JP3032198B1 - Method and apparatus for firing lime mud - Google Patents
Method and apparatus for firing lime mudInfo
- Publication number
- JP3032198B1 JP3032198B1 JP11060961A JP6096199A JP3032198B1 JP 3032198 B1 JP3032198 B1 JP 3032198B1 JP 11060961 A JP11060961 A JP 11060961A JP 6096199 A JP6096199 A JP 6096199A JP 3032198 B1 JP3032198 B1 JP 3032198B1
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- fluidized
- raw material
- exhaust gas
- fine powder
- 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 - Fee Related
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Abstract
【要約】
【課題】 小型・コンパクト化することができる高熱効
率の石灰泥焼成装置を提供する。
【解決手段】 粒状の流動媒体で流動層が形成される流
動層乾燥機１０に石灰泥を原料として投入し乾燥させた
後、乾燥排ガスから乾燥機サイクロン５２で捕捉された
乾燥微粉原料を主原料として粒状の流動媒体で流動層が
形成される流動層焼成炉１４に導入し焼成して生石灰微
粉とし、流動層焼成炉１４からの排ガスを焼成炉サイク
ロン２６に導入して排ガスから焼成生石灰微粉を分離・
捕集し、捕集された生石灰微粉を気流式クーラ３０に投
入し冷却用空気と接触させて冷却し、焼成炉サイクロン
２６からの排ガスを流動層乾燥機１０の風箱に導入し流
動化ガス兼乾燥用ガスとして用いるとともに熱回収す
る。A high-thermal-efficiency lime mud firing apparatus that can be reduced in size and size is provided. SOLUTION: Lime mud is fed as a raw material into a fluidized bed dryer 10 in which a fluidized bed is formed with a granular fluidized medium and dried, and then a dried fine powder raw material captured by a dryer cyclone 52 from a dried exhaust gas is used as a main raw material. Into a fluidized bed calcining furnace 14 in which a fluidized bed is formed with a granular fluidized medium, and calcined into calcined lime fine powder. Exhaust gas from the fluidized bed calcining furnace 14 is introduced into a calcining furnace cyclone 26 to produce calcined quick lime fine powder from the flue gas. Separation
The collected quicklime powder is collected and introduced into an air-flow cooler 30 to be brought into contact with cooling air to be cooled. Exhaust gas from the firing furnace cyclone 26 is introduced into a wind box of the fluidized-bed dryer 10 to be fluidized gas. Used as a gas for drying and heat recovery.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、石灰泥（主として
ＣａＣＯ3 からなる）を流動層焼成して生石灰（Ｃａ
Ｏ）微粉を製造する石灰泥の焼成方法及び装置に関する
ものである。BACKGROUND OF THE INVENTION The present invention is lime mud (mainly consisting of CaCO 3) a fluidized bed calcined to lime (Ca
O) A method and an apparatus for firing lime mud for producing fine powder.
【０００２】[0002]
【従来の技術】クラフトパルプを取り扱う製紙プロセス
や製糖プロセス等に生石灰が使用されており、副産物と
して、不純物を含む高水分の石灰泥が生成される。従
来、石灰泥の一部は気流乾燥機付ロータリキルン等で焼
成されて生石灰として再生され利用されているが、石灰
泥の大半は廃棄処分されている。2. Description of the Related Art Quick lime is used in a paper making process, a sugar making process, and the like that handle kraft pulp, and as a by-product, high-moisture lime mud containing impurities is generated. Conventionally, a part of lime mud is burned in a rotary kiln equipped with a flash dryer and the like is recycled and used as quicklime, but most of the lime mud is disposed of.
【０００３】石灰泥を気流乾燥機付ロータリキルンで焼
成する場合、ロータリキルンは熱効率が悪いため設備が
大型化する。一方、流動層炉で石灰石を焼成する装置は
熱効率が良く、装置を小型化することができるが、原料
粒度は数mmのオーダーに限定され、μm オーダーの石灰
泥を焼成することは困難であった。その理由は、通常、
流動化速度は原料粒度にほぼ比例するので、石灰泥を焼
成するためには炉径を大きくして流動化速度を小さくす
る必要があり、流動化速度が小さいことにより、微粉が
造粒され流動化停止に至るからである。When calcining lime mud with a rotary kiln equipped with a flash dryer, the rotary kiln has a poor thermal efficiency, resulting in an increase in equipment size. On the other hand, an apparatus for firing limestone in a fluidized bed furnace has good thermal efficiency and can be downsized.However, the raw material particle size is limited to the order of several mm, and it is difficult to fire lime mud on the order of μm. Was. The reason is usually
Since the fluidization speed is almost proportional to the raw material particle size, it is necessary to increase the furnace diameter and reduce the fluidization speed in order to bake lime mud. This is because of the suspension.
【０００４】従来、石灰泥を生石灰として回収する方法
及び装置としては、例えば、特開昭５４−６６３９８号
公報に、石灰泥原料と石灰泥乾燥粉（乾粉原料）とをパ
ドルミキサで撹拌混合した後、ケージミルを有する気流
乾燥機で粉砕しながらキルン排ガスで気流乾燥し、つい
でサイクロンで集塵し、捕集された乾燥粉の一部を気流
式仮焼炉で仮焼した後、ロータリキルンで焼成する石灰
泥回収方法及び装置が記載されている。Conventionally, as a method and an apparatus for recovering lime mud as quick lime, for example, Japanese Patent Application Laid-Open No. Sho 54-66398 discloses a method in which a lime mud raw material and a lime mud dry powder (dry powder raw material) are stirred and mixed by a paddle mixer. After drying with a kiln exhaust gas while pulverizing with a flash dryer with a cage mill, dust was collected with a cyclone, and a portion of the collected dry powder was calcined in a flash calciner and then fired in a rotary kiln. A lime mud recovery method and apparatus is described.
【０００５】また、特開平４−６０３８１号公報には、
流動層焼成炉とその上方のサスペンションプレヒータと
の間に、流動層型又は噴流層型の仮焼装置（熱交換器）
を配設した粉粒状原料の予熱装置が開示されている。[0005] Also, Japanese Patent Application Laid-Open No. Hei 4-60381 discloses that
Fluid bed or spouted bed type calcining device (heat exchanger) between the fluidized bed firing furnace and the suspension preheater above it
Is disclosed.
【０００６】[0006]
【発明が解決しようとする課題】前記の特開昭５４−６
６３９８号公報記載の方式では、高水分の石灰泥を気流
乾燥機で乾燥させるために、パドルミキサ及びケージミ
ルが必要になり、装置が複雑になるばかりでなくメンテ
ナンスのための停止時間及び費用も多大となる。また、
気流式仮焼炉のみでは滞留時間が短いため十分仮焼する
ことができないので、ロータリキルンが不可欠となる
が、熱効率が悪く装置が大型化するという問題がある。The above-mentioned Japanese Patent Application Laid-Open No. 54-6 / 1979.
