JP2016056070A - Method for treating chlorine bypass exhaust gas - Google Patents

Method for treating chlorine bypass exhaust gas Download PDF

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JP2016056070A
JP2016056070A JP2014184917A JP2014184917A JP2016056070A JP 2016056070 A JP2016056070 A JP 2016056070A JP 2014184917 A JP2014184917 A JP 2014184917A JP 2014184917 A JP2014184917 A JP 2014184917A JP 2016056070 A JP2016056070 A JP 2016056070A
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exhaust gas
gas
dust
chlorine bypass
kiln
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淳一 寺崎
Junichi Terasaki
淳一 寺崎
裕太 田原
Yuta Tawara
裕太 田原
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Taiheiyo Cement Corp
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Abstract

PROBLEM TO BE SOLVED: To provide a method for treating chlorine bypass exhaust gas, in which the chlorine bypass exhaust gas is treated stably while keeping down an equipment cost.SOLUTION: A part G6 of a combustion gas is extracted from a kiln exhaust gas flow passage, which is extended from a kiln tail of a cement kiln 2 to a lowermost-stage cyclone, while cooling the combustion gas. Chlorine bypass dust D5 is recovered in a dry state from an extraction gas G7 and then a desulfurizing agent DA of a powder state is added to an outlet gas G11 of a dust collector 12. The chlorine bypass dust-recovered outlet gas of the dust collector is merged with an exhaust gas G2 of a preheater arranged incidentally to the cement kiln. It does not matter if the desulfurizing agent of the powder state is added to an exhaust gas G3 (G4) being the merged gas. As the desulfurizing agent, a coarse powder D1, which is obtained by sorting hydrated lime and the extraction gas, or dust D6, which is recovered by another dust collector 5 for collecting dust from the exhaust gas of the cement kiln, can be used. The SOconcentration of a downstream-side exhaust gas G5 of the dust collector 5 is measured and the amount of the desulfurizing agent to be thrown can be controlled according to the measured SOconcentration.SELECTED DRAWING: Figure 1

Description

本発明は、塩素バイパス排ガスの処理方法に関し、特に、塩素バイパスダストを回収した後のガスに含まれるＳＯ2の濃度を低減する方法に関する。 The present invention relates to a method for treating chlorine bypass exhaust gas, and more particularly to a method for reducing the concentration of SO 2 contained in a gas after chlorine bypass dust is recovered.

近年、セメント製造工程で処理されるリサイクル廃棄物の量が増加している。しかし、これに伴い、セメント製造装置から排出されるガス中の環境負荷物質の増加が懸念される。そのため、前記排ガス中のＳＯ2に関して、高濃度のＳＯ2を含む塩素バイパス排ガスをセメントキルンに付設されたプレヒータなどに戻してＳＯ2濃度を低減しているが、熱量損失やセメントキルンの安定運転の阻害要因となっている。 In recent years, the amount of recycled waste processed in the cement manufacturing process has increased. However, along with this, there is a concern about an increase in environmentally hazardous substances in the gas discharged from the cement manufacturing apparatus. Therefore, with respect to SO 2 in the flue gas, chlorine bypass exhaust gases back like a preheater which is attached to the cement kiln is reduced to SO 2 concentration, but the stable operation of the heat losses and cement kiln containing a high concentration of SO 2 It is an obstruction factor.

そこで、特許文献１には、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排ガスの一部を冷却しながら抽気するプローブと、プローブによる抽気ガスを湿式で脱硫する脱硫装置と、脱硫装置から排出されるスラリーを分級する湿式分級装置とを備える塩素バイパスシステムが提案されている。   Therefore, in Patent Document 1, a probe for extracting air while cooling a part of the combustion exhaust gas from the kiln exhaust gas passage from the bottom of the kiln of the cement kiln to the lowermost cyclone of the preheater, and the extraction gas by the probe are desulfurized in a wet manner. A chlorine bypass system has been proposed that includes a desulfurization apparatus that performs the above and a wet classification apparatus that classifies the slurry discharged from the desulfurization apparatus.

