JP5885276B2 - Cement kiln extraction gas processing system and processing method - Google Patents

Cement kiln extraction gas processing system and processing method Download PDF

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JP5885276B2
JP5885276B2 JP2014110760A JP2014110760A JP5885276B2 JP 5885276 B2 JP5885276 B2 JP 5885276B2 JP 2014110760 A JP2014110760 A JP 2014110760A JP 2014110760 A JP2014110760 A JP 2014110760A JP 5885276 B2 JP5885276 B2 JP 5885276B2
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淳一 寺崎
淳一 寺崎
慶展 辰巳
慶展 辰巳
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Description

本発明は、セメントキルン抽気ガスの処理システム及び処理方法に関し、特に、セメン
トキルンの窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より抽
気した抽気ガスに含まれるダストを湿式集塵するシステム等に関する。 The present invention relates to a cement kiln extraction gas processing system and a processing method, and in particular, wet collection of dust contained in extraction gas extracted from a kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the lowermost cyclone of the preheater. It is related with the system etc. which do.

従来、セメント製造設備におけるプレヒータの閉塞等の問題を引き起こす原因となる塩素、硫黄、アルカリ等の中で、塩素が特に問題となることに着目し、セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より、燃焼ガスの一部を冷却しながら抽気して塩素を除去する塩素バイパス設備が用いられている。   Focusing on chlorine, sulfur, alkali, etc., which causes problems such as blockage of preheaters in cement manufacturing facilities, from the bottom of the kiln of the cement kiln to the bottom cyclone From the kiln exhaust gas flow path, a chlorine bypass facility for extracting chlorine while extracting a part of the combustion gas while cooling is used.

この塩素バイパス設備は、図３に示すように、セメントキルン７２の窯尻から燃焼ガスの一部を冷却しながら抽気するプローブ７３と、プローブ７３に冷風Ａを供給する冷却ファン７４と、プローブ７３で抽気した燃焼ガスＧ１に含まれるダストの粗粉Ｃを分離するサイクロン７５と、サイクロン７５の排ガスＧ２に含まれる微粉Ｆを湿式集塵する湿式集塵機７６と、湿式集塵機７６から排出されるスラリーＳ２を固液分離して石膏Ｇと塩水ＳＷとを得るための固液分離機７７と、湿式集塵機７６からの排ガスＧ３を誘引する誘引ファン７８等で構成される。   As shown in FIG. 3, this chlorine bypass facility includes a probe 73 that bleeds while cooling a part of the combustion gas from the kiln bottom of the cement kiln 72, a cooling fan 74 that supplies cold air A to the probe 73, and a probe 73. The cyclone 75 that separates the dust coarse powder C contained in the combustion gas G1 extracted in step 1, the wet dust collector 76 that wet-collects the fine powder F contained in the exhaust gas G2 of the cyclone 75, and the slurry S2 discharged from the wet dust collector 76 The solid-liquid separator 77 for obtaining the gypsum G and the salt water SW by solid-liquid separation, the induction fan 78 for attracting the exhaust gas G3 from the wet dust collector 76, and the like.

また、湿式集塵機７６は、微粉Ｆを含む排ガスＧ２をスラリーＳ１中の水分と接触させて冷却するスクラバ７６ａと、スクラバ７６ａからのスラリーを受け、スクラバ７６ａに供給するための循環液槽７６ｂと、工水を噴霧する洗浄塔７６ｃとを備える。   Further, the wet dust collector 76 is a scrubber 76a that cools the exhaust gas G2 containing fine powder F by contacting with moisture in the slurry S1, a circulating liquid tank 76b that receives the slurry from the scrubber 76a and supplies the slurry to the scrubber 76a, And a cleaning tower 76c for spraying industrial water.

