JPH061209Y2 - Gas-solid separation chamber - Google Patents
Gas-solid separation chamberInfo
- Publication number
- JPH061209Y2 JPH061209Y2 JP1987124769U JP12476987U JPH061209Y2 JP H061209 Y2 JPH061209 Y2 JP H061209Y2 JP 1987124769 U JP1987124769 U JP 1987124769U JP 12476987 U JP12476987 U JP 12476987U JP H061209 Y2 JPH061209 Y2 JP H061209Y2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- separation chamber
- riser
- solid separation
- solid
- 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 - Lifetime
Links
- 238000000926 separation method Methods 0.000 title claims description 73
- 239000007787 solid Substances 0.000 title claims description 52
- 239000000843 powder Substances 0.000 claims description 3
- 239000008187 granular material Substances 0.000 claims 1
- 239000002245 particle Substances 0.000 description 22
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000010419 fine particle Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000007664 blowing Methods 0.000 description 3
- 239000011362 coarse particle Substances 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000001464 adherent effect Effects 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
Landscapes
- Separating Particles In Gases By Inertia (AREA)
- Cyclones (AREA)
Description
【考案の詳細な説明】 〔産業上の利用分野〕 本考案は流動層を用いて、固体、液体あるいはスラリー
状の廃棄物及び可燃物を熱処理するための気固混相流の
循環装置における気固分離室に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial field of application] The present invention is directed to a gas-solid mixed-phase circulation apparatus for heat-treating solid, liquid or slurry wastes and combustibles using a fluidized bed. Regarding separation room.
高速流動層，希薄輸送層あるいは乱流流動層を用い、こ
れにサイクロン等を組合せて高温の粉粒体を循環する回
路を形成し、この回路に供給されるナフサあるいは残渣
油等を接触熱分解する、いわゆるFCCプロセスの各種の
型式が発表されている。これらの公知例の代表として、
ガルフ社の接触分解方式を第５図に示す。第５図におい
てライザー１１、気固分離室１２、ダウンカマー１３、
再生器２２及び傾斜管１５により気固混相流の循環回路
が形成される。気固分離室１２及び再生器２２はそれぞ
れ内蔵サイクロン１９及び２１を有し、固体粒子は再生
器２２の下部において、エアーヒータ１６から供給され
る熱風により加熱された後、傾斜管１５を下降し、次い
でライザー１１を上昇する。この循環回路において、分
解される残渣油等の原料はライザー１１の下部１７及び
その上部から水蒸気と共に供給される。次いでライザー
１１を上昇する間に熱い固体粒子と接触して熱分解さ
れ、さらに気固分離室１２下部のストリッパー２３に供
給される水蒸気により放散されて内蔵サイクロン１９を
経て製品ガスが得られる。一方排ガスは再生器２２の上
部から内蔵サイクロン２１を経て排出される。A high-speed fluidized bed, a dilute transport layer or a turbulent fluidized bed is used, and a cyclone is combined with this to form a circuit that circulates high-temperature particles, and naphtha or residual oil supplied to this circuit is catalytically pyrolyzed. Various types of so-called FCC processes have been announced. As a representative of these known examples,
Fig. 5 shows the catalytic cracking system of Gulf Company. In FIG. 5, the riser 11, the gas-solid separation chamber 12, the downcomer 13,
The regenerator 22 and the inclined pipe 15 form a gas-solid mixed-phase circulation circuit. The gas-solid separation chamber 12 and the regenerator 22 have built-in cyclones 19 and 21, respectively, and the solid particles are heated in the lower part of the regenerator 22 by the hot air supplied from the air heater 16 and then descend the inclined pipe 15. Then, the riser 11 is raised. In this circulation circuit, raw materials such as residual oil to be decomposed are supplied from the lower part 17 of the riser 11 and the upper part thereof together with steam. Then, while rising in the riser 11, the solid gas comes into contact with hot solid particles to be thermally decomposed, and is further dissipated by the steam supplied to the stripper 23 below the gas-solid separation chamber 12 to obtain a product gas through the built-in cyclone 19. On the other hand, the exhaust gas is discharged from the upper part of the regenerator 22 through the built-in cyclone 21.
