JPS597500B2 - Stirred fluidized bed equipment - Google Patents
Stirred fluidized bed equipmentInfo
- Publication number
- JPS597500B2 JPS597500B2 JP3780680A JP3780680A JPS597500B2 JP S597500 B2 JPS597500 B2 JP S597500B2 JP 3780680 A JP3780680 A JP 3780680A JP 3780680 A JP3780680 A JP 3780680A JP S597500 B2 JPS597500 B2 JP S597500B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- raw material
- distribution plate
- product
- gas distribution
- 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.)
- Expired
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/382—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it with a rotatable device only
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Description
【発明の詳細な説明】
本発明は、流動層により粉粒状物質（以下、原料粉とい
う。DETAILED DESCRIPTION OF THE INVENTION The present invention provides a method for producing powdery granular materials (hereinafter referred to as raw material powder) using a fluidized bed.
）を加熱してある種の反応を起させ、その際における粒
子相互の固着は攪拌により防ぐ攪拌式流動層装置に関す
る。This invention relates to a stirred fluidized bed apparatus in which particles are heated to cause a certain reaction, and particles are prevented from sticking to each other by stirring.
流動層において６００℃以上の還元雰囲気で、数μない
し数十μの鉄粉を脱炭し、あるいは数μないし数十μの
酸化鉄粉を還元したり、又はセメント原料粉を１３５０
℃以上で暁成しクリンカーを製造しようとする場合、上
記の原料粉は、流動層内で反応によって表面に粘着力を
有するようになり、その粘着力による造粒作用により、
造粒しつつ大径化して当初の微粉時に設定される作動ガ
スの空塔速度では流動化が不能となり、遂には大粒子相
互が固着して固塊状になることが知られている。In a fluidized bed in a reducing atmosphere at 600°C or higher, iron powder of several microns to several tens of microns is decarburized, iron oxide powder of several microns to several tens of microns is decarburized, or cement raw material powder is decarburized to 1350°C.
When attempting to produce clinker by forming at temperatures above ℃, the above-mentioned raw material powder becomes sticky on the surface due to reaction in the fluidized bed, and due to the granulation effect due to the sticky force,
It is known that during granulation, the particle size increases and fluidization becomes impossible at the superficial velocity of the working gas set at the time of initial pulverization, and eventually the large particles stick to each other and form a solid lump.
そこで従来では反応過程における粒子相互の固着を防止
するために、第１図に示すように流動層１′の下部を絞
ってこの部分にガス分散板２′を設け、これにより作動
ガスＧの速度を増加させて原料粉Ｍをその粒子が相互に
衝突するよう激しく攪拌せしめたり、あるいは、第２図
に示すように流動層１内に攪拌機３を設け、その回転羽
根４をガス分散板２′に沿い定速で回転させて原料粉Ｍ
を攪拌せしめたりしている。Conventionally, in order to prevent the particles from sticking to each other during the reaction process, the lower part of the fluidized bed 1' is squeezed and a gas dispersion plate 2' is provided in this area, as shown in Fig. 1, which increases the velocity of the working gas G. Alternatively, as shown in FIG. 2, a stirrer 3 may be provided in the fluidized bed 1 and its rotating blades 4 may be connected to the gas dispersion plate 2'. The raw material powder M is rotated at a constant speed along the
The mixture is stirred.
しかしながら、第１図に示す噴流式動層装置や第２図に
示す攪拌式流動層装置では、原料粉Ｍが流動層で反応を
完結するためにはその温度によりかなり異なるが数分な
いし数十分の滞留時間が必要であるにもかかわらず、新
たに投入された原料粉Ｍが成品Ｐあるいはこれに近いも
のに直に混合してしまって、流動層から取出されるもの
は未反応粉子から反応を完結した粉子までほぼ均等に分
布する事になるから、原料粉Ｍの個々の粒子が反応にあ
ずかる時間はまちまちとなり、従って取出される成品Ｐ
の品質が一定しない欠点があった。However, in the spouted fluidized bed apparatus shown in FIG. 1 and the stirred fluidized bed apparatus shown in FIG. Even though a residence time of 30 minutes is required, the newly introduced raw material powder M is directly mixed with the product P or something similar to it, and what is taken out from the fluidized bed is unreacted powder. Since the powder from which the reaction has been completed is almost evenly distributed, the time that each particle of the raw material powder M participates in the reaction varies, and therefore the product P to be taken out.