上記構成において、セメントキルン７２の燃焼ガスの一部をプローブ７３で冷却しながら抽気すると、塩素化合物の結晶が生成される。その際、抽気した燃焼ガスＧ１に含まれるダストの微粉Ｆ側に塩素が偏在しているため、サイクロン７５で分級した粗粉Ｃをセメントキルン系に戻すとともに、塩素含有率の高い微粉Ｆ及び排ガスＧ２を湿式集塵機７６に導き、循環液槽７６ｂから供給されるスラリーＳ１の水分等によって冷却する。また、循環液槽７６ｂに消石灰（Ｃａ（ＯＨ）2）を添加し、排ガスＧ２に含まれるＳＯ2と反応させて石膏を生成させる。そして、排ガスＧ２中の微粉Ｆを湿式集塵機７６によって集塵し、集塵ダストスラリーＳ２を固液分離機７７によって石膏Ｇと、ＫＣｌを含む塩水ＳＷとに分離し、石膏Ｇを回収するとともに、分離された塩水ＳＷをセメント粉砕工程に添加したり、水処理後に下水又は海洋に放流して処理する（例えば、特許文献１参照）。 In the above configuration, when a part of the combustion gas in the cement kiln 72 is extracted while being cooled by the probe 73, crystals of a chlorine compound are generated. At that time, since the chlorine is unevenly distributed on the fine powder F side of the dust contained in the extracted combustion gas G1, the coarse powder C classified by the cyclone 75 is returned to the cement kiln system, and the fine powder F and exhaust gas having a high chlorine content. G2 is guided to the wet dust collector 76, and is cooled by moisture of the slurry S1 supplied from the circulating liquid tank 76b. Further, slaked lime (Ca (OH) 2 ) is added to the circulating liquid tank 76b and reacted with SO 2 contained in the exhaust gas G2 to generate gypsum. Then, the fine powder F in the exhaust gas G2 is collected by the wet dust collector 76, the dust collection dust slurry S2 is separated into the gypsum G and the salt water SW containing KCl by the solid-liquid separator 77, and the gypsum G is recovered. The separated salt water SW is added to the cement pulverization process, or discharged into sewage or the ocean after the water treatment (for example, see Patent Document 1).

特開２００９−３５４５０号公報JP 2009-35450 A

しかし、上記塩素バイパス設備７１においては、湿式集塵機７６に持ち込まれるダスト（微粉Ｆ）の量や、湿式集塵機７６に供給される排ガスＧ２中のＳＯ2濃度が一定ではない。そのため、持ち込みダスト量の増減や、ＳＯ2濃度に応じて添加する消石灰の添加量の変化により、循環液槽７６ｂ中のスラリー濃度を一定に維持するのは困難である。 However, in the chlorine bypass facility 71, the amount of dust (fine powder F) brought into the wet dust collector 76 and the SO 2 concentration in the exhaust gas G2 supplied to the wet dust collector 76 are not constant. Therefore, it is difficult to keep the slurry concentration in the circulating liquid tank 76b constant by increasing or decreasing the amount of dust brought in or by changing the amount of slaked lime added according to the SO 2 concentration.

ここで、循環液槽７６ｂ内のスラリー濃度が高過ぎると、循環液槽７６ｂ内に堆積物が増加したり、排出ポンプ７９が閉塞したり、循環ポンプ８０が過負荷で停止したり、スクラバ７６ａが閉塞するなどの懸念がある。   Here, if the slurry concentration in the circulating liquid tank 76b is too high, deposits increase in the circulating liquid tank 76b, the discharge pump 79 is blocked, the circulating pump 80 stops due to overload, or the scrubber 76a. There are concerns such as obstruction.

一方、循環液槽７６ｂ内のスラリー濃度が低過ぎると、固液分離機７７から排出されるケーキ層の形成が不十分となり、固液分離機７７の効率低下を招き、運転コストが増加するという問題があった。また、固液分離機７７で分離された塩水中の浮遊物質（ＳＳ）が増加するという問題もあった。   On the other hand, if the slurry concentration in the circulating liquid tank 76b is too low, the formation of the cake layer discharged from the solid-liquid separator 77 becomes insufficient, causing the efficiency of the solid-liquid separator 77 to decrease, and the operating cost increases. There was a problem. There is also a problem that suspended matter (SS) in salt water separated by the solid-liquid separator 77 increases.

