JP2001294856A - Method for manufacturing ground improving material and equipment for the same - Google Patents
Method for manufacturing ground improving material and equipment for the sameInfo
- Publication number
- JP2001294856A JP2001294856A JP2000111657A JP2000111657A JP2001294856A JP 2001294856 A JP2001294856 A JP 2001294856A JP 2000111657 A JP2000111657 A JP 2000111657A JP 2000111657 A JP2000111657 A JP 2000111657A JP 2001294856 A JP2001294856 A JP 2001294856A
- Authority
- JP
- Japan
- Prior art keywords
- cyclone
- fluidized bed
- bed furnace
- exhaust gas
- kiln
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/82—Recycling of waste of electrical or electronic equipment [WEEE]
Landscapes
- Treatment Of Sludge (AREA)
- Curing Cements, Concrete, And Artificial Stone (AREA)
- Soil Conditioners And Soil-Stabilizing Materials (AREA)
- Consolidation Of Soil By Introduction Of Solidifying Substances Into Soil (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
【0001】[0001]
【発明の属する技術分野】本発明は、下水汚泥、産廃汚
泥等の脱水ケーキに生石灰、消石灰等の石灰を混合して
脱水乾燥後造粒し、流動層炉で乾燥、有機物の焼却、消
石灰の分解などの熱処理した後、ロータリキルンで焼成
して地盤改良材を製造する方法及び装置、詳しくは、サ
イクロン内壁面を再炭酸化温度以下に冷却することによ
り、ダストの付着を確実に防止することができる地盤改
良材の製造方法及び装置に関するものである。TECHNICAL FIELD The present invention relates to a dewatered cake of sewage sludge or industrial waste sludge mixed with lime such as quicklime or slaked lime, dehydrated and dried, granulated, dried in a fluidized bed furnace, incinerated with organic matter, and slaked lime. Method and apparatus for producing ground improvement material by heat treatment such as decomposition and then firing in a rotary kiln, in particular, to reliably prevent dust adhesion by cooling the inner wall of cyclone to recarbonation temperature or lower The present invention relates to a method and an apparatus for manufacturing a ground improvement material that can be used as a ground improvement material.
【0002】[0002]
【従来の技術】下水汚泥、産廃汚泥等は、脱水乾燥され
た後、流動層炉又はロータリキルン等で汚泥中の有機物
を焼却して埋立処分されていたが、近年、焼成、乾留等
の処理を行う種々のリサイクル方法が開発されつつあ
る。従来、汚泥の脱水乾燥焼却方法及び装置として、例
えば特開平6−15297号公報には、汚泥と生石灰と
を混合して汚泥の脱水・乾燥を行う脱水乾燥工程と、生
成した固形分を流動層炉又は気流炉で加熱して汚泥中の
有機物を焼却するとともに有機物の燃焼熱により消石灰
を焼成して生石灰に再生する焼却再生工程からなる汚泥
の脱水乾燥焼却システムが開示されている。2. Description of the Related Art Sewage sludge, industrial waste sludge, etc. have been dewatered and dried and then incinerated in a fluidized bed furnace or a rotary kiln to incinerate organic matter in the sludge and landfilled. Various recycling methods for performing the above are being developed. Conventionally, as a method and an apparatus for dehydrating, drying and incinerating sludge, for example, Japanese Patent Application Laid-Open No. 6-15297 discloses a dehydration and drying step of mixing sludge and quicklime to dehydrate and dry sludge; A dewatering / drying / incineration system for sludge comprising an incineration / regeneration step of heating in a furnace or an airflow furnace to incinerate organic matter in the sludge and burning slaked lime by the heat of combustion of the organic matter to regenerate into quicklime is disclosed.
【0003】また、特開平10−237852号公報に
は、下水汚泥等の有機汚泥と生石灰、消石灰等の石灰類
とを混合し、その混合物を1〜10mmに造粒した原料を
ロータリキルンで800〜1000℃の温度で乾燥・脱
水・有機物焼却・消石灰焼成して地盤改良材を製造する
方法が開示されている。JP-A-10-237852 discloses an organic sludge such as sewage sludge mixed with lime such as quicklime and slaked lime, and granulating the mixture to a size of 1 to 10 mm. There is disclosed a method for producing a ground improvement material by drying, dehydrating, burning organic matter, and firing slaked lime at a temperature of ~ 1000 ° C.
【0004】[0004]
【発明が解決しようとする課題】上記の特開平6−15
297号公報記載の汚泥の脱水乾燥焼却システムにおい
ては、流動層炉又は気流炉での滞留時間が短いため十分
焼成できず、地盤改良材としての性能を満足させること
ができない。また、生石灰の微粉が再炭酸化及び再水酸
化して装置内部に付着し、長期連続運転を行うことがで
きないという問題がある。また、特開平10−2378
52号公報記載の地盤改良材の製造方法においては、ロ
ータリキルンは伝熱性能が悪いため、ロータリキルンの
みの乾焼・脱水・焼却・焼成では装置が大型化し、ま
た、キルン排ガス中のダストが熱交換器に付着して連続
運転を阻害し、付着物の除去に多大の労力を要する問題
がある。The above-mentioned Japanese Patent Application Laid-Open No. 6-15 / 1994
In the dewatering / drying / incineration system for sludge described in Japanese Patent No. 297, the residence time in a fluidized bed furnace or an airflow furnace is short, so that it cannot be sufficiently fired and the performance as a ground improvement material cannot be satisfied. In addition, there is a problem that the fine powder of quicklime is re-carbonated and re-hydroxylated and adheres to the inside of the apparatus, so that long-term continuous operation cannot be performed. Also, Japanese Patent Application Laid-Open No. 10-2378
In the method for producing a ground improvement material described in JP-A-52-52, since the rotary kiln has poor heat transfer performance, the apparatus becomes large in dry baking, dehydration, incineration, and baking of the rotary kiln alone, and dust in the kiln exhaust gas is reduced. There is a problem that it adheres to the heat exchanger, hinders continuous operation, and requires a great deal of labor to remove the adhered matter.
【0005】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、高伝熱性能の流動層炉で造粒物
(原料)の乾燥、乾燥・予熱又は乾燥・有機物焼却・消
石灰焼成(分解)を行わせることにより、ロータリキル
ンを小型化することができ、性能の良い地盤改良材を製
造することができるとともに、サイクロン内壁面へのダ
スト付着を確実に防止することができる方法及び装置を
提供することにある。また、本発明の目的は、造粒物
(原料)の製造工場で発生する臭気を熱交換器で流動層
炉サイクロン排ガスと熱交換させることにより加熱した
後、ロータリキルンの燃焼用空気としてロータリキルン
に、並びに流動層炉の風箱及び/又はフリーボード部に
吹き込むことにより、臭気処理をも確実に行うことがで
きる地盤改良材の製造方法及び装置を提供することにあ
る。The present invention has been made in view of the above points, and an object of the present invention is to dry, dry, preheat or dry, incinerate, incinerate, and slak lime a granulated material (raw material) in a fluidized-bed furnace having high heat transfer performance. By performing firing (decomposition), the rotary kiln can be miniaturized, a ground improvement material with good performance can be manufactured, and dust adhesion to the inner wall surface of the cyclone can be reliably prevented. And a device. Another object of the present invention is to heat the odor generated in a granule (raw material) manufacturing plant by exchanging heat with a cyclone exhaust gas in a fluidized bed furnace using a heat exchanger, and then use the rotary kiln as combustion air for the rotary kiln. Another object of the present invention is to provide a method and an apparatus for producing a soil improvement material that can reliably perform odor treatment by blowing air into a wind box and / or a freeboard portion of a fluidized bed furnace.
