JP3115545B2 - Operation method of chlorine bypass equipment - Google Patents
Operation method of chlorine bypass equipmentInfo
- Publication number
- JP3115545B2 JP3115545B2 JP09191403A JP19140397A JP3115545B2 JP 3115545 B2 JP3115545 B2 JP 3115545B2 JP 09191403 A JP09191403 A JP 09191403A JP 19140397 A JP19140397 A JP 19140397A JP 3115545 B2 JP3115545 B2 JP 3115545B2
- Authority
- JP
- Japan
- Prior art keywords
- probe
- cyclone
- exhaust gas
- chlorine
- amount
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Biodiversity & Conservation Biology (AREA)
- Ecology (AREA)
- Environmental & Geological Engineering (AREA)
- Environmental Sciences (AREA)
- Public Health (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】この発明は、塩素バイパス設
備の運転方法に係り、特にバイパス率によらずに効率の
よい塩素除去を行うことができる方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for operating a chlorine bypass facility, and more particularly to a method for efficiently removing chlorine regardless of a bypass ratio.
【０００２】[0002]
【従来の技術】一般に、セメントクリンカをキルンにて
焼成する場合、セメント原料及び燃料から持ち込まれる
塩素、アルカリ、硫黄等の揮発性成分は、キルン・プレ
ヒータ系内で循環することにより次第に濃縮され、短時
間で平衡状態に達し、セメント原料及び燃料から持ち込
まれる揮発性成分の量とセメントクリンカにより系外へ
持ち出される揮発性成分の量とが等しくなることが知ら
れている。このため、セメント原料及び燃料から持ち込
まれる揮発性成分の量が多いと、セメントクリンカ中に
含まれる揮発性成分量も多くなって製品としてのセメン
トの品質に悪影響を与えることとなる。また、系内の揮
発性成分量が多くなると、低融点化合物が形成されるた
めにプレヒータサイクロンが閉塞して、キルンの安定運
転が損なわれる惧れがある。2. Description of the Related Art Generally, when a cement clinker is fired in a kiln, volatile components such as chlorine, alkali, and sulfur brought from the cement raw material and fuel are gradually concentrated by circulating in a kiln / preheater system. It is known that an equilibrium state is reached in a short time, and the amount of volatile components brought in from a cement raw material and fuel is equal to the amount of volatile components taken out of a system by a cement clinker. For this reason, when the amount of the volatile component brought in from the cement raw material and the fuel is large, the amount of the volatile component contained in the cement clinker is also increased, which adversely affects the quality of the cement as a product. Further, when the amount of volatile components in the system increases, the preheater cyclone may be blocked due to the formation of a low melting point compound, and the stable operation of the kiln may be impaired.
【０００３】そこで、従来、キルン・プレヒータ系内の
揮発性成分量を減少させるために、アルカリバイパス法
が採用されてきた。この方法は、揮発性成分濃度の高い
キルン排ガスをプローブを用いて系外に抜き出し、排ガ
スからアルカリを除去する方法である。しかしながら、
このアルカリバイパス法は、温度約１０００℃のキルン
排ガスを系外へ排出するために、熱損失が大きく、また
大量のダストを系外へ排出して廃棄処分を行うために処
分場所の確保が年々困難になりつつある。[0003] Therefore, in order to reduce the amount of volatile components in a kiln preheater system, an alkali bypass method has conventionally been employed. In this method, a kiln exhaust gas having a high volatile component concentration is extracted out of the system using a probe, and alkali is removed from the exhaust gas. However,
This alkaline bypass method has a large heat loss in order to discharge kiln exhaust gas at a temperature of about 1000 ° C outside the system. In addition, it is necessary to secure a disposal site every year to discharge a large amount of dust outside the system for disposal. It's getting harder.
【０００４】このような背景の下、揮発性成分の中で、
塩素は特に揮発率が高く、少量の抽気量（バイパス率）
で塩素濃度の大幅な低減化が可能であることがわかり、
キルン排ガスからの塩素の除去を目的とした塩素バイパ
ス法が開発された。この塩素バイパス法を行うための設
備を概略的に図５に示す。キルン１の窯尻からプローブ
２によって排ガスを抽気すると共にプローブ２内に冷風
（外気）を供給して排ガスを急冷する。このとき、排ガ
ス中に含まれる塩素は塩素化合物の融点である６００〜
７００℃程度以下まで冷却されて微粒子として固化す
る。抽出された排ガスは分級器３に送られ、ここで塩素
濃度の低い粗粉ダストと塩素濃度の高い微粉ダストとに
分級され、粗粉ダストは再びキルン系へ戻される。一
方、微粉ダストは排ガスと共に冷却器４でさらに冷却さ
れた後、集塵機５で高塩素濃度のダストが回収されて許
容濃度範囲内でセメントに添加され、排ガスはキルン系
に戻される。Under such a background, among volatile components,
Chlorine has a particularly high volatility, and a small amount of bleed air (bypass rate)
Shows that it is possible to greatly reduce the chlorine concentration.
A chlorine bypass method has been developed to remove chlorine from kiln exhaust gas. The equipment for performing this chlorine bypass method is schematically shown in FIG. Exhaust gas is extracted by the probe 2 from the kiln butt of the kiln 1 and cool air (outside air) is supplied into the probe 2 to rapidly cool the exhaust gas. At this time, chlorine contained in the exhaust gas has a melting point of chlorine compound of 600 to 600.
