JP2009281723A - Water-containing object combustion treatment facility and its method - Google Patents

Water-containing object combustion treatment facility and its method Download PDF

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JP2009281723A
JP2009281723A JP2009166311A JP2009166311A JP2009281723A JP 2009281723 A JP2009281723 A JP 2009281723A JP 2009166311 A JP2009166311 A JP 2009166311A JP 2009166311 A JP2009166311 A JP 2009166311A JP 2009281723 A JP2009281723 A JP 2009281723A
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heat exchanger
indirect heat
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exhaust gas
stage indirect
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JP4841011B2 (en
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Hisashi Endo
久 遠藤
Hiroyuki Yokomaku
宏幸 横幕
Kiyoshi Kojima
喜代志 小島
Masaichi Bando
政一 坂東
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Tsukishima Kikai Co Ltd
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Abstract

<P>PROBLEM TO BE SOLVED: To supply a drying heat source of stable temperature to a dryer. <P>SOLUTION: This water-containing object combustion treatment facility comprises the dryer 3 for drying water-containing waste using a heat medium as the drying heat source, and a treating furnace 5 for incinerating or melting the dried waste dried by the dryer 3. When the used heat medium used by the dryer 3 is heated by heat exchange with exhaust gas in the treating furnace 5 in a first stage indirect heat exchanger 8, a second stage indirect heat exchanger 9 and a third stage indirect heat exchanger 10 and circulated and supplied again to the dryer 3, the used heat medium is circulated in the order of the first stage indirect heat exchanger 8, the second stage indirect heat exchanger 9 and the third stage indirect heat exchanger 10, while the exhaust gas in the treating furnace 5 is circulated in the order of the first stage indirect heat exchanger 8, the third stage indirect heat exchanger 10 and the second stage indirect heat exchanger 9. <P>COPYRIGHT: (C)2010,JPO&amp;INPIT

Description

本発明は、焼却や溶融処理に先立って乾燥を要する下水汚泥や生ごみ等の含水廃棄物の処理設備及びその方法に関する。   The present invention relates to a treatment facility and a method for water-containing waste such as sewage sludge and garbage that require drying prior to incineration or melting treatment.

近年の廃棄物処理設備においては、省エネルギー化の要請により、焼却や溶融に伴って発生する排熱を回収し、同設備内の熱源として又は発電機により電気エネルギーとして有効利用している。   In recent waste treatment facilities, in response to a request for energy saving, exhaust heat generated by incineration or melting is recovered and effectively used as a heat source in the facility or as electric energy by a generator.

例えば含水廃棄物処理設備において排熱の有効利用を図るものとしては、特公平７−２４７３３号公報に開示される技術がある。この従来技術は、蒸気と含水廃棄物とを直接接触させて乾燥を行う蒸気直接乾燥機と、この乾燥機により乾燥した乾燥廃棄物を燃焼する燃焼炉とを備え、熱交換器を用いて乾燥機により使用した使用済み蒸気を燃焼炉の排ガスとの熱交換により加熱し、再び乾燥機に循環供給するように構成したものである。   For example, there is a technique disclosed in Japanese Patent Publication No. 7-24733 as an effective utilization of exhaust heat in a hydrous waste treatment facility. This prior art includes a steam direct dryer that performs drying by directly contacting steam and water-containing waste, and a combustion furnace that burns dry waste dried by the dryer, and is dried using a heat exchanger. The used steam used by the machine is heated by heat exchange with the exhaust gas of the combustion furnace, and is circulated again to the dryer.

特公平７−２４７３３号公報Japanese Patent Publication No. 7-24733 特開昭５４−１３１３４４号公報JP 54-131344 A 特開平６−２６６２９号公報JP-A-6-26629 特開昭６１−２０９０９９号公報JP-A 61-209099

しかしながら、乾燥機の乾燥熱源として用いる熱媒の加熱を燃焼炉排ガスとの熱交換だけに依存する構成とすると、熱媒の温度が、燃焼処理量や燃焼炉排ガスの温度によって変動してしまい、安定した乾燥熱源の確保が困難となる。   However, if the heating medium used as the drying heat source of the dryer is configured to rely only on heat exchange with the combustion furnace exhaust gas, the temperature of the heating medium varies depending on the combustion processing amount and the temperature of the combustion furnace exhaust gas. It becomes difficult to secure a stable drying heat source.

そこで、本発明の主たる課題は、安定した温度の熱媒を乾燥機に供給できるようにすることにある。   Then, the main subject of this invention is to enable it to supply the heat medium of the stable temperature to a dryer.

上記課題を解決した本発明は、熱媒を乾燥熱源として含水物の乾燥を行う乾燥機と、この乾燥機により乾燥した乾燥物を燃焼する燃焼炉とを備え、前記乾燥機により使用した使用済み熱媒を前記燃焼炉の排ガスとの熱交換により加熱し、再び前記乾燥機に循環供給するように構成した含水物燃焼処理設備において、
前記使用済み熱媒と燃焼炉の排ガスとの熱交換を行う、一段目の間接熱交換器、二段目の間接熱交換器及び三段目の間接熱交換器を備え、
前記使用済み熱媒が、前記一段目の間接熱交換器、前記二段目の間接熱交換器及び前記三段目の間接熱交換器の順に流通される一方、前記燃焼炉の排ガスが前記一段目の間接熱交換器、前記三段目の間接熱交換器及び前記二段目の間接熱交換器の順に流通されるように構成された、
ことを特徴とする含水物燃焼処理設備である。 The present invention that has solved the above problems comprises a dryer that dries hydrated material using a heat medium as a drying heat source, and a combustion furnace that burns the dried material dried by the dryer, and is used by the dryer. In the hydrated material combustion treatment facility configured to heat the heat medium by heat exchange with the exhaust gas of the combustion furnace and to circulate and supply again to the dryer,
The first stage indirect heat exchanger, the second stage indirect heat exchanger, and the third stage indirect heat exchanger that perform heat exchange between the used heat medium and the exhaust gas of the combustion furnace,
The used heat medium is circulated in the order of the first-stage indirect heat exchanger, the second-stage indirect heat exchanger, and the third-stage indirect heat exchanger, while the combustion furnace exhaust gas is in the first-stage indirect heat exchanger. The indirect heat exchanger of the eye, the indirect heat exchanger of the third stage and the indirect heat exchanger of the second stage are configured to be distributed in this order.
This is a hydrated material combustion treatment facility.