【0006】[0006]
【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、本発明の地盤改良材の製造方法は、汚泥脱水ケー
キに石灰を混合撹拌し造粒した造粒物を、下流のロータ
リキルンの排ガスを流動化ガスとする流動層炉に投入し
造粒物を流動媒体として乾燥、乾燥・予熱又は乾燥・有
機物焼却・消石灰焼成(分解)を行った後、流動層炉か
らの粒状物をロータリキルンに導入して焼成し、焼成粒
状物(焼却灰とCaOの混合物)を流動層クーラに導入
して冷却する方法であって、流動層炉の排ガスを一部又
は全部がジャケット構造の流動層炉サイクロンに導入し
てダストを捕集するとともに、ジャケットに冷却用流体
を導入し間接的冷却して該サイクロンを冷却するように
構成されている(図1参照)。冷却用流体としては、空
気、水等が用いられるが、とくに空気を用いることが好
ましい。In order to achieve the above object, a method for producing a ground improvement material according to the present invention comprises mixing a lime with a sludge dewatered cake, stirring and granulating the sludge dewatered cake with a downstream rotary kiln. Into a fluidized bed furnace using the flue gas of the fluidized gas as a fluidizing gas, and drying, drying and preheating or drying, incineration of organic matter, and calcination of slaked lime (decomposition) using the granulated material as a fluidized medium. This is a method in which the mixture is introduced into a rotary kiln, fired, and fired granules (a mixture of incinerated ash and CaO) are introduced into a fluidized bed cooler for cooling. Dust is collected by being introduced into the layered furnace cyclone, and a cooling fluid is introduced into the jacket to cool the cyclone by indirect cooling (see FIG. 1). As the cooling fluid, air, water, or the like is used, and it is particularly preferable to use air.
【0007】上記の方法において、流動層炉サイクロン
で捕集されたダストをロータリキルンのバーナ近傍に吹
き込み、望ましくはバーナ上方のキルンから吹き込み、
キルン排ガスとともに排出されるまでの間に焼成するよ
うに構成することが好ましい(図1参照)。また、ロー
タリキルンの排ガスを一部又は全部がジャケット構造の
キルンサイクロンに導入してダストを分離するととも
に、ジャケットに冷却用流体を導入し間接冷却して該サ
イクロンを冷却することが好ましい(図1参照)。この
場合も、冷却用流体としては、空気、水等が用いられる
が、とくに空気を用いることが好ましい。In the above method, dust collected in the fluidized-bed furnace cyclone is blown into the vicinity of a burner of the rotary kiln, preferably from a kiln above the burner.
It is preferable that the sintering be carried out before being discharged together with the kiln exhaust gas (see FIG. 1). In addition, it is preferable that the exhaust gas from the rotary kiln is partially or wholly introduced into a kiln cyclone having a jacket structure to separate dust, and that a cooling fluid is introduced into the jacket to cool the cyclone by indirect cooling (FIG. 1). reference). In this case as well, air, water and the like are used as the cooling fluid, but it is particularly preferable to use air.
【0008】サイクロンでは、600〜800℃の温度
域において、排ガスに同伴される焼成された粉体とこの
排ガスに含まれている炭酸ガスとが再炭酸化反応する。
この反応によって炭酸カルシウム等の微粉が生じ、この
温度域におけるサイクロンの内壁には硬質の付着物が生
成し易く、これによって長期間にわたる連続運転ができ
なくなる。このため、流動層炉サイクロン及びキルンサ
イクロンの内壁温度が600℃以下、望ましくは550
℃以下となるように冷却する。In the cyclone, in the temperature range of 600 to 800 ° C., the calcined powder entrained in the exhaust gas and the carbon dioxide contained in the exhaust gas undergo a recarbonation reaction.
Fine powder such as calcium carbonate is generated by this reaction, and hard deposits tend to be formed on the inner wall of the cyclone in this temperature range, whereby continuous operation cannot be performed for a long period of time. Therefore, the inner wall temperature of the fluidized bed furnace cyclone and kiln cyclone is not more than 600 ° C., preferably 550 ° C.
Cool down to below ℃.
【0009】これらの方法において、造粒物の粒径を流
動層操作に適した1〜20mm、望ましくは2〜10mmと
する。また、流動層炉からの排ガスを流動層炉サイクロ
ンで除塵した後、流動層炉サイクロンからの排ガスを熱
交換器に導入して熱回収することが好ましい(図1参
照)。また、熱交換器からの排ガスをバグフィルタに導
入してダストを捕集し、捕集されたダストを流動層炉サ
イクロンからのダストとともに、ロータリキルンのバー
ナ近傍に吹き込むことが好ましい(図1参照)。このよ
うにすれば、歩留まりをさらに大きくすることができ
る。In these methods, the particle size of the granulated product is 1 to 20 mm, preferably 2 to 10 mm, which is suitable for fluidized bed operation. Further, it is preferable that after removing the exhaust gas from the fluidized bed furnace with the cyclone in the fluidized bed furnace, the exhaust gas from the cyclone in the fluidized bed furnace is introduced into a heat exchanger to recover heat (see FIG. 1). Further, it is preferable that the exhaust gas from the heat exchanger is introduced into a bag filter to collect dust, and the collected dust is blown into the vicinity of a burner of a rotary kiln together with dust from a cyclone in a fluidized bed furnace (see FIG. 1). ). By doing so, the yield can be further increased.
【0010】また、造粒物の製造過程、すなわち、原料
製造工場で発生する臭気を熱交換器に導入して昇温し、
加熱臭気をロータリキルンの燃焼用空気として回収する
とともに、余剰の加熱臭気を流動層炉の風箱及び/又は
フリーボード部に吹き込んで脱臭することが好ましい
(図1参照)。加熱臭気を流動層炉の風箱に吹き込むた
めに、ロータリキルンの窯尻へ吹き込むか、キルンサイ
クロンに吹き込むか又は流動層炉の風箱へ直接吹き込む
ようにする。さらに加熱臭気のロータリキルンへの吹込
量、並びに加熱臭気の流動層炉の風箱への吹込量及び/
又は加熱臭気の流動層炉のフリーボード部への吹込量を
夫々調整することができるように構成することが好まし
い。また、キルンサイクロンの集塵効率を流動層炉サイ
クロンの集塵効率より大きくすることが好ましい。この
ように構成することにより、微粉の系内循環がなくな
り、安定運転を継続することが可能となる。[0010] Further, the odor generated in the production process of the granulated material, that is, in the raw material production plant, is introduced into the heat exchanger and the temperature is increased.