In the method described in Japanese Patent No. 6398, a paddle mixer and a cage mill are required to dry high-moisture lime mud with a flash dryer, which not only complicates the apparatus but also requires a large amount of downtime and cost for maintenance. Become. Also,
A rotary kiln is indispensable because only the air-flow type calciner cannot be calcined due to a short residence time. However, there is a problem that the heat efficiency is poor and the apparatus becomes large.
【０００７】また、前述の特開平４−６０３８１号公報
記載の方式では、流動層は非常に高伝熱性であるので小
型でかつコンパクトな装置となり、均一な高品質の焼成
品が得られるとされているが、通常、流動層はmmオーダ
ーの原料を処理するのに適しており、乾燥された石灰泥
のような微粉の場合は、正常な流動層を形成するために
流動化速度を小さくしなければならないので、炉径を大
きくする必要があり大型化するので、流動層を採用する
ことができない。In the method described in the above-mentioned Japanese Patent Application Laid-Open No. Hei 4-60381, the fluidized bed has a very high heat conductivity, so that the apparatus is small and compact, and a uniform high-quality fired product can be obtained. However, fluidized beds are usually suitable for processing raw materials of the order of mm, and in the case of fine powder such as dried lime mud, the fluidization rate should be reduced to form a normal fluidized bed. Therefore, it is necessary to increase the diameter of the furnace and increase the size of the furnace, so that a fluidized bed cannot be adopted.
【０００８】また、８００〜５５０℃の温度領域が存在
すれば、焼成された生石灰が再炭酸化して炭酸カルシウ
ムになり、装置内壁等に付着するという問題がある。本
発明は、上記の諸点に鑑みなされたもので、本発明の目
的は、流動層炉を小型化、コンパクト化することがで
き、かつ、生石灰の再炭酸化の問題も生じることのな
い、高熱効率の石灰泥流動層焼成方法及び装置を提供す
ることにある。Further, if a temperature range of 800 to 550 ° C. exists, there is a problem that calcined quicklime is recarbonated to calcium carbonate and adheres to the inner wall of the apparatus. The present invention has been made in view of the above-mentioned points, and an object of the present invention is to provide a fluidized bed furnace that can be reduced in size and size, and that does not cause a problem of re-carbonation of quick lime. An object of the present invention is to provide a method and an apparatus for burning a fluidized bed of lime mud with high efficiency.
【０００９】[0009]
【課題を解決するための手段】上記の目的を達成するた
めに本発明の石灰泥の焼成方法は、粒状の流動媒体で流
動層が形成される流動層乾燥機に石灰泥を原料として投
入し乾燥させた後、乾燥排ガスから捕捉された乾燥微粉
原料を主原料として粒状の流動媒体で流動層が形成され
る流動層焼成炉に導入し焼成して生石灰微粉とし、流動
層焼成炉からの排ガスを焼成炉サイクロンに導入して排
ガスから焼成生石灰微粉を分離・捕集し、捕集された生
石灰微粉を気流式クーラに投入し冷却用空気と接触させ
て冷却し、焼成炉サイクロンからの排ガスを流動層乾燥
機に導入し流動化ガス兼乾燥用ガスとして用いるととも
に熱回収するように構成されている（図１〜図５参
照）。In order to achieve the above object, a method for calcining lime mud according to the present invention comprises the steps of charging lime mud as a raw material into a fluidized bed dryer in which a fluidized bed is formed with a granular fluidized medium. After drying, the dried fine powder raw material captured from the dried exhaust gas is introduced into a fluidized bed firing furnace in which a fluidized bed is formed with a granular fluidized medium using the granular raw material as a main raw material and fired to produce quick lime fine powder. Into the firing furnace cyclone to separate and collect the calcined quick lime fines from the exhaust gas, put the collected quick lime fines into the air-flow cooler, contact it with cooling air and cool, and remove the exhaust gas from the firing furnace cyclone. It is configured to be introduced into a fluidized bed dryer, used as a fluidizing gas and a drying gas, and to recover heat (see FIGS. 1 to 5).
【００１０】この方法において、流動層乾燥機からの流
動媒体及び造粒された乾燥原料、並びに乾燥排ガスから
捕捉された乾燥微粉原料を流動層焼成炉の流動層内に導
入する場合もある（図２、図５参照）。また、流動層乾
燥機からの排ガスをサイクロン等の乾燥機集塵器に導入
して排ガスから乾燥された微粉原料を分離・捕集し、捕
集された微粉原料を流動層焼成炉の流動層内に供給する
ことが好ましい（図１、図２、図４、図５参照）。この
場合、乾燥機集塵器で捕集された微粉原料をエジェクタ
ーにより流動層焼成炉の流動層内に吹き込むことが好ま
しい（図１、図２、図４、図５参照）。In this method, a fluidized medium and a granulated dry raw material from a fluidized bed dryer, and a dry fine powder raw material captured from a dried exhaust gas may be introduced into a fluidized bed of a fluidized bed firing furnace (see FIG. 1). 2, see FIG. 5). In addition, the exhaust gas from the fluidized bed dryer is introduced into a dust collector such as a cyclone to separate and collect the dried fine powder raw material from the exhaust gas, and the collected fine powder raw material is fluidized bed of a fluidized bed firing furnace. It is preferable to supply it into the inside (see FIGS. 1, 2, 4, and 5). In this case, it is preferable that the fine powder raw material collected by the dryer dust collector be blown into the fluidized bed of the fluidized bed baking furnace by an ejector (see FIGS. 1, 2, 4, and 5).
【００１１】また、これらの方法において、定常粉化相
当量の流動媒体を流動層乾燥機又は／及び流動層焼成炉
に投入することが好ましい（図１、図２、図４、図５参
照）。粒状の流動媒体は平均粒径数mmのオーダー、すな
わち、０．５〜６mm、望ましくは１〜３mmの流動媒体で
ある。平均粒径が上記の範囲未満の場合は、炉径が大き
くなり経済的に不利なばかりでなく、原料が造粒されて
流動化停止に至ることとなり、一方、平均粒径が上記の
範囲を超える場合は、流動化流速が速いため、微粉の滞
留時間が不足し、十分焼成されないこととなる。また、
気流式クーラは１段又は複数段のサイクロンで構成さ
れ、冷却後の熱風を流動層焼成炉に導入し流動化兼燃焼
用空気として用いることが好ましい（図１、図２、図
４、図５参照）。Further, in these methods, it is preferable to introduce a fluidized medium in an amount equivalent to the steady pulverization into a fluidized-bed dryer and / or a fluidized-bed firing furnace (see FIGS. 1, 2, 4, and 5). . The granular fluid medium is a fluid medium having an average particle size of several mm, that is, 0.5 to 6 mm, preferably 1 to 3 mm. When the average particle size is less than the above range, not only is the furnace diameter large and economically disadvantageous, but also the raw material is granulated and the fluidization stops, while the average particle size falls within the above range. If it exceeds, the fluidization flow rate is high, so that the residence time of the fine powder is insufficient, and the powder is not sufficiently fired. Also,
The air-flow type cooler is composed of one or more stages of cyclones, and it is preferable that hot air after cooling is introduced into a fluidized bed firing furnace and used as air for fluidization and combustion (FIGS. 1, 2, 4, and 5). reference).
