JPS6096825A - Incinerating method of sludge - Google Patents

Incinerating method of sludge

Info

Publication number
JPS6096825A
JPS6096825A JP58205401A JP20540183A JPS6096825A JP S6096825 A JPS6096825 A JP S6096825A JP 58205401 A JP58205401 A JP 58205401A JP 20540183 A JP20540183 A JP 20540183A JP S6096825 A JPS6096825 A JP S6096825A
Authority
JP
Japan
Prior art keywords
stage
sludge
drying
heat
furnace
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.)
Pending
Application number
JP58205401A
Other languages
Japanese (ja)
Inventor
Omiyoshi Iwasaki
岩崎　臣良
Akito Kitoin
祁答院　昭人
Etsuo Chimura
千村　悦男
Masaichi Bando
坂東　政一
Norichika Tanaka
田中　法親
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to JP58205401A priority Critical patent/JPS6096825A/en
Publication of JPS6096825A publication Critical patent/JPS6096825A/en
Pending legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treatment Of Sludge (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Incineration Of Waste (AREA)

Abstract

PURPOSE:To prevent a furnace from complex structure thereof by a method wherein the whole amount of high temperature burning gas is drawn from the burning stage of multi-stage furnace, the burning gas is treated by a high temperature oxidation deodorizing under a sufficient retention time, then the recovered heat is utilized for the predrying of sludge. CONSTITUTION:At a start-up time or the trouble of a predryer 3, sludge 2 to be incinerated is fed through a furnace top introducing port 4 of a main body 1. At a normal operation time, the sludge 2 to be incinerated is fed through a introducing port 5 at the lower part of a drying stage I via the predryer 3. A high temperature burning exhaust gas 6 is drawn from the upper part of a burning stage II, introduced to a retention chamber 7, odor contents such as CO, H2S and the like contained in the exhaust gas are treated by a high temperature oxidation deodorizing. Meanwhile, a drying air 9 is introduced to a heat exchanger 8, then the heat exchanger 8 is heated by a high temperature gas of a deodorizing agent exhausted from the retention chamber 7, the drying air 9 is heated up to the high temperature air, introduced to the predryer 3, utilized for the drying of the sludge. Thereby, a high deodorizing efficiency can be achieved.

Description

【発明の詳細な説明】 ［発明の技術分野］ 本発明は、下水処理場またはし尿処理場などで発生する
汚泥や塵芥等（汚泥類という）を焼却する方法に関する
。DETAILED DESCRIPTION OF THE INVENTION [Technical Field of the Invention] The present invention relates to a method for incinerating sludge, garbage, etc. (referred to as sludge) generated in a sewage treatment plant or human waste treatment plant.

［発明の技術的背景とその問題点］ 従来、この種の汚泥類を焼却するに当って、竪型多段焼
却炉が汎く用いられている。一方、下水汚泥の脱水に際
して、脱水ケーキのエネルギー価値を高め、あるいは投
棄場所の確保難に対処するための減容化等を目的として
、石灰系凝集剤に代って高分子凝集剤を用いることが近
年特に多くなっている。[Technical background of the invention and its problems] Conventionally, vertical multistage incinerators have been widely used to incinerate this type of sludge. On the other hand, when dewatering sewage sludge, polymer flocculants are used instead of lime-based flocculants for the purpose of increasing the energy value of the dehydrated cake or reducing the volume to cope with the difficulty of securing a dumping site. has become particularly common in recent years.

しかし、この高分子凝集剤を用いると、第１表に示すよ
うに、高分子ケーキのエネルギー価値が石灰ケーキに比
して高く焼却に当って有利である反面、焼却炉からの排
ガスの臭気濃度が、第１図に示すように２石灰ケーキを
焼却する場合より高いという問題がある。However, when this polymer coagulant is used, as shown in Table 1, the energy value of the polymer cake is higher than that of lime cake, which is advantageous for incineration, but on the other hand, the odor concentration of exhaust gas from the incinerator is However, as shown in FIG. 1, there is a problem that the amount is higher than that in the case of incinerating two lime cakes.

