JPH08332347A - Dry-type desulfurization and denitration apparatus - Google Patents
Dry-type desulfurization and denitration apparatusInfo
- Publication number
- JPH08332347A JPH08332347A JP7139378A JP13937895A JPH08332347A JP H08332347 A JPH08332347 A JP H08332347A JP 7139378 A JP7139378 A JP 7139378A JP 13937895 A JP13937895 A JP 13937895A JP H08332347 A JPH08332347 A JP H08332347A
- Authority
- JP
- Japan
- Prior art keywords
- hopper
- catalyst
- particle size
- denitration
- moving
- 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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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、脱硫と脱硝とを反応塔
内において同時に行うことができる乾式脱硫・脱硝装置
に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a dry desulfurization / denitration apparatus capable of simultaneously performing desulfurization and denitration in a reaction tower.
【０００２】[0002]
【従来の技術】従来、乾式脱硫・脱硝装置においては、
反応塔の上端から下端に向けて活性炭等の触媒を移動さ
せ、その間に被処理ガスを通すことによって脱硫と脱硝
とを同時に行い、亜硫酸ガス（ＳＯ2 ）等の硫黄酸化物
及び窒素酸化物（ＮＯX ）を除去するようにしている。2. Description of the Related Art Conventionally, in a dry desulfurization / denitration device,
A catalyst such as activated carbon is moved from the upper end to the lower end of the reaction tower, and desulfurization and denitration are simultaneously performed by passing a gas to be treated therebetween, so that sulfur oxides such as sulfurous acid gas (SO 2 ) and nitrogen oxides ( NO x ) is removed.
【０００３】図２は従来の反応塔の斜視図、図３は従来
の反応塔の断面図、図４は従来の粒度分布の測定結果を
表す図である。図において、１１は内部に互いに平行な
一対の移動層１０が形成された反応塔本体であり、角錐
（すい）形状を有する上部ホッパ１２、該上部ホッパ１
２と連結された断面が矩（く）形の胴部１３、該胴部１
３と連結された角錐形状を有する下部ホッパ１４から成
る。そして、前記上部ホッパ１２は上端に供給口１５
を、前記下部ホッパ１４は下端に排出口１６を有し、前
記供給口１５から落下した触媒１７は上部ホッパ１２、
移動層１０及び下部ホッパ１４内を下方に移動し、排出
口１６から外部に排出される。さらに、前記排出口１６
から排出された触媒１７は、図示しない再生装置におい
て再生させられ、再び供給口１５に供給される。FIG. 2 is a perspective view of a conventional reaction tower, FIG. 3 is a cross-sectional view of the conventional reaction tower, and FIG. 4 is a view showing the result of measuring the conventional particle size distribution. In the figure, 11 is a reaction tower main body in which a pair of moving layers 10 parallel to each other are formed, an upper hopper 12 having a pyramid shape, and the upper hopper 1
A body 13 having a rectangular cross section connected to the body 2, and the body 1
It is composed of a lower hopper 14 having a pyramid shape and connected with 3. The upper hopper 12 has a supply port 15 at the upper end.
The lower hopper 14 has a discharge port 16 at the lower end, and the catalyst 17 dropped from the supply port 15 has an upper hopper 12,
It moves downward in the moving layer 10 and the lower hopper 14 and is discharged to the outside from the discharge port 16. Further, the discharge port 16
The catalyst 17 discharged from is regenerated by a regenerator (not shown) and is resupplied to the supply port 15.
【０００４】前記胴部１３の側壁の一方には、被処理ガ
スが供給される被処理ガス供給部１８が、側壁の他方に
は、被処理ガスが排出される被処理ガス排出部２０が配
設される。また、前記胴部１３内において、前記被処理
ガス供給部１８から供給された被処理ガスは左右に分流
され、各移動層１０内を移動し、被処理ガス排出部２０
から排出される。A processed gas supply unit 18 for supplying a processed gas is arranged on one side wall of the body 13, and a processed gas discharge unit 20 for discharging a processed gas is arranged on the other side wall. Set up. Further, in the body portion 13, the processing target gas supplied from the processing target gas supply portion 18 is split into the left and right, moves in each moving layer 10, and the processing target gas discharge portion 20.
Emitted from.
【０００５】そして、前記移動層１０は、入口ルーバ１
０ａ及び出口ルーバ１０ｂを有する。前記入口ルーバ１
０ａは媒体１７が落下しないような開口構造を有し、出
口ルーバ１０ｂは多孔プレートから成り、被処理ガスを
通過させることができるようになっている。また、前記
出口ルーバ１０ｂの多孔プレートの各穴の径は前記触媒
１７の粒子径より小さく設定され、触媒１７が入口ルー
バ１０ａ及び出口ルーバ１０ｂから外部に流出すること
がないようになっている。The moving layer 10 has an inlet louver 1
0a and outlet louver 10b. The entrance louver 1
Reference numeral 0a has an opening structure that prevents the medium 17 from falling, and the outlet louver 10b is made of a perforated plate so that the gas to be treated can pass therethrough. Further, the diameter of each hole of the perforated plate of the outlet louver 10b is set smaller than the particle diameter of the catalyst 17 so that the catalyst 17 does not flow out from the inlet louver 10a and the outlet louver 10b.