【００１２】本発明の石灰泥の焼成装置は、石灰泥を原
料として投入し乾燥させるための、粒状の流動媒体で流
動層が形成される流動層乾燥機と、流動層乾燥機からの
排ガスから乾燥微粉原料を捕集するためのサイクロン等
の乾燥機集塵器と、乾燥機集塵器からの乾燥微粉原料を
導入して焼成するための、粒状の流動媒体で流動層が形
成される流動層焼成炉と、流動層焼成炉からの排ガスを
導入して排ガスから焼成生石灰微粉を分離・捕集するた
めの焼成炉サイクロンと、焼成炉サイクロンからの焼成
生石灰微粉を冷却するための気流式クーラと、焼成炉サ
イクロンの排ガス出口と流動層乾燥機の風箱とを接続す
る排ガス導入ダクトとを備えたことを特徴としている
（図１〜図５参照）。A lime mud firing apparatus according to the present invention comprises a fluidized bed dryer in which a fluidized bed is formed with a granular fluidized medium for charging and drying lime mud as a raw material, and an exhaust gas from the fluidized bed dryer. Fluid in which a fluidized bed is formed with a granular fluidized medium for introducing and firing the dry fine powder material from the dryer dust collector such as a cyclone for collecting the dry fine powder material and the dry fine powder material from the dryer dust collector Baking furnace cyclone for introducing flue gas from fluidized bed baking furnace and separating and collecting calcined quick lime fine powder from flue gas, and air flow cooler for cooling calcined quick lime fine powder from calcining furnace cyclone And an exhaust gas introduction duct connecting the exhaust gas outlet of the firing furnace cyclone and the wind box of the fluidized bed dryer (see FIGS. 1 to 5).
【００１３】この装置において、先端が流動層焼成炉の
流動層内に挿入・位置するように、流動媒体及び造粒さ
れた乾燥原料の導入管を設けて構成する場合もある（図
２、図５参照）。また、流動層乾燥機からの排ガスから
乾燥された微粉原料を分離・捕集するための乾燥機集塵
器と、乾燥機集塵器からの乾燥された微粉原料を流動層
焼成炉の流動層内に供給するための微粉原料導入手段と
を備えるように構成することが好ましい（図１、図２、
図４、図５参照）。この場合、微粉原料導入手段として
エジェクターを用いることが好ましい（図１、図２、図
４、図５参照）。流動層焼成炉の流動層及び流動層乾燥
機の流動層は、平均粒径数mmオーダー、すなわち、０．
５〜６mm、望ましくは１〜３mmの流動媒体で形成され
る。In some cases, this apparatus is provided with a fluid medium and an inlet pipe for the granulated dry raw material so that the tip is inserted and positioned in the fluidized bed of the fluidized bed firing furnace (FIGS. 2 and 3). 5). Also, a dryer dust collector for separating and collecting the dried fine powder raw material from the exhaust gas from the fluidized bed dryer, and a dried fine powder raw material from the dryer dust collector for a fluidized bed of a fluidized bed firing furnace. And a fine powder raw material introduction means for supplying the raw material into the inside (FIG. 1, FIG. 2, FIG.
4 and 5). In this case, it is preferable to use an ejector as the fine powder raw material introduction means (see FIGS. 1, 2, 4, and 5). The fluidized bed of the fluidized-bed baking furnace and the fluidized bed of the fluidized-bed dryer have an average particle size on the order of a few mm, that is, a fluidized bed of a fluidized bed.
It is formed of a fluid medium of 5-6 mm, preferably 1-3 mm.
【００１４】また、焼成炉サイクロンとして、上側部に
接線方向に排ガスを導入する排ガス導入口を有するとと
もに、上面中央部に排ガス排出管を有する円筒胴体の下
部に、略逆円錐胴体を連設し、この略逆円錐胴体の下部
に拡大壁部を連設し、さらに、この拡大壁部に略逆円錐
胴部を連設し、略逆円錐胴体の下端部内径Ｄ１と排ガス
排出管の内径ｄがＤ１≧ｄの関係を有し、円筒胴体の内
径Ｄと拡大壁部の下端部内径Ｄ２との間にＤ２＝（０．
８〜１．０）×Ｄの関係を有するようにした高効率サイ
クロンを用いることが好ましい（図３参照）。また、気
流式クーラは、１段又は複数段のサイクロンで構成さ
れ、最上段のサイクロンの熱風出口と流動層焼成炉の風
箱とが熱風導入ダクトを介して接続されているように構
成することが好ましい（図１、図２、図４、図５参
照）。[0014] Further, as a firing furnace cyclone, a substantially inverted conical body is continuously connected to a lower part of a cylindrical body having an exhaust gas introduction port for introducing exhaust gas in a tangential direction at an upper part thereof and an exhaust gas discharge pipe at a center part of an upper surface. An enlarged wall portion is continuously provided at a lower portion of the substantially inverted conical body, and a substantially inverted conical body portion is continuously provided on the enlarged wall portion. A lower end inner diameter D1 of the substantially inverted conical body and an inner diameter d of the exhaust gas discharge pipe are provided. Has a relationship of D1 ≧ d, and D2 = (0 .0) between the inner diameter D of the cylindrical body and the lower end inner diameter D2 of the enlarged wall portion.
It is preferable to use a high-efficiency cyclone having a relationship of 8 to 1.0) × D (see FIG. 3). In addition, the air-flow cooler is configured with one or more stages of cyclones, and the hot air outlet of the uppermost cyclone and the wind box of the fluidized bed firing furnace are connected via a hot air introduction duct. (See FIGS. 1, 2, 4, and 5).