このように構成することで、安定した温度の熱媒を乾燥機に供給することができる。   By comprising in this way, the heat medium of the stable temperature can be supplied to a dryer.

本発明は、前記熱媒が蒸気であり、前記乾燥機が蒸気と含水物とを直接接触させて乾燥を行う蒸気直接乾燥機である設備に特に好適である。   The present invention is particularly suitable for equipment in which the heat medium is steam and the dryer is a steam direct dryer that performs drying by directly contacting the steam and the hydrated material.

他方、本発明の含水物燃焼処理方法は、熱媒を乾燥熱源として含水物の乾燥を行い、この乾燥した乾燥物を燃焼する一方で、前記乾燥に使用した使用済み熱媒を前記燃焼により生成する燃焼炉排ガスとの熱交換により加熱し、再び前記乾燥に利用するにあたり、
前記使用済み熱媒と燃焼炉の排ガスとの熱交換を行う、一段目の間接熱交換器、二段目の間接熱交換器及び三段目の間接熱交換器を用い、
前記使用済み熱媒を、前記一段目の間接熱交換器、前記二段目の間接熱交換器及び前記三段目の間接熱交換器の順に流通させる一方、前記燃焼炉の排ガスを前記一段目の間接熱交換器、前記三段目の間接熱交換器及び前記二段目の間接熱交換器の順に流通させる、
ことを特徴とするものである。 On the other hand, the hydrated material combustion treatment method of the present invention performs drying of the hydrated material using the heating medium as a drying heat source, and burns the dried dried material, while generating the used heating medium used for the drying by the combustion. When heating by heat exchange with the combustion furnace exhaust gas to be used again for the drying,
Using the first stage indirect heat exchanger, the second stage indirect heat exchanger, and the third stage indirect heat exchanger that perform heat exchange between the used heat medium and the exhaust gas of the combustion furnace,
The spent heat medium is circulated in the order of the first-stage indirect heat exchanger, the second-stage indirect heat exchanger, and the third-stage indirect heat exchanger, while the combustion furnace exhaust gas is passed through the first-stage indirect heat exchanger. Indirect heat exchanger, the third-stage indirect heat exchanger and the second-stage indirect heat exchanger in order,
It is characterized by this.

以上のとおり本発明によれば、安定した温度の乾燥熱源を乾燥機に供給できるようになる。   As described above, according to the present invention, a drying heat source having a stable temperature can be supplied to a dryer.

本発明に係る汚泥処理設備例の前段フロー図である。It is a front | former flow chart of the example of sludge processing equipment which concerns on this invention. 後段フロー図である。It is a latter part flow diagram. 排熱回収部の拡大図である。It is an enlarged view of a waste heat recovery part. 排ガス連通路の拡大斜視図である。It is an expansion perspective view of an exhaust gas communicating path.

以下、本発明について、下水汚泥処理設備の例を引いて詳説する。
図１及び図２は、本発明を適用した下水汚泥処理設備例のフロー図を示している。図１中の符号１は、汚泥ピットを示しており、ここに貯留された汚泥Ｓは、図示しないクレーン等により図示しないホッパーに移送されそこに付属する汚泥供給ポンプ２により乾燥機３に供給される。 Hereinafter, the present invention will be described in detail with reference to an example of sewage sludge treatment equipment.
FIG.1 and FIG.2 has shown the flowchart of the example of the sewage sludge processing equipment to which this invention is applied. Reference numeral 1 in FIG. 1 denotes a sludge pit, and the sludge S stored therein is transferred to a hopper (not shown) by a crane (not shown) and supplied to a dryer 3 by a sludge supply pump 2 attached thereto. The

乾燥機３においては、後述する排ガスとの熱交換によって加熱済みの約４００℃程度の蒸気を乾燥熱源として汚泥が乾燥される。乾燥機３としては、乾燥熱源として蒸気等の熱媒を循環利用できるものであれば、図示例のように蒸気と含水廃棄物とを直接接触させて乾燥を行う蒸気直接乾燥タイプのものでなくても良い。また循環熱媒としては蒸気に限られない。   In the dryer 3, the sludge is dried using a steam of about 400 ° C. that has been heated by heat exchange with the exhaust gas described later as a drying heat source. The dryer 3 is not of a steam direct drying type in which steam and water-containing waste are directly brought into contact as shown in the illustrated example as long as a heat medium such as steam can be circulated as a drying heat source. May be. The circulating heat medium is not limited to steam.

汚泥との熱交換により減温した蒸気は、約１５０℃程度となって集塵機３Ｃに対して供給され、ここで乾燥汚泥ダストが分離回収された後、蒸気循環ファン３Ｆにより後述の一段目の蒸気加熱器８に供給される。なお、集塵機３Ｃとしてはバグフィルタまたはサイクロンを複数段設けるのが好ましい。   The steam reduced in temperature by heat exchange with the sludge is supplied to the dust collector 3C at about 150 ° C. After the dried sludge dust is separated and recovered here, the first-stage steam described later by the steam circulation fan 3F. It is supplied to the heater 8. As the dust collector 3C, it is preferable to provide a plurality of stages of bag filters or cyclones.

