JPS62252350A - Treatment for cement kiln exhaust gas - Google Patents
Treatment for cement kiln exhaust gasInfo
- Publication number
- JPS62252350A JPS62252350A JP9314286A JP9314286A JPS62252350A JP S62252350 A JPS62252350 A JP S62252350A JP 9314286 A JP9314286 A JP 9314286A JP 9314286 A JP9314286 A JP 9314286A JP S62252350 A JPS62252350 A JP S62252350A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- dust
- temperature
- kiln
- alkali
- 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.)
- Granted
Links
- 239000004568 cement Substances 0.000 title claims description 21
- 239000000428 dust Substances 0.000 claims description 53
- 239000003513 alkali Substances 0.000 claims description 24
- 239000002245 particle Substances 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 13
- 150000001875 compounds Chemical class 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000002844 melting Methods 0.000 claims description 5
- 230000008018 melting Effects 0.000 claims description 5
- 239000000725 suspension Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 53
- 238000001816 cooling Methods 0.000 description 11
- 238000010586 diagram Methods 0.000 description 10
- 239000002994 raw material Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 230000005611 electricity Effects 0.000 description 4
- 239000007921 spray Substances 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 102000006463 Talin Human genes 0.000 description 1
- 108010083809 Talin Proteins 0.000 description 1
- 238000010009 beating Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000002452 interceptive effect Effects 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
- C04B7/60—Methods for eliminating alkali metals or compounds thereof, e.g. from the raw materials or during the burning process; methods for eliminating other harmful components
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Ceramic Engineering (AREA)
- Health & Medical Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Public Health (AREA)
- Toxicology (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
［発明の目的］
（産業上の利用分野）
本発明は、セメントキルン排ガスの処理方法、特にアル
カリバイパスによってセメントキルンから排ガスの一部
を抽気する場合に適用されるセメントキルン排ガスの処
理方法に関するものである。Detailed Description of the Invention [Object of the Invention] (Industrial Application Field) The present invention relates to a method for treating cement kiln exhaust gas, particularly a method for treating cement kiln exhaust gas, which is applied to extracting a part of the exhaust gas from a cement kiln by an alkaline bypass. The present invention relates to a method for treating kiln exhaust gas.
（従来の技術）
一般に、セメントクリンカをＳＰキルン又はＮＳＰキル
ンにて焼成する場合、セメント原料及び燃料から持込ま
れるアルカリ等の揮発性成分は、キルン・ブレヒータ系
内で循環することにより、順次濃縮される。(Prior art) Generally, when cement clinker is fired in an SP kiln or NSP kiln, volatile components such as alkali brought in from cement raw materials and fuel are sequentially concentrated by circulating within the kiln/breheater system. Ru.
しかし、この種の循環は、数時間で平衡に達し、セメン
ト原料及び燃料から系内に持込まれる揮発性成分のＲと
、セメントクリンカにより系外へ持出される揮発性成分
の母とが等しくなる。However, this type of circulation reaches equilibrium in a few hours, and R of the volatile components brought into the system from cement raw materials and fuel becomes equal to the ratio of volatile components taken out of the system by the cement clinker. .
この場合、セメント原料と燃料とが持込むアルカリ吊が
多いと、クリンカのアルカリωが必然的に多くなり、セ
メントの品質が落ちてしまう。In this case, if the cement raw material and fuel bring in a large amount of alkali, the amount of alkali ω in the clinker will inevitably increase, and the quality of the cement will deteriorate.
又、系内に揮発性成分（アルカリ、塩素、硫黄）が多い
と、系内に低融点化合物が形成され、特にブレヒータが
頻繁に閉塞して、キルン操業の妨げとなる。Furthermore, if there are many volatile components (alkali, chlorine, sulfur) in the system, low melting point compounds will be formed in the system, which will frequently clog the breheater, interfering with kiln operation.
従っＣ１系内のアルカリ岳を減少させる必要があり、こ
の場合に所謂アルカリバイパスが行なわれる。Therefore, it is necessary to reduce the alkaline content in the C1 system, and in this case, a so-called alkaline bypass is performed.
即ち、アルカリ濃度の高いキルン排ガスをアルカリバイ
パスによって系外に抜出す手法である。That is, this is a method in which kiln exhaust gas with a high alkali concentration is extracted from the system through an alkali bypass.
