JP2001276594A - Method for mixing fine particles with fluidized bed - Google Patents
Method for mixing fine particles with fluidized bedInfo
- Publication number
- JP2001276594A JP2001276594A JP2000101781A JP2000101781A JP2001276594A JP 2001276594 A JP2001276594 A JP 2001276594A JP 2000101781 A JP2000101781 A JP 2000101781A JP 2000101781 A JP2000101781 A JP 2000101781A JP 2001276594 A JP2001276594 A JP 2001276594A
- Authority
- JP
- Japan
- Prior art keywords
- particles
- fine particles
- fluidized bed
- fine
- mixing
- 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.)
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、混合方法に関し、
更に詳しくは、流動層を用いて微粒子を混合する方法に
関する。The present invention relates to a mixing method,
More specifically, the present invention relates to a method of mixing fine particles using a fluidized bed.
【０００２】[0002]
【従来の技術】最近、電子材料、燃料電池、ファインセ
ラミックス等の技術領域ではサブミクロンから数ミクロ
ンのオーダーの微粒子状で物性の異なる材料を複数組み
合わせて混合し、この混合物に焼成等の処理を施すこと
により新たな物性を持った複合材料を作ることが多くな
ってきている。このような複合材料を作るには、物性の
異なる複数の微粒子素材を均質に混合することが極めて
重要な技術になっている。しかも、このような微粒子素
材は益々微粒子化が進み１０数ミクロンからサブミクロ
ンオーダーに達するものも珍しいことではない。2. Description of the Related Art Recently, in the technical fields of electronic materials, fuel cells, fine ceramics, etc., a plurality of materials having different physical properties in the form of fine particles of the order of submicron to several microns are mixed and mixed, and the mixture is subjected to a treatment such as firing. Application of such materials has increased the production of composite materials having new physical properties. In order to produce such a composite material, it has become a very important technique to uniformly mix a plurality of fine particle materials having different physical properties. In addition, it is not uncommon for such fine particle materials to be increasingly finely divided and reach the order of several tens of microns to submicron.
【０００３】ところが、一般に、３０〜４０μｍ以下の
微粒子は付着、凝集性が強く、微粒子同士が互いに容易
に付着、凝集して二次粒子を形成したり、装置の壁面等
に簡単に付着するなどし、その取り扱いが極めて難し
い。例えば、１μｍの微粒子は１００万個凝集して１０
０μｍ程度の粒子径の二次粒子を形成することも希なこ
とではない。However, in general, fine particles having a size of 30 to 40 μm or less have strong adhesion and cohesive properties, and the fine particles easily adhere to each other and aggregate to form secondary particles, or easily adhere to the wall surface of an apparatus. And its handling is extremely difficult. For example, 1 million fine particles are
It is not unusual to form secondary particles having a particle size of about 0 μm.
【０００４】ところで、従来の粉粒体の混合方式として
は、例えば、容器回転方式、機械撹拌方式、気流方式あ
るいはこれらを適宜組み合わせた複合方式が広く知られ
ている。これらの混合方式は、粒子径が比較的大きく粉
粒体同士が凝集しない場合には均質に混合することがで
きる。By the way, as a conventional mixing method of powders and granules, for example, a container rotation method, a mechanical stirring method, an air flow method, or a combination method appropriately combining these is widely known. These mixing methods can be homogeneously mixed when the particles have a relatively large particle size and do not agglomerate.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、従来の
混合方式を用いて前述のサブミクロンオーダーないし１
０数ミクロンオーダーの微粒子を複数種混合する場合に
は、前述のように互いの凝集力によって一次粒子が凝
集、付着して二次粒子を形成し易く、しかもこのような
塊は簡単には一次粒子レベルに戻らないため、二次粒子
の状態のまま混合され、混合物には二次粒子の塊として
局在し、一次粒子レベルで万遍なく均質に混合すること
は極めて難しいという課題があった。However, using the conventional mixing method, the above-mentioned submicron order or 1-micron order is used.
When a plurality of types of fine particles of the order of 0 microns are mixed, as described above, the primary particles are easily aggregated and adhered to each other to form secondary particles due to the cohesive force of each other. Because it does not return to the particle level, it is mixed as it is in the form of secondary particles, it is localized as a mass of secondary particles in the mixture, and there is a problem that it is extremely difficult to mix uniformly at the primary particle level .
【０００６】本発明は、上記課題を解決するためになさ
れたもので、凝集して二次粒子を形成し易いサブミクロ
ンオーダーの微粒子であっても複数種類の微粒子をそれ
ぞれ二次粒子から一次粒子へと解砕して一次粒子レベル
で均質に混合することができる微粒子の混合方法を提供
することを目的としている。SUMMARY OF THE INVENTION The present invention has been made to solve the above-mentioned problems, and a plurality of types of fine particles are each converted from a secondary particle to a primary particle even if the fine particles are on the order of submicrons that are likely to aggregate to form secondary particles. It is an object of the present invention to provide a method of mixing fine particles which can be crushed into fine particles and uniformly mixed at a primary particle level.