乾燥機３により乾燥され排出された乾燥汚泥、および集塵機３Ｃにより回収した乾燥汚泥ダストは、次いで乾燥汚泥輸送ブロワ４による空気輸送にて溶融炉５へ供給され、燃焼溶融される。燃焼溶融炉５は、本発明では特に限定されないが、図示例の場合、竪型旋回式の予備燃焼炉５０と、その下端に一端が接続された横型主燃焼炉５１と、その他端にスラグシュート５２を介して接続された竪型の混合冷却器５３とから構成された自然放冷式のものであり、乾燥汚泥は予備燃焼炉５０の上部に吹き込まれる。予備燃焼炉５０の上部にはバーナー５４が設けられ、このバーナー５４に対して都市ガス、重油、灯油、廃油等の燃料、ならびにファン５５からの燃焼空気が供給されるように構成されており、予備燃焼炉５０内に旋回方向に沿って吹き込まれた乾燥汚泥は、旋回降下しながらバーナー５４による燃焼フレームにより燃焼溶融され、主燃焼炉５１内を経て、スラグシュート５２から溶融スラグとして排出される。排出した溶融スラグは、水冷スラグコンベヤ６により冷却固化された後に取り出される。   The dried sludge dried and discharged by the dryer 3 and the dried sludge dust collected by the dust collector 3C are then supplied to the melting furnace 5 by pneumatic transportation by the dried sludge transportation blower 4, and are burned and melted. Although the combustion melting furnace 5 is not particularly limited in the present invention, in the illustrated example, a vertical swirl type preliminary combustion furnace 50, a horizontal main combustion furnace 51 having one end connected to the lower end, and a slag chute at the other end. This is a naturally-cooled type composed of a saddle-type mixing cooler 53 connected via 52, and the dried sludge is blown into the upper portion of the preliminary combustion furnace 50. A burner 54 is provided in the upper portion of the pre-combustion furnace 50, and fuel such as city gas, heavy oil, kerosene, waste oil, and combustion air from the fan 55 are supplied to the burner 54. The dried sludge blown into the pre-combustion furnace 50 along the swirl direction is burned and melted by the combustion frame by the burner 54 while swirling down, and is discharged from the slag chute 52 as molten slag through the main combustion furnace 51. . The discharged molten slag is taken out after being cooled and solidified by the water-cooled slag conveyor 6.

他方、溶融炉５の排ガスは約１３５０〜１４５０℃となっており、これが混合冷却器５３を経て約８５０℃程度まで放冷された後に、空気予熱器７および複数段の蒸気加熱器８〜１０からなる排熱回収部に送られる。本例では、空気予熱器７および一段目の蒸気加熱器８がそれぞれ輻射式熱交換器からなり、二段目および三段目の蒸気加熱器９，１０がシェルアンドチューブ式熱交換器からなるものとされているが、本発明においてはかかる種類及び組み合わせに限定されず、他の公知の熱交換器を用いることもできる。   On the other hand, the exhaust gas from the melting furnace 5 is about 1350 to 1450 ° C., and after this is cooled to about 850 ° C. through the mixing cooler 53, the air preheater 7 and the multistage steam heaters 8 to 10 are cooled. It is sent to the exhaust heat recovery unit consisting of In this example, the air preheater 7 and the first stage steam heater 8 are each composed of a radiant heat exchanger, and the second and third stage steam heaters 9 and 10 are each composed of a shell and tube heat exchanger. However, the present invention is not limited to such types and combinations, and other known heat exchangers can also be used.

空気予熱器７は、約２０〜２００℃程度の空気を炉内過熱防止のために主燃焼炉５１内に吹き込むにあたり極端な温度低下を避けるべく、予め溶融炉排ガスとの熱交換により予熱するための熱交換器であり、より詳細には図３に示すように、上部供給口７ｉから下端排出口７ｅへ向けて溶融炉排ガスが流通される縦置き配置の筒状部７Ｔ（例えば、内径１５００〜２５００ｍｍ程度）と、筒状部７Ｔ内の流通排ガスを取り囲むように設けられ、燃焼空気が上端部供給口７ｍから下端部排出口７ｎへ流通される筒状ジャケット部７Ｊとから構成されている。そして、例えば図示のように大気を空気予熱器７に対して直接供給し、供給された空気はジャケット部７Ｊ内を下側へ流通する過程で、筒状部７Ｔ内を並流する溶融炉排ガスとの間接熱交換により、約５００℃程度まで予熱された後、主燃焼炉５１に送られ、炉内温度が適温に抑制される。この予熱空気は予備燃焼炉５０に対しても供給することができる。また、予備燃焼炉５０の上部冷却ジャケットから取り出した約２００℃程度の冷却空気を、大気とともに或いは大気に代えて単独で空気予熱器７に対して供給することもできる。   The air preheater 7 is preheated by heat exchange with the melting furnace exhaust gas in advance in order to avoid an extreme temperature drop when blowing air of about 20 to 200 ° C. into the main combustion furnace 51 to prevent overheating in the furnace. More specifically, as shown in FIG. 3, a vertically-arranged cylindrical portion 7T (for example, an inner diameter 1500) through which melting furnace exhaust gas is circulated from the upper supply port 7i toward the lower end discharge port 7e. ˜2500 mm) and a cylindrical jacket portion 7J which is provided so as to surround the circulating exhaust gas in the cylindrical portion 7T and through which combustion air flows from the upper end supply port 7m to the lower end discharge port 7n. . For example, as shown in the drawing, the atmospheric air is directly supplied to the air preheater 7, and the supplied air flows in the jacket portion 7J in the downward direction, and the melting furnace exhaust gas flows in parallel in the cylindrical portion 7T. Is preheated to about 500 ° C. by indirect heat exchange, and then sent to the main combustion furnace 51 to suppress the furnace temperature to an appropriate temperature. This preheated air can also be supplied to the precombustion furnace 50. Further, the cooling air of about 200 ° C. taken out from the upper cooling jacket of the pre-combustion furnace 50 can be supplied to the air preheater 7 alone or in place of the air.

空気予熱器７を通過した溶融炉排ガスは、約８１１℃程度となって排ガス連通路７０を介して一段目の蒸気加熱器８に供給される。一段目の蒸気加熱器８は、空気予熱器７と基本的には同様の構造とされている。すなわち一段目の蒸気加熱器８は、図３に詳細示すように、下端供給口８ｉから上部排出口８ｅへ向けて溶融炉排ガスが流通される縦置き配置の筒状部８Ｔと、筒状部８Ｔ内の流通排ガスを取り囲むように配置され、乾燥機３から排出された蒸気が下端部供給口８ｍから上端部排出口８ｎへ向けて流通される筒状ジャケット部８Ｊとから構成されている。乾燥機３から排出された約１５０℃程度の蒸気は、ジャケット部８Ｊ内を流通する過程で、筒状部８Ｔ内を流通する溶融炉排ガスとの間接熱交換により約１８１℃程度に加熱される。一方、これにより溶融炉排ガスは約７５０度程度まで冷却される。   The melting furnace exhaust gas that has passed through the air preheater 7 reaches about 811 ° C. and is supplied to the first stage steam heater 8 via the exhaust gas communication passage 70. The first stage steam heater 8 has basically the same structure as the air preheater 7. That is, as shown in detail in FIG. 3, the first stage steam heater 8 includes a vertically disposed cylindrical portion 8 </ b> T through which melting furnace exhaust gas flows from the lower end supply port 8 i to the upper discharge port 8 e, and the cylindrical portion. It arrange | positions so that the distribution | circulation waste gas in 8T may be surrounded, and it is comprised from the cylindrical jacket part 8J through which the vapor | steam discharged | emitted from the dryer 3 distribute | circulates from the lower end part supply port 8m toward the upper end part discharge port 8n. The steam of about 150 ° C. discharged from the dryer 3 is heated to about 181 ° C. by indirect heat exchange with the melting furnace exhaust gas flowing in the cylindrical portion 8T in the process of circulating in the jacket portion 8J. . On the other hand, the melting furnace exhaust gas is cooled to about 750 degrees.