It is cooled to about 700 ° C. or less and solidified as fine particles. The extracted exhaust gas is sent to the classifier 3, where it is classified into coarse dust having a low chlorine concentration and fine dust having a high chlorine concentration, and the coarse dust is returned to the kiln system again. On the other hand, the fine dust is further cooled by the cooler 4 together with the exhaust gas, and then the dust having a high chlorine concentration is collected by the dust collector 5 and added to the cement within an allowable concentration range, and the exhaust gas is returned to the kiln system.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、このよ
うな塩素バイパス設備の運転においては、キルン１への
インプット塩素量、キルン１の運転状態等に応じてその
時点の最適なバイパス率があり、この最適バイパス率を
無視して設備能力の最大バイパス率（負荷１００％）で
運転すると、以下のような問題点が発生して効率のよい
塩素除去を行うことができなくなる。すなわち、抽出ガ
ス量が必要以上に増加し、それに比例して熱量損失が増
大すると共にバイパスダスト量が増大する。また、バイ
パスダスト量の増加に伴ってダストの塩素濃度が低下す
る。However, in the operation of such a chlorine bypass facility, there is an optimum bypass ratio at that time depending on the amount of chlorine input to the kiln 1, the operating state of the kiln 1, and the like. If the operation is performed at the maximum bypass ratio (load 100%) of the facility capacity ignoring the optimum bypass ratio, the following problems occur, and efficient chlorine removal cannot be performed. That is, the amount of the extracted gas increases more than necessary, and the heat loss increases in proportion thereto, and the amount of the bypass dust increases. In addition, the chlorine concentration of the dust decreases as the amount of bypass dust increases.
【０００６】このため、一般的には、その時点における
最適バイパス率、すなわち低負荷で運転されることが多
い。このとき、例えば７０％以上の負荷であれば問題な
いが、さらに負荷を下げてバイパス率を低く設定する
と、今度はプローブ２の内部及びプローブ２と分級器３
との間のダクト内でガス流速が低下し、ここにダストの
堆積が発生するという問題が生じてくる。また、分級器
３の入口流速が低下するため、分級効率が悪化し、バイ
パスダスト量の増加及びダストの塩素濃度の低下を来し
てしまう。For this reason, in general, the vehicle is often operated with an optimum bypass ratio at that time, that is, a low load. At this time, if the load is, for example, 70% or more, there is no problem. However, if the load is further reduced and the bypass ratio is set low, the inside of the probe 2 and the
The gas flow velocity is reduced in the duct between them, and a problem arises in that dust accumulation occurs here. Further, since the inlet flow velocity of the classifier 3 decreases, the classification efficiency deteriorates, and the amount of bypass dust increases and the chlorine concentration of dust decreases.
【０００７】従って、特に、将来のインプット塩素量増
加を見越して大容量、すなわち最大バイパス率の大きな
設備を設置し、現状ではインプット塩素量が計画値に達
しない場合には、最大負荷で運転しても、低負荷で運転
しても、効率のよい塩素除去ができないという問題があ
る。[0007] Accordingly, in particular, a large capacity facility, that is, a large maximum bypass ratio is installed in anticipation of an increase in the amount of input chlorine in the future, and if the input chlorine amount does not reach the planned value at present, operation is performed at the maximum load. However, there is a problem that even when operated at a low load, efficient chlorine removal cannot be performed.
【０００８】この発明はこのような問題点を解消するた
めになされたもので、バイパス率に左右されずに効率の
よい塩素除去を行うことができる塩素バイパス設備の運
転方法を提供することを目的とする。The present invention has been made in order to solve such a problem, and an object of the present invention is to provide a method of operating a chlorine bypass facility capable of performing efficient chlorine removal without being influenced by a bypass ratio. And
【０００９】[0009]
【課題を解決するための手段】第１の発明に係る塩素バ
イパス設備の運転方法は、所定のサイクロン入口ガス流
速が得られるようにキルン排ガスの抽気量に応じてプロ
ーブ内に供給する外気の量を調整する方法である。第２
の発明に係る塩素バイパス設備の運転方法は、サイクロ
ンの入口に可変絞りを設け、キルン排ガスの抽気量に応
じて可変絞りの開度を調整することにより所定のサイク
ロン入口ガス流速を確保する方法である。第３の発明に
係る塩素バイパス設備の運転方法は、プローブに並列に
２系列のサイクロンを接続し、キルン排ガスの抽気量が
最大値の５０％以下のときに一方のサイクロンを閉じて
他方のサイクロンのみで分級を行うことにより所定のサ
イクロン入口ガス流速を確保する方法である。この場
合、さらに他方のサイクロンの入口に可変絞りを設け、
キルン排ガスの抽気量に応じて可変絞りの開度を調整す
るようにしてもよい。第４の発明に係る塩素バイパス設
備の運転方法は、プローブとサイクロンをそれぞれ並列
に２系列配置し、キルン排ガスの抽気量が最大値の５０
％以下のときに一方のプローブからの抽気を停止して他
方のプローブのみで抽気を行うことにより所定のサイク
ロン入口ガス流速を確保する方法である。According to a first aspect of the present invention, there is provided a method for operating a chlorine bypass facility, comprising: an amount of outside air supplied to a probe according to an amount of extracted kiln exhaust gas so as to obtain a predetermined cyclone inlet gas flow velocity. It is a method of adjusting. Second
The operation method of the chlorine bypass facility according to the invention of the present invention is a method in which a variable throttle is provided at the inlet of the cyclone, and a predetermined cyclone inlet gas flow rate is secured by adjusting the opening of the variable throttle according to the amount of extracted air of the kiln exhaust gas. is there. In the method for operating a chlorine bypass facility according to a third aspect of the present invention, two cyclones are connected in parallel to the probe, and when the amount of bled gas of the kiln exhaust gas is 50% or less of the maximum value, one cyclone is closed and the other cyclone is closed. This is a method of securing a predetermined cyclone inlet gas flow velocity by performing classification only by using a classification. In this case, a variable throttle is provided at the inlet of the other cyclone,
The opening degree of the variable throttle may be adjusted in accordance with the amount of the extracted kiln exhaust gas. The operation method of the chlorine bypass facility according to the fourth invention is such that the probe and the cyclone are respectively arranged in two lines in parallel, and the amount of extracted gas of the kiln exhaust gas is 50, which is the maximum value.