It is preferable that the heated odor is recovered as combustion air for the rotary kiln, and the excess heated odor is blown into a wind box and / or a free board portion of the fluidized bed furnace to deodorize (see FIG. 1). In order to blow the heated odor into the wind box of the fluidized bed furnace, it is blown into the bottom of the rotary kiln, into the kiln cyclone, or directly into the wind box of the fluidized bed furnace. Further, the amount of heated odor blown into the rotary kiln, and the amount of heated odor blown into the wind box of the fluidized bed furnace and / or
Alternatively, it is preferable that the amount of the heated odor blown into the freeboard portion of the fluidized bed furnace can be adjusted. Further, it is preferable that the dust collection efficiency of the kiln cyclone is made larger than the dust collection efficiency of the fluidized bed furnace cyclone. With this configuration, the circulation of the fine powder in the system is eliminated, and the stable operation can be continued.
【0011】本発明の地盤改良材の製造装置は、汚泥脱
水ケーキと石灰とを混練し造粒した造粒物を投入し造粒
物を流動媒体として乾燥、乾燥・予熱又は乾燥・有機物
焼却・消石灰焼成を行うための流動層炉と、流動層炉か
らの粒状物を導入して焼成するためのロータリキルン
と、ロータリキルンからの焼成粒状物を冷却するための
流動層クーラと、ロータリキルンの窯尻にロータリーキ
ルン排ガス導管を介して接続された、一部又は全部がジ
ャケット構造に構成されたキルンサイクロンと、キルン
サイクロンと流動層炉の風箱とを接続するためのキルン
サイクロン排ガス導管と、流動層炉からの排ガスを導入
してダストを分離するための、一部又は全部がジャケッ
ト構造に構成された流動層炉サイクロンと、流動層炉サ
イクロンからの排ガスを導入して熱回収するための熱交
換器と、熱交換器からの排ガスを導入してダストを分離
するためのバグフィルタと、流動層炉サイクロンの下部
とロータリキルンのバーナ近傍、望ましくはバーナ上方
のキルンとを接続するサイクロン捕集ダスト導入手段と
を備えたことを特徴としている(図1参照)。The apparatus for manufacturing a soil improvement material according to the present invention is characterized in that a sludge dewatered cake and lime are kneaded and granulated, and the granulated material is used as a fluid medium for drying, drying / preheating or drying / incineration of organic matter. A fluidized bed furnace for performing slaked lime firing, a rotary kiln for introducing and firing the particulate matter from the fluidized bed furnace, a fluidized bed cooler for cooling the fired granular matter from the rotary kiln, and a rotary kiln. A kiln cyclone partially or entirely connected to the kiln butt via a rotary kiln exhaust gas conduit, a kiln cyclone exhaust gas conduit for connecting the kiln cyclone and a wind box of a fluidized bed furnace, A fluidized bed furnace cyclone, part or all of which has a jacket structure, for introducing exhaust gas from a bed furnace and separating dust, and an exhaust gas from the fluidized bed furnace cyclone. A heat exchanger for introducing and recovering heat, a bag filter for introducing exhaust gas from the heat exchanger to separate dust, a lower part of the fluidized bed furnace cyclone and a burner of the rotary kiln, preferably a burner And a cyclone collecting dust introduction means for connecting the kiln to the upper kiln (see FIG. 1).
【0012】上記の装置において、バグフィルタの下部
とサイクロン捕集ダスト導入手段又はロータリキルンの
バーナ近傍、望ましくはバーナ上方のキルンとがバグフ
ィルタ捕集ダスト供給管を介して接続された構成とする
ことが好ましい(図1参照)。また、汚泥脱水ケーキと
石灰とを混練するための混練機と、混練機からの混練物
を造粒するための造粒機を備えるように構成することが
好ましい(図1参照)。In the above apparatus, the lower portion of the bag filter is connected to the cyclone trapping dust introducing means or the kiln near the burner of the rotary kiln, preferably above the burner via a bag filter collecting dust supply pipe. Preferably (see FIG. 1). Further, it is preferable to provide a kneader for kneading the sludge dewatered cake and lime and a granulator for granulating the kneaded material from the kneader (see FIG. 1).
【0013】キルンサイクロン及び流動層炉サイクロン
としては、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
2参照)。The kiln cyclone and the fluidized bed furnace cyclone have an exhaust gas inlet for introducing exhaust gas in a tangential direction at the upper part and a substantially inverted conical body at the lower part of a cylindrical body having an exhaust gas discharge pipe at the center of the 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 exhaust gas discharge pipe are provided. Has a relationship of D1 ≧ d, and a relationship of D2 = (0.8 to 1.0) × D between the inside diameter D of the cylindrical body and the inside diameter D2 of the lower end portion of the enlarged wall portion. It is preferable to use a highly efficient cyclone (see FIG. 2).
【0014】また、熱交換器としては、臭気を通過させ
て加熱するための伝熱管が鉛直に配置された構造のもの
を用いることが好ましい(図3参照)。さらに、流動層
炉のガス分散板として、板体に貫通固定された多数の筒
体の天壁部に、直径が流動媒体径の3倍以下、望ましく
は2倍以下の複数の小孔が設けられた構造のものを用い
ることが好ましい(図4、図5参照)。また、流動層炉
のガス分散板の上側近傍に補助バーナを設けて、立ち上
げ時も臭気の脱臭が可能なように構成することが好まし
い(図1参照)。As the heat exchanger, it is preferable to use a heat exchanger having a structure in which a heat transfer tube for passing an odor and heating it is arranged vertically (see FIG. 3). Further, as a gas dispersion plate for a fluidized bed furnace, a plurality of small holes having a diameter of 3 times or less, preferably 2 times or less the diameter of the fluidized medium are provided on the top wall of a large number of cylindrical bodies fixed through the plate. It is preferable to use one having a given structure (see FIGS. 4 and 5). Further, it is preferable that an auxiliary burner is provided near the upper side of the gas dispersion plate of the fluidized-bed furnace so that the odor can be deodorized even at startup (see FIG. 1).
【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形態による地盤改良材
の製造装置を示している。10は原料(造粒物)製造工
場で、混練機12、造粒機14等を備えている。汚泥脱
水ケーキと石灰類、例えば、生石灰を混練機12に投入
して混練する。生石灰は水分を吸収して消石灰となり、
さらに、発熱反応により汚泥脱水ケーキの水分を蒸発さ
せる。生石灰の割合は混練物の水分が造粒に適した範囲
で、造粒物が流動層で破壊しない強度を有するよう選ば
れる。汚泥脱水ケーキの性状によるが、例えば混練物の
水分は20〜30%である。混練物は造粒機14に導入
されて粒径1〜20mm、望ましくは2〜10mmに造粒さ
れる。なお、造粒機能を備えた混練機を用いることによ
り、混練と造粒とを1台の装置で同時に行うように構成
することも可能である。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 an apparatus for manufacturing a ground improvement material according to a first embodiment of the present invention. Reference numeral 10 denotes a raw material (granulated material) manufacturing plant, which includes a kneader 12, a granulator 14, and the like. The sludge dewatered cake and limes, for example, quick lime, are put into the kneader 12 and kneaded. Quicklime absorbs water and becomes slaked lime,
Further, the moisture of the sludge dewatered cake is evaporated by an exothermic reaction. The proportion of quicklime is selected so that the water content of the kneaded material is suitable for granulation, and the granulated material has a strength that does not break in the fluidized bed. Depending on the properties of the sludge dewatered cake, for example, the water content of the kneaded material is 20 to 30%. The kneaded material is introduced into a granulator 14 and granulated to a particle size of 1 to 20 mm, preferably 2 to 10 mm. In addition, by using a kneading machine having a granulation function, it is also possible to configure so that kneading and granulation are simultaneously performed by one apparatus.