このガルフプロセスはライザー１１の各位置に成分の異
なる原料を供給できる効率のよいプロセスであるが、気
固分離室１２及び再生器２２はそれぞれ内蔵サイクロン
１９，２１を有し、かつライザー１１頂部の開口２０が
気固分離室１２の垂直軸線上に設けられ、さらに該開口
２０はスロツト１４を備えている。従って構造が複雑で
あるため、圧力損失が大きく、また操作性が悪い。特に
粘着性物質あるいは灰分を発生する原料を処理する場合
は、これが前記スロツト及び内蔵サイクロン等に付着し
て閉塞させるおそれがある。This Gulf process is an efficient process that can supply raw materials with different components to each position of the riser 11, but the gas-solid separation chamber 12 and the regenerator 22 have built-in cyclones 19 and 21, and the top of the riser 11 is An opening 20 is provided on the vertical axis of the gas-solid separation chamber 12, and the opening 20 is provided with a slot 14. Therefore, since the structure is complicated, the pressure loss is large and the operability is poor. In particular, when treating a sticky substance or a raw material that generates ash, this may adhere to the slot and the built-in cyclone, and may cause blockage.
このような欠点をなくした気固分離室として第３図，第
４図に示す構造の分離器が知られている。これらのうち
第３図の装置はライザー１の開口10が分離室２の垂直中
心軸上に位置し、かつ直接に上方に向けて開口させたも
のであり、また第４図に示す装置はライザー１の上部を
分離器２に入る手前で曲げ、分離器２内の接続方向に開
口させたものである。このような装置は構造が簡単で付
着の問題がなく粗粒の分離に有利に用いられる。しかし
ながらこれらの分離器は下記のような欠点を有する。As a gas-solid separation chamber without such a defect, a separator having a structure shown in FIGS. 3 and 4 is known. Of these, the device of FIG. 3 is one in which the opening 10 of the riser 1 is located on the vertical central axis of the separation chamber 2 and is opened directly upward, and the device shown in FIG. The upper part of 1 is bent before entering the separator 2 and opened in the connecting direction in the separator 2. Such a device has a simple structure and has no problem of adhesion, and is advantageously used for separating coarse particles. However, these separators have the following drawbacks.
すなわち第３図のような装置では沈降室の塔高を十分に
とらないと塔頂に粒子が衝突するため粒子の分離が悪く
なる。また付着性の粒体の場合は付着堆積するおそれも
生じる。そこでライザー吹き上げ速度に見合う沈降室の
塔高が必要となり、大型化が困難となる問題を生じる。
また第４図のような装置では分離器２の直前の曲管部で
流体の方向転換を行うため、曲管部の内壁と粒子の直接
衝突により摩耗を生じあるいは流体速度の減速のため、
曲管部内壁に粒子の堆積現象が生じ、閉塞の原因とな
る。That is, in the apparatus shown in FIG. 3, unless the height of the sedimentation chamber is sufficiently high, the particles collide with the top of the tower, resulting in poor particle separation. Further, in the case of adherent particles, there is a possibility that they may adhere and accumulate. Therefore, the tower height of the settling chamber that is commensurate with the riser blowing speed is required, which causes a problem of difficulty in increasing the size.
Further, in the device as shown in FIG. 4, since the direction of the fluid is changed in the curved pipe section immediately before the separator 2, direct collision between the inner wall of the curved pipe section and the particles causes wear or deceleration of the fluid velocity.
A particle deposition phenomenon occurs on the inner wall of the curved tube portion, which causes blockage.
本考案は以上の問題点を解決し、装置の内壁に固体粒子
の付着や堆積及び摩耗がなく、気固分離室の塔高を低く
した状態でも広範囲の流体速度変化にも適応できる気固
分離室の提供を目的とする。The present invention solves the above problems, and there is no solid particle adhesion, accumulation or wear on the inner wall of the device, and gas-solid separation that can adapt to a wide range of fluid velocity changes even when the tower height of the gas-solid separation chamber is low. The purpose is to provide a room.