%, The extraction from one probe is stopped, and the extraction is performed only by the other probe to ensure a predetermined cyclone inlet gas flow rate.
【００１０】これら第１〜第４の発明によれば、それぞ
れサイクロンの入口において所定のガス流速が得られる
ため、プローブとサイクロンとの間のダクト内における
ダストの堆積が防止されると共にサイクロンにおける分
級効率の低下が防止され、効率のよい塩素除去が可能と
なる。According to the first to fourth aspects of the present invention, since a predetermined gas flow velocity is obtained at each of the cyclone inlets, dust accumulation in the duct between the probe and the cyclone is prevented, and classification in the cyclone is performed. A decrease in efficiency is prevented, and efficient chlorine removal becomes possible.
【００１１】[0011]
【発明の実施の形態】以下、この発明の実施の形態を添
付図面に基づいて説明する。 実施の形態１．図１にこの発明の実施の形態１に係る運
転方法を実施するための塩素バイパス設備を示す。キル
ン１１の窯尻にプローブ１２が設けられている。プロー
ブ１２は内管と外管からなる二重管構造を有しており、
内管を通してキルン１１の窯尻からキルン排ガスを抽気
するが、このときプローブ冷却ファン１３によって外部
から内管と外管との間を通してキルン１１の窯尻方向に
外気を供給することによりキルン排ガスは温度６００〜
７００℃程度以下にまで一次冷却される。この一次冷却
によりキルン排ガス中の塩素分は主にＫＣｌとして凝固
し、粒径５〜７μｍ程度以下の微粉ダストとなって排ガ
スと共に内管を通して抽出される。Embodiments of the present invention will be described below with reference to the accompanying drawings. Embodiment 1 FIG. FIG. 1 shows a chlorine bypass facility for carrying out the operating method according to Embodiment 1 of the present invention. A probe 12 is provided at the kiln end of the kiln 11. The probe 12 has a double tube structure including an inner tube and an outer tube,
Kiln exhaust gas is extracted from the kiln tail of the kiln 11 through the inner pipe. At this time, the kiln exhaust gas is supplied by supplying outside air from the outside to the kiln tail direction of the kiln 11 through the space between the inner pipe and the outer pipe by the probe cooling fan 13. Temperature 600 ~
The primary cooling is performed to about 700 ° C. or less. By this primary cooling, the chlorine content in the kiln exhaust gas is mainly solidified as KCl, and is converted into fine powder dust having a particle size of about 5 to 7 μm or less through the inner pipe together with the exhaust gas.
【００１２】プローブ１２の内管の出口には、例えば分
級点を５〜７μｍに設定した粗粉分級サイクロン１４が
接続されている。プローブ１２による抽気ガス中のダス
トは、この粗粉分級サイクロン１４で分級され、粒径５
〜７μｍ以上の粗粉ダストは含有塩素濃度が低いためキ
ルン１１へ再循環される。一方、微粉ダストは抽気ガス
と共に冷却器１５に送られ、ここで冷却器冷風ファン１
６から供給された冷風により温度２００℃以下に二次冷
却される。その後、抽気ガス中の微粉ダストは、バグフ
ィルタ１７で捕捉され、回収ダストタンク１８に回収さ
れる。この微粉ダストは、高濃度の塩素を含有している
が、通常キルン生産量の０．１％以下と少量であり、ミ
ル添加用タンク１９及び定量供給器２０を介してセメン
ト粉砕系に送られ、許容範囲内でセメントに添加され
る。なお、この高濃度の塩素を含有する微粉ダストは、
セメント生産量の０．１％までの添加であれば、セメン
トの品質上の問題はほとんどないことが確認されてい
る。また、バグフィルタ１７で微粉ダストが除去された
抽気ガスは、排気ファン２１によりキルン系に戻され
る。An outlet of the inner tube of the probe 12 is connected to a coarse powder classification cyclone 14 having a classification point of, for example, 5 to 7 μm. Dust in the extracted gas by the probe 12 is classified by the coarse powder classification cyclone
The coarse dust having a diameter of 7 μm or more is recirculated to the kiln 11 because the chlorine content is low. On the other hand, the fine dust is sent to the cooler 15 together with the bleed gas, where the cooler fan 1
The secondary cooling is performed to a temperature of 200 ° C. or less by the cool air supplied from 6. Thereafter, the fine dust in the extracted gas is captured by the bag filter 17 and collected in the collection dust tank 18. Although this fine dust contains a high concentration of chlorine, it is usually a small amount of 0.1% or less of the kiln production amount, and is sent to the cement grinding system via the mill addition tank 19 and the fixed amount feeder 20. , Are added to the cement within acceptable limits. The fine dust containing high concentration of chlorine is
It has been confirmed that there is almost no problem with the quality of cement if it is added up to 0.1% of the cement production. The extracted gas from which fine dust has been removed by the bag filter 17 is returned to the kiln system by the exhaust fan 21.
