JPS5830209B2 - Separation and transportation method of powder and granular materials - Google Patents
Separation and transportation method of powder and granular materialsInfo
- Publication number
- JPS5830209B2 JPS5830209B2 JP55114689A JP11468980A JPS5830209B2 JP S5830209 B2 JPS5830209 B2 JP S5830209B2 JP 55114689 A JP55114689 A JP 55114689A JP 11468980 A JP11468980 A JP 11468980A JP S5830209 B2 JPS5830209 B2 JP S5830209B2
- Authority
- JP
- Japan
- Prior art keywords
- powder
- gas
- granules
- fluidized bed
- cyclone
- 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
Landscapes
- Air Transport Of Granular Materials (AREA)
Description
【発明の詳細な説明】
本発明は石炭、鉱石、石灰石等の粉粒体を分離輸送する
方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for separating and transporting granular materials such as coal, ore, and limestone.
ガス輸送された粉粒体を分離するため、従来は第1図に
示すごときサイクロンが使用されている。Conventionally, a cyclone as shown in FIG. 1 has been used to separate the gas-transported powder and granular material.
第1図において、粉粒体の混入したガスaは本体すの接
線方向よりその中に入り、粉粒体は本体す内において回
転力による遠心力により本体す内壁側に飛散させられ、
内壁に沿い重力により落下して粉粒体出口Cより外部へ
取出され、一方分離されたガスは上部ガス出口dより大
気中へ排出される。In FIG. 1, gas a mixed with powder and granules enters the main body from the tangential direction, and the powder and granules are scattered toward the inner wall of the main body by centrifugal force due to rotational force within the main body.
The powder falls due to gravity along the inner wall and is taken out from the powder outlet C, while the separated gas is discharged into the atmosphere from the upper gas outlet d.
しかるに前記サイクロンにおいては、
1)粉粒体が本体す内壁に衝突するため装置の損傷が激
しい。However, in the above-mentioned cyclone, 1) the granular material collides with the inner wall of the main body, causing severe damage to the device;
11)ガス中中の粉粒体量の増加により、サイクロンの
分離性能が低下する。11) Separation performance of the cyclone decreases due to an increase in the amount of powder in the gas.
111)粉粒体の混入したガスはサイクロンに対し水平
方向から流入するため、下方から上方へガスを送る場合
には、サイクロン入口前に必ず曲管を必要とし、該曲管
部での輸送管の摩耗が激しい。111) Gas mixed with powder and granules flows horizontally into the cyclone, so when sending gas from below to above, a bent pipe is always required before the cyclone entrance, and the transport pipe at the bent pipe part Severe wear.
等の欠点がある。There are drawbacks such as.
本発明は従来手段の有する前述の欠点を除去することを
目的としてなしたもので、粉粒体を混入したガスを直管
状の輸送管により輸送し、該粉粒体を混入したガスを下
方より分離槽内に送給し、該分離槽内に収納され且つ前
記ガス中に混入された粉粒体と同じ材料の粉ね体を流動
化して流動層を形成させ、前記下方から上方へ送られる
ガス中の粉粒体を流動層により捕獲することによりガス
から分離し、流動層から排出されたガスをサイクロンに
送って微粉体を分離し、前記分離槽で分離させた微粉体
を分離槽側部に取付けた斜め下方に向いている溢流管へ
流出させると共に前記サイクロンで分離させた微粉体も
溢流管へ送り、粉粒体と微粉体とを一緒に溢流管から次
工程へ輸送することを特徴とするものである。The present invention has been made with the aim of eliminating the above-mentioned drawbacks of the conventional means, and involves transporting gas mixed with powder and granules through a straight transport pipe, and transporting the gas mixed with powder and granules from below. A powder body of the same material as the powder body contained in the separation tank and mixed in the gas is fluidized to form a fluidized bed, and the powder body is sent from the lower side to the upper side. Particles in the gas are separated from the gas by being captured by a fluidized bed, the gas discharged from the fluidized bed is sent to a cyclone to separate fine powder, and the fine powder separated in the separation tank is transferred to the separation tank side. At the same time, the fine powder separated by the cyclone is also sent to the overflow pipe, and the powder and fine powder are transported together from the overflow pipe to the next process. It is characterized by:
以下本発明の実施例を図面を参照しつつ説明する。Embodiments of the present invention will be described below with reference to the drawings.