さらに、上記塩素バイパス設備７１において、循環液槽７６ｂ内から排出されるスラリーには、ＳＯ2と反応していない消石灰が含まれているため、固液分離機７７から排出さ
れる石膏の純度が低下するという問題もあった。 Furthermore, in the chlorine bypass facility 71, the slurry discharged from the circulating liquid tank 76b contains slaked lime that has not reacted with SO 2 , so the purity of the gypsum discharged from the solid-liquid separator 77 is high. There was also the problem of a drop.

そこで、本発明は、上記従来技術の問題点に鑑みてなされたものであって、安定運転を維持しながら、運転コストの増加を招くことなく、純度の高い石膏を得ることなどが可能なセメントキルン抽気ガスの処理システム等を提供することを目的とする。   Accordingly, the present invention has been made in view of the above-mentioned problems of the prior art, and is a cement capable of obtaining high-purity gypsum without causing an increase in operating cost while maintaining stable operation. An object of the present invention is to provide a kiln extraction gas processing system and the like.

上記目的を達成するため、本発明は、セメントキルン抽気ガスの処理システムであって、セメントキルンの窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を抽気したガスに含まれるダストを湿式集塵する湿式集塵機と、該湿式集塵機によって得られたスラリーの密度を測定する密度測定装置と、該密度測定装置による測定値が所定の値より小さい場合に、前記湿式集塵機からの前記スラリーの排出を停止すること、前記スラリーの排出量を減少させること、前記湿式集塵機への水の供給を停止すること、前記湿式集塵機への水の供給量を減少させることのうち少なくとも１つを行い、前記測定値が所定の値より大きい場合に、前記湿式集塵機への水の供給量を増加させることにより、前記測定値が所定の範囲内となるように前記湿式集塵機内のスラリーの密度を調整する密度調整手段とを備えることを特徴とする。 In order to achieve the above object, the present invention is a cement kiln extraction gas processing system, in which a part of combustion gas is extracted from a kiln exhaust gas passage from a kiln bottom of a cement kiln to a lowermost cyclone of a preheater. the dust contained in the gas and wet dust collector for wet type dust collector, and the density measuring device for measuring the density of the slurry obtained by the wet dust collector, if the measured value that by the said seal measuring device is smaller than a predetermined value, Stopping the discharge of the slurry from the wet dust collector, reducing the discharge amount of the slurry, stopping the supply of water to the wet dust collector, reducing the supply amount of water to the wet dust collector at least one carried out in the case the measured value is larger than a predetermined value, by increasing the amount of water supplied to the wet dust collector, the measurements Characterized in that it comprises a density adjusting means for adjusting the density of the slurry in the wet dust collector to be within the range of the constant.

そして、本発明によれば、密度調整手段によって、湿式集塵機によって得られたスラリーの密度が所定の範囲内となるように湿式集塵機内のスラリーの密度を調整するため、スラリーの性状を安定させることができ、湿式集塵機の安定運転を維持することができる。   According to the present invention, the density of the slurry in the wet dust collector is adjusted by the density adjusting means so that the density of the slurry obtained by the wet dust collector is within a predetermined range. And stable operation of the wet dust collector can be maintained.

また、本発明は、セメントキルンの窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を抽気し、抽気ガスに含まれるダストを湿式集塵機で湿式集塵するセメントキルン抽気ガスの処理方法であって、前記湿式集塵によって得られたスラリーの密度を測定し、該測定値が所定の値より小さい場合に、前記湿式集塵機からの前記スラリーの排出を停止すること、前記スラリーの排出量を減少させること、前記湿式集塵機への水の供給を停止すること、前記湿式集塵機への水の供給量を減少させることのうち少なくとも１つを行い、前記測定値が所定の値より大きい場合に、前記湿式集塵機への水の供給量を増加させることにより、前記測定値が所定の範囲内となるように前記湿式集塵機内のスラリーの密度を調整することを特徴とする。本発明によれば、上記発明と同様に、スラリーの性状を安定させることができ、安定して湿式集塵を行うことができる。 Further, the present invention is a cement for extracting a part of combustion gas from a kiln exhaust gas passage from a kiln bottom of a cement kiln to a lowermost cyclone of a preheater, and collecting dust contained in the extracted gas with a wet dust collector. a method of processing kiln extracted gas, the density of the slurry obtained by the wet type dust collector was measured, when the measured value is smaller than a predetermined value, stopping the discharge of the slurry from the wet dust collector , At least one of reducing the discharge amount of the slurry, stopping the supply of water to the wet dust collector, and reducing the supply amount of water to the wet dust collector, and the measured value is predetermined. is larger than the value, the by increasing the amount of water supplied to the wet dust collector, dense slurry in the wet dust collector so that the measured value is within a predetermined range And adjusting the. According to the present invention, similar to the above-described invention, the properties of the slurry can be stabilized, and wet dust collection can be performed stably.