第１図によれば、臭気濃度は１オーダも高いことが判る
。According to FIG. 1, it can be seen that the odor concentration is one order of magnitude higher.

第１表 排ガスの脱臭を図るには、第１に特公昭Ｑ−２０５８８
号公報記載のように竪型多段焼却炉自体の構造に工夫し
たものがあるが、炉の構造が複雑になるとともに、乾燥
ゾーンが間接加熱であるため、必らずしも十分な脱臭効
果が得られない。第２に、乾燥段より排出した臭気ガス
（約２００〜４００℃）の全量を、脱臭炉において７０
０°Ｃ以上にｙ１温し、直下燃焼により高温酸化脱臭を
図る方法があるが、この方法の最大の欠点は昇温に当っ
ての燃費が嵩むことである。第３に、触媒酸化による方
法があるが、この方法は触媒層を通すため、事前に電気
集塵機で脱塵する必要があり、また脱臭温度が第２の方
法より低い約４００°Ｃ程度であるので、燃費は第２の
方法に比し節約できるが触媒層を通過させるための動力
費比は増大し、さらに、触媒は高価なものである共に、
入替補充の運転費も無視できない。Table 1 In order to deodorize exhaust gas, the first step is to use the
As described in the publication, there are some devised structures for the vertical multi-stage incinerator itself, but the structure of the furnace is complicated and the drying zone is indirectly heated, so it is not always possible to have a sufficient deodorizing effect. I can't get it. Second, the entire amount of the odor gas (approximately 200 to 400°C) discharged from the drying stage is heated to 70°C in a deodorizing furnace.
There is a method of raising the temperature y1 to 0°C or higher and performing direct combustion to achieve high-temperature oxidation and deodorization, but the biggest drawback of this method is that the fuel consumption increases when raising the temperature. Third, there is a method using catalytic oxidation, but since this method passes through a catalyst layer, it is necessary to remove dust with an electrostatic precipitator in advance, and the deodorizing temperature is about 400°C, which is lower than the second method. Therefore, fuel consumption can be saved compared to the second method, but the power cost ratio for passing through the catalyst layer increases, and furthermore, the catalyst is expensive,
Operating costs for replacement and replenishment cannot be ignored.

このように、いずれにしても従来法においては、炉から
の排出ガスの熱を回収して汚泥類の乾燥を行うことは行
われていない。そして、別途脱臭設備が不要で、燃費が
著しく低い方法についての開示もない。As described above, in any conventional method, the heat of the exhaust gas from the furnace is not recovered to dry the sludge. Furthermore, there is no disclosure of a method that does not require separate deodorizing equipment and has extremely low fuel consumption.

［発明の目的］ 本発明は、前記従来の問題点を解決するために提案され
たもので、その目的とするところは、炉の構造の複雑化
を防止し、燃費および運転費が軽減し、しがも脱臭効率
が高い汚泥類の焼却方法を提供することにある。そして
、脱臭効率の点については、臭気濃度の法規制では、工
場地帯で１０００、準工場地帯で５００　、住宅地で３
００となっているが、本発明は少なくとも３００〜５０
０以下を達成しようとしている。[Object of the Invention] The present invention was proposed in order to solve the above-mentioned conventional problems, and its purpose is to prevent the structure of the furnace from becoming complicated, reduce fuel consumption and operating costs, Another object of the present invention is to provide a method for incinerating sludge with high deodorizing efficiency. Regarding deodorization efficiency, the legal regulations regarding odor concentration are 1,000 in industrial areas, 500 in semi-industrial areas, and 3 in residential areas.
00, but the present invention provides at least 300 to 50
I'm trying to achieve 0 or less.

［発明の構成］ この１］的を達成するための第１発明は、汚泥類を竪型
多段炉で焼却するとともに、前記多段炉の燃焼段から高
温の燃焼カスを全敬抜き出し、これを十分な滞留時間を
もって高温酸化脱臭を行い、その後熱回収設備へ導き熱
回収をなし、その回収熱を汚泥類の予備乾燥用熱源とす
ることを特徴とするものである。[Structure of the Invention] A first invention for achieving the object 1 is to incinerate sludge in a vertical multi-stage furnace, extract all high-temperature combustion scum from the combustion stage of the multi-stage furnace, and thoroughly remove the high-temperature combustion scum. The system is characterized in that it performs high-temperature oxidative deodorization with a residence time of about 100 to 200 m, and then leads to a heat recovery facility to recover the heat, and uses the recovered heat as a heat source for pre-drying the sludge.