【００１５】[0015]
【発明の実施の形態】以下、本発明の実施の形態を説明
するが、本発明は下記の実施の形態に何ら限定されるも
のではなく、適宜変更して実施することができるもので
ある。図１は本発明の実施の第１形態による石灰泥の焼
成装置を示している。１０は流動層乾燥機で、粒状の流
動媒体（石灰石、砂等）で流動層１２が形成される。１
４は流動層焼成炉で、粒状の流動媒体（石灰石、砂等）
で流動層１６が形成される。１８は原料投入管、２０は
流動媒体及び造粒された乾燥原料の抜出管、２２は流動
媒体及び造粒された乾燥原料の導入管である。抜出管２
０は焼成炉への流動媒体（ＢＭ）補給用で、粉化量より
造粒量が多い場合はＢＭ補給が不要となり、造粒された
乾燥原料を焼成炉に投入する。なお、石灰泥を乾燥する
と大半は微粉化し、排ガスとともに排出される。このた
め、サイクロン等の集塵器は不可欠である。DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described. However, the present invention is not limited to the following embodiments, and can be implemented with appropriate modifications. FIG. 1 shows a lime mud firing apparatus according to a first embodiment of the present invention. Numeral 10 denotes a fluidized bed dryer, which forms a fluidized bed 12 with a granular fluidized medium (limestone, sand, etc.). 1
Reference numeral 4 denotes a fluidized bed firing furnace, which is a granular fluidized medium (limestone, sand, etc.).
Thus, a fluidized bed 16 is formed. Reference numeral 18 denotes a raw material introduction pipe, 20 denotes a fluid medium and a discharge pipe for granulated dry raw material, and 22 denotes a flow medium and a granulated dry raw material introduction pipe. Extraction pipe 2
Numeral 0 is for replenishing the fluidized medium (BM) to the firing furnace. When the amount of granulation is larger than the amount of powder, BM replenishment becomes unnecessary, and the granulated dry raw material is charged into the firing furnace. When lime mud is dried, most of it is pulverized and discharged together with exhaust gas. For this reason, a dust collector such as a cyclone is indispensable.
【００１６】流動層焼成炉１４の排ガス出口２４には焼
成炉サイクロン２６が接続され、この焼成炉サイクロン
２６の下部は焼成生石灰微粉導入管２８を介して１段又
は複数段のサイクロンからなる気流式クーラ３０に接続
されている。図１では、一例として２段のサイクロン３
２ａ、３２ｂからなる気流式クーラ３０を示しており、
焼成生石灰微粉導入管２８は、下段サイクロン３２ａと
上段サイクロン３２ｂとの間の熱風ダクト３４に接続さ
れている。また、焼成炉サイクロン２６の排ガス出口３
６と、流動層乾燥機１０の風箱３８とは、排ガス導入ダ
クト４０を介して接続されている。また、気流式クーラ
３０の上段サイクロン３２ｂの熱風出口４２と、流動層
焼成炉１４の風箱４４とは、熱風導入ダクト４６を介し
て接続されている。４８はバーナである。A flue gas outlet 24 of the fluidized bed calciner 14 is connected to a calciner cyclone 26. The lower part of the calciner cyclone 26 is an air flow type comprising one or more stages of cyclones through a calcined quick lime fine powder introduction pipe 28. It is connected to the cooler 30. In FIG. 1, as an example, a two-stage cyclone 3
2 shows an airflow type cooler 30 composed of 2a and 32b;
The calcined quick lime fine powder introduction pipe 28 is connected to a hot air duct 34 between the lower cyclone 32a and the upper cyclone 32b. Also, the exhaust gas outlet 3 of the firing furnace cyclone 26
6 and the wind box 38 of the fluidized bed dryer 10 are connected via an exhaust gas introduction duct 40. The hot air outlet 42 of the upper cyclone 32 b of the air-flow type cooler 30 is connected to the wind box 44 of the fluidized-bed baking furnace 14 via a hot air introduction duct 46. 48 is a burner.
【００１７】流動層乾燥機１０の排ガス出口５０には、
乾燥機集塵器、たとえば乾燥機サイクロン５２が接続さ
れ、この乾燥機サイクロン５２の下部は、微粉原料導入
管５４を介して微粉原料導入手段、例えばエジェクター
５６に接続されている。５８、６０、６２、６４、６６
は気密排出手段、６８、７０はガス分散手段である。な
お、風箱及びガス分散手段を設けた流動層とする代り
に、散気管タイプの流動層とすることも可能である。The exhaust gas outlet 50 of the fluidized-bed dryer 10 has:
A dryer dust collector, for example, a dryer cyclone 52 is connected, and a lower portion of the dryer cyclone 52 is connected to a fine powder raw material introduction unit, for example, an ejector 56 via a fine powder raw material introduction pipe 54. 58, 60, 62, 64, 66
Is an airtight discharge means, and 68 and 70 are gas dispersion means. Instead of a fluidized bed provided with a wind box and gas dispersion means, it is also possible to use an air diffuser type fluidized bed.
【００１８】上記の装置において、乾燥機サイクロン５
２の集塵効率よりも、焼成炉サイクロン２６の集塵効率
を大きくして、系内を循環する微粉量を少なくする必要
がある。このため、焼成炉サイクロン２６としては、例
えば、実公平７−４６３５７号公報に示されているよう
な高効率サイクロン（コマ型サイクロン）を用いること
が好ましい。この高効率サイクロンは、図３に示すよう
に、上側部に接線方向に排ガスを導入する排ガス導入口
７２を有するとともに、上面中央部に排ガス排出管７４
を有する円筒胴体７６の下部に、略逆円錐胴体７８を連
設し、この略逆円錐胴体７８の下部に拡大壁部８０を連
設し、さらに、この拡大壁部８０に略逆円錐胴部８２を
連設し、略逆円錐胴体７８の下端部内径Ｄ１と排ガス排
出管７４の内径ｄがＤ１≧ｄの関係を有し、円筒胴体７
６の内径Ｄと拡大壁部８０の下端部内径Ｄ２との間にＤ
２＝（０．８〜１．０）×Ｄの関係を有するように構成
されたものである。このような構造のサイクロンを使用
することにより、５〜１０μm 程度以上の生石灰微粉を
効率よく捕集することができる。In the above apparatus, the dryer cyclone 5
It is necessary to make the dust collection efficiency of the firing furnace cyclone 26 larger than the dust collection efficiency of No. 2 and reduce the amount of fine powder circulating in the system. For this reason, as the firing furnace cyclone 26, for example, it is preferable to use a high-efficiency cyclone (coma-type cyclone) as disclosed in Japanese Utility Model Publication No. 7-46357. As shown in FIG. 3, the high-efficiency cyclone has an exhaust gas inlet 72 for introducing exhaust gas in a tangential direction at an upper part, and an exhaust gas discharge pipe 74 at a central part of an upper surface.
