WO2017185431A1 - 一种装配扇环型凹面叶片的气液分散搅拌器装置 - Google Patents

一种装配扇环型凹面叶片的气液分散搅拌器装置 Download PDF

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Publication number
WO2017185431A1
WO2017185431A1 PCT/CN2016/082483 CN2016082483W WO2017185431A1 WO 2017185431 A1 WO2017185431 A1 WO 2017185431A1 CN 2016082483 W CN2016082483 W CN 2016082483W WO 2017185431 A1 WO2017185431 A1 WO 2017185431A1
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Prior art keywords
blade
stirring
liquid
agitator
disk
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PCT/CN2016/082483
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English (en)
French (fr)
Inventor
郑志永
孙东东
詹晓北
高敏杰
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江南大学
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Application filed by 江南大学 filed Critical 江南大学
Priority to US15/548,080 priority Critical patent/US10322386B2/en
Publication of WO2017185431A1 publication Critical patent/WO2017185431A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/112—Stirrers characterised by the configuration of the stirrers with arms, paddles, vanes or blades
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/115—Stirrers characterised by the configuration of the stirrers comprising discs or disc-like elements essentially perpendicular to the stirrer shaft axis
    • B01F27/1152—Stirrers characterised by the configuration of the stirrers comprising discs or disc-like elements essentially perpendicular to the stirrer shaft axis with separate elements other than discs fixed on the discs, e.g. vanes fixed on the discs
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/86—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis co-operating with deflectors or baffles fixed to the receptacle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B01F27/906—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms  with fixed axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/93—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with rotary discs
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/50—Mixing receptacles
    • B01F35/53—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components
    • B01F35/531—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components with baffles, plates or bars on the wall or the bottom
    • B01F35/5312—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components with baffles, plates or bars on the wall or the bottom with vertical baffles mounted on the walls
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
    • B01F2101/2204—Mixing chemical components in generals in order to improve chemical treatment or reactions, independently from the specific application
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
    • B01F23/2336—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer
    • B01F23/23362—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer the gas being introduced under the stirrer