次いで本例では、一段目の蒸気加熱器８を通過した蒸気は二段目の蒸気加熱器９、三段目の蒸気加熱器１０の順に流通され、反対に溶融炉排ガスは三段目の蒸気加熱器１０、二段目の蒸気加熱器９の順に流通され、相互に逆流する形態で間接熱交換がなされるようになっている。そしてこれら二段目及び三段目の蒸気加熱器９，１０は、図３に詳細に示すように、シェル９Ｓ，１０Ｓ内に多数のチューブ９Ｔ，１０Ｔを備えたいわゆるシェルアンドチューブ式の熱交換器であり、蒸気がシェル９Ｓ，１０Ｓ内面とチューブ９Ｔ，１０Ｔ外面との間に、および溶融炉排ガスがチューブ９Ｔ，１０Ｔ内にそれぞれ流通され、その過程で蒸気が溶融炉排ガスとの間接熱交換により加熱されるようになっている。   Next, in this example, the steam that has passed through the first stage steam heater 8 is circulated in the order of the second stage steam heater 9 and the third stage steam heater 10, and conversely, the melting furnace exhaust gas is the third stage steam. The heater 10 and the second-stage steam heater 9 are circulated in this order, and indirect heat exchange is performed in such a manner that they flow backward to each other. These second-stage and third-stage steam heaters 9 and 10 are, as shown in detail in FIG. 3, a so-called shell-and-tube heat exchange having a large number of tubes 9T and 10T in the shells 9S and 10S. Steam is circulated between the inner surface of the shell 9S, 10S and the outer surface of the tubes 9T, 10T, and the melting furnace exhaust gas is circulated in the tubes 9T, 10T. In the process, the steam is indirectly heat exchanged with the melting furnace exhaust gas. Is heated by.

蒸気の流れに沿って詳説すると、先ず二段目の蒸気加熱器９に対しては、一段目の蒸気加熱器８において加熱を終えた約１８１℃程度の蒸気が蒸気連通路８０を介して、および三段目の蒸気加熱器１０において熱交換を終えた約４００℃程度の溶融炉排ガスが排ガス連通路７２を介してそれぞれ供給される。これにより、シェル９Ｓ内を流通する蒸気が、チューブ９Ｔ内を流通する排ガスとの間接熱交換により約２３２℃程度まで加熱される。また溶融炉排ガスは約２５０℃程度まで冷却される。次に、三段目の蒸気加熱器１０には、二段目の蒸気加熱器９において加熱を終えた約２３２℃程度の蒸気が蒸気連通路８１を介して、および一段目の蒸気加熱器８において熱交換を終えた約７５０℃程度の溶融炉排ガスが排ガス連通路７１を介してそれぞれ供給される。これにより、シェル１０Ｓ内を流通する蒸気が、チューブ１０Ｔ内を流通する排ガスとの間接熱交換により約３６９℃程度まで加熱される。また溶融炉排ガスは約４００℃程度まで冷却される。   To explain in detail along the flow of the steam, first, with respect to the second stage steam heater 9, the steam of about 181 ° C. that has been heated in the first stage steam heater 8 is passed through the steam communication path 80. The melting furnace exhaust gas at about 400 ° C. after the heat exchange in the third stage steam heater 10 is supplied through the exhaust gas communication path 72. Thereby, the vapor | steam which distribute | circulates the inside of the shell 9S is heated to about 232 degreeC by indirect heat exchange with the waste gas which distribute | circulates the inside of the tube 9T. The melting furnace exhaust gas is cooled to about 250 ° C. Next, in the third stage steam heater 10, the steam of about 232 ° C. that has been heated in the second stage steam heater 9 passes through the steam communication path 81 and the first stage steam heater 8. The melting furnace exhaust gas at about 750 ° C. after the heat exchange is supplied through the exhaust gas communication passage 71. Thereby, the vapor | steam which distribute | circulates the inside of the shell 10S is heated to about 369 degreeC by indirect heat exchange with the waste gas which distribute | circulates the inside of the tube 10T. The melting furnace exhaust gas is cooled to about 400 ° C.

他方、溶融炉排ガスに含まれるダストは、空気予熱器７、一段目〜３段目の蒸気加熱器８〜１０の下端部に堆積して回収され、図示しない飛灰処理設備で異物除去等の処理を行った後に安定化して外部処分するか、あるいは乾燥汚泥輸送ブロワ４の入側に戻し、乾燥汚泥に混入する。   On the other hand, the dust contained in the melting furnace exhaust gas accumulates and collects at the lower end of the air preheater 7 and the first to third steam heaters 8 to 10, and removes foreign matter etc. with a fly ash treatment facility (not shown). It stabilizes after processing, and it disposes outside or returns to the entrance side of dry sludge transport blower 4, and mixes in dry sludge.