The drawback was that the quality was inconsistent.
本発明は前記従来の問題点を解決するために創案された
もので、その目的は原料粉の固着による弊害を防止しつ
つ各粒子の反応時間（滞留時間）をできるだけ一定に保
って成品の品質を向上させうる攪拌式流動層装置を提供
することにある。The present invention was devised to solve the above-mentioned conventional problems, and its purpose is to maintain the reaction time (residence time) of each particle as constant as possible while preventing the adverse effects caused by the sticking of raw material powder, thereby improving the quality of the finished product. An object of the present invention is to provide an agitated fluidized bed apparatus that can improve the performance.
以下、本発明を第３図〜第５図に示す実施例により説明
すると、円筒状の流動層罐体５の下部にはガス分散板２
が、さらにその下段に作動ガス入口管６に連なるウイン
ドボックス７が設けられ、また流動層罐体５内にはその
中心を通る回転軸８の下端部周りに放射状に取付けた多
数枚の回転羽根４がガス分散板２に沿い図示矢印方向に
回転するよう設けられている。Hereinafter, the present invention will be explained with reference to the embodiments shown in FIGS.
However, a wind box 7 connected to the working gas inlet pipe 6 is further provided at the lower stage, and a large number of rotating blades are installed radially around the lower end of a rotating shaft 8 passing through the center of the fluidized bed housing 5. 4 is provided to rotate along the gas distribution plate 2 in the direction of the arrow shown in the figure.
ガス分散板２はこの回転羽根４により成品Ｐを払出せる
ような切欠状の成品取出口９を有し、この成品取出口９
０羽根回転方向前後のある範囲（図示Ｃ，Ａの範囲）に
は、これを作動ガスＧの通過を防《゛構造として粉粒体
堆積部１３．１４が設けられ、その他の範囲（一示Ｂの
範囲）だけ作動ガスＧが通過する構造とされている。The gas distribution plate 2 has a cutout-shaped product outlet 9 through which the product P can be discharged by the rotating blade 4.
In a certain range before and after the rotation direction of the zero blade (ranges C and A shown in the figure), a powder accumulation part 13.14 is provided with a structure to prevent the passage of the working gas G, and in other ranges (the range shown in the figure) The structure is such that the working gas G passes through only the range B).
このようなガス分散板２の範囲Ｂ内の攪拌始め部上に原
料粉Ｍが供給できるよう流動層罐体５の下側部には原料
入口ダウンカマー１０が設けられ、また、成品取出口９
には成品出ロシュート１１がウインドボックス７から仕
切って設けられている。A raw material inlet downcomer 10 is provided at the lower part of the fluidized bed housing 5 so that the raw material powder M can be supplied onto the stirring start part within the range B of the gas distribution plate 2, and a product outlet 9
A finished product output roaster chute 11 is provided separated from the wind box 7.
前記回転羽根４は回転軸８の外端部に設けた回転制御手
段（図示せず）によって例えば１５分間に１回転の回転
速度カ積−できるものとされている。The rotating blade 4 is capable of accumulating a rotational speed of one rotation per 15 minutes, for example, by a rotation control means (not shown) provided at the outer end of the rotating shaft 8.
図中１２はガス出口管を示す。In the figure, 12 indicates a gas outlet pipe.
以上の構成において、原料粉Ｍは、原料入口ダウンカマ
−１０を通じガス分散板２上に供給される。In the above configuration, the raw material powder M is supplied onto the gas distribution plate 2 through the raw material inlet downcomer 10.