以上のように、本発明によれば、安定運転を維持し、運転コストの増加を招かず、純度の高い石膏を得ることなどが可能なセメントキルン抽気ガスの処理システム等を提供することができる。   As described above, according to the present invention, it is possible to provide a cement kiln bleed gas treatment system and the like that can maintain stable operation, increase operating costs, and obtain high-purity gypsum. .

本発明にかかるセメントキルン抽気ガスの処理システムの一実施の形態を示す全体構成図である。1 is an overall configuration diagram showing an embodiment of a cement kiln extraction gas processing system according to the present invention. セメントキルンの抽気ガス処理装置の湿式集塵機の循環液槽内のスラリーの密度とスラリーの固形分含有率の関係を示すグラフである。It is a graph which shows the relationship between the density of the slurry in the circulating liquid tank of the wet dust collector of the extraction gas processing apparatus of a cement kiln, and the solid content rate of a slurry. 従来のセメントキルン抽気ガスの処理システムの一例を示す全体構成図である。It is a whole block diagram which shows an example of the processing system of the conventional cement kiln extraction gas.

次に、本発明を実施するための形態について、図面を参照しながら詳細に説明する。   Next, an embodiment for carrying out the present invention will be described in detail with reference to the drawings.

図１は、本発明にかかるセメントキルン抽気ガスの処理システムの一実施の形態を示し、この処理システム１は、セメントキルン２の窯尻から燃焼ガスの一部を冷却しながら抽気するプローブ３と、プローブ３に冷風Ａを供給する冷却ファン４と、プローブ３で抽気した燃焼ガスＧ１に含まれるダストの粗粉Ｃを分離するサイクロン５と、サイクロン５から排出された排ガスＧ２に含まれる微粉Ｆを湿式集塵する湿式集塵機６と、湿式集塵機６から排出されるスラリーＳ２を湿式分級する湿式分級機１１と、湿式分級機１１から排出された微粒スラリーＳ４を貯留するタンク１２と、湿式分級機１１から排出された粗粒スラリーＳ５を湿式集塵機６に戻すルート１４と、タンク１２から供給されたスラリーＳ６を固液分離して石膏Ｇと塩水ＳＷとを得る固液分離機１３と、湿式集塵機６からの排ガスＧ３を誘引する誘引ファン９等で構成される。   FIG. 1 shows an embodiment of a cement kiln extraction gas processing system according to the present invention. This processing system 1 includes a probe 3 for extracting a part of combustion gas from the bottom of a kiln 2 while cooling it. , A cooling fan 4 that supplies cold air A to the probe 3, a cyclone 5 that separates coarse dust C contained in the combustion gas G1 extracted by the probe 3, and a fine powder F contained in the exhaust gas G2 discharged from the cyclone 5. Wet-type dust collector 6 for wet-dust collection, wet-classifier 11 for wet-classifying slurry S2 discharged from wet-type dust collector 6, tank 12 for storing fine-particle slurry S4 discharged from wet-classifier 11, and wet-classifier 11 and the route 14 for returning the coarse-grain slurry S5 discharged to the wet dust collector 6 and the slurry S6 supplied from the tank 12 to solid-liquid separation, and gypsum G and salt water S A solid-liquid separator 13 to obtain the bets composed of induced draft fan 9 or the like to attract an exhaust gas G3 from the wet dust collector 6.

