JPS6343134B2 - - Google Patents
Info
- Publication number
- JPS6343134B2 JPS6343134B2 JP59001967A JP196784A JPS6343134B2 JP S6343134 B2 JPS6343134 B2 JP S6343134B2 JP 59001967 A JP59001967 A JP 59001967A JP 196784 A JP196784 A JP 196784A JP S6343134 B2 JPS6343134 B2 JP S6343134B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- dust
- prevention plate
- dust collector
- swirling
- 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
- 239000000428 dust Substances 0.000 claims description 106
- 230000002265 prevention Effects 0.000 claims description 24
- 238000003466 welding Methods 0.000 description 10
- 239000002245 particle Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 6
- 238000000227 grinding Methods 0.000 description 6
- 238000005498 polishing Methods 0.000 description 6
- 239000004677 Nylon Substances 0.000 description 3
- IDCBOTIENDVCBQ-UHFFFAOYSA-N TEPP Chemical compound CCOP(=O)(OCC)OP(=O)(OCC)OCC IDCBOTIENDVCBQ-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229920001778 nylon Polymers 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 1
- 239000003365 glass fiber Substances 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
- B04C3/06—Construction of inlets or outlets to the vortex chamber
Description
〔発明の利用分野〕
この発明は、粒子径が10μm〜２mmの範囲に分
布する粉じんを、効率よく捕集する遠心力集じん
機に関するものである。
〔発明の背景〕
グラインダ等による研摩、研削作業やアーク溶
接およびガス溶接等の溶接作業等に伴つて発生す
る粉じんは、作業場の環境を汚染するので、集じ
ん機を設置して粉じんを捕集し、作業場の環境を
改善している。
グラインダ等による研摩、研削作業時に鋼材や
砥石から飛散する粉じんは、鋼材と砥石との摩擦
によつて発生する熱のために、また、アーク溶接
およびガス溶接等の溶接作業時に飛散するスラグ
や溶融金属の小粉子等の粉じんすなわちスパツタ
は、アークやガス炎による熱のために、ともに、
数100℃から1000℃を超える温度に加熱されてお
り、粉子径はともに0.1μm〜２mmの範囲に分布し
ている。この内、粉子径が0.1μm〜20μmの範囲
の粉じんは例えばバグフイルタ等のろ過集じん機
によつて、また、10μm〜２mmの範囲の粉じんは
例えばルーパ形等の慣性力集じん機または例えば
サイクロン形等の遠心力集じん機によつて、夫々
捕集するのが効果的である。
ろ過集じん機のろ布材としては、最高連続使用
温度が250℃のガラスフアイバは高価であるので、
大部分は最高連続使用温度110℃〜150℃のナイロ
ンやテトロンが用いられる。しかし前記のよう
に、粉じんの温度は数100℃〜1000℃以上である
ため、ナイロンやテトロンから成るろ布は焼損す
るので、集じん効率が低下することがある。それ
故、個々の粉じんの粒子が保有する熱量と、粉じ
んが発生源からろ布に到達するまでの時間とを検
討した結果、まず、慣性力集じん機または遠心力
集じん機によつて、粉子径50μm以上の粉じんを
捕集してからろ過集じん機を使用するようにすれ
ば、粉じんが発生してからろ過集じん機に到達す
るまでの時間を長くすることができる。したがつ
て、粉じん発生時は数100℃から1000℃を超える
粉じんの温度が、常温近くの温度にまで低下する
ため、ろ過集じん機のナイロンやテトロンからな
るろ布の焼損を防止できるとともに、慣性力集じ
ん機または遠心力集じん機によつて粉子径50μm
以上の粉じんを、またろ過集じん機によつて粉子
径50μm以下の粉じんを、夫々捕集することとな
るので、捕集する粉じんの粒子径に合致した集じ
ん機を使用することができる。
例えばルーバ形等の慣性力集じん機は、設置面
積および設置費用を小さくするために小型にする
と、集じん機内のガス流速が速くなつて、捕集し
た粉じんが再飛散して集じん効率が低下する。ま
た、例えばサイクロン形等の遠心力集じん機は、
集じん効率が85％〜95％と高くて圧力損失が60mm
H2O〜80mmH2Oと比較的低い反面、設置高さが
高くてろ過集じん機の前処理用の粗粒粉じんの集
じん機としては価格が高い。それ故、従来は、サ
イクロン形の遠心力集じん機の変形として、直進
流形サイクロンおよび接線流入形サイクロン等が
用いられている。
第１図は直進流形サイクロンの概略を示す図で
あり、第２図は接線流入形サイクロンの概略を示
す図である。第１図において、直進流形サイクロ