このように、本例では溶融炉排ガスの排熱回収を順次行う複数段の熱交換器７〜１０のうち、蒸発金属の再固化によるダストが発生し易い前段側熱交換器（空気予熱器７及び一段目の蒸気加熱器８）として、前述構成の輻射式熱交換器を用いたことにより、筒状部の内周面に多少ダストが付着しても、排ガスの流通を阻害又は閉塞するような事態までは至りにくく、清掃も容易であり、かつ高温耐性も十分に確保される。しかも、単にかかる輻射式熱交換器を用いるだけでは熱交換効率が低いために排熱回収部全体の設置スペースが過大となってしまうが、本例では更に、蒸発金属によるダストが発生しにくい後段側熱交換器（二段目及び三段目の蒸気加熱器９，１０）として、単位設置面積あたりの熱交換効率が非常に高くかつ高温耐性も十分にあるシェルアンドチューブ式熱交換器を組み合わせることによって、ダストによる排ガス流通系の閉塞のおそれを少なくしながらも、排熱回収部の設置スペースを最小限に抑えることができる。   As described above, in this example, among the heat exchangers 7 to 10 that sequentially recover the exhaust heat of the melting furnace exhaust gas, the front heat exchanger (air preheater 7) that easily generates dust due to re-solidification of the evaporated metal. In addition, by using the radiant heat exchanger having the above-described configuration as the first stage steam heater 8), even if some dust adheres to the inner peripheral surface of the cylindrical portion, the flow of the exhaust gas is inhibited or blocked. It is difficult to reach a serious situation, cleaning is easy, and high temperature resistance is sufficiently secured. Moreover, simply using such a radiant heat exchanger results in a low heat exchange efficiency, and therefore the installation space of the entire exhaust heat recovery unit becomes excessive. In this example, the latter stage is further difficult to generate dust due to evaporated metal. Combined as a side heat exchanger (second and third stage steam heaters 9 and 10) is a shell and tube heat exchanger with very high heat exchange efficiency per unit installation area and sufficient high-temperature resistance As a result, it is possible to minimize the installation space of the exhaust heat recovery unit while reducing the risk of blockage of the exhaust gas circulation system due to dust.

ただし、以上のような組み合わせ構成を採用したとしても、熱交換器７〜１０内にダストが付着するのを完全に抑えることはできず、定期的な清掃が必要である。しかし清掃が必要であるとしても、複数段ある熱交換器の全てにダストが付着するのでは、清掃作業が非常に煩雑となる。そこで好適には、図４に示すように、少なくとも蒸発金属によるダストが発生し易い最上流側の熱交換器（空気予熱器７）からの排ガスを次段の熱交換器（一段目蒸気加熱器８）へ送給する排ガス連通路７０に、内部の排ガス流速がその上流側の熱交換器７よりも低速となるように、例えば排ガス流通方向に対する横断面積が上流側の熱交換器７よりも大きいダスト捕捉スペース７０Ｓ，７０Ｓを形成するのが望ましい。特に好適には、ダスト捕捉スペース７０Ｓ，７０Ｓ内における流速が、当該ダスト捕捉スペース７０Ｓ，７０Ｓよりも上流の全ての排ガス流路（すなわち本例の場合、熱交換器７、およびこれと混合冷却器５３との連通路７２）内よりも低速となるように構成するのが望ましい。このダスト捕捉スペース７０Ｓ，７０Ｓにおける流速低下度合いは、一概にはいえないが例えば約２〜５ｍ／秒であるのが望ましい。より具体的には、連通路７２内の流速が５〜１０ｍ／秒、熱交換器７内の流速が３〜６ｍ／秒、およびダスト捕捉スペース７０Ｓ内の流速が２〜５ｍ／秒となるように設計するのが望ましい。   However, even if the above combined configuration is adopted, dust cannot be completely prevented from adhering in the heat exchangers 7 to 10, and regular cleaning is required. However, even if cleaning is necessary, cleaning work becomes very complicated if dust adheres to all of the heat exchangers in a plurality of stages. Therefore, preferably, as shown in FIG. 4, the exhaust gas from the heat exchanger (air preheater 7) on the most upstream side where dust due to evaporated metal is likely to be generated is used as the heat exchanger (first stage steam heater) at the next stage. 8) In the exhaust gas communication passage 70 fed to 8), for example, the cross-sectional area with respect to the exhaust gas flow direction is higher than that of the upstream heat exchanger 7 so that the internal exhaust gas flow velocity is lower than that of the upstream heat exchanger 7. It is desirable to form large dust capture spaces 70S, 70S. Particularly preferably, the flow rates in the dust trapping spaces 70S and 70S are all exhaust gas passages upstream of the dust trapping spaces 70S and 70S (that is, in this example, the heat exchanger 7 and the mixed cooler). It is desirable that the speed is lower than that in the communication path 72) with 53. The degree of decrease in the flow velocity in the dust trapping spaces 70S and 70S cannot be generally specified, but is preferably about 2 to 5 m / second, for example. More specifically, the flow velocity in the communication path 72 is 5 to 10 m / second, the flow velocity in the heat exchanger 7 is 3 to 6 m / second, and the flow velocity in the dust trapping space 70S is 2 to 5 m / second. It is desirable to design.

これにより、最上流側の熱交換器７における冷却により発生したダストを伴う排ガスの流速が、次段への排ガス連通路７０内のダスト捕捉スペース７０Ｓ，７０Ｓにおいて低下し、そこに含まれるダストが捕捉スペース７０Ｓ，７０Ｓ内において集中的に捕捉される。よって、最上流側の熱交換器７内にはダストが多少付着するかもしれないが、当該排ガス連通路７０以降の熱交換器８〜１０内ではダストが発生・付着しにくく、流路閉塞のおそれも少なくなり、また清掃作業が著しく容易になる。   Thereby, the flow velocity of the exhaust gas accompanied by dust generated by cooling in the heat exchanger 7 on the most upstream side is lowered in the dust trapping spaces 70S and 70S in the exhaust gas communication passage 70 to the next stage, and the dust contained therein is reduced. The trapping spaces 70S and 70S are trapped in a concentrated manner. Therefore, some dust may adhere to the heat exchanger 7 on the most upstream side, but dust is less likely to be generated / attached in the heat exchangers 8 to 10 after the exhaust gas communication path 70, and the flow path is blocked. The risk is also reduced and the cleaning work is greatly facilitated.

また図示のように、空気予熱器７と蒸気加熱器８とをつなぐ横向き排ガス連通路（ダクト）７０が、一端部上壁の供給口７０ｉにおいて空気予熱器７の筒状部の下端排出口７ｅと着脱自在に接続され、他端部上壁の排出口７０ｅにおいて蒸気加熱器８の筒状部の下端供給口８ｉと接続されていると排ガス連通路７０内の清掃が容易となる利点がある。   Further, as shown in the drawing, a sideways exhaust gas communication path (duct) 70 connecting the air preheater 7 and the steam heater 8 is provided at the lower end discharge port 7e of the cylindrical portion of the air preheater 7 at the supply port 70i on the upper end wall. When the exhaust port 70e is connected to the lower end supply port 8i of the tubular portion of the steam heater 8 at the discharge port 70e on the upper wall of the other end, there is an advantage that the exhaust gas communication passage 70 can be easily cleaned. .

