CN119588205B_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of stirring equipment technology, and in particular to a radial stirring impeller and a stirring reaction vessel device. Background Technology
[0002] Stirred reactors, as mixing vessels for materials, are widely used in industrial production. The impeller is the core component of a stirred reactor, and impellers can be classified into radial flow impellers and axial flow impellers based on the flow pattern they generate within the reactor. In radial flow impellers, the fluid pumped by the impeller blades flows radially outward from the center of the blades, splitting into upper and lower main circulation flows upon encountering the reactor wall. Axial flow impellers, on the other hand, pump fluid downwards or upwards towards the bottom or surface of the reactor, depending on the blade tilt angle and rotation direction, circulating upon encountering the bottom or surface, thus forming a single main circulation within the stirred reactor.
[0003] For immiscible solution systems, there is usually a density difference between the dispersed and continuous phases, and the greater the density difference, the higher the requirements for mixing and dispersion in the stirred reactor. If there are weak mixing zones or dead zones within the reactor, not only will the dispersed phase droplets be large, but the two phases will also easily separate. Furthermore, when the stirred reactor is operating continuously, the continuously entering dispersed or continuous phase is prone to short-circuiting, causing the volume ratio of the two phases inside and at the outlet to deviate significantly from the designed volume ratio, resulting in reactor instability. Because radial flow impellers have significantly higher shear capacity than axial flow impellers, they are widely used for stirring and dispersing immiscible solution systems. For example, the most commonly used radial flow impellers include the Rushton impeller, etc. Figure 1As shown, the Rushton impeller includes a rotating shaft 100' and a disk 200'. The rotating shaft 100' is vertically mounted at the center of the disk 200', and rectangular blades 300' are evenly distributed along the edge of the disk 200', giving the Rushton impeller strong shearing capability. However, since the torque of the existing radial flow impeller is mainly generated at the end far from the impeller shaft, such as the rectangular blades 300' of the Rushton impeller which are only distributed along the edge of the disk 200', and the area near the rotating shaft 100' is not closed between the rectangular blades 300' and the disk 200', the main flow is not conducive to improving the radial circulation of the radial flow impeller, resulting in uneven stirring and insufficient stirring effect. Specifically, when the density difference between the dispersed phase and the continuous phase increases, the shearing and circulation provided by the Rushton impeller in the reactor cannot meet the requirements for sufficient liquid-liquid dispersion, resulting in excessively large droplet diameters and a dispersion / continuous phase volume ratio at the outlet that deviates significantly from the process set value during continuous operation. While increasing the stirring speed is one way to enhance mixing within the reactor, the increase in circulation volume is limited. Furthermore, increasing the stirring speed may further increase the turbulent energy dissipation rate in the strong shear zone, while the turbulent energy dissipation rate in the weak shear zone changes only slightly, resulting in insignificant enhancement of the dispersion of immiscible solutions within the reactor. Therefore, there is an urgent need to propose a radial stirring impeller and a stirred reactor device to solve the above problems. Summary of the Invention
[0004] The first objective of this invention is to provide a radial stirring paddle that can improve the uniformity of material mixing, provide good mixing effect, and consume less energy.
[0005] To achieve this objective, the present invention adopts the following technical solution:
[0006] Radial stirring impeller, comprising:
[0007] A rotating shaft, which can be driven to rotate by a drive output end;
[0008] A disc, wherein the rotating shaft is vertically mounted at the center of the disc;
[0009] Multiple radial flow blades are distributed at intervals along the outer circumference of the disk. Each radial flow blade is fixed perpendicularly to the disk and extends radially along the disk. Each radial flow blade extends beyond the edge of the disk on the side closest to the outer edge of the disk. The radial flow blades are asymmetrical about the disk surface. A gap is left between each radial flow blade and the rotation shaft.