【００１３】なお、冷却器１５の入口ダクトには一次冷
却後の抽気ガスの温度を検出する温度センサ２２が設け
られ、プローブ冷却ファン１３にはダンパ２３が接続さ
れると共にこのダンパ２３の開度を調整するためのモー
タ２４が設けられており、温度センサ２２で検出された
抽気ガスの温度が６００〜７００℃程度以下の設定値に
なるように、モータ２４によってダンパ２３の開度が調
整される。また、バグフィルタ１７の入口ダクトには二
次冷却後の抽気ガスの温度を検出する温度センサ２５が
設けられており、この温度センサ２５で検出された抽気
ガスの温度が２００℃程度以下の設定値になるように、
冷却器冷風ファン１６の回転数が調整される。ここで、
温度センサ２２及び温度センサ２５で検出される温度の
各設定値は、例えばキルン１１の運転状況やバイパス率
によって最適な値に設定される。The inlet duct of the cooler 15 is provided with a temperature sensor 22 for detecting the temperature of the extracted gas after the primary cooling, and a damper 23 is connected to the probe cooling fan 13 and the opening degree of the damper 23 is increased. Is provided, and the opening degree of the damper 23 is adjusted by the motor 24 so that the temperature of the bleed gas detected by the temperature sensor 22 becomes a set value of about 600 to 700 ° C. or less. You. The inlet duct of the bag filter 17 is provided with a temperature sensor 25 for detecting the temperature of the bleed gas after the secondary cooling. The temperature of the bleed gas detected by the temperature sensor 25 is set to about 200 ° C. or less. To be a value,
The rotation speed of the cooler cool air fan 16 is adjusted. here,
Each set value of the temperature detected by the temperature sensor 22 and the temperature sensor 25 is set to an optimum value according to, for example, the operation state of the kiln 11 and the bypass ratio.
【００１４】また、排気ファン２１にはダンパ２６が接
続されると共にこのダンパ２６の開度を調整するための
モータ２７が設けられており、ダンパ２６の開度を変え
ることによりキルン１１の窯尻からの抽気量、すなわち
バイパス率を調整することができる。塩素バイパス設備
の能力として、例えば最大バイパス率５％程度に設定さ
れるが、キルン１１内に持ち込まれる塩素量やキルン１
１の運転状態に応じてダンパ２６の開度を調整し、バイ
パス率をそのときの最適な値にまで下げて運転が行われ
る。このとき、バイパス率を下げることにより、プロー
ブ１２から粗粉分級サイクロン１４に流れるガス量が少
なくなるので、バイパス率によってはダクト内にダスト
が堆積したり、粗粉分級サイクロン１４における分級効
率が低下する惧れがある。A damper 26 is connected to the exhaust fan 21 and a motor 27 for adjusting the opening of the damper 26 is provided. By changing the opening of the damper 26, the kiln bottom of the kiln 11 is changed. , That is, the bypass ratio can be adjusted. The capacity of the chlorine bypass facility is set, for example, to a maximum bypass rate of about 5%.
The operation is performed by adjusting the opening degree of the damper 26 in accordance with the operation state 1 and reducing the bypass ratio to the optimum value at that time. At this time, by reducing the bypass ratio, the amount of gas flowing from the probe 12 to the coarse particle classification cyclone 14 decreases, so that dust accumulates in the duct and the classification efficiency in the coarse particle classification cyclone 14 decreases depending on the bypass ratio. There is a fear.
【００１５】そこで、この実施の形態１においては、粗
粉分級サイクロン１４の入口で所定のガス流速が得られ
るように、バイパス率すなわち抽気量に応じてモータ２
４によりダンパ２３の開度を変えてプローブ冷却ファン
１３からプローブ１２へ供給される外気の量を調整す
る。具体的には、バイパス率を下げたときには、温度セ
ンサ２２で検出される温度の設定値を低くすることによ
りダンパ２３の開度を大きくしてプローブ冷却ファン１
３からの外気量を増加する。これにより、ダクト内のダ
ストの堆積や粗粉分級サイクロン１４における分級効率
の低下が事前に防止される。また、同時に、プローブ１
２に供給する外気量の増大に伴ってプローブ１２におけ
る一次冷却の効果が増大するため、温度センサ２２で検
出される抽気ガスの温度は低くなる。ただし、このとき
抽気ガスの温度が酸露点（８０℃程度）を下回らないよ
うにすることが望ましい。Therefore, in the first embodiment, the motor 2 is controlled in accordance with the bypass ratio, that is, the amount of extracted air, so that a predetermined gas flow rate is obtained at the inlet of the coarse powder classification cyclone 14.
