JPH0975699A - Agitator - Google Patents
AgitatorInfo
- Publication number
- JPH0975699A JPH0975699A JP7233068A JP23306895A JPH0975699A JP H0975699 A JPH0975699 A JP H0975699A JP 7233068 A JP7233068 A JP 7233068A JP 23306895 A JP23306895 A JP 23306895A JP H0975699 A JPH0975699 A JP H0975699A
- Authority
- JP
- Japan
- Prior art keywords
- blade
- stirring
- tank
- liquid
- upper blade
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】この発明は撹拌装置、特に低
粘度から高粘度までの広い粘度域の流体を速やかにかつ
均一に撹拌混合できる撹拌装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a stirrer, and more particularly to a stirrer capable of rapidly and uniformly stirring and mixing a fluid having a wide viscosity range from low viscosity to high viscosity.
【０００２】[0002]
【従来の技術】撹拌槽と、撹拌槽内に回転可能に支持さ
れた回転軸と、撹拌槽内で回転可能に回転軸に固定され
た撹拌翼とを備えた撹拌装置は従来から化学工業の分野
において広く使用されている。2. Description of the Related Art A stirrer equipped with a stirring tank, a rotating shaft rotatably supported in the stirring tank, and a stirring blade fixed to the rotating shaft so as to be rotatable in the stirring tank has been conventionally used in the chemical industry. Widely used in the field.
【０００３】例えば、特開平５−４９８９０号公報に
は、竪型円筒状の撹拌槽内中心部に回転軸を垂設し、こ
の回転軸に複数のパドル翼を上下多段に装着すると共
に、最下段のパドル翼を撹拌槽の底面に近接させて配置
し、かつ上段に位置する各パドル翼を上下で近接する下
段のパドル翼に対して９０度未満の交差角度で回転方向
に先行させて配置した撹拌装置が開示されている。この
撹拌装置では、上下段のパドル翼を９０度未満の交差角
度で配置することにより、撹拌槽全体に及ぶ１つの大き
な循環流が形成されるので、遷移流から層流域に至る撹
拌操作条件下における流体の撹拌効率を大幅に向上する
ことができる利点を有する。また、特公平１−３７１７
３号公報には、撹拌槽内中心部に槽外から回転可能な撹
拌軸を配設し、撹拌槽の底壁面に下端部を摺接させて槽
底部に配置されるボトムパドルを撹拌軸に装着し、アー
ム部分及びアーム部分と直角方向に延びるストリップか
ら構成される格子翼を撹拌軸のボトムパドルより上位部
分に装着すると共に、撹拌槽の側壁面に下部から上部ま
で軸方向に沿う複数本の邪魔板を間隔をおき配設した撹
拌機が開示されている。この撹拌機では、ボトムパドル
により槽底部の液体が半径方向に吐出されて槽側壁面に
衝突し、邪魔板により槽内の液体が円運動を抑制されて
槽上部へ上昇させられ、格子翼のアーム部分とストリッ
プにより槽内を下降中の液体が剪断細分化されると共に
この細分化された液体がアーム部分とストリップの後側
に発生する微細渦に巻込まれて混合される。したがっ
て、細分化された液体をそれぞれ混合することにより撹
拌槽内全体の液体を混合できるので、撹拌所要動力が小
さくて済むと共に低速回転撹拌時（低所要動力時）の混
合性能を向上させることができる利点を有する。また、
特開平６−１９８１５５号公報には、上下方向に配置さ
れた回転する撹拌軸を撹拌槽内に設置し、撹拌軸の軸心
に対して平行に配置された垂直平板翼及び垂直平板翼と
反対方位に配置され下降流を発生するように撹拌軸の軸
心に対して傾斜角を持つ複数の傾斜平板翼よりなる翼群
の複数個を上下方向に配置して撹拌軸に取付け、隣接す
る前記翼群の垂直平板翼と傾斜平板翼との方位を互いに
ずらせた撹拌装置が開示されている。この撹拌装置で
は、垂直平板翼により撹拌槽内壁面付近の被処理物に上
昇流を生じさせ、傾斜平板翼により撹拌槽内中心部付近
の被処理物に下降流を生じさせることによって、撹拌槽
内全域に亘る流動が形成されるので、２種類以上の異な
る粘度の液体を迅速でかつ効率良く混合させることがで
きる利点を有する。For example, in Japanese Unexamined Patent Publication (Kokai) No. 5-49890, a rotary shaft is vertically provided at the center of a vertical cylindrical stirring tank, and a plurality of paddle blades are mounted on the rotary shaft in a vertical multistage manner. The lower paddle blades are arranged close to the bottom of the stirring tank, and the upper paddle blades are arranged in the direction of rotation at an intersection angle of less than 90 degrees with respect to the vertically adjacent lower paddle blades. Disclosed is a stirring device. In this stirring device, by arranging the upper and lower paddle blades at a crossing angle of less than 90 degrees, one large circulation flow is formed over the entire stirring tank, so that the stirring operation conditions from the transition flow to the laminar flow region are satisfied. This has the advantage that the stirring efficiency of the fluid in step 1 can be greatly improved. In addition, Japanese Patent Publication No. 1-3717
In Japanese Patent Publication No. 3, a stirring shaft rotatable from outside the tank is arranged in the center of the stirring tank, and a bottom paddle arranged at the bottom of the tank is slidably in contact with the bottom wall surface of the stirring tank. Attach a grid blade consisting of an arm part and a strip extending in the direction perpendicular to the arm part to the upper part of the stirring shaft above the bottom paddle, and on the side wall of the stirring tank, from the bottom to the top, along the axial direction. Disclosed is a stirrer in which baffle plates are arranged at intervals. In this stirrer, the liquid at the bottom of the tank is discharged in the radial direction by the bottom paddle and collides with the side wall surface of the tank.The baffle plate suppresses the circular motion of the liquid in the tank and raises it to the upper part of the tank. The liquid descending in the tank is shear-divided by the arm portions and the strips, and the subdivided liquids are wound and mixed in a fine vortex generated on the rear side of the arm portions and the strips. Therefore, since the liquids in the entire stirring tank can be mixed by mixing the liquids that have been subdivided, it is possible to reduce the required power for stirring and to improve the mixing performance during low-speed rotation stirring (when the required power is low). It has the advantage that Also,
In Japanese Patent Laid-Open No. 6-198155, a rotating stirring shaft arranged vertically is installed in a stirring tank, and a vertical flat plate blade arranged parallel to the axis of the stirring shaft and a vertical flat plate blade are opposed. A plurality of blade groups composed of a plurality of inclined flat plate blades that are arranged in the azimuth direction and have an inclination angle with respect to the axial center of the stirring shaft so as to generate a downward flow, are attached to the stirring shaft, and are adjacent to each other. A stirring device is disclosed in which the orientations of the vertical flat plate blade and the inclined flat plate blade of the blade group are offset from each other. In this stirring device, a vertical flat plate blade causes an upward flow in the object to be treated near the inner wall of the agitating tank, and an inclined flat plate blade causes a downward flow in the object to be treated near the center of the agitating tank. Since the flow is formed over the entire area, there is an advantage that two or more kinds of liquids having different viscosities can be mixed rapidly and efficiently.
【０００４】また、撹拌槽１と、撹拌槽１内に回転可能
に支持された回転軸２と、撹拌槽１内で回転可能に回転
軸２に固定されかつ回転軸２に対して傾斜して径方向か
つ上下方向に延びる一対の半楕円形状の上部翼３と上部
翼３に接近して配置されかつ撹拌槽１の底面付近まで回
転軸２から下方かつ径方向に延びる下部翼４とを有する
撹拌翼５と、撹拌槽１の内壁と撹拌翼５との間に設けら
れた邪魔板６とを備えた撹拌装置を図１４及び図１５に
示す。図１４及び図１５の撹拌装置では、大きな上下方
向の循環流を半楕円形状の上部翼３により発生させるこ
とができるので、撹拌槽１内の液体を速やかにかつ効率
良く撹拌混合できる利点を有する。低粘度領域の液体の
撹拌混合に使用される撹拌装置の撹拌翼には、例えば図
１６に示すように４枚パドル翼１６aを上下２組設けて
成る４枚ピッチドパドル翼１６が使用され、高粘度領域
の液体の撹拌混合に使用される撹拌装置の撹拌翼には、
例えば図１７に示すように螺旋状のリボン羽根部材１７
aを一対に設けて成るヘリカルリボン翼１７が使用され
る。Further, a stirring tank 1, a rotary shaft 2 rotatably supported in the stirring tank 1, a rotary shaft 2 rotatably fixed in the stirring tank 1 and inclined with respect to the rotary shaft 2. It has a pair of semi-elliptical upper blades 3 extending in the radial direction and the vertical direction, and a lower blade 4 arranged close to the upper blade 3 and extending downward from the rotating shaft 2 in the radial direction to the vicinity of the bottom surface of the stirring tank 1. 14 and 15 show a stirring device including the stirring blade 5 and the baffle plate 6 provided between the inner wall of the stirring tank 1 and the stirring blade 5. Since the stirring device of FIGS. 14 and 15 can generate a large up-and-down circulation flow by the semi-elliptical upper blade 3, it has an advantage that the liquid in the stirring tank 1 can be rapidly and efficiently stirred and mixed. . As the stirring blades of the stirring device used for stirring and mixing the liquid in the low viscosity region, for example, as shown in FIG. 16, a four-piece pitched paddle blade 16 having two sets of four paddle blades 16a provided at the upper and lower sides is used. The stirring blades of the stirring device used for stirring and mixing the liquid in the area
For example, as shown in FIG. 17, a spiral ribbon blade member 17
A helical ribbon blade 17 having a pair of a is used.