また、特許文献２には、プローブによる抽気ガスに水を噴霧し、抽気ガス中の生石灰と水とで生成された消石灰を、抽気ガス中のＳＯ2と反応させて抽気ガス中のＳＯ2を除去するスプレー塔と、スプレー塔の排ガスに含まれるダスト（石膏）を回収する乾式集塵機とを備えるセメントキルン燃焼排ガスの処理装置が提案されている。ここで、スプレー塔に、水に代えて、又は水と共に、水と消石灰からなるスラリーを噴霧することができる。 Further, in Patent Document 2, water is sprayed on the extraction gas by the probe, and slaked lime generated from quick lime and water in the extraction gas is reacted with SO 2 in the extraction gas, thereby obtaining SO 2 in the extraction gas. A cement kiln combustion exhaust gas treatment apparatus including a spray tower to be removed and a dry dust collector for collecting dust (gypsum) contained in the exhaust gas of the spray tower has been proposed. Here, the slurry which consists of water and slaked lime can be sprayed to a spray tower instead of water or with water.

特開２０１４−１０８９０７号公報JP 2014-108907 A 特開２０１４−１０８９０６号公報JP 2014-108906 A

しかし、上記特許文献１、２に記載の塩素バイパスシステムは、不純物の少ない脱塩ケーキを回収して塩素バイパスダストの用途を拡大したり、水の使用量を抑えて塩素バイパス排ガスを処理することができるが、ＳＯ2濃度の変動が大きい塩素バイパス排ガスを安定して処理するためには大規模な設備が必要になる。 However, the chlorine bypass system described in Patent Documents 1 and 2 collects desalted cake with less impurities and expands the use of chlorine bypass dust, or treats chlorine bypass exhaust gas while reducing the amount of water used. However, a large-scale facility is required to stably treat the chlorine bypass exhaust gas having a large variation in SO 2 concentration.

そこで、本発明は、上記従来の技術における問題点に鑑みてなされたものであって、用水の確保、及び排水や回収物の処理を勘案することなく、設備コストを低く抑えながら、塩素バイパス排ガスを安定して処理することを目的とする。   Therefore, the present invention has been made in view of the problems in the above-described conventional technology, and it is possible to reduce the facility cost and reduce the chlorine bypass exhaust gas without taking into consideration the securing of water and the treatment of drainage and collected matter. It aims at processing stably.

上記目的を達成するため、本発明の塩素バイパス排ガスの処理方法は、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、該抽気ガスから乾式で塩素バイパスダストを回収した後の集塵機出口ガスに粉体状の脱硫剤を添加することを特徴とする。   In order to achieve the above object, the chlorine bypass exhaust gas treatment method of the present invention bleeds while cooling a part of the combustion gas from the kiln exhaust gas passage from the kiln bottom of the cement kiln to the lowermost cyclone. A powdery desulfurizing agent is added to the dust collector outlet gas after the chlorine bypass dust is recovered from the gas by a dry method.

本発明によれば、粉体状の脱硫剤を塩素バイパスダストを回収した後の集塵機出口ガスに添加するだけであるため、設備コストを低く抑えながら、ＳＯ2濃度の変動が大きい塩素バイパス排ガスを安定して処理することができる。また、塩素バイパスダストを回収した後の集塵機出口ガスは、脱硫剤との反応性を高く保持できるため脱硫剤の添加位置として適する。 According to the present invention, since the powder desulfurization agent is only added to the dust collector outlet gas after the chlorine bypass dust is recovered, the chlorine bypass exhaust gas having a large variation in SO 2 concentration can be obtained while keeping the equipment cost low. It can be processed stably. Further, the dust collector outlet gas after recovering the chlorine bypass dust is suitable as a desulfurization agent addition position because it can maintain high reactivity with the desulfurization agent.