Definitions

  • the invention relates to a gas-liquid dispersing agitator device for assembling a fan-ring type concave blade, belonging to the fields of bioengineering, chemical engineering and environmental engineering equipment.
  • Gas-liquid two-phase mixing is widely used in process units such as ventilation fermentation, oxidation reaction, hydrogenation reaction, and biological aeration. Chemical engineers expect to invent a device that enables efficient gas-liquid dispersion.
  • the devices capable of realizing gas-liquid two-phase dispersion mainly include: (1) a bubble column reactor; (2) an airlift type reactor; (3) a stirring device with a gas-liquid dispersion agitator; and (4) a rotary nozzle based on Hybrid system.
  • the radial flow agitator is a kind of agitator especially suitable for gas-liquid dispersion function, which comprises a hub, a disc and a plurality of blades evenly distributed on the disc, and the disc can collect the bubbles under the agitator and introduce them into the air.
  • the area of the blade is sheared to produce a good gas-liquid dispersion effect.
  • Rushton first invented the Rushton mixer, which was innovatively applied in the field of penicillin fermentation, and pioneered the gas-liquid dispersion type agitator.
  • Bakker invented the asymmetric concave paddle, the BT-6 agitator, with the leading edge of the blade extending tangentially beyond the leading edge of the lower blade so that the blade can capture More bubbles, and its more deeply concave surface can significantly reduce the formation of cavitation behind the blade, thereby improving the gas-liquid dispersion efficiency and the flooding point, so that the gas-liquid dispersion efficiency of the agitator is significantly improved.
  • the power consumption of the radial flow agitator is related to conditions such as agitation speed, aeration, fluid properties, etc., and also to the structure and installation conditions of the agitator. Due to the cavitation phenomenon, the design idea of the radial flow agitator is developed to a more concave surface. However, there is a serious problem that the use of more concave blades without increasing the width of the blades can reduce the power consumption, but the radial displacement performance is also greatly reduced.
  • Increasing the blade width is beneficial to improve its radial displacement performance, but the diameter of the outer edge apex is much larger than the diameter of the tail point, so that the blade generates great torque and power consumption at the apex region of the outer edge, and contributes to the radial displacement. It is small.
  • the present invention employs a special concave blade structure similar to the shape of a fan ring, and the blade design is projected on the horizontal plane into the shape of a fan ring.
  • the blade thus designed changes the width of the conventional blade into an increase in the arc length of the blade in the present invention, and the diameter of the apex of the outer edge is equal to the diameter of the tail point, thereby avoiding excessive protrusion at the periphery of the blade, and effectively improving The dispersion and mixing properties of the agitator.
  • the radial contour of the blade of the invention is a spatial curve obtained by bending a concave planar curve along a cylindrical surface, which is advantageous for achieving high-efficiency dispersion of the gas-liquid two phases in the radial discharge process.
  • the stirring device of the invention has lower power consumption, higher gas-liquid dispersion and mixing performance, and greatly reduces the occurrence of cavitation, and improves the flooding point, that is, can withstand higher at the same rotation speed. Ventilation enhances gas holding performance.
  • the present invention provides a stirrer device for gas-liquid dispersion and mixing in a reactor; the device comprises three parts of a stirring impeller, a stirring shaft and a power device; the stirring impeller comprises a plurality of radially extending concave blades; a concave surface
  • the projection shape of the upper and lower portions of the blade on the horizontal surface is a fan ring, and the arc of the fan ring projected from the upper portion of the blade is larger than the curvature of the fan ring obtained in the lower portion.
  • Both the radially inner side edge and the radially outer side edge of the blade are on a cylindrical surface centered on the stirring shaft, and the difference in radius between the two cylindrical surfaces is the length of the blade.
  • a spatial curve is obtained, which is called a radial contour.
  • the radial contour can be considered to be obtained by bending a plane curve along a cylindrical surface, which is considered to be the basic shape line of the blade.
  • the radial contour of the blade is therefore on a cylindrical surface centered on the agitator shaft.
  • the basic shape line of the blade includes two vertices and one tail point. With the plane of the disk as the boundary, the part between the tail point and the upper vertex is the upper shape line, the part between the tail point and the lower vertex is the lower shape line, and the tail point is on the horizontal plane.
  • structural features such as vertices and tail points in the contour line correspond to points in the basic shape line.
  • the contour line and the lower part are projected onto the horizontal plane to obtain two arcs.
  • the arc length of the upper part of the contour projection is larger than the lower part, that is, the arc of the upper part of the contour is larger than the arc of the lower part.
  • the blade is obtained by taking the radially innermost contour of the blade as a baseline and extending a certain length in the radial direction.
  • the arc of the arc obtained by projecting the contours of the contours to the horizontal plane remains unchanged, and the arc length gradually increases.
  • the axial height between the contour line and the lower vertex is called the opening height, and the opening height remains unchanged during the radial extension.
  • the line connecting the vertices on each contour line constitutes the upper leading edge of the blade, and the line connecting the lower apex constitutes the lower leading edge of the blade, and the line connecting the tail point constitutes the trailing edge of the blade.
  • the leading edge, the lower leading edge and the trailing edge of the blade pass through the center line of the stirring shaft, and their projection lines on the horizontal plane intersect at a point, that is, the center point of the disk.
  • the upper portion of the blade has a fan-shaped protruding portion more than the lower portion.
  • the function of the protruding portion is to facilitate the capture of rising bubbles and enhance the gas holding capacity of the agitator.
  • the blade of the stirring device is a shape similar to a fan ring, and the projection of the blade on the horizontal surface is in the shape of a fan ring.
  • a blade changes the manner in which the conventional radial flow blades extend only in parallel along the radial direction of the trailing edge, but each portion of the blade expands and expands in the respective radial directions, thereby forming the shape of the above-mentioned fan ring.
  • the blade is designed into the above shape, so that the contour of the blade is in the direction of rotation of the impeller, so that each part of the blade can be directly flowed, thereby radially discharging it, thereby improving the utilization efficiency of the blade.
  • the portion of the upper portion of the blade that protrudes more from the lower portion is advantageous for capturing the rising bubbles and enhancing the gas holding property, so that the bubbles are easily discharged radially and dispersed in the liquid.
  • the agitating impeller further comprises a disc and a hub, and the concave vane is mounted on the disc; the concave vane is divided into upper and lower portions by a plane of the disc.
  • each blade has a thickness that is the same shape as the liquid-facing surface.
  • both the radially inner side edge and the radially outer side edge of the blade are on a cylindrical surface centered on the agitating shaft, and the difference in radius between the two cylindrical faces is the length of the blade.
  • the distance from the lower point to the horizontal plane is equal to the distance from the upper corresponding point to the plane of the disk at the contour of any radial position of the blade. This ensures uniformity of the upper and lower extension of the blade so that the flow field during the agitation process is relatively stable. However, the portion of the upper portion of the blade that protrudes more than the lower portion cannot find a corresponding point in the lower portion of the blade. This results in a partial downward axial flow that enhances the circulation at the bottom of the impeller.
  • the value of the fan ring curvature ⁇ obtained by projecting the upper portion of the liquid-facing surface of the blade on the plane of the disk is generally between 0.52 and 2.09.
  • the ratio of the fan ring curvatures ⁇ and ⁇ obtained by projecting the lower and upper portions of the liquid-facing surface of the blade to the plane of the disk is generally between 0.45 and 0.85.
  • the agitating impeller further includes a hub connecting the disc and the agitator shaft.
  • the agitating impeller further includes a horizontal disc and a plurality of concave vanes extending radially like a fan ring are mounted around the disc; the asymmetrical upper and lower portions of the vane are in the disc Connected at the plane.
  • the thickness of the disk does not exceed its radius, and the blades are evenly distributed around the disk.
  • the ratio of the diameter of the disk to the diameter of the agitator is between 0.5 and 0.8.
  • the ratio of the axial height of the liquid-facing surface to the diameter of the agitator is between 0.1 and 0.35.
  • the ratio of the length of the liquid-facing surface to the diameter of the agitator is between 0.15 and 0.4.
  • the number of blades of the agitating impeller is between 3 and 10.
  • the extension of the lower leading edge and the trailing edge of the blade on the horizontal plane intersects at a point which is the center point of the disk.
  • the curvature of the arc of the blade contour projection on the horizontal plane remains constant during the radial extension.
  • the contour of the liquid-facing surface of the blade is a spatial curve, which can be obtained by bending an elliptical arc, a circular arc, a parabola or other similarly shaped planar curve along the cylindrical surface.
  • the shape of the plane curve is generally a parabola.
  • the agitator device is typically fabricated from stainless steel or may be fabricated from other materials such as carbon steel, high strength plastic, and the like.
  • the hub and the disc may be detachable or closed, and may be selected according to different working conditions.
  • the hub is coupled to the agitator shaft by fastening screws, or by tightening bolts, or flat keys.
  • the agitation means is typically used in a cylindrical reactor with an elliptical head or a dished head mounted on its central axis.
  • the ratio of the diameter of the agitator to the inner diameter of the reactor is between 0.25 and 0.6.
  • the agitator is mounted at the bottom of the reactor and can be used alone or in combination with other agitators.
  • a gas distributor is installed under the agitator, and the ventilation direction of the gas distributor may be upward or downward.
  • the agitator rotates in a horizontal direction, and the direction of rotation is a direction in which the concave surfaces of the blades face each other.