【０００５】[0005]
【発明が解決しようとする課題】ところで、従来の撹拌
装置では撹拌槽内の液体が中粘度以上になると上下方向
の循環流が弱くなるため、撹拌槽内の液体の流動が悪化
して撹拌流が上下方向に分割され、撹拌槽内全体の液体
を均一に撹拌混合できない欠点があった。また、図１４
に示す撹拌装置では撹拌槽内の液体の粘度が高くなるに
つれて、図１８に示すように半楕円形状の上部翼３の下
端３aにて径方向外側への液体の流れが生じ、撹拌槽１
内の液体を下部翼４に引き込む流れが弱くなる。図１４
に示す撹拌装置において、撹拌槽１内を粘度７４Ｐの水
飴水溶液で満たしかつその水溶液中に粒子径４.４ｍｍ
のトレーサ粒子（ＰＭＭＡ粒子）を混入させ、撹拌翼３
の回転数を９０ｒｐｍとして運転した場合の撹拌槽１内
のトレーサ粒子の流動軌跡及び到達深度を図１９(Ａ)及
び(Ｂ)にそれぞれ示す。即ち、図１９(Ａ)の太線はトレ
ーサ粒子が最も高頻度に流れる軌跡を示し、図１９(Ｂ)
は液面から槽底部までを深さ方向に１０分割したときの
各々の分割箇所におけるトレーサ粒子の存在する頻度を
百分率で示したものである。図１９(Ａ)及び(Ｂ)から撹
拌槽１内のトレーサ粒子が槽底部まで到達する頻度が低
いことがわかる。このため、撹拌槽１内に発生する循環
流が槽底部まで到達せず、撹拌槽１の底面付近の液体を
十分に撹拌できない欠点があった。By the way, in the conventional stirring device, when the liquid in the stirring tank has a medium viscosity or higher, the circulation flow in the vertical direction becomes weak, so that the flow of the liquid in the stirring tank is deteriorated and the stirring flow is deteriorated. Was vertically divided, and there was a drawback that the entire liquid in the stirring tank could not be stirred and mixed uniformly. In addition, FIG.
In the stirrer shown in FIG. 18, as the viscosity of the liquid in the stirring tank increases, the liquid flows radially outward at the lower end 3a of the semi-elliptical upper blade 3 as shown in FIG.
The flow that draws the liquid inside into the lower blade 4 weakens. FIG.
In the stirrer shown in Fig. 1, the stirring tank 1 is filled with a starch syrup aqueous solution having a viscosity of 74P, and the particle diameter is 4.4 mm in the aqueous solution.
Mix the tracer particles (PMMA particles) of
19 (A) and 19 (B) show the flow path and the reaching depth of the tracer particles in the stirring tank 1 when operated at a rotation speed of 90 rpm. That is, the thick line in FIG. 19 (A) indicates the locus of tracer particles flowing most frequently, and the thick line in FIG. 19 (B).
Shows the frequency of tracer particles present at each of the divided portions when dividing from the liquid surface to the bottom of the tank in the depth direction by 10 in percentage. 19A and 19B that the tracer particles in the stirring tank 1 rarely reach the bottom of the tank. Therefore, the circulating flow generated in the stirring tank 1 does not reach the bottom of the tank, and there is a drawback that the liquid near the bottom of the stirring tank 1 cannot be sufficiently stirred.
【０００６】撹拌装置の混合性能は、例えばヨード−ハ
イポ水溶液等の脱色反応を利用して脱色までに要する時
間で評価することができる。図７の対数グラフのＢ線及
びＣ線は、それぞれ図１６に示す４枚ピッチドパドル翼
１６を備えた撹拌装置及び図１７に示すヘリカルリボン
翼１７を備えた撹拌装置においてヨード−ハイポ水溶液
の撹拌混合による脱色反応を行なった場合のレイノルズ
数Ｒeと無次元混合時間数ＮTMとの関係を示したもので
ある。ここで、レイノルズ数Ｒeはその数が大きいほど
撹拌槽１内の液体の粘度が低いことを示し、無次元混合
時間数ＮTMは撹拌翼の回転数にヨード−ハイポ水溶液の
脱色に要する時間、即ち脱色時間を乗じた値を示す。図
７のＢ線に示すように、図１６に示す４枚ピッチドパド
ル翼１６の場合は、レイノルズ数Ｒeが１００以上の比
較的粘度が低い領域では無次元混合時間数ＮTMが小さく
脱色時間が短いので混合が早いが、Ｒeが１００以下で
は急激に無次元混合時間数ＮTMが増加し混合性能が低下
する。また、図７のＣ線に示すように、図１７に示すヘ
リカルリボン翼１７の場合は、レイノルズ数Ｒeが１０
０以下の比較的粘度が高い領域では無次元混合時間数Ｎ
TMの変化が比較的小さく混合性能が優れるが、Ｒeが１
００以上の低粘度領域では図１６の４枚ピッチドパドル
翼１６に比較して混合性能が低下する。このため、液体
の粘度に応じて図１６の４枚ピッチドパドル翼１６の類
の低粘度翼と図１７に示すヘリカルリボン翼１７の類の
高粘度翼とを使い分けなければならない。したがって、
従来の撹拌装置では、重縮合反応等の液体の粘度が広い
範囲で変化する場合において１種類の撹拌翼で速やかに
かつ効率よく撹拌混合できない欠点があった。The mixing performance of the stirrer can be evaluated by the time required for decolorization by utilizing the decolorization reaction of, for example, an aqueous iodine-hypo solution. B and C lines of the logarithmic graph of FIG. 7 are the stirring and mixing of the iodine-hypo aqueous solution in the stirring device having the four-pitch paddle blade 16 shown in FIG. 16 and the stirring device having the helical ribbon blade 17 shown in FIG. 17, respectively. 2 shows the relationship between the Reynolds number Re and the dimensionless mixing time number N TM when the decolorization reaction is carried out by. Here, the Reynolds number Re indicates that the larger the number is, the lower the viscosity of the liquid in the stirring tank 1, the non-dimensional mixing time number N TM is the rotation speed of the stirring blade, and the time required for decolorizing the iodine-hypoaqueous solution. That is, a value obtained by multiplying the bleaching time is shown. As shown by the line B in FIG. 7, in the case of the four-pitch paddle blade 16 shown in FIG. 16, the dimensionless mixing time number N TM is small and the bleaching time is short in a region where the Reynolds number Re is 100 or more and the viscosity is relatively low. Therefore, mixing is fast, but when Re is 100 or less, the number of non-dimensional mixing times N TM increases rapidly and the mixing performance deteriorates. Further, as shown by the line C in FIG. 7, in the case of the helical ribbon blade 17 shown in FIG. 17, the Reynolds number Re is 10
In the region where the viscosity is 0 or less and the viscosity is relatively high, the dimensionless mixing time N
Change in TM is relatively small and mixing performance is excellent, but Re is 1
In the low viscosity region of 00 or more, the mixing performance is lower than that of the four-pitch paddle blade 16 of FIG. Therefore, a low-viscosity blade such as the four-pitch paddle blade 16 shown in FIG. 16 and a high-viscosity blade such as the helical ribbon blade 17 shown in FIG. 17 must be properly used according to the viscosity of the liquid. Therefore,
The conventional stirring device has a drawback that one kind of stirring blade cannot swiftly and efficiently stir and mix when the viscosity of liquid such as polycondensation reaction changes in a wide range.
【０００７】そこで、この発明では低粘度から高粘度ま
での広い粘度域の流体を速やかにかつ均一に撹拌混合で
きる撹拌装置を提供することを目的とする。Therefore, it is an object of the present invention to provide a stirring device capable of rapidly and uniformly stirring and mixing a fluid having a wide viscosity range from low viscosity to high viscosity.