また、本発明の塩素バイパス排ガスの処理方法は、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、該抽気ガスから乾式で塩素バイパスダストを回収した後の集塵機出口ガスが、前記セメントキルンに付設されたプレヒータの排ガスと合流した後の排ガスに粉体状の脱硫剤を添加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、設備コストを低く抑えながら、ＳＯ2濃度の変動が大きい塩素バイパス排ガスを安定して処理することができる。 In addition, the chlorine bypass exhaust gas treatment method of the present invention performs extraction while cooling a part of the combustion gas from the kiln exhaust gas passage from the kiln bottom of the cement kiln to the lowermost cyclone, The dust collector outlet gas after collecting the bypass dust adds a powdery desulfurizing agent to the exhaust gas after joining the exhaust gas of the preheater attached to the cement kiln. According to the present invention, similarly to the above-described invention, it is possible to stably treat the chlorine bypass exhaust gas having a large variation in SO 2 concentration while keeping the equipment cost low.

上記塩素バイパス排ガスの処理方法において、前記粉体状の脱硫剤を、消石灰、前記抽気ガスを分級して得られた粗粉、又は前記セメントキルンの排ガスから除塵する集塵機で回収されたダストとすることができる。これら粗粉や集塵機で回収されたダストを用いることで運転コストも低減することができる。   In the chlorine bypass exhaust gas treatment method, the powdery desulfurizing agent is slaked lime, coarse powder obtained by classifying the extracted gas, or dust collected by a dust collector that removes dust from the exhaust gas of the cement kiln. be able to. Operating costs can be reduced by using these coarse powders and dust collected by a dust collector.

また、前記セメントキルンの排ガスから除塵する集塵機の下流側の排ガスのＳＯ2濃度を測定し、該ＳＯ2濃度に応じて前記脱硫剤の投入量を制御することができ、脱硫剤の投入量を適切に制御することができる。 Further, the SO 2 concentration of the exhaust gas downstream of the dust collector that removes dust from the exhaust gas of the cement kiln can be measured, and the input amount of the desulfurizing agent can be controlled according to the SO 2 concentration. It can be controlled appropriately.

以上のように、本発明によれば、設備コストを低く抑えながら、塩素バイパス排ガスを安定して処理することができる。   As described above, according to the present invention, chlorine bypass exhaust gas can be stably treated while keeping facility costs low.

本発明に係る塩素バイパス排ガスの処理方法を適用したセメント製造装置を示す全体構成図である。It is a whole block diagram which shows the cement manufacturing apparatus to which the processing method of the chlorine bypass exhaust gas which concerns on this invention is applied.

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, embodiments for carrying out the present invention will be described in detail with reference to the drawings.