第５図は従来のアルカリバイパスを説明するシステム構
成列国であり、これによって従来行なわれている手法を
説明する。FIG. 5 shows the system configuration of various countries for explaining the conventional alkaline bypass, and the conventional method will be explained using this figure.
第５図において、キルン１から抽気ダクト２を介して抽
気した１１００℃のキルン排ガスは、冷却室３内に導入
され、ここでファン４からの冷空気と混合されて、ガス
温度を４００〜４５０℃に低下させる。In FIG. 5, kiln exhaust gas at 1100°C extracted from kiln 1 through bleed duct 2 is introduced into cooling chamber 3, where it is mixed with cold air from fan 4 to raise the gas temperature to 400-450°C. Lower to ℃.
この際、ガス温度の低下によってダストの表面にアルカ
リ化合物を凝縮させ、更に次のスプレー塔５で水を噴霧
して温度を１５０℃程度に迄下げた後、所定のダストを
排出し、更に電気集塵機６にて集塵し、残りのガスはフ
ァン７を介して大気中に排出している。又、回収された
ダストはアルカリで汚染されているため、廃棄処分され
ている。At this time, alkaline compounds are condensed on the surface of the dust by lowering the gas temperature, and water is further sprayed in the next spray tower 5 to lower the temperature to about 150°C, after which a predetermined amount of dust is discharged, and further electricity is The dust is collected by a dust collector 6, and the remaining gas is discharged into the atmosphere via a fan 7. In addition, the collected dust is contaminated with alkali and is therefore disposed of.
（発明が解決しようとづる問題点）
上記した従来手法では、アルカリバイパスによって１１
００℃の抽気したキルン排ガスを系外に排出してしまう
こととなり、この場合の熱損失が大きく、従って燃料消
費量が増加する。因みに、総キルン排ガス中の１０％を
バイパスした場合、ＳＰキルンの場合で、４０〜５０
ｋ ｃａ Ｉ／に９−クリンカ、ＮＳＰキルンの場合で
２０〜３０ｋｃａｌ／Ｎｆｆ−クリンカ程度に迄なる。(Problems to be solved by the invention) In the conventional method described above, 11
The bled kiln exhaust gas at 00° C. will be discharged to the outside of the system, resulting in large heat loss and therefore increased fuel consumption. By the way, if 10% of the total kiln exhaust gas is bypassed, in the case of SP kiln, 40 to 50
kcal/Nff-clinker, and in the case of NSP kiln it amounts to about 20 to 30 kcal/Nff-clinker.
熱損失を回収する方法として、従来よりブレヒータ排ガ
スの熱量をボイラと蒸気タービンにより、電力として回
収することが一般に行なわれており、アルカリバイパス
の排ガスも同様に電力として回収する方法が考えられる
が、その場合、ブレヒータ排ガス系とバイパス排ガス系
に別々にボイラを設けるよりも、一つのボイラで両方の
排ガスの熱量を回収するのが有利である。しかし、バイ
パス排ガスをそのままブレヒータ排ガスに合流させると
、セメント製造工程上、アルカリもブレヒータ排ガス中
のダストと共に、原料として再度ブレヒータに戻される
ことになり、アルカリバイパスした意味がなくなる。従
ってバイパス排ガス中のアルカリを除去した後、ブレヒ
ータ排ガスと合流させる必要がある。Conventionally, as a method of recovering heat loss, the calorific value of the breheater exhaust gas is recovered as electricity using a boiler and a steam turbine.Although it is possible to recover the exhaust gas of the alkaline bypass as electricity in the same way, In that case, it is advantageous to recover the heat of both exhaust gases with one boiler, rather than providing separate boilers for the breheater exhaust gas system and the bypass exhaust gas system. However, if the bypass exhaust gas is directly combined with the breheater exhaust gas, the alkali will be returned to the breheater as a raw material together with the dust in the breheater exhaust gas during the cement manufacturing process, and the alkali bypass will be meaningless. Therefore, after removing the alkali in the bypass exhaust gas, it is necessary to combine it with the breheater exhaust gas.
本発明は上記問題点を解決するためになされたものであ
り、アルカリバイパス処理を行なうに際して、熱損失を
少なくしたセメントキルン排ガスの処理方法を提供する
ことを目的としている。The present invention has been made to solve the above problems, and an object of the present invention is to provide a method for treating cement kiln exhaust gas that reduces heat loss when performing an alkali bypass treatment.