【０００７】[0007]
【課題を解決するための手段】本発明の請求項１に記載
の微粒子の混合方法は、粗粒子からなる流動層へ気体を
供給して粗粒子を流動化し、その流動層へ凝集性のある
種類の異なる複数種の微粒子を供給し、凝集した各種の
微粒子を上記流動層において解砕しながら混合すること
を特徴とするものである。According to a first aspect of the present invention, there is provided a method of mixing fine particles, wherein a gas is supplied to a fluidized bed composed of coarse particles to fluidize the coarse particles, and the fluidized bed has a cohesive property. A plurality of different types of fine particles are supplied, and the various types of aggregated fine particles are mixed while being crushed in the fluidized bed.
【０００８】また、本発明の請求項２に記載の微粒子の
混合方法は、請求項１に記載の発明において、上記各微
粒子として０．１〜２０μｍの粒子径からなる微粒子を
供給することを特徴とするものである。[0008] The method of mixing fine particles according to claim 2 of the present invention is characterized in that, in the invention according to claim 1, fine particles having a particle diameter of 0.1 to 20 µm are supplied as the respective fine particles. It is assumed that.
【０００９】また、本発明の請求項３に記載の微粒子の
混合方法は、請求項１または請求項２に記載の発明にお
いて、上記粗粒子として３００〜１５００μｍの粒子径
の粗粒子を用いることを特徴とするものである。Further, the method for mixing fine particles according to claim 3 of the present invention is characterized in that, in the invention according to claim 1 or 2, coarse particles having a particle diameter of 300 to 1500 μm are used as the coarse particles. It is a feature.
【００１０】また、本発明の請求項４に記載の微粒子の
混合方法は、請求項１〜請求項３のいずれか１項に記載
の発明において、上記粗粒子として一定の粒子径に揃っ
た粗粒子を用いることを特徴とするものである。The method for mixing fine particles according to claim 4 of the present invention is the method according to any one of claims 1 to 3, wherein the coarse particles have a uniform particle diameter as the coarse particles. It is characterized by using particles.
【００１１】また、本発明の請求項５に記載の微粒子の
混合方法は、請求項１〜請求項４のいずれか１項に記載
の発明において、上記分散板型流動層または噴流型流動
層を用いることを特徴とするものである。The method for mixing fine particles according to claim 5 of the present invention is the method according to any one of claims 1 to 4, wherein the dispersion plate type fluidized bed or the jet fluidized bed is used. It is characterized in that it is used.
【００１２】[0012]
【発明の実施の形態】以下、図１〜図４に示す実施形態
に基づいて本発明を説明する。尚、図１は本発明の混合
方法を実施する際に用いられる流動層の一例を示す模式
図、図２の（ａ）、（ｂ）はそれぞれ流動層の粗粒子同
士が衝突、摩擦を繰り返して微粒子の二次粒子を一次粒
子に解砕する状況を説明するための説明図、図３は本発
明の混合方法を実施する際に用いられる流動層の他の一
例を示す模式図、図４は本発明の混合方法を検証するた
めの試験装置を示す模式図である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below based on the embodiments shown in FIGS. FIG. 1 is a schematic view showing an example of a fluidized bed used when the mixing method of the present invention is carried out. FIGS. 2A and 2B are diagrams in which coarse particles of the fluidized bed repeatedly collide and friction. FIG. 3 is an explanatory view for explaining a situation in which secondary particles of fine particles are broken into primary particles by using the method. FIG. 3 is a schematic view showing another example of a fluidized bed used when performing the mixing method of the present invention, and FIG. FIG. 2 is a schematic view showing a test apparatus for verifying the mixing method of the present invention.
【００１３】本発明の混合方法を実施する場合には例え
ば図１で模式的に示す分散板型の混合器、噴流型の混合
器が用いられる。図１に示す分散板型の混合器１０は、
同図に示すように、主として直胴部１１Ａ及びコーン部
１１Ｂからなる容器１１と、この容器１１内に粗粒子Ｐ
を充填して形成された流動層１２とを備えている。容器
１１の直胴部１１Ａとコーン部１１Ｂの境界には分散板
１３が介在し、この分散板１３上に所定量の粗粒子Ｐが
充填されている。この分散板１３には多数の孔１３Ａが
全面に分散して形成されている。孔１３Ａは流動層１２
を形成する粗粒子Ｐが漏出しない大きさであれば良い。
また、コーン部１１Ｂの下端には空気等の気体を流動層
１２へ供給し流動層１２を流動化するための給気口１１
Ｃが形成されている。流動層１２を形成する粗粒子Ｐは
給気口１１Ｃから供給される気体によって流動化して直
胴部１１Ａ内を激しく動き廻り、互いに衝突、摩擦を繰
り返す。尚、図１では直胴部１１Ａの上端を開放してあ
るが、実際にはコーン状、ドーム状等の屋根が取り付け
られ、その一部に流出管が接続されている。When the mixing method of the present invention is carried out, for example, a dispersion plate type mixer or a jet type mixer schematically shown in FIG. 1 is used. The dispersion plate type mixer 10 shown in FIG.
As shown in the figure, a container 11 mainly composed of a straight body 11A and a cone 11B, and coarse particles P
And a fluidized bed 12 formed by filling. A dispersion plate 13 is interposed at the boundary between the straight body 11A and the cone 11B of the container 11, and a predetermined amount of coarse particles P is filled on the dispersion plate 13. The dispersion plate 13 has a large number of holes 13A dispersed throughout the surface. The holes 13A are in the fluidized bed 12
Any size may be used as long as the coarse particles P forming the above do not leak.