ンは横型のサイクロンであつて、外筒３の中心軸
Ｘ−Ｘが水平になつている。外筒３の一端にはガ
ス流入口１が設けられ、流入ガスに旋回運動を与
えるための案内羽根５が固定軸６に固定されてい
る。外筒３の他端の底部にはダストボツクス７
が、また、外筒３の軸Ｘ−Ｘ方向の他端には、外
筒３の軸Ｘ−Ｘと軸が一致するような内筒４が、
夫々取付けられており、内筒４は研摩、研削作業
場または溶接作業場の屋外に開口しているガス流
出口２と連結されている。このように構成されて
いるため、ガス流入口１から流入した粉じんを含
んだガスは、案内羽根５によつて旋回運動が与え
られる。それ故、ガスに含まれている粉じんは、
遠心力によつて外筒３の内壁に押しつけられると
ともに、ガスの流れにしたがつて外筒の他端に移
動し、ダストボツクス７の中に落下して蓄積され
る。一方、粉じんを分離された清浄なガスは、案
内羽根５によつて旋回させられたまま案内羽根５
から内筒４の方向へ進行し、内筒４を経てガス流
出口２から研摩、研削作業場または溶接作業場の
屋外に排出される。
第２図において、接線流入形サイクロンは縦型
のサイクロンであつて、外筒３の中心軸Ｘ−Ｘが
垂直になつている。外筒３の上端部には、流入ガ
スの流入方向が外筒３の接線方向と一致するよう
に、ガス流入口１が開口している。また、外筒３
の軸Ｘ−Ｘと軸が一致するような旋回円筒８が取
付けられ、ガス流入口１から流入したガスが旋回
するときの旋回の中心となつている。外筒３の下
端部には、ダストボツクス７と、外筒３の軸Ｘ−
Ｘに軸が一致するような内筒４とが設けられ、内
筒４は研摩、研削作業場または溶接作業場の屋外
に開口しているガス流出口２と連結されている。
このように構成されているため、ガス流入口１か
ら円筒３の接線方向に流入した粉じんを含んだガ
スは、旋回円筒８を中心として旋回される。それ
故、ガスに含まれている粉じんは、遠心力によつ
て外筒３の内壁に押しつけられるとともに、重力
の作用とガスの流れとにしたがつて外筒３の下端
部に移動し、ダストボツクス７の中に落下して蓄
積される。一方、粉じんを分離された清浄なガス
は、旋回されたまま内筒４の方向へ進行し、内筒
４を経てガス流出口２から研摩、研削作業場また
は溶接作業場の屋外に排出される。
上記のように、直進流形サイクロンおよび接線
流入形サイクロンは構造は簡単であるが、流入ガ
スが十数ｍ／ｓの旋回速度のまま内筒４に流入す
るため、圧力損失が150mmH2Oと高い欠点があ
る。また、外筒３の内壁を旋回しながら進行した
ガスの一部が、ダストボツクス７の底部に到達し
て反転するときに、ダストボツクス７内に蓄積さ
れたダストを持ち去るいわゆる再飛散現象によつ
て、集じん効率が低下する欠点がある。
〔発明の目的〕
この発明は、上記の欠点を解消するためになさ
れたもので、圧力損失が低く、集じん効率が高い
遠心力集じん機を提供することを目的とするもの
である。
〔発明の概要〕
この発明は、遠心力によつて粉じんを分離され
た清浄なガスの旋回運動を、ガス旋回防止板を取
付けて停止することにより、圧力損失の上昇を抑
制するとともに、粉じんを分離された清浄なガス
がダストボツクス内に流入することを、ガス流入
防止板を取付けて防止することにより、既に捕集
した粉じんの再飛散を防止して集じん効率を高め
ることを特徴とするものである。
特に、圧力損失の上昇を抑え、効率的に粉じん
を除するために、ガス旋回防止板は前記ガス流出
口内に設けられた前記ガスの旋回運動を直進運動
にするに十分な流れ方向に対する長さを有する整
流部と、該整流部の上流側で前記ガス流出口外に
設けられた前記ガス流出口の入口口径より大きく
前記ガスの旋回運動を実質的に停止させるに十分
な径方向の長さ及び前記ガス流出口への流れ方向
に対する長さを有する停止部を備えるようにした
ものである。
〔発明の実施例〕
この発明に係わる実施例を図面にもとづいて説
明する。第３図はこの発明の遠心力集じん機の一
実施例の断面図であり、第４図は第３図に示した
遠心力集じん機の分解斜視図である。第３図およ
び第４図において、遠心力集じん機は縦型になつ
ており、流入ガスの流入方向が外筒３の接線方向
と一致するように、ガス流入口１が外筒３の上端
部に開口している。外筒３の下端部は外凾１１の
上面部と接続され、外筒３の垂直軸Ｘ−Ｘと軸が
一致するような内筒４が、外凾１１の上面部の円
形開口部１５を突きぬけて取付けられている。ガ
ス旋回防止板９は、ガスの旋回運動を停止する部
分Ａの板ａと、旋回運動が停止されたガスの流れ
を整流する部分Ｂの板ｂとが、上下に連続して一
つの垂直な平面を形成するように構成されてい
る。また、ガスの旋回運動を停止する部分Ａの板
ａの水平方向の長さは、旋回運動が停止されたガ
スの流れを整流する部分Ｂの板ｂの水平方向の長
さよりも、部分Ｃの長さだけ長く形成されてい
る。そして、この長く形成された部分Ｃが、内筒
４の上縁１２に載置されることによつて、ガスの
旋回運動を停止する部分Ａが内筒４の上縁１２の
上に露出するように、また、旋回運動が停止され
たガスの流れを整流する部分Ｂが内筒４の内部に
隠れるように、挿入されている。この場合、ガス
の旋回運動を停止する部分Ａは、水平方向の長さ
が、外筒３の内面と内筒４の外面との間の中間点
に達するように、また、垂直方向の長さが、内筒
４の内径の1/2の長さになるように構成されてい
る。旋回運動が停止されたガスの流れを整流する
部分Ｂは、水平方向の長さが、内筒４の内径より
僅かに小さくなるように、また、部分Ｂの下端
が、円形のガス流出口２の中心点に達するように
構成されている。ガス旋回防止板９は４枚板の十
字形のものを図示したが、２枚板の一の字形、ま
たは６枚板の星形のものでもよい。ガス流入防止
板１０は、上縁１３が下縁１４よりも高く位置
し、上縁１３と下縁１４とで形成する面が斜めに
なつていて、傘形のリング状をなしている。ガス
流入防止板１０の上縁１３は内筒４の上縁１２に
固定され、下縁１４と外凾１１の上面部の円形開
口縁１６との間の距離が10mm程度に保持されてい