[0010] A plurality of radial auxiliary blades are provided, the radial auxiliary blades being perpendicular to the disk, each of the radial auxiliary blades being located in one of the gaps, and the radial auxiliary blades abutting against the sidewall of the radial flow blade and the outer wall of the rotating shaft at both ends along the radial direction of the disk, respectively.
[0011] As an alternative technical solution for radial stirring impellers, the radial flow blades are provided with a notch on the side near the rotating shaft, and the disc is engaged in the notch.
[0012] As an optional technical solution for radial stirring impellers, the number of radial auxiliary blades is equal to the number of radial flow blades, and they correspond one-to-one.
[0013] As an alternative technical solution for radial stirring impellers, the radial auxiliary blades are located on the side of the disk near the drive output end.
[0014] As an alternative technical solution for radial stirring impellers, the radial auxiliary blades are located on the side of the disk opposite to the drive output end.
[0015] As an optional technical solution for a radial stirring impeller, the radial flow blade is rectangular, the radial auxiliary blade is a right-angled triangle, one right-angled side of the right-angled triangle abuts against the surface of the disk, and the other right-angled side of the right-angled triangle abuts against the radial flow blade and is flush with the side of the radial flow blade near the drive output end.
[0016] As an optional technical solution for a radial stirring impeller, the radial flow blade is rectangular, the radial auxiliary blade is a right-angled trapezoid with a hypotenuse, the short base of the right-angled trapezoid abuts against the outer wall of the rotating shaft, the long base of the right-angled trapezoid abuts against the radial flow blade and is flush with the side of the radial flow blade near the drive output end, and the right-angled side of the right-angled trapezoid abuts against the disk.
[0017] As an alternative technical solution for a radial stirring impeller, both the radial flow blade and the radial auxiliary blade are rectangular, with the side of the radial flow blade near the drive output end and the side of the radial auxiliary blade near the drive output end being flush.
[0018] As an optional technical solution for a radial stirring impeller, the radial flow blade is rectangular, 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 near the drive output end, the right-angled side of the curved right-angled trapezoid abuts against the disk, and the curved side of the curved right-angled trapezoid bends toward the disk.
[0019] The second objective of this invention is to provide a stirred reactor apparatus that can improve the uniformity of material mixing, achieve good mixing effect, and have low energy consumption.
[0020] To achieve this objective, the present invention adopts the following technical solution:
[0021] A stirred reactor apparatus includes a reactor body and the aforementioned radial stirring blade, wherein the radial stirring blade is vertically disposed within the reactor body.
[0022] The beneficial effects of this invention are:
[0023] The radial stirring impeller provided by this invention includes a rotating shaft, a disk, multiple radial flow blades, and several radial auxiliary blades. The rotating shaft is vertically mounted at the center of the disk. The multiple radial flow blades are spaced apart along the outer circumference of the disk. Each radial flow blade extends beyond the outer edge of the disk radially, and the radial flow blades are asymmetrical about the disk surface, increasing the shearing effect of the radial flow blades on the material and thus improving the stirring effect of the radial stirring impeller. A gap is left between each radial flow blade and the rotating shaft. The radial auxiliary blades are located in one of these gaps, and their two ends abut against the sidewalls of the radial flow blades and the outer wall of the rotating shaft, respectively. This creates a closed state between the radial auxiliary blades and the disk in the area near the rotating shaft (i.e., the gap), increasing the radial velocity component of the fluid in this area and inducing more material to enter the upper or lower circulation flow, thereby increasing the radial displacement of the radial stirring impeller. Therefore, without significantly increasing the stirring power consumption, this radial stirring impeller can enhance material circulation, resulting in more uniform material mixing and a better stirring effect. Attached Figure Description
[0024] Figure 1 This is a schematic diagram of the structure of a traditional Rushton propeller in the existing technology;
[0025] Figure 2 This is a schematic diagram of the first structure of the radial stirring impeller provided in Embodiment 1 of the present invention;
[0026] Figure 3 This is a schematic diagram of the second structure of the radial stirring impeller provided in Embodiment 1 of the present invention;
[0027] Figure 4 This is a schematic diagram of the first structure of the radial stirring impeller provided in Embodiment 2 of the present invention;
[0028] Figure 5 This is a schematic diagram of the second structure of the radial stirring impeller provided in Embodiment 2 of the present invention;
[0029] Figure 6 This is a schematic diagram of the first structure of the radial stirring impeller provided in Embodiment 3 of the present invention;
[0030] Figure 7 This is a schematic diagram of the second structure of the radial stirring impeller provided in Embodiment 3 of the present invention;
[0031] Figure 8This is a schematic diagram of the first structure of the radial stirring impeller provided in Embodiment 4 of the present invention;
[0032] Figure 9 This is a schematic diagram of the second structure of the radial stirring impeller provided in Embodiment 4 of the present invention.