このとき、ガス分散板２に作動ガスＧを下から通過させ
ればこの原料粉Ｍがガス分散板２で均一に分散された行
動ガスＧにより流動化されるから、回転羽根４を回転さ
せれば、原料紛Ｍは、漸次反応しながら図示の羽根回転
方向に進行し、反応の進行に伴い造粒に支障がある粒子
相互の固着は回転羽根４による攪拌で防止されている。At this time, if the working gas G is passed through the gas distribution plate 2 from below, the raw material powder M will be fluidized by the working gas G uniformly dispersed by the gas distribution plate 2, so the rotating blade 4 can be rotated. For example, the raw material powder M advances in the direction of rotation of the illustrated blades while gradually reacting, and as the reaction progresses, the particles are prevented from sticking to each other, which would hinder granulation, by stirring by the rotating blades 4.
しかも、ガス分散板２の粉粒体堆積部１３に至ると作動
ガスＧが通過せずそれによる流動化機能はない。Moreover, when the working gas G reaches the particulate matter accumulation section 13 of the gas distribution plate 2, the working gas G does not pass therethrough, so there is no fluidization function.
従って、原料粉Ｍは、反応を完結し、かつ良好に造粒し
た成品Ｐとなってその安息角以下の角度でガス分散板２
の範囲Ｃ上に堆積する。Therefore, the raw material powder M completes the reaction and becomes a well-granulated product P, and the gas distribution plate 2
It is deposited on range C of .
また、回転羽根４が第５図に示す状態にあれば、原料粉
Ｍの一部は、作動ガスＧにより流動化されて、ガス分散
板２の範囲Ｃと同様に作動ガスＧが通過しない粉粒体堆
積部１４上に原料粉Ｍの安息角以下の角度で堆積する。Furthermore, when the rotary blade 4 is in the state shown in FIG. The particles are deposited on the particle deposition section 14 at an angle equal to or less than the angle of repose of the raw material powder M.
この場合当該粉粒体堆積部１３，１４の大きさを調節し
ておけば成品取出口９まで流動化された原料粉Ｍと成品
Ｐが飛んで落込むのを防ぐことができる。In this case, by adjusting the sizes of the powder and granular material accumulation parts 13 and 14, it is possible to prevent the fluidized raw material powder M and product P from flying up to the product outlet 9 and falling.
ガス分散板２の粉粒体堆積部１４上の原料粉Ｍと粉粒体
堆積部１３上の成品Ｐとは、回転羽根４によって範囲Ｂ
に至らない限り流動化することはなく、流動化している
粉粒体（原料粉、成品）の堰となる。The raw material powder M on the powder/granular material accumulation section 14 of the gas distribution plate 2 and the product P on the powder/granular material accumulation section 13 are separated by the rotating blade 4 into a range B.
It will not become fluidized unless it reaches this point, and will act as a dam for the fluidized powder (raw material powder, finished product).
ガス分散板２の粉粒体堆積部１３上の成品Ｐは、回転羽
根４によって成品取出口９へと払落され成品出ロシュー
ト１１を経て装置外部に取出される。The product P on the particulate matter accumulation section 13 of the gas distribution plate 2 is swept off by the rotary blade 4 to the product outlet 9 and taken out to the outside of the apparatus via the product output chute 11.
また、ガス分散板２の粉粒体堆積部１４上の原料粉Ｍは
、やはり流動化した原料粉Ｍの堰となりつつ回転羽根４
によって範囲Ｂへと移動させられて作動ガスＧにより再
び流動化する。In addition, the raw material powder M on the powder/granular material accumulation part 14 of the gas distribution plate 2 acts as a dam for the fluidized raw material powder M, and the rotating blade 4
is moved to range B by the working gas G and fluidized again by the working gas G.
他方、回転羽根４の回転速度を回転制御手段によって変
更することによりガス分散板２の粉粒体堆積部１３．１
４上に形成された堰の高さが任意に変えられるから、原
料粉Ｍの各粒子の流動層内での滞留時間をできるだけ最
適値に設定することができる。On the other hand, by changing the rotational speed of the rotary blade 4 by the rotation control means, the particulate material accumulation section 13.1 of the gas distribution plate 2 is
Since the height of the weir formed on the weir 4 can be changed arbitrarily, the residence time of each particle of the raw material powder M in the fluidized bed can be set to the optimum value as possible.