【0016】造粒機14からの造粒物(原料)はホッパ
16に一旦貯留された後、供給機、例えばベルトフィー
ダ18により流動層炉20に供給される。流動層炉20
は、下部に風箱22を備え、風箱上部のガス分散板24
の上側に造粒物が流動媒体となる流動層26が形成され
るように構成されている。この風箱22には、後述のロ
ータリキルン28からの排ガスがロータリキルン排ガス
導管31、キルンサイクロン33及びキルンサイクロン
排ガス導管35を介して導入され、流動化ガスとして用
いられる。The granulated material (raw material) from the granulator 14 is temporarily stored in a hopper 16 and then supplied to a fluidized bed furnace 20 by a feeder, for example, a belt feeder 18. Fluidized bed furnace 20
Is equipped with a wind box 22 at the bottom and a gas distribution plate 24 at the top of the wind box.
A fluidized bed 26 in which the granulated material becomes a fluidized medium is formed on the upper side of the fluidized bed. Exhaust gas from a rotary kiln 28 described later is introduced into the wind box 22 through a rotary kiln exhaust gas conduit 31, a kiln cyclone 33, and a kiln cyclone exhaust gas conduit 35, and is used as a fluidizing gas.
【0017】流動層炉20に投入された造粒物(原料)
は、ロータリキルン28からキルンサイクロン33を経
由して導入された排ガスで流動化して、乾燥、又は乾燥
・予熱、又は乾燥・汚泥中の有機物焼却・消石灰焼成
(分解)が行われる。流動層炉20からの粒状物(処理
物)は気密排出機構、例えばLバルブ32を介してロー
タリキルン28の窯尻34に投入されてロータリキルン
28内で800〜1000℃、望ましくは850〜90
0℃の温度で焼成される。36はキルンバーナである。
ロータリキルン28で焼成された焼成粒状物(焼却灰と
CaOの混合物)は流動層クーラー38に投入されて冷
却用空気により冷却され、排出機、例えばロータリフィ
ーダ40により排出され、輸送機42により製品として
搬出される。流動層クーラ38からの排ガスはバグフィ
ルタ44に導入されてダスト(微細焼成物)が分離され
た後、大気に放出される。捕集されたダストは輸送機4
2により製品の一部として搬出される。46は押込ブロ
ワである。Granules (raw materials) charged into the fluidized bed furnace 20
Is fluidized by exhaust gas introduced from the rotary kiln 28 via the kiln cyclone 33, and drying, or drying and preheating, or drying and incineration of organic matter in sludge and calcination of slaked lime (decomposition) are performed. The granular material (processed material) from the fluidized bed furnace 20 is charged into the kiln butt 34 of the rotary kiln 28 via an airtight discharge mechanism, for example, an L valve 32, and is put into the rotary kiln 28 at 800 to 1000 ° C, preferably 850 to 90 ° C.
It is fired at a temperature of 0 ° C. 36 is a kiln burner.
The fired granules (mixture of incinerated ash and CaO) fired in the rotary kiln 28 are charged into a fluidized bed cooler 38, cooled by cooling air, discharged by a discharger, for example, a rotary feeder 40, and manufactured by a transporter 42. It is carried out as. Exhaust gas from the fluidized bed cooler 38 is introduced into the bag filter 44 to separate dust (finely burned material), and then discharged to the atmosphere. The collected dust is transported 4
2 is carried out as a part of the product. 46 is a pushing blower.
【0018】流動層炉20からの排ガスは流動層炉サイ
クロン48に導入されてダストが捕集され、流動層炉サ
イクロン48からの排ガスは熱交換器に導入される。流
動層炉サイクロン48及び前記キルンサイクロン33と
しては、例えば、実用新案登録第2521152号公報
に示されているような、サイクロンの一部又は全部を冷
却用ジャケット構造、すなわち二重構造とし、このジャ
ケット部分に冷却用流体、例えば空気を供給して冷却す
るようにした構造のサイクロンが用いられる。91、9
3は冷却ファンである。流動層炉サイクロン48及びキ
ルンサイクロン33のジャケット部に冷却用空気を送り
込んでサイクロンの内壁温度が600℃以下、望ましく
は550℃以下となるように冷却することにより、すな
わち、再炭酸化温度以下に冷却することにより、炭酸カ
ルシウム等の微粉の付着を確実に防止することができ、
安定運転が可能となる。Exhaust gas from the fluidized bed furnace 20 is introduced into a fluidized bed furnace cyclone 48 to collect dust, and exhaust gas from the fluidized bed furnace cyclone 48 is introduced into a heat exchanger. As the fluidized bed furnace cyclone 48 and the kiln cyclone 33, for example, as shown in Utility Model Registration No. 252152, a part or all of the cyclone has a cooling jacket structure, that is, a double structure. A cyclone having a structure in which a cooling fluid, for example, air is supplied to the portion to cool the portion is used. 91, 9
3 is a cooling fan. By sending cooling air to the jackets of the fluidized bed furnace cyclone 48 and the kiln cyclone 33 to cool the inner wall temperature of the cyclone to 600 ° C. or lower, preferably 550 ° C. or lower, By cooling, adhesion of fine powder such as calcium carbonate can be reliably prevented,
Stable operation becomes possible.
【0019】前記熱交換器としては、排ガス流に対して
直列に2段に設けることが好ましい。以下、熱交換器を
2段に設けた場合について説明する。高温側の熱交換器
50には原料製造工場10で発生した臭気が臭気ファン
54により導入され、低温側の熱交換器52には冷却用
空気(大気)が押込ブロワ56により導入される。低温
側の熱交換器52からの排ガスは排ガス誘引ファン58
によりバグフィルタ60に導入され、ここでダストが分
離された後、煙突62から排出される。高温側の熱交換
器50で加熱された臭気の一部は、ロータリキルン28
の燃焼用空気としてロータリキルンのバーナ36の近傍
又は直接バーナ36に吹き込まれ、ロータリキルン内で
臭気成分が燃焼又は分解して脱臭される。高温側の熱交
換器50で加熱された臭気の残部は、ロータリキルンの
窯尻34、キルンサイクロン33もしくは流動層炉の風
箱22に吹き込まれるか、又は流動層炉のフリーボード
部64に吹き込まれて脱臭される。The heat exchanger is preferably provided in two stages in series with the exhaust gas flow. Hereinafter, a case where the heat exchanger is provided in two stages will be described. The odor generated in the raw material manufacturing factory 10 is introduced into the heat exchanger 50 on the high temperature side by the odor fan 54, and the cooling air (atmosphere) is introduced into the heat exchanger 52 on the low temperature side by the forced blower 56. Exhaust gas from the low-temperature side heat exchanger 52 is exhausted by an exhaust gas inducing fan 58.
Is introduced into the bag filter 60, where the dust is separated and then discharged from the chimney 62. A part of the odor heated by the heat exchanger 50 on the high temperature side is
The combustion air is blown into the vicinity of or directly into the burner 36 of the rotary kiln, and the odor components are burned or decomposed and deodorized in the rotary kiln. The remainder of the odor heated by the high-temperature side heat exchanger 50 is blown into the kiln butt 34 of the rotary kiln, the kiln cyclone 33 or the wind box 22 of the fluidized bed furnace, or is blown into the free board section 64 of the fluidized bed furnace. It is deodorized.