【０００８】[0008]
【課題を解決するための手段】この発明による撹拌装置
は、撹拌槽と、撹拌槽内に回転可能に支持された回転軸
と、撹拌槽内で回転可能に回転軸に固定された撹拌翼と
を備え、撹拌翼は回転軸に対して傾斜して径方向かつ上
方に延びる第１の上部翼と、第１の上部翼の下方に配置
されかつ回転軸に対して傾斜して径方向かつ下方に延び
る第２の上部翼と、第２の上部翼に接近して配置されか
つ撹拌槽の底面付近まで回転軸から下方かつ径方向に延
びる下部翼とを有し、第１の上部翼及び第２の上部翼は
下部翼と略同一の半径で延出する部分を有しかつ回転軸
方向に所定の間隔で接近して配置され、第１の上部翼の
下辺部及び第２の上部翼の上辺部は互いに軸方向に重複
する部分を有する。図示の実施例では、第１の上部翼は
撹拌槽内の液体を下方に移動させ、第２の上部翼は第１
の上部翼との重複部分に発生する吸引力により撹拌槽内
の液体を槽底部に移動させ、下部翼は撹拌槽内の槽底部
の液体を径方向外側に移動させるので、液体は撹拌槽の
内壁に沿って上方に移動される。第１の上部翼及び第２
の上部翼はそれぞれ回転軸に対して対称に配置された一
対の四半楕円形状の平板から構成され、第１及び第２の
上部翼一対で半楕円形上部翼を形成する。第１の上部翼
の上端及び第２の上部翼の下端間の水平面距離ｄと第１
及び第２の上部翼の回転軸方向の間隔Ｃとの比の範囲は
０.０５≦Ｃ／ｄ≦０.６が望ましく、水平面に対する第
１及び第２の上部翼の傾斜角度θの範囲は３０°≦θ≦
６０°が望ましい。また、撹拌槽の内壁と撹拌翼との間
に邪魔板が設けられている。邪魔板は撹拌翼の径方向端
部に近接して設けられている。更に、第２の上部翼の底
辺部に下部翼の上辺部と軸方向に重複する部分を設けて
もよい。A stirring device according to the present invention comprises a stirring tank, a rotary shaft rotatably supported in the stirring tank, and a stirring blade rotatably fixed to the rotary shaft in the stirring tank. The stirring blade includes a first upper blade that is inclined with respect to the rotation axis and extends radially and upward, and a stirring blade that is disposed below the first upper blade and is inclined with respect to the rotation axis and radially and downward. A second upper blade extending in the direction of the first upper blade and a lower blade that is arranged close to the second upper blade and that extends downward and radially from the rotation axis to near the bottom surface of the stirring tank. The upper blade of 2 has a portion extending with substantially the same radius as the lower blade and is arranged close to each other at a predetermined interval in the direction of the rotation axis, and the lower side portion of the first upper blade and the second upper blade The upper side portion has portions that overlap each other in the axial direction. In the illustrated embodiment, the first upper blade moves the liquid in the stirring tank downward and the second upper blade moves the first upper blade.
The liquid in the stirring tank moves to the bottom of the tank by the suction force generated in the overlapping portion with the upper blade of the, and the lower blade moves the liquid in the bottom of the stirring tank to the outside in the radial direction. Moved up along the inner wall. First upper wing and second
The upper wing is composed of a pair of quasi-elliptical flat plates arranged symmetrically with respect to the rotation axis, and the first and second upper wing pairs form a semi-elliptical upper wing. The horizontal plane distance d between the upper end of the first upper wing and the lower end of the second upper wing and the first
And the ratio of the ratio of the second upper blade to the interval C in the rotation axis direction is preferably 0.05 ≦ C / d ≦ 0.6, and the range of the inclination angle θ of the first and second upper blades with respect to the horizontal plane is 30 ° ≦ θ ≦
60 ° is desirable. Further, a baffle plate is provided between the inner wall of the stirring tank and the stirring blade. The baffle plate is provided close to the radial end of the stirring blade. Further, the bottom portion of the second upper blade may be provided with a portion that axially overlaps with the upper portion of the lower blade.
【０００９】第１及び第２の上部翼と下部翼とからなる
撹拌翼を回転させると、第１の上部翼により撹拌槽内の
液体が下方に移動され、下方に移動された液体が更に第
２の上部翼により槽底部に移動される。このとき、第１
の上部翼と第２の上部翼の下面側に正圧が発生し上面側
に負圧が発生するので、第１の上部翼の下辺部と第２の
上部翼の上辺部との重複部分に吸引力が発生し、第１の
上部翼により下方に移動された撹拌槽内の液体が前記重
複部分を通じて第２の上部翼により槽底部に確実に引き
込まれる。第２の上部翼により槽底部に引き込まれた液
体は下部翼により径方向外側に移動され、更にこの液体
は撹拌槽の内壁に沿って上方に移動される。これによっ
て、撹拌槽内の液体に比較的強力でかつ槽底部まで到達
する大きな循環流が発生するので、低粘度から高粘度ま
での広い粘度域の液体を速やかにかつ効率良く撹拌混合
できる。また、第１の上部翼と第２の上部翼との重複部
分に発生する吸引力により撹拌槽内の液体を槽底部まで
確実に引き込むことができるので、撹拌槽内全体の液体
を速やかにかつ均一に撹拌混合できる。また、第１及び
第２の上部翼をそれぞれ一対の四半楕円形状の平板から
構成して第１及び第２の上部翼一対で一対の半楕円形上
部翼を形成した場合は、翼を径方向一杯まで広く伸ばす
ことができるので、撹拌槽内の液体を隅々まで撹拌でき
る。更に、撹拌槽の内壁と撹拌翼との間に邪魔板を設け
た場合は、撹拌翼の回転方向に沿う液体の流れを阻止し
て上昇流に変え、槽内の循環流を促進することができ
る。When the stirring blade composed of the first and second upper blades and the lower blade is rotated, the liquid in the stirring tank is moved downward by the first upper blade, and the liquid moved downward is further It is moved to the bottom of the tank by the upper blade of 2. At this time, the first
Since positive pressure is generated on the lower surface side of the upper blade and second upper blade and negative pressure is generated on the upper surface side of the upper blade, the lower side of the first upper blade and the upper side of the second upper blade overlap. A suction force is generated, and the liquid in the stirring tank moved downward by the first upper blade is reliably drawn into the tank bottom by the second upper blade through the overlapping portion. The liquid drawn into the bottom of the tank by the second upper blade is moved radially outward by the lower blade, and further this liquid is moved upward along the inner wall of the stirring tank. As a result, a large circulating flow that is relatively strong and reaches the bottom of the tank is generated in the liquid in the stirring tank, so that the liquid in a wide viscosity range from low viscosity to high viscosity can be rapidly and efficiently stirred and mixed. Further, since the liquid in the stirring tank can be reliably drawn to the bottom of the tank by the suction force generated in the overlapping portion of the first upper blade and the second upper blade, the liquid in the entire stirring tank can be swiftly and It can be stirred and mixed uniformly. Also, when the first and second upper blades are each formed of a pair of quarter-elliptical flat plates and the pair of first and second upper blades form a pair of semi-elliptical upper blades, the blades are arranged in the radial direction. Since it can be extended to the full extent, the liquid in the stirring tank can be stirred in every corner. Furthermore, when a baffle plate is provided between the inner wall of the stirring tank and the stirring blade, it is possible to prevent the liquid flow along the rotation direction of the stirring blade and convert it into an upward flow, thereby promoting the circulation flow in the tank. it can.
【００１０】[0010]
【発明の実施の形態】以下、この発明による撹拌装置の
最良の実施の形態を図１〜図１１に基づいて説明する。
但し、これらの図面では図１４〜図１９と実質的に同一
の部分には同一の符号を付し、その説明を省略する。こ
の発明による撹拌装置は、図１に示すように、図１４に
示す撹拌装置における撹拌翼５の代わりに、回転軸２に
対して傾斜して径方向かつ上方に延びる第１の上部翼７
と、第１の上部翼７の下方に配置されかつ回転軸２に対
して傾斜して径方向かつ下方に延びる第２の上部翼８
と、第２の上部翼８に接近して配置されかつ撹拌槽１の
底面付近まで回転軸２から下方かつ径方向に延びる下部
翼９とを有する撹拌翼１０を設けたものである。第１の
上部翼７及び第２の上部翼８は、下部翼９と略同一の半
径で延出する部分を有し、上下方向に間隔Ｃで接近して
配置される。したがって、第１の上部翼７の下辺部７a
及び第２の上部翼８の上辺部８aは互いに軸方向に重複
する部分を有する。第１の上部翼７の上端７b及び第２
の上部翼８の下端８b間の水平面距離ｄと第１及び第２
の上部翼７、８の上下方向の間隔Ｃとの比の範囲は０.