4, the opening degree of the damper 23 is changed to adjust the amount of outside air supplied from the probe cooling fan 13 to the probe 12. Specifically, when the bypass ratio is lowered, the opening of the damper 23 is increased by lowering the set value of the temperature detected by the temperature sensor 22 to increase the probe cooling fan 1.
3. Increase the outside air volume from 3. As a result, the accumulation of dust in the duct and the decrease in classification efficiency in the coarse powder classification cyclone 14 are prevented in advance. At the same time, probe 1
Since the effect of the primary cooling in the probe 12 increases with an increase in the amount of outside air supplied to the probe 2, the temperature of the bleed gas detected by the temperature sensor 22 decreases. However, at this time, it is desirable that the temperature of the extracted gas does not fall below the acid dew point (about 80 ° C.).
【００１６】実施の形態２．図１に示した塩素バイパス
設備において、図２に示されるように、粗粉分級サイク
ロン１４の入口に可変絞り３１を設け、キルン排ガスの
抽気量に応じて可変絞り３１の開度を調整するように構
成することもできる。具体的には、バイパス率を下げて
抽気量が少ない場合に、可変絞り３１の開度を小さくし
て、所定のサイクロン入口ガス流速を確保する。これに
より、ガス流速の低下に起因する分級効率の低下を防止
することができる。Embodiment 2 In the chlorine bypass facility shown in FIG. 1, as shown in FIG. 2, a variable throttle 31 is provided at the inlet of the coarse powder classification cyclone 14, and the opening degree of the variable throttle 31 is adjusted according to the amount of bled gas of the kiln exhaust gas. Can also be configured. Specifically, when the amount of bleed air is small by reducing the bypass ratio, the opening degree of the variable throttle 31 is reduced to secure a predetermined cyclone inlet gas flow velocity. As a result, it is possible to prevent a decrease in classification efficiency due to a decrease in gas flow velocity.
【００１７】実施の形態３．図１に示した塩素バイパス
設備において、図３に示されるように、粗粉分級サイク
ロン１４として第１及び第２のサイクロン４１及び４２
からなる２系列のダブルサイクロンを使用し、これら第
１及び第２のサイクロン４１及び４２を並列にプローブ
１２に接続することができる。さらに、第１のサイクロ
ン４１の入口にはこの第１のサイクロン４１への抽気ガ
スの流入を遮断するためのシャッタ４３が設けられ、第
２のサイクロン４２の入口には可変絞り４４が設けられ
ている。また、第１及び第２のサイクロン４１及び４２
の出口ダクトは合流して１系列とした後、冷却器１５に
接続されている。Embodiment 3 In the chlorine bypass facility shown in FIG. 1, as shown in FIG. 3, first and second cyclones 41 and 42 are used as coarse powder classification cyclones 14.
And the first and second cyclones 41 and 42 can be connected to the probe 12 in parallel. Further, at the entrance of the first cyclone 41, a shutter 43 for blocking the inflow of the bleed gas into the first cyclone 41 is provided, and at the entrance of the second cyclone 42, a variable throttle 44 is provided. I have. Also, the first and second cyclones 41 and 42
Outlet ducts are merged into one line, and then connected to the cooler 15.
【００１８】このような構成の粗粉分級サイクロン１４
を用い、バイパス率に応じてシャッタ４３及び可変絞り
４４を調整する。具体的には、最大バイパス率で運転す
る際には、シャッタ４３を開くと共に可変絞り４４を全
開とし、バイパス率が下がるにつれて可変絞り４４の開
度を小さくして所定のサイクロン入口ガス流速を確保す
る。そして、バイパス率が最大バイパス率の５０％以下
になった場合には、シャッタ４３を閉じて第１のサイク
ロン４１への抽気ガスの流入を遮断すると共に可変絞り
４４を大きく開いて第２のサイクロン４２のみで分級を
行う。さらに、バイパス率が下がるにつれて可変絞り４
４の開度を小さくする。このようにすることにより、極
めて広範囲のバイパス率に対して所定のサイクロン入口
ガス流速を確保することができ、ガス流速の低下に起因
する分級効率の低下を防止することが可能となる。The coarse powder classification cyclone 14 having the above-described structure.
To adjust the shutter 43 and the variable aperture 44 according to the bypass ratio. Specifically, when operating at the maximum bypass ratio, the shutter 43 is opened and the variable throttle 44 is fully opened, and as the bypass ratio decreases, the opening of the variable throttle 44 is reduced to secure a predetermined cyclone inlet gas flow rate. I do. When the bypass ratio becomes 50% or less of the maximum bypass ratio, the shutter 43 is closed to block the flow of the bleed gas into the first cyclone 41, and the variable throttle 44 is greatly opened to open the second cyclone. Classification is performed with only 42. Further, as the bypass ratio decreases, the variable throttle 4
4 is made smaller. By doing so, a predetermined cyclone inlet gas flow rate can be secured for an extremely wide range of bypass ratio, and it is possible to prevent a decrease in classification efficiency due to a decrease in gas flow rate.