[0033] In the picture:
[0034] 100', Rotating shaft; 200', Disk; 300', Rectangular blade;
[0035] 100, Rotating shaft; 200, Disk; 300, Radial flow blade; 400, Radial auxiliary blade. Detailed Implementation
[0036] The present invention will now be described in further detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and not intended to limit it. Furthermore, it should be noted that, for ease of description, the accompanying drawings show only the parts relevant to the present invention, and not all of the structures.
[0037] In the description of this invention, unless otherwise explicitly specified and limited, the terms "connected," "linked," and "fixed" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.
[0038] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.
[0039] In the description of this embodiment, the terms "upper," "lower," "right," etc., refer to the orientation or positional relationship shown in the accompanying drawings. They are used only for ease of description and simplification of operation, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the present invention. In addition, the terms "first" and "second" are used only for distinction in description and have no special meaning.
[0040] Example 1
[0041] The radial stirring paddle provided in this embodiment can improve the uniformity of material mixing, achieve good mixing effect, and consume less energy.
[0042] Specifically, such as Figure 2 As shown, the radial stirring impeller includes a rotating shaft 100, a disk 200, a plurality of radial flow blades 300, and a plurality of radial auxiliary blades 400. The rotating shaft 100 is driven to rotate by a drive output end and is vertically mounted at the center of the disk 200. The plurality of radial flow blades 300 are distributed at intervals along the outer circumference of the disk 200. For example, there may be two, three, four, or six radial flow blades 300. Each radial flow blade 300 is fixed perpendicularly to the disk 200 and extends radially along the disk 200. Each radial flow blade 300 extends beyond the edge of the disk 200 on one side of the disk 200, and the radial flow blades 300 are asymmetrical about the disk surface of the disk 200. A gap is left between each radial flow blade 300 and the rotating shaft 100. The radial auxiliary blades 400 are perpendicular to the disk 200, and each radial auxiliary blade 400 is located in one of the gaps. Furthermore, the radial auxiliary blades 400 abut against the sidewalls of the radial flow blades 300 and the outer wall of the rotating shaft 100 at both ends of the disk 200 in the radial direction.
[0043] Based on the above design, the rotating shaft 100 is rotatable and is vertically mounted at the center of the disk 200, enabling the rotation of the radial stirring paddle. Multiple radial flow blades 300 are spaced apart along the outer circumference of the disk 200. Each radial flow blade 300 is vertically fixed to the disk 200 and extends radially along the disk 200, achieving radial stirring of the material and ensuring uniform force distribution across all radial flow blades 300. Each radial flow blade 300 extends beyond the edge of the disk 200 along its radial direction, closer to the outer edge of the disk 200. Furthermore, the radial flow blades 300 are asymmetrical about the disk surface, meaning the disk 200 divides the radial flow blades 300 into upper and lower parts with different dimensions, increasing the shearing force of the radial flow blades 300 on the material and thus improving the stirring effect of the radial stirring paddle. A gap is left between each radial flow blade 300 and the rotating shaft 100. A radial auxiliary blade 400 is located in one of these gaps, with its two ends abutting against the sidewall of the radial flow blade 300 and the outer wall of the rotating shaft 100, respectively. This creates a closed loop between the radial auxiliary blade 400 and the disk 200 in the area near the rotating shaft 100 (i.e., the gap), increasing the radial velocity component of the fluid in this area and inducing more material to enter the upper or lower circulation flow, thereby increasing the radial displacement of the radial impeller. Therefore, without significantly increasing the mixing power consumption, this radial impeller can enhance material circulation, resulting in more uniform mixing and better mixing effect.