図１は、本発明に係る塩素バイパス排ガスの処理方法を適用したセメント製造装置を示し、このセメント製造装置１は、セメントキルン２に付設されたプレヒータ（不図示）の排ガスＧ１を誘引する誘引ファン３と、誘引ファン３から排ガスＧ２が供給され、セメント原料を乾燥又は／及び粉砕するドライヤ又は／及び原料ミル（以下「ドライヤ等」という。）４と、ドライヤ等４の排ガスＧ４から除塵する電気集塵機等の集塵機５と、集塵機５の排ガスＧ５のＳＯ2濃度を測定するＳＯ2測定器６と、セメントキルン２の窯尻から最下段サイクロン（不図示）に至るまでのキルン排ガス流路から燃焼ガスＧ６を抽気しながら低温ガスにより冷却するプローブ８と、プローブ８からの抽気ガスＧ７を粗粉Ｄ１と、微粉Ｄ２を含む排ガスＧ８とに分離する分級機としてのサイクロン９と、サイクロン９からの微粉Ｄ２を含む排ガスＧ８を冷却する冷却器１０と、冷却器１０からの排ガスＧ９から微粉Ｄ４を回収するバグフィルタ（集塵機）１１と、バグフィルタ１１の排ガスＧ１０を誘引ファン３の出口側に戻すための排気ファン１２と、排気ファン１２の排ガスＧ１１に粉体状の脱硫剤ＤＡを投入する脱硫剤投入装置１３とを備える。 FIG. 1 shows a cement manufacturing apparatus to which a chlorine bypass exhaust gas treatment method according to the present invention is applied. This cement manufacturing apparatus 1 is an induction fan for attracting an exhaust gas G1 of a preheater (not shown) attached to a cement kiln 2. 3, an exhaust gas G2 is supplied from the induction fan 3, and a dryer or / and a raw material mill (hereinafter referred to as “dryer etc.”) 4 for drying or / and pulverizing the cement raw material, and an electricity for removing dust from the exhaust gas G4 of the dryer 4 etc. Combustion from the dust collector 5 such as a dust collector, the SO 2 measuring device 6 for measuring the SO 2 concentration of the exhaust gas G5 of the dust collector 5, and the kiln exhaust gas passage from the bottom of the cement kiln 2 to the lowermost cyclone (not shown) The probe 8 that cools the gas G6 with the low-temperature gas while extracting the gas G6, the extracted gas G7 from the probe 8 into the coarse powder D1 and the exhaust gas G8 containing the fine powder D2 A cyclone 9 as a classifier to be separated, a cooler 10 for cooling the exhaust gas G8 containing the fine powder D2 from the cyclone 9, a bag filter (dust collector) 11 for collecting the fine powder D4 from the exhaust gas G9 from the cooler 10, and a bug An exhaust fan 12 for returning the exhaust gas G10 of the filter 11 to the outlet side of the induction fan 3 and a desulfurization agent charging device 13 for charging the powdery desulfurization agent DA into the exhaust gas G11 of the exhaust fan 12 are provided.

上記セメント製造装置１において、ＳＯ2測定器６及び脱硫剤投入装置１３以外の各装置は、一般的なセメント製造装置や塩素バイパスシステムで用いられるものであって、これらについての説明は省略する。また、セメント製造装置には、廃熱発電設備や、誘引ファン３に加えてさらに煙突７の上流側に誘引ファン等を設けるのが一般的であるが、これらの設備等についての記載も省略する。また、集塵機５には電気集塵機に代えてバグフィルタを用いることもある。 In the cement manufacturing apparatus 1, the apparatus other than SO 2 meter 6 and desulfurization agent dispenser 13, which is used in a general cement manufacturing apparatus and chlorine bypass system, the description thereof will be omitted. In addition to the waste heat power generation facility and the induction fan 3, the cement manufacturing apparatus is generally provided with an induction fan or the like further upstream of the chimney 7, but description of these facilities and the like is also omitted. . In addition, a bag filter may be used for the dust collector 5 instead of the electric dust collector.

次に、上記セメント製造装置１における、本発明に係る塩素バイパス排ガスの処理方法について、図１を参照しながら詳細に説明する。   Next, the chlorine bypass exhaust gas treatment method according to the present invention in the cement production apparatus 1 will be described in detail with reference to FIG.

誘引ファン３によって誘引されたプレヒータの排ガスＧ１は、ドライヤ等４でセメント原料の乾燥等に利用され、集塵機５で除塵された後煙突７から大気に放出される。集塵機５で回収されたダストＤ６の一部は、脱硫剤の一部として脱硫剤投入装置１３に供給される。また、煙突７から大気に放出される前の排ガスＧ５のＳＯ2濃度がＳＯ2測定器６によって測定される。 The preheater exhaust gas G1 attracted by the attracting fan 3 is used for drying the cement raw material by the dryer 4 or the like, and is discharged from the chimney 7 after being removed by the dust collector 5. Part of the dust D6 collected by the dust collector 5 is supplied to the desulfurizing agent charging device 13 as a part of the desulfurizing agent. Further, the SO 2 concentration of the exhaust gas G5 before being released from the chimney 7 to the atmosphere is measured by the SO 2 measuring device 6.