［発明の構成］
（問題点を解決するための手段）
本発明者らは排出されるダストと、このダストがどの程
度のアルカリ覆を持出すのかについて種々研究を重ねた
結果、これらの間にはある特菫な関係があることを知見
した。[Structure of the Invention] (Means for Solving the Problems) The present inventors have conducted various studies on the emitted dust and how much alkali cover this dust brings out, and found that there is a difference between them. It was discovered that there is a special relationship between
第２図がこの関係を示す図表である。即ち、第２図は横
軸にダストの粒径をとり、縦軸に累積粒度分布とアルカ
リｆｆ１（ＲｚＯ）分布とをとったものである。Figure 2 is a chart showing this relationship. That is, in FIG. 2, the horizontal axis represents the particle size of dust, and the vertical axis represents the cumulative particle size distribution and the alkali ff1 (RzO) distribution.
この図から明らかなように、粒径１０μｍ程度以下のダ
ストが、ダストが持出す全アルカリ但の８０％程度を含
んでいると言うことである。しかも粒径１μｍ以下の部
分に全体の約７０％のアルカリが濃縮されている。As is clear from this figure, dust with a particle size of about 10 μm or less contains about 80% of the total alkali taken out by the dust. Moreover, about 70% of the alkali is concentrated in the part with a particle size of 1 μm or less.
従って、アルカリバイパスによって抽気したキルン排ガ
ス中に含まれるダストのうらから、粒径１０μｍを境に
分離し、粒径１０μｍ以下を排出し、それ以上を再びキ
ルンへ戻してやれば、系外へのダストの排出量は半減し
、しかもキルンへ戻されるダストは既に仮焼反応が終了
したものであるため、熱損失も低減することになる。Therefore, if the dust contained in the kiln exhaust gas extracted by the alkaline bypass is separated at a particle size of 10 μm as a boundary, the particles with a particle size of 10 μm or less are discharged, and the larger particles are returned to the kiln. The amount of dust emitted is halved, and since the dust returned to the kiln has already undergone the calcination reaction, heat loss is also reduced.
次に、排ガスをブレヒータ排ガスに合流させる前に、ア
ルカリの濃縮された１０μｍ以下のダストを除去する必
要がある。このような微粒ダス１−の捕集には、従来バ
ッグフィルタが用いられてきたが、バッグフィルタを用
いるためには、ガス温１身を１２０〜１４０℃程麿まで
下げなければならない。Next, it is necessary to remove the alkali-concentrated dust of 10 μm or less before the exhaust gas is merged with the breheater exhaust gas. Conventionally, bag filters have been used to collect such fine dust 1-, but in order to use bag filters, the gas temperature must be lowered to about 120 to 140°C.
一方、ボイラの効率を高めるためには、ガス温度はでき
るだけ高い方が有利である。但し、アルカリ化合物の融
点以上の温度では、管路の閉塞が起るので、６００〜７
００℃が望ましく、この湿度ではバッグフィルタは使用
できない。On the other hand, in order to increase the efficiency of the boiler, it is advantageous for the gas temperature to be as high as possible. However, if the temperature is higher than the melting point of the alkaline compound, clogging of the pipe will occur, so
00° C. is desirable, and bag filters cannot be used at this humidity.
（作用）
従って、本発明ではアルカリバイパスによって抽気した
キルン排ガスを一旦、分級器に導いて粗粒ダストを分離
し、これをキルンへ戻すと共に、微粒ダストを含んだ６
００〜７００℃の排ガスを高温用束ａ機へ導いて微粒ダ
ストを除去して後、サスペンションプレヒータの排ガス
と合流させてボイラに導き、熱回収するようにしている
。(Function) Therefore, in the present invention, the kiln exhaust gas extracted by the alkaline bypass is once led to the classifier to separate the coarse dust, and then returned to the kiln, and the 6 gas containing the fine dust is
After the exhaust gas at 00 to 700°C is led to a high temperature bundle a machine to remove fine dust, it is combined with the exhaust gas from the suspension preheater and led to the boiler for heat recovery.
（実施例） 以下図面を参照して実施例を説明する。(Example) Examples will be described below with reference to the drawings.
第１図は本発明によるセメントキルン排ガスの処理方法
を説明する一実施例の構成図である。FIG. 1 is a block diagram of an embodiment of the method for treating cement kiln exhaust gas according to the present invention.