特に排ガス連通路７０は、図４に詳細に示すように、空気予熱器７の下端排出口７ｅと直列接続される筒状上側部分ｔ１および下端頂点部にダスト排出口ｘ１を有する円錐状下側部分ｃ１からなる入側竪型筒状部７０Ａと、蒸気加熱器８の下端供給口８ｉに直列接続される筒状上側部分ｔ２および下端頂点部にダスト排出口ｘ２を有する円錐状下側部分ｃ２からなる出側竪型筒状部７０Ｂと、入側が入側竪型筒状部７０Ａの側部に及び出側が出側竪型筒状部７０Ｂの側部にそれぞれ連通され、入側部分内の下面ｅｎが入側竪型筒状部の下端排出口ｘ１まで及び出側部分内の下面ｅｘが出側竪型筒状部の下端排出口ｘ２までそれぞれ連続的に下向き傾斜した横向きダクト部７０Ｃとを一体的に形成したものが好ましい。この排ガス連通路７０では、横向きダクト部７０Ｃ中央の縮径部ｃｅの両側全体がそれぞれダスト捕捉スペースとなる。このように構成するとで、縮径部ｃｅを除く連通路７０の略全体がダスト捕捉スペースとなるだけでなく、下側部分の略全てｃ１，ｅｎ，ｅｘ，ｃ２が下向き傾斜面で形成されるため、下面の略全体にわたり水平面がなく、流速が低下し降下したダストの略全部がいずれかの排出口ｘ１，ｘ２に滑り落ちることになる。よって、排ガス連通路７０内でのダスト捕捉能力がより高くなるとともに、降下ダストの略全てを排出口ｘ１，ｘ２に収集して排出させることができるようになる。   In particular, as shown in detail in FIG. 4, the exhaust gas communication passage 70 has a cylindrical upper portion t1 connected in series with the lower end discharge port 7e of the air preheater 7, and a conical lower side having a dust discharge port x1 at the lower end vertex. A conical lower portion c2 having an inlet side cylindrical portion 70A composed of a portion c1, a cylindrical upper portion t2 connected in series to the lower end supply port 8i of the steam heater 8, and a dust discharge port x2 at the lower end apex portion. The entrance side saddle-shaped cylindrical portion 70B is connected to the side of the entrance-side saddle-shaped cylindrical portion 70A and the exit side is connected to the side of the exit-side saddle-shaped cylindrical portion 70B. A lateral duct portion 70C in which the lower surface en is continuously inclined downward to the lower end discharge port x1 of the entry side saddle-shaped cylindrical portion and the lower surface ex in the exit side portion is continuously inclined downward to the lower end discharge port x2 of the exit side saddle-shaped cylindrical portion; Are preferably formed integrally. In the exhaust gas communication passage 70, the entire sides of the reduced diameter portion ce at the center of the lateral duct portion 70C serve as dust capturing spaces. With this configuration, not only the entire communication path 70 excluding the reduced diameter portion ce becomes a dust capturing space, but also substantially all of the lower portion c1, en, ex, c2 are formed with downward inclined surfaces. Therefore, there is no horizontal surface over substantially the entire lower surface, and almost all of the dust that has fallen due to a decrease in the flow velocity slides down to one of the discharge ports x1 and x2. Therefore, the dust capturing ability in the exhaust gas communication passage 70 is further increased, and substantially all of the descending dust can be collected and discharged at the discharge ports x1 and x2.

他方、溶融炉排ガスとの熱交換により加熱された蒸気は乾燥機３に対して循環供給される。そしてこの際、必要に応じて補助加熱器１１（間接熱交換器）において、都市ガス等の燃料を燃焼する補助炉１２からのクリーン排ガスとの熱交換により所定温度、例えば４００℃まで加熱した後に、乾燥機３に対して供給する。このため、図示しないが、乾燥機３に対して戻される蒸気の温度を測定する温度測定装置を設け、この温度測定装置による測定結果に基づいて加熱器１１へのクリーン排ガス送風量や補助炉１２の燃焼度合いを調節するように構成するのが望ましい。符号１３は、補助炉へ燃焼空気を送り込む補助炉ファンを示している。   On the other hand, the steam heated by heat exchange with the melting furnace exhaust gas is circulated and supplied to the dryer 3. At this time, if necessary, the auxiliary heater 11 (indirect heat exchanger) is heated to a predetermined temperature, for example, 400 ° C. by heat exchange with clean exhaust gas from the auxiliary furnace 12 that burns fuel such as city gas. And supplied to the dryer 3. For this reason, although not shown, a temperature measuring device for measuring the temperature of the steam returned to the dryer 3 is provided, and the amount of clean exhaust gas blown to the heater 11 and the auxiliary furnace 12 based on the measurement result by the temperature measuring device. It is desirable to configure so as to adjust the degree of combustion. Reference numeral 13 denotes an auxiliary furnace fan that feeds combustion air to the auxiliary furnace.