０５≦Ｃ／ｄ≦０.６が望ましく、また水平面に対する
第１及び第２の上部翼７、８の傾斜角度θの範囲は３０
°≦θ≦６０°が望ましい。図１に示す例においては、
Ｃ／ｄ＝０.１３、θ＝４５°である。BEST MODE FOR CARRYING OUT THE INVENTION The best mode for carrying out the stirring apparatus according to the present invention will be described below with reference to FIGS.
However, in these drawings, substantially the same parts as those in FIGS. 14 to 19 are designated by the same reference numerals, and the description thereof will be omitted. As shown in FIG. 1, the stirring device according to the present invention includes, instead of the stirring blade 5 in the stirring device shown in FIG. 14, a first upper blade 7 that is inclined with respect to the rotating shaft 2 and extends radially and upward.
And a second upper blade 8 that is arranged below the first upper blade 7 and that extends in the radial direction and is inclined with respect to the rotating shaft 2 and extends downward.
And a lower blade 9 that is disposed close to the second upper blade 8 and that extends downwardly and radially from the rotary shaft 2 to the vicinity of the bottom surface of the stirring tank 1. The first upper wing 7 and the second upper wing 8 have portions that extend with substantially the same radius as the lower wing 9, and are arranged close to each other at an interval C in the vertical direction. Therefore, the lower side portion 7a of the first upper wing 7 is
Also, the upper side portion 8a of the second upper wing 8 has portions that overlap each other in the axial direction. The upper end 7b of the first upper wing 7 and the second
The horizontal plane distance d between the lower ends 8b of the upper wings 8 and the first and second
The range of the ratio of the upper wing 7 and the upper wing 7 and the vertical spacing C is 0.
05 ≦ C / d ≦ 0.6 is desirable, and the range of the inclination angle θ of the first and second upper wings 7 and 8 with respect to the horizontal plane is 30.
It is desirable that θ ≦ θ ≦ 60 °. In the example shown in FIG.
C / d = 0.13 and θ = 45 °.
【００１１】図２に示すように、第１の上部翼７及び第
２の上部翼８はそれぞれ回転軸２に対して対称に配置さ
れた一対の四半楕円形状の平板１１から構成され、図３
に示すように第１及び第２の上部翼７、８一対で半楕円
形上部翼を形成する。また、図４に示すように、下部翼
９は回転軸２に対して平行に下方へ延出しかつ対称に配
置された一対の平板１２から構成され、下部翼９の一対
の平板１２の両端辺にはそれぞれ回転方向に対する後退
角が４５°の折曲部１２aが形成されている。更に、下
部翼９の一対の平板１２の底辺には撹拌槽１の底皿部と
の接触を避けるための傾斜部１２bが形成されている。
図５に示すように、邪魔板６は撹拌槽１の円周方向に三
箇所設けられ、撹拌翼１０の径方向端部１０aに近接し
ている。その他の構成は図１４に示す撹拌装置と同一で
ある。As shown in FIG. 2, each of the first upper wing 7 and the second upper wing 8 is composed of a pair of quarter-elliptical flat plates 11 symmetrically arranged with respect to the rotation axis 2.
As shown in FIG. 5, a pair of first and second upper wings 7 and 8 form a semi-elliptical upper wing. Further, as shown in FIG. 4, the lower blade 9 is composed of a pair of flat plates 12 extending downward in parallel with the rotating shaft 2 and symmetrically arranged. Each of them has a bent portion 12a having a receding angle of 45 ° with respect to the rotation direction. Further, an inclined portion 12b is formed on the bottom side of the pair of flat plates 12 of the lower blade 9 to avoid contact with the bottom plate portion of the stirring tank 1.
As shown in FIG. 5, the baffle plates 6 are provided at three locations in the circumferential direction of the stirring tank 1 and are close to the radial end 10 a of the stirring blade 10. Other configurations are the same as those of the stirring device shown in FIG.
【００１２】回転軸２を矢印方向に回転させることによ
って第１及び第２の上部翼７、８と下部翼９とが回転
し、第１の上部翼７は撹拌槽１内の液体を下方に移動さ
せ、第２の上部翼８は第１の上部翼７により下方に移動
された液体を更に撹拌槽１の底部に移動させる。このと
き、第１の上部翼７の表面７cにかかる圧力と第２の上
部翼８の背面８cの負圧とにより、第１の上部翼７の下
辺部７aと第２の上部翼８の上辺部８aとの重複部分に吸
引力が発生する。このため、図６に示すように第１の上
部翼７により下方に移動された撹拌槽１内の液体が重複
部分に引き込まれて更に下方へ押し出され、第２の上部
翼８により撹拌槽１の底部に確実に引き込まれる。撹拌
槽１の底部に引き込まれた液体は下部翼９により径方向
外側に移動され、邪魔板６により撹拌翼１０の回転方向
に沿う液体の流れが阻止される。これにより、撹拌槽１
内の液体は撹拌槽１の内壁に沿って上方に移動される。
このとき、第１及び第２の上部翼７、８により液体を下
方へ移動させる量と下部翼９により液体を径方向外側に
移動させる量とが平衡して液体の流れが連続し、また撹
拌翼１０の面積が比較的大きくかつ撹拌翼１０の径方向
端部１０aと邪魔板６との間の間隙が極めて狭いので、
撹拌槽１内の液体に比較的強力でかつ槽底部まで到達す
る大きな循環流が発生する。図１の撹拌装置においてヨ
ード−ハイポ水溶液の撹拌混合による脱色反応を行なっ
た場合のレイノルズ数Ｒeと無次元混合時間数ＮTMとの
関係を図７の対数グラフのＡ線に示す。図７によれば、
図１の撹拌装置の場合（Ａ線）は、図１６に示す４枚ピ
ッチドパドル翼を備えた撹拌装置の場合（Ｂ線）及び図
１７に示すヘリカルリボン翼を備えた撹拌装置の場合
（Ｃ線）に比較して幅広い粘度域に亘り無次元混合時間
数ＮTMが小さいので、脱色時間が短いことがわかる。こ
のため、低粘度から高粘度までの広い粘度域に亘って撹
拌槽１内の液体を速やかにかつ効率良く撹拌混合でき
る。また、第１の上部翼７と第２の上部翼８との重複部
分に発生する吸引力により撹拌槽１内の液体を底部まで
確実に引き込むことができるので、撹拌槽１内全体の液
体を速やかにかつ均一に撹拌混合できる。更に、この例
では第１及び第２の上部翼７、８一対で一対の半楕円形
上部翼を形成するので、翼を径方向一杯まで広く伸ばす
ことができ、邪魔板６とのクリアランスを小さくして槽
内の液体を隅々まで撹拌できる。また、下部翼９の一対
の平板１２の両端辺にそれぞれ折曲部１２aが形成され
ているので、撹拌槽１の底部の液体を径方向外側へ速や
かに移動させることができる。また、下部翼９の一対の
平板１２の底辺に傾斜部１２bが形成されているので、
翼を下方に広く伸ばすことができ、撹拌槽１の底皿部と
のクリアランスを小さくして槽内の液体を隅々まで撹拌
できる。By rotating the rotary shaft 2 in the direction of the arrow, the first and second upper blades 7 and 8 and the lower blade 9 rotate, and the first upper blade 7 moves the liquid in the stirring tank 1 downward. The second upper blade 8 moves the liquid moved downward by the first upper blade 7 to the bottom of the stirring tank 1. At this time, due to the pressure applied to the surface 7c of the first upper blade 7 and the negative pressure on the back surface 8c of the second upper blade 8, the lower side portion 7a of the first upper blade 7 and the upper side of the second upper blade 8 are A suction force is generated in the overlapping portion with the portion 8a. Therefore, as shown in FIG. 6, the liquid in the stirring tank 1 moved downward by the first upper blade 7 is drawn into the overlapping portion and pushed further downward, and the liquid is stirred by the second upper blade 8 by the second upper blade 8. Is reliably pulled into the bottom of the. The liquid drawn into the bottom of the stirring tank 1 is moved radially outward by the lower blade 9, and the baffle plate 6 blocks the flow of the liquid along the rotation direction of the stirring blade 10. As a result, the stirring tank 1
The liquid inside is moved upward along the inner wall of the stirring tank 1.
At this time, the amount by which the liquid is moved downward by the first and second upper blades 7 and 8 and the amount by which the liquid is moved radially outward by the lower blade 9 are in equilibrium, and the liquid flow is continuous, and the stirring is continued. Since the area of the blade 10 is relatively large and the gap between the radial end 10a of the stirring blade 10 and the baffle plate 6 is extremely narrow,
A large circulation flow that is relatively strong and reaches the bottom of the tank is generated in the liquid in the stirring tank 1. The line A of the logarithmic graph in FIG. 7 shows the relationship between the Reynolds number Re and the dimensionless mixing time number N TM when the decolorization reaction is performed by stirring and mixing the aqueous iodine-hypo solution in the stirring apparatus of FIG. According to FIG.