一方、セメントキルン２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Ｇ６をプローブ８によって抽気しながら塩素化合物の融点である７００℃程度以下に急冷する。次いで、サイクロン９において、プローブ８からの抽気ガスＧ７を粗粉Ｄ１と、微粉Ｄ２を含む排ガスＧ８とに分離し、粗粉Ｄ１の一部Ｄ８を脱硫剤の一部として脱硫剤投入装置１３に供給すると共に、残りの粗粉Ｄ７をセメントキルン系に戻す。脱硫剤として使用する粗粉Ｄ８は、塩素分を除去すると共に、ハンドリング性等を考慮し、水洗後脱水乾燥させたものが好ましい。また、粗粉Ｄ８を再度分級して粒度調整したものを用いることもできる。脱硫剤投入装置１３には、さらに消石灰ＳＬが供給される。   On the other hand, the combustion gas G6 is rapidly cooled to about 700 ° C. or less, which is the melting point of the chlorine compound, while the combustion gas G6 is extracted from the kiln exhaust gas flow path from the bottom of the kiln 2 to the lowermost cyclone. Next, in the cyclone 9, the extracted gas G7 from the probe 8 is separated into the coarse powder D1 and the exhaust gas G8 containing the fine powder D2, and a part D8 of the coarse powder D1 is used as a part of the desulfurizing agent to the desulfurizing agent charging device 13. At the same time, the remaining coarse powder D7 is returned to the cement kiln system. The coarse powder D8 used as the desulfurizing agent is preferably one obtained by removing chlorine and taking into consideration handling properties and the like, followed by dehydration and drying. Further, coarse powder D8 can be classified again and the particle size adjusted can be used. The desulfurization agent charging device 13 is further supplied with slaked lime SL.

一方、排ガスＧ８及び微粉Ｄ２は、冷却器１０において冷風により１５０℃〜２５０℃に冷却した後、バグフィルタ１１に導入する。バグフィルタ１１において、微粉Ｄ４が集塵され、冷却器１０で回収された微粉Ｄ３と共に塩素バイパスダストＤ５としてセメント焼成工程の系外に排出して処理する。   On the other hand, the exhaust gas G8 and the fine powder D2 are cooled to 150 ° C. to 250 ° C. with cool air in the cooler 10 and then introduced into the bag filter 11. In the bag filter 11, the fine powder D4 is collected, and discharged together with the fine powder D3 collected by the cooler 10 as chlorine bypass dust D5 outside the cement firing process.

バグフィルタ１１から排出された排ガスＧ１０は、排気ファン１２を介して誘引ファン３の出口側（ドライヤ等４の上流側）に戻され、排ガスＧ２と合流する。その際、排気ファン１２の排ガスＧ１１に脱硫剤投入装置１３から脱硫剤ＤＡが添加される。脱硫剤ＤＡは、排気ファン１２の出口に、負圧を利用して自然吸い込みによって供給してもよく、ロータリバルブを介して供給したり、粉体の吹込みが可能な装置（エジェクタ、ルーツブロアによる圧送吹込み）を用いて供給してもよい。また、排ガスＧ１１に脱硫剤ＤＡを拡散させながら供給する。この脱硫剤ＤＡは、上述のように、集塵機５で回収されたダストＤ６、サイクロン９で分離された粗粉Ｄ１、消石灰ＳＬであり、消石灰ＳＬがＳＯ2との反応性を考慮して最適であるが、これらのいずれか一つでも、二つ以上であってもよい。脱硫剤ＤＡとして投入する粉体の種類は、排ガスＧ１１のＳＯ2濃度や目標のＳＯ2濃度に応じて適宜選択する。 The exhaust gas G10 discharged from the bag filter 11 is returned to the outlet side of the induction fan 3 (upstream side of the dryer 4 and the like) through the exhaust fan 12, and merges with the exhaust gas G2. At that time, the desulfurization agent DA is added to the exhaust gas G11 of the exhaust fan 12 from the desulfurization agent charging device 13. The desulfurizing agent DA may be supplied to the outlet of the exhaust fan 12 by natural suction using negative pressure, or may be supplied via a rotary valve or a device capable of blowing powder (by an ejector or a roots blower). You may supply using pressure blowing. Further, the desulfurization agent DA is supplied to the exhaust gas G11 while being diffused. As described above, the desulfurizing agent DA is the dust D6 collected by the dust collector 5, the coarse powder D1 separated by the cyclone 9, and the slaked lime SL, and the slaked lime SL is optimum in consideration of the reactivity with SO 2. However, any one or two or more of these may be used. Type of powder to be introduced as a desulfurizing agent DA is suitably selected depending on the SO 2 concentration in the SO 2 concentration and the target exhaust gas G11.