[0044] Optionally, the radial flow blade 300 has a notch on the side near the rotating shaft 100, and the disk 200 is fitted into 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 disk 200.
[0045] Optionally, the number of radial auxiliary blades 400 is equal to the number of radial flow blades 300, and they correspond one-to-one, that is, each gap is provided with a radial auxiliary blade 400 to improve the stirring effect of the radial stirring impeller.
[0046] In this embodiment, the radial flow blade 300 is rectangular, and the radial auxiliary blade 400 is a right triangle. One right-angled side 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 near 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 and the second structure of the radial stirring impeller in this embodiment. Specifically, continuing as follows... Figure 2 As shown, the triangular radial auxiliary blades 400 are located on the side of the disk 200 near the drive output end (i.e., the upper surface of the disk 200). Figure 3 As shown, the triangular radial auxiliary blade 400 can also be located on the side of the disk 200 away from the drive output end (i.e., 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 stirred reactor device, which has a good stirring effect on materials.
[0050] Specifically, the stirred reactor apparatus includes a reactor body and the aforementioned radial stirring paddle, which is vertically disposed within the reactor body. Due to the radial stirring paddle, this stirred reactor apparatus can stir materials more uniformly, resulting in a better stirring effect.
[0051] The following four sets of comparative experiments were conducted between the radial stirring impeller provided in this embodiment (Experimental Examples 1-4) and the conventional Rushton impeller in the prior art (Comparative Examples 1-4): Experimental Example 1 and Comparative Example 1 in the first set of experiments; Experimental Example 2 and Comparative Example 2 in the second set of experiments; Experimental Example 3 and Comparative Example 3 in the third set of experiments; and Experimental Example 4 and Comparative Example 4 in the fourth set of experiments. The reactor body used in each set of experiments was the same, and the specific experimental parameters and results are as follows:
[0052] First group of experiments:
[0053] Example 1: The reactor body has an inner diameter T = 200 mm and a height of 280 mm, including an elliptical bottom head height of 50 mm and a straight section height of 230 mm. Four baffles are installed close to the inner wall of the reactor, each with a width of T / 10. A radial flow impeller is installed on the stirring shaft at a height of T / 3 from the bottom of the reactor. The stirring shaft diameter is 10 mm, the entire radial flow impeller diameter is 67 mm, and the disc 200 diameter is 50 mm. There are six radial flow blades 300, each with a width (i.e., width perpendicular to the radial direction of the disc 200) of 14 mm and a length (i.e., length along the radial direction of the disc 200) of 17 mm. There are six radial auxiliary blades 400 on the side of the disc 200 near the drive output end, and they are triangular in shape. The dispersed phase was n-hexane with a density of 600 kg / m³; the continuous phase was water with a density of 1000 kg / m³. The reactor was operated continuously, with a dispersed phase feed flow rate of 25 mL / min and a continuous phase feed flow rate of 275 mL / min. Both the dispersed and continuous phases were added from the side wall of the reactor, with the dispersed phase inlet 60 mm from the bottom and the continuous phase inlet 12 mm from the bottom. The reactor had one overflow outlet 200 mm from the bottom, and the theoretical outlet dispersed phase volume ratio was 0.083. The stirring speed was 450 rpm. Power was measured using the shaft torque method, and the outlet dispersed phase volume ratio after continuous operation stabilized was measured using a sampling method.