【０００６】前記移動層１０の下端、すなわち、前記胴
部１３と下部ホッパ１４との間には、図示しない駆動系
によって回転させられ、移動層１０のレベルを一定に調
整しながら排出口１６から触媒１７を定量ずつ排出する
ための切出装置２２が配設される。したがって、移動層
１０内の触媒１７は一定の速度で下方に移動し、その間
に被処理ガスと接触し、脱硫と脱硝とを同時に行う。The lower end of the moving bed 10, that is, between the body portion 13 and the lower hopper 14, is rotated by a drive system (not shown), and the level of the moving bed 10 is adjusted to a constant level through the discharge port 16. A cutting device 22 is provided for discharging the catalyst 17 in a fixed amount. Therefore, the catalyst 17 in the moving bed 10 moves downward at a constant speed, contacts the gas to be treated in the meantime, and simultaneously performs desulfurization and denitration.
【０００７】ところで、前記触媒１７は反応塔本体１１
の上方の１箇所に形成された供給口１５から落下させら
れるので、移動層１０の上端に所定の安息角θを有する
触媒１７の山が形成される。なお、胴部１３の幅をＬと
し、上部ホッパ１２内に形成された触媒１７の山の高さ
をＨとすると、前記安息角θは θ＝ｔａｎ-1｛Ｈ／（Ｌ／２）｝ で表すことができる。By the way, the catalyst 17 is the reaction tower body 11
Since it is dropped from the supply port 15 formed at one position above, a peak of the catalyst 17 having a predetermined angle of repose θ is formed at the upper end of the moving layer 10. When the width of the body 13 is L and the height of the peak of the catalyst 17 formed in the upper hopper 12 is H, the angle of repose θ is θ = tan −1 {H / (L / 2)} Can be expressed as
【０００８】[0008]
【発明が解決しようとする課題】しかしながら、前記従
来の乾式脱硫・脱硝装置においては、触媒１７として活
性炭を使用した場合、図４に示すような広範囲の粒度分
布を有し、また、粒径は均一ではないので、所定の安息
角θを有する触媒１７の山が形成されたとき、粒径の大
きな触媒１７は、斜面に沿って落下して移動層１０の幅
Ｌ方向における周辺部に集まり、粒径の小さな触媒１７
は、移動層１０の幅Ｌ方向における中央部に集まってし
まう。However, in the above-mentioned conventional dry desulfurization / denitration apparatus, when activated carbon is used as the catalyst 17, it has a wide range of particle size distribution as shown in FIG. Since they are not uniform, when the peaks of the catalyst 17 having a predetermined angle of repose θ are formed, the catalyst 17 having a large particle size falls along the slope and gathers in the peripheral portion of the moving layer 10 in the width L direction, Small particle size catalyst 17
Gather in the central portion of the moving layer 10 in the width L direction.
【０００９】したがって、移動層１０内においても同様
に、粒径の大きな触媒１７は、移動層１０の幅Ｌ方向に
おける周辺部に集まり、粒径の小さな触媒１７は、移動
層１０の幅Ｌ方向における中央部に集まってしまう。こ
の場合、被処理ガスは、移動層１０内の周辺部に流れや
すく、中央部に流れにくくなり、ガス偏流を発生させて
しまうので、脱硝率が低くなってしまう。本発明は、前
記従来の乾式脱硫・脱硝装置の問題点を解決して、ガス
偏流を発生させることがなく、脱硝率を高くすることが
できる乾式脱硫・脱硝装置を提供することを目的とす
る。Therefore, also in the moving bed 10, the catalysts 17 having a large particle diameter gather in the peripheral portion of the moving bed 10 in the width L direction, and the catalysts 17 having a small particle diameter are in the width L direction of the moving bed 10. Will gather in the central part of. In this case, the gas to be processed easily flows to the peripheral portion in the moving layer 10 and becomes difficult to flow to the central portion, causing a gas drift, so that the denitrification rate becomes low. An object of the present invention is to solve the problems of the conventional dry desulfurization / denitration apparatus and to provide a dry desulfurization / denitration apparatus capable of increasing the denitration rate without generating gas drift. .
【００１０】[0010]
【課題を解決するための手段】そのために、本発明の乾
式脱硫・脱硝装置においては、上壁に触媒入口を備え、
下壁に逆円錐形状を有する下部逆円錐部が形成された上
部分配ホッパと、触媒を下方に移動させるとともに、被
処理ガスを通すための一対の移動層と、該各移動層の上
端に配設され、複数のホッパ室を備えた上部ホッパと、
前記下部逆円錐部における同一円上の複数箇所に形成さ
れたシュート入口と前記各ホッパ室とを連結するシュー
トとを有する。To that end, in the dry desulfurization / denitration apparatus of the present invention, a catalyst inlet is provided on the upper wall,
An upper distribution hopper having a lower wall having an inverted conical shape on the lower wall, a pair of moving layers for moving the catalyst downward and passing the gas to be treated, and an upper end of each moving layer. An upper hopper that is installed and has multiple hopper chambers,
Chute inlets formed at a plurality of locations on the same circle in the lower inverted cone portion and chutes connecting the hopper chambers are provided.