  • the agitator shaft in the apparatus of the present invention is used to connect the agitating impeller and the power unit to drive the agitating impeller to rotate to capture the rising bubbles and disperse them.
  • the agitating impeller is reinforced with the agitator shaft through the hub.
  • the blade of the stirring device of the present invention is a spatial shape similar to a fan ring, and the projection of the blade on the horizontal surface is in the shape of a fan ring.
  • a blade changes the manner in which the conventional radial flow vanes extend only in the radial direction of the trailing edge, but each portion of the vane extends in the respective radial directions to form the shape of the above-described fan ring.
  • the blade is designed to have the above shape such that any radial contour of the blade is in the direction of rotation of the impeller, so that each portion of the blade can be directly flowed, thereby radially discharging it, thereby improving the utilization efficiency of the blade.
  • the protruding portion generated at the lower portion of the upper portion of the blade facilitates the capture of the rising air bubbles, enhancing the gas holding property, so that the air bubbles are easily discharged radially and dispersed in the liquid.
  • the device of the invention has the characteristics of high dispersing efficiency and low energy consumption, the air pocket behind the blade is smaller, the gas dispersion is more sufficient, and the gas flooding point is higher during the aeration stirring operation.
  • the high-efficiency and energy-saving gas-liquid dispersing agitator device of the invention can be applied to a reactor such as aeration agitation fermentation, hydrogenation reaction, oxidation reaction and biological aeration, so that it has lower power consumption, higher mixing performance and gas holding. Mass transfer performance, the gas can be dispersed in the liquid with high efficiency and energy saving.
  • Figure 1 Front view of the agitator unit in the reactor
  • Figure 2 A perspective view of the agitator
  • Figure 3 A perspective view of the liquid-facing surface of the agitator blade
  • Figure 4 Top view of the liquid-facing surface of a single blade of the agitator
  • Figure 5 Front view of the liquid-facing surface of a single blade of the agitator
  • Figure 6 Top view of the agitator.
  • the agitating device (20) comprises an agitator (17), a stirring shaft (18) and a set of power units (19), wherein the agitator (17) comprises A disc (15), a hub (16) and a plurality of radially extending vanes (14).
  • the blade (14) is obtained by increasing the thickness of the liquid-facing surface (12) backward, and after thickening, the blade (14) is obtained, and the back surface (13) is obtained.
  • the technical characteristics of the liquid-facing surface (12) represent the technical features of the blade (14).
  • the liquid-contacting surface (12) is a concave shape surrounded by a radially inner edge (10), a radially outer edge (11), an upper leading edge (8) and a lower leading edge (9).
  • the inner edge (10) extends radially to the shape of the fan ring formed by the outer edge (11).
  • the inner edge (10) includes an upper vertex (3), a lower vertex (4), and a tail point (1).
  • the outer edge includes an upper vertex (5), a lower vertex (6), and a tail point (2).
  • the upper vertex (3) extends radially to the upper vertex (5) to form the upper leading edge (8)
  • the lower vertex (4) extends radially to the lower vertex (6) to form the lower leading edge (9)
  • the trailing point (1) is radial Extend to the end point (2) to form the trailing edge (7).
  • the inner edge (10) is on the cylindrical surface at the radial position where the tail point (1) is located, and the outer edge (11) is on the cylindrical surface at the radial position where the tail point (2) is located.
  • the intersection of the cylindrical surface at each radial position on the trailing edge and the liquid-facing surface (12) is the same spatial shape as the inner edge (10) and the outer edge (11), which are collectively referred to as the liquid-facing surface (12).
  • contour line is a space curve obtained by bending a plane curve perpendicular to the trailing edge at the position of the tail point along the cylindrical surface.
  • the shape of the plane curve can be an elliptical arc, a parabola, a circular arc, or other curved shape, preferably a parabola.
  • the projection of the liquid-facing surface (12) on the horizontal plane ⁇ is in the shape of a fan ring.
  • the horizontal plane ⁇ is the horizontal plane where the disc (15) is located. With the horizontal plane ⁇ as the boundary, the liquid-facing surface (12) can be divided into upper and lower parts. The upper and lower portions of the liquid-facing surface (12) are projected on the horizontal plane ⁇ to form two fan rings of different curvatures.
  • the arc is constant during the radial extension of the inner edge (10) to the outer edge (11).
  • the upper guide edge (8) and the lower guide edge (9) of the liquid-facing surface (12) intersect at a point O on the projection line on the horizontal plane and the extension line of the trailing edge (7).
  • Point O is the center point of the disc (15).
  • the fan ring curvature (indicated by ⁇ ) projected on the upper surface of the liquid-facing surface (12) on the horizontal plane ⁇ is larger than the fan-arc curvature (indicated by ⁇ ) projected from the lower part on the horizontal plane ⁇ to make the liquid-facing surface (12)
  • the upper portion produces a larger portion than the lower portion, thereby facilitating the capture of rising bubbles (23) to enhance gas-liquid dispersion.
  • the upper part of the liquid-facing surface (12) is projected on the horizontal plane.
  • the value of the fan ring curvature ⁇ to which it is obtained is generally between 0.52 and 2.09 (corresponding to a central angle of 30 to 120), and is preferably 1.25 (corresponding to a central angle of 72).
  • the ratio of the circle arc ⁇ obtained by the lower part of the liquid-facing surface to the curvature ⁇ of the upper part of the projection is generally between 0.45 and 0.85, and 0.75 (corresponding to a central angle of 43°) is optimal.
  • the height of the inner edge (10) of the liquid-facing surface (12) and the height of the outer edge (11) are identical.
  • the height of the inner edge (10) of the liquid-facing surface (12) refers to the axial height between the upper vertex (3) and the lower vertex (4); the height of the outer edge (11) refers to the upper vertex (5) and The axial height between the lower vertices (6).
  • the height of the contour at any radial position of the liquid-facing surface (12) refers to the axial height between the upper and lower vertices.
  • the axial height of the contour at any radial position of the liquid-facing surface (12) is the same, and this axial height is the height of the liquid-facing surface (12) (indicated by h).
  • the above is the shape and size characteristics of the liquid-facing surface (12), which represents the shape and size characteristics of the blade (14).
  • the blade (14) is obtained by thickening the liquid-facing surface (12) toward the outside of the concave surface.
  • the agitator (17) has six blades (14) mounted on the disc (15).
  • the number of blades can be 3 to 10, and 6 is better.
  • the blades (14) are evenly distributed around the disc (15), and the trailing edge (7) is fixed with the disc (15), i.e., the vane (14) is partially embedded in the disc (15) to ensure its mechanical strength.
  • Diameter of the disk (15) (indicated by d 3) of the agitator (17) ratio of the diameter (indicated by D) is preferably between 0.5 and 0.8, more preferably 0.68.
  • the ratio of the axial height of the liquid-facing surface (12) to the diameter D of the agitator (17) is preferably between 0.1 and 0.35, and 0.2 is optimal.
  • the ratio of the length of the liquid-contacting surface (12) (indicated by L) to the diameter D of the agitator (17) is preferably between 0.15 and 0.4, and 0.3 is the best.
  • the disc (15) may be of other shapes, such as a striped strip in the middle, or the like.
  • the thickness of the disc (15) is less than its radius.
  • the agitator (17) is coupled to the agitator shaft (18) via a hub (16), and the hub (16) allows the agitator (17) to be coupled to the agitator shaft (18) to be very strong.
  • the hub (16) to the inner side within the scope of the stirring shaft (18) the diameter of the blade (14) (denoted by d 1) smaller than the diameter of the hub (16) (represented by d 2).
  • the diameter of the agitator shaft (18) and the hub (16) should be as small as possible to ensure sufficient mechanical strength to not affect the performance of the agitator (17) and the overall flow field.
  • the hub (16) and the disc (15) can be either detachable or closed, and can be selected according to different working conditions.
  • the power unit (19) includes a motor and a speed reducer (not shown in detail) to enable the agitator (17) to obtain rotational power.
  • the agitator (17) is preferably rotated in a horizontal direction to maintain its balance.
  • the agitator (17) is used in a reactor (26) containing a quantity of fluid (25) which may be a liquid, a mixture of several liquids or a suspension of particles, etc.
  • the shape of the reactor (26) may be a rectangular parallelepiped, a cylinder or the like, preferably a cylindrical container having an elliptical head.
  • a baffle (22) is generally added to the reactor (26) to prevent Or reduce the vortex when rotating.
  • the ratio of the diameter D of the agitator (17) to the diameter of the reactor (26) is preferably between 0.25 and 0.6, more preferably 0.4.
  • the agitator (17) is preferably installed near the bottom of the reactor (26) and may be used alone or in combination with other radial or axial flow agitator mixing systems.
  • the hub (16) is connected to the agitator shaft (18) by means of fastening screws, or by tightening bolts, or flat keys, so that the agitator (17) rotates with the agitator shaft (18).
  • the fluid (25) in the reactor (26) is required to be submerged in the agitator (17) when it is used, i.e., the liquid level (24) is higher than the agitator (17).
  • a gas distributor (21) is installed below the agitator (17), and the gas distributor (21) functions to introduce bubbles (23) into the fluid (25).
  • the gas distributor (21) is a venting ring.
  • the gas distributor (21) may also be one or several vent tubes, metal sintered mesh or other types, and the gas distributor (24) may have a venting direction that is either upward or downward.
  • a ventilating ring with a ventilating direction is relatively common.
  • the material of the stirring device (20) is stainless steel, and it can also be other high-strength and corrosion-resistant materials such as carbon steel and high-strength plastic.
  • the specific operation of the stirring device (20) is as follows: the gas distributor (21) blows a bubble (23) into the fluid (25) in the reactor (26), and the bubble (23) rises due to its low density, and the power device (19) Providing power to cause the agitator shaft (18) and the agitator (17) to rotate in a horizontal direction at a certain rotational speed, and the rotating blade (14) captures the rising bubble (23) so as to be along with the surrounding fluid (25). To the movement, the bubble (23) is broken by the shearing action during the movement to be dispersed in the fluid (25). Two circulation flow patterns are formed above and below the agitator (17) for gas-liquid dispersion and mixing by the release of the bubble (23) in the gas distributor (21) and the rotation of the agitator (17).