また、湿式集塵機６は、微粉Ｆを含む排ガスＧ２をスラリーＳ１中の水分と接触させて冷却するスクラバ６ａと、スクラバ６ａからのスラリーを受け、スクラバ６ａに供給するための循環液槽６ｂと、給水装置（不図示）からの工水Ｗを噴霧する洗浄塔６ｃとを備える。   In addition, the wet dust collector 6 includes a scrubber 6a that cools the exhaust gas G2 containing fine powder F in contact with moisture in the slurry S1, a circulating liquid tank 6b that receives the slurry from the scrubber 6a and supplies the slurry to the scrubber 6a, And a cleaning tower 6c for spraying the construction water W from a water supply device (not shown).

さらに、湿式集塵機６は、循環液槽６ｂとスクラバ６ａとの間でスラリーＳ１を循環させる循環ポンプ１５と、循環液槽６ｂ内のスラリーの密度をγ線を利用して測定する密度測定装置１０と、循環液槽６ｂ内のスラリーを密度測定装置１０に供給する供給ポンプ（第１の供給装置）１７と、循環液槽６ｂからスラリーＳ２を湿式分級機１１に供給する排出ポンプ（第２の供給装置）１６とを備える。   Further, the wet dust collector 6 includes a circulation pump 15 that circulates the slurry S1 between the circulating liquid tank 6b and the scrubber 6a, and a density measuring device 10 that measures the density of the slurry in the circulating liquid tank 6b using γ rays. A supply pump (first supply device) 17 for supplying the slurry in the circulating liquid tank 6b to the density measuring device 10, and a discharge pump (second pump) for supplying the slurry S2 from the circulating liquid tank 6b to the wet classifier 11 Supply device) 16.

湿式分級機１１は、湿式集塵機６から排出されたスラリーＳ２を湿式分級するために備えられ、この湿式分級機１１には、湿式サイクロン等の湿式遠心分級機等であって分級点が１０μｍ〜４０μｍ程度のものを使用することができる。   The wet classifier 11 is provided to wet-classify the slurry S2 discharged from the wet dust collector 6, and the wet classifier 11 is a wet centrifugal classifier such as a wet cyclone, and has a classification point of 10 μm to 40 μm. Something of a degree can be used.

次に、上記構成を有する抽気ガス処理システム１の動作について図１及び図２を参照しながら説明する。   Next, the operation of the extraction gas processing system 1 having the above configuration will be described with reference to FIGS.

セメントキルン２の燃焼ガスの一部をプローブ３で冷却しながら抽気し、抽気した燃焼ガスＧ１をサイクロン５で分級し、粗粉Ｃをセメントキルン系に戻すとともに、塩素含有率の高い微粉Ｆ及び排ガスＧ２を湿式集塵機６に導き、スクラバ６ａにおいて循環液槽６ｂから供給されるスラリーＳ１の水分等によって冷却し、微粉Ｆを湿式集塵する。また、循環液槽６ｂに消石灰を添加し、排ガスＧ２に含まれるＳＯ2と反応させて石膏を生成させる。 A part of the combustion gas of the cement kiln 2 is extracted while being cooled by the probe 3, the extracted combustion gas G1 is classified by the cyclone 5, the coarse powder C is returned to the cement kiln system, and the fine powder F having a high chlorine content and The exhaust gas G2 is guided to the wet dust collector 6 and cooled by the moisture of the slurry S1 supplied from the circulating liquid tank 6b in the scrubber 6a, and the fine powder F is wet collected. Further, slaked lime is added to the circulating liquid tank 6b and reacted with SO 2 contained in the exhaust gas G2 to generate gypsum.

循環液槽６ｂ内のスラリーの一部（スラリーＳ３）を供給ポンプ１７によって密度測定装置１０に供給し、スラリーＳ３の密度を測定する。測定されたスラリーＳ３の密度とスラリーＳ３中の固形分との関係は、図２に示す通りである。   A part of the slurry (slurry S3) in the circulating liquid tank 6b is supplied to the density measuring device 10 by the supply pump 17, and the density of the slurry S3 is measured. The relationship between the measured density of the slurry S3 and the solid content in the slurry S3 is as shown in FIG.