A substantially inverted conical body 78 is continuously connected to a lower portion of the cylindrical body 76 having the following. An enlarged wall portion 80 is continuously connected to a lower portion of the substantially inverted conical body 78. Further, the substantially inverted conical body portion is connected to the enlarged wall portion 80. 82, the inner diameter D1 of the lower end of the substantially inverted conical body 78 and the inner diameter d of the exhaust gas discharge pipe 74 have a relationship of D1 ≧ d, and the cylindrical body 7
6 between the inner diameter D of the inner wall 6 and the inner diameter D2 of the lower end of the enlarged wall 80.
2 = (0.8 to 1.0) × D. By using a cyclone having such a structure, quicklime fine powder of about 5 to 10 μm or more can be efficiently collected.
【００１９】つぎに本発明の作用について説明する。上
記のように構成された焼成装置において、流動層乾燥機
１０の原料投入管１８に、一例として水分３５〜４０％
を含む石灰泥が原料として投入され乾燥される。流動媒
体及び造粒された乾燥原料が抜出管２０、気密排出手段
５８を備えた導管８４及び導入管２２を介して流動層焼
成炉１４の流動層１６に導入される。なお、抜出管２０
をオーバーフロー排出ではなく、流動層底部に接続する
ことも可能である。流動層乾燥機１０からの排ガスは乾
燥機サイクロン５２に導入され、排ガスから乾燥された
微粉原料が分離・捕集され、捕集された微粉原料は気密
排出手段６０を備えた導管５４からエジェクター５６に
供給され、吹込空気（圧縮空気）により流動層焼成炉１
４の流動層１６内に吹き込まれる。このように、微粉原
料は流動層１６内に吹き込まれるので、流動層１６内に
おける微粉原料の滞留時間を気相部に吹き込む場合に比
べて長くすることができ、このため、十分焼成すること
ができる。Next, the operation of the present invention will be described. In the sintering apparatus configured as described above, for example, the raw material input pipe 18 of the fluidized bed dryer 10 has a water content of 35 to 40%.
Is added as a raw material and dried. The fluidized medium and the granulated dry raw material are introduced into the fluidized bed 16 of the fluidized-bed baking furnace 14 through the extraction pipe 20, the conduit 84 having the airtight discharge means 58, and the introduction pipe 22. The extraction tube 20
Can be connected to the bottom of the fluidized bed instead of overflow discharge. Exhaust gas from the fluidized bed dryer 10 is introduced into a dryer cyclone 52, and the fine powder material dried from the exhaust gas is separated and collected. The collected fine powder material is discharged from a conduit 54 having an airtight discharge means 60 to an ejector 56. Fluidized-bed firing furnace 1 by blowing air (compressed air)
4 into the fluidized bed 16. As described above, since the fine powder raw material is blown into the fluidized bed 16, the residence time of the fine powder raw material in the fluidized bed 16 can be made longer than in the case where the fine powder raw material is blown into the gas phase portion. it can.
【００２０】流動層焼成炉１４からのＣＯ2 リッチの高
温（例えば１０００℃前後）の排ガスは焼成炉サイクロ
ン２６に導入され、排ガスから焼成生石灰微粉が分離・
捕集され、捕集された生石灰微粉は気流式クーラ３０に
投入され冷却用空気と接触して冷却され、ＣａＯ微粉の
焼成品となる。焼成炉サイクロン２６からの高温（例え
ば１０００℃前後）の排ガスは流動層乾燥機１０の風箱
３８に導入され流動化ガス兼乾燥用ガスとして用いられ
るとともに熱回収される。このガスは流動層１２内で高
水分の石灰泥を乾燥させ、多量の水の蒸発潜熱により３
４０℃前後まで短時間で冷却される。The CO 2 -rich high-temperature (for example, around 1000 ° C.) exhaust gas from the fluidized-bed firing furnace 14 is introduced into a firing furnace cyclone 26, where calcined quicklime is separated from the exhaust gas.
The collected quicklime fines are charged into the air-flow cooler 30 and contacted with the cooling air to be cooled, thereby obtaining a calcined product of the CaO fines. Exhaust gas at a high temperature (for example, around 1000 ° C.) from the baking furnace cyclone 26 is introduced into a wind box 38 of the fluidized bed dryer 10 and used as a fluidizing gas and a drying gas, and heat is recovered. This gas dries high-moisture lime mud in the fluidized bed 12 and generates a large amount of water due to latent heat of vaporization.
It is cooled in a short time to around 40 ° C.
【００２１】流動層乾燥機１０、流動層焼成炉１４の両
方又はいずれかに、定常粉化相当量の流動媒体が原料と
ともに、又は別々に投入・補給される。なお、流動媒体
の平均粒径は数mm、すなわち、０．５〜６mm、望ましく
は１〜３mmである。気流式クーラ３０の下段サイクロン
３２ａに接続された気流導管８６には冷却用空気が供給
され、この導管８６に上段サイクロン３２ｂで捕集され
た生石灰微粉が気密排出手段６４を備えた導管８８を介
して導入される。下段サイクロン３２ａと上段サイクロ
ン３２ｂとを接続する熱風ダクト３４には、焼成炉サイ
クロン２６で捕集された生石灰微粉が導入され、上段サ
イクロン４２からの熱風（例えば３１０℃前後）は熱風
導入ダクト４６を経て流動層焼成炉１４の風箱４４に導
入され、流動化兼燃焼用空気として回収される。なお、
このガスは流動層１６内で直ちに１０００℃前後の高温
ガスとなる。なお、焼成炉１４において造粒物が多い場
合は、抜出し装置７１を設けることが必要で、焼成炉へ
の流動媒体の補給は不要となる。An amount of fluidized medium corresponding to steady powdering is supplied to and / or supplied to the fluidized-bed dryer 10 and / or the fluidized-bed baking furnace 14 together with or separately from the raw materials. The average particle size of the fluid medium is several mm, that is, 0.5 to 6 mm, and preferably 1 to 3 mm. Cooling air is supplied to an airflow conduit 86 connected to the lower cyclone 32 a of the airflow cooler 30, and quicklime fine powder collected by the upper cyclone 32 b is supplied to the conduit 86 via a conduit 88 provided with an airtight discharge means 64. Is introduced. Hot lime fine powder collected in the firing furnace cyclone 26 is introduced into the hot air duct 34 connecting the lower cyclone 32a and the upper cyclone 32b, and the hot air (for example, around 310 ° C.) from the upper cyclone 42 flows through the hot air introduction duct 46. After that, it is introduced into the wind box 44 of the fluidized-bed firing furnace 14 and collected as air for fluidization and combustion. In addition,
This gas immediately becomes a high temperature gas of about 1000 ° C. in the fluidized bed 16. When the granulated material is large in the firing furnace 14, it is necessary to provide the extraction device 71, and it is not necessary to supply the fluidized medium to the firing furnace.