脱硫剤ＤＡの添加により、排ガスＧ１１中のＳＯ2が脱硫剤ＤＡに含まれるＣａ（ＯＨ）2、ＣａＯ、ＣａＣＯ3と反応してＣａＳＯ3又はＣａＳＯ4となり脱硫される。ＳＯ2測定器６によって測定されたＳＯ2濃度に応じて脱硫剤ＤＡの投入量を増減する。脱硫後の排ガスＧ１２は、誘引ファン３の排ガスＧ２と合流し、ドライヤ等４、集塵機５及びＳＯ2測定器６を経て煙突７から大気に放出される。 By the addition of the desulfurizing agent DA, SO 2 in the exhaust gas G11 reacts with Ca (OH) 2 , CaO, and CaCO 3 contained in the desulfurizing agent DA to become CaSO 3 or CaSO 4 and is desulfurized. The input amount of the desulfurization agent DA is increased or decreased according to the SO 2 concentration measured by the SO 2 measuring device 6. The exhaust gas G12 after desulfurization merges with the exhaust gas G2 of the induction fan 3, and is discharged from the chimney 7 to the atmosphere through the dryer 4 and the like, the dust collector 5 and the SO 2 measuring device 6.

尚、上記実施の形態においては、ＳＯ2濃度が高く、排ガスＧ２に比べガス量の少ない排ガスＧ１１に脱硫剤ＤＡを直接添加することで脱硫効果を高めることができて好ましいが、排ガスＧ１１に代えて又は排ガスＧ１１に添加すると共に、図１に示す排ガスＧ１２と排ガスＧ２とが合流した後の排ガス（排ガスＧ３、Ｇ４等）に添加してもよい。 In the above embodiment, the desulfurization effect can be enhanced by adding the desulfurization agent DA directly to the exhaust gas G11 having a high SO 2 concentration and a smaller gas amount than the exhaust gas G2. Or in addition to the exhaust gas G11, it may be added to the exhaust gas (exhaust gas G3, G4, etc.) after the exhaust gas G12 and the exhaust gas G2 shown in FIG.

セメント製造工場において、排ガスＧ１１、排ガスＧ４及び排ガスＧ３に、空気圧送装置（ジェクター：Ｊリンク社製）を用いて消石灰を投入した（消石灰投入量は適宜調整）。投入前のＳＯ2測定器の濃度から求められるＳＯ2モル量（排ガス量×ＳＯ2濃度）と消石灰投入によるＣａモル量とから、その比（Ｃａ／Ｓ）を求め、投入前ＳＯ2濃度を１として投入後のＳＯ2濃度を算出した。その結果を表１に示す。 In the cement manufacturing plant, slaked lime was introduced into the exhaust gas G11, the exhaust gas G4, and the exhaust gas G3 by using a pneumatic feeder (Jector: manufactured by J-Link Co., Ltd.). The ratio (Ca / S) is obtained from the SO 2 molar amount (exhaust gas amount × SO 2 concentration) obtained from the concentration of the SO 2 measuring instrument before charging and the Ca molar amount due to slaked lime charging, and the SO 2 concentration before charging is determined. The SO 2 concentration after charging was calculated as 1. The results are shown in Table 1.