ここで、本発明者らが行った実験によると、スラリーが含有する固形分が５％以上２０％以下の範囲内にあるときには、循環液槽６ｂ内に堆積物が増加したり、排出ポンプ１６が閉塞したり、循環ポンプ１５が過負荷で停止したり、スクラバ６ａが閉塞するなどの不具合が発生せず、安定した運転を維持することができるとともに、循環液槽６ｂから排出されるスラリーＳ２の濃度が低過ぎて後段の固液分離機１３の運転効率が低下することもないことが確かめられている。   Here, according to experiments conducted by the present inventors, when the solid content contained in the slurry is in the range of 5% or more and 20% or less, deposits increase in the circulating liquid tank 6b, or the discharge pump 16 The slurry S2 discharged from the circulating liquid tank 6b can be maintained without causing problems such as blocking, circulation pump 15 stopping due to overload, and scrubber 6a blocking. It has been confirmed that the operation efficiency of the solid-liquid separator 13 in the subsequent stage is not lowered because the concentration of the liquid is too low.

そこで、密度測定装置１０によって測定されるスラリーＳ３の密度が１．０１以上１．１０以下となるように調整する。具体的には、スラリーＳ３の密度が１．０１未満の場合には、排出ポンプ１６の運転を停止するか、回転数を低下させて湿式分級機１１への供給量を低く抑えたり、給水装置（不図示）から洗浄塔６ｃへの工水Ｗの添加を停止したり、工水Ｗの添加量を下げるなどの操作を行う。一方、スラリーＳ３の密度が１．１０を超える場合には、逆に、洗浄塔６ｃへの工水Ｗの添加量を増加させる。   Therefore, the density of the slurry S3 measured by the density measuring device 10 is adjusted to be 1.01 or more and 1.10 or less. Specifically, when the density of the slurry S3 is less than 1.01, the operation of the discharge pump 16 is stopped or the number of revolutions is decreased to keep the supply amount to the wet classifier 11 low, or the water supply device Operations such as stopping the addition of the working water W from the (not shown) to the washing tower 6c and reducing the amount of the working water W added are performed. On the other hand, when the density of the slurry S3 exceeds 1.10, the amount of the working water W added to the cleaning tower 6c is increased.

次に、上記密度範囲にあるスラリーＳ２を、循環液槽６ｂから排出ポンプ１６を介して湿式分級機１１に供給する。ここで、湿式分級機１１に供給されたスラリーＳ２には、排ガスＧ２に含まれるＳＯ2との反応がなされずに循環液槽６ｂに沈降していた消石灰が含まれているが、表１に示すように、石膏と消石灰とが混在するスラリーの粒径は、消石灰スラリーのみの粒径に比較して小さく、特に、通過粒子径を１０〜４０μｍとした場合の粗粒分で比較すると、消石灰スラリーの割合がかなり大きくなることが判る。そこで、湿式分級機１１の分級点を１０μｍ以上４０μｍ以下とすることで、粗粒スラリー側に消石灰を多く含むスラリーを分離することができ、この粗粒スラリーＳ５をルート１４を介して循環液槽６ｂに戻し、再度ＳＯ2と反応させて石膏を生成させることにより、固液分離機１３で回収する石膏の純度を上昇させることができる。また、湿式集塵機６に添加する消石灰の量を低減することができる。 Next, the slurry S2 in the above density range is supplied from the circulating liquid tank 6b to the wet classifier 11 through the discharge pump 16. Here, the slurry S2 supplied to the wet classifier 11 contains slaked lime that has settled in the circulating liquid tank 6b without reacting with SO 2 contained in the exhaust gas G2, but is shown in Table 1. As shown, the particle size of the slurry in which gypsum and slaked lime are mixed is small compared to the particle size of only the slaked lime slurry, especially when compared with coarse particles when the passing particle size is 10 to 40 μm. It can be seen that the proportion of slurry is quite large. Therefore, by setting the classification point of the wet classifier 11 to 10 μm or more and 40 μm or less, the slurry containing a large amount of slaked lime can be separated on the coarse slurry side, and this coarse slurry S5 is circulated through the route 14 to the circulating liquid tank. By returning to 6b and reacting again with SO 2 to produce gypsum, the purity of gypsum recovered by the solid-liquid separator 13 can be increased. Moreover, the quantity of the slaked lime added to the wet dust collector 6 can be reduced.