第１図において、１はキルンであり、燃料の燃焼によっ
て土じた排ガスは仮焼炉８へ導入され、更に図示しない
クリンカ冷却装置からの高温空気により生じた燃料ガス
と混合された後、仮焼されたセメント原料粉末を分離す
るためのサイクロン９を経て順次、その上段のサイクロ
ン１０．１１．１２へと）９かれ、その間にセメント原
料粉末との熱交換が行なわれて排出ガス温度を低下させ
、更に最終υ１出ガスをボイラ１３へ導入して熱回収さ
せる部分は従来同様のものである。In FIG. 1, reference numeral 1 denotes a kiln, and exhaust gas emitted by combustion of fuel is introduced into a calciner 8, where it is further mixed with fuel gas generated by high-temperature air from a clinker cooling device (not shown). After passing through cyclone 9 for separating the burned cement raw material powder, it is sequentially transferred to the upper cyclones 10, 11, and 12)9, during which heat exchange with the cement raw material powder is performed to lower the exhaust gas temperature. The portion where the final υ1 output gas is further introduced into the boiler 13 for heat recovery is the same as the conventional one.
１４は冷却室、１５は分級器、１６は高温用集塵機であ
り、本発明において追加した構成である。14 is a cooling chamber, 15 is a classifier, and 16 is a high-temperature dust collector, which are additional configurations in the present invention.
本実施例では、高温用集塵機として移１ＦＪ１層式の集
塵機を用いているが、他の集塵機でし？：５温に耐える
ものであれば良いのは勿論である。In this example, a 1FJ single-layer dust collector is used as a high-temperature dust collector, but other dust collectors may be used. : Of course, it is good as long as it can withstand 5 temperatures.
又、分級器の型式は何でもよいが、分級粒径を１０μｍ
程度とする場合は、例えばサイクロンが適している。Also, any type of classifier may be used, but the classified particle size should be 10 μm.
For example, a cyclone is suitable.
叩ら、キルン排ガスを抽気して冷却室１４経山で分級器
１５に導入し、この分級器では前記した通りダストの粒
径１０μｍを基準にして分離し、粒径１０μｍ以上の粗
粒ダストは再びキルン１へ戻し、それ以外の微粒ダスト
は、例えば移動層式の集塵機１６へ導いて微粒ダストを
除去してから、サスペンションプレヒータの排ガスと合
流させ、ボイラ１３にて熱回収するものである。After beating, the kiln exhaust gas is extracted and introduced into the classifier 15 in the cooling chamber 14, where the classifier separates the dust based on the particle size of 10 μm as described above, and coarse dust with a particle size of 10 μm or more is separated. The remaining particulate dust is returned to the kiln 1, and the remaining particulate dust is removed by, for example, a moving bed type dust collector 16, and then combined with the exhaust gas of the suspension preheater, where the heat is recovered in the boiler 13.
この場合、従来は抽気した排ガスを冷却室１４にて４０
０〜４５０℃に下げて排ガス４１ｆｆをアルカリ化合物
の融点以下としていたが、本発明においては、この温度
を６００〜７００℃とすることにより、熱回収効率を向
上させている。なお、温度６００〜７００℃はアルカリ
化合物の融点（１６８℃）以下であるため、何らの問題
はない。In this case, conventionally the extracted exhaust gas was stored in the cooling chamber 14 for 40 minutes.
Although the exhaust gas 41ff was lowered to 0 to 450°C to be below the melting point of the alkali compound, in the present invention, the heat recovery efficiency is improved by lowering this temperature to 600 to 700°C. Note that since the temperature of 600 to 700°C is below the melting point of the alkali compound (168°C), there is no problem.
しかし、温度が６００〜７００℃とした結果、通常の集
塵機では耐えられないため、前記した移！ｌＪ層式の集
１１ｉ１Ｇを用いている。However, as a result of the temperature reaching 600 to 700°C, a normal dust collector cannot withstand it, so the above-mentioned transfer is required. IJ layer type collection 11i1G is used.
又、アルカリバイパスをした結果、ブレヒータの排ガス
温度が低下してしまい、この排ガスを導入したボイラ効
率が低下するため、６００℃のバイパス排ガスを、前記
ブレヒータの排ガスに混合してボイラ入口ガス温度を上
昇させている。In addition, as a result of the alkali bypass, the temperature of the exhaust gas from the breheater decreases, and the efficiency of the boiler into which this exhaust gas is introduced decreases. is increasing.