【0020】熱交換器を2段にする場合は、熱回収量は
減少するが、装置を小型化(伝熱面積が1/3〜1/4
となる)でき、また冷却用空気量を調整することによ
り、排ガス温度を一定にすることができる。このため、
後流のバグフィルタを保護することができ、安定運転を
継続することができるという利点がある。When the heat exchanger has two stages, the amount of heat recovery is reduced, but the size of the apparatus is reduced (the heat transfer area is 1/3 to 1/4).
The exhaust gas temperature can be kept constant by adjusting the amount of cooling air. For this reason,
There is an advantage that the bag filter on the downstream side can be protected and stable operation can be continued.
【0021】高温側の熱交換器50からの加熱臭気の分
岐管66、68、70には、それぞれバルブ72、7
4、76が設けられており、加熱臭気のロータリキルン
28のバーナ36近傍もしくはバーナへの吹込量、並び
に加熱臭気のロータリキルンの窯尻34、キルンサイク
ロン33もしくは流動層炉の風箱22への吹込量及び/
又は加熱臭気の流動層炉のフリーボード部64への吹込
量を、それぞれ調整することができるように構成されて
いる。このように、臭気の吹込配分を調整することがで
きるので、各部の温度をダスト付着のない温度、すなわ
ち、例えば、流動層炉風箱750〜800℃以上、熱交
換器入口550〜600℃以下に設定することができ
る。The branched pipes 66, 68, 70 for the heated odor from the heat exchanger 50 on the high temperature side are provided with valves 72, 7 respectively.
4 and 76 are provided, and the amount of the heated odor blown into or near the burner 36 of the rotary kiln 28, and the amount of the heated odor to the kiln butt 34, kiln cyclone 33 or wind box 22 of the fluidized bed furnace of the rotary kiln. Blow volume and / or
Alternatively, the amount of the heated odor to be blown into the freeboard portion 64 of the fluidized bed furnace can be adjusted. In this way, since the distribution of the odor can be adjusted, the temperature of each part is adjusted to a temperature at which dust is not attached, that is, for example, a fluidized bed furnace box 750 to 800 ° C or higher, and a heat exchanger inlet 550 to 600 ° C or lower. Can be set to
【0022】流動層炉サイクロン48で分離されたダス
トは、排出機、例えばロータリフィーダ77によりダス
ト搬送管78に排出され、ブロワ、例えばルーツブロワ
79によりロータリキルンのバーナ36の近傍、例えば
バーナ上方のキルンに吹き込まれ、キルン排ガスととも
に排出されるまでの間に焼成される。この場合、ロータ
リフィーダ77、ルーツブロワ79及びダスト搬送管7
8でサイクロン捕集ダスト導入手段が構成される。熱交
換器50、52の下流のバグフィルタ60で捕集された
ダストの一部は、ダストの循環を避けるためにダスト系
外抜出管80を介して系外へ抜き出され、ダストの残部
はバグフィルタ捕集ダスト供給管81を介してロータリ
キルンのバーナ36の近傍、例えばバーナ上方のキルン
に吹き込まれる。The dust separated by the fluidized bed furnace cyclone 48 is discharged to a dust conveying pipe 78 by a discharger, for example, a rotary feeder 77, and is blown by, for example, a roots blower 79, near the burner 36 of the rotary kiln, for example, a kiln above the burner. And fired before being discharged together with the kiln exhaust gas. In this case, the rotary feeder 77, the roots blower 79, and the dust transfer pipe 7
8, a cyclone collecting dust introduction means is constituted. Part of the dust collected by the bag filter 60 downstream of the heat exchangers 50 and 52 is extracted to the outside through a dust extraction pipe 80 in order to avoid dust circulation, and the remaining dust is removed. Is blown into the vicinity of the burner 36 of the rotary kiln, for example, into the kiln above the burner via the bag filter collecting dust supply pipe 81.
【0023】キルンサイクロン33で捕集されたダスト
は、排出機、例えばロータリフィーダ83によりダスト
搬送管85に排出され、ブロワ、例えばルーツブロワ8
7により製品タンクへ搬送されて回収される。製品タン
クとしては、粗粒・微粉共用のもの1基のみを用いても
よく、又は粗粒用タンクと微粉用タンクの2基を用い、
流動層クーラ38からの粗粒を粗粒用タンクに輸送し、
流動層クーラー下流のバグフィルタ44で捕集された微
粉ダスト及びキルンサイクロン33で捕集された微粉ダ
ストを微粉用タンクに輸送するようにしてもよい。The dust collected by the kiln cyclone 33 is discharged to a dust conveying pipe 85 by a discharger, for example, a rotary feeder 83, and is blown by, for example, a roots blower 8.
7 to be conveyed to the product tank and collected. As the product tank, only one unit for both coarse and fine powders may be used, or two tanks for the coarse and fine powders may be used.
The coarse particles from the fluidized bed cooler 38 are transported to a coarse particle tank,
The fine dust collected by the bag filter 44 downstream of the fluidized bed cooler and the fine dust collected by the kiln cyclone 33 may be transported to a fine powder tank.
【0024】また、微粉の系内循環を避け、安定運転を
行うために、キルンサイクロン33の集塵効率が、流動
層炉サイクロン48の集塵効率より高くなるように構成
することが好ましい。Further, in order to prevent the fine powder from circulating in the system and perform a stable operation, it is preferable that the dust collecting efficiency of the kiln cyclone 33 be higher than that of the fluidized bed furnace cyclone 48.
【0025】また、熱交換器50、52内のダストの付
着を減少させて熱効率を維持する必要がある。このた
め、流動層炉サイクロン48及びキルンサイクロン33
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
2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82を有するとともに、上面中央部に排ガ
ス排出管84を有する円筒胴体86の下部に、略逆円錐
胴体88を連設し、この略逆円錐胴体88の下部に拡大
壁部90を連設し、さらに、この拡大壁部90に略逆円
錐胴部92を連設し、略逆円錐胴体88の下端部内径D
1と排ガス排出管84の内径dがD1≧dの関係を有
し、円筒胴体86の内径Dと拡大壁部90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、流動層炉20及びロー
タリーキルン28からの排ガス中のダストを効率よく捕
集することができる。この高効率サイクロンを用いる場
合は、前述のように、ジャケット構造にして用いられ
る。Further, it is necessary to maintain the thermal efficiency by reducing the adhesion of dust in the heat exchangers 50 and 52. Therefore, the fluidized bed furnace cyclone 48 and the kiln cyclone 33
For example, a high-efficiency cyclone (commercial cyclone) as disclosed in Japanese Utility Model Publication No. 7-46357
It is preferable to use As shown in FIG. 2, the high-efficiency cyclone has an exhaust gas inlet 82 for introducing exhaust gas in a tangential direction on the upper side, and a substantially inverted cylinder body 86 having an exhaust gas discharge pipe 84 in the center of the upper surface. A conical body 88 is continuously provided, an enlarged wall portion 90 is continuously provided below the substantially inverted conical body 88, and a substantially inverted conical body portion 92 is continuously provided on the enlarged wall portion 90. Lower end inside diameter D
1 and the inner diameter d of the exhaust gas discharge pipe 84 have a relationship of D1 ≧ d, and D2 = (0.8 to 1.0) between the inner diameter D of the cylindrical body 86 and the lower end inner diameter D2 of the enlarged wall portion 90. It is configured to have a relationship of × D. By using the cyclone having such a structure, dust in exhaust gas from the fluidized bed furnace 20 and the rotary kiln 28 can be efficiently collected. When this high-efficiency cyclone is used, it is used in a jacket structure as described above.