る。内筒４は外凾１１の垂直面を突きぬけてガス
流出口２に連結され、外凾１１の底部にはダスト
ボツクス７が出し入れ自在に挿入されている。
このように構成されているため、粉じんを含ん
だガスは、ガス流入口１から外筒３の接線方向に
流入して旋回される。それ故、ガスに含まれてい
る粉じんは、遠心力によつて外筒３の内壁に押し
つけられるとともに、重力の作用とガスの流れと
にしたがつて外筒３の下端部に移動する。そし
て、外筒３の内壁に沿つて落下してきた粉じん
と、ガス流入防止板１０の上縁１３と下縁１４と
で形成する傘形の斜面上に落下した粉じんとは、
ともに、ガス流入防止板１０の下縁１４と、外凾
１１の上面部の円形開口縁１６との間を通つて落
下し、ダストボツクス７に蓄積される。一方、粉
じんを分離された清浄なガスは、ガス旋回防止板
９の部分Ａによつて旋回が停止されるとともに、
ガス流入防止板１０によつて外凾１１の中へのガ
ス流入が防止されて内筒４に進入し、ガス旋回防
止板９の部分Ｂによつて流れが整流されてガス流
出口２から排出される。
つぎに、従来の遠心力集じん機の圧力損失およ
び集じん率と、この発明の遠心力集じん機の圧力
損失および集じん率との比較について説明する。
第１図に示した直進流形サイクロン、第２図に示
した接線流入形サイクロンおよび第３図、第４図
に示したこの発明の遠心力集じん機の夫々につい
て、外筒３の直径を400mm、外筒３の高さまたは
長さを500mm、内筒４の直径を200mm、ガス流入口
１におけるガスの流入速度を15m／ｓとした場
合、ガス流入口１とガス流出口２との間の圧力損
失は、従来の第１図に示した直進流形サイクロン
および第２図に示した接線流入形サイクロンでは
130mmH2Oであつたが、この発明の第３図、第４
図に示した遠心力集じん機では63mmH2Oであり、
従来の遠心力集じん機の圧力損失の約半分であつ
た。また、高速切断機で1.5Bのガス管を切断し
たときに発生する粉じんの粉子径別の集じん率
は、下表のように、第３図、第４図に示したこの
発明の遠心力集じん機が一番高かつた。
[Field of Application of the Invention] The present invention relates to a centrifugal dust collector that efficiently collects dust particles having particle diameters in the range of 10 μm to 2 mm. [Background of the Invention] Dust generated during polishing and grinding work using a grinder, etc., and welding work such as arc welding and gas welding contaminates the workplace environment, so a dust collector is installed to collect the dust. and improving the workplace environment. Dust that scatters from steel materials and whetstones during polishing and grinding operations using a grinder, etc. is caused by the heat generated by the friction between the steel materials and the whetstone, and also due to the slag and molten particles that are scattered during welding operations such as arc welding and gas welding. Dust such as small metal particles, or spatter, are both susceptible to heat due to the arc and gas flame.
It is heated to temperatures ranging from several 100 degrees Celsius to over 1000 degrees Celsius, and the powder diameters range from 0.1 μm to 2 mm. Among these, dust with a particle diameter in the range of 0.1 μm to 20 μm is collected by a filtration dust collector such as a bag filter, and dust with a diameter of 10 μm to 2 mm is collected by an inertial force dust collector such as a looper type or It is effective to collect each type of dust using a centrifugal dust collector such as a cyclone type dust collector. Glass fiber, which has a maximum continuous operating temperature of 250℃, is expensive as a filter material for filter dust collectors, so