Figure 2016056070
Figure 2016056070

同表から明らかなように、排ガスＧ１１、排ガスＧ３及び排ガスＧ４のいずれに消石灰を投入しても効果があるが、排ガスＧ１１への投入がより効果的である。また、上記関係等と用いることにより、ＳＯ2測定器の濃度から安定した脱硫剤の投入量を適切に制御し、所望のＳＯ2濃度にすることができる。 As apparent from the table, it is effective to put slaked lime into any of the exhaust gas G11, the exhaust gas G3, and the exhaust gas G4, but the introduction into the exhaust gas G11 is more effective. Further, by using the above relationship and the like, it is possible to appropriately control the amount of the desulfurization agent that is stably supplied from the concentration of the SO 2 measuring device, and to obtain a desired SO 2 concentration.

１ セメント製造装置
２ セメントキルン
３ 誘引ファン
４ ドライヤ等
５ 集塵機
６ ＳＯ2測定器
７ 煙突
８ プローブ
９ サイクロン
１０ 冷却器
１１ バグフィルタ
１２ 排気ファン
Ｄ１ 粗粉
Ｄ２〜Ｄ４ 微粉
Ｄ５ 塩素バイパスダスト
Ｄ６ ダスト
Ｄ７、Ｄ８ 粗粉
ＤＡ 脱硫剤
Ｇ１〜Ｇ５、Ｇ８〜Ｇ１２ 排ガス
Ｇ６ 燃焼ガス
Ｇ７ 抽気ガス
ＳＬ 消石灰 1 cement manufacturing apparatus 2 cement kiln 3 induction fan 4 dryer, etc. 5 dust collector 6 SO 2 measurement instrument 7 chimney 8 probe 9 cyclone 10 the cooler 11 bag filter 12 exhaust fan D1 coarse D2~D4 fine D5 chlorine bypass dust D6 dust D7, D8 Coarse powder DA Desulfurization agent G1-G5, G8-G12 Exhaust gas G6 Combustion gas G7 Extraction gas SL Slaked lime

Claims (4)

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、該抽気ガスから塩素バイパスダストを回収した後の集塵機出口ガスに粉体状の脱硫剤を添加することを特徴とする塩素バイパス排ガスの処理方法。   A part of the combustion gas is extracted from the kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the lowermost cyclone while cooling, and after the chlorine bypass dust is recovered from the extracted gas, the dust collector outlet gas is in the form of powder. A method for treating chlorine bypass exhaust gas, which comprises adding a desulfurizing agent. 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、該抽気ガスから塩素バイパスダストを回収した後の集塵機出口ガスが、前記セメントキルンに付設されたプレヒータの排ガスと合流した後の排ガスに粉体状の脱硫剤を添加することを特徴とする塩素バイパス排ガスの処理方法。   A part of the combustion gas is extracted from the kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the bottom cyclone while cooling, and the dust collector outlet gas after recovering the chlorine bypass dust from the extracted gas is the cement kiln. A treatment method for chlorine bypass exhaust gas, comprising adding a powdery desulfurizing agent to the exhaust gas after joining with the exhaust gas of the preheater attached to the preheater. 前記粉体状の脱硫剤は、消石灰、前記抽気ガスを分級して得られた粗粉、又は前記セメントキルンの排ガスから除塵する集塵機で回収されたダストであることを特徴とする請求項１又は２に記載の塩素バイパス排ガスの処理方法。   The powdery desulfurizing agent is slaked lime, coarse powder obtained by classifying the extracted gas, or dust collected by a dust collector that removes dust from the exhaust gas of the cement kiln. 2. A method for treating chlorine bypass exhaust gas according to 2. 前記セメントキルンの排ガスから除塵する集塵機の下流側の排ガスのＳＯ2濃度を測定し、該ＳＯ2濃度に応じて前記脱硫剤の投入量を制御することを特徴とする請求項１、２又は３に記載の塩素バイパス排ガスの処理方法。 The SO 2 concentration of the exhaust gas downstream of the dust collector that removes dust from the exhaust gas of the cement kiln is measured, and the input amount of the desulfurizing agent is controlled according to the SO 2 concentration. A method for treating chlorine bypass exhaust gas according to claim 1.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017036165A (en) * 2015-08-07 2017-02-16 太平洋セメント株式会社 Operational method of cement burning device