【００１１】[0011]
【作用】本発明によれば、前記のように乾式脱硫・脱硝
装置においては、上壁に触媒入口を備え、下壁に逆円錐
形状を有する下部逆円錐部が形成された上部分配ホッパ
と、触媒を下方に移動させるとともに、被処理ガスを通
すための一対の移動層と、該各移動層の上端に配設さ
れ、複数のホッパ室を備えた上部ホッパと、前記下部逆
円錐部における同一円上の複数箇所に形成されたシュー
ト入口と前記各ホッパ室とを連結するシュートとを有す
る。According to the present invention, as described above, in the dry desulfurization / denitration apparatus, the upper distribution hopper is provided with the catalyst inlet on the upper wall and the lower reverse cone having the reverse cone shape on the lower wall. While moving the catalyst downward, a pair of moving layers for passing the gas to be treated, an upper hopper provided at the upper end of each moving layer and having a plurality of hopper chambers, and the same in the lower inverted cone portion It has a chute inlet formed at a plurality of points on a circle and a chute that connects the hopper chambers.
【００１２】この場合、触媒入口から上部分配ホッパに
供給された触媒は、前記上部分配ホッパ内に所定の安息
角を有する山を形成する。そして、上部分配ホッパ内の
触媒は、各シュートを介して上部ホッパの各ホッパ室に
供給され、移動層を下方に移動させられる。また、被処
理ガスは移動層に供給されて触媒と接触させられ、該触
媒によって脱硫・脱硝される。In this case, the catalyst supplied from the catalyst inlet to the upper distribution hopper forms a mountain having a predetermined angle of repose in the upper distribution hopper. Then, the catalyst in the upper distribution hopper is supplied to each hopper chamber of the upper hopper via each chute, and the moving bed is moved downward. Further, the gas to be treated is supplied to the moving bed, brought into contact with the catalyst, and desulfurized and denitrated by the catalyst.
【００１３】[0013]
【実施例】以下、本発明の実施例について図面を参照し
ながら詳細に説明する。図１は本発明の実施例における
乾式脱硫・脱硝装置の概略図、図５は本発明の実施例に
おける乾式脱硫・脱硝装置の平面図である。図におい
て、３１は反応塔本体、３５は触媒供給コンベヤであ
り、該触媒供給コンベヤ３５によって搬送された触媒１
７は、上部分配ホッパ３６に落下する。Embodiments of the present invention will now be described in detail with reference to the drawings. FIG. 1 is a schematic diagram of a dry desulfurization / denitration apparatus according to an embodiment of the present invention, and FIG. 5 is a plan view of the dry desulfurization / denitration apparatus according to an embodiment of the present invention. In the figure, 31 is a reaction tower main body, 35 is a catalyst supply conveyor, and the catalyst 1 conveyed by the catalyst supply conveyor 35
7 falls onto the upper distribution hopper 36.
【００１４】該上部分配ホッパ３６は、直径が約３
〔ｍ〕の円柱形状を有し、上壁に触媒入口３７を備える
とともに、下壁に角度が４５〔°〕の逆円錐形状を有す
る下部逆円錐部３８が形成される。該下部逆円錐部３８
の斜面には、半径１〔ｍ〕の同一円上の１６箇所にシュ
ート入口３９が形成される。また、下部逆円錐部３８の
最下部には、１個のパージ穴４０が形成され、該パージ
穴４０にパージパイプ４１が接続される。The upper distribution hopper 36 has a diameter of about 3
In addition to having a columnar shape of [m], a catalyst inlet 37 is provided on the upper wall, and a lower inverted conical portion 38 having an inverted conical shape with an angle of 45 [°] is formed on the lower wall. The lower inverted cone portion 38
Chute inlets 39 are formed at 16 points on the same circle having a radius of 1 [m] on the slope. Further, one purge hole 40 is formed at the lowermost part of the lower inverted conical portion 38, and a purge pipe 41 is connected to the purge hole 40.
【００１５】また、一対の移動層５５は、それぞれ上端
に上部ホッパ４２、４３を備え、該各上部ホッパ４２、
４３はそれぞれ８個の角錐形状のホッパ室４５から成
る。そして、前記各シュート入口３９と各ホッパ室４５
とが、直径が２５０〔ｍｍ〕の鉄製パイプから成るシュ
ート４７によって接続される。前記上部ホッパ４２、４
３の下方には、それぞれ矩形の断面を有する胴部４８が
配設され、該各胴部４８内に前記移動層５５が形成され
る。また、該各移動層５５は７個の区画板４９によって
区画され、前記各ホッパ室４５に対応する８個の区画室
５０が形成される。The pair of moving layers 55 are provided with upper hoppers 42 and 43 at their upper ends, respectively.