第３図はダストを分級しない場合と、１０μｍ以上のダ
ストをキルンへ戻した場合とのタリン力焼成用の熱消費
量をバイパス比率について示した図表である。FIG. 3 is a chart showing the heat consumption for talin force firing with respect to the bypass ratio when the dust is not classified and when the dust of 10 μm or more is returned to the kiln.
図から明らかなように、１０μ…以上のダストを戻づこ
とにより熱消費ｊを低減させることが出来る。As is clear from the figure, heat consumption j can be reduced by returning dust of 10 μm or more.
史に、本発明のように冷空気混合後のガス温度を６００
〜７００℃にすれば、通過ガスａが減少するため、その
結果、集塵機の処理ガスｍが減少し、これらに要する設
備費及び消費電力が低減される。Historically, as in the present invention, the gas temperature after mixing with cold air was set at 600°C.
If the temperature is set to 700° C., the passing gas a is reduced, and as a result, the processing gas m of the dust collector is reduced, and the equipment costs and power consumption required for these are reduced.
一方、冷却室の温度を６００〜７００℃としたため、従
来の４００〜４５０℃の場合に比して冷空気を減少出来
、温度上昇分だけボイラ入口温度が上昇して回収熱効率
が向上する。On the other hand, since the temperature of the cooling chamber is set to 600 to 700°C, the amount of cold air can be reduced compared to the conventional case of 400 to 450°C, and the boiler inlet temperature rises by the amount of temperature rise, improving the heat recovery efficiency.
第４図は効果確認のためにボイラ入口ガス温度を各場合
に分けて示している。即ち、ブレヒータ排ガスのみをボ
イラへ導入した場合、従来のように冷７４１ 温度を４
５０℃とした場合、本発明のように冷２Ｊｌ温度を６０
０℃とした場合がバイパス比率に応じて示されている。Figure 4 shows the boiler inlet gas temperature for each case to confirm the effect. In other words, if only the breheater exhaust gas is introduced into the boiler, the temperature will be lowered to 4.
When the temperature is 50℃, the cold 2Jl temperature is 60℃ as in the present invention.
The case where the temperature is 0°C is shown according to the bypass ratio.
図から明らかなように、冷却温度を４５０℃の詩に比べ
て本発明の場合、バイパス比率１０％の時で１４℃程度
上界していることが理解出来る。As is clear from the figure, compared to the case where the cooling temperature is 450°C, it can be seen that in the case of the present invention, the cooling temperature is about 14°C higher when the bypass ratio is 10%.
［発明の効果コ
以上説明した如く、本発明によればキルン排ガスを分級
器へ導いてダストの粒径に応じて分級し、この分級によ
って生じた粗粒ダストをキルンへ戻すと共に、微粒ダス
トを含んだ排ガスを高温用集塵機に導いて微粒ダストを
除去してからブレヒータの排ガスと合流させてボイラへ
導入するようにしているので、以下に示す効果がある。[Effects of the Invention] As explained above, according to the present invention, the kiln exhaust gas is guided to the classifier and classified according to the particle size of the dust, and the coarse dust generated by this classification is returned to the kiln, and the fine dust is The contained exhaust gas is led to a high-temperature dust collector to remove particulate dust, and then combined with the exhaust gas from the breheater and introduced into the boiler, resulting in the following effects.
■排ガス吊の減少により、ボイラがコンバク１〜に出来
ると同時に、ボイラ入口温度が上昇し、回収熱効率が大
となる。- Due to the reduction in exhaust gas flow, the boiler can be heated to 1 or more, and at the same time, the boiler inlet temperature rises and the heat recovery efficiency increases.
■集塵機の処理ガス聞が減少し、これらに要する設備費
及び電力母が減少する。■The processing gas volume of the dust collector is reduced, and the equipment costs and electricity required for these are reduced.
■冷却室における冷空気の伍を減少出来る。■Can reduce the amount of cold air in the cooling room.
■アルカリバイパスによって排出していた粗粒ダストの
回収が出来るため、資源の有効利用が図れる。■Coarse dust emitted by the alkali bypass can be recovered, allowing effective use of resources.