[0054] Comparative Example 1: The radial flow agitator in Experimental Example 1 was replaced with a conventional Rushton impeller. The conventional Rushton impeller diameter remained 67 mm, the disk 200 diameter remained 50 mm, the number of rectangular blades remained six, the width remained 14 mm, and the length remained 17 mm. The stirring speed remained 450 rpm, and the power was measured using the shaft torque method. The outlet dispersed phase volume ratio after continuous operation and stabilization was measured using the sampling method.
[0055] Experimental Example 1 and Comparative Example 1 were conducted under the same stirring speed and operating medium properties. The experimental results show that the radial flow stirring impeller in Experimental Example 1 has comparable power consumption to the conventional Rushton impeller in Comparative Example 1. However, in Experimental Example 1, the dispersed phase volume ratio at the reactor body outlet under continuous stirring was 0.084, with a deviation of only 1.2% from the theoretical value of 0.083; while in Comparative Example 1, the dispersed phase volume ratio at the reactor body outlet under continuous stirring was 0.103, with a deviation as high as 24.1% from the theoretical value of 0.083. Therefore, this set of experiments shows that the radial flow stirring impeller provided in this embodiment can significantly promote the mixing of immiscible solutions in the reactor body under continuous stirring without increasing power consumption, enhance the dispersion of the dispersed phase, reduce its short-circuiting, and make the fluid in the reactor approach a fully mixed flow, with the dispersed phase volume ratio at the outlet approaching the theoretical value.
[0056] Second group of experiments:
[0057] Experiment Example 2: Based on Experiment Example 1 in the first group of experiments, the diameter distribution of the dispersed phase droplets inside the reactor was photographed using a telecentric multiphase measurement instrument, thereby obtaining the Sauter mean diameter D. 32 .
[0058] Comparative Example 2: Based on Comparative Example 1 of the first group of experiments, the diameter distribution of the dispersed phase droplets inside the vessel was photographed using a telecentric multiphase measurement instrument, thereby obtaining the Sauter mean diameter d. 32 .
[0059] Experimental results show that the radial flow impeller provided in Experiment Example 2 can be used to measure D. 32 =120μm, d obtained by conventional Rushton propeller measurement in Comparative Example 2 32 =150μm. That is, compared with the conventional Rushton impeller in Comparative Example 2, the radial flow stirring impeller provided in Experimental Example 2 significantly reduced the diameter of the dispersed phase droplets in the reactor, by 20%. Therefore, this set of experiments shows that the radial flow stirring impeller provided in this embodiment can enhance the fragmentation of dispersed phase droplets in immiscible solution systems and reduce the diameter of dispersed phase droplets.
[0060] Third group of experiments:
[0061] Experiment Example 3: Based on Experiment Example 1 in the first group of experiments, only the feed positions of the dispersed phase and the continuous phase were adjusted from the side wall of the reactor body to be added from above the liquid surface. The stirring speed remained at 450 rpm. The power was measured using the shaft torque method, and the volume ratio of the dispersed phase at the outlet after continuous operation was stabilized was measured using the sampling method.
[0062] Comparative Example 3: Based on Comparative Example 1 in the first group of experiments, only the feed positions of the dispersed phase and the continuous phase were adjusted from the side wall of the reactor body to being added from above the liquid surface. The stirring speed remained at 450 rpm. The power was measured using the shaft torque method, and the volume ratio of the dispersed phase at the outlet after continuous operation was stabilized was measured using 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 positions of the dispersed and continuous phases does not affect the stirring power consumption. However, in this group of experiments, because the feed position is located above the liquid surface, closer to the overflow outlet, the dispersed phase volume ratio at the outlet of Experimental Example 3 is higher than that of Experimental Example 1, with an increase of 15.5%; the dispersed phase volume ratio at the outlet of Comparative Example 3 is also higher than that of Comparative Example 1, with an increase of 19.4%. Furthermore, in Experimental Example 3, the dispersed phase volume ratio at the outlet of the reactor body deviates from the theoretical value of 0.083 by 16.9%; while in Comparative Example 3, the dispersed phase volume ratio at the outlet of the reactor body deviates from the theoretical value of 0.083 by as much as 48.2%. Therefore, this set of experiments fully demonstrates that the radial flow stirring impeller provided in this embodiment can induce more fluid to enter the upper circulation flow inside the vessel through the radial auxiliary blades 400, thereby increasing the radial displacement of the radial flow stirring impeller. This can significantly promote continuous stirring and mixing inside the vessel body of immiscible solutions, enhance the dispersion of the dispersed phase, reduce its short circuit, and make the volume ratio of the dispersed phase at the vessel outlet close to the theoretical value.