第2図に示すように、上下方向へ延びる輸送管1の上方
に、粉粒体とガスにより流動層2を形成するのに適した
断面積を有する分離槽3を接続し、該分離槽3の側部で
流動層2の上面より多少下方に、斜め下方に向いた溢流
管4を接続し、該溢流管4の途中に粉粒体の排出量を制
御する流量制御弁5髄己設し前記分離槽3内部0上方に
サイクロン6を収納しガスを矢印X方向から該サイクロ
ン6に導入し得るように改サイクロン6の上部にガス出
口管7を取付け、サイクロン6の下部にサイクロン6で
分離された微粉体を排出する微粉体溢流管8を接続し、
該微粉体溢流管8を前記溢流管4の流量制御弁5を配設
した部分より上流側へ接続する。As shown in FIG. 2, a separation tank 3 having a cross-sectional area suitable for forming a fluidized bed 2 with powder and gas is connected above the transport pipe 1 extending in the vertical direction. An overflow pipe 4 facing diagonally downward is connected to a side part of the fluidized bed 2 slightly below the upper surface thereof, and a flow control valve 5 is installed in the middle of the overflow pipe 4 to control the discharge amount of powder and granules. A cyclone 6 is installed above the interior 0 of the separation tank 3, a gas outlet pipe 7 is attached to the upper part of the modified cyclone 6 so that gas can be introduced into the cyclone 6 from the direction of arrow X, and a cyclone 6 is installed in the lower part of the cyclone 6. Connect a fine powder overflow pipe 8 for discharging the fine powder separated by
The fine powder overflow pipe 8 is connected to the upstream side of the part of the overflow pipe 4 where the flow rate control valve 5 is provided.
粉粒体を混入したガスGは輸送管1を通って下方より分
離槽3内の流動層2に入る。Gas G mixed with powder and granules passes through a transport pipe 1 and enters a fluidized bed 2 in a separation tank 3 from below.
そうすると、ガスは流速が低下すると共に流動層2の流
動状態を維持させつつ該流動層2を形成する粉粒体間を
通り上昇する。Then, the flow rate of the gas decreases and the gas passes through the particles forming the fluidized bed 2 and rises while maintaining the fluidized state of the fluidized bed 2.
又ガスが流動層2を通っている間にガスに混入していた
粉粒体が該流動層2の粉粒体と衝突して捕獲され、該粉
粒体は流動層2の一部となる。Further, while the gas passes through the fluidized bed 2, the powder and granules mixed in the gas collide with the powder and granules of the fluidized bed 2 and are captured, and the powder and granules become part of the fluidized bed 2. .
粉粒体を分離されて流動層2上部へ出たガスは、分離槽
3上部よりサイクロン6に入り、該サイクロン6で微粉
体を分離され、ガス出口管7から外部へ排出される。The gas that has been separated from the powder and granules and exits to the upper part of the fluidized bed 2 enters the cyclone 6 from the upper part of the separation tank 3, where the cyclone 6 separates the fine powder, and the gas is discharged to the outside from the gas outlet pipe 7.
サイクロン6で分離された微粉体は微粉体温流管8を通
って溢流管4へ送られる。The fine powder separated by the cyclone 6 is sent to the overflow pipe 4 through a fine powder thermoflow pipe 8.
流動層2に捕獲された粉粒体が増加すると、流動層2の
レベルが高くなろうとするが、流量制御弁5を開いてレ
ベルが略一定の位置になるよう粉粒体を溢流管4から外
部へ排出する。As the amount of powder and granules captured in the fluidized bed 2 increases, the level of the fluidized bed 2 tends to rise, but by opening the flow rate control valve 5, the powder and granules are transferred to the overflow pipe 4 so that the level remains approximately constant. and discharged to the outside.
サイクロン6で分離されて微粉体温流管8へ送られた微
粉体も流動層を形成していた粉粒体と共に溢流管4を通
って外部へ排出される。The fine powder separated by the cyclone 6 and sent to the fine powder heat flow tube 8 is also discharged to the outside through the overflow tube 4 together with the powder and granules forming the fluidized bed.
第3図は第2図に示す装置を、燃料ガス中の硫化水素を
吸収剤9と反応させて除去する高温乾式脱硫装置へ実際
に適用した例を示し、吸収剤を収納した流動吸収塔10
の側部に流量制御弁12を有する溢流管11を斜め下方
に向けて取付け、該溢流管11の下端を輸送用流動層1
3を形成するようにした中間基14の側部に接続し、該
中間基14の下部に粉粒体用弁16を有する導管15を
接続すると共に該導管15の側部に流量制御弁18を有
する輸送用ガス管17を接続し、中間基14の上方に前
記輸送管1の下端を接続し、前記溢流管4の下端を再生
塔19の側部に接続する。FIG. 3 shows an example in which the device shown in FIG. 2 is actually applied to a high-temperature dry desulfurization device that removes hydrogen sulfide in fuel gas by reacting it with an absorbent 9.