この目的を達成するため、本考案の気固分離室が、該気
固分離室の垂直軸線から偏心し、該気固分離室の底部か
ら内壁に沿って鉛直上方にライザーを貫設し、該ライザ
ーの頂部が該ライザーに直交するい水平面に対して３０
〜６０°上向きに傾斜し、かつ排出する気固混相流が該
気固分離室の内壁に沿って旋回する方向に開口している
とともに、ガス排出口を気固分離室の頂部に設けた構成
にしたことを特徴とする。To achieve this object, the gas-solid separation chamber of the present invention is eccentric from the vertical axis of the gas-solid separation chamber and has a riser penetrating vertically upward along the inner wall from the bottom of the gas-solid separation chamber, The top of the riser is 30 with respect to the horizontal plane perpendicular to the riser.
A configuration in which the gas-solid mixed phase flow to be discharged is inclined upward by -60 ° and is discharged in a direction to swirl along the inner wall of the gas-solid separation chamber, and the gas discharge port is provided at the top of the gas-solid separation chamber. It is characterized by having done.
以下本考案を図により説明する。The present invention will be described below with reference to the drawings.
第１図は本考案の気固分離室の構造を示す図で、このう
ち(1)は正面図、(2)は(1)のＸ−Ｘ断面図、(3)は(2)の
Ｙ−Ｙ断面図である。また第２図は本考案の気固分離室
の使用状態を示す図である。FIG. 1 is a view showing the structure of the gas-solid separation chamber of the present invention, in which (1) is a front view, (2) is a sectional view taken along line XX of (1), and (3) is Y of (2). It is a -Y sectional view. FIG. 2 is a view showing the use state of the gas-solid separation chamber of the present invention.
第１図の正面図(1)に示すように本考案の気固分離室２
（以下分離室と略称す）は水平方向の断面積を下部方向
に順次先細り状に縮小させ、かつ傾斜させて、その先端
をダウンカマー３に接続すると共に分離室２の直胴部分
の底部にライザー１を分離室２の内壁に沿って上向きに
貫設させ、さらにライザー１は分離室２の直胴部分の中
間位置で曲げると共に、その先端開口１０を、その開口
から排出する気固混相流が分離室２の内壁に沿って旋回
する方向に開口させる。上記ライザー１は第１図(1)に
おけるＸ−Ｘ方向の断面図、第１図(3)に示すようにラ
イザー１の垂直軸線と直交する水平面に対して３０〜６
０°の角度をもって斜め上向きに傾斜させる。換言すれ
ばライザー１の上部はライザー１の垂直軸線に対して上
方に向かって１２０〜１５０°の角度をもって傾斜させ
る。しかしてこの曲管の先端は第１図(2)に示すように
分離室２の内壁に沿って旋回流が生じる方向に開口させ
る。すなわちライザー１の頂部開口１０は、第１図(2)
に示す分離室２の断面内周の同心円Ｚ上に開口する。ま
た縦方向には、この同心円を通り紙面に垂直な仮想円筒
の表面に、該頂部開口１０の中心が位置するように水平
から３０乃至６０°、好ましくは４５°±５°程度の角
度をもって上向きに開口させる。As shown in the front view (1) of FIG. 1, the gas-solid separation chamber 2 of the present invention
(Hereinafter, abbreviated as a separation chamber) is such that the horizontal cross-sectional area is gradually reduced in a downward direction and is inclined, and its tip is connected to the downcomer 3 and at the bottom of the straight body portion of the separation chamber 2. The riser 1 is provided so as to extend upward along the inner wall of the separation chamber 2, and the riser 1 is bent at an intermediate position of the straight body portion of the separation chamber 2, and its tip opening 10 is discharged from the opening in a gas-solid mixed phase flow. Open along the inner wall of the separation chamber 2 in the direction of swirling. The riser 1 is a cross-sectional view taken along line XX in FIG. 1 (1), and as shown in FIG. 1 (3), the riser 1 is 30 to 6 with respect to a horizontal plane orthogonal to the vertical axis.
Tilt diagonally upward with an angle of 0 °. In other words, the upper part of the riser 1 is inclined upward with respect to the vertical axis of the riser 1 at an angle of 120 to 150 °. However, the tip of the bent tube is opened along the inner wall of the separation chamber 2 in the direction in which a swirl flow is generated, as shown in FIG. That is, the top opening 10 of the riser 1 is shown in FIG. 1 (2).