[0064] Fourth group of experiments:
[0065] Experiment Example 4: Based on Experiment Example 1 in the first group of experiments, only the feed flow rates of the dispersed phase and the continuous phase were adjusted. The feed flow rate of the dispersed phase was 150 mL / min, the feed flow rate of the continuous phase was 150 mL / min, and the theoretical outlet dispersed phase volume ratio was 0.5. The stirring speed remained at 450 rpm. The power was measured using the shaft torque method, and the outlet dispersed phase volume ratio after continuous operation was stabilized was measured using the sampling method.
[0066] Comparative Example 4: Based on Comparative Example 1 in the first group of experiments, only the feed flow rates of the dispersed phase and the continuous phase were adjusted. The feed flow rate of the dispersed phase was 150 mL / min, and the feed flow rate of the continuous phase was 150 mL / min. The theoretical outlet dispersed phase volume ratio was 0.5. The stirring speed remained at 450 rpm. The power was measured using the shaft torque method, and the outlet dispersed phase volume ratio after continuous operation was stabilized was measured using 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 Experiment 4 has comparable power consumption to the conventional Rushton impeller in Comparative Example 4. However, the dispersed phase volume ratio at the reactor outlet in Experiment 4 was 0.513, deviating from the theoretical value of 0.5 by only 2.6%; while in Comparative Example 4, the dispersed phase volume ratio at the reactor outlet was 0.582, deviating from the theoretical value of 0.5 by as much as 16.4%. Therefore, this set 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, enhance the dispersion of the dispersed phase, reduce its short-circuiting, and make the fluid in the reactor approach a fully mixed flow, with the dispersed phase volume ratio at the outlet closer to the theoretical value.
[0068] In summary, the radial stirring impeller provided in this embodiment can significantly promote the mixing of immiscible solutions, enhance the dispersion of the dispersed phase, reduce its short circuits, and make the fluid in the reactor close to a fully mixed flow, with the volume ratio of the dispersed phase at the outlet close to the theoretical value. On the other hand, it can enhance the breakup of dispersed phase droplets in the immiscible solution system and reduce the diameter of the dispersed phase droplets.
[0069] Example 2
[0070] The similarities between this embodiment and Embodiment 1 will not be repeated here. The following only describes the differences between this embodiment and Embodiment 1:
[0071] In this embodiment, as Figure 4 and Figure 5 As shown, the radial flow blade 300 is rectangular, and the radial auxiliary blade 400 is a right-angled trapezoid with a hypotenuse. The shorter base of the right-angled trapezoid abuts against the outer wall of the rotating shaft 100, and the longer base abuts against the radial flow blade 300 and is flush with the side of the radial flow blade 300 near the drive output end. The right-angled side of the right-angled trapezoid abuts against the disk 200. In the radial stirring impeller provided in this embodiment, the radial auxiliary blade 400 with a hypotenuse is simply designed, which can increase the enclosure of the radial flow blade 300 and the disk 200, and improve the stirring effect of the radial stirring impeller.
[0072] Furthermore, the radial auxiliary blades 400, which are shaped like right-angled trapezoids with inclined sides, can be located on both sides of the disk 200, forming the first structure and the second structure of the radial stirring impeller in this embodiment. Specifically, continuing as follows... Figure 4 As shown, the radial auxiliary blade 400, which is a right trapezoid with a hypotenuse, is located on the side of the disk 200 near the drive output end (i.e., the upper surface of the disk 200). Figure 5 As shown, the radial auxiliary blade 400, which is a right trapezoid with a hypotenuse, can also be located on the side of the disk 200 away from the drive output end (i.e., the lower surface of the disk 200).