An air supply port 11 for supplying gas such as air to the fluidized bed 12 and fluidizing the fluidized bed 12 is provided at a lower end of the cone portion 11B.
C is formed. The coarse particles P forming the fluidized bed 12 are fluidized by the gas supplied from the air supply port 11C, move violently in the straight body 11A, and repeatedly collide and friction with each other. Although the upper end of the straight body 11A is opened in FIG. 1, a cone-shaped or dome-shaped roof is actually attached, and an outflow pipe is connected to a part of the roof.
【００１４】而して、上記粗粒子Ｐは略一定の粒子径を
有し、しかもその粒子径は例えば３００〜１５００μｍ
の範囲内にある。略一定の粒子径とは実質的に所定の粒
子径に揃っている状態で、厳密にはその粒子径から多少
はずれた粒子径が含まれている状態を云う。粒子径が３
００μｍ未満では粗粒子Ｐ自体が空気等の気体と一緒に
流出するため好ましくない。また、粒子径が１５００μ
ｍを超えると流動層１２の流動化に気体の流速を必要以
上の大きさに設定しなくてはならないため好ましくな
い。粗粒子Ｐに用いられる材料は、特に制限されるもの
ではないが、粗粒子Ｐの材料としては例えばセラミッ
ク、シラスバルーン、石灰石、シリカサンド、ガラスビ
ーズ等を挙げることができる。また、粗粒子Ｐの表面は
付着した微粒子ｐが剥離し離脱し易いものが好ましい。The coarse particles P have a substantially constant particle size, and the particle size is, for example, 300 to 1500 μm.
Within the range. A substantially constant particle size refers to a state in which the particle diameter is substantially equal to a predetermined particle diameter, and strictly speaking, a state in which a particle diameter slightly deviating from the particle diameter is included. Particle size 3
If the thickness is less than 00 μm, the coarse particles P themselves flow out together with a gas such as air, which is not preferable. In addition, the particle diameter is 1500μ
If it exceeds m, the flow velocity of the gas must be set to a value larger than necessary for fluidizing the fluidized bed 12, which is not preferable. The material used for the coarse particles P is not particularly limited, but examples of the material for the coarse particles P include ceramic, shirasu balloon, limestone, silica sand, and glass beads. Further, it is preferable that the surface of the coarse particles P is such that the attached fine particles p are easily separated and separated.
【００１５】また、上記混合器１０には配管１４を介し
て微粒子供給機１５が接続されている。微粒子供給機１
５は複数種の微粒子ｐを所定の配合比で予備混合した複
数種の微粒子ｐをコンプレッサ等の給気手段（図示せ
ず）を用いて配管１４内を気体輸送し混合器１０へ供給
するものである。配管１４は例えば混合器１０のコーン
部１１Ｂに接続され、コーン部１１Ｂに供給される気体
を介して複数種の微粒子ｐを流動層１２内へ供給するよ
うにしてある。微粒子供給機１５において予備混合され
る複数種の微粒子ｐは、それぞれ例えば０．１〜２０μ
ｍの粒子径を有している。そのため、各種の微粒子ｐは
一次粒子同士が互いに凝集して付着し、二次粒子を形成
している。二次粒子は微粒子供給機１５での予備混合で
は殆ど解砕されず、そのまま混合器１０へ供給される。
尚、以下では微粒子ｐのうち、凝集していない微粒子を
一次粒子ｐとして、また、凝集した微粒子を二次粒子
ｐ’として説明する。A fine particle feeder 15 is connected to the mixer 10 via a pipe 14. Particle feeder 1
Reference numeral 5 denotes a method in which a plurality of types of fine particles p obtained by pre-mixing a plurality of types of fine particles p at a predetermined mixing ratio are gas-transported in a pipe 14 using an air supply means (not shown) such as a compressor and supplied to the mixer 10. It is. The pipe 14 is connected to, for example, the cone portion 11B of the mixer 10 so that a plurality of types of fine particles p are supplied into the fluidized bed 12 via gas supplied to the cone portion 11B. The plurality of types of fine particles p that are premixed in the fine particle feeder 15 are each 0.1 to 20 μm, for example.
m. Therefore, the primary particles of the various fine particles p are aggregated and adhere to each other to form secondary particles. The secondary particles are hardly disintegrated by the preliminary mixing in the fine particle feeder 15 and are supplied to the mixer 10 as they are.
Hereinafter, among the fine particles p, the fine particles that are not aggregated will be described as primary particles p, and the aggregated fine particles will be described as secondary particles p ′.