The opening is on a concentric circle Z on the inner circumference of the cross section of the separation chamber 2 shown in FIG. Further, in the vertical direction, the surface of a virtual cylinder passing through the concentric circles and perpendicular to the paper surface is directed upward with an angle of about 30 to 60 °, preferably 45 ° ± 5 ° from the horizontal so that the center of the top opening 10 is located. To open.
さらに、気固混相流から固体粒子を分離した後の気体を
系外へ排出するために、気固分離室の頂部にガス排出口
を設けるようにする。Further, in order to discharge the gas after separating the solid particles from the gas-solid mixed phase flow to the outside of the system, a gas discharge port is provided at the top of the gas-solid separation chamber.
このように構成された本考案の分離室２は下記のように
使用される。The separation chamber 2 of the present invention thus constructed is used as follows.
すなわち第２図において分離室２はダウンカマー３、傾
斜管５及びサイクロン４と共に流動層を系する気固混相
流の循環系を構成する。この分離室２はライザー１の内
径の約５倍の内径を有し、流動化ガス吹込み口６より供
給される熱風により循環粒子を加熱すると共に流動化す
る。これにより気固混相流は終末速度の２〜５倍の空塔
ガス速度でライザー１内を上昇する。次いでこの混相流
はラウザー１の頂部曲管の先端開口から分離室２の内壁
に向けて旋回方向に噴射され、遠心力により粒子を分離
室２の内壁に衝突させて分離する。次いで分離した粒子
はダウンカマー３に沈降する。That is, in FIG. 2, the separation chamber 2 constitutes, together with the downcomer 3, the inclined pipe 5 and the cyclone 4, a circulation system of a gas-solid mixed phase flow forming a fluidized bed. This separation chamber 2 has an inner diameter that is about 5 times the inner diameter of the riser 1, and heats the circulating particles with the hot air supplied from the fluidizing gas blowing port 6 and fluidizes them. As a result, the gas-solid mixed phase flow rises in the riser 1 at a superficial gas velocity of 2 to 5 times the final velocity. Next, this multiphase flow is jetted in the swirling direction from the tip end opening of the top curved tube of the Rouser 1 toward the inner wall of the separation chamber 2, and the particles collide with the inner wall of the separation chamber 2 by centrifugal force to separate the particles. The separated particles then settle in Downcomer 3.
また該分離室２で捕集できなかった微細粒子は、気固分
離室の頂部に設けたガス排出口８を経てサイクロンに導
かれ、サイクロン４で捕集され、ダウンカマー３に戻さ
れる。この際ライザー１の空塔ガス速度は流動化ガス吹
込み口６におけるガス量の調節により行われ、また、粒
子循環速度は、ガス吹込み口７，７におけるガス量の調
節により調整される。Further, fine particles that could not be collected in the separation chamber 2 are guided to a cyclone via a gas discharge port 8 provided at the top of the gas-solid separation chamber, collected in the cyclone 4 and returned to the downcomer 3. At this time, the superficial gas velocity of the riser 1 is adjusted by adjusting the gas amount at the fluidizing gas injection port 6, and the particle circulation velocity is adjusted by adjusting the gas amount at the gas injection ports 7 and 7.
以上のように構成された分離室２においてライザー１内
を粒子終末速度以上にガス流速により上昇する気固混相
流は分離室２の中心軸から偏心した位置に、水平面に対
して３０−６０°の角度で、かつ接線方向に吹き付ける
ことにより粗粒子は沈降分離し細粒子も遠心力集塵効果
により同時に捕集分離される。一方向固体粒子を分離し
た残りの気体は、気固分離室の頂部に設けたガス排出口
８より室外へ排出される。In the separation chamber 2 configured as described above, the gas-solid multiphase flow that rises in the riser 1 due to the gas flow velocity above the terminal particle velocity is located at a position eccentric from the central axis of the separation chamber 2 and at 30-60 ° with respect to the horizontal plane. By spraying at an angle of and tangentially, the coarse particles settle and separate, and the fine particles are simultaneously collected and separated by the centrifugal dust collection effect. The remaining gas from which the unidirectional solid particles have been separated is discharged to the outside from the gas discharge port 8 provided at the top of the gas-solid separation chamber.