【0026】また、熱交換器50としては、図3に示す
ように、臭気を通過させて加熱するための伝熱管94が
鉛直に配置された構造のものを用いることが好ましい。
このように構成すれば、ダストの付着、堆積が少なく清
掃も容易となる。なお、低温側の熱交換器52も同様の
構造とすることが好ましい。さらに、流動層炉20のガ
ス分散板24として、例えば、実公平7−37113号
公報に示されているような特殊構造の分散板とすること
が好ましい。この特殊構造の分散板は、図4及び図5に
示すように、板体96に貫通固定された多数の筒体98
の天壁部100に、直径が流動媒体径の3倍以下、望ま
しくは2倍以下の複数の小孔102が設けられたもので
ある。このような構造の分散板を用いることにより、流
動媒体を高温のまま保持するホットバンキングが可能と
なる。また、ガス分散板24の上側近傍に補助バーナ1
04を設けることが好ましく、このように構成すれば、
立ち上げ時や、トラブル時のようにロータリキルンの運
転ができない場合に、臭気の脱臭を行うことができる。As the heat exchanger 50, as shown in FIG. 3, it is preferable to use a heat exchanger having a structure in which a heat transfer tube 94 for passing an odor and heating it is arranged vertically.
With this configuration, the amount of dust attached and deposited is small, and cleaning is easy. Note that the heat exchanger 52 on the low temperature side preferably has the same structure. Further, as the gas dispersion plate 24 of the fluidized bed furnace 20, for example, a dispersion plate having a special structure as disclosed in Japanese Utility Model Publication No. 7-37113 is preferably used. As shown in FIGS. 4 and 5, the dispersion plate having this special structure has a large number of cylindrical bodies 98 fixed through the plate body 96.
Is provided with a plurality of small holes 102 whose diameter is three times or less, preferably two times or less, the diameter of the fluid medium. By using the dispersion plate having such a structure, hot banking in which the fluid medium is maintained at a high temperature becomes possible. The auxiliary burner 1 is located near the upper side of the gas distribution plate 24.
04 is preferably provided. With such a configuration,
The odor can be deodorized when the rotary kiln cannot be operated, such as during startup or trouble.
【0027】[0027]
【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) 高伝熱性能の流動層炉で原料(造粒物)の乾
燥、又は乾燥・予熱、又は乾燥・有機物の焼却・消石灰
の焼成(分解)を行うので、下流のロータリキルンを小
型化することができる上に、サイクロンをジャケット構
造にしてサイクロン内壁面を再炭酸化温度以下に冷却す
ることにより、微粉の付着を確実に防止することがで
き、安定運転を行うことができる。 (2) 原料が造粒物であるので、造粒物自体が流動媒
体となり、他の流動媒体は不要である。また、クーラと
して小型、高効率の流動層クーラを使用することができ
る。 (3) 流動層炉からの処理物をロータリキルンで十分
時間をかけて焼成することができるので、高品質の地盤
改良材を得ることができる。 (4) 流動層炉の排ガスで臭気を加熱し熱回収するこ
とにより、熱消費を低減することができる。 (5) 臭気の吹込配分を調整する場合は、各部の温度
をダスト付着のない温度に設定することができる。ま
た、各部の温度を脱臭可能な温度に設定することができ
るので、臭気処理を確実に行うことができる。 (6) キルンサイクロンの集塵効率を流動層炉サイク
ロンの集塵効率より大きくする場合は、微粉の系内循環
がなくなり、安定運転が可能となる。 (7) 流動層炉の排ガスを高集塵効率のサイクロンで
除塵する場合は、熱交換器内のダスト付着が大幅に減少
し、熱効率を維持することができるとともに、長期連続
運転が可能となる。 (8) 伝熱管が鉛直に配列された熱交換器を用いる場
合は、ダストの付着、堆積が少なく清掃も容易となる。 (9) 特殊構造のガス分散板を用いる場合は、ホット
バンキングを行うことが可能となる。従って、起動・停
止操作が短時間で行なえ、異常時の操作も容易である。 (10) 流動層炉において、補助バーナを設ける場合
は、立ち上げ時やトラブル時に臭気の脱臭を行うことが
できる。As described above, the present invention has the following effects. (1) Since the raw material (granulated material) is dried or dried and preheated, or dried, incinerated and burnt (decomposed) of slaked lime in a fluidized bed furnace with high heat transfer performance, the rotary kiln downstream is downsized. In addition to this, the cyclone has a jacket structure and the inner wall surface of the cyclone is cooled to a temperature not higher than the recarbonation temperature, so that adhesion of fine powder can be reliably prevented, and stable operation can be performed. (2) Since the raw material is a granulated material, the granulated material itself becomes a fluid medium, and no other fluid medium is required. In addition, a compact, high-efficiency fluidized bed cooler can be used as the cooler. (3) Since the treated material from the fluidized bed furnace can be fired in a rotary kiln for a sufficient time, a high quality ground improvement material can be obtained. (4) Heat consumption can be reduced by heating the odor with the exhaust gas of the fluidized bed furnace and recovering heat. (5) When adjusting the distribution of the odor, the temperature of each part can be set to a temperature at which dust does not adhere. Further, since the temperature of each part can be set to a temperature at which deodorization can be performed, odor treatment can be reliably performed. (6) When the dust collection efficiency of the kiln cyclone is made larger than the dust collection efficiency of the fluidized-bed furnace cyclone, the circulation of fine powder in the system is eliminated, and stable operation becomes possible. (7) When the exhaust gas from a fluidized bed furnace is removed by a cyclone with high dust collection efficiency, dust adhesion in the heat exchanger is greatly reduced, and the heat efficiency can be maintained and long-term continuous operation can be performed. . (8) When a heat exchanger in which the heat transfer tubes are arranged vertically is used, dust is less likely to adhere and accumulate and cleaning is easy. (9) When a gas dispersion plate having a special structure is used, hot banking can be performed. Therefore, the start / stop operation can be performed in a short time, and the operation at the time of abnormality is easy. (10) When an auxiliary burner is provided in a fluidized bed furnace, odor can be deodorized at the time of startup or trouble.
【図1】本発明の実施の第1形態による地盤改良材の製
造装置を示す系統的概略構成図である。FIG. 1 is a systematic schematic configuration diagram showing an apparatus for manufacturing a ground improvement material according to a first embodiment of the present invention.
【図2】図1におけるサイクロンの一例を示す立面説明
図である。FIG. 2 is an elevational view showing an example of the cyclone in FIG. 1;
【図3】図1における熱交換器の一例を示す立面説明図
である。FIG. 3 is an elevational view showing an example of the heat exchanger in FIG. 1;
【図4】図1における流動層炉のガス分散板の一例を示
す断面説明図である。FIG. 4 is an explanatory sectional view showing an example of a gas dispersion plate of the fluidized bed furnace in FIG.