以上の通り本発明は、原料粉の粒子の反応時間（滞留時
間）を＝定に、それも最適値に設定することができると
共に、原料粉の粒子の固着を防止し、これによる幣害を
回避できる構成であるから成品品質を確実に向上させる
ことができる。As described above, the present invention makes it possible to set the reaction time (residence time) of the raw material powder particles to a constant value, and also to an optimal value, and also prevents the sticking of the raw material powder particles and prevents damage caused by this. Since the configuration allows avoidance, the quality of finished products can be reliably improved.
また簡単な構成で済むから、容易にかつ低コストで製作
できる。Furthermore, since it requires a simple configuration, it can be manufactured easily and at low cost.
第１図は従来の噴流式流動層装置の縦断面図、第２図は
従来の攪拌式流動層装置の縦断面図、第３図，第４図，
第５図は本発明の実施例を示す縦断面図、平面図、第３
図のｖ−ｖ線断面図である。
１，１′・・・・・・流動層、２，２′・・・・・・ガ
ス分散板、３・・・・・攪拌機、４・・・・・・回転羽
根、５・・・・・・流動層罐体、６・・・・・・作動ガ
ス入口管、Ｔ・・・・・・ウィンドボックス、８・・・
・・・回転軸、９・・・・・・成品取出口、１０・・・
・・・原料入口ダウンカマー、１１・・・・・・成品出
ロシュート、１２・・・・・・ガス出口管、Ｍ・・・・
・・原料粉、Ｇ・・・・・・作動ガス、Ｐ・・・・・・
成品。Figure 1 is a vertical cross-sectional view of a conventional spouted fluidized bed apparatus, Figure 2 is a vertical cross-sectional view of a conventional stirred fluidized bed apparatus, Figures 3 and 4,
FIG. 5 is a vertical sectional view, a plan view, and a third view showing an embodiment of the present invention.
It is a sectional view taken along the v-v line in the figure. 1, 1'... Fluidized bed, 2, 2'... Gas distribution plate, 3... Stirrer, 4... Rotating blade, 5... ... Fluidized bed housing, 6 ... Working gas inlet pipe, T ... Wind box, 8 ...
...Rotating shaft, 9...Product outlet, 10...
...Raw material inlet downcomer, 11...Product output roschutes, 12...Gas outlet pipe, M...
・・Raw material powder, G・・Working gas, P・・・・
Finished product.
Claims (1)
分散板に沿い回転可能で、かつ、回転数を制御可能な攪
拌用回転羽根を設置し、前記ガス分散板に回転羽根によ
り成品を払出せるような成品取出口を設け、かつ．、該
成品取出口の羽根回転方向前後のある範囲を作動ガスが
通過するを防ぐように形成した粉粒体堆積部としたこと
を特徴とする攪拌式流動層装置。1. A stirring rotary blade that can rotate along the gas distribution plate and whose rotation speed can be controlled is installed on the gas distribution plate disposed in the fluidized bed housing, and the product is transferred to the gas distribution plate by the rotation blade. Provide a product outlet for dispensing the product, and. An agitated fluidized bed apparatus, characterized in that a particulate material accumulation part is formed to prevent working gas from passing through a certain range before and after the product outlet in the direction of blade rotation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3780680A JPS597500B2 (en) | 1980-03-25 | 1980-03-25 | Stirred fluidized bed equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3780680A JPS597500B2 (en) | 1980-03-25 | 1980-03-25 | Stirred fluidized bed equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56133025A JPS56133025A (en) | 1981-10-17 |
| JPS597500B2 true JPS597500B2 (en) | 1984-02-18 |
Family
ID=12507748
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3780680A Expired JPS597500B2 (en) | 1980-03-25 | 1980-03-25 | Stirred fluidized bed equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS597500B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62207027A (en) * | 1986-03-07 | 1987-09-11 | Sony Corp | Compression digitizing circuit for sound signal |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60118233A (en) * | 1983-11-29 | 1985-06-25 | Mitsui Eng & Shipbuild Co Ltd | Bowling-pin with rounded bottom shaped fluidized layer reaction apparatus |
-
1980
- 1980-03-25 JP JP3780680A patent/JPS597500B2/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62207027A (en) * | 1986-03-07 | 1987-09-11 | Sony Corp | Compression digitizing circuit for sound signal |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56133025A (en) | 1981-10-17 |
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