【００１６】上記微粒子ｐの粒子径は例えば上述のよう
に０．１〜２０μｍの範囲内のものが好ましい。そし
て、種類の異なる複数の微粒子ｐは、それぞれの粒子径
が同一であっても異なっていても良い。この範囲の粒子
径を有する微粒子ｐは、前述したように極めて凝集力が
強く簡単に二次粒子ｐ’を形成し、しかも従来の混合方
式では簡単には一次粒子ｐに解砕することが極めて難し
い。粒子径が０．１μｍ未満の微粒子ｐは粗粒子Ｐに強
く付着し、解砕後の微粒子ｐの回収率が低下する虞があ
るため好ましくない。また、粒子径が２０μｍを超える
微粒子ｐは凝集性があっても従来の混合方式で一次粒子
ｐに解砕できる可能性があり、敢えて本発明方法を用い
ることもないため、好ましくない。また、微粒子ｐは特
定の材料に制限されるものではなく、無機化合物、有機
化合物のいずれであっても良い。例えば前述した電子材
料、燃料電池、ファインセラミックス等の技術領域で用
いられる微粒子素材に対して本発明方法を好適に用いる
ことができる。The particle diameter of the fine particles p is preferably, for example, in the range of 0.1 to 20 μm as described above. The plurality of fine particles p of different types may have the same or different particle diameters. The fine particles p having a particle diameter in this range have a very strong cohesive force and easily form the secondary particles p ′ as described above, and can be easily disintegrated into the primary particles p by the conventional mixing method. difficult. The fine particles p having a particle diameter of less than 0.1 μm are not preferable because they may strongly adhere to the coarse particles P and the recovery rate of the fine particles p after crushing may decrease. Further, the fine particles p having a particle diameter of more than 20 μm are not preferable because they may be crushed into the primary particles p by a conventional mixing method even if they have a cohesive property, and the method of the present invention is not intentionally used. The fine particles p are not limited to a specific material, and may be any of an inorganic compound and an organic compound. For example, the method of the present invention can be suitably used for fine particle materials used in technical fields such as the above-mentioned electronic materials, fuel cells, fine ceramics, and the like.
【００１７】次に、上記混合器１０を用いた本発明の混
合方法について説明する。例えば空気をコーン部１１Ｂ
の下端の給気口１１Ｃから矢印Ａ方向へ供給すると、空
気は分散板１３の孔１３Ａを経由して直胴部１１Ａ内を
上昇流で通過する際に、この上昇流で流動層１２の粗粒
子Ｐが流動化して直胴部１１Ａ内を縦横無尽に動き廻
る。この時、微粒子供給機１５内において予備混合した
複数種（例えば三種類）の微粒子ｐを配管１４を介して
混合器１０のコーン部１１Ｂへ供給する。微粒子供給機
１５では三種類の微粒子ｐが予備混合されてもそれぞれ
の大部分を二次粒子ｐ’のままコーン部１１Ｂへ供給す
る。コーン部１１Ｂでは各種の微粒子ｐは給気口１１Ｃ
からの空気流に乗って直胴部１１Ａ内で流動化した流動
層１２内へ流入する。Next, the mixing method of the present invention using the mixer 10 will be described. For example, air is supplied to the cone 11B.
When air is supplied in the direction of arrow A from the air supply port 11C at the lower end of the fluidized bed, the air flows through the hole 13A of the dispersing plate 13 in the straight body 11A in an ascending flow. The particles P are fluidized and move around in the straight body 11A in all directions. At this time, plural kinds (for example, three kinds) of fine particles p preliminarily mixed in the fine particle feeder 15 are supplied to the cone portion 11B of the mixer 10 through the pipe 14. In the fine particle feeder 15, most of the three types of fine particles p are supplied to the cone portion 11B as the secondary particles p 'even if they are preliminarily mixed. In the cone portion 11B, various fine particles p are supplied to the air supply port 11C.
And flows into the fluidized bed 12 fluidized in the straight body portion 11A on the airflow from the air.
【００１８】流動層１２内では三種類の微粒子ｐの大部
分は図２の（ａ）に示すようにそれぞれ二次粒子ｐ’の
まま個々の粗粒子Ｐ表面へ付着する。これらの粗粒子Ｐ
は直胴部１１Ａ内で縦横無尽に動き廻っているため、粗
粒子Ｐ同士が図２の（ａ）で示すように衝突、摩擦を繰
り返し、この間に同図に（ｂ）で示すように各粗粒子Ｐ
に付着した二次粒子ｐ’を一次粒子ｐまで解砕すると共
に、解砕された各種の一次粒子ｐは粗粒子Ｐから剥離し
て離脱する。離脱した微粒子ｐは上昇気流を介して流動
層１２の空隙を縫って流動層１２から浮上し、容器１１
上端から図示しない流出管を経由してバグフィルタ（図
示せず）等の捕集手段に達して回収される。流動層１２
から浮上した複数種の浮遊微粒子ｐは容器１１からバグ
フィルタに達する間に空気を介して万遍なく混合され、
捕集手段で回収した段階では各種の微粒子ｐは一次粒子
レベルで均質に混合された混合物になっている。In the fluidized bed 12, most of the three types of fine particles p adhere to the surfaces of the individual coarse particles P as secondary particles p 'as shown in FIG. 2A. These coarse particles P
Is moving around endlessly in the straight body 11A, so that the coarse particles P repeatedly collide and friction as shown in FIG. 2A, and during this time, as shown in FIG. Coarse particles P
The secondary particles p ′ adhered to the particles are crushed into primary particles p, and the crushed various primary particles p are separated from the coarse particles P and separated. The separated fine particles p rise through the fluidized bed 12 through the ascending airflow through the gaps of the fluidized bed 12 and rise to the container 11.