Each of 43 is composed of eight pyramidal hopper chambers 45. Then, each chute inlet 39 and each hopper chamber 45
Are connected by a chute 47 made of an iron pipe having a diameter of 250 mm. The upper hoppers 42, 4
Underneath 3, the body parts 48 each having a rectangular cross section are arranged, and the moving layer 55 is formed in each of the body parts 48. Further, each moving layer 55 is partitioned by seven partition plates 49, and eight partition chambers 50 corresponding to each hopper chamber 45 are formed.
【００１６】なお、前記胴部４８の下方には、従来の乾
式脱硫・脱硝装置と同様に、図示しない角錐形状の下部
ホッパが連結され、該下部ホッパに切出装置、排出口が
配設される。また、前記各移動層５５間には被処理ガス
供給室６１が、移動層５５の外側には一対の被処理ガス
排出室６２、６３がそれぞれ配設され、前記被処理ガス
供給室６１に被処理ガス入口６５が、前記被処理ガス排
出室６２、６３にそれぞれ被処理ガス出口６６、６７が
接続される。A pyramid-shaped lower hopper (not shown) is connected to the lower part of the body portion 48, as in the conventional dry desulfurization / denitrification device, and a cutting device and a discharge port are arranged in the lower hopper. It Further, a to-be-processed gas supply chamber 61 is provided between the moving layers 55, and a pair of to-be-processed gas discharge chambers 62 and 63 are provided outside the moving layer 55, respectively. The processing gas inlet 65 is connected to the processing gas discharge chambers 62 and 63, and the processing gas outlets 66 and 67 are connected thereto.
【００１７】したがって、被処理ガス入口６５から供給
された被処理ガスは、被処理ガス供給室６１において左
右（図５における上下）に分流され、各移動層５５内を
通過して被処理ガス排出室６２、６３に至り、被処理ガ
ス出口６６、６７から排出される。前記構成の乾式脱硫
・脱硝装置において、触媒供給コンベヤ３５によって搬
送された触媒１７は上部分配ホッパ３６に供給される。
このとき、前記触媒１７は、上部分配ホッパ３６内の中
心部に落下し、粒径の大きな触媒１７は、山の斜面に沿
って落下して上部分配ホッパ３６の周辺部に集まり、粒
径の小さな触媒１７は、上部分配ホッパ３６の中央部に
集まるが、円周方向においては、同じ粒度分布で集ま
る。したがって、同じ粒径の触媒１７が、各シュート４
７を通り、上部ホッパ４２、４３の各ホッパ室４５に供
給される。Therefore, the gas to be processed supplied from the gas to be processed inlet 65 is split into left and right (up and down in FIG. 5) in the gas to be processed supply chamber 61, passes through each moving layer 55, and is discharged. The gas reaches the chambers 62 and 63 and is discharged from the processed gas outlets 66 and 67. In the dry desulfurization / denitration apparatus having the above structure, the catalyst 17 conveyed by the catalyst supply conveyor 35 is supplied to the upper distribution hopper 36.
At this time, the catalyst 17 falls to the central portion in the upper distribution hopper 36, and the catalyst 17 having a large particle diameter falls along the slope of the mountain and gathers in the peripheral portion of the upper distribution hopper 36 to reduce the particle diameter. The small catalysts 17 gather in the central portion of the upper distribution hopper 36, but gather in the same particle size distribution in the circumferential direction. Therefore, the catalyst 17 having the same particle size is used for each chute 4
7 and is supplied to each hopper chamber 45 of the upper hoppers 42 and 43.
【００１８】そして、該各ホッパ室４５の触媒１７は、
それぞれ各区画室５０に供給され、区画室５０内を下方
に落下するが、その間に被処理ガス供給室６１から供給
された被処理ガスと直交流に接触し、被処理ガス中の亜
硫酸ガスを吸着するとともに、窒素酸化物を無害な窒素
（Ｎ2 ）と水（Ｈ2 Ｏ）とに分解する。なお、前記上部
分配ホッパ３６の内径をＤ1 とし、各シュート入口３９
の中心を通る円の直径をＤ2 とし、シュート４７の直径
をＤ3 とし、上部ホッパ４２、４３の分割数、すなわ
ち、該各上部ホッパ４２、４３におけるホッパ室４５の
数をｎ、各シュート入口３９間のピッチをＰとすると、 Ｄ2 ＝（２ｎ×Ｄ3 ＋２ｎ×Ｐ）／π の関係になる。The catalyst 17 in each hopper chamber 45 is
Each of them is supplied to each of the compartments 50 and drops downward in the compartment 50, but during that time, it comes into contact with the to-be-processed gas supplied from the to-be-processed gas supply chamber 61 in a cross flow and adsorbs sulfurous acid gas in the to-be-processed gas. At the same time, nitrogen oxides are decomposed into harmless nitrogen (N 2 ) and water (H 2 O). The inner diameter of the upper distribution hopper 36 is set to D 1, and each chute inlet 39
The diameter of the circle passing through the center of the chute is D 2 , the diameter of the chute 47 is D 3, and the number of divisions of the upper hoppers 42, 43, that is, the number of hopper chambers 45 in each of the upper hoppers 42, 43 is n, and each chute is When the pitch between the inlets 39 is P, the relationship of D 2 = (2n × D 3 + 2n × P) / π is established.