[0073] It should be noted that, Figure 4 and Figure 5 The Chinese version only shows one set of radial flow blades 300 and radial auxiliary blades 400.
[0074] Example 3
[0075] The similarities between this embodiment and Embodiment 1 will not be repeated here. The following only describes the differences between this embodiment and Embodiment 1:
[0076] In this embodiment, as Figure 6 and Figure 7 As shown, both the radial flow blade 300 and the radial auxiliary blade 400 are rectangular, with the side of the radial flow blade 300 near the drive output end and the side of the radial auxiliary blade 400 near the drive output end flush. In the radial stirring impeller provided in this embodiment, since both the radial flow blade 300 and the radial auxiliary blade 400 are rectangular, they can be manufactured and used simultaneously, simplifying manufacturing and saving costs. Furthermore, the rectangular radial auxiliary blades 400 can be located on both sides of the disk 200, forming the first structure and the second structure of the radial stirring impeller in this embodiment. Specifically, continuing as... Figure 6 As shown, the rectangular radial auxiliary blades 400 are located on the side of the disk 200 near the drive output end (i.e., the upper surface of the disk 200). Figure 7 As shown, the rectangular radial auxiliary blade 400 can also be located on the side of the disk 200 away from the drive output end (i.e., the lower surface of the disk 200).
[0077] It should be noted that, Figure 6 and Figure 7 The Chinese version only shows one set of radial flow blades 300 and radial auxiliary blades 400.
[0078] Example 4
[0079] The similarities between this embodiment and Embodiment 1 will not be repeated here. The following only describes the differences between this embodiment and Embodiment 1:
[0080] In this embodiment, as Figure 8 and Figure 9As shown, the radial flow blade 300 is rectangular, and the radial auxiliary blade 400 is a curved right-angled trapezoid. The long base of the curved right-angled trapezoid abuts against the outer wall of the rotating shaft 100, and the short base abuts against the radial flow blade 300 and is flush with the side of the radial flow blade 300 near the drive output end. The right-angled side of the curved right-angled trapezoid abuts against the disk 200, and the curved side of the curved right-angled trapezoid bends towards the disk 200. Compared with the radial stirring blades provided in Embodiments 1, 2, and 3, the radial auxiliary blade 400 with its curved right-angled trapezoidal shape provides better enclosure of the radial flow blade 300 and the disk 200, and the curved side facilitates material flow, resulting in better stirring effect.
[0081] Furthermore, the curved right-angled trapezoidal radial auxiliary blades 400 can be located on both sides of the disk 200, forming the first structure and the second structure of the radial stirring impeller in this embodiment. Specifically, continuing as follows... Figure 8 As shown, the curved right-angled trapezoidal radial auxiliary blade 400 is located on the side of the disk 200 near the drive output end (i.e., the upper surface of the disk 200). Figure 9 As shown, the curved right-angled trapezoidal radial auxiliary blade 400 can also be located on the side of the disk 200 away from the drive output end (i.e., the lower surface of the disk 200).
[0082] It should be noted that, Figure 8 and Figure 9 The Chinese version only shows one set of radial flow blades 300 and radial auxiliary blades 400.
[0083] Of course, the radial auxiliary blade 400 can also be other shapes, not limited to the shapes in Embodiment 1, Embodiment 2, Embodiment 3 and Embodiment 4. The specific shape can be set as needed.