From the upper end, it reaches a collecting means such as a bag filter (not shown) via an outflow pipe (not shown) and is collected. Fluidized bed 12
Are mixed uniformly via air while reaching the bag filter from the container 11,
At the stage of recovery by the collecting means, the various fine particles p are in a homogeneously mixed mixture at the primary particle level.
【００１９】以上説明したように本実施形態によれば、
粗粒子Ｐからなる流動層１２へ空気を供給して粗粒子Ｐ
を流動化し、その流動層１２へ凝集性のある三種類の微
粒子ｐを供給し、凝集した各種の微粒子ｐの二次粒子
ｐ’を流動層１２において解砕しながら混合するように
したため、三種類の微粒子ｐが凝集して二次粒子ｐ’を
形成し易いサブミクロンオーダーの微粒子ｐであっても
それぞれの微粒子ｐを二次粒子ｐ’から一次粒子ｐまで
解砕して一次粒子レベルで均質に混合することができ、
各微粒子ｐの特性を効果的に引き出し、安定した品質の
混合物を得ることができる。As described above, according to the present embodiment,
Air is supplied to the fluidized bed 12 composed of coarse particles P
Is fluidized, and three types of fine particles p having cohesiveness are supplied to the fluidized bed 12, and secondary particles p ′ of the various types of aggregated fine particles p are mixed while being crushed in the fluidized bed 12. Even in the case of submicron-order fine particles p in which various kinds of fine particles p are easily aggregated to form secondary particles p ′, each fine particle p is disintegrated from the secondary particles p ′ to the primary particles p at the primary particle level. Can be mixed homogeneously,
The characteristics of each fine particle p can be effectively extracted, and a mixture of stable quality can be obtained.
【００２０】また、本実施形態によれば、微粒子ｐとし
て０．１〜２０μｍの粒子径からなる微粒子ｐを供給す
るようにしたため、凝集性の強い微粒子ｐの大部分を一
次粒子レベルで均質に混合することができる。また、流
動層１２の粗粒子Ｐとして３００〜１５００μｍの粒子
径の粗粒子を用いるようにしたため、微粒子ｐを粗粒子
Ｐから確実に分離して均質に混合することができる。ま
た、粗粒子Ｐとして一定の粒子径に揃った粗粒子Ｐを用
いるようにしたため、圧力損失が略一定し安定した混合
操作を行うことができる。更に、流動層１２として分散
板型の流動層を用いたため、既存の流動層を利用して微
粒子ｐの混合操作を行うことができる。Further, according to the present embodiment, since the fine particles p having a particle diameter of 0.1 to 20 μm are supplied as the fine particles p, most of the finely-aggregated fine particles p can be uniformly dispersed at the primary particle level. Can be mixed. In addition, since coarse particles having a particle diameter of 300 to 1500 μm are used as the coarse particles P of the fluidized bed 12, the fine particles p can be surely separated from the coarse particles P and uniformly mixed. Further, since the coarse particles P having a uniform particle diameter are used as the coarse particles P, the pressure loss is substantially constant, and a stable mixing operation can be performed. Furthermore, since a fluidized bed of a dispersion plate type is used as the fluidized bed 12, the mixing operation of the fine particles p can be performed using an existing fluidized bed.
【００２１】また、図３は噴流型の混合器２０を模式的
に示す図である。この混合器２０の容器２１は直胴部２
１Ａとコーン部２１Ｂとからなり、その内部に粗粒子Ｐ
が充填されて流動層２２を形成している。コーン部２１
Ｂ下端の給気口２１Ｃから空気等の気体を供給するよう
になっている。また、コーン部２１Ｂの下方には配管２
４を介して微粒子供給機２５が接続されている。FIG. 3 is a view schematically showing a jet-type mixer 20. As shown in FIG. The container 21 of the mixer 20 has a straight body 2
1A and a cone portion 21B, in which coarse particles P
Are filled to form the fluidized bed 22. Cone part 21
A gas such as air is supplied from an air supply port 21C at the lower end of B. A pipe 2 is provided below the cone 21B.
The fine particle feeder 25 is connected to the control unit 4 via the control unit 4.