【００２２】図２は本発明の実施の第２形態による石灰
泥の焼成装置を示している。本実施形態は、流動層焼成
炉１４の流動層１６へ流動媒体及び造粒された乾燥原料
を供給する導入管２２ａの先端（例えば下端）を、流動
層１６内に位置するように設けて、サイクロンで捕集さ
れた乾燥微粉原料を流動媒体等とともに流動層１６内に
供給し滞留時間を長くして十分焼成できるようにしたも
のである。この場合、微粉原料導入管５４を導入管２２
ａに接続することにより、エジェクターは不要となる。
なお、エジェクターを設ける構成とすることも勿論可能
である。他の構成及び作用は実施の第１形態の場合と同
様である。FIG. 2 shows a lime mud firing apparatus according to a second embodiment of the present invention. In the present embodiment, the leading end (for example, the lower end) of the introduction pipe 22a that supplies the fluidized medium and the granulated dry raw material to the fluidized bed 16 of the fluidized bed baking furnace 14 is provided so as to be located in the fluidized bed 16. The dry fine powder raw material collected by the cyclone is supplied into the fluidized bed 16 together with the fluidized medium and the like, so that the residence time is lengthened to enable sufficient firing. In this case, the fine powder raw material introduction pipe 54 is connected to the introduction pipe 22.
By connecting to a, an ejector becomes unnecessary.
In addition, it is of course possible to adopt a configuration in which an ejector is provided. Other configurations and operations are the same as those in the first embodiment.
【００２３】図４は本発明の実施の第３形態による石灰
泥の焼成装置を示している。本実施形態は、気流式クー
ラ３０ａを１段のサイクロン３２で構成したものであ
る。この場合、焼成炉サイクロン２６で捕集された生石
灰微粉は、気流式クーラ３０ａの気流導管８６に投入さ
れる。他の構成及び作用は実施の第１形態の場合と同様
である。FIG. 4 shows a lime mud firing apparatus according to a third embodiment of the present invention. In this embodiment, the air-flow type cooler 30a is configured by a single-stage cyclone 32. In this case, the quicklime fine powder collected in the firing furnace cyclone 26 is introduced into the airflow conduit 86 of the airflow cooler 30a. Other configurations and operations are the same as those in the first embodiment.
【００２４】図５は本発明の実施の第４形態による石灰
泥の焼成装置を示している。本実施形態は、導入管２２
ａの先端（例えば下端）を、流動層１６内に位置するよ
うに設け、かつ、気流式クーラ３０ａを１段のサイクロ
ン３２で構成したものである。他の構成及び作用は実施
の第２、３形態の場合と同様である。FIG. 5 shows a lime mud firing apparatus according to a fourth embodiment of the present invention. In the present embodiment, the introduction pipe 22
The front end (for example, the lower end) of a is provided so as to be located in the fluidized bed 16, and the air-flow type cooler 30 a is constituted by a single-stage cyclone 32. Other configurations and operations are the same as those of the second and third embodiments.
【００２５】[0025]
【発明の効果】本発明は上記のように構成されているの
で、つぎのような効果を奏する。 （１） 粒状の流動媒体で乾燥機及び焼成炉の流動層を
形成するので、乾燥機及び焼成炉を小型化することがで
き、このため、装置全体を小型化、コンパクト化するこ
とができる。 （２） エジェクター等の微粉原料導入手段で微粉原料
を焼成炉の流動層内に吹き込む場合は、微粉でも、短時
間で飛散することなく、比較的長時間層内に滞留し十分
焼成することができる。 （３） 流動層乾燥機には高水分の石灰泥を、予備乾燥
や予備脱水を行うことなく直接投入することができるの
で、装置が簡略化される。 （４） 流動媒体としては粉化が少ないものを用いるの
が好ましいが、石灰石を用いる場合は粉化相当量を補給
することにより、焼成品の品質に影響することなく流動
層を維持することができる。 （５） きわめて簡単な装置であるので、容易に微粉の
内部循環を少なくすることができ、また、８００〜５５
０℃の再炭酸化温度領域、すなわち、付着温度領域を避
けることができる。 （６） 焼成炉サイクロンとしてコマ型サイクロン等の
高効率サイクロンを用いる場合は、排ガスダスト量を少
なくすることができる。 （７） 焼成炉排ガスの顕熱を効率良く熱回収するの
で、熱消費を低減することができる。さらに、気流式ク
ーラからの熱風を流動層焼成炉の風箱に導入する場合
は、焼成品の顕熱を効率良く熱回収するので、熱消費を
より低減することができる。 （８） 流動媒体及び造粒された乾燥原料の導入管の先
端を流動層焼成炉の流動層内に挿入・位置させ、この導
入管に微粉原料導入管を接続する場合は、エジェクター
等が不要になる。As described above, the present invention has the following effects. (1) Since the fluidized bed of the dryer and the baking furnace is formed with the granular fluid medium, the dryer and the baking furnace can be reduced in size, and thus the entire apparatus can be reduced in size and size. (2) When the fine powder raw material is blown into the fluidized bed of the firing furnace by means of a fine powder raw material introduction means such as an ejector, even the fine powder can stay in the bed for a relatively long time without being scattered in a short time and sufficiently fired. it can. (3) Since the lime mud having a high moisture content can be directly supplied to the fluidized bed dryer without performing preliminary drying or preliminary dehydration, the apparatus is simplified. (4) As the fluid medium, it is preferable to use one with less powdering, but when using limestone, it is possible to maintain a fluidized bed without affecting the quality of the fired product by replenishing a substantial amount of powdering. it can. (5) Since it is a very simple device, the internal circulation of fine powder can be easily reduced, and 800-55
The 0 ° C. recarbonation temperature range, ie, the deposition temperature range, can be avoided. (6) When a high-efficiency cyclone such as a top cyclone is used as the firing furnace cyclone, the amount of exhaust gas dust can be reduced. (7) Since the sensible heat of the furnace exhaust gas is efficiently recovered, the heat consumption can be reduced. Furthermore, when the hot air from the air-flow cooler is introduced into the wind box of the fluidized-bed firing furnace, the sensible heat of the fired product is efficiently recovered, so that the heat consumption can be further reduced. (8) When the leading end of the fluid medium and the granulated dry raw material introduction tube is inserted and positioned in the fluidized bed of the fluidized bed firing furnace, an ejector is not required when connecting the fine powder material introduction tube to this introduction tube. become.
【図１】本発明の実施の第１形態による石灰泥の焼成装
置の概略構成図である。FIG. 1 is a schematic configuration diagram of a lime mud firing apparatus according to a first embodiment of the present invention.
【図２】本発明の実施の第２形態による石灰泥の焼成装
置の概略構成図である。FIG. 2 is a schematic configuration diagram of a lime mud firing apparatus according to a second embodiment of the present invention.