[0084] It should also be noted that the comparative experimental setup methods for the radial stirring impeller and the traditional Rushton impeller in Examples 2, 3, and 4 are the same as those in Example 1, and the same conclusions can be drawn. Therefore, they will not be repeated here. In summary, the radial stirring impeller provided by this invention can significantly promote the mixing of immiscible solutions, enhance the dispersion of the dispersed phase, reduce short-circuiting, and make the fluid in the reactor approach a fully mixed flow, with the dispersed phase volume ratio at the outlet approaching the theoretical value. Furthermore, it can enhance the breakup of dispersed phase droplets in the immiscible solution system, reducing the diameter of the dispersed phase droplets. Obviously, the above embodiments of this invention are merely examples to clearly illustrate the invention and are not intended to limit the implementation of the invention. For those skilled in the art, various obvious changes, readjustments, and substitutions can be made without departing from the scope of protection of this invention. It is neither necessary nor possible to exhaustively describe all embodiments here. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of this invention should be included within the scope of protection of the claims of this invention.
Claims
1. A radial stirring impeller, characterized in that, include: A rotating shaft (100) is capable of being driven to rotate by a drive output end; A disk (200), wherein the rotating shaft (100) is vertically mounted at the center of the disk (200); Multiple radial flow blades (300) are distributed at intervals along the outer circumference of the disk (200). Each radial flow blade (300) is fixed perpendicularly to the disk (200) and extends radially along the disk (200). Each radial flow blade (300) extends beyond the edge of the disk (200) on the side of the disk (200) closer to the outer edge of the disk (200) in the radial direction. The radial flow blades (300) are asymmetrical about the disk surface of the disk (200). A gap is left between each radial flow blade (300) and the rotating shaft (100). A plurality of radial auxiliary blades (400) are perpendicular to the disk (200), each of the radial auxiliary blades (400) is located in one of the gaps, and the radial auxiliary blades (400) abut against the side wall of the radial flow blade (300) and the outer wall of the rotating shaft (100) at both ends of the disk (200) in the radial direction.
2. The radial stirring impeller according to claim 1, characterized in that, The radial flow blade (300) has a notch on the side near the rotating shaft (100), and the disk (200) is engaged in the notch.
3. The radial stirring impeller according to claim 1, characterized in that, The number of radial auxiliary blades (400) is equal to the number of 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 the side of the disk (200) near the drive output end.
5. The radial stirring impeller according to claim 1, characterized in that, The radial auxiliary blade (400) is located on the side of the disk (200) opposite to the drive output end.
6. The radial stirring impeller according to any one of claims 1-5, characterized in that, The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a right triangle. One right-angled side of the right triangle abuts the surface of the disk (200), and the other right-angled side of the right triangle abuts the radial flow blade (300) and is flush with the side of the radial flow blade (300) near the drive output end.
7. The radial stirring impeller according to any one of claims 1-5, characterized in that, The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a right trapezoid with a hypotenuse. The short base of the right trapezoid abuts against the outer wall of the rotating shaft (100), the long base of the right trapezoid abuts against the radial flow blade (300) and is flush with the side of the radial flow blade (300) near the drive output end, and the right-angled side of the right trapezoid abuts against the disk (200).
8. The radial stirring impeller according to any one of claims 1-5, characterized in that, Both the radial flow blade (300) and the radial auxiliary blade (400) are rectangular. The radial flow blade (300) is flush with the side of the drive output end and the radial auxiliary blade (400) is flush with the side of the drive output end.
9. The radial stirring impeller according to any one of claims 1-5, characterized in that, The radial flow blade (300) is rectangular, and the radial auxiliary blade (400) is a curved right-angled trapezoid. The long base of the curved right-angled trapezoid abuts against the outer wall of the rotating shaft (100), and the short base of the curved right-angled trapezoid abuts against the radial flow blade (300) and is flush with the side of the radial flow blade (300) near the drive output end. The right-angled side of the curved right-angled trapezoid abuts against the disk (200), and the curved side of the curved right-angled trapezoid bends toward the disk (200).
10. A stirred reaction vessel apparatus, characterized in that, It includes a reactor body and a radial stirring impeller as described in any one of claims 1-9, wherein the radial stirring impeller is vertically disposed within the reactor body.
Citation Information
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