本考案の分離室においてライザーを水平方向から３０〜
６０°の角度で上向きに曲げる。この限定の理由は３０
°未満では、この曲管部において衝突による磨耗、粉体
の付着あるいは圧損の増大等を生成し、またこの傾斜が
60゜を超えれば分離室上部二分体が衝突する傾向が大と
なり、この吹き上げに見合う分離室の高さが必要とな
り、本考案の目的上好ましくない。以上の理由は本考案
におけるライザーは水平方向から３０〜６０°の曲げ角
度とするが特に好ましい範囲は４５±５°程度である。In the separation chamber of the present invention, the riser is placed horizontally from 30 to 30.
Bend upward at an angle of 60 °. The reason for this limitation is 30
If the angle is less than °, abrasion due to collision, powder adhesion, increase in pressure loss, etc. are generated in this curved pipe section, and this inclination is
If it exceeds 60 °, the upper half of the separation chamber tends to collide with each other, and the height of the separation chamber is required to meet the blowing up, which is not preferable for the purpose of the present invention. The reason for the above is that the riser in the present invention has a bending angle of 30 to 60 ° from the horizontal direction, but a particularly preferable range is about 45 ± 5 °.
また本考案においてライザーは分離室の垂直軸線から偏
心させて分離室の内壁に接近させて分離室内に貫設し、
かつライザー頂部開口を水平から３０乃去６０°、好ま
しくは４５°±５°程度上向きに開口させる。これによ
り分離室の内壁への急激な衝突を回避し、そのため圧損
を少なく、かつ良好な分離効率が得られる。このライザ
ー頂部開口の角度範囲外では分離室内における気固混相
流の旋回方向が下向きあるいは上向きに偏って分離効率
を阻害して好ましくない。Further, in the present invention, the riser is eccentric from the vertical axis of the separation chamber to approach the inner wall of the separation chamber and penetrate into the separation chamber.
In addition, the riser top opening is opened at an angle of 30 ° from the horizontal and 60 °, preferably about 45 ° ± 5 °. This avoids a sudden collision with the inner wall of the separation chamber, thus reducing pressure loss and obtaining good separation efficiency. Outside the angle range of the riser top opening, the swirling direction of the gas-solid mixed phase flow in the separation chamber is biased downward or upward, which impedes the separation efficiency, which is not preferable.
第２図の装置を用いた実験を行った。この装置仕様とし
てライザー１は４０Ａ（内径38.4mm）、高さ3000mmで、
気固分離室の底部から内壁に沿って鉛直上方に貫設し、
その先端を水平方向から４５°の角度で斜め上向きに傾
斜させるとともに、分離室の内壁に沿って旋回流が生じ
る方向に開口させ、気固分離室２を２００Ａ（内径208.
3mm）、高さ５００mmとし、その頂部にガス排出口を設
け、ダウンカマー３と傾斜管５を６５Ａ（内径７0.3m
m）、傾斜管５の 傾斜角度60゜とする透明塩化ビニル製
の高速循環流動層にケイ砂（▲▼＝0.2mm、ρｓ＝2
485kg/m3、Umf＝0.038、Ut＝1.66m/s）を１２ｋｇ充填
し、常温の空気で運転した。なお、先の記号は以下のこ
とを表わすものである。▲▼：平均粒子径、Ｕmf：
流動開始速度、ρｓ：粒子の真密度、Ｕｔ：粒子終末速
度 まず、ライザーの空塔ガス速度4.6m/s（Utの2.8倍）の
場合にライザー最下部からのガス量を0.92Nm3／Ｈ（Umf
の２倍）と一定にし、開口部下端から約１５０mmの位置
に配設した内径１6.７mmのガス吹込み口7′からの傾斜
管へのガス量を０から1Nm3/H（Umfの3.７倍）の範囲で
変化させた。その結果ライザー断面積基準のケイ砂の循
環速度は５７から２５０kg/m2・sであった。An experiment was conducted using the apparatus shown in FIG. As for this equipment specification, the riser 1 is 40A (inner diameter 38.4mm), height 3000mm,
Along the inner wall from the bottom of the gas-solid separation chamber penetrates vertically upward,
The tip is inclined obliquely upward at an angle of 45 ° from the horizontal direction, and is opened in the direction in which a swirl flow is generated along the inner wall of the separation chamber, so that the gas-solid separation chamber 2 is 200 A (inner diameter 208.