第１図は本発明によるセメントキルン排ガスの処理方法
を説明するための一実施例構成図、第２図はダストの粒
度とアルカリωとの関係を示ザ図、第３図はダストを分
級してキルンへ戻した場合と分綴りない揚台との熱消費
晒を示した図、第４図は効果Ｋｔ認のためのボイラ入口
温度を各場合に分けて示した図である。
１・・・キルン ２・・・抽気ダクト３．１４
・・・冷却室 ４．７．１７．１８・・・）１ン５
・・・スプレー塔 ６・−・集塵機８・・・仮焼炉
９．１０．１１．１２・・・サイクロン１３・・・ボイ
ラ １５・・・分級器１６・・・高温用集塵機
特許出願人 秩父セメント株式会社
代理人 弁理士 石 井 紀 男第１図
第２図
一粗径（μ町
第３図
第４図
バイパス比率（′Ａ）
第５図
手続補正書は式）
％式％
１ 事件の表示
昭和６１ 年 特許願 第 ９３１４２ 号３、補正
をする者
住 所 〒１０６ 東京都港区麻布台１丁目１番２
０号代理権を証明する書面２図面の簡単な説明の欄７、
補正の内容
別紙の通り
補 正 の 内 容
（１）代理権を証明する書面（委任状）は、昭和６１年
５月２７日付Ｓ留郵便にて、既に差出済です。
（２）図面の簡単な説明の欄を下記のように訂正する。
記
第１図は本発明によるセメントキルン排ガスの処理方法
を説明するための一実施例溝成図、第２図はダストの粒
度とアルカリ量との関係を示す図、第３図はダストを分
級してキルンへ戻した場合と分級しない場合との熱消費
量を示した図、第４図は効果確認のためのボイラ入口温
度を各場合に分けて示した図、第５図は従来のアルカリ
バイパスを説明するシステム構成測量である。
１・・・キルン ２・・・抽気ダクト３．１４
・・・冷却室 ４．７．１７．１８・・・ファン５
・・・スプレー塩 ６・・・集塵機８・・・仮焼炉
９．１０．１１．１２・・・サイクロン１３・・・ボイ
ラ １５・・・分級器１６・・・高温用集塵機
以上Fig. 1 is a block diagram of an embodiment for explaining the method of treating cement kiln exhaust gas according to the present invention, Fig. 2 is a diagram showing the relationship between dust particle size and alkali ω, and Fig. 3 is a diagram showing the relationship between dust particle size and alkali ω. Fig. 4 is a diagram showing the heat consumption exposure in the case where the boiler is returned to the kiln and the case where the boiler is returned to the kiln, and Fig. 4 is a diagram showing the boiler inlet temperature for evaluating the effect Kt in each case. 1...Kiln 2...Bleed air duct 3.14
...cooling room 4.7.17.18...)1n5
... Spray tower 6 ... Dust collector 8 ... Calciner 9.10.11.12 ... Cyclone 13 ... Boiler 15 ... Classifier 16 ... High temperature dust collector Patent applicant Chichibu Norio Ishii, Agent for Cement Co., Ltd. Patent Attorney Norio Ishii Figure 1 Figure 2 - Rough Diameter (μ Town Figure 3 Figure 4 Bypass Ratio ('A) Figure 5 Procedure Amendment Form) % Formula % 1 of the incident Indication: 1985 Patent Application No. 93142 3, Address of the person making the amendment: 1-1-2 Azabudai, Minato-ku, Tokyo 106
Document certifying No. 0 representative authority 2 Column 7 for brief explanation of drawings,
Contents of the amendments Contents of the amendments (1) The document certifying the power of attorney (power of attorney) has already been sent by S mail dated May 27, 1986. (2) Correct the brief description column of the drawing as follows. Figure 1 is a diagram showing an example of a groove diagram for explaining the method of treating cement kiln exhaust gas according to the present invention, Figure 2 is a diagram showing the relationship between the particle size of dust and the amount of alkali, and Figure 3 is a diagram showing the classification of dust. Figure 4 shows the boiler inlet temperature for each case to confirm the effect, and Figure 5 shows the heat consumption when returning to the kiln after being classified. This is a system configuration survey to explain the bypass. 1...Kiln 2...Bleed air duct 3.14
...Cooling room 4.7.17.18...Fan 5
... Spray salt 6 ... Dust collector 8 ... Calciner 9.10.11.12 ... Cyclone 13 ... Boiler 15 ... Classifier 16 ... High-temperature dust collector or higher
Claims (2)
のアルカリ量を減少させるアルカリバイパスによるセメ
ントキルン排ガスの処理方法において、前記したキルン
排ガスに冷空気を混合して排ガス温度をアルカリ化合物
の融点以下の６００〜７００℃に低下させた後、分級器
に導いて排ガス中の粗粒ダストを分離してキルンへ戻す
と共に、残余の微粒ダストを含む排ガスは高温用集塵機
を介して微粒ダストを除去した後、サスペンションプレ
ヒータからの排ガスと合流させてボイラに導き、熱回収
することを特徴とするセメントキルン排ガスの処理方法
。(1) In a cement kiln exhaust gas treatment method using an alkaline bypass, in which a portion of the cement kiln exhaust gas is extracted to reduce the amount of alkali in the clinker, cold air is mixed with the above-mentioned kiln exhaust gas to lower the exhaust gas temperature to below the melting point of the alkali compound. After lowering the temperature to 600-700℃, the exhaust gas was led to a classifier to separate the coarse dust in the exhaust gas and returned to the kiln, and the remaining exhaust gas containing fine dust was passed through a high-temperature dust collector to remove the fine dust. A method for treating cement kiln exhaust gas, which is characterized in that it is then combined with exhaust gas from a suspension preheater and guided to a boiler for heat recovery.