Abstract

一种装配扇环型凹面叶片的气液分散搅拌器装置（20），搅拌器装置（20）由搅拌叶轮、搅拌轴（18）和动力装置（19）三部分组成，搅拌叶轮包括圆盘（15）、轮毂（16）和数个径向伸展的凹面叶片（14）。每个叶片（14）是由径向伸展且类似扇环形状的凹面组成，叶片（14）上下两部分在水平面上的投影是两个弧度不同的扇环，上部投影所得扇环弧度大于下部。

Description

一种装配扇环型凹面叶片的气液分散搅拌器装置 技术领域
本发明涉及一种装配扇环型凹面叶片的气液分散搅拌器装置，属于生物工程、化学工程和环境工程装备领域。
背景技术
气液两相混合广泛应用于通风发酵、氧化反应、氢化反应、生物曝气等过程单元。化工工程师期望能发明一种能实现高效气液分散的装置。目前能实现气液两相分散的装置主要有：(1)鼓泡塔反应器；(2)气升式反应器；(3)带气液分散搅拌器的搅拌装置；(4)基于旋转喷嘴的混合系统。
径向流搅拌器是一类特别适合气液分散功能的搅拌器，包含轮毂、圆盘和多个均匀分布在圆盘上的叶片，它的圆盘能收集到搅拌器下方的气泡并导入至高剪切的叶片区域，从而产生良好的气液分散效果。1950年Rushton首先发明了Rushton搅拌器，在青霉素发酵等领域得到创新性的应用，开创了气液分散型搅拌器的先河。但人们逐渐发现它存在着一些缺点：(1)通气条件下的搅拌功率比不通气条件下的功率值下降约50％以上，这意味着较高的能量耗散和较低的气液传质效率；(2)在较低通气强度时就易发生气泛现象，导致气液分散能力受到削弱。以上两个缺点都是由于Rushton搅拌器在运行过程中，其桨叶背后易产生高速、低压的尾涡，从而导致流体边界层的分离。在气液分散过程中，尾涡的低压核心吸引气泡聚并并在桨叶背后形成气穴，而这些气穴正是导致能量耗散和效率低下的主要原因。
在经典Rushton搅拌器的基础上，许多工程师对搅拌器叶片的形状、尺寸和细节结构做了许多调整和优化，开发了箭叶搅拌器、CD-6搅拌器(Smith搅拌器)、凹面搅拌器等，提高了搅拌器的气液分散效率。以上这些搅拌器的叶片都是上下对称的，直到1998年Bakker发明了不对称凹面桨——BT-6搅拌器，其上叶片前缘切向伸展并超出下叶片前缘，这样叶片就能捕获更多的气泡，而其更加深陷的凹面能显著减少叶片背后的气穴形成，从而提高气液分散效率和气泛点，使搅拌器的气液分散效率得到显著提升。
径向流搅拌器的功率消耗既与搅拌转速、通气量、流体物性等条件有关，也与搅拌器的结构和安装条件有关。由于气穴现象的提出，使得径向流搅拌器的设计思路都往更凹陷的曲面发展。但有一个严重的问题是，在不增加叶片宽度的条件下采用更凹陷的叶片虽然能降低功耗，但径向排量性能也会大大降低。增加叶片宽度有利于改善其径向排量性能，但其外边缘顶点的直径远大于尾点的直径，使叶片在外边缘顶点区域产生极大的力矩和功率消耗，而对径向排量的贡献却很小。
发明内容
为解决上述问题，本发明采用了一种特殊的类似于扇环形状的凹面叶片结构，将桨叶设计在水平面上投影为扇环的形状。这样设计的叶片使传统桨叶宽度的增加变为本发明中桨叶弧长的增加，外边缘顶点的直径与尾点的直径相等，避免了桨叶外围产生多余的伸出部分，有效的改善了搅拌器的分散和混合性能。本发明采用桨叶的径向轮廓线是由凹形平面曲线沿圆柱面弯曲而得到的空间曲线，有利于气液两相在径向排出过程中实现高效分散。本发明的搅拌装置具有较低的功率消耗、较高的气液分散和混合性能，也极大的减小了气穴现象的发生，提高了气泛点，即在相同转速下可承受更高的通气量，增强了持气性能。
本发明提供了一种用于反应器中气液分散和混合的搅拌器装置；所述装置包含了搅拌叶轮、搅拌轴和动力装置三部分；搅拌叶轮包含若干个径向伸展的凹面叶片；凹面叶片的上、下部分在水平面上的投影形状为扇环，叶片的上面部分投影得到的扇环的弧度比下面部分得到的扇环的弧度大。
叶片的径向内侧边缘与径向外侧边缘都在以搅拌轴为中心的圆柱面上，两个圆柱面之间的半径差值为叶片的长度。以不同半径的圆柱面切割叶片，都可得到一条空间曲线，这些空间曲线称为径向轮廓线。径向轮廓线可以视为是由平面曲线沿圆柱面弯曲得到的，该平面曲线视为叶片的基本形状线。因此叶片的径向轮廓线在以搅拌轴为中心的圆柱面上。
叶片的基本形状线包括两个顶点和一个尾点。以圆盘平面为界，尾点和上顶点之间的部分为上部形状线，尾点和下顶点之间的部分为下部形状线，尾点在水平面上。这样就构成了上下分叉的、夹角为锐角的基本形状线。该基本形状线被弯曲成轮廓线后，轮廓线中的顶点、尾点等结构特征都是与基本形状线中的点相对应。
轮廓线上、下部分投影到水平面上得到两段圆弧。上部分轮廓线投影得到的弧长大于下部分，即上部分轮廓线投影得到的弧度大于下部分得到的弧度。
以叶片径向最内侧轮廓线为基线，径向延伸一定长度即可得到叶片。在径向延伸过程中，各轮廓线上、下部分投影到水平面得到的弧的弧度保持不变，而弧长逐渐增大。轮廓线上、下顶点之间的轴向高度称为开口高度，开口高度在径向延伸过程中也保持不变。各轮廓线上顶点的连线构成了叶片的上导边，下顶点的连线构成了叶片的下导边，尾点的连线构成了叶片的尾边。叶片上导边、下导边及尾边都通过搅拌轴的中心线，它们在水平面上的投影线相交于一点，即圆盘的中心点。
由于轮廓线的上部弧长大于下部弧长，因此径向延伸得到叶片后，叶片上部比下部多出一块扇环形状的突出部分。该突出部分的作用是利于捕获上升的气泡，增强搅拌器的持气能力。