3mm), height 500mm, a gas outlet is provided on the top, and the downcomer 3 and the inclined pipe 5 are 65A (inner diameter 70.3m).
m), a high-speed circulating fluidized bed made of transparent vinyl chloride with an inclination angle of 60 ° and silica sand (▲ ▼ = 0.2 mm, ρ s = 2
12 kg of 485 kg / m 3 , Umf = 0.038, U t = 1.66 m / s) were filled and the system was operated at room temperature air. The above-mentioned symbols represent the following. ▲ ▼: Average particle size, Umf:
Flow rate of initiation, .rho.s: true density of the particle, Ut: particle terminal velocity First, 0.92 nm and the amount of gas from the riser bottom when the superficial gas velocity 4.6 m / s of the riser (2.8 times the U t) 3 / H (U mf
The amount of gas from the gas inlet 7'with an inner diameter of 16.7 mm, which is arranged at a position of about 150 mm from the lower end of the opening, to the inclined tube is 0 to 1 Nm 3 / H (U mf (3.7 times). As a result, the circulation rate of silica sand based on the riser cross-sectional area was 57 to 250 kg / m 2 · s.
次にライザー最下部からのガス量と傾斜管へのガス量を
それぞれ0.92Nm3/H（Umfの２倍）、0.48Nm3/H（Ummfの
１倍）と一定にしてライザー空塔ガス速度2.２から１０
m/s（Utの1.３から６倍）と変化させた。その結果粒子
循環速度は９０から２００kg/m2・sであった。Next, the amount of gas from the bottom of the riser and the amount of gas to the inclined pipe were kept constant at 0.92 Nm 3 / H (twice U mf ) and 0.48 Nm 3 / H (one time U m mf ) respectively, and the riser empty tower Gas velocity 2.2 to 10
m / s (1.3 6 times of U t) and is varied. As a result, the particle circulation speed was 90 to 200 kg / m 2 · s.
以上のように本考案の気固分離室は上記実施例において
殆どの細粒子まで分離が可能であり、分離室の内壁への
付着及び堆積は観察されなかつた。またライザー空塔ガ
ス速度を2.２から１０m/sの範囲で変化させても気固分
離室の塔高は十分満足できる分離効率が得られるもので
あった。As described above, in the gas-solid separation chamber of the present invention, most fine particles can be separated in the above-mentioned embodiment, and no adhesion or deposition on the inner wall of the separation chamber was observed. Further, even if the gas velocity of the riser superficial column was changed within the range of 2.2 to 10 m / s, the column height of the gas-solid separation chamber was sufficiently high and the separation efficiency was obtained.
本考案の気固分離室を用いることにより、ライザーを上
昇して該分離室内に噴射される気固混相流は分離室の内
壁に対して斜め上向きで、かつ接線方向に流れるため、
分離室の高さが従来法に比して低い状態で沈降分離と遠
心力集塵効果の相乗効果により、粗粒子から細粒子まで
一度に分離できる。また分離室の内壁への付着堆積及び
摩耗のおそれも少なくなる。またさらに幅広い粒体の種
類及び条件での粉体分離操作が可能となる。By using the gas-solid separation chamber of the present invention, since the gas-solid multiphase flow that rises the riser and is injected into the separation chamber flows obliquely upward and tangential to the inner wall of the separation chamber,
When the height of the separation chamber is lower than that of the conventional method, coarse particles and fine particles can be separated at once by the synergistic effect of sedimentation separation and centrifugal force dust collection effect. Further, the risk of adhesion and deposition on the inner wall of the separation chamber and abrasion is reduced. Further, it becomes possible to perform the powder separation operation under a wider variety of particle types and conditions.