Nylon and Tetron, which have a maximum continuous operating temperature of 110°C to 150°C, are mostly used. However, as mentioned above, since the temperature of the dust is several 100 degrees Celsius to over 1000 degrees Celsius, the filter cloth made of nylon or tetron is burned out, which may reduce the dust collection efficiency. Therefore, after considering the amount of heat held by each dust particle and the time it takes for the dust to reach the filter cloth from the source, we found that first, by using an inertial force dust collector or a centrifugal force dust collector, If you use a filter dust collector after collecting dust with a diameter of 50 μm or more, you can lengthen the time from when the dust is generated until it reaches the filter dust collector. Therefore, when dust is generated, the temperature of the dust, which ranges from several 100 degrees Celsius to over 1000 degrees Celsius, is reduced to a temperature close to room temperature, which prevents the filter cloth made of nylon or Tetron in the filter dust collector from burning out. Powder diameter 50μm by inertial force dust collector or centrifugal force dust collector
Since the above-mentioned dust and the dust with a particle size of 50 μm or less will be collected by the filter dust collector, it is possible to use a dust collector that matches the particle size of the dust to be collected. . For example, if an inertial force dust collector such as a louver type is made smaller in order to reduce the installation area and installation cost, the gas flow rate inside the dust collector will increase, and the collected dust will be re-dispersed, reducing the dust collection efficiency. descend. In addition, for example, centrifugal dust collectors such as cyclone type,
High dust collection efficiency of 85% to 95% and pressure loss of 60mm
Although the H 2 O to 80 mm H 2 O is relatively low, the installation height is high and the price is high for a coarse dust collector for pre-treatment of a filtration dust collector. Therefore, conventionally, as a modification of the cyclone type centrifugal dust collector, a straight flow type cyclone, a tangential flow type cyclone, etc. have been used. FIG. 1 is a diagram schematically showing a straight flow type cyclone, and FIG. 2 is a diagram schematically showing a tangential flow type cyclone. In FIG. 1, the straight flow type cyclone is a horizontal cyclone, and the central axis XX of the outer cylinder 3 is horizontal. A gas inlet 1 is provided at one end of the outer cylinder 3, and a guide vane 5 for giving swirling motion to the inflowing gas is fixed to a fixed shaft 6. There is a dust box 7 at the bottom of the other end of the outer cylinder 3.