また図示するように、乾燥機３に対して戻される蒸気の一部を溶融炉５内に供給し、過熱防止を図るのも好適である。すなわち本例のように汚泥に蒸気を直接接触させて乾燥する場合、汚泥乾燥時の水分の蒸発により循環蒸気は経時的に増加するため、これを必要に応じて系外に排出する必要がある。他方、前述のように溶融炉５が自然放冷式の場合、過熱を防ぐためには多量の空気を炉内に供給しなければならない。しかるに、炉５内に循環蒸気の一部を吹き込むことにより、循環蒸気量の調節を行えるだけでなく、蒸気の比熱が空気の約４倍程度あるために、空気のみの場合と比較して著しく少ない吹き込み量で炉内温度を調節できるのである。また循環蒸気には多量の悪臭成分が含まれているが、溶融炉５内に吹き込まれると悪臭成分が熱分解されるという副次的な利点もある。ただし、本例のように溶融炉５内に吹き込む蒸気が低温（約３７０℃程度）の場合には、炉内温度が急激に下がり温度調節に支障が生じるので、そのような場合には図示のように予熱器７から溶融炉５内に吹き込まれる空気と混合してから炉内に吹き込むのが好ましい。本例の溶融炉５の場合、上記利点を得るためには、循環蒸気を主燃焼炉５１に吹き込みその余りを混合冷却器５３に吹き込むようにするのが望ましい。また図示しないが、循環蒸気量の調節のために、乾燥機３内圧を測定する圧力計と、この圧力計の測定結果に応じて溶融炉５へ供給する循環蒸気量を制御する手段とを設けるのが望ましい。   As shown in the drawing, it is also preferable to supply a part of the steam returned to the dryer 3 into the melting furnace 5 to prevent overheating. That is, when the steam is brought into direct contact with the sludge and dried as in this example, the circulating steam increases with time due to the evaporation of moisture during sludge drying, and therefore it is necessary to discharge it outside the system as necessary. . On the other hand, when the melting furnace 5 is a natural cooling type as described above, a large amount of air must be supplied into the furnace in order to prevent overheating. However, by blowing part of the circulating steam into the furnace 5, not only can the amount of circulating steam be adjusted, but the specific heat of the steam is about four times that of air, so it is remarkably compared to the case of air alone. The furnace temperature can be adjusted with a small amount of blowing. The circulating steam contains a large amount of malodorous components, but there is a secondary advantage that when the steam is blown into the melting furnace 5, the malodorous components are thermally decomposed. However, when the steam blown into the melting furnace 5 is at a low temperature (about 370 ° C.) as in this example, the temperature in the furnace is drastically lowered and the temperature adjustment is hindered. Thus, it is preferable to mix with the air blown into the melting furnace 5 from the preheater 7 and then blow it into the furnace. In the case of the melting furnace 5 of this example, in order to obtain the above advantages, it is desirable to blow the circulating steam into the main combustion furnace 51 and the remainder into the mixing cooler 53. Although not shown, a pressure gauge for measuring the internal pressure of the dryer 3 and means for controlling the amount of the circulating steam supplied to the melting furnace 5 according to the measurement result of the pressure gauge are provided for adjusting the amount of the circulating steam. Is desirable.

他方、蒸気との熱交換により約２５０℃程度まで冷却した溶融炉排ガスは、排ガス冷却器１００において冷却水および冷却エアの噴霧により、約２００℃程度まで冷却され、次いでバグフィルタ１０１により除塵される。またこれら排ガス冷却器１００およびバグフィルタ１０１で回収されるダストも、図示しない飛灰処理設備で異物除去等の処理を行った後に安定化して外部処分するか、あるいは乾燥汚泥輸送ブロワ４の入側に戻し、乾燥汚泥に混入する。バグフィルタ１０１を経た排ガスは、次いで排煙処理塔１０２（スクラバー）に供給され、洗浄水により洗浄集塵される。またその過程で約５０℃程度まで冷却された後、誘引ファン１０３により脱硝処理部１１０に導入される。   On the other hand, the melting furnace exhaust gas cooled to about 250 ° C. by heat exchange with steam is cooled to about 200 ° C. by spraying cooling water and cooling air in the exhaust gas cooler 100, and then removed by the bag filter 101. . The dust collected by the exhaust gas cooler 100 and the bag filter 101 is also stabilized and disposed of after being subjected to foreign matter removal or the like in a fly ash treatment facility (not shown), or on the inlet side of the dry sludge transport blower 4 And mix with dry sludge. The exhaust gas that has passed through the bag filter 101 is then supplied to the flue gas treatment tower 102 (scrubber) and cleaned and collected with cleaning water. Further, after being cooled to about 50 ° C. in the process, it is introduced into the denitration processing unit 110 by the induction fan 103.

脱硝処理部１１０は、溶融炉排ガスを脱硝予熱器（間接熱交換器）１１１において排熱との熱交換により予め２５０℃程度まで予熱し、次いで都市ガス等の燃料を用いる加熱炉１１２により約３５０℃の反応塔供給温度まで加熱した後、尿素水、エア及び希釈水等を添加して反応塔１１３内において脱硝反応による脱硝処理を行うものである。蒸気循環系の補助加熱器１１において使用したクリーン排ガスが適温（約４００℃）となっており、そのまま排出するのは不経済なのでその全部（一部でも良い）を予熱器１１１での加熱媒体として利用するのが望ましい。また図示のように脱硝処理後の排ガスも適温（約３５０℃）となるので、これと補助加熱器１１からのクリーン排ガスとを合流混合した後に予熱器１１１で用いるのも好ましい。この混合ガスは、予熱器１１１での熱交換後、煙突１１４から大気放出される。特に、このように補助加熱器１１において使用したクリーン排ガスを脱硝処理後の排ガスに混入することにより、大気放出する際の白煙の発生を防止することができる利点がある。またもちろん、補助加熱器１１からのクリーン排ガスのみ、脱硝処理済み排ガスのみ、又は他の熱源を用いることもできる。なお、符号１１５は加熱炉に空気を送り込む空気ファンを示している。   The denitration processing unit 110 preheats the melting furnace exhaust gas to about 250 ° C. in advance by heat exchange with exhaust heat in a denitration preheater (indirect heat exchanger) 111, and then heats about 350 by the heating furnace 112 using a fuel such as city gas. After heating to the reaction tower supply temperature of 0 ° C., urea water, air, dilution water, and the like are added, and denitration treatment by denitration reaction is performed in the reaction tower 113. The clean exhaust gas used in the auxiliary heater 11 of the steam circulation system has an appropriate temperature (about 400 ° C.), and it is uneconomic to discharge it as it is, so that all (or a part of) may be used as a heating medium in the preheater 111. It is desirable to use it. Further, as shown in the figure, the exhaust gas after the denitration treatment also has an appropriate temperature (about 350 ° C.), so it is also preferable to use it in the preheater 111 after this and the clean exhaust gas from the auxiliary heater 11 are mixed and mixed. The mixed gas is released into the atmosphere from the chimney 114 after heat exchange in the preheater 111. In particular, by mixing the clean exhaust gas used in the auxiliary heater 11 into the exhaust gas after the denitration treatment, there is an advantage that the generation of white smoke when released into the atmosphere can be prevented. Of course, only clean exhaust gas from the auxiliary heater 11, only denitrated exhaust gas, or other heat sources can be used. Reference numeral 115 denotes an air fan that feeds air into the heating furnace.