【００１９】そして、 Ｄ2 ／Ｄ1 ＝２／３ とし、また、触媒１７の直径をＤ4 としたとき、各シュ
ート４７の直径Ｄ3 を、 Ｄ3 ＝Ｋ1 ×Ｄ4（Ｋ1 ：１０〜３０） とする。なお、通常は、 Ｄ4 ＝１０〔ｍｍ〕 ｎ＝８〜１２ Ｐ＝５０〜１００〔ｍｍ〕 であるので、 Ｄ1 ＝２〜３〔ｍ〕 Ｄ2 ＝１．３〜２〔ｍ〕 程度とするのが好ましい。When D 2 / D 1 = 2/3 and the diameter of the catalyst 17 is D 4 , the diameter D 3 of each chute 47 is D 3 = K 1 × D 4 (K 1 : 10 to 30). Normally, since a D 4 = 10 [mm] n = 8~12 P = 50~100 mm., D 1 = 2 to 3 [m] D 2 = 1.3 to 2 [m] degree Is preferred.
【００２０】前記上部分配ホッパ３６の高さをＨとし、
上部分配ホッパ３６の上壁から上部分配ホッパ３６内に
形成される触媒１７の山の頂上までの高さをｈ1 とし、
山の頂上から山の麓（ふもと）までの高さをｈ2 とし、
山の麓から上部分配ホッパ３６の下壁までの高さをｈ3
とすると、 Ｈ＝ｈ1 ＋ｈ2 ＋ｈ3 になり、ほぼ ｈ1 ＝ｈ2 ＝ｈ3 になる。The height of the upper distribution hopper 36 is H,
The height from the upper wall of the upper distribution hopper 36 to the top of the peak of the catalyst 17 formed in the upper distribution hopper 36 is h 1 .
The height from the top of the mountain to the foot of the mountain is assumed to be h 2 ,
The height from the foot of the mountain to the lower wall of the upper distribution hopper 36 is h 3
Then, H = h 1 + h 2 + h 3 and almost h 1 = h 2 = h 3 .
【００２１】また、触媒１７の山の安息角θは、 θ＝ｔａｎ-1｛ｈ2 ／（Ｄ1 ／２）｝ になり、通常、３５〔°〕程度である。そして、各シュ
ート４７と各上部ホッパ４２、４３とが連結される部分
の傾き角をθ1 〜θ8 とすると、傾き角θ1 〜θ8 は、 θ1 ＝θ8 ＜θ2 ＝θ7 ＜θ3 ＝θ6 ＜θ4 ＝θ5 になるように設定される。通常、傾き角θ1 は４５
〔°〕以上にするのが好ましい。さらに、各移動層５５
の幅をＬとし、各ホッパ室４５の底部の長さをＬ1 〜Ｌ
8 とし、各ホッパ室４５の高さをｈ4 とすると、 Ｌ＝Ｋ2 ×Ｌ1 （Ｋ2 ：４〜１０）Ｌ1 ＝Ｌ2 ＝Ｌ3 ＝Ｌ4 ＝Ｌ5 ＝Ｌ
6 ＝Ｌ7 ＝Ｌ8 であり、各ホッパ室４５の角錐の角度θ´は、 θ´＝ｔａｎ-1｛ｈ4 ／（Ｌ1 ／２）｝ で表すことができ、稜（りょう）角で４０〔°〕とする
のが好ましい。Further, the angle of repose of the mountain theta catalyst 17, theta = tan becomes -1 {h 2 / (D 1 /2)}, usually about 35 [°]. Then, when the inclination angle of the portion connecting the chutes 47 and the upper hoppers 42 and 43 is θ 1 to θ 8 , the inclination angles θ 1 to θ 8 are θ 1 = θ 8 <θ 2 = θ 7 It is set so that <θ 3 = θ 6 <θ 4 = θ 5 . Normally, the tilt angle θ 1 is 45
[°] or more is preferable. Furthermore, each moving layer 55
Is L, and the length of the bottom of each hopper chamber 45 is L 1 to L
8 and the height of each hopper chamber 45 is h 4 , L = K 2 × L 1 (K 2 : 4 to 10) L 1 = L 2 = L 3 = L 4 = L 5 = L
6 = a L 7 = L 8, pyramid angle [theta] & apos each hopper chamber 45 can be expressed by θ'= tan -1 {h 4 / (L 1/2)}, edge (Ryo) square Is preferably 40 [°].
【００２２】また、移動層５５の層厚ｗ1 は、脱硝率に
よって左右され、 ｗ1 ＝１〜２〔ｍ〕 とするのが好ましく、また、移動層５５間の距離ｗ
2 は、 ｗ2 ＝Ｋ3 ｗ1（Ｋ3 ：１〜３） である。Further, the layer thickness w 1 of the moving layer 55 depends on the denitration rate, and it is preferable that w 1 = 1 to 2 [m], and the distance w between the moving layers 55.