たことを特徴とする特許請求の範囲第１項記載のセメン
トキルン排ガスの処理方法。(2) The method for treating cement kiln exhaust gas according to claim 1, wherein the classification standard of the classifier is a dust particle size of approximately 10 μm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9314286A JPS62252350A (en) | 1986-04-22 | 1986-04-22 | Treatment for cement kiln exhaust gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9314286A JPS62252350A (en) | 1986-04-22 | 1986-04-22 | Treatment for cement kiln exhaust gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62252350A true JPS62252350A (en) | 1987-11-04 |
| JPH0372027B2 JPH0372027B2 (en) | 1991-11-15 |
Family
ID=14074274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9314286A Granted JPS62252350A (en) | 1986-04-22 | 1986-04-22 | Treatment for cement kiln exhaust gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62252350A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012444A1 (en) * | 1998-08-28 | 2000-03-09 | Taiheiyo Cement Corporation | Device and method of bypassing kiln exhaust gas |
| JP2002284550A (en) * | 2001-03-27 | 2002-10-03 | Taiheiyo Cement Corp | Treatment method of gas emissions from cement production |
| JP2007261886A (en) * | 2006-03-29 | 2007-10-11 | Sumitomo Osaka Cement Co Ltd | Method and apparatus for treating exhaust gas from cement firing facility |
| JP2011079738A (en) * | 2011-01-14 | 2011-04-21 | Sumitomo Osaka Cement Co Ltd | Method and apparatus for treating exhaust gas from cement firing facility |
| CN102114387A (en) * | 2010-12-22 | 2011-07-06 | 浙江工商大学 | Process for preventing cement clinker produced from high-sulfur raw material from skinning |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2818918B1 (en) * | 2000-12-29 | 2003-09-19 | Fcb | PROCESS AND DEVICE FOR REMOVING NEFAST VOLATIVE ELEMENTS, ESPECIALLY CHLORIDES AND / OR SULFATES, CONTAINED IN A FLOW OF SMOKE. |
-
1986
- 1986-04-22 JP JP9314286A patent/JPS62252350A/en active Granted
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012444A1 (en) * | 1998-08-28 | 2000-03-09 | Taiheiyo Cement Corporation | Device and method of bypassing kiln exhaust gas |
| JP4294871B2 (en) * | 1998-08-28 | 2009-07-15 | 太平洋セメント株式会社 | Kiln exhaust gas bypass device and bypass method |
| JP2002284550A (en) * | 2001-03-27 | 2002-10-03 | Taiheiyo Cement Corp | Treatment method of gas emissions from cement production |
| JP2007261886A (en) * | 2006-03-29 | 2007-10-11 | Sumitomo Osaka Cement Co Ltd | Method and apparatus for treating exhaust gas from cement firing facility |
| CN102114387A (en) * | 2010-12-22 | 2011-07-06 | 浙江工商大学 | Process for preventing cement clinker produced from high-sulfur raw material from skinning |
| JP2011079738A (en) * | 2011-01-14 | 2011-04-21 | Sumitomo Osaka Cement Co Ltd | Method and apparatus for treating exhaust gas from cement firing facility |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0372027B2 (en) | 1991-11-15 |
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