＜その他＞
（イ）上記例の熱交換器は４段設けられているが、熱交換機の段数は、排熱回収度合いに応じて適宜定めることができる。 <Others>
(B) Although the heat exchanger of the above example is provided in four stages, the number of stages of the heat exchanger can be appropriately determined according to the degree of exhaust heat recovery.

（ロ）また上記例の乾燥用熱媒は蒸気とされているが、本発明では他の熱媒を用いることもできる。 (B) Although the drying heat medium in the above example is steam, other heat medium may be used in the present invention.

（ハ）さらに上記例は下水汚泥の溶融処理設備であるが、本発明はこれに限定されず、含水物であれば他の廃棄物や非廃棄物などの処理にも適用でき、また溶融までは行わない焼却設備等の燃焼処理設備にも適用することができる。 (C) Further, the above example is a sewage sludge melting treatment facility, but the present invention is not limited to this, and it can be applied to treatment of other wastes and non-wastes as long as it contains water. It can also be applied to combustion treatment equipment such as incineration equipment that is not performed.

１…汚泥ピット、２…汚泥供給ポンプ、３…乾燥機、４…乾燥汚泥輸送ブロワ、５…溶融炉、６…水冷スラグコンベヤ、７…空気予熱器、８，９，１０…蒸気加熱器、１１…補助加熱器、１２…補助炉、７０，７１，７２…排ガス連通路、８０，８１…蒸気連通路、１００…排ガス冷却器、１０１…バグフィルタ、１０２…排煙処理塔、１１１…脱硝予熱器、１１２…加熱炉、１１３…反応塔、１１４…煙突。   DESCRIPTION OF SYMBOLS 1 ... Sludge pit, 2 ... Sludge supply pump, 3 ... Dryer, 4 ... Dry sludge transport blower, 5 ... Melting furnace, 6 ... Water-cooled slag conveyor, 7 ... Air preheater, 8, 9, 10 ... Steam heater, DESCRIPTION OF SYMBOLS 11 ... Auxiliary heater, 12 ... Auxiliary furnace, 70, 71, 72 ... Exhaust gas communication path, 80, 81 ... Steam communication path, 100 ... Exhaust gas cooler, 101 ... Bag filter, 102 ... Smoke treatment tower, 111 ... Denitration Preheater, 112 ... heating furnace, 113 ... reaction tower, 114 ... chimney.

Claims (3)

熱媒を乾燥熱源として含水物の乾燥を行う乾燥機と、この乾燥機により乾燥した乾燥物を燃焼する燃焼炉とを備え、前記乾燥機により使用した使用済み熱媒を前記燃焼炉の排ガスとの熱交換により加熱し、再び前記乾燥機に循環供給するように構成した含水物燃焼処理設備において、
前記使用済み熱媒と燃焼炉の排ガスとの熱交換を行う、一段目の間接熱交換器、二段目の間接熱交換器及び三段目の間接熱交換器を備え、
前記使用済み熱媒が、前記一段目の間接熱交換器、前記二段目の間接熱交換器及び前記三段目の間接熱交換器の順に流通される一方、前記燃焼炉の排ガスが前記一段目の間接熱交換器、前記三段目の間接熱交換器及び前記二段目の間接熱交換器の順に流通されるように構成された、
ことを特徴とする含水物燃焼処理設備。 A drying machine that dries the hydrated material using a heating medium as a drying heat source; and a combustion furnace that burns the dried material dried by the drying machine, and the spent heating medium used by the drying machine is an exhaust gas of the combustion furnace. In the hydrated material combustion treatment equipment configured to heat by heat exchange and to circulate and supply again to the dryer,
The first stage indirect heat exchanger, the second stage indirect heat exchanger, and the third stage indirect heat exchanger that perform heat exchange between the used heat medium and the exhaust gas of the combustion furnace,
The used heat medium is circulated in the order of the first-stage indirect heat exchanger, the second-stage indirect heat exchanger, and the third-stage indirect heat exchanger, while the combustion furnace exhaust gas is in the first-stage indirect heat exchanger. The indirect heat exchanger of the eye, the indirect heat exchanger of the third stage and the indirect heat exchanger of the second stage are configured to be distributed in this order.
A hydrated substance combustion treatment facility characterized by that. 前記熱媒が蒸気であり、前記乾燥機が蒸気と含水物とを直接接触させて乾燥を行う蒸気直接乾燥機である、請求項１記載の含水物燃焼処理設備。   The hydrate-containing combustion treatment facility according to claim 1, wherein the heat medium is steam, and the dryer is a steam direct dryer that performs drying by directly contacting the steam and the hydrated material. 熱媒を乾燥熱源として含水物の乾燥を行い、この乾燥した乾燥物を燃焼する一方で、前記乾燥に使用した使用済み熱媒を前記燃焼により生成する燃焼炉排ガスとの熱交換により加熱し、再び前記乾燥に利用するにあたり、
前記使用済み熱媒と燃焼炉の排ガスとの熱交換を行う、一段目の間接熱交換器、二段目の間接熱交換器及び三段目の間接熱交換器を用い、
前記使用済み熱媒を、前記一段目の間接熱交換器、前記二段目の間接熱交換器及び前記三段目の間接熱交換器の順に流通させる一方、前記燃焼炉の排ガスを前記一段目の間接熱交換器、前記三段目の間接熱交換器及び前記二段目の間接熱交換器の順に流通させる、
ことを特徴とする含水物燃焼処理方法。 The water-containing material is dried using a heat medium as a drying heat source, and the dried dry material is combusted, while the used heat medium used for the drying is heated by heat exchange with the combustion furnace exhaust gas generated by the combustion, In using again for the drying,
Using the first stage indirect heat exchanger, the second stage indirect heat exchanger, and the third stage indirect heat exchanger that perform heat exchange between the used heat medium and the exhaust gas of the combustion furnace,
The spent heat medium is circulated in the order of the first-stage indirect heat exchanger, the second-stage indirect heat exchanger, and the third-stage indirect heat exchanger, while the combustion furnace exhaust gas is passed through the first-stage indirect heat exchanger. Indirect heat exchanger, the third-stage indirect heat exchanger and the second-stage indirect heat exchanger in order,
A hydrated combustion method characterized by the above.
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