However, at the other end of the outer cylinder 3 in the axis XX direction, there is an inner cylinder 4 whose axis coincides with the axis XX of the outer cylinder 3.
The inner cylinder 4 is connected to a gas outlet 2 which is open to the outside of the polishing, grinding or welding workshop. With this configuration, the dust-containing gas flowing in from the gas inlet 1 is given a swirling motion by the guide vanes 5. Therefore, the dust contained in the gas is
It is pressed against the inner wall of the outer cylinder 3 by centrifugal force, moves to the other end of the outer cylinder according to the gas flow, falls into the dust box 7, and is accumulated. On the other hand, the clean gas from which dust has been separated remains rotated by the guide vane 5.
The gas flows from the gas toward the inner cylinder 4, passes through the inner cylinder 4, and is discharged from the gas outlet 2 to the outside of the polishing or grinding workshop or the welding workshop. In FIG. 2, the tangential flow type cyclone is a vertical cyclone, and the central axis X--X of the outer cylinder 3 is vertical. A gas inlet 1 is opened at the upper end of the outer cylinder 3 so that the inflow direction of the inflow gas coincides with the tangential direction of the outer cylinder 3. In addition, the outer cylinder 3
A rotating cylinder 8 whose axis coincides with the axis X--X of the gas inlet 1 is attached, and serves as the center of rotation when the gas flowing in from the gas inlet 1 swirls. At the lower end of the outer cylinder 3, there is a dust box 7 and an axis X-
An inner cylinder 4 whose axis coincides with X is provided, and the inner cylinder 4 is connected to a gas outlet 2 which is open to the outside of a polishing or grinding workshop or a welding workshop.
With this configuration, the dust-containing gas that flows in from the gas inlet 1 in the tangential direction of the cylinder 3 is rotated around the rotating cylinder 8 . Therefore, the dust contained in the gas is pressed against the inner wall of the outer cylinder 3 by centrifugal force, and moves to the lower end of the outer cylinder 3 according to the action of gravity and the gas flow, and the dust is removed. It falls into Box 7 and accumulates. On the other hand, the clean gas from which the dust has been separated travels toward the inner cylinder 4 while being swirled, passes through the inner cylinder 4, and is discharged from the gas outlet 2 to the outdoors of the polishing or grinding workplace or the welding workplace. As mentioned above, the straight flow type cyclone and the tangential flow type cyclone have simple structures, but because the inflow gas flows into the inner cylinder 4 at a swirling speed of more than 10 m/s, the pressure loss is 150 mmH 2 O. There are high disadvantages. In addition, when a part of the gas that has traveled while swirling around the inner wall of the outer cylinder 3 reaches the bottom of the dust box 7 and turns around, a so-called re-scattering phenomenon occurs in which the dust accumulated in the dust box 7 is carried away. However, there is a drawback that the dust collection efficiency decreases. [Object of the Invention] The present invention was made in order to eliminate the above-mentioned drawbacks, and an object of the present invention is to provide a centrifugal dust collector with low pressure loss and high dust collection efficiency. [Summary of the Invention] This invention suppresses the increase in pressure loss and prevents dust by installing a gas swirl prevention plate to stop the swirling movement of clean gas from which dust has been separated by centrifugal force. A gas inflow prevention plate is installed to prevent the separated clean gas from flowing into the dust box, thereby preventing the already collected dust from scattering again and increasing the dust collection efficiency. It is something. In particular, in order to suppress the increase in pressure loss and efficiently remove dust, the gas swirl prevention plate is provided in the gas outlet and has a length in the flow direction sufficient to convert the swirling motion of the gas into a straight motion. and a radial length larger than the inlet diameter of the gas outlet provided outside the gas outlet on the upstream side of the rectifier and sufficient to substantially stop swirling movement of the gas. and a stop portion having a length with respect to the flow direction toward the gas outlet. [Embodiments of the Invention] Examples of the present invention will be described based on the drawings. FIG. 3 is