2, w 2 = K 3 w 1 (K 3: 1~3) is.
【００２３】本実施例においては、 ０．６＜Ｌ1 ／ｗ1 ≦１．０ である。次に、従来の乾式脱硫・脱硝装置と本発明の乾
式脱硫・脱硝装置との粒度分布の差について説明する。In this embodiment, 0.6 <L 1 / w 1 ≦ 1.0. Next, the difference in particle size distribution between the conventional dry desulfurization / denitration apparatus and the dry desulfurization / denitration apparatus of the present invention will be described.
【００２４】図６は従来の乾式脱硫・脱硝装置における
粒度分布を示す図、図７は本発明の実施例における乾式
脱硫・脱硝装置の粒度分布を示す図である。なお、図に
おいて、横軸に触媒１７（図１）全体及び各区画室（本
発明においては、区画室５０）＃１〜＃８を、縦軸に粒
度分布を採ってある。この場合、各区画室＃１〜＃８に
供給された触媒１７の粒度分布を示している。FIG. 6 is a diagram showing a particle size distribution in a conventional dry desulfurization / denitration device, and FIG. 7 is a diagram showing a particle size distribution in the dry desulfurization / denitration device in the embodiment of the present invention. In the figure, the abscissa represents the entire catalyst 17 (FIG. 1) and each compartment (compartment 50 in the present invention) # 1 to # 8, and the ordinate represents the particle size distribution. In this case, the particle size distribution of the catalyst 17 supplied to each of the compartments # 1 to # 8 is shown.
【００２５】図６から分かるように、従来の乾式脱硫・
脱硝装置においては、粒径の大きな触媒１７は移動層１
０（図３）の幅Ｌ方向における周辺部の区画室＃１、＃
８に集まり、粒径の小さな触媒１７は移動層１０の幅Ｌ
方向における中央部の区画室＃４、＃５に集まってしま
う。この場合、粒径のばらつきを示す標準偏差σは１
４．７４である。As can be seen from FIG. 6, conventional dry desulfurization /
In the denitration device, the catalyst 17 having a large particle size is used as the moving bed 1
0 (FIG. 3) in the width L direction of the peripheral compartments # 1, #
8, the catalyst 17 having a small particle diameter has a width L of the moving bed 10.
Will be gathered in the central compartments # 4 and # 5 in the direction. In this case, the standard deviation σ showing the variation in particle size is 1
It is 4.74.
【００２６】これに対して、図７から分かるように、本
発明の乾式脱硫・脱硝装置においては、粒径の大きな触
媒１７も粒径の小さな触媒１７も、移動層５５の幅Ｌ方
向における全体に均一に供給される。この場合、標準偏
差σは２．９９である。次に、本実施例における脱硝
率、空間速度及び粒径の関係について説明する。図８は
本発明の実施例における脱硝率、空間速度及び粒径の関
係を示した図である。なお、図において、横軸に空間速
度ｓｖを、縦軸に脱硝率を採ってある。On the other hand, as can be seen from FIG. 7, in the dry desulfurization / denitration apparatus of the present invention, both the catalyst 17 having a large particle size and the catalyst 17 having a small particle size are entirely in the width L direction of the moving layer 55. Is evenly supplied. In this case, the standard deviation σ is 2.99. Next, the relationship between the denitration rate, the space velocity and the particle size in this example will be described. FIG. 8 is a diagram showing the relationship among the denitration rate, the space velocity and the particle size in the example of the present invention. In the figure, the horizontal axis represents the space velocity sv and the vertical axis represents the denitration rate.
【００２７】ここで、空間速度ｓｖとは、被処理ガスの
量を触媒１７（図１）の量で割って得られる値であり、
一定量の触媒１７によって処理を行うことができる被処
理ガスの量を示す。図に示すように、空間速度ｓｖが低
くなると、脱硝率が高くなり、また、粒径が小さいほど
脱硝率が高くなる。Here, the space velocity sv is a value obtained by dividing the amount of the gas to be treated by the amount of the catalyst 17 (FIG. 1),
The amount of the gas to be treated that can be treated by a certain amount of the catalyst 17 is shown. As shown in the figure, when the space velocity sv is low, the denitration rate is high, and as the particle size is smaller, the denitration rate is higher.
【００２８】前述したように、前記移動層５５の幅Ｌ方
向において粒度分布は均一になるので、被処理ガスに偏
流が発生することはない。したがって、空間速度ｓｖを
一様に低くすることができ、脱硝率を高くすることがで
きる。図９は各区画室ごとの脱硝率について、従来の乾
式脱硫・脱硝装置と本発明の乾式脱硫・脱硝装置とを比
較した図、図１０は各区画室ごとの空間速度について、
従来の乾式脱硫・脱硝装置と本発明の乾式脱硫・脱硝装
置とを比較した図である。なお、図９において、横軸に
区画室＃１〜＃８を、縦軸に脱硝率を、図１０におい
て、横軸に区画室＃１〜＃８を、縦軸に空間速度を採っ
てある。As described above, since the particle size distribution is uniform in the width L direction of the moving layer 55, no uneven flow is generated in the gas to be treated. Therefore, the space velocity sv can be uniformly lowered, and the denitration rate can be increased. FIG. 9 is a diagram comparing the denitrification rate of each compartment with the conventional dry desulfurization / denitration apparatus and the dry desulfurization / denitration apparatus of the present invention, and FIG. 10 is the space velocity of each compartment.