【００２２】従って、例えば給気口２１Ｃから空気を矢
印Ａ方向へ供給すると、空気はコーン部２１Ｂの出口を
塞いでいる流動層２２の下端から吹き上げて流動層２２
の上面から噴出する。空気が流動層２２の下端からその
上方へ噴出する時に流動層２２の粗粒子Ｐを流動化す
る。一方、微粒子供給機２５から配管２４を介して微粒
子ｐを空気輸送すると、微粒子ｐは給気口２１Ｃからの
空気の上昇流に乗って流動化した流動層２２内へ噴出す
る。この際、微粒子ｐの一次粒子及び二次粒子が粗粒子
Ｐに付着し、微粒子ｐが付着した粗粒子Ｐ同士が衝突、
摩擦を繰り返し、粗粒子Ｐ表面の二次粒子が解砕され、
一次粒子となって粗粒子Ｐから剥離し、粗粒子Ｐの空隙
を縫って流動層２２上へ浮上する。その後、容器２０か
ら図示しない流出管を介してバグフィルタ等の捕集手段
へ達する。容器２０から捕集手段へ到達する間にも微粒
子ｐは混合作用を受け、捕集手段に達した時点で均質な
混合物になる。本実施形態においても上記実施形態と同
様の作用効果を期することができる。●は微粒子ｐが付
着した粗粒子Ｐを示している。Therefore, for example, when air is supplied from the air supply port 21C in the direction of arrow A, the air blows up from the lower end of the fluidized bed 22 closing the outlet of the cone portion 21B, and
Erupts from the upper surface. When air is blown upward from the lower end of the fluidized bed 22, the coarse particles P of the fluidized bed 22 are fluidized. On the other hand, when the fine particles p are pneumatically transported from the fine particle feeder 25 via the pipe 24, the fine particles p are jetted into the fluidized fluidized bed 22 on the upward flow of air from the air supply port 21C. At this time, the primary particles and the secondary particles of the fine particles p adhere to the coarse particles P, and the coarse particles P to which the fine particles p adhere collide with each other,
The friction is repeated, and the secondary particles on the surface of the coarse particles P are crushed,
The particles become primary particles and are separated from the coarse particles P, and float on the fluidized bed 22 through the voids of the coarse particles P. Thereafter, the water reaches the collecting means such as a bag filter from the container 20 via an outflow pipe (not shown). The fine particles p are also subjected to the mixing action while reaching the collecting means from the container 20, and become a homogeneous mixture when reaching the collecting means. In this embodiment, the same operation and effect as those in the above embodiment can be expected. ● indicates coarse particles P to which fine particles p adhered.
【００２３】次に、本発明の混合方法を検証するための
試験装置について図４を参照しながら説明する。本試験
装置は、図４に示すように、空気供給装置４１と、微粒
子供給機４２と、微粒子の混合器４３と、バグフィルタ
ー４４とを備えている。Next, a test apparatus for verifying the mixing method of the present invention will be described with reference to FIG. As shown in FIG. 4, the test apparatus includes an air supply device 41, a fine particle supply device 42, a fine particle mixer 43, and a bag filter 44.
【００２４】上記空気供給装置４１は、図４に示すよう
に、空気を圧送するコンプレッサ４５と、このコンプレ
ッサ４５から圧送される空気から油分を除去するオイル
フィルタ４６と、このフィルタ４６を経由した空気を徐
湿する徐湿器（シリカゲル塔）４７と、このシリカゲル
塔４７からの徐湿空気の圧力を調整する圧力調整弁４８
とを備え、これらの各機器は配管４９によって連結され
ている。この配管４９は圧力調整弁４８の下流側で三方
に分岐している。As shown in FIG. 4, the air supply device 41 includes a compressor 45 for supplying air, an oil filter 46 for removing oil from the air supplied from the compressor 45, and an air filter passing through the filter 46. (Silica gel tower) 47 for humidifying the air, and a pressure regulating valve 48 for adjusting the pressure of the humidified air from the silica gel tower 47.
And these devices are connected by a pipe 49. This pipe 49 branches off in three directions downstream of the pressure regulating valve 48.
【００２５】第１分岐管４９Ａには上流側から下流側へ
流量計（オリフィス）５０及び微粒子供給機４２がこの
順序で配設され、第１分岐管４９Ａの下流端に混合器４
３が接続されている。第２分岐管４９Ｂには上流側から
下流側へ流量計５０及び調湿器５１がこの順序で配設さ
れ、第３分岐管４９Ｃには流量計５０が配設され、第
２、第３分岐管４９Ｂ、４９Ｃは調湿器５１の下流側で
合流している。第２、第３分岐管４９Ｂ、４９Ｃの合流
管４９Ｄの下流端には混合器４３が接続されている。更
に、混合器４３は配管４９を介してバグフィルタ４４に
接続されている。混合器４３内には３００〜１５００μ
ｍの粒子が流動層４３Ａとして充填されている。A flow meter (orifice) 50 and a fine particle feeder 42 are arranged in this order from the upstream side to the downstream side in the first branch pipe 49A, and the mixer 4 is provided at the downstream end of the first branch pipe 49A.
3 are connected. A flow meter 50 and a humidity controller 51 are provided in this order from the upstream side to the downstream side in the second branch pipe 49B, and a flow meter 50 is provided in the third branch pipe 49C. The pipes 49B and 49C join on the downstream side of the humidity controller 51. The mixer 43 is connected to the downstream end of the merging pipe 49D of the second and third branch pipes 49B and 49C. Further, the mixer 43 is connected to a bag filter 44 via a pipe 49. 300-1500μ in the mixer 43
m particles are packed as a fluidized bed 43A.
【００２６】従って、第２、第３分岐管４９Ｂ、４９Ｃ
から調湿後の空気を混合器４３へ供給し、その内部の流
動層４３Ａを流動化すると共に微粒子供給機４２から複
数種の微粒子ｐの予備混合物を連続的に空気輸送する
と、各微粒子ｐは混合器４３に達する。各微粒子ｐは一
次粒子と二次粒子が混じった状態で調湿後の空気流に乗
って流動化した流動層４３Ａ内に入り、粗粒子Ｐの表面
に付着た後、粗粒子Ｐ同士の衝突、摩擦により二次粒子
は一次粒子となって混合器４３から流出してバグフィル
タ４４で各微粒子ｐの均質な混合物として回収される。Therefore, the second and third branch pipes 49B, 49C
Is supplied to the mixer 43 to fluidize the fluidized bed 43A therein and continuously pneumatically transport a premix of a plurality of types of fine particles p from the fine particle feeder 42. The mixture reaches the mixer 43. Each of the fine particles p enters the fluidized bed 43A fluidized by the air flow after humidity control in a state where the primary particles and the secondary particles are mixed, and adheres to the surface of the coarse particles P, and then the coarse particles P collide with each other. The secondary particles become primary particles due to friction, flow out of the mixer 43, and are collected by the bag filter 44 as a homogeneous mixture of the fine particles p.