【図5】図4におけるガス分散板の要部の平面図であ
る。FIG. 5 is a plan view of a main part of the gas dispersion plate in FIG.
10 原料製造工場 12 混練機 14 造粒機 16 ホッパ 18 ベルトフィーダ 20 流動層炉 22 風箱 24 ガス分散板 26 流動層 28 ロータリキルン 31 ロータリキルン排ガス導管 32 Lバルブ 33 キルンサイクロン 34 窯尻 35 キルンサイクロン排ガス導管 36 キルンバーナ 38 流動層クーラ 40、77、83 ロータリフィーダ 42 輸送機 44、60 バグフィルタ 46、56 押込ブロワ 48 流動層炉サイクロン 50、52 熱交換器 54 臭気ファン 58 排ガス誘引ファン 62 煙突 64 フリーボード部 66、68、70 加熱臭気の分岐管 72、74、76 バルブ 78、85 ダスト搬送管 79、87 ルーツブロワ 80 ダスト系外抜出管 81 バグフィルタ捕集ダスト供給管 82 排ガス導入口 84 排ガス排出管 86 円筒胴体 88 略逆円錐胴体 90 拡大壁部 91、93 冷却ファン 92 略逆円錐胴部 94 伝熱管 96 板体 98 筒体 100 天壁部 102 小孔 104 補助バーナ DESCRIPTION OF SYMBOLS 10 Raw material manufacturing plant 12 Kneader 14 Granulator 16 Hopper 18 Belt feeder 20 Fluidized bed furnace 22 Wind box 24 Gas dispersion plate 26 Fluidized bed 28 Rotary kiln 31 Rotary kiln exhaust gas conduit 32 L valve 33 Kiln cyclone 34 Kiln end 35 Kiln cyclone Exhaust gas conduit 36 Kiln burner 38 Fluidized bed cooler 40, 77, 83 Rotary feeder 42 Transporter 44, 60 Bag filter 46, 56 Push-in blower 48 Fluidized bed furnace cyclone 50, 52 Heat exchanger 54 Odor fan 58 Exhaust gas inducing fan 62 Chimney 64 Free Board section 66, 68, 70 Branch pipe for heated odor 72, 74, 76 Valve 78, 85 Dust transfer pipe 79, 87 Roots blower 80 Dust extraction pipe 81 Bag filter collection dust supply pipe 82 Exhaust gas inlet 84 Exhaust gas exhaust 86 cylindrical body 88 substantially inverted conical body 90 expanded wall portion 91, 93 cooling fan 92 substantially inverted cone trunk portion 94 the heat transfer tube 96 plate body 98 the cylindrical body 100 top wall 102 small holes 104 auxiliary burner
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 FI テーマコート゛(参考) C04B 7/47 C04B 7/47 (72)発明者 村尾 三樹雄 神戸市長田区川西通2丁目4番地 川崎エ ンジニアリング株式会社内 Fターム(参考) 4D059 AA03 BB01 BB02 BB06 BB13 BB14 BE00 BK01 BK09 CA10 CA14 CA16 CA30 CB30 CC10 DA04 4G012 KD04 KD06 4H026 CA02 CC06 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 Identification FI FI Theme Court ゛ (Reference) C04B 7/47 C04B 7/47 (72) Inventor Mikio Murao 2-4 Kawanishidori, Nagata-ku, Kobe Kawasaki Engineer F-term in Ring Co., Ltd. (Reference) 4D059 AA03 BB01 BB02 BB06 BB13 BB14 BE00 BK01 BK09 CA10 CA14 CA16 CA30 CB30 CC10 DA04 4G012 KD04 KD06 4H026 CA02 CC06
Claims (17)
した造粒物を、下流のロータリキルンの排ガスを流動化
ガスとする流動層炉に投入し造粒物を流動媒体として乾
燥、乾燥・予熱又は乾燥・有機物焼却・消石灰焼成を行
った後、流動層炉からの粒状物をロータリキルンに導入
して焼成し、焼成粒状物を流動層クーラに導入して冷却
する方法であって、流動層炉の排ガスを一部又は全部が
ジャケット構造の流動層炉サイクロンに導入してダスト
を捕集するとともに、ジャケットに冷却用流体を導入し
間接的冷却して該サイクロンを冷却することを特徴とす
る地盤改良材の製造方法。1. A granulated material obtained by mixing and agitating lime to a sludge dewatered cake, and granulating the sludge dewatered cake into a fluidized bed furnace using the exhaust gas of a downstream rotary kiln as a fluidizing gas, and drying and drying the granulated material as a fluid medium.・ After performing preheating or drying, incineration of organic matter, and calcination of slaked lime, a method of introducing granular materials from a fluidized bed furnace into a rotary kiln and calcining the same, introducing the calcined granular materials into a fluidized bed cooler and cooling, The exhaust gas from the fluidized bed furnace is partially or entirely introduced into a cyclone having a jacket structure to collect dust, and a cooling fluid is introduced into the jacket to cool the cyclone indirectly. Manufacturing method of ground improvement material.
がジャケット構造のキルンサイクロンに導入してダスト
を分離するとともに、ジャケットに冷却用流体を導入し
間接冷却して該サイクロンを冷却する請求項1記載の地
盤改良材の製造方法。2. The method according to claim 1, wherein exhaust gas from the rotary kiln is partially or entirely introduced into a kiln cyclone having a jacket structure to separate dust, and a cooling fluid is introduced into the jacket to cool the cyclone by indirect cooling. A method for producing the ground improvement material as described above.
をロータリキルンのバーナ近傍に吹き込み、キルン排ガ
スとともに排出されるまでの間に焼成し、キルンサイク
ロンで捕集して製品として回収する請求項1又は2記載
の地盤改良材の製造方法。3. The dust collected in a fluidized-bed furnace cyclone is blown into the vicinity of a burner of a rotary kiln, fired before being discharged together with kiln exhaust gas, collected by the kiln cyclone and collected as a product. 3. The method for producing the ground improvement material according to 1 or 2.
ンの内壁温度が600℃以下となるように冷却する請求
項3記載の地盤改良材の製造方法。4. The method for producing a ground improvement material according to claim 3, wherein the fluidized-bed furnace cyclone and the kiln cyclone are cooled so that the inner wall temperature is 600 ° C. or less.
1〜4のいずれかに記載の地盤改良材の製造方法。5. The method for producing a ground improvement material according to claim 1, wherein the particle size of the granulated product is 1 to 20 mm.
ロンで除塵した後、流動層炉サイクロンからの排ガスを
熱交換器に導入して熱回収する請求項1〜5のいずれか
に記載の地盤改良材の製造方法。6. The exhaust gas from a fluidized bed furnace cyclone is dust-removed in a fluidized bed furnace cyclone, and then the exhaust gas from the fluidized bed furnace cyclone is introduced into a heat exchanger to recover heat. Manufacturing method of ground improvement material.
導入してダストを捕集し、捕集されたダストを流動層炉
サイクロンからのダストとともに、ロータリキルンのバ
ーナ近傍に吹き込む請求項6記載の地盤改良材の製造方
法。7. The exhaust gas from a heat exchanger is introduced into a bag filter to collect dust, and the collected dust is blown together with dust from a cyclone in a fluidized bed furnace near a burner of a rotary kiln. Method of manufacturing ground improvement material.