如上所述，该搅拌装置的叶片是一种类似于扇环的形状，叶片在水平面上的投影为扇环形状。这种叶片改变了以往径向流叶片只沿尾边所在半径方向平行伸展的方式，而是叶片的每一部分都是沿各自所在半径方向扩张伸展的，从而形成了上述类似扇环的形状。将叶片设计成上述形状，使叶片的轮廓线在叶轮旋转方向上，可以使叶片的每一部分都正对来流，从而将其径向排出，提高了叶片的利用效率。叶片上部较下部更多突出的部分有利于捕获上升的气泡，增强持气性能，从而使气泡易于被径向排出，分散在液体里面。
在一种实施方式中，所述搅拌叶轮还包含圆盘、轮毂，凹面叶片安装在圆盘上；凹面叶片以圆盘平面为界分为上、下两部分。
在一种实施方式中，每个叶片都具有一定厚度，其形状与迎液面相同。
在一种实施方式中，叶片的径向内侧边缘与径向外侧边缘都在以搅拌轴为中心的圆柱面上，两个圆柱面之间的半径差值为叶片的长度。
在一种实施方式中，在叶片任一径向位置的轮廓线上，下部一点到水平面的距离与上部对应点到圆盘平面的距离相等。这样保证了叶片上、下伸展的统一，以使搅拌过程中的流场相对稳定。但叶片上部比下部更多突出的部分在叶片下部找不到对应的点。因此产生了部分方向向下的轴向流动，增强了叶轮底部的循环。
在一种实施方式中，叶片迎液面上面部分在圆盘平面投影得到的扇环弧度β的值一般在0.52～2.09之间。
在一种实施方式中，叶片迎液面下面部分和上面部分分别在圆盘平面投影所得扇环弧度α和β的比值一般在0.45～0.85之间。
在一种实施方式中，所述搅拌叶轮还包括一个轮毂，连接圆盘和搅拌轴。
在一种实施方式中，所述搅拌叶轮还包括一个水平的圆盘并且围绕圆盘安装了多个径向伸展类似于扇环的凹面叶片；叶片的不对称的上、下两部分在圆盘平面处相连。
在一种实施方式中，所述圆盘的厚度不超过其半径，所述的叶片均匀分布于该圆盘周围。
在一种实施方式中，圆盘直径与搅拌器直径之比在0.5～0.8之间。
在一种实施方式中，迎液面的轴向高度与搅拌器直径的比值在0.1～0.35之间。
在一种实施方式中，迎液面长度与搅拌器直径的比值在0.15～0.4之间。
在一种实施方式中，搅拌叶轮的叶片个数在3～10个之间。
在一种实施方式中，叶片迎液面上下导边及尾边在水平面上投影的延长线相交于一点，该点为圆盘中心点。
在一种实施方式中，叶片轮廓线投影在水平面上圆弧的弧度在径向延伸的过程中保持不变。
在一种实施方式中，叶片迎液面的轮廓线为空间曲线，可由椭圆弧线、圆弧线、抛物线或其他类似形状的平面曲线沿圆柱面弯曲得到。平面曲线的形状一般为抛物线。
在一种实施方式中，所述搅拌器装置一般用不锈钢制造，也可用碳钢、高强度塑料等其他材料制造。
在一种实施方式中，轮毂和圆盘可以是可拆对开式的，也可以是闭式的，可根据不同工况进行选择。
在一种实施方式中，轮毂与搅拌轴的连接方式为紧固螺钉，或并紧螺栓，或平键来连接。
在一种实施方式中，所述的搅拌装置，一般用于带有椭圆封头或碟形封头的圆柱形反应器内，安装在其中心轴线上。
在一种实施方式中，搅拌器直径与反应器内径之比在0.25～0.6之间。
在一种实施方式中，所述的搅拌器安装在反应器的底部，可单独使用，也可与其他搅拌器组合使用。
在一种实施方式中，所述的搅拌器下需安装气体分布器，气体分布器的通气方向可以是向上也可以是向下。
在一种实施方式中，所述的搅拌器在水平方向旋转，旋转方向为使叶片凹面正对来流的方向。
本发明装置中的搅拌轴用于连接搅拌叶轮和动力装置，带动搅拌叶轮旋转以捕获上升的气泡并将其分散。搅拌叶轮通过轮毂加固与搅拌轴的连接。
本发明的有益效果：
(1)本发明的搅拌装置的叶片是一种类似于扇环的空间形状，叶片在水平面上的投影为扇环形状。这种叶片改变了以往径向流叶片只沿尾边所在半径方向伸展的方式，而是叶片的每一部分都是沿各自所在半径方向伸展的，从而形成了上述类似扇环的形状。将叶片设计成上述形状，使叶片的任一径向轮廓线都在叶轮旋转方向上，可以使叶片的每一部分都正对来流，从而将其径向排出，提高了叶片的利用效率。叶片上部较下部产生的突出部分利于捕获上升的气泡，增强了持气性能，从而使气泡易于被径向排出，分散在液体里面。
(2)本发明的装置具有分散效率高、能耗低的特点，叶片背后的气穴更小，气体分散更充分，通气搅拌操作时气泛点更高。本发明高效、节能的气液分散搅拌器装置，可应用于通风搅拌发酵、氢化反应、氧化反应和生物曝气等反应器中，使其具有较低功率消耗、较高的混合性能及持气传质性能，能够高效节能的将气体分散于液体中。
附图说明
图1：搅拌器装置在反应器中的正视图；
图2：搅拌器的立体图；
图3：搅拌器叶片迎液面的立体图；
图4：搅拌器单个叶片迎液面的俯视图；
图5：搅拌器单个叶片迎液面的正视图；
图6：搅拌器的俯视图。
具体实施方式
如图1和图2所示，本发明所涉及的搅拌装置(20)包括一个搅拌器(17)、一根搅拌轴(18)和一套动力装置(19)，其中搅拌器(17)包括一个圆盘(15)、一个轮毂(16)和几个径向伸展的叶片(14)。
叶片(14)是由迎液面(12)向后增加一定的厚度得到的，加厚后得到叶片(14)，并得到背液面(13)。迎液面(12)的技术特征代表了叶片(14)的技术特征。
如图3所示，迎液面(12)是由径向内边缘(10)、径向外边缘(11)、上导边(8)和下导边(9)围成的凹面形状，也是内边缘(10)径向延伸至外边缘(11)形成的类似于扇环的形状。内边缘(10)包括上顶点(3)、下顶点(4)和尾点(1)。外边缘包括上顶点(5)、下顶点(6)和尾点(2)。上顶点(3)径向延伸至上顶点(5)形成上导边(8)，下顶点(4)径向延伸至下顶点(6)形成下导边(9)，尾点(1)径向延伸至尾点(2)形成尾边(7)。
内边缘(10)在尾点(1)所在径向位置的圆柱面上，外边缘(11)在尾点(2)所在径向位置的圆柱面上。尾边上每一径向位置的圆柱面与迎液面(12)相交部分都是和内边缘(10)和外边(11)形状相同的空间曲线，将其统称为迎液面(12)的轮廓线。轮廓线是由其尾点位置处与尾边垂直的平面曲线沿圆柱面弯曲得到的空间曲线。平面曲线的形状可以是椭圆弧线、抛物线、圆弧线或其他曲线形状，以抛物线为佳。