【図３】焼成炉サイクロンの一例を示す立面説明図であ
る。FIG. 3 is an elevation explanatory view showing an example of a firing furnace cyclone.
【図４】本発明の実施の第３形態による石灰泥の焼成装
置の概略構成図である。FIG. 4 is a schematic configuration diagram of a lime mud firing apparatus according to a third embodiment of the present invention.
【図５】本発明の実施の第４形態による石灰泥の焼成装
置の概略構成図である。FIG. 5 is a schematic configuration diagram of a lime mud firing apparatus according to a fourth embodiment of the present invention.
１０ 流動層乾燥機 １２、１６ 流動層 １４ 流動層焼成炉 １８ 原料投入管 ２０ 抜出管 ２２、２２ａ 導入管 ２４、３６、５０ 排ガス出口 ２６ 焼成炉サイクロン ２８ 焼成生石灰微粉導入管 ３０、３０ａ 気流式クーラ ３２、３２ａ、３２ｂ サイクロン ３４ 熱風ダクト ３８、４４ 風箱 ４０ 排ガス導入ダクト ４２ 熱風出口 ４６ 熱風導入ダクト ４８ バーナ ５２ 乾燥機サイクロン ５４ 微粉原料導入管 ５６ エジェクター ５８、６０、６２、６４、６６ 気密排出手段 ６８、７０ ガス分散手段 ７１ 抜出し装置 ７２ 排ガス導入口 ７４ 排ガス排出管 ７６ 円筒胴体 ７８ 略逆円錐胴体 ８０ 拡大壁部 ８２ 略逆円錐胴部 ８４、８８ 導管 ８６ 気流導管 DESCRIPTION OF SYMBOLS 10 Fluidized bed dryer 12, 16 Fluidized bed 14 Fluidized bed baking furnace 18 Raw material input pipe 20 Extraction pipe 22, 22a Introducing pipe 24, 36, 50 Exhaust gas outlet 26 Firing furnace cyclone 28 Firing quick lime fine powder introduction pipe 30, 30a Air flow type Cooler 32, 32a, 32b Cyclone 34 Hot air duct 38, 44 Wind box 40 Exhaust gas introduction duct 42 Hot air outlet 46 Hot air introduction duct 48 Burner 52 Dryer cyclone 54 Fine powder material introduction pipe 56 Ejector 58, 60, 62, 64, 66 Airtight discharge Means 68, 70 Gas dispersing means 71 Extraction device 72 Exhaust gas inlet 74 Exhaust gas exhaust pipe 76 Cylindrical body 78 Substantially inverted cone body 80 Enlarged wall section 82 Substantially inverted cone body section 84, 88 Duct 86 Airflow duct
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭58−145815（ＪＰ，Ａ) 特開 平８−247426（ＪＰ，Ａ) 特開 平10−152353（ＪＰ，Ａ) 特開 平10−148474（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C04B 2/12 C02F 11/00 ──────────────────────────────────────────────────続 き Continuation of front page (56) References JP-A-58-145815 (JP, A) JP-A-8-247426 (JP, A) JP-A-10-152353 (JP, A) JP-A-10-108 148474 (JP, A) (58) Field surveyed (Int. Cl. 7 , DB name) C04B 2/12 C02F 11/00
Claims (14)
動層乾燥機に石灰泥を原料として投入し乾燥させた後、
乾燥排ガスから捕捉された乾燥微粉原料を主原料として
粒状の流動媒体で流動層が形成される流動層焼成炉に導
入し焼成して生石灰微粉とし、流動層焼成炉からの排ガ
スを焼成炉サイクロンに導入して排ガスから焼成生石灰
微粉を分離・捕集し、捕集された生石灰微粉を気流式ク
ーラに投入し冷却用空気と接触させて冷却し、焼成炉サ
イクロンからの排ガスを流動層乾燥機に導入し流動化ガ
ス兼乾燥用ガスとして用いるとともに熱回収することを
特徴とする石灰泥の焼成方法。Claims 1. A lime mud as a raw material is dried in a fluidized bed dryer in which a fluidized bed is formed with a granular fluidized medium, and dried.
The dried fine powder raw material captured from the dried exhaust gas is introduced into a fluidized bed firing furnace in which a fluidized bed is formed using a granular fluidized medium as the main raw material, and calcined into quick lime fine powder, and the exhaust gas from the fluidized bed firing furnace is converted into a firing furnace cyclone. The calcined quick lime fine powder is separated and collected from the exhaust gas, and the collected quick lime fine powder is introduced into an air flow cooler, brought into contact with cooling air and cooled, and the exhaust gas from the firing furnace cyclone is discharged into a fluidized bed dryer. A calcining method for lime mud, which is introduced, used as a fluidizing gas and a drying gas, and recovers heat.
れた乾燥原料、並びに乾燥排ガスから捕捉された乾燥微
粉原料を流動層焼成炉の流動層内に導入する請求項１記
載の石灰泥の焼成方法。2. The lime mud according to claim 1, wherein the fluidized medium and the granulated dry raw material from the fluidized bed dryer and the dry fine powder raw material captured from the dried exhaust gas are introduced into the fluidized bed of the fluidized bed firing furnace. Firing method.
器に導入して排ガスから乾燥された微粉原料を分離・捕
集し、捕集された微粉原料を流動層焼成炉の流動層内に
供給する請求項１又は２記載の石灰泥の焼成方法。3. The exhaust gas from the fluidized bed dryer is introduced into a dryer dust collector to separate and collect the dried fine powder raw material from the exhaust gas, and the collected fine powder raw material is fluidized in a fluidized bed firing furnace. The calcination method for lime mud according to claim 1 or 2, wherein the lime mud is supplied to the inside.
ジェクターにより流動層焼成炉の流動層内に吹き込む請
求項３記載の石灰泥の焼成方法。4. The lime mud firing method according to claim 3, wherein the fine powder raw material collected by the dryer dust collector is blown into the fluidized bed of the fluidized bed firing furnace by an ejector.
機又は／及び流動層焼成炉に投入する請求項１〜４のい
ずれかに記載の石灰泥の焼成方法。5. The method for calcining lime mud according to claim 1, wherein an amount of fluidized medium equivalent to steady powdering is introduced into a fluidized bed dryer and / or a fluidized bed calcining furnace.
の流動媒体である請求項１〜５のいずれかに記載の石灰
泥の焼成方法。6. The granular fluid medium has an average particle size of 0.5 to 6 mm.
The calcination method for lime mud according to claim 1, which is a fluidized medium.
ロンで構成され、冷却後の熱風を流動層焼成炉に導入し
流動化兼燃焼用空気として用いる請求項１〜６のいずれ
かに記載の石灰泥の焼成方法。7. The air-flow cooler comprises one or more stages of cyclones, and the cooled hot air is introduced into a fluidized-bed firing furnace and used as air for fluidization and combustion. Lime mud firing method.