【００１９】実施の形態４．図１に示した塩素バイパス
設備において、図４に示されるように、プローブとサイ
クロンをそれぞれ並列に２系列配置することもできる。
すなわち、キルン１１の窯尻に二重管構造のプローブ５
１及び５２が設けられ、これらプローブ５１及び５２の
内管の出口にそれぞれ粗粉分級サイクロン５３及び５４
が接続される。粗粉分級サイクロン５３及び５４の出口
ダクトは合流して１系列とした後、冷却器１５に接続さ
れている。プローブ５１及び５２には、それぞれ外部か
ら内管と外管との間を通してキルン１１の窯尻方向に外
気を供給するためのプローブ冷却ファン５５及び５６が
接続され、各プローブ冷却ファン５５及び５６にダクト
５７及び５８とダクト駆動用モータ５９及び６０が接続
されている。Embodiment 4 In the chlorine bypass facility shown in FIG. 1, as shown in FIG. 4, two series of probes and cyclones can be arranged in parallel.
That is, a probe 5 having a double tube structure is attached to the kiln bottom of the kiln 11.
1 and 52 are provided, and coarse powder classification cyclones 53 and 54 are provided at the outlets of the inner tubes of the probes 51 and 52, respectively.
Is connected. The outlet ducts of the coarse powder classifying cyclones 53 and 54 are combined into one line, and then connected to the cooler 15. Probe cooling fans 55 and 56 for supplying outside air to the kiln end of the kiln 11 from the outside through the inner pipe and the outer pipe are connected to the probes 51 and 52, respectively. Ducts 57 and 58 and duct driving motors 59 and 60 are connected.
【００２０】そして、バイパス率が最大バイパス率の５
０％より高いときには、２系列のプローブ５１及び５２
の双方から抽気して２台の粗粉分級サイクロン５３及び
５４で分級を行い、バイパス率が最大バイパス率の５０
％以下になった場合には、一方のプローブ５１からの抽
気を停止し、他方のプローブ５２のみで抽気を行い、一
つの粗粉分級サイクロン５４のみで分級を行う。このよ
うにすることにより、ダクト内とサイクロン入口におい
て所定のガス流速を確保することができ、ダクト内のダ
ストの堆積や分級効率の低下を防止することが可能とな
る。The bypass ratio is 5 which is the maximum bypass ratio.
When it is higher than 0%, the two series of probes 51 and 52
The air is extracted from both sides and classified by two coarse powder classification cyclones 53 and 54, and the bypass ratio is set to the maximum bypass ratio of 50.
%, The extraction from one probe 51 is stopped, the extraction is performed only by the other probe 52, and the classification is performed only by one coarse powder classification cyclone 54. By doing so, a predetermined gas flow velocity can be secured in the duct and in the cyclone inlet, and it is possible to prevent accumulation of dust in the duct and a decrease in classification efficiency.
【００２１】なお、予めプローブ５１と粗粉分級サイク
ロン５３とを接続するダクト等にダンパを設けておき、
このダンパを閉じることによってプローブ５１からの抽
気を停止することができる。A damper is provided in a duct or the like connecting the probe 51 and the coarse powder classification cyclone 53 in advance.
By closing this damper, the bleeding from the probe 51 can be stopped.
【００２２】上述した実施の形態１〜４の運転方法は、
それぞれ単独に行うこともでき、あるいは互いに併用す
ることもできる。The operating method according to the first to fourth embodiments is as follows.
Each of them can be performed alone or in combination with each other.
【００２３】[0023]
【発明の効果】以上説明したように、この発明によれ
ば、サイクロンの入口において所定のガス流速が確保さ
れるので、プローブとサイクロンとの間のダクト内にお
けるダストの堆積及びサイクロンにおける分級効率の低
下が防止され、効率のよい塩素除去を行うことが可能と
なる。As described above, according to the present invention, a predetermined gas flow rate is ensured at the inlet of the cyclone, so that dust accumulation in the duct between the probe and the cyclone and the classification efficiency in the cyclone are reduced. The decrease is prevented, and efficient chlorine removal can be performed.
【図１】この発明の実施の形態１に係る運転方法を実施
するための塩素バイパス設備を示すフロー図である。FIG. 1 is a flowchart showing a chlorine bypass facility for implementing an operation method according to Embodiment 1 of the present invention.
【図２】実施の形態２に係る運転方法を実施するための
粗粉分級サイクロンを示す図である。FIG. 2 is a diagram showing a coarse powder classification cyclone for implementing an operation method according to a second embodiment.
【図３】実施の形態３に係る運転方法を実施するための
粗粉分級サイクロンを示す図である。FIG. 3 is a diagram showing a coarse powder classification cyclone for performing an operation method according to a third embodiment.
【図４】実施の形態４に係る運転方法を実施するための
塩素バイパス設備を示す部分的なフロー図である。FIG. 4 is a partial flow chart showing a chlorine bypass facility for performing an operation method according to a fourth embodiment.
【図５】塩素バイパス設備における概略的なフロー図で
ある。FIG. 5 is a schematic flow chart in a chlorine bypass facility.