またｗｒＪ２発明は、汚泥類を竪型多段炉で焼却すると
ともに、前記多段炉の燃焼段における高温の燃焼ガスの
一部を乾燥段に通気して乾燥を行い、乾燥排ガスの実質
的に全ｔＩｉを燃焼段の下部または冷却段の上部に返送
することを連続的に行い、前記燃焼ガスの残量を抜き出
し、これを十分な滞留時間をもって高温酸化脱臭を行い
、その後熱回収設備へ導き熱回収をなし、その回収熱を
汚泥類の予備乾燥用熱源とすることを特徴とするもので
ある。In addition, the wrJ2 invention incinerates sludge in a vertical multi-stage furnace, and also ventilates a part of the high-temperature combustion gas in the combustion stage of the multi-stage furnace to a drying stage for drying, so that substantially all of the dry exhaust gas tIi The remaining amount of the combustion gas is extracted and subjected to high-temperature oxidation and deodorization with sufficient residence time, after which it is guided to a heat recovery facility for heat recovery. The feature is that the recovered heat is used as a heat source for preliminary drying of sludge.

このように、本発明は、乾燥段から排出される低温のガ
スに対して脱臭を図るものでなく、燃焼段から７００〜
９００°Ｃの高温のまま抜き出し、十分な滞留時間をも
たせて臭気成分を高温酸化脱臭させることにより、単に
滞留室を設けるのみで、特別な脱臭設備を不要とし、し
かも脱臭効果として従来と同等かそれ以上のものを得る
ものである。また幸い滞留室を出たガスは、なお高温で
あるので、その熱を熱回収設備たとえば熱交換器あるい
は廃熱ボイラーにおいて回収し汚泥類の予備乾燥機の熱
源として利用することにより、処理系全体の省エネルギ
ーを図るものである。As described above, the present invention does not aim to deodorize the low-temperature gas discharged from the drying stage, but rather deodorizes the low-temperature gas discharged from the combustion stage.
By extracting the product at a high temperature of 900°C and allowing sufficient residence time to oxidize and deodorize the odor components at high temperature, special deodorizing equipment is not required by simply providing a retention chamber, and the deodorizing effect is equivalent to that of conventional products. You get more than that. Fortunately, the gas leaving the retention chamber is still at a high temperature, so the heat can be recovered in a heat recovery device, such as a heat exchanger or waste heat boiler, and used as a heat source for the sludge pre-dryer. This aims to save energy.

さらに、熱量不足のこともある場合には、第２発明に従
って、燃焼ガスの一部を乾燥段に通風させることにより
汚泥類の乾燥を行い、乾燥排ガスは実質的に全量を燃焼
段の下部または冷却段上部に返送することにより熱量不
足を解消し、乾燥排ガス中の臭気成分を燃焼段において
高温燃焼分解させようとするものである。Furthermore, if there is a shortage of heat, the sludge is dried by ventilating a part of the combustion gas to the drying stage according to the second invention, and substantially all of the dry exhaust gas is sent to the lower part of the combustion stage or By returning the exhaust gas to the upper part of the cooling stage, the lack of heat quantity is resolved, and the odor components in the dry exhaust gas are decomposed by high-temperature combustion in the combustion stage.

なお、乾燥段および燃焼段なる語の定義として足ったも
のは現在ない。しかし、着火以前の段を乾燥段、着火・
燃焼が行なわれている段を燃焼段と通常呼ぶ。There is currently no sufficient definition of the terms drying stage and combustion stage. However, the stage before ignition is the drying stage, the ignition/
The stage in which combustion is taking place is usually called the combustion stage.