In the case of the stirrer of FIG. 1 (line A), the case of the stirrer with four pitched paddle blades shown in FIG. 16 (line B) and the case of the stirrer with helical ribbon blades shown in FIG. 17 (line C) It can be seen that the bleaching time is short because the dimensionless mixing time number N TM is small over a wide viscosity range as compared with (1). Therefore, the liquid in the stirring tank 1 can be rapidly and efficiently stirred and mixed over a wide viscosity range from low viscosity to high viscosity. Moreover, since the liquid in the stirring tank 1 can be surely drawn to the bottom by the suction force generated in the overlapping portion of the first upper blade 7 and the second upper blade 8, the liquid in the entire stirring tank 1 is Can be stirred and mixed rapidly and uniformly. Further, in this example, since the pair of first and second upper blades 7 and 8 form a pair of semi-elliptical upper blades, the blades can be widely expanded to the radial direction and the clearance with the baffle plate 6 can be reduced. Then, the liquid in the tank can be stirred in every corner. Further, since the bent portions 12a are formed on both end sides of the pair of flat plates 12 of the lower blade 9, the liquid at the bottom of the stirring tank 1 can be rapidly moved to the outside in the radial direction. Further, since the inclined portions 12b are formed on the bottom sides of the pair of flat plates 12 of the lower blade 9,
The blades can be extended widely downward, the clearance with the bottom plate portion of the stirring tank 1 can be reduced, and the liquid in the tank can be stirred in every corner.
【００１３】[0013]
【実施例】図１に示す撹拌装置において、前述の図１４
に示す撹拌装置と同様に撹拌槽１内を粘度７４Ｐの水飴
水溶液で満たしかつその水溶液中に粒子径４.４ｍｍの
トレーサ粒子（ＰＭＭＡ粒子）を混入させ、撹拌翼３の
回転数を９０ｒｐｍとして運転した場合の撹拌槽１内の
トレーサ粒子の流動軌跡及び到達深度を図８(Ａ)及び
(Ｂ)にそれぞれ示す。ここで、図１９(Ａ)及び(Ｂ)と図
８(Ａ)及び(Ｂ)とを比較すると、図１に示す撹拌装置に
おける水溶液中のトレーサ粒子が槽底部まで到達する頻
度が高いので、撹拌槽１内の液体に発生する循環流が槽
底部まで到達し、撹拌槽１内全体の液体を速やかにかつ
均一に撹拌混合できることがわかる。なお、図１に示す
撹拌装置の各部寸法は図９に示すような関係となるよう
に設定されている。EXAMPLE In the stirring device shown in FIG.
The stirring tank 1 is filled with a starch syrup aqueous solution having a viscosity of 74P, and tracer particles (PMMA particles) having a particle diameter of 4.4 mm are mixed in the stirring tank 1 in the same manner as the stirring device shown in FIG. The flow path and the reaching depth of the tracer particles in the stirring tank 1 in the case of
Each is shown in (B). Here, comparing FIGS. 19 (A) and (B) with FIGS. 8 (A) and (B), since the tracer particles in the aqueous solution in the stirring device shown in FIG. 1 reach the bottom of the tank at a high frequency, It can be seen that the circulating flow generated in the liquid in the stirring tank 1 reaches the bottom of the tank, and the liquid in the entire stirring tank 1 can be rapidly and uniformly stirred and mixed. The dimensions of each part of the stirring device shown in FIG. 1 are set so as to have the relationship shown in FIG.
【００１４】［比較例１］図１の撹拌装置において、第
１及び第２の上部翼７、８の傾斜角度θを４５°一定と
しかつＣ／ｄの値を０.０５、０.１３、０.６として撹
拌混合によりヨード−ハイポ水溶液の脱色反応を行なっ
た場合のレイノルズ数Ｒeが９のときの脱色時間を表１
に示す。但し、この比較例では撹拌槽１の容量を１０リ
ットル、撹拌翼１０の回転数を８４ｒｐｍとして比較を
行なった。また、ヨード−ハイポ水溶液は粘度５０Ｐの
水飴水溶液中にヨードが１に対してハイポが１.２の割
合で含有して成る。[Comparative Example 1] In the stirring apparatus of FIG. 1, the inclination angles θ of the first and second upper blades 7 and 8 were kept constant at 45 °, and the C / d values were 0.05, 0.13, The decolorization time when the Reynolds number Re was 9 when the decolorization reaction of the iodine-hypo aqueous solution was carried out by stirring and mixing as 0.6 is shown in Table 1.
Shown in However, in this comparative example, the capacity of the stirring tank 1 was 10 liters, and the rotation speed of the stirring blade 10 was 84 rpm for comparison. The iodine-hypo aqueous solution is a solution of starch syrup having a viscosity of 50 P at a ratio of 1 iodine to 1.2 hypo.
【表１】 表１に示すように、第１の上部翼７の上端７b及び第２
の上部翼８の下端８b間の水平面距離ｄと第１及び第２
の上部翼７、８の上下方向の間隔Ｃとの比Ｃ／ｄの値が
０.１３の場合が最も脱色時間、即ち脱色に要する時間
が短いので、Ｃ／ｄの値が０.１３に近いほど混合の効
率が良いことがわかる。この場合、第１及び第２の上部
翼７、８により水溶液を下方向へ移動させる量と下部翼
９により水溶液を径方向外側に移動させる量とが平衡し
て水溶液の流れが連続し、槽内全体を流れる循環流が形
成されるためと考えられる。Ｃ／ｄの値が０.０５の場
合は、第１及び第２の上部翼７、８の重複部分に吸い込
まれる水溶液の量が減少するので、第２の上部翼８の下
端８b付近にて径方向外側への水溶液の流れが生じる。
このため、槽底部まで水溶液が移動し難くなり、混合の
効率が低下する。したがって、Ｃ／ｄ＝０.１３の場合
に比較してヨード−ハイポ水溶液の脱色時間が長くな
る。また、Ｃ／ｄの値が０.６の場合は、第１及び第２
の上部翼７、８の上下方向の間隔が広くなるので、第１
及び第２の上部翼７、８の重複部分に発生する吸引力が
弱くなり、第１及び第２の上部翼７、８により水溶液を
槽底部に押し下げる力が低下する。このため、槽内に発
生する循環流の流速が遅くなるので、水溶液が槽内を循
環する平均循環時間が長くなり、混合の効率が低下す
る。したがって、この場合においてもＣ／ｄ＝０.１３
の場合に比較してヨード−ハイポ水溶液の脱色時間が長
くなる。よって、上記の比較例１から第１の上部翼７の
上端７b及び第２の上部翼８の下端８b間の水平面距離ｄ
と第１及び第２の上部翼７、８の上下方向の間隔Ｃとの
比Ｃ／ｄの値は、０.０５≦Ｃ／ｄ≦０.６の範囲に設定
するのが望ましく、またＣ／ｄの値は０.１３に設定す
るのが最良であることがわかる。[Table 1] As shown in Table 1, the upper end 7b of the first upper wing 7 and the second
The horizontal plane distance d between the lower ends 8b of the upper wings 8 and the first and second
When the ratio C / d of the upper blades 7 and 8 to the vertical distance C is 0.13, the bleaching time is the shortest, that is, the time required for bleaching is the shortest. It can be seen that the closer the efficiency is, the better the mixing efficiency. In this case, the amount of moving the aqueous solution downward by the first and second upper blades 7 and 8 and the amount of moving the aqueous solution radially outward by the lower blade 9 are in equilibrium so that the flow of the aqueous solution is continuous, It is thought that this is because a circulating flow that flows through the entire interior is formed. When the value of C / d is 0.05, the amount of the aqueous solution sucked into the overlapping portion of the first and second upper blades 7 and 8 is reduced, so that the lower end 8b of the second upper blade 8 is near. A flow of the aqueous solution occurs radially outward.
Therefore, it becomes difficult for the aqueous solution to move to the bottom of the tank, and the efficiency of mixing decreases. Therefore, the decolorization time of the aqueous iodine-hypo solution is longer than that in the case of C / d = 0.13. When the value of C / d is 0.6, the first and second
Since the vertical gap between the upper wings 7 and 8 of the
Also, the suction force generated in the overlapping portion of the second upper blades 7 and 8 becomes weak, and the force of pushing the aqueous solution down to the bottom of the tank by the first and second upper blades 7 and 8 decreases. For this reason, the flow velocity of the circulation flow generated in the tank becomes slow, and the average circulation time for the aqueous solution to circulate in the tank becomes long, so that the mixing efficiency decreases. Therefore, even in this case, C / d = 0.13
The time required for decolorizing the aqueous iodine-hypo solution is longer than that in the above case. Therefore, the horizontal plane distance d between the upper end 7b of the first upper wing 7 and the lower end 8b of the second upper wing 8 from Comparative Example 1 above.