１１ キルン １２，５１，５２ プローブ １３，５５，５６ プローブ冷却ファン １４，５３，５４ 粗粉分級サイクロン １５ 冷却器 １６ 冷却器冷風ファン １７ バグフィルタ １８ 回収ダストタンク ２１ 排気ファン ２２，２５ 温度センサ ２３，２６，５７，５８ ダンパ ２４，２７，５９，６０ モータ ３１，４４ 可変絞り ４１ 第１のサイクロン ４２ 第２のサイクロン ４３ シャッタ Reference Signs List 11 Kiln 12, 51, 52 Probe 13, 55, 56 Probe cooling fan 14, 53, 54 Cyclone for coarse powder classification 15 Cooler 16 Cooler cool air fan 17 Bag filter 18 Collection dust tank 21 Exhaust fan 22, 25 Temperature sensor 23, 26, 57, 58 Damper 24, 27, 59, 60 Motor 31, 44 Variable throttle 41 First cyclone 42 Second cyclone 43 Shutter
───────────────────────────────────────────────────── フロントページの続き (58)調査した分野(Int.Cl.7，ＤＢ名) C04B 7/00 - 7/60 ──────────────────────────────────────────────────続 き Continued on front page (58) Field surveyed (Int. Cl. 7 , DB name) C04B 7/ 00-7/60
Claims (5)
と共にプローブ内に外気を取り入れて一次冷却し、サイ
クロンで粗粉を分離した後、冷却器で二次冷却し、さら
に集塵機で高塩素濃度の微粉ダストを回収する塩素バイ
パス設備の運転方法において、 所定のサイクロン入口ガス流速が得られるようにキルン
排ガスの抽気量に応じてプローブ内に供給する外気の量
を調整することを特徴とする塩素バイパス設備の運転方
法。1. A kiln exhaust gas is bled by a probe, primary air is cooled by taking in outside air into the probe, coarse powder is separated by a cyclone, secondary cooled by a cooler, and fine dust having a high chlorine concentration by a dust collector. The method of operating a chlorine bypass facility for recovering water, wherein the amount of outside air supplied to the probe is adjusted according to the amount of bled gas of the kiln exhaust gas so that a predetermined cyclone inlet gas flow rate is obtained. how to drive.
と共にプローブ内に外気を取り入れて一次冷却し、サイ
クロンで粗粉を分離した後、冷却器で二次冷却し、さら
に集塵機で高塩素濃度の微粉ダストを回収する塩素バイ
パス設備の運転方法において、 サイクロンの入口に可変絞りを設け、キルン排ガスの抽
気量に応じて可変絞りの開度を調整することにより所定
のサイクロン入口ガス流速を確保することを特徴とする
塩素バイパス設備の運転方法。2. A kiln exhaust gas is bled by a probe, and outside air is taken into the probe for primary cooling, coarse powder is separated by a cyclone, secondary cooling is performed by a cooler, and fine dust having a high chlorine concentration is further collected by a dust collector. The method of operating a chlorine bypass facility that recovers wastewater is characterized in that a variable throttle is provided at the cyclone inlet, and a predetermined cyclone inlet gas flow rate is secured by adjusting the opening of the variable throttle according to the amount of extracted bleached kiln exhaust gas. How to operate chlorine bypass equipment.
と共にプローブ内に外気を取り入れて一次冷却し、サイ
クロンで粗粉を分離した後、冷却器で二次冷却し、さら
に集塵機で高塩素濃度の微粉ダストを回収する塩素バイ
パス設備の運転方法において、 プローブに並列に２系列のサイクロンを接続し、キルン
排ガスの抽気量が最大値の５０％以下のときに一方のサ
イクロンを閉じて他方のサイクロンのみで分級を行うこ
とにより所定のサイクロン入口ガス流速を確保すること
を特徴とする塩素バイパス設備の運転方法。3. A kiln exhaust gas is bled by a probe and outside air is taken into the probe to be cooled primarily, separated into coarse particles by a cyclone, secondary cooled by a cooler, and further finely dusted with a high chlorine concentration by a dust collector. In the operation method of the chlorine bypass facility for recovering wastewater, two series of cyclones are connected in parallel with the probe, and when the amount of bled gas of kiln exhaust gas is 50% or less of the maximum value, one cyclone is closed and classification is performed using only the other cyclone. A method of operating a chlorine bypass facility, wherein a predetermined cyclone inlet gas flow rate is secured by performing the following.
け、キルン排ガスの抽気量に応じて可変絞りの開度を調
整することを特徴とする請求項３に記載の塩素バイパス
設備の運転方法。4. The method for operating a chlorine bypass facility according to claim 3, wherein a variable throttle is provided at the inlet of the other cyclone, and the opening of the variable throttle is adjusted according to the amount of extracted air of the kiln exhaust gas.