It is the figure which compared the conventional dry desulfurization / denitration apparatus with the dry desulfurization / denitration apparatus of this invention. In FIG. 9, compartments # 1 to # 8 are plotted on the abscissa, denitration rates are plotted on the ordinate, and in FIG. 10, compartments # 1 to # 8 are plotted on the abscissa and space velocity is plotted on the ordinate. .
【００２９】図から分かるように、本発明の乾式脱硫・
脱硝装置においては、脱硝率及び空間速度ｓｖのいずれ
も各区画室＃１〜＃８にわたって平均的な値を有するこ
とができるので、乾式脱硫・脱硝装置の全体で脱硝率を
約１．２〔％〕高くすることができる。なお、本実施例
においては、乾式脱硫・脱硝装置の反応塔本体３１（図
１）について説明しているが、本発明を触媒補給槽、脱
離塔等に適用することもできる。As can be seen from the figure, the dry desulfurization of the present invention
In the denitration apparatus, both the denitration rate and the space velocity sv can have an average value over each of the compartments # 1 to # 8. Therefore, the denitration rate of the dry desulfurization / denitration apparatus as a whole is approximately 1.2%. ] It can be higher. In addition, although the reaction tower main body 31 (FIG. 1) of the dry desulfurization / denitration apparatus is described in the present embodiment, the present invention can be applied to a catalyst replenishment tank, a desorption tower, and the like.
【００３０】また、触媒１７としては、活性炭のほか
に、金属系脱硝触媒等の一般的触媒を使用することもで
きる。なお、本発明は前記実施例に限定されるものでは
なく、本発明の趣旨に基づいて種々変形させることが可
能であり、それらを本発明の範囲から排除するものでは
ない。As the catalyst 17, in addition to activated carbon, a general catalyst such as a metallic denitration catalyst can be used. It should be noted that the present invention is not limited to the above-described embodiments, and various modifications can be made based on the spirit of the present invention, and they are not excluded from the scope of the present invention.
【００３１】[0031]
【発明の効果】以上詳細に説明したように、本発明によ
れば、乾式脱硫・脱硝装置においては、上壁に触媒入口
を備え、下壁に逆円錐形状を有する下部逆円錐部が形成
された上部分配ホッパと、触媒を下方に移動させるとと
もに、被処理ガスを通すための一対の移動層と、該各移
動層の上端に配設され、複数のホッパ室を備えた上部ホ
ッパと、前記下部逆円錐部における同一円上の複数箇所
に形成されたシュート入口と前記各ホッパ室とを連結す
るシュートとを有する。As described above in detail, according to the present invention, in the dry desulfurization / denitration apparatus, the upper wall is provided with the catalyst inlet, and the lower wall is formed with the lower inverted cone portion having the inverted cone shape. An upper distribution hopper, a pair of moving layers for moving the catalyst downward and passing a gas to be treated, an upper hopper provided at the upper end of each moving layer and having a plurality of hopper chambers, The lower inverted conical portion has chute inlets formed at a plurality of locations on the same circle and the chutes that connect the hopper chambers.
【００３２】この場合、触媒入口から上部分配ホッパに
供給された触媒は、前記上部分配ホッパ内に所定の安息
角を有する山を形成する。このとき、粒径の大きな触媒
は、山の斜面に沿って落下して上部分配ホッパの周辺部
に集まり、粒径の小さな触媒は、上部分配ホッパの中央
部に集まるが、円周方向においては、同じ粒度分布で集
まる。したがって、同じ粒径の触媒が各シュートを通
り、上部ホッパの各ホッパ室に供給される。In this case, the catalyst supplied from the catalyst inlet to the upper distribution hopper forms a mountain having a predetermined angle of repose in the upper distribution hopper. At this time, the catalyst with a large particle diameter falls along the slope of the mountain and gathers in the peripheral portion of the upper distribution hopper, and the catalyst with a small particle diameter gathers in the central portion of the upper distribution hopper, but in the circumferential direction. , With the same particle size distribution. Therefore, the catalyst having the same particle size is supplied to each hopper chamber of the upper hopper through each chute.
【００３３】その結果、前記移動層内において被処理ガ
スは偏流を発生することはないので、空間速度を一様に
低くすることができ、脱硝率を高くすることができる。As a result, the gas to be treated does not generate a drift in the moving bed, so that the space velocity can be uniformly lowered and the denitration rate can be increased.
【図１】本発明の実施例における乾式脱硫・脱硝装置の
概略図である。FIG. 1 is a schematic diagram of a dry desulfurization / denitration apparatus according to an embodiment of the present invention.