如图4和图6所示，迎液面(12)在水平面γ上的投影为扇环形状。水平面γ为圆盘(15)所在的水平面。以水平面γ为界，可将迎液面(12)分为上下两部分。迎液面(12)上、下部分投影在水平面γ上形成两个弧度不同的扇环。
如图4所示，内边缘(10)径向延伸至外边缘(11)的过程中，弧度是不变的。迎液面(12)的上导边(8)、下导边(9)在水平面上投影线及尾边(7)的延长线相交于一点O。点O为圆盘(15)的中心点。
迎液面(12)上面部分在水平面γ上投影得到的扇环弧度(用β表示)大于下面部分在水平面γ上投影得到的扇环弧度(用α表示)，以使迎液面(12)上部产生比下部多出的突出部分，从而有利于捕获上升的气泡(23)以加强气液分散。迎液面(12)上面部分在水平面投影得 到的扇环弧度β的值一般在0.52～2.09(对应圆心角为30°～120°)之间，以1.25(对应圆心角为72°)为最佳。迎液面下面部分投影所得圆环弧度α与上面部分投影所得弧度β的比值一般在0.45～0.85之间，以0.75(对应圆心角为43°)为最佳。
如图5所示，迎液面(12)内侧边缘(10)的高度和外侧边缘(11)的高度是一致的。迎液面(12)内侧边缘(10)的高度是指其上顶点(3)和下顶点(4)之间的轴向高度；外侧边缘(11)的高度是指其上顶点(5)和下顶点(6)之间的轴向高度。同理，迎液面(12)任意径向位置处轮廓线的高度都是指其上下顶点之间的轴向高度。迎液面(12)任意径向位置处轮廓线的轴向高度都是相同的，这个轴向高度即是迎液面(12)的高度(用h表示)。
以上所述为迎液面(12)的形状和尺寸特征，它代表了叶片(14)的形状和尺寸特征。叶片(14)为迎液面(12)向凹面外侧加厚得到。
如图1、图2和图6所示，搅拌器(17)有六个叶片(14)安装在圆盘(15)上。叶片的数量可以是3～10个，6个更好。叶片(14)被均布于圆盘(15)周围，尾边(7)与圆盘(15)固定在一起，即叶片(14)被部分嵌入圆盘(15)中以保证其机械强度。圆盘(15)的直径(用d3表示)与搅拌器(17)直径(用D表示)的比值最好在0.5～0.8之间，0.68更佳。
迎液面(12)的轴向高度与搅拌器(17)直径D的比值最好在.0.1～0.35之间，0.2最佳。
如图2、图6所示，迎液面(12)的长度(用L表示)与搅拌器(17)直径D的比值最好在0.15～0.4之间，0.3最好。
圆盘(15)可以是其他形状，如中间镂空的条带状等。圆盘(15)的厚度要小于其半径。
搅拌器(17)通过轮毂(16)与搅拌轴(18)连接，并且轮毂(16)可以使搅拌器(17)与搅拌轴(18)连接的非常牢固。
如图6所示，轮毂(16)要在叶片(14)内侧范围之内，搅拌轴(18)的直径(用d1表示)小于轮毂(16)的直径(用d2表示)。搅拌轴(18)和轮毂(16)的直径要在保证其足够机械强度的情况下尽量小一点，以不影响搅拌器(17)的性能和整体流场。
轮毂(16)和圆盘(15)既可以是可拆对开式的，也可以是闭式的，可根据不同工况进行选择。
动力装置(19)包括电机和减速机(未详细画出)，能使搅拌器(17)获得旋转的动力。搅拌器(17)最好在水平方向上旋转，以保持其平衡。
如图1所示，搅拌器(17)被用于装有一定量流体(25)的反应器(26)中，流体(25)可以是一种液体、几种液体的混合物或颗粒悬浮物等，反应器(26)的形状可以是长方体、圆柱体等，以带有椭圆封头的圆柱体容器为佳。反应器(26)中一般加入挡板(22)，以防止 或减小旋转时产生漩涡。
搅拌器(17)直径D与反应器(26)直径(用T表示，图中未画出)比最好在0.25～0.6之间，0.4更佳。
搅拌器(17)最好安装在反应器(26)的底部附近，可以单独使用，也可以与其他径向流或轴向流搅拌器组成搅拌系统组合使用。轮毂(16)与搅拌轴(18)的连接方式为紧固螺钉，或并紧螺栓，或平键来连接，使搅拌器(17)随着搅拌轴(18)一起旋转。使用时反应器(26)内的流体(25)需浸没搅拌器(17)，即液面(24)高于搅拌器(17)。
搅拌器(17)的下面需安装气体分布器(21)，气体分布器(21)的作用是向流体(25)中通入气泡(23)。
如图1所示，气体分布器(21)是一个通气环。气体分布器(21)还可以是一根或者几根通气管、金属烧结网或其他类型，气体分布器(24)的通气方向可以是向上，也可以是向下。其中以通气方向向上的通气环较为常用。
搅拌装置(20)的材料为不锈钢，也可以是其他强度高且耐腐蚀的材料，如碳钢和高强度塑料等。
搅拌装置(20)的具体操作如下：气体分布器(21)向反应器(26)内流体(25)中鼓入气泡(23)，气泡(23)因其密度低而上升，动力装置(19)提供动力使搅拌轴(18)和搅拌器(17)以一定转速在水平方向上旋转，旋转的叶片(14)捕获上升的气泡(23)，使其与周围的流体(25)一起沿径向运动，在运动过程中通过剪切作用使气泡(23)发生破碎从而分散在流体(25)中。在搅拌器(17)的上面和下面形成两个循环流型，通过气体分布器(21)中气泡(23)的释放和搅拌器(17)的旋转达到气液分散和混合的目的。
上述装置形式为本发明优选实例，但本发明的形式并不仅限于此，允许在一定范围内做出修改。
虽然本发明已以较佳实施例公开如上，但其并非用以限定本发明，任何熟悉此技术的人，在不脱离本发明的精神和范围内，都可做各种的改动与修饰，因此本发明的保护范围应该以权利要求书所界定的为准。