第１図は本考案の詳細説明図で、その(1)は一部断面を
含む正面図、(2)は(1)のＸ−Ｘ断面図、(3)は(2)のＹ−
Ｙ断面図である。第２図は本考案の使用状態を示す図で
ある。第３図，第４図は分離室の公知例を示し、第５図
は従来の分離室を備えた流動接触分解装置を示す。 １…ライザー ２…気固分離室 ３…ダウンカマー ４…サイクロン ５…傾斜管 ６…流動化ガス吹込み口 ７，７′…ガス吹込み口 ８…ガス排出口 ９…製品ガス排出口 １０…ライザー頂部開口 １１…ライザー １２…気固分離器 １３…排出管 １４…スロット １５…傾斜管 １６…エアーヒータ １７…ライザー底部 １８…原料供給ライン １９…内蔵サイクロン ２０…ライザー頂部開口 ２１…内蔵サイクロン ２２…再生器 ２３…ストリッパー ２４…加熱部FIG. 1 is a detailed explanatory view of the present invention, in which (1) is a front view including a partial cross section, (2) is a cross-sectional view taken along line XX of (1), and (3) is taken along line Y- of (2).
It is a Y sectional view. FIG. 2 is a view showing a usage state of the present invention. 3 and 4 show a known example of a separation chamber, and FIG. 5 shows a conventional fluid catalytic cracking apparatus having a separation chamber. 1 ... Riser 2 ... Gas-solid separation chamber 3 ... Downcomer 4 ... Cyclone 5 ... Inclined tube 6 ... Fluidized gas inlet 7, 7 '... Gas inlet 8 ... Gas outlet 9 ... Product gas outlet 10 ... Riser top opening 11 ... Riser 12 ... Gas-solid separator 13 ... Discharge pipe 14 ... Slot 15 ... Inclined pipe 16 ... Air heater 17 ... Riser bottom 18 ... Raw material supply line 19 ... Built-in cyclone 20 ... Riser top opening 21 ... Built-in cyclone 22 … Regenerator 23… Stripper 24… Heating part
Claims (1)
備え、高速流動層を形成させた粉粒体の循環系における
気固分離室において、該ライザーが該気固分離室の垂直
軸線から偏心し、該気固分離室の底部から内壁に沿って
鉛直上方に貫設され、その頂部が該ライザーの軸線に直
交する水平面に対して３０〜６０°の角度で上向きに傾
斜し、かつ排出する気固混相流が該気固分離室の内壁に
沿って旋回する方向に開口しており、該気固分離室の頂
部にガス排出口を設けていることを特徴とする高速流動
層の気固分離室。A riser, a gas-solid separation chamber, and a downcomer are provided, and the riser is eccentric from a vertical axis of the gas-solid separation chamber in a gas-solid separation chamber in a circulation system of powder and granules forming a high-speed fluidized bed. The bottom of the gas-solid separation chamber extends vertically upward along the inner wall, and the top of the gas-solid separation chamber inclines upward at an angle of 30 to 60 ° with respect to the horizontal plane orthogonal to the axis of the riser and discharges the gas. A gas-solid multiphase flow is opened in a direction of swirling along the inner wall of the gas-solid separation chamber, and a gas discharge port is provided at the top of the gas-solid separation chamber. Separation room.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1987124769U JPH061209Y2 (en) | 1987-08-18 | 1987-08-18 | Gas-solid separation chamber |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1987124769U JPH061209Y2 (en) | 1987-08-18 | 1987-08-18 | Gas-solid separation chamber |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6428925U JPS6428925U (en) | 1989-02-21 |
| JPH061209Y2 true JPH061209Y2 (en) | 1994-01-12 |
Family
ID=31374793
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1987124769U Expired - Lifetime JPH061209Y2 (en) | 1987-08-18 | 1987-08-18 | Gas-solid separation chamber |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH061209Y2 (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5759812U (en) * | 1980-09-25 | 1982-04-08 | ||
| GB8516335D0 (en) * | 1985-06-28 | 1985-07-31 | Shell Int Research | Process for solids-fluid separation |
-
1987
- 1987-08-18 JP JP1987124769U patent/JPH061209Y2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6428925U (en) | 1989-02-21 |
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