めの、粒状の流動媒体で流動層が形成される流動層乾燥
機と、 流動層乾燥機からの排ガスから乾燥微粉原料を捕集する
ための乾燥機集塵器と、 乾燥機集塵器からの乾燥微粉原料を導入して焼成するた
めの、粒状の流動媒体で流動層が形成される流動層焼成
炉と、 流動層焼成炉からの排ガスを導入して排ガスから焼成生
石灰微粉を分離・捕集するための焼成炉サイクロンと、 焼成炉サイクロンからの焼成生石灰微粉を冷却するため
の気流式クーラと、 焼成炉サイクロンの排ガス出口と流動層乾燥機の風箱と
を接続する排ガス導入ダクトとを備えたことを特徴とす
る石灰泥の焼成装置。8. A fluidized bed dryer in which a fluidized bed is formed with a granular fluidized medium for charging and drying lime mud as a raw material, and for collecting a dry fine powder raw material from exhaust gas from the fluidized bed dryer. A dryer dust collector, a fluidized bed firing furnace in which a fluidized bed is formed with a granular fluidized medium for introducing and firing the dry fine powder raw material from the dryer dust collector, Firing furnace cyclone for separating and collecting calcined quick lime fines from exhaust gas by introducing flue gas, air flow cooler for cooling calcined quick lime fines from calcining furnace cyclone, flue gas outlet and fluidized bed of calciner cyclone An apparatus for firing lime mud, comprising: an exhaust gas introduction duct connecting a wind box of a dryer.
位置するように、流動媒体及び造粒された乾燥原料の導
入管が設けられた請求項８記載の石灰泥の焼成装置。9. The tip is inserted into a fluidized bed of a fluidized bed firing furnace.
9. The lime mud baking apparatus according to claim 8, wherein an inlet pipe for the fluidized medium and the granulated dry raw material is provided so as to be located.
れた微粉原料を分離・捕集するための乾燥機集塵器と、 乾燥機集塵器からの乾燥された微粉原料を流動層焼成炉
の流動層内に供給するための微粉原料導入手段とを備え
た請求項８又は９記載の石灰泥の焼成装置。10. A dryer dust collector for separating and collecting a dried fine powder material from an exhaust gas from a fluidized bed dryer, and a fluidized bed firing furnace for drying the dried fine powder material from the dryer dust collector. 10. The lime mud firing apparatus according to claim 8, further comprising a fine powder raw material introduction means for supplying the lime mud to the fluidized bed.
る請求項１０記載の石灰泥の焼成装置。11. The lime mud firing apparatus according to claim 10, wherein the fine powder raw material introducing means is an ejector.
機の流動層が、平均粒径０．５〜６mmの流動媒体で形成
されている請求項８〜１１のいずれかに記載の石灰泥の
焼成装置。12. The lime according to claim 8, wherein the fluidized bed of the fluidized-bed baking furnace and the fluidized bed of the fluidized-bed dryer are formed of a fluidized medium having an average particle size of 0.5 to 6 mm. Mud firing equipment.
向に排ガスを導入する排ガス導入口を有するとともに、
上面中央部に排ガス排出管を有する円筒胴体の下部に、
略逆円錐胴体を連設し、この略逆円錐胴体の下部に拡大
壁部を連設し、さらに、この拡大壁部に略逆円錐胴部を
連設し、略逆円錐胴体の下端部内径Ｄ１と排ガス排出管
の内径ｄがＤ１≧ｄの関係を有し、円筒胴体の内径Ｄと
拡大壁部の下端部内径Ｄ２との間にＤ２＝（０．８〜
１．０）×Ｄの関係を有するようにした高効率サイクロ
ンである請求項８〜１２のいずれかに記載の石灰泥の焼
成装置。13. A firing furnace cyclone has an exhaust gas inlet for introducing exhaust gas in a tangential direction on an upper portion thereof,
In the lower part of the cylindrical body having an exhaust gas discharge pipe in the center of the upper surface,
A substantially inverted conical body is continuously provided, an enlarged wall portion is continuously provided at a lower portion of the substantially inverted conical body, and a substantially inverted conical body portion is further continuously provided on the enlarged wall portion. D1 and the inner diameter d of the exhaust gas discharge pipe have a relationship of D1 ≧ d, and D2 = (0.8 to 0.8) between the inner diameter D of the cylindrical body and the lower end inner diameter D2 of the enlarged wall portion.
1.0) The apparatus for firing lime mud according to any one of claims 8 to 12, wherein the apparatus is a high-efficiency cyclone having a relationship of × D.
イクロンで構成され、最上段のサイクロンの熱風出口と
流動層焼成炉の風箱とが熱風導入ダクトを介して接続さ
れている請求項８〜１３のいずれかに記載の石灰泥の焼
成装置。14. The air-flow cooler is constituted by one or more stages of cyclones, and the hot air outlet of the uppermost cyclone and the wind box of the fluidized bed firing furnace are connected via a hot air introduction duct. A lime mud firing apparatus according to any one of 8 to 13.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11060961A JP3032198B1 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for firing lime mud |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11060961A JP3032198B1 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for firing lime mud |
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| Publication Number | Publication Date |
|---|---|
| JP3032198B1 true JP3032198B1 (en) | 2000-04-10 |
| JP2000256045A JP2000256045A (en) | 2000-09-19 |
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|---|---|---|---|
| JP11060961A Expired - Fee Related JP3032198B1 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for firing lime mud |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107311478A (en) * | 2017-08-16 | 2017-11-03 | 杨泽荣 | White clay reclaims the energy saving and environment friendly recovery method of comprehensive utilization |
| CN108358474A (en) * | 2018-05-23 | 2018-08-03 | 绵竹市拱星氧化钙厂 | It uninterruptedly blows the batch mixing formula limekiln economized on coal |
-
1999
- 1999-03-09 JP JP11060961A patent/JP3032198B1/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107311478A (en) * | 2017-08-16 | 2017-11-03 | 杨泽荣 | White clay reclaims the energy saving and environment friendly recovery method of comprehensive utilization |
| CN107311478B (en) * | 2017-08-16 | 2020-03-20 | 杨泽荣 | Energy-saving environment-friendly recovery method for comprehensively recycling white mud |
| CN108358474A (en) * | 2018-05-23 | 2018-08-03 | 绵竹市拱星氧化钙厂 | It uninterruptedly blows the batch mixing formula limekiln economized on coal |
| CN108358474B (en) * | 2018-05-23 | 2023-07-18 | 四川马氏窑技术发展有限公司 | Continuous air supply coal-saving mixing lime kiln |
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| Publication number | Publication date |
|---|---|
| JP2000256045A (en) | 2000-09-19 |
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