Claims (27)

  1. 一种搅拌装置，包括搅拌叶轮、搅拌轴和动力装置；其特征在于，所述搅拌叶轮包含若干个径向伸展的凹面叶片；凹面叶片的上下部分在水平面上的投影形状为扇环，叶片的径向轮廓线、径向内侧边缘与径向外侧边缘都在以搅拌轴为中心的圆柱面上，叶片的上面部分投影得到扇环的弧度比下面部分得到扇环的弧度大。
  2. 根据权利要求1所述的搅拌装置，其特征在于，所述搅拌叶轮还包含圆盘、轮毂，凹面叶片安装在圆盘上；凹面叶片以圆盘平面为界分为上、下两部分；在叶片任一径向位置的轮廓线上，下面部分一点到圆盘平面的距离与上面部分对应点到圆盘平面的距离相等。
  3. 根据权利要求1或2所述的搅拌装置，其特征在于，所述轮廓线可以是抛物线、椭圆弧线、双曲线或圆弧线等类似曲线沿圆柱面弯曲而得到的空间曲线。
  4. 根据权利要求1所述的搅拌装置，其特征在于，叶片迎液面上面部分在圆盘平面投影得到的扇环弧度β的值在0.52～2.09之间。
  5. 根据权利要求1所述的搅拌装置，其特征在于，叶片迎液面下面部分和上面部分分别在圆盘平面投影所得扇环弧度α和β的比值一般在0.45～0.85之间。
  6. 根据权利要求1所述的搅拌装置，其特征在于，迎液面长度与搅拌器直径的比值在0.15～0.4之间。
  7. 根据权利要求1所述的搅拌装置，其特征在于，圆盘直径与搅拌器直径之比在0.5～0.8之间。
  8. 根据权利要求1所述的搅拌装置，其特征在于，叶片轮廓线投影在水平面上圆弧的弧度在径向延伸的过程中保持不变。
  9. 根据权利要求1所述的搅拌装置，其特征在于，叶片迎液面上下导边及尾边在水平面上投影的延长线相交于一点，该点为圆盘中心点。
  10. 根据权利要求1所述的搅拌装置，其特征在于，所述叶片的每一个都具有一定厚度，其形状与迎液面相同。
  11. 根据权利要求1所述的搅拌装置，其特征在于，所述叶片的径向内侧边缘与径向外侧边缘都在以搅拌轴为中心的圆柱面上，两个圆柱面之间的半径差值为叶片的长度。
  12. 根据权利要求2所述的搅拌装置，其特征在于，所述轮毂连接圆盘和搅拌轴。
  13. 根据权利要求2所述的搅拌装置，其特征在于，所述叶片的上、下两部分在圆盘平面处相连。
  14. 根据权利要求2所述的搅拌装置，其特征在于，所述圆盘的厚度不超过其半径，所述 叶片均匀分布于圆盘周围。
  15. 根据权利要求4所述的搅拌装置，其特征在于，迎液面的轴向高度与搅拌装置直径的比值在0.1～0.35之间。
  16. 根据权利要求1所述的搅拌装置，其特征在于，所述搅拌叶轮的叶片个数在3～10个之间。
  17. 根据权利要求2所述的搅拌装置，其特征在于，所述叶片的迎液面上下导边及尾边在水平面上投影的延长线相交于一点，该点为圆盘中心点。
  18. 根据权利要求1所述的搅拌装置，其特征在于，所述叶片的轮廓线投影在水平面上圆弧的弧度在径向延伸的过程中保持不变。
  19. 根据权利要求1所述的搅拌装置，其特征在于，所述搅拌装置一般用不锈钢制造，也可用碳钢、高强度塑料等其他材料制造。
  20. 根据权利要求2所述的搅拌装置，其特征在于，所述轮毂和圆盘可以是可拆对开式的，也可以是闭式的，可根据不同工况进行选择。
  21. 根据权利要求12所述的搅拌装置，其特征在于，所述轮毂与搅拌轴的连接方式为紧固螺钉，或并紧螺栓，或平键来连接。
  22. 根据权利要求1所述的搅拌装置，其特征在于，所述的搅拌装置，一般用于带有椭圆封头或碟形封头的圆柱形反应器内，安装在其中心轴线上。
  23. 根据权利要求22所述的搅拌装置，其特征在于，所述搅拌装置的直径与反应器的内径之比在0.25～0.6之间。
  24. 根据权利要求22所述的搅拌装置，其特征在于，所述的搅拌装置安装在反应器的底部，可单独使用，也可与其他搅拌装置组合使用。
  25. 根据权利要求22所述的搅拌装置，其特征在于，所述的搅拌装置下需安装气体分布器，气体分布器的通气方向可以是向上也可以是向下。
  26. 根据权利要求1所述的搅拌装置，其特征在于，所述的搅拌装置在水平方向旋转，旋转方向为使叶片凹面正对来流的方向。
  27. 含有权利要求1-26任一所述搅拌装置的设备。
PCT/CN2016/082483 2016-04-27 2016-05-18 一种装配扇环型凹面叶片的气液分散搅拌器装置 WO2017185431A1 (zh)