したがって、処理ケーキの水分量に応じてその境界は変
動する。ただ一般的には、５０Ｔ／Ｄ〜３００Ｔ／Ｄ処
理量の焼却炉では、８段構成の場合、乾燥段：上から４
段、燃焼段：その下２段、冷却段：下２段、また１２段
構成の場合、乾燥段ニーＬから６〜８段、燃焼段、：そ
の下２〜３段、冷却段：燃焼段の下全段程度である。Therefore, the boundary changes depending on the moisture content of the treated cake. However, in general, in incinerators with a throughput of 50T/D to 300T/D, in the case of an 8-stage configuration, drying stages: 4 from the top.
stage, combustion stage: 2 stages below, cooling stage: 2 stages below, and in case of 12 stage configuration, 6 to 8 stages from drying stage knee L, combustion stage: 2 to 3 stages below, cooling stage: combustion stage It is about the entire bottom row of .

［発明の具体例］ 次に本発明をまずｔ５２図に示す第１具体例によって説
明する。[Specific Example of the Invention] Next, the present invention will be described first with reference to a first specific example shown in diagram t52.

１は竪型多段焼却炉本体で、その構造例は前述の特公昭
４４−２０５８８号あるいは４８−３８２６９号公報等
によって公知のものであるためその詳細説明は省略する
。この本体ｌ内は上から順に乾燥段ニ、燃焼段ＩＩおよ
び冷却段■に区分できる。なお、燃料系および回転軸に
対する軸冷空気については図示を省略しである。Reference numeral 1 denotes a vertical multi-stage incinerator body, the structure of which is known from Japanese Patent Publication No. 44-20588 or Japanese Patent Publication No. 48-38269, etc., and detailed explanation thereof will be omitted. The inside of this main body 1 can be divided into a drying stage 2, a combustion stage II, and a cooling stage 2 in order from the top. Note that illustration of the fuel system and shaft cooling air for the rotating shaft is omitted.

被焼却汚泥２は、スタートアップ時または予備乾燥機３
の故障時には本体ｌの炉頂役人ＩＴＪ　４から投入され
るが、通常運転時にはｐ備乾燥機３を経て乾燥段ニド部
の投入１」５から投入される。燃焼段ＩＩ上部からは７
００〜８００℃通常７５０〜８００°Ｃの高温燃焼排ガ
ス６が抜き出され、滞留室７に導かれ、ここで０．５秒
以上かつ８００〜８００°Ｃの状態を保つことによって
、排ガス申のＣＯやＨ２Ｓ等の臭気成分が高温酸化脱臭
される。その脱臭済ガスは熱交換器８を経て、２００〜
５００℃まで温度低下しガス処理設備としての吸収冷却
塔および電気集塵機を順に通った後、誘引送風機により
煙突から排出される（後工程についてはいずれも図示せ
ず）。一方、熱交換器８には乾燥用空気９が通され、滞
留室７から排出された脱臭済の高温カスにより加熱され
、自らは高温空気となって予備乾燥機３へ与えられ、汚
泥の乾燥に用いられる。乾燥に供せられた使用済空気ｌ
Ｏは除湿器１１において除湿が図られた後、再び熱交換
器８へ戻り循環使用されるようになっている。１２は新
低温空気で、除湿器１１の出側に吹込まれる。乾燥用循
環空気の一部は熱交換器８の入側および／または出側に
おいて分岐され燃焼用空気１３Ａ、ｉａＢとして燃焼段
Ｈの下部に吹込まれる。この吸込は、比較的温度の高い
空気を燃焼用として用いることができるとともに、循環
空気のダスト等の法線を防止するために行なわれる。The incinerated sludge 2 is collected at startup or in the pre-dryer 3.
In the event of a failure, it is fed from the furnace top official ITJ 4 of the main body 1, but during normal operation, it is fed from the feed 1'5 of the drying stage nid section via the dryer 3. 7 from the top of combustion stage II
00 to 800°C High-temperature combustion exhaust gas 6, normally 750 to 800°C, is extracted and guided to a retention chamber 7, where it is kept at a temperature of 800 to 800°C for 0.5 seconds or more to reduce the amount of exhaust gas. Odor components such as CO and H2S are deodorized by high temperature oxidation. The deodorized gas passes through a heat exchanger 8,
After the temperature drops to 500° C. and passes through an absorption cooling tower and an electrostatic precipitator as gas processing equipment, it is discharged from the chimney by an induced blower (none of the post-processes are shown). On the other hand, drying air 9 is passed through the heat exchanger 8, heated by the deodorized high-temperature scum discharged from the retention chamber 7, and turned into high-temperature air and supplied to the pre-dryer 3 to dry the sludge. used for. Used air used for drying l
After the O is dehumidified in the dehumidifier 11, it returns to the heat exchanger 8 and is used for circulation. 12 is fresh low-temperature air, which is blown into the outlet side of the dehumidifier 11. A portion of the drying circulating air is branched at the inlet and/or outlet side of the heat exchanger 8 and blown into the lower part of the combustion stage H as combustion air 13A, iaB. This suction is performed so that relatively high-temperature air can be used for combustion, and at the same time, to prevent dust and the like from entering the circulating air.