Figure 0005885276
Figure 0005885276

一方、湿式分級機１１によって分離された石膏を多く含む微粒スラリーＳ４を、一時的にタンク１２に貯留した後、固液分離機１３に供給し、石膏Ｇと、ＫＣｌを含む塩水ＳＷとに分離し、石膏Ｇを回収するとともに、分離された塩水ＳＷをセメント粉砕工程に添加したり、水処理後に下水又は海洋に放流して処理する。   On the other hand, the fine slurry S4 containing a large amount of gypsum separated by the wet classifier 11 is temporarily stored in the tank 12, and then supplied to the solid-liquid separator 13, and separated into gypsum G and salt water SW containing KCl. Then, the gypsum G is recovered, and the separated salt water SW is added to the cement pulverization step, or is discharged to sewage or the ocean after the water treatment.

尚、上記実施の形態においては、湿式分級機１１及びルート１４を設け、粗粒スラリーＳ５をルート１４を介して循環液槽６ｂに戻し、再度ＳＯ2と反応させて石膏を生成させ、固液分離機１３で回収する石膏の純度を上昇させたが、所望の純度の石膏が得られる場合には、湿式分級機１１及びルート１４を設けずに、スラリーＳ２を、循環液槽６ｂから排出ポンプ１６を介してそのままタンク１２に貯留した後、固液分離機１３で固液分離して石膏Ｇと塩水ＳＷとを得ることもできる。 In the above embodiment, the wet classifier 11 and the route 14 are provided, and the coarse slurry S5 is returned to the circulating liquid tank 6b via the route 14 to react with SO 2 again to produce gypsum. Although the purity of the gypsum recovered by the separator 13 is increased, when gypsum having a desired purity is obtained, the slurry S2 is discharged from the circulating liquid tank 6b without using the wet classifier 11 and the route 14. After being stored in the tank 12 as it is via 16, the solid-liquid separator 13 performs solid-liquid separation to obtain gypsum G and salt water SW.

また、上記実施の形態においては、セメントキルン２の窯尻から燃焼ガスの一部を抽気したが、セメントキルン２の窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より抽気した抽気ガスを上述のようにして処理することもできる。   Further, in the above embodiment, a part of the combustion gas is extracted from the kiln bottom of the cement kiln 2, but is extracted from the kiln exhaust gas passage from the kiln bottom of the cement kiln 2 to the lowermost cyclone of the preheater. The gas can also be processed as described above.

さらに、上記実施の形態では、プローブ３と湿式集塵機６の間にサイクロン５を配置しているが、サイクロン５を設けずに、プローブ３から抽気ガスを直接湿式集塵機６に導入してもよい。   Furthermore, in the said embodiment, although the cyclone 5 is arrange | positioned between the probe 3 and the wet dust collector 6, you may introduce extraction gas into the wet dust collector 6 directly from the probe 3 without providing the cyclone 5. FIG.