【図２】従来の反応塔の斜視図である。FIG. 2 is a perspective view of a conventional reaction tower.
【図３】従来の反応塔の断面図である。FIG. 3 is a cross-sectional view of a conventional reaction tower.
【図４】従来の粒度分布の測定結果を表す図である。FIG. 4 is a diagram showing a conventional measurement result of particle size distribution.
【図５】本発明の実施例における乾式脱硫・脱硝装置の
平面図である。FIG. 5 is a plan view of a dry desulfurization / denitration apparatus according to an embodiment of the present invention.
【図６】従来の乾式脱硫・脱硝装置における粒度分布を
示す図である。FIG. 6 is a diagram showing a particle size distribution in a conventional dry desulfurization / denitration apparatus.
【図７】本発明の実施例における乾式脱硫・脱硝装置の
粒度分布を示す図である。FIG. 7 is a diagram showing a particle size distribution of a dry desulfurization / denitration device in an example of the present invention.
【図８】本発明の実施例における脱硝率、空間速度及び
粒径の関係を示した図である。FIG. 8 is a diagram showing a relationship among a denitration rate, a space velocity and a particle diameter in an example of the present invention.
【図９】各区画室ごとの脱硝率について、従来の乾式脱
硫・脱硝装置と本発明の乾式脱硫・脱硝装置とを比較し
た図である。FIG. 9 is a diagram comparing the denitration rate of each compartment between the conventional dry desulfurization / denitration device and the dry desulfurization / denitration device of the present invention.
【図１０】各区画室ごとの空間速度について、従来の乾
式脱硫・脱硝装置と本発明の乾式脱硫・脱硝装置とを比
較した図である。FIG. 10 is a diagram comparing the space velocity of each compartment between the conventional dry desulfurization / denitration device and the dry desulfurization / denitration device of the present invention.
１７ 触媒 ３６ 上部分配ホッパ ３７ 触媒入口 ３８ 下部逆円錐部 ３９ シュート入口 ４２、４３ 上部ホッパ ４５ ホッパ室 ４７ シュート ５５ 移動層 17 catalyst 36 upper distribution hopper 37 catalyst inlet 38 lower inverted cone 39 chute inlet 42, 43 upper hopper 45 hopper chamber 47 chute 55 moving bed
Claims (1)
円錐形状を有する下部逆円錐部が形成された上部分配ホ
ッパと、（ｂ）触媒を下方に移動させるとともに、被処
理ガスを通すための一対の移動層と、（ｃ）該各移動層
の上端に配設され、複数のホッパ室を備えた上部ホッパ
と、（ｄ）前記下部逆円錐部における同一円上の複数箇
所に形成されたシュート入口と前記各ホッパ室とを連結
するシュートとを有することを特徴とする乾式脱硫・脱
硝装置。1. An upper distribution hopper having (a) a catalyst inlet on an upper wall and a lower inverted conical portion having an inverted conical shape on a lower wall, and (b) moving a catalyst downward and treating the treated material. A pair of moving layers for passing gas, (c) an upper hopper provided at the upper end of each moving layer and having a plurality of hopper chambers, and (d) a plurality of lower circular cones on the same circle. A dry desulfurization / denitration apparatus having a chute inlet formed at a location and a chute connecting the hopper chambers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13937895A JP3351658B2 (en) | 1995-06-06 | 1995-06-06 | Dry desulfurization / denitration equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13937895A JP3351658B2 (en) | 1995-06-06 | 1995-06-06 | Dry desulfurization / denitration equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08332347A true JPH08332347A (en) | 1996-12-17 |
| JP3351658B2 JP3351658B2 (en) | 2002-12-03 |
Family
ID=15243932
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13937895A Expired - Fee Related JP3351658B2 (en) | 1995-06-06 | 1995-06-06 | Dry desulfurization / denitration equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3351658B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7368090B2 (en) * | 2000-11-21 | 2008-05-06 | Uop Llc | FCC spent catalyst distributor |
| JP2010167406A (en) * | 2008-12-26 | 2010-08-05 | Mitsubishi Chemicals Corp | Method for charging fillers in plate reactor |
| JP2013052377A (en) * | 2011-09-06 | 2013-03-21 | Sumitomo Heavy Ind Ltd | Exhaust gas treatment apparatus and exhaust gas treatment method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7086216B2 (en) * | 2018-11-08 | 2022-06-17 | 三菱電機株式会社 | Air conditioner |
-
1995
- 1995-06-06 JP JP13937895A patent/JP3351658B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7368090B2 (en) * | 2000-11-21 | 2008-05-06 | Uop Llc | FCC spent catalyst distributor |
| JP2010167406A (en) * | 2008-12-26 | 2010-08-05 | Mitsubishi Chemicals Corp | Method for charging fillers in plate reactor |
| JP2013052377A (en) * | 2011-09-06 | 2013-03-21 | Sumitomo Heavy Ind Ltd | Exhaust gas treatment apparatus and exhaust gas treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3351658B2 (en) | 2002-12-03 |
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