It is desirable that the value of the ratio C / d between the vertical distance C between the first and second upper blades 7 and 8 and C is set in the range of 0.05 ≦ C / d ≦ 0.6. It can be seen that it is best to set the value of / d to 0.13.
【００１５】［比較例２］次に、図１の撹拌装置におい
て、Ｃ／ｄの値を０.１３一定としかつ第１及び第２の
上部翼７、８の傾斜角度θを３０°、４５°、６０°と
して撹拌混合によりヨード−ハイポ水溶液の脱色反応を
行なった場合のレイノルズ数Ｒeが９のときの脱色時間
を表２に示す。但し、この比較例では撹拌槽１の容量を
１０リットル、撹拌翼１０の回転数を８４ｒｐｍとして
比較を行なった。また、ヨード−ハイポ水溶液は粘度５
０Ｐの水飴水溶液中にヨードが１に対してハイポが１.
２の割合で含有して成る。[Comparative Example 2] Next, in the stirrer of FIG. 1, the value of C / d was kept constant at 0.13 and the inclination angles θ of the first and second upper blades 7, 8 were 30 °, 45. Table 2 shows the decolorization time when the Reynolds number Re was 9 when the decolorization reaction of the iodine-hypoaqueous solution was carried out by stirring and mixing at 60 ° and 60 °. However, in this comparative example, the capacity of the stirring tank 1 was 10 liters, and the rotation speed of the stirring blade 10 was 84 rpm for comparison. The iodine-hypo solution has a viscosity of 5
Hypo is 1. for 1 iodine in 0P starch syrup aqueous solution.
It is contained in a ratio of 2.
【表２】 表２に示すように、第１及び第２の上部翼７、８の傾斜
角度θが４５°の場合が最も脱色時間が短いので、傾斜
角度θが４５°に近いほど良好な槽内循環が得られるこ
とがわかる。第１及び第２の上部翼７、８の傾斜角度θ
が３０°の場合は、槽底面から液面までの高さに対して
撹拌翼の高さを充分に高くできないので、液面付近の水
溶液の撹拌が充分に行なわれず、停滞気味になる。ま
た、第１及び第２の上部翼７、８と下部翼９との液体吐
出量のバランスにおいて、第１及び第２の上部翼７、８
の下方向への液体吐出量が下部翼９の上方向への液体吐
出量より少ないため、撹拌槽１内の循環流が上下に分割
され円滑な槽内循環が得られない。したがって、θ＝４
５°の場合に比較してヨード−ハイポ水溶液の脱色時間
が長くなる。また、第１及び第２の上部翼７、８の傾斜
角度θが６０°の場合は、第１及び第２の上部翼７、８
の下方向への液体吐出量に比較して径方向外側への液体
吐出量が増加し、水溶液を槽底部へ押しやる量が減少す
るので、撹拌槽１内の循環流が上下に分割され円滑な槽
内循環が得られない。したがって、この場合においても
θ＝４５°の場合に比較してヨード−ハイポ水溶液の脱
色時間が長くなる。よって、上記の比較例２から水平面
に対する第１及び第２の上部翼７、８の傾斜角度θは３
０°≦θ≦６０°の範囲に設定するのが望ましく、また
θは４５°に設定するのが最良であることがわかる。[Table 2] As shown in Table 2, the decolorization time is the shortest when the inclination angle θ of the first and second upper blades 7 and 8 is 45 °, and thus the closer the inclination angle θ is to 45 °, the better the circulation in the tank. You can see that you can get it. Inclination angle θ of the first and second upper wings 7, 8
When the angle is 30 °, the height of the stirring blade cannot be made sufficiently high with respect to the height from the bottom surface of the tank to the liquid surface, so that the aqueous solution in the vicinity of the liquid surface is not sufficiently stirred and becomes stagnant. In addition, in the balance of the liquid discharge amounts of the first and second upper blades 7 and 8 and the lower blade 9, the first and second upper blades 7 and 8 are
Since the liquid discharge amount in the downward direction is smaller than the liquid discharge amount in the upward direction of the lower blade 9, the circulation flow in the stirring tank 1 is divided into upper and lower parts, and smooth in-tank circulation cannot be obtained. Therefore, θ = 4
The decolorization time of the aqueous iodine-hypo solution is longer than that in the case of 5 °. When the inclination angle θ of the first and second upper wings 7, 8 is 60 °, the first and second upper wings 7, 8 are
The amount of liquid discharged to the outside in the radial direction is increased as compared with the amount of liquid discharged downward, and the amount of the aqueous solution pushed to the bottom of the tank is reduced. Circulation in the tank cannot be obtained. Therefore, also in this case, the decolorization time of the aqueous iodine-hypo solution is longer than that in the case of θ = 45 °. Therefore, from the above Comparative Example 2, the inclination angle θ of the first and second upper wings 7 and 8 with respect to the horizontal plane is 3
It can be seen that it is desirable to set in the range of 0 ° ≦ θ ≦ 60 °, and that θ is best set to 45 °.
【００１６】［比較例３］更に、槽底部近傍に錨型のア
ンカー翼を備えた従来の撹拌装置と図１に示す撹拌装置
とにおいて、ヨードを含む粘度５０Ｐの水飴水溶液にハ
イポを添加して各々撹拌混合により脱色反応を行なった
場合の水溶液の脱色経過を図１０及び図１１にそれぞれ
示す。但し、従来の撹拌装置におけるアンカー翼の回転
数は６６ｒｐｍ、レイノルズ数Ｒeは１１.４であり、図
１の撹拌装置における撹拌翼１０の回転数は９３ｒｐ
ｍ、レイノルズ数Ｒeは８.９である。また、双方の単位
容積当たりの消費動力は共に１.０ｋｗ／ｍ3、水飴水溶
液中のヨードとハイポの含有比は１：１.２である。図
１０及び図１１によれば、３００秒後において従来の撹
拌装置に比較して図１の撹拌装置の方が邪魔板６、第１
及び第２の撹拌翼７、８及び下部翼９等が明確に現われ
ているので、略槽内全体に亘り脱色が完了していること
がわかる。ちなみに図１０には示していないが、従来の
撹拌装置において槽内全体に亘り脱色が完了する時間は
４００秒後である。したがって、図１の撹拌装置では従
来の撹拌装置に比較して撹拌槽１内全体の水溶液を速や
かにかつ均一に撹拌混合できることがわかる。[Comparative Example 3] Further, in the conventional stirring device having anchor-type anchor blades near the bottom of the tank and the stirring device shown in FIG. 1, hypo was added to a starch syrup aqueous solution containing iodine and having a viscosity of 50P. The decolorization process of the aqueous solution when the decolorization reaction was performed by stirring and mixing are shown in FIGS. 10 and 11, respectively. However, the rotation speed of the anchor blade in the conventional stirring device is 66 rpm, the Reynolds number Re is 11.4, and the rotation speed of the stirring blade 10 in the stirring device of FIG. 1 is 93 rp.
m, Reynolds number Re is 8.9. The power consumption of both units per unit volume is both 1.0 kw / m 3 , and the content ratio of iodine and hypo in the starch syrup aqueous solution is 1: 1.2. According to FIG. 10 and FIG. 11, after 300 seconds, the stirring device of FIG.
Since the second stirring blades 7 and 8 and the lower blade 9 and the like are clearly shown, it can be seen that decolorization is completed over substantially the entire tank. By the way, although not shown in FIG. 10, the time required for decolorization over the entire tank in the conventional stirring device is 400 seconds. Therefore, it can be seen that the stirring apparatus of FIG. 1 can swiftly and uniformly stir and mix the entire aqueous solution in the stirring tank 1 as compared with the conventional stirring apparatus.