【００２７】次に、図４に示す試験装置を用いた本発明
の混合方法の試験例について説明する。 ［試験例１］本試験例では調湿器５１から調湿後の空気
を下記条件でガラスビーズを流動層４３Ａとする混合器
４３へ供給して流動層４３Ａを流動化する一方、微粒子
供給機４２から二種類の微粒子ｐの混合物を下記条件で
混合器４３へ供給し、混合器４３において二種類の微粒
子ｐを混合した後、混合物をバグフィルタ４４で回収し
た。そして、バグフィルタ４４で回収された混合物を目
視観察したところ、アルミナと石灰石が一次粒子レベル
で均質に混合していることが判った。 混合器（塩化ビニル製円筒）：内径１０ｃｍ、高さ１００ｃｍ ガラスビーズ（粗粒子） ：６００μｍ ガラスビーズの充填量 ：２０００ｇ 静止層高 ：１７ｃｍ 流動化空気速度 ：０．８ｍ／秒 微粒子 ：１μｍのアルミナ、１μｍの石灰石 アルミナの供給速度 ：２６ｇ／分 石灰石の供給速度 ：２６ｇ／分Next, a test example of the mixing method of the present invention using the test apparatus shown in FIG. 4 will be described. Test Example 1 In this test example, air after humidity control was supplied from a humidity controller 51 to a mixer 43 having glass beads as a fluidized bed 43A under the following conditions to fluidize the fluidized bed 43A, while a fine particle feeder was used. A mixture of two types of fine particles p was supplied from 42 to a mixer 43 under the following conditions. After mixing the two types of fine particles p in the mixer 43, the mixture was collected by a bag filter 44. When the mixture collected by the bag filter 44 was visually observed, it was found that alumina and limestone were homogeneously mixed at the primary particle level. Mixer (vinyl chloride cylinder): inner diameter 10 cm, height 100 cm Glass beads (coarse particles): 600 μm Filling amount of glass beads: 2000 g Stationary bed height: 17 cm Fluidized air velocity: 0.8 m / sec Fine particles: 1 μm alumina 1 μm limestone Alumina feed rate: 26 g / min Limestone feed rate: 26 g / min
【００２８】［試験例２］本試験例では粗粒子Ｐの条
件、微粒子ｐの条件及び流動化空気速度を変えて下記の
二種類の微粒子ｐを混合し、バグフィルタ４４で回収さ
れた混合物を目視観察したところ、アルミナと酸化チタ
ンが一次粒子レベルで均質に混合していることが判っ
た。 混合器（塩化ビニル製円筒）：内径１０ｃｍ、高さ１００ｃｍ シリカサンド（粗粒子） ：５００μｍ ガラスビーズの充填量 ：１５００ｇ 静止層高 ：１３ｃｍ 流動化空気速度 ：０．６ｍ／秒 微粒子 ：１μｍのアルミナ、０．５μｍの酸化チタン アルミナの供給速度 ：２５ｇ／分 酸化チタンの供給速度 ：１５ｇ／分Test Example 2 In this test example, the following two kinds of fine particles p were mixed by changing the conditions of the coarse particles P, the conditions of the fine particles p, and the fluidizing air velocity, and the mixture recovered by the bag filter 44 was used. Visual observation revealed that alumina and titanium oxide were homogeneously mixed at the primary particle level. Mixer (vinyl chloride cylinder): Inner diameter 10 cm, height 100 cm Silica sand (coarse particles): 500 μm Filling amount of glass beads: 1500 g Stationary bed height: 13 cm Fluidizing air velocity: 0.6 m / sec Fine particles: 1 μm alumina 0.5 μm titanium oxide Alumina supply rate: 25 g / min Titanium oxide supply rate: 15 g / min
【００２９】尚、本発明は上記各実施形態に何等制限さ
れるものではない。例えば、上記各実施形態では無機物
からなる微粒子ｐを混合する場合について説明したが、
有機物（例えば、合成樹脂等の微粒子）に対しても適用
できることは云うまでもない。また、上記各実施形態で
は微粒子供給機１５、２５から配管１４、２４を介して
混合器１０、２０のコーン部１１Ｂ、２１Ｂを経由させ
て直胴部１１Ａ、２１Ａへ微粒子ｐを供給する場合につ
いて説明したが、配管１４、２４を混合器１０、２０の
直胴部１１Ａ、２１Ａへ接続し、微粒子供給機１５、２
５から直胴部１１Ａ、２１Ａへ微粒子ｐを直接供給する
ようにしても良い。The present invention is not limited to the above embodiments. For example, in each of the embodiments described above, the case where the fine particles p made of an inorganic substance are mixed is described.