a sectional view of one embodiment of the centrifugal dust collector of the present invention, and FIG. 4 is an exploded perspective view of the centrifugal dust collector shown in FIG. 3. In FIGS. 3 and 4, the centrifugal dust collector is of a vertical type, and the gas inlet 1 is located at the upper end of the outer cylinder 3 so that the inflow direction of the inflow gas coincides with the tangential direction of the outer cylinder 3. It is open in the middle. The lower end of the outer cylinder 3 is connected to the upper surface of the outer case 11, and the inner cylinder 4 whose axis coincides with the vertical axis XX of the outer case 3 opens the circular opening 15 on the upper surface of the outer case 11. It is installed through. The gas swirl prevention plate 9 has a plate a of a portion A that stops swirling motion of gas and a plate b of a portion B that rectifies the flow of gas whose swirling motion has been stopped, which are vertically continuous and form one vertical structure. It is configured to form a plane. In addition, the horizontal length of plate a of portion A that stops the swirling motion of gas is longer than the horizontal length of plate b of portion B that rectifies the flow of gas whose swirling motion has been stopped. It is formed to be long in length. By placing this long portion C on the upper edge 12 of the inner cylinder 4, the portion A that stops the swirling movement of the gas is exposed above the upper edge 12 of the inner cylinder 4. Also, a portion B for rectifying the flow of gas whose swirling motion has been stopped is inserted so as to be hidden inside the inner cylinder 4. In this case, the portion A that stops the swirling movement of the gas is designed such that its horizontal length reaches the midpoint between the inner surface of the outer cylinder 3 and the outer surface of the inner cylinder 4, and its vertical length is configured to have a length that is 1/2 of the inner diameter of the inner cylinder 4. The portion B that rectifies the flow of gas whose swirling motion has been stopped is designed so that its horizontal length is slightly smaller than the inner diameter of the inner cylinder 4, and the lower end of the portion B is connected to the circular gas outlet 2. is configured to reach the center point of Although the gas swirl prevention plate 9 is illustrated as having a cross shape with four plates, it may also be a one-shaped plate with two plates or a star shape with six plates. The gas inflow prevention plate 10 has an upper edge 13 located higher than a lower edge 14, and a surface formed by the upper edge 13 and lower edge 14 is oblique, forming an umbrella-shaped ring shape. The upper edge 13 of the gas inflow prevention plate 10 is fixed to the upper edge 12 of the inner cylinder 4, and the distance between the lower edge 14 and the circular opening edge 16 on the upper surface of the outer case 11 is maintained at about 10 mm. The inner cylinder 4 penetrates the vertical surface of the outer case 11 and is connected to the gas outlet 2, and a dust box 7 is inserted into the bottom of the outer case 11 so as to be freely removable. With this configuration, gas containing dust flows in from the gas inlet 1 in the tangential direction of the outer cylinder 3 and is swirled. Therefore, the dust contained in the gas is pressed against the inner wall of the outer cylinder 3 by centrifugal force, and moves to the lower end of the outer cylinder 3 according to the action of gravity and the flow of the gas. The dust that has fallen along the inner wall of the outer cylinder 3 and the dust that has fallen on the umbrella-shaped slope formed by the upper edge 13 and lower edge 14 of the gas inflow prevention plate 10 are:
Both fall through the space between the lower edge 14 of the gas inflow prevention plate 10 and the circular opening edge 16 on the upper surface of the outer case 11, and are accumulated in the dust box 7. On the other hand, the clean gas from which dust has been separated is stopped from swirling by part A of the gas swirl prevention plate 9, and
The gas inflow prevention plate 10 prevents gas from flowing into the outer case 11 and enters the inner cylinder 4, and the flow is rectified by the part B of the gas swirl prevention plate 9 and is discharged from the gas outlet 2. be done. Next, a comparison between the pressure loss and dust collection rate of a conventional centrifugal dust collector and the pressure loss and dust collection rate of the centrifugal dust collector of the present invention will be explained.