【００１７】この発明の実施態様は前記の実施の形態に
限定されず、変更が可能である。例えば、上記の実施の
形態では一対の四半楕円形状の平板１１で構成された第
１及び第２の上部翼７、８一対で半楕円形上部翼を形成
した例を示したが、第１及び第２の上部翼７、８の形状
は半楕円形に限定されず、種々の形状にすることができ
る。例えば、図１２及び図１３に示すように一辺に傾斜
部１３aを有する一対の台形状の平板１３で第１及び第
２の上部翼１４、１５を構成し、各上部翼１４、１５一
対で半六角形上部翼を形成してもよい。また、第２の上
部翼８の下端部は下部翼９の上辺部と軸方向に重複する
部分を含んでもよい。The embodiment of the present invention is not limited to the above-mentioned embodiment and can be modified. For example, in the above-described embodiment, an example is shown in which the first and second upper blades 7 and 8 formed of the pair of quarter semi-elliptical flat plates 11 form a pair of semi-elliptical upper blades. The shape of the second upper wings 7 and 8 is not limited to the semi-elliptical shape, and can be various shapes. For example, as shown in FIGS. 12 and 13, a pair of trapezoidal flat plates 13 each having an inclined portion 13a on one side constitutes the first and second upper blades 14 and 15, and each pair of upper blades 14 and 15 has a half shape. A hexagonal upper wing may be formed. Further, the lower end portion of the second upper blade 8 may include a portion that axially overlaps with the upper side portion of the lower blade 9.
【００１８】[0018]
【発明の効果】以上のように、この発明によれば低粘度
から高粘度までの広い粘度域の流体を速やかにかつ均一
に撹拌混合できるので、重縮合反応等の流体の粘度が広
い範囲で変化する場合でも撹拌翼を交換することなく使
用できると共に撹拌効率を向上して高品質の重合体を得
ることが可能となる。また、撹拌槽の内壁と撹拌翼との
間に邪魔板を設けた場合は、撹拌翼の回転方向に沿う液
体の流れを阻止して上昇流に変え、槽内の循環流を促進
する効果が得られる。また、高発熱重合に対して撹拌槽
内に冷却コイルを垂直バッフル状又はヘリカルコイル状
に設置した場合においても、冷却コイルによって邪魔板
を設けた場合と同様の効果が得られ、槽内の循環流が促
進される利点がある。As described above, according to the present invention, a fluid having a wide viscosity range from low viscosity to high viscosity can be rapidly and uniformly mixed with stirring, so that the viscosity of the fluid in a polycondensation reaction or the like can be kept in a wide range. Even if it changes, it can be used without changing the stirring blade and the stirring efficiency can be improved to obtain a high quality polymer. Further, when the baffle plate is provided between the inner wall of the stirring tank and the stirring blade, the effect of promoting the circulation flow in the tank by blocking the flow of the liquid along the rotation direction of the stirring blade and converting it into an upward flow is provided. can get. In addition, even if the cooling coil is installed in a vertical baffle shape or a helical coil shape in the stirring tank against the high exothermic polymerization, the same effect as when the baffle plate is provided by the cooling coil is obtained, and circulation in the tank is achieved. There is an advantage that the flow is promoted.
【図１】 この発明による撹拌装置の最良の実施の形態
を示す側断面図FIG. 1 is a side sectional view showing a best mode for a stirring device according to the present invention.
【図２】 図１の撹拌装置で使用する第１およぴ第２の
上部翼の形状を示す斜視図FIG. 2 is a perspective view showing the shapes of the first and second upper blades used in the stirring device of FIG.
【図３】 図１の撹拌装置の正面断面図FIG. 3 is a front sectional view of the stirring device of FIG.
【図４】 図１の撹拌装置で使用する下部翼の形状を示
す斜視図FIG. 4 is a perspective view showing a shape of a lower blade used in the stirring device of FIG.
【図５】 図１の撹拌装置の平面断面図5 is a plan sectional view of the stirring device of FIG.
【図６】 図１の撹拌装置の第１及び第２の上部翼にお
ける液体の流れを示す側断面図6 is a side sectional view showing the flow of liquid in the first and second upper blades of the stirring device of FIG.
【図７】 各種撹拌装置の脱色反応時におけるレイノル
ズ数Ｒeと無次元混合時間数ＮTMとの関係を示すグラフFIG. 7 is a graph showing the relationship between Reynolds number Re and dimensionless mixing time number N TM during decolorization reaction of various stirring devices.
【図８】 図１の撹拌装置の液体中のトレーサ粒子の流
動軌跡を示す一部正面断面図及び撹拌槽の各分割箇所に
おけるトレーサ粒子の存在頻度を示すグラフ8 is a partial front cross-sectional view showing a flow locus of tracer particles in a liquid of the stirring device of FIG. 1 and a graph showing a tracer particle existence frequency at each divided portion of the stirring tank.
【図９】 図１の撹拌装置の各部寸法の関係を示す三断
面図9 is a cross-sectional view showing the relationship between the dimensions of each part of the stirring device of FIG.
【図１０】 アンカー翼を備えた撹拌装置におけるヨー
ド−ハイポ混合液の脱色経過を示す図FIG. 10 is a view showing a decolorization process of an iodine-hypo mixed solution in a stirring device equipped with anchor blades.
【図１１】 図１の撹拌装置におけるヨード−ハイポ混
合液の脱色経過を示す図11 is a diagram showing the decolorization process of the iodine-hypo mixed solution in the stirring device of FIG.
【図１２】 この発明の他の実施の形態における第１及
び第２の上部翼の形状を示す斜視図FIG. 12 is a perspective view showing the shapes of first and second upper wings according to another embodiment of the present invention.
【図１３】 図１２の第１及び第２の上部翼の正面図及
び平面図13 is a front view and a plan view of the first and second upper wings shown in FIG.
【図１４】 撹拌装置の従来例を示す側断面図FIG. 14 is a side sectional view showing a conventional example of a stirring device.
【図１５】 図１４の撹拌装置で使用する上部翼の形状
を示す斜視図及び平面図15 is a perspective view and a plan view showing the shape of an upper blade used in the stirring device of FIG.
【図１６】 ４枚ピッチドパドル翼の形状を示す斜視図FIG. 16 is a perspective view showing the shape of a 4-pitch paddle blade.
【図１７】 ヘリカルリボン翼の形状を示す斜視図FIG. 17 is a perspective view showing the shape of a helical ribbon wing.
【図１８】 図１４の撹拌装置の上部翼における液体の
流れを示す側断面図FIG. 18 is a side sectional view showing the flow of liquid in the upper blade of the stirring device in FIG.
【図１９】 図１４の撹拌装置の液体中のトレーサ粒子
の流動軌跡を示す一部正面断面図及び撹拌槽の各分割箇
所におけるトレーサ粒子の存在頻度を示すグラフ19 is a partial front cross-sectional view showing the flow trajectory of tracer particles in the liquid of the stirring device of FIG. 14 and a graph showing the presence frequency of tracer particles at each divided portion of the stirring tank.
１．．．撹拌槽、２．．．回転軸、３．．．上部翼、３
a．．．下端、４．．．下部翼、５．．．撹拌翼、
６．．．邪魔板、７．．．第１の上部翼、７a．．．下
辺部、７b．．．上端、７c．．．表面、８．．．第２の
上部翼、８a．．．上辺部、８b．．．下端、８c．．．
背面、９．．．下部翼、１０．．．撹拌翼、１０
a．．．径方向端部、１１，１２．．．一対の平板、１
２a．．．折曲部、１２b．．．傾斜部1. . . Stirring tank, 2. . . Axis of rotation, 3. . . Upper wing, 3
a. . . Bottom edge, 4. . . Lower wing, 5. . . Stirring blade,
6. . . Baffle, 7. . . First upper wing, 7a. . . Lower side, 7b. . . Top, 7c. . . Surface, 8. . . Second upper wing, 8a. . . Upper side, 8b. . . Bottom edge, 8c. . .
Back, 9. . . Lower wing, 10. . . Stirring blade, 10
a. . . Radial ends, 11, 12. . . A pair of flat plates, 1
2a. . . Bent portion, 12b. . . Slope
───────────────────────────────────────────────────── フロントページの続き (72)発明者 城野 三千男 東京都豊島区高田３−29−５ 綜研化学株 式会社内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Michio Jono 3-29-5 Takada, Toshima-ku, Tokyo Soken Chemical Co., Ltd.
Claims (8)
れた回転軸と、撹拌槽内で回転可能に回転軸に固定され
た撹拌翼とを備えた撹拌装置において、 撹拌翼は、回転軸に対して傾斜して径方向かつ上方に延
びる第１の上部翼と、第１の上部翼の下方に配置されか
つ回転軸に対して傾斜して径方向かつ下方に延びる第２
の上部翼と、第２の上部翼に接近して配置されかつ撹拌
槽の底面付近まで回転軸から下方かつ径方向に延びる下
部翼とを有し、第１の上部翼及び第２の上部翼は下部翼
と略同一の半径で延出する部分を有しかつ回転軸方向に
所定の間隔で接近して配置され、第１の上部翼の下辺部
及び第２の上部翼の上辺部は互いに軸方向に重複する部
分を有することを特徴とする撹拌装置。1. A stirring device comprising a stirring tank, a rotating shaft rotatably supported in the stirring tank, and a stirring blade fixed to the rotating shaft so as to be rotatable in the stirring tank. A first upper wing that is inclined with respect to the rotation axis and extends radially and upward, and a second upper blade that is disposed below the first upper wing and extends radially and downward with respect to the rotation axis.