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Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106434301A (zh) * 2016-12-07 2017-02-22 广西大学 一种沼气池搅拌装置
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CN107254389A (zh) * 2017-08-14 2017-10-17 合肥明英富海生物科技有限公司 一种发酵装置的螺旋刀
CN107254388A (zh) * 2017-08-14 2017-10-17 合肥明英富海生物科技有限公司 发酵装置
CN108014711B (zh) * 2017-12-07 2024-02-09 中国恩菲工程技术有限公司 气液机械耦合搅拌装置
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CN108640181A (zh) * 2018-06-22 2018-10-12 山东瑞清环境科技发展有限公司 一种污水处理用高速搅拌专用叶轮
CN108748760A (zh) * 2018-06-29 2018-11-06 德清意欣塑料制品有限公司 搅拌效果好的破碎塑料搅拌装置
EP3659700B1 (en) * 2018-11-29 2022-04-20 Alfa Laval Corporate AB Magnetically-coupled liquid mixer
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CN110141984B (zh) * 2019-05-31 2021-05-18 福州大学 一种新型车漆搅拌桨
DE102020127989A1 (de) 2020-10-23 2022-04-28 Uutechnic Oy Begasungsturbine
CN113457502B (zh) * 2021-07-05 2022-08-02 广西大学 一种搅拌装置及其搅拌器
CN113731219B (zh) * 2021-09-06 2022-05-10 中国科学院过程工程研究所 一种后掠式圆盘涡轮搅拌桨
CN113813811B (zh) * 2021-10-09 2022-09-27 中国石油大学(华东) 一种平、折页型搅拌桨、用于高粘度物料发酵的搅拌桨系统及方法
CN113813812B (zh) * 2021-10-09 2022-09-30 中国石油大学(华东) 一种新型搅拌桨及适用于高粘度物料发酵的搅拌桨系统和发酵方法
CN114632444B (zh) * 2022-02-14 2023-02-21 江南大学 一种具有自吸和气液分散功能的搅拌器

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5759625A (en) * 1980-09-29 1982-04-10 Yoichi Nagase Stirring blade
US5316443A (en) * 1991-10-04 1994-05-31 Chemineer, Inc. Reversible mixing impeller
US5791780A (en) * 1997-04-30 1998-08-11 Chemineer, Inc. Impeller assembly with asymmetric concave blades
CN2481403Y (zh) * 2001-06-15 2002-03-13 温州市江南减速机厂 气液混合搅拌器
CN2813083Y (zh) * 2005-03-25 2006-09-06 浙江长城减速机有限公司 一种气液混合搅拌器
CN2902438Y (zh) * 2006-03-01 2007-05-23 浙江长城减速机有限公司 气液分散搅拌器
CN101306333A (zh) * 2007-02-16 2008-11-19 Spx公司 抛物线径向流推动器
CN101480587A (zh) * 2008-12-31 2009-07-15 江南大学 一种针对高粘度发酵过程的气液分散型搅拌桨

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE461444B (sv) * 1985-11-21 1990-02-19 Boerje Skaanberg Impellerapparat foer omroerning av vaetska under dispergering av gas daeri
US5198156A (en) * 1986-02-17 1993-03-30 Imperial Chemical Industries Plc Agitators
DE29621683U1 (de) * 1996-12-13 1997-02-13 Ekato Ruehr Mischtechnik Rührorgan
US6190033B1 (en) * 1999-04-09 2001-02-20 Pfaulder, Inc. High gas dispersion efficiency glass coated impeller
KR20100126276A (ko) * 2007-12-21 2010-12-01 필라델피아 믹싱 솔루션스, 엘티디. 기체 포일 임펠러

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5759625A (en) * 1980-09-29 1982-04-10 Yoichi Nagase Stirring blade
US5316443A (en) * 1991-10-04 1994-05-31 Chemineer, Inc. Reversible mixing impeller
US5791780A (en) * 1997-04-30 1998-08-11 Chemineer, Inc. Impeller assembly with asymmetric concave blades
CN2481403Y (zh) * 2001-06-15 2002-03-13 温州市江南减速机厂 气液混合搅拌器
CN2813083Y (zh) * 2005-03-25 2006-09-06 浙江长城减速机有限公司 一种气液混合搅拌器
CN2902438Y (zh) * 2006-03-01 2007-05-23 浙江长城减速机有限公司 气液分散搅拌器
CN101306333A (zh) * 2007-02-16 2008-11-19 Spx公司 抛物线径向流推动器
CN101480587A (zh) * 2008-12-31 2009-07-15 江南大学 一种针对高粘度发酵过程的气液分散型搅拌桨

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