It is needless to say that the present invention can be applied to organic substances (for example, fine particles such as synthetic resin). In each of the above embodiments, the fine particles p are supplied from the fine particle feeders 15 and 25 to the straight body portions 11A and 21A via the pipes 14 and 24 and the cone portions 11B and 21B of the mixers 10 and 20. As described above, the pipes 14 and 24 are connected to the straight body portions 11A and 21A of the mixers 10 and 20, and the fine particle feeders 15 and 2 are connected.
Alternatively, the fine particles p may be directly supplied to the straight body portions 11A and 21A from the portion 5.
【００３０】[0030]
【発明の効果】以上説明したように本発明の請求項１〜
５に記載の発明によれば、凝集して二次粒子を形成し易
いサブミクロンオーダーの微粒子であっても複数種類の
微粒子をそれぞれ二次粒子から一次粒子へと解砕して一
次粒子レベルで均質に混合することができる微粒子の混
合方法を提供することができる。According to the present invention, as described above,
According to the invention described in 5, even sub-micron-order fine particles that are easily aggregated to form secondary particles, a plurality of types of fine particles are each crushed from secondary particles to primary particles, and at the primary particle level. It is possible to provide a method of mixing fine particles which can be mixed homogeneously.
【図１】本発明の混合方法を実施する際に用いられる流
動層の一例を示す模式図である。FIG. 1 is a schematic diagram showing an example of a fluidized bed used when performing a mixing method of the present invention.
【図２】（ａ）、（ｂ）はそれぞれ流動層の粗粒子同士
が衝突、摩擦を繰り返して微粒子の二次粒子を一次粒子
に解砕する状況を説明するための説明図である。FIGS. 2 (a) and 2 (b) are explanatory diagrams for explaining a situation in which coarse particles of a fluidized bed repeatedly collide and rub each other to break up secondary particles of fine particles into primary particles.
【図３】本発明の混合方法を実施する際に用いられる流
動層の他の一例を示す模式図である。FIG. 3 is a schematic diagram showing another example of a fluidized bed used when performing the mixing method of the present invention.
【図４】本発明の混合方法を検証するための試験装置を
示す模式図である。FIG. 4 is a schematic diagram showing a test apparatus for verifying the mixing method of the present invention.
１０、２０ 混合器 １１、２１ 容器 １２、２２ 流動層 １３ 分散板 Ｐ 粗粒子 ｐ 微粒子（一次粒子） ｐ’ 微粒子（二次粒子） 10, 20 Mixer 11, 21 Container 12, 22 Fluidized bed 13 Dispersion plate P Coarse particle p Fine particle (primary particle) p 'Fine particle (secondary particle)
Claims (5)
粗粒子を流動化し、その流動層へ凝集性のある種類の異
なる複数種の微粒子を供給し、凝集した各種の微粒子を
上記流動層において解砕しながら混合することを特徴と
する微粒子の混合方法。1. A method comprising: supplying a gas to a fluidized bed composed of coarse particles to fluidize the coarse particles; supplying a plurality of types of fine particles having different types of cohesiveness to the fluidized bed; A method for mixing fine particles, wherein mixing is performed while crushing in a layer.
粒子径からなる微粒子を供給することを特徴とする請求
項１に記載の微粒子の混合方法。2. The method for mixing fine particles according to claim 1, wherein fine particles having a particle diameter of 0.1 to 20 μm are supplied as each of the fine particles.
の粒子径の粗粒子を用いることを特徴とする請求項１ま
たは請求項２に記載の微粒子の混合方法。3. The particle size of the coarse particles is 300 to 1500 μm.
The method for mixing fine particles according to claim 1 or 2, wherein coarse particles having a particle diameter of (1) are used.
粗粒子を用いることを特徴とする請求項１〜請求項３の
いずれか１項に記載の微粒子の混合方法。4. The method for mixing fine particles according to claim 1, wherein coarse particles having a uniform particle diameter are used as the coarse particles.
を用いることを特徴とする請求項１〜請求項４のいずれ
か１項に記載の微粒子の混合方法。5. The method for mixing fine particles according to claim 1, wherein the dispersion plate type fluidized bed or the spouted fluidized bed is used.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000101781A JP2001276594A (en) | 2000-04-04 | 2000-04-04 | Method for mixing fine particles with fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000101781A JP2001276594A (en) | 2000-04-04 | 2000-04-04 | Method for mixing fine particles with fluidized bed |
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| Publication Number | Publication Date |
|---|---|
| JP2001276594A true JP2001276594A (en) | 2001-10-09 |
Family
ID=18615764
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102614801A (en) * | 2012-03-14 | 2012-08-01 | 东南大学 | Ultrafine particle mixing device |
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| JPS61209032A (en) * | 1985-03-12 | 1986-09-17 | Res Dev Corp Of Japan | Method and apparatus for mixing ultra-fine particles |
| JPS63283728A (en) * | 1987-05-14 | 1988-11-21 | Chuo Kakoki Kk | Powder material dispersing and mixing device |
| JPH0268151A (en) * | 1988-09-01 | 1990-03-07 | Matsushita Electric Ind Co Ltd | Medium stirring type pulverizer |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102614801A (en) * | 2012-03-14 | 2012-08-01 | 东南大学 | Ultrafine particle mixing device |
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