Upper blade and a lower blade that is arranged close to the second upper blade and extends downward and radially from the rotation axis to near the bottom surface of the stirring tank, and the first upper blade and the second upper blade Has a portion extending with substantially the same radius as the lower wing and is arranged close to each other at a predetermined interval in the rotation axis direction, and the lower side of the first upper wing and the upper side of the second upper wing are mutually An agitator having an axially overlapping portion.
移動させ、第２の上部翼は第１の上部翼との重複部分に
発生する吸引力により撹拌槽内の液体を槽底部に移動さ
せ、下部翼は撹拌槽内の槽底部の液体を径方向外側に移
動させ、液体は撹拌槽の内壁に沿って上方に移動される
「請求項１」に記載の撹拌装置。2. The first upper blade moves the liquid in the agitation tank downward, and the second upper blade agitates the liquid in the agitation tank by the suction force generated at the overlapping portion with the first upper blade. The stirring device according to claim 1, wherein the liquid is moved to the bottom, the lower blade moves the liquid at the bottom of the tank in the stirring tank to the outside in the radial direction, and the liquid is moved upward along the inner wall of the stirring tank.
れ回転軸に対して対称に配置された一対の四半楕円形状
の平板から構成され、第１及び第２の上部翼一対で半楕
円形上部翼を形成する「請求項１」又は「請求項２」に
記載の撹拌装置。3. The first upper blade and the second upper blade are each composed of a pair of quarter-elliptical flat plates symmetrically arranged with respect to the rotation axis. The stirring device according to claim 1 or claim 2, which forms an elliptical upper blade.
下端間の水平面距離ｄと第１及び第２の上部翼の回転軸
方向の間隔Ｃとの比の範囲が ０.０５≦Ｃ／ｄ≦０.６ である「請求項１」〜「請求項３」のいずれかに記載の
撹拌装置。4. The range of the ratio between the horizontal plane distance d between the upper end of the first upper blade and the lower end of the second upper blade and the distance C in the rotational axis direction between the first and second upper blades is 0.05. The stirrer according to any one of "claim 1" to "claim 3" wherein ≤C / d≤0.6.
傾斜角度θの範囲が ３０°≦θ≦６０° である「請求項１」〜「請求項４」のいずれかに記載の
撹拌装置。5. The stirring device according to any one of claims 1 to 4, wherein a range of inclination angles θ of the first and second upper blades with respect to a horizontal plane is 30 ° ≦ θ ≦ 60 °. .
設けられた「請求項１」〜「請求項５」のいずれかに記
載の撹拌装置。6. The stirring device according to claim 1, wherein a baffle plate is provided between the inner wall of the stirring tank and the stirring blade.
設けられた「請求項６」に記載の撹拌装置。7. The stirring device according to claim 6, wherein the baffle plate is provided in the vicinity of the radial end of the stirring blade.
と軸方向に重複する部分を有する「請求項１」〜「請求
項７」のいずれかに記載の撹拌装置。8. The stirring device according to claim 1, wherein the bottom portion of the second upper blade has a portion that axially overlaps with the upper portion of the lower blade.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23306895A JP3224498B2 (en) | 1995-09-11 | 1995-09-11 | Stirrer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23306895A JP3224498B2 (en) | 1995-09-11 | 1995-09-11 | Stirrer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0975699A true JPH0975699A (en) | 1997-03-25 |
| JP3224498B2 JP3224498B2 (en) | 2001-10-29 |
Family
ID=16949306
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP23306895A Expired - Fee Related JP3224498B2 (en) | 1995-09-11 | 1995-09-11 | Stirrer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3224498B2 (en) |
Cited By (12)
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| WO2005012218A1 (en) * | 2003-08-05 | 2005-02-10 | Mitsui Chemicals, Inc. | Method for producing terephthalic acid and terephthalic acid |
| WO2007037263A1 (en) * | 2005-09-29 | 2007-04-05 | Shi Mechanical & Equipment Inc. | Agitator |
| JP2007137978A (en) * | 2005-11-16 | 2007-06-07 | Toagosei Co Ltd | Apparatus for producing urethane (meth)acrylate or epoxy (meth)acrylate and method for production |
| JP2008036480A (en) * | 2006-08-02 | 2008-02-21 | Dainippon Ink & Chem Inc | Stirring device and production method of high-viscosity synthetic resin |
| US7488513B2 (en) | 2002-03-22 | 2009-02-10 | Toyo Ink Mfg. Co., Ltd. | Process for producing microcapsule enclosing electrophoretic particle dispersion, microcapsule enclosing electrophoretic particle dispersion and reversible display medium containing the same |
| JP2010502430A (en) * | 2006-09-11 | 2010-01-28 | クォン，サンドン | Stirrer for organic waste treatment (ANAGITATORFORTREATINGORGANICWASTE) |
| JP2010058027A (en) * | 2008-09-02 | 2010-03-18 | Flo-Tec Ltd | Agitation apparatus and agitation tank |
| JP2011525988A (en) * | 2008-06-27 | 2011-09-29 | ジーイー・ヘルスケア・バイオサイエンス・アクチボラグ | Separation medium slurry tank |
| US8485716B2 (en) | 2009-01-16 | 2013-07-16 | Dic Corporation | Agitation apparatus and agitation method |
| CN109453684A (en) * | 2018-11-26 | 2019-03-12 | 衡阳思迈科科技有限公司 | The stock stirring device of conductive silver glue processing |
| CN109954418A (en) * | 2018-01-02 | 2019-07-02 | 孙宇航 | Double-directional rotary mixing component, blender and its working method using the component |
| KR20220002476U (en) * | 2021-04-07 | 2022-10-14 | 손영윤 | Supporter for agitator of urethane waterproof paint |
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1995
- 1995-09-11 JP JP23306895A patent/JP3224498B2/en not_active Expired - Fee Related
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7488513B2 (en) | 2002-03-22 | 2009-02-10 | Toyo Ink Mfg. Co., Ltd. | Process for producing microcapsule enclosing electrophoretic particle dispersion, microcapsule enclosing electrophoretic particle dispersion and reversible display medium containing the same |
| JPWO2005012218A1 (en) * | 2003-08-05 | 2006-09-14 | 三井化学株式会社 | Method for producing terephthalic acid and terephthalic acid |
| CN100393688C (en) * | 2003-08-05 | 2008-06-11 | 三井化学株式会社 | Method for producing terephthalic acid and terephthalic acid |
| WO2005012218A1 (en) * | 2003-08-05 | 2005-02-10 | Mitsui Chemicals, Inc. | Method for producing terephthalic acid and terephthalic acid |
| JP4701056B2 (en) * | 2005-09-29 | 2011-06-15 | 住友重機械プロセス機器株式会社 | Stirrer |
| WO2007037263A1 (en) * | 2005-09-29 | 2007-04-05 | Shi Mechanical & Equipment Inc. | Agitator |
| JP2007090265A (en) * | 2005-09-29 | 2007-04-12 | Shi Mechanical & Equipment Inc | Stirring apparatus |
| JP2007137978A (en) * | 2005-11-16 | 2007-06-07 | Toagosei Co Ltd | Apparatus for producing urethane (meth)acrylate or epoxy (meth)acrylate and method for production |
| JP2008036480A (en) * | 2006-08-02 | 2008-02-21 | Dainippon Ink & Chem Inc | Stirring device and production method of high-viscosity synthetic resin |
| JP2010502430A (en) * | 2006-09-11 | 2010-01-28 | クォン，サンドン | Stirrer for organic waste treatment (ANAGITATORFORTREATINGORGANICWASTE) |
| JP2011525988A (en) * | 2008-06-27 | 2011-09-29 | ジーイー・ヘルスケア・バイオサイエンス・アクチボラグ | Separation medium slurry tank |
| JP2010058027A (en) * | 2008-09-02 | 2010-03-18 | Flo-Tec Ltd | Agitation apparatus and agitation tank |
| US8485716B2 (en) | 2009-01-16 | 2013-07-16 | Dic Corporation | Agitation apparatus and agitation method |
| CN109954418A (en) * | 2018-01-02 | 2019-07-02 | 孙宇航 | Double-directional rotary mixing component, blender and its working method using the component |
| CN109453684A (en) * | 2018-11-26 | 2019-03-12 | 衡阳思迈科科技有限公司 | The stock stirring device of conductive silver glue processing |
| KR20220002476U (en) * | 2021-04-07 | 2022-10-14 | 손영윤 | Supporter for agitator of urethane waterproof paint |
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| JP3224498B2 (en) | 2001-10-29 |
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