また通常は、燃焼ガスの全量を抜き出して滞留室７へそ
のまま導くが、汚泥の種別によって熱量不足を生しるこ
とがある。この場合、乾燥段Ｉでの乾燥を十分に行うべ
く、燃焼カスの一部を乾燥段Ｉに通気し、汚泥の乾燥を
行い、炉頂から抜き出し、循環ファン１４により循環路
１５を通して燃焼段ＩＩの下部（図示例）または冷却段
ＩＩＩ」二部へ連続的に返送するようにる。返送ガスは
燃焼段ＩＩにて脱臭が図られる。勿論、この場合も乾燥
段ＩＩ　ｌ一部から抽気するが、この抽気量と循環路１
５を通る＠環量とは汚泥の種別や性状により適宜決定さ
れる。Further, normally, the entire amount of combustion gas is extracted and guided directly to the retention chamber 7, but depending on the type of sludge, a lack of heat may occur. In this case, in order to sufficiently dry the drying stage I, a part of the combustion sludge is vented to the drying stage I, the sludge is dried, and the sludge is extracted from the furnace top and passed through the circulation path 15 by the circulation fan 14 to the combustion stage II. (in the illustrated example) or to the second part of Cooling Stage III. The return gas is deodorized in combustion stage II. Of course, in this case as well, air is extracted from a portion of the drying stage II, but the amount of air extracted and the circulation path 1
The amount of @ ring passing through 5 is appropriately determined depending on the type and properties of the sludge.

第２図は第２具体例を示したもので、上記例と異なる所
は、脱臭剤ガスを廃熱ボイラー１６に通して熱回収を図
り、蒸気１７として乾燥機３へその熱源として供給する
ものである。また燃焼用空気１３Ｇは、新低温空気１２
を予熱器１８により予熱して得る。予熱器１８の熱源は
、熱回収蒸気から得ればよい。熱量不足の場合、前記例
と同様に乾燥済ガスの循環に加えて、専焼ボイラー１８
による熱を与えることができる。FIG. 2 shows a second specific example, which differs from the above example in that the deodorizing gas is passed through a waste heat boiler 16 to recover heat and is supplied as steam 17 to the dryer 3 as a heat source. It is. Also, the combustion air 13G is the new low temperature air 12
is obtained by preheating with the preheater 18. The heat source for the preheater 18 may be obtained from heat recovery steam. In case of insufficient heat, in addition to circulating the dried gas as in the previous example, the dedicated boiler 18
can provide heat.

このように、炉頂からの＋ＪＩガスに対して脱臭処理を
行うのではなくして、燃焼段上部から抜き出した燃焼ガ
スに対して脱臭処理に行うものであるため、燃焼ガスが
７００〜８００℃の高温であるから、特別の脱臭炉は不
要で単に十分な滞留時間を確保するための滞留室を設け
るのみで、高温酸化脱臭が可能であり、処理設備が安価
であり、しかも所望の脱臭効果を得ることができる。さ
らに、脱臭後の排ガスを乾燥用熱源として回収するもの
であるから、処理系全体の燃料もしくは電力消費量が著
しく少くて済む。In this way, instead of deodorizing the +JI gas from the top of the furnace, the deodorizing process is performed on the combustion gas extracted from the upper part of the combustion stage. Since the temperature is high, there is no need for a special deodorizing furnace, and high-temperature oxidation deodorization is possible by simply providing a retention chamber to ensure sufficient residence time.The treatment equipment is inexpensive, and the desired deodorizing effect can be achieved. Obtainable. Furthermore, since the exhaust gas after deodorization is recovered as a heat source for drying, the fuel or power consumption of the entire treatment system can be significantly reduced.