と共にプローブ内に外気を取り入れて一次冷却し、サイ
クロンで粗粉を分離した後、冷却器で二次冷却し、さら
に集塵機で高塩素濃度の微粉ダストを回収する塩素バイ
パス設備の運転方法において、 プローブとサイクロンをそれぞれ並列に２系列配置し、
キルン排ガスの抽気量が最大値の５０％以下のときに一
方のプローブからの抽気を停止して他方のプローブのみ
で抽気を行うことにより所定のサイクロン入口ガス流速
を確保することを特徴とする塩素バイパス設備の運転方
法。5. A kiln exhaust gas is bled by a probe, outside air is taken into the probe and cooled primarily, a coarse powder is separated by a cyclone, secondary cooled by a cooler, and fine dust having a high chlorine concentration by a dust collector. In the operation method of the chlorine bypass facility for recovering wastewater, two lines of probes and cyclones are arranged in parallel,
Chlorine characterized in that when the amount of extracted gas of the kiln exhaust gas is 50% or less of the maximum value, the extraction from one probe is stopped and the extraction is performed only by the other probe to secure a predetermined gas flow rate at the cyclone inlet. How to operate bypass equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09191403A JP3115545B2 (en) | 1997-07-16 | 1997-07-16 | Operation method of chlorine bypass equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09191403A JP3115545B2 (en) | 1997-07-16 | 1997-07-16 | Operation method of chlorine bypass equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH1135354A JPH1135354A (en) | 1999-02-09 |
| JP3115545B2 true JP3115545B2 (en) | 2000-12-11 |
Family
ID=16274033
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP09191403A Expired - Lifetime JP3115545B2 (en) | 1997-07-16 | 1997-07-16 | Operation method of chlorine bypass equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3115545B2 (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020067820A (en) * | 2001-02-19 | 2002-08-24 | 전채현 | Plant for bypassing chlorine |
| JP4650983B2 (en) * | 2001-03-27 | 2011-03-16 | 太平洋セメント株式会社 | Cement production exhaust gas treatment method |
| US7947242B2 (en) | 2002-12-11 | 2011-05-24 | Taiheiyo Cement Corporation | Cement kiln chlorine/sulfur bypass system |
| US7048784B2 (en) * | 2003-01-22 | 2006-05-23 | Taiheiyo Cement Corporation | Method and system for treating exhaust gas from cement manufacturing equipment |
| JP2006089298A (en) * | 2004-09-21 | 2006-04-06 | Sumitomo Osaka Cement Co Ltd | Method and apparatus for disposing exhaust gas in cement firing facility |
| JP4512473B2 (en) * | 2004-11-15 | 2010-07-28 | 太平洋セメント株式会社 | Merger and branching device for extracted gas from cement manufacturing process |
| JP5050330B2 (en) * | 2005-08-31 | 2012-10-17 | 宇部興産株式会社 | Cement kiln extraction exhaust gas treatment method and apparatus |
| JP5157841B2 (en) * | 2008-11-13 | 2013-03-06 | 三菱マテリアル株式会社 | Exhaust gas treatment method and treatment system for cement firing equipment |
| JP5348792B2 (en) * | 2010-03-17 | 2013-11-20 | 太平洋セメント株式会社 | Combustion gas extraction probe and operating method thereof |
| JP6602175B2 (en) * | 2015-11-27 | 2019-11-06 | 太平洋セメント株式会社 | Cement kiln exhaust gas treatment apparatus and treatment method |
-
1997
- 1997-07-16 JP JP09191403A patent/JP3115545B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH1135354A (en) | 1999-02-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP3115545B2 (en) | Operation method of chlorine bypass equipment | |
| JP2007518661A (en) | Cement clinker manufacturing method for extracting a part of rotary furnace exhaust gas stream containing harmful substances | |
| US5937771A (en) | Method of processing kiln exhaust gases by chlorine bypass system and apparatus therefor | |
| JP3125248B2 (en) | Exhaust gas cooling method and device in kiln bypass | |
| JP3552463B2 (en) | Method and apparatus for firing cement raw material | |
| JP3438489B2 (en) | Method and apparatus for treating exhaust gas from a bleed cement kiln | |
| JP4897893B2 (en) | Cyclone with classifier inlet and small particle bypass | |
| JP2008516186A (en) | Cyclone bypass for circulating fluidized bed reactors | |
| CN101717208A (en) | Process method and process system of exhaust gas of cement calcination equipment | |
| EP0801987A2 (en) | Cement clinker grinding apparatus using vertical roller mill and its method | |
| KR102243955B1 (en) | Extracting and cooling device, chlorine bypass system, cement kiln extracted gas treatment method and cement burning apparatus | |
| JP4294871B2 (en) | Kiln exhaust gas bypass device and bypass method | |
| JP3172131B2 (en) | Method and apparatus for removing harmful substances from cement firing equipment | |
| JP2000146458A (en) | Device and method for regulating chlorine concentration of bypass dust | |
| JP2006089298A (en) | Method and apparatus for disposing exhaust gas in cement firing facility | |
| JP2787555B2 (en) | Method and apparatus for reducing unburned coal ash | |
| JP2022128169A (en) | Chlorine bypass system and operation method thereof | |
| JP4158860B2 (en) | Method and apparatus for treating dust in exhaust gas from cement kiln | |
| JPH0372027B2 (en) | ||
| JP2022099642A (en) | Chlorine bypass equipment and operation method thereof, cement clinker production apparatus, and cement clinker production method | |
| JP2004122024A (en) | Zinc-containing slurry treatment apparatus and treatment method | |
| JP4512473B2 (en) | Merger and branching device for extracted gas from cement manufacturing process | |
| JPH1160297A (en) | Flue gas treatment from cement kiln | |
| JP4483150B2 (en) | Air conditioning system for aircraft | |
| JP2022099641A (en) | Chlorine bypass equipment and operation method thereof, cement clinker production apparatus, and cement clinker production method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080929 Year of fee payment: 8 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080929 Year of fee payment: 8 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090929 Year of fee payment: 9 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090929 Year of fee payment: 9 |
|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090929 Year of fee payment: 9 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100929 Year of fee payment: 10 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100929 Year of fee payment: 10 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110929 Year of fee payment: 11 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120929 Year of fee payment: 12 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130929 Year of fee payment: 13 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| EXPY | Cancellation because of completion of term |