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10330136A (en) * 1997-05-30 1998-12-15 Ube Ind Ltd Calcination of cement raw material and apparatus for calcination
JP2007031188A (en) * 2005-07-25 2007-02-08 Sumitomo Osaka Cement Co Ltd Method and apparatus for treating waste gas in cement firing equipment
JP2009035449A (en) * 2007-08-02 2009-02-19 Taiheiyo Cement Corp System and method for treating cement kiln extraction gas
JP2009234859A (en) * 2008-03-27 2009-10-15 Taiheiyo Cement Corp Method for desulfurizing tail gas in cement production
WO2009154088A1 (en) * 2008-06-17 2009-12-23 太平洋セメント株式会社 Apparatus and method for treating gas discharged from cement kiln
JP2012140313A (en) * 2011-01-06 2012-07-26 Taiheiyo Cement Corp Chlorine bypass system, and method for treatment of chlorine bypass extracted gas
JP2012200627A (en) * 2011-03-24 2012-10-22 Taiheiyo Cement Corp Apparatus and method for treating chlorine bypass exhaust gas
JP2013049580A (en) * 2011-08-30 2013-03-14 Taiheiyo Cement Corp Treatment method for cement kiln flue gas
JP2013230980A (en) * 2013-07-22 2013-11-14 Taiheiyo Cement Corp Method and system for treating cement kiln bleed gas
JP2014108907A (en) * 2012-12-03 2014-06-12 Taiheiyo Cement Corp Treatment device for cement kiln combustion exhaust gas and treatment method therefor

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10330136A (en) * 1997-05-30 1998-12-15 Ube Ind Ltd Calcination of cement raw material and apparatus for calcination
JP2007031188A (en) * 2005-07-25 2007-02-08 Sumitomo Osaka Cement Co Ltd Method and apparatus for treating waste gas in cement firing equipment
JP2009035449A (en) * 2007-08-02 2009-02-19 Taiheiyo Cement Corp System and method for treating cement kiln extraction gas
JP2009234859A (en) * 2008-03-27 2009-10-15 Taiheiyo Cement Corp Method for desulfurizing tail gas in cement production
WO2009154088A1 (en) * 2008-06-17 2009-12-23 太平洋セメント株式会社 Apparatus and method for treating gas discharged from cement kiln
JP2012140313A (en) * 2011-01-06 2012-07-26 Taiheiyo Cement Corp Chlorine bypass system, and method for treatment of chlorine bypass extracted gas
JP2012200627A (en) * 2011-03-24 2012-10-22 Taiheiyo Cement Corp Apparatus and method for treating chlorine bypass exhaust gas
JP2013049580A (en) * 2011-08-30 2013-03-14 Taiheiyo Cement Corp Treatment method for cement kiln flue gas
JP2014108907A (en) * 2012-12-03 2014-06-12 Taiheiyo Cement Corp Treatment device for cement kiln combustion exhaust gas and treatment method therefor
JP2013230980A (en) * 2013-07-22 2013-11-14 Taiheiyo Cement Corp Method and system for treating cement kiln bleed gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017036165A (en) * 2015-08-07 2017-02-16 太平洋セメント株式会社 Operational method of cement burning device

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