An overflow pipe 11 having a flow rate control valve 12 is attached diagonally downward to the side of the transport fluidized bed 1.
A conduit 15 having a powder valve 16 is connected to the lower part of the intermediate base 14, and a flow rate control valve 18 is connected to the side of the conduit 15. The lower end of the transport pipe 1 is connected above the intermediate base 14, and the lower end of the overflow pipe 4 is connected to the side of the regeneration tower 19.
なお図中20は分離槽3内に設けた分散板、又図中第2
図に示す符号と同一の符号のものは同一のものを示す。In addition, 20 in the figure is the dispersion plate installed in the separation tank 3, and 20 in the figure
The same reference numerals as those shown in the figures indicate the same elements.
流動吸収塔10には、図示してないが燃料ガスが下方よ
り供給されると共に吸収剤が供給され、燃料ガスによっ
て吸収剤が流動化し、燃料ガス中の硫化水素は吸収剤に
吸収され、硫化水素の除去された燃料ガスは流動吸収塔
10より燃料消費機器へ送られる。Although not shown in the drawings, the fluidized absorption tower 10 is supplied with fuel gas from below and an absorbent.The absorbent is fluidized by the fuel gas, and the hydrogen sulfide in the fuel gas is absorbed by the absorbent and sulfurized. The fuel gas from which hydrogen has been removed is sent from the fluidized absorption tower 10 to fuel consuming equipment.
一方、流動吸収塔10内で硫化水素を吸収した吸収剤は
、溢流管11取付部まで上昇して該溢流管11内へ流出
し、該溢流管11を流下して中間基14に導入される。On the other hand, the absorbent that has absorbed hydrogen sulfide in the fluidized absorption tower 10 rises to the attachment part of the overflow pipe 11, flows out into the overflow pipe 11, flows down the overflow pipe 11, and reaches the intermediate group 14. be introduced.
又輸送用ガス管17からは、不活性ガス等の輸送用ガス
が中間基14に供給され、中間基14内の吸収剤は輸送
用ガスによりその層高が激しく変動し、流動化している
。Further, a transport gas such as an inert gas is supplied to the intermediate base 14 from the transport gas pipe 17, and the layer height of the absorbent in the intermediate base 14 fluctuates drastically due to the transport gas, making it fluid.
このため、輸送管1下端に達した吸収剤は、輸送用ガス
と共に輸送管1内に導入され、輸送管1を上昇して分離
槽3下部へ入る。Therefore, the absorbent that has reached the lower end of the transport pipe 1 is introduced into the transport pipe 1 together with the transport gas, ascends the transport pipe 1, and enters the lower part of the separation tank 3.
輸送管1より分離槽3へ導入された吸収剤を混入したガ
スは1分離槽3内でその流速が低下し。The flow rate of the gas mixed with the absorbent introduced from the transport pipe 1 into the separation tank 3 decreases within the separation tank 3.
流動層2を形成する吸収剤の間を通る間にガス中の吸収
剤が流動層2に衝突して捕獲される。While passing between the absorbents forming the fluidized bed 2, the absorbent in the gas collides with the fluidized bed 2 and is captured.
ガスは流動層2上部からサイクロン6に流入し、ここで
ガス中の微細な吸収剤が分離され、清浄になったガスは
外部へ排出され、微細な吸収剤は微粉体溢流管8より溢
流管4へ送られる。The gas flows into the cyclone 6 from the upper part of the fluidized bed 2, where the fine absorbent in the gas is separated, the purified gas is discharged to the outside, and the fine absorbent overflows from the fine powder overflow pipe 8. It is sent to flow tube 4.
又分離槽3で分離された吸収剤は、連続的に送られてく
る吸収剤を混入したガスにより流動層2を形成し、流動
化しつつ分散板20を通って上昇し、溢流管4へ流出し
、前記微粉体溢流管8より送られてきた微細な吸収剤と
共に再生塔19へ送られ、ここで再生されて再び使用に
供される。In addition, the absorbent separated in the separation tank 3 forms a fluidized bed 2 with the gas mixed with the absorbent that is continuously sent, rises through the dispersion plate 20 while being fluidized, and flows into the overflow pipe 4. It flows out and is sent to the regeneration tower 19 together with the fine absorbent sent from the fine powder overflow pipe 8, where it is regenerated and used again.
なお本発明の実施例は、前述の実施例に限定されるもの
ではなく、本発明の要旨を逸脱しない範曲内で種々変更
を加え得ることは勿論である。Note that the embodiments of the present invention are not limited to the above-described embodiments, and it goes without saying that various changes may be made within the range without departing from the gist of the present invention.