For each of the straight flow type cyclone shown in FIG. 1, the tangential flow type cyclone shown in FIG. 2, and the centrifugal force dust collector of the present invention shown in FIGS. 3 and 4, the diameter of the outer cylinder 3 is 400 mm, the height or length of the outer tube 3 is 500 mm, the diameter of the inner tube 4 is 200 mm, and the gas inflow speed at the gas inlet 1 is 15 m/s. The pressure loss between
130mmH 2 O, but as shown in Figs. 3 and 4 of this invention.
In the centrifugal dust collector shown in the figure, it is 63 mmH 2 O,
The pressure loss was about half of that of conventional centrifugal dust collectors. In addition, the dust collection rate according to the particle diameter of the dust generated when cutting a 1.5B gas pipe with a high-speed cutting machine is as shown in the table below. The power dust collector was the most expensive.
この発明の遠心力集じん機は、ガス旋回防止板
９によつて、粉じんが分離された清浄なガスの旋
回運動を停止してガスの流れを整流しているの
で、ガス流入口１とガス流出口２との間の圧力損
失が低くなる効果がある。また、ガス流入防止板
１０によつて、粉じんが分離された清浄なガスが
ダストボツクス７の中に流入することを防止して
いるので、既に捕集した粉じんの再飛散がなくな
り、集じん効率が向上する効果がある。
In the centrifugal dust collector of the present invention, the gas swirl prevention plate 9 stops the swirling movement of clean gas from which dust has been separated and rectifies the gas flow. This has the effect of lowering the pressure loss between the outlet and the outlet 2. In addition, the gas inflow prevention plate 10 prevents clean gas from which dust has been separated from flowing into the dust box 7, which eliminates the re-scattering of already collected dust and improves dust collection efficiency. It has the effect of improving.
第１図は従来の直進流形サイクロンの概略を示
す図、第２図は従来の接線流入形サイクロンの概
略を示す図、第３図はこの発明の遠心力集じん機
の一実施例の断面図、第４図は第３図に示した遠
心力集じん機の分解斜視図、第５図は旋回防止板
の長さＨと集じん率及び圧力損失との関係を示す
線図、第６図は旋回防止板の長さＷと集じん率及
び圧力損失との関係を示す線図である。
１……ガス流入口、２……ガス流出口、３……
外筒、４……内筒、５……案内羽根、６……固定
軸、７……ダストボツクス、８……旋回円筒、９
……ガス旋回防止板、１０……ガス流入防止板、
１１……外凾、１２……内筒４の上縁、１３……
ガス流入防止板１０の上縁、１４……ガス流入防
止板１０の下縁、１５……外凾８の上面部の円形
開口部、１６……外凾８の上面部の開口縁、７，
１７′……取付ネジ。
Fig. 1 is a diagram schematically showing a conventional straight flow type cyclone, Fig. 2 is a diagram schematically showing a conventional tangential flow type cyclone, and Fig. 3 is a cross section of an embodiment of the centrifugal dust collector of the present invention. Figure 4 is an exploded perspective view of the centrifugal dust collector shown in Figure 3, Figure 5 is a diagram showing the relationship between the rotation prevention plate length H, dust collection rate and pressure loss, and Figure 6 The figure is a diagram showing the relationship between the length W of the rotation prevention plate, the dust collection rate, and the pressure loss. 1...Gas inlet, 2...Gas outlet, 3...