換器に導入して昇温し、加熱臭気をロータリキルンの燃
焼用空気として回収するとともに、余剰の加熱臭気を流
動層炉の風箱及び/又はフリーボード部に吹き込んで脱
臭する請求項1〜7のいずれかに記載の地盤改良材の製
造方法。8. An odor generated in the process of producing the granulated product is introduced into a heat exchanger and heated to recover the heated odor as combustion air for a rotary kiln. The method for producing a ground improvement material according to any one of claims 1 to 7, wherein the deodorization is performed by blowing into a wind box and / or a free board portion.
並びに加熱臭気の流動層炉の風箱への吹込量及び/又は
加熱臭気の流動層炉のフリーボード部への吹込量を夫々
調整する請求項8記載の地盤改良材の製造方法。9. The amount of heated odor blown into the rotary kiln;
The method for producing a ground improvement material according to claim 8, wherein the amount of the heated odor blown into the wind box of the fluidized bed furnace and / or the amount of the heated odor blown into the freeboard portion of the fluidized bed furnace are adjusted.
炉サイクロンの集塵効率より大きくする請求項3又は4
記載の地盤改良材の製造方法。10. The dust collection efficiency of a kiln cyclone is made larger than the dust collection efficiency of a fluidized bed furnace cyclone.
A method for producing the ground improvement material as described above.
した造粒物を投入し造粒物を流動媒体として乾燥、乾燥
・予熱又は乾燥・有機物焼却・消石灰焼成を行うための
流動層炉と、 流動層炉からの粒状物を導入して焼成するためのロータ
リキルンと、 ロータリキルンからの焼成粒状物を冷却するための流動
層クーラと、 ロータリキルンの窯尻にロータリキルン排ガス導管を介
して接続された、一部又は全部がジャケット構造に構成
されたキルンサイクロンと、 キルンサイクロンと流動層炉の風箱とを接続するための
キルンサイクロン排ガス導管と、 流動層炉からの排ガスを導入してダストを分離するため
の、一部又は全部がジャケット構造に構成された流動層
炉サイクロンと、 流動層炉サイクロンからの排ガスを導入して熱回収する
ための熱交換器と、 熱交換器からの排ガスを導入してダストを分離するため
のバグフィルタと、 流動層炉サイクロンの下部とロータリキルンのバーナ近
傍とを接続するサイクロン捕集ダスト導入手段とを備え
たことを特徴とする地盤改良材の製造装置。11. A fluidized bed furnace for kneading and granulating sludge dewatered cake and lime, feeding granules, and using the granules as a fluid medium for drying, drying and preheating or drying, incineration of organic matter and calcination of slaked lime. A rotary kiln for introducing and firing the particulate matter from the fluidized bed furnace; a fluidized bed cooler for cooling the fired particulate matter from the rotary kiln; and a rotary kiln exhaust gas conduit at the bottom of the rotary kiln. A kiln cyclone partially or wholly configured in a jacket structure, a kiln cyclone exhaust gas conduit for connecting the kiln cyclone to the wind box of the fluidized bed furnace, and an exhaust gas from the fluidized bed furnace. Fluidized-bed furnace cyclone, part or all of which is configured in a jacket structure, for separating dust by heating, and for introducing heat from the fluidized-bed furnace cyclone to recover heat. A heat exchanger, a bag filter for introducing exhaust gas from the heat exchanger to separate dust, and a cyclone collecting dust introducing means for connecting a lower part of the fluidized bed furnace cyclone and a vicinity of a burner of the rotary kiln. An apparatus for manufacturing a ground improvement material.
ダスト導入手段又はロータリキルンのバーナ近傍とがバ
グフィルタ捕集ダスト供給管を介して接続された請求項
11記載の地盤改良材の製造装置。12. The apparatus for manufacturing a ground improvement material according to claim 11, wherein a lower portion of the bag filter and a portion near the cyclone dust collecting means or a burner of the rotary kiln are connected via a bag filter collecting dust supply pipe.
めの混練機と、混練機からの混練物を造粒するための造
粒機を備えた請求項11又は12記載の地盤改良材の製
造装置。13. The production of a ground improvement material according to claim 11, comprising a kneader for kneading the sludge dewatered cake and lime, and a granulator for granulating the kneaded material from the kneader. apparatus.
サイクロンが、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D
2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11、12
又は13記載の地盤改良材の製造装置。14. A kiln cyclone and / or a fluidized bed furnace cyclone having an exhaust gas inlet for introducing exhaust gas in a tangential direction at an upper portion and a substantially inverted lower portion of a cylindrical body having an exhaust gas discharge pipe at the center of the upper surface. Conical fuselage is connected,
An enlarged wall section is connected to the lower part of this substantially inverted conical body,
A substantially inverted conical body is connected to the enlarged wall, and a lower end inner diameter D1 of the substantially inverted conical body and an inner diameter d of the exhaust gas discharge pipe have a relationship of D1 ≧ d. Lower end inside diameter D
13. A high-efficiency cyclone having a relationship of D2 = (0.8 to 1.0) .times.D with the second cyclone.
Or a manufacturing apparatus for a ground improvement material according to 13.
るための伝熱管が鉛直に配置された構造である請求項1
1〜14のいずれかに記載の地盤改良材の製造装置。15. The heat exchanger according to claim 1, wherein the heat exchanger has a structure in which heat transfer tubes for passing odor and heating the odor are arranged vertically.
An apparatus for manufacturing a ground improvement material according to any one of 1 to 14.
固定された多数の筒体の天壁部に、直径が流動媒体径の
3倍以下の複数の小孔が設けられた構造である請求項1
1〜15のいずれかに記載の地盤改良材の製造装置。16. A structure in which a gas dispersion plate of a fluidized bed furnace is provided with a plurality of small holes having a diameter of three times or less the diameter of a fluid medium in a top wall portion of a large number of cylindrical members fixedly penetrating through the plate members. Claim 1
An apparatus for manufacturing a ground improvement material according to any one of 1 to 15.
助バーナを設けた請求項11〜16のいずれかに記載の
地盤改良材の製造装置。17. The apparatus for manufacturing a soil improvement material according to claim 11, wherein an auxiliary burner is provided near the upper side of the gas dispersion plate of the fluidized bed furnace.
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JP2000111657A JP3905682B2 (en) | 2000-04-13 | 2000-04-13 | Method and apparatus for manufacturing ground improvement material |
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JP2000111657A JP3905682B2 (en) | 2000-04-13 | 2000-04-13 | Method and apparatus for manufacturing ground improvement material |
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Cited By (5)
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JP2003137621A (en) * | 2001-10-29 | 2003-05-14 | Mitsubishi Materials Corp | Method for treating air containing bad smell |
CN103063015A (en) * | 2013-01-31 | 2013-04-24 | 伍耀明 | Vacuum rotary kiln with mine dust return system |
JP2013086981A (en) * | 2011-10-13 | 2013-05-13 | Taiheiyo Cement Corp | System and method for producing phosphatic fertilizer |
CN103708701A (en) * | 2013-12-31 | 2014-04-09 | 一重集团大连设计研究院有限公司 | After-treatment system of dried fine-powder sludge and treatment method |
CN106517726A (en) * | 2016-12-26 | 2017-03-22 | 南昌航空大学 | Two-stage sludge drying device and method |
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