本発明の粉粒体の分離輸送方法は、前述のごとき構成で
あるから、下記のごとき種々の優れた効果を奏し得る。Since the method for separating and transporting granular materials of the present invention has the above-described configuration, it can achieve various excellent effects as described below.
■)ガス中の粉粒体を該粉粒体と同じ粉粒体で形成され
る流動層により捕獲するため、ガス中の粉ね体が装置に
直接ぶつかることが少なく、従って装置の摩耗、損傷が
少なくなる。■) Powder in the gas is captured by a fluidized bed made of the same powder as the powder, so the powder in the gas rarely hits the equipment directly, resulting in wear and tear on the equipment. becomes less.
■)構造が簡単なため、高温、高圧下での使用ができる
。■) Due to its simple structure, it can be used at high temperatures and high pressures.
■)輸送管を曲部のない直管にできるため、輸送管の摩
耗、損傷が少ない。■) Since the transport pipe can be made straight without any bends, there is less wear and damage to the transport pipe.
■)捕獲した微粉体は流動層外で粉粒体と合流させるの
で、流動層内で再循環することがない。(2) The captured fine powder is combined with the powder outside the fluidized bed, so there is no recirculation within the fluidized bed.
第1図イ2口は従来例の説明図、第2@は本発明の説明
図、第3図は第2図のものを燃料ガス中の硫化水素を吸
収する吸収剤の分離輸送に使用した場合の説明図である
。
図中1は輸送管、2は流動層、3は分離槽、4は溢流管
、6はサイクロン、8は微粉体溢流管を示す。Figure 1 A 2 is an explanatory diagram of the conventional example, 2 @ is an explanatory diagram of the present invention, and Figure 3 is the one in Figure 2 used for separating and transporting an absorbent that absorbs hydrogen sulfide in fuel gas. FIG. In the figure, 1 is a transport pipe, 2 is a fluidized bed, 3 is a separation tank, 4 is an overflow pipe, 6 is a cyclone, and 8 is a fine powder overflow pipe.
Claims (1)
し、該粉粒体を混入したガスを下方より分離槽内に送給
し、該分離槽内に収納され且つ前記ガス中に混入された
粉粒体と同じ材料の粉粒体を流動化して流動層を形成さ
せ、前記下方から上方へ送られるガス中の粉粒体を流動
層により捕獲することによりガスから分離し、流動層か
ら排出されたガスをサイクロンに送って微粉体を分離し
、前記分離槽で分離させた微粉体を分離槽側部に取付け
た斜め下方に向いている溢流管へ流出させると共に前記
サイクロンで分離させた微粉体も溢流管へ送り、粉粒体
と微粉体とを一緒に溢流管から次工程へ輸送することを
特徴とする粉粒体の分離輸送方法。1. Transport the gas mixed with powder and granules through a straight transport pipe, feed the gas mixed with the powder and granules from below into a separation tank, and store the gas in the separation tank and mix it into the gas. The powder and granules made of the same material as the powder and granules are fluidized to form a fluidized bed, and the powder and granules in the gas sent from the bottom to the top are captured by the fluidized bed and separated from the gas. The gas discharged from the tank is sent to a cyclone to separate fine powder, and the fine powder separated in the separation tank is flowed out to an overflow pipe that is attached to the side of the separation tank and faces diagonally downward, and is separated by the cyclone. A method for separating and transporting powder and granular material, characterized in that the resulting fine powder is also sent to an overflow pipe, and the powder and granule are transported together from the overflow pipe to the next process.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP55114689A JPS5830209B2 (en) | 1980-08-22 | 1980-08-22 | Separation and transportation method of powder and granular materials |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP55114689A JPS5830209B2 (en) | 1980-08-22 | 1980-08-22 | Separation and transportation method of powder and granular materials |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS5742423A JPS5742423A (en) | 1982-03-10 |
JPS5830209B2 true JPS5830209B2 (en) | 1983-06-28 |
Family
ID=14644167
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP55114689A Expired JPS5830209B2 (en) | 1980-08-22 | 1980-08-22 | Separation and transportation method of powder and granular materials |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS5830209B2 (en) |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5364387A (en) * | 1976-11-17 | 1978-06-08 | Sintokogio Ltd | Method and apparatus for pneumatically conveying powder |
-
1980
- 1980-08-22 JP JP55114689A patent/JPS5830209B2/en not_active Expired
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5364387A (en) * | 1976-11-17 | 1978-06-08 | Sintokogio Ltd | Method and apparatus for pneumatically conveying powder |
Also Published As
Publication number | Publication date |
---|---|
JPS5742423A (en) | 1982-03-10 |
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