Outer cylinder, 4... Inner cylinder, 5... Guide vane, 6... Fixed shaft, 7... Dust box, 8... Rotating cylinder, 9
...Gas swirl prevention plate, 10...Gas inflow prevention plate,
11... Outer case, 12... Upper edge of inner tube 4, 13...
Upper edge of the gas inflow prevention plate 10, 14...Lower edge of the gas inflow prevention plate 10, 15...Circular opening on the top surface of the outer case 8, 16...Opening edge on the top surface of the outer case 8, 7,
17'...Mounting screw.
Claims (1)
力によつてガス中の粉じんを分離除去する遠心力
集じん機において、粉じんを分離した清浄なガス
のガス流出口への通路にガスの旋回流を防止する
ガス旋回防止板及び、分離された粉じんのダスト
ボツクスへの通路にガス流入防止板が設けられ、
前記ガス旋回防止板は前記ガス流出口内に設けら
れた前記ガスの旋回運動を直進運動にするに十分
な流れ方向に対する長さを有する整流部と、該整
流部の上流側で前記ガス流出口外に設けられた前
記ガス流出口の入口口径より大きく前記ガスの旋
回運動を実質的に停止させるに十分な径方向の長
さ及び前記ガス流出口への流れ方向に対する長さ
を有する停止部を備えたことを特徴とする遠心力
集じん機。 ２ 前記ガス流入防止板は傘形の形状をなし、ダ
ストボツクス７の上面に設けられた特許請求の範
囲第１項記載の遠心力集じん機。[Scope of Claims] 1. In a centrifugal force dust collector that gives swirling motion to a gas containing dust and separates and removes dust from the gas using centrifugal force, the clean gas from which the dust has been separated is sent to the gas outlet. A gas swirl prevention plate is provided in the passageway for preventing gas swirling, and a gas inflow prevention plate is provided in the passageway for the separated dust to the dust box.
The gas swirl prevention plate includes a rectifying section provided in the gas outlet and having a length in the flow direction sufficient to convert the swirling motion of the gas into a rectilinear motion, and a rectifying section provided in the gas outlet and having a length in the flow direction sufficient to convert the swirling motion of the gas into a rectilinear motion. a stop portion having a radial length larger than the inlet diameter of the gas outlet provided in the gas outlet and having a length in the flow direction to the gas outlet that is sufficient to substantially stop the swirling movement of the gas; A centrifugal dust collector characterized by: 2. The centrifugal dust collector according to claim 1, wherein the gas inflow prevention plate has an umbrella shape and is provided on the upper surface of the dust box 7.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP196784A JPS60147267A (en) | 1984-01-11 | 1984-01-11 | Centrifugal dust collector |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP196784A JPS60147267A (en) | 1984-01-11 | 1984-01-11 | Centrifugal dust collector |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60147267A JPS60147267A (en) | 1985-08-03 |
| JPS6343134B2 true JPS6343134B2 (en) | 1988-08-29 |
Family
ID=11516348
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP196784A Granted JPS60147267A (en) | 1984-01-11 | 1984-01-11 | Centrifugal dust collector |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60147267A (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3625980B2 (en) * | 1997-03-12 | 2005-03-02 | 株式会社日立製作所 | Cyclone system for separating solid components in gas |
| KR20010014570A (en) * | 1999-04-23 | 2001-02-26 | 구자홍 | reduction device for the pressure of loss in cyclone dust collector |
| KR100565574B1 (en) * | 1999-12-03 | 2006-03-30 | 엘지전자 주식회사 | A cyclone type dust collector for a vacuum cleaner |
| KR100606703B1 (en) * | 2000-02-09 | 2006-07-31 | 엘지전자 주식회사 | cyclone collector for vaccum cleaner |
| KR100606753B1 (en) * | 2000-02-19 | 2006-07-31 | 엘지전자 주식회사 | multi cyclone vacuum cleaner |
| JP4597598B2 (en) * | 2004-07-16 | 2010-12-15 | 株式会社マキタ | Slide circular saw with dust collector |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS475461U (en) * | 1971-02-09 | 1972-09-18 |
-
1984
- 1984-01-11 JP JP196784A patent/JPS60147267A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60147267A (en) | 1985-08-03 |
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