１ セメントキルン抽気ガスの処理システム
２ セメントキルン
３ プローブ
４ 冷却ファン
５ サイクロン
６ 湿式集塵機
６ａ スクラバ
６ｂ 循環液槽
６ｃ 洗浄塔
９ 誘引ファン
１０ スラリー密度測定装置
１１ 湿式分級機
１２ タンク
１３ 固液分離機
１４ （粗粒スラリーを湿式集塵機に戻す）ルート
１５ 循環ポンプ
１６ 排出ポンプ
１７ 供給ポンプ
Ａ 冷風
Ｃ 粗粉
Ｆ 微粉
Ｇ 石膏
Ｇ１ 燃焼ガス
Ｇ２、Ｇ３ 排ガス
Ｓ１〜Ｓ３、Ｓ６ スラリー
Ｓ４ 微粒スラリー
Ｓ５ 粗粒スラリー
ＳＷ 塩水
Ｗ 工水 DESCRIPTION OF SYMBOLS 1 Cement kiln extraction gas processing system 2 Cement kiln 3 Probe 4 Cooling fan 5 Cyclone 6 Wet dust collector 6a Scrubber 6b Circulating liquid tank 6c Washing tower 9 Induction fan 10 Slurry density measuring device 11 Wet classifier 12 Tank 13 Solid-liquid separator 14 (Return coarse slurry to wet dust collector) Route 15 Circulation pump 16 Discharge pump 17 Supply pump A Cold air C Coarse powder F Fine powder G Gypsum G1 Combustion gas G2, G3 Exhaust gas S1-S3, S6 Slurry S4 Fine particle slurry S5 Coarse slurry SW Salt water W Industrial water

Claims (2)

セメントキルンの窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を抽気したガスに含まれるダストを湿式集塵する湿式集塵機と、
該湿式集塵機によって得られたスラリーの密度を測定する密度測定装置と、
該密度測定装置による測定値が所定の値より小さい場合に、前記湿式集塵機からの前記スラリーの排出を停止すること、前記スラリーの排出量を減少させること、前記湿式集塵機への水の供給を停止すること、前記湿式集塵機への水の供給量を減少させることのうち少なくとも１つを行い、前記測定値が所定の値より大きい場合に、前記湿式集塵機への水の供給量を増加させることにより、前記測定値が所定の範囲内となるように前記湿式集塵機内のスラリーの密度を調整する密度調整手段とを備えることを特徴とするセメントキルン抽気ガスの処理システム。 A wet dust collector that wet-collects dust contained in the gas extracted from the kiln exhaust gas passage from the kiln bottom of the cement kiln to the lowermost cyclone of the preheater,
A density measuring device for measuring the density of the slurry obtained by the wet dust collector;
If the measured value that by the said seal measuring device is smaller than a predetermined value, stopping the discharge of the slurry from the wet dust collector, reducing the emissions of the slurry, the supply of water to the wet dust collector And at least one of reducing the amount of water supplied to the wet dust collector and increasing the amount of water supplied to the wet dust collector when the measured value is greater than a predetermined value. And a density adjusting means for adjusting the density of the slurry in the wet dust collector so that the measured value falls within a predetermined range. セメントキルンの窯尻からプレヒータの最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を抽気し、抽気ガスに含まれるダストを湿式集塵機で湿式集塵するセメントキルン抽気ガスの処理方法であって、
前記湿式集塵機によって得られたスラリーの密度を測定し、
該測定値が所定の値より小さい場合に、前記湿式集塵機からの前記スラリーの排出を停止すること、前記スラリーの排出量を減少させること、前記湿式集塵機への水の供給を停止すること、前記湿式集塵機への水の供給量を減少させることのうち少なくとも１つを行い、前記測定値が所定の値より大きい場合に、前記湿式集塵機への水の供給量を増加させることにより、前記測定値が所定の範囲内となるように前記湿式集塵機内のスラリーの密度を調整することを特徴とするセメントキルン抽気ガスの処理方法。 Cement kiln extraction gas processing method that extracts part of the combustion gas from the kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the lowermost cyclone of the preheater and wet-collects the dust contained in the extraction gas with a wet dust collector Because
Measure the density of the slurry obtained by the wet dust collector,
If the measurement value is smaller than a predetermined value, stopping the discharge of the slurry from the wet dust collector, reducing the emissions of the slurry, to stop the supply of water to the wet dust collector, wherein Performing at least one of reducing the amount of water supplied to the wet dust collector, and increasing the amount of water supplied to the wet dust collector when the measured value is greater than a predetermined value. A method for treating a cement kiln bleed gas, wherein the density of the slurry in the wet dust collector is adjusted so that is within a predetermined range.
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