他方、熱量不足の場合、燃焼ガスの一部を乾燥段に通気
し乾燥を行うことによりこれを解消でき、しかも燃焼段
の下部または冷却段上部に戻すべく循環させるので、燃
焼段にて高温燃焼分解させ脱臭を図ると、脱臭と熱量不
足の解消とを同時に達成できる。On the other hand, in the case of insufficient heat, this can be resolved by drying a portion of the combustion gas by ventilating it into the drying stage.In addition, it is circulated back to the lower part of the combustion stage or the upper part of the cooling stage, so that high-temperature combustion can be achieved in the combustion stage. By decomposing and deodorizing, it is possible to simultaneously achieve deodorization and resolving the lack of heat.

［実施例］ 次に実施例を示す。[Example] Next, examples will be shown.

（実施例１） 外形２３６０ｍ／ｍ　＋段数８段のＩＯＴ／日　竪型多
段炉において、含水率７８ｚ９発熱量４３００ｋｃａ　
ｌ／ｋｇ−固形物ノスラッジを全量抽気により脱臭後７
００〜θ００°Ｃの燃焼排ガスを３００℃まで木管ボイ
ラー（蒸気発生量３００　ｋｇ／Ｈ）にて熱回収し、熱
回収された７　ｋｇ／ｃｒｎ’蒸気をＩＯＴ／１Ｊ−伝
熱式低速型乾燥機に供給し、スラッジ水分を３０２まで
乾燥させて、そのドレンを４　ｋｇ／ｃｒｎ’でボイラ
ーに戻した。乾燥後のスラッジを炉の４段目より投入し
焼却したものと従来の直ド脱臭法（すなわち、４０’Ｏ
まで冷却し排煙処理した拮ガスを直下脱臭後の排ガスと
熱交換し、５００°Ｃまで１温したのち、八−すにより
７５０°Ｃまでｙ１温し脱臭する）との比較を第１表に
示す。(Example 1) External diameter 2360 m/m + number of stages IOT/day 8 stages Vertical multi-stage furnace, moisture content 78z9 calorific value 4300 kca
l/kg - After deodorizing the solid nosludge by extraction with air 7
Heat is recovered from the combustion exhaust gas at 00 to θ00°C to 300°C using a wood tube boiler (steam generation amount: 300 kg/H), and the recovered 7 kg/crn' steam is subjected to IOT/1J-heat transfer low-speed drying. The sludge was fed to the boiler, the sludge moisture was dried to 302, and the condensate was returned to the boiler at 4 kg/crn'. The dried sludge was charged into the fourth stage of the furnace and incinerated, and the conventional direct deodorization method (i.e., 40'O
Table 1 shows a comparison between the following gases, which have been cooled to 750°C and then treated with the exhaust gas directly under deodorization. Shown below.

第　１　表 （実施例２） 外径２３Ｈｍ／ｍ　、段数８段のＩＯＴ／日　竪型多段
炉において含水率７８χ９発熱量４３００ｋｃａｌ／ｋ
ｇ−ｄｓ＋７）　スラッジを全量抽気により脱臭後？０
０〜ｓｏｏ’ｃの燃焼排ガスを３０Ｏ℃まで熱交換によ
り熱回収し、熱回収されたｅｏｏ’ｃ空気を直接乾燥機
に供給し、スラッジ水分を３０１まで乾燥させる。乾燥
後の水分を多量に含んだ１５０　℃の空気を４０°Ｃま
で冷却し、除湿した。除湿後の空気の一部を炉に供給し
、不足分を大気でおぎない、混合空気を再度、直接乾燥
機用熱源として利用する。乾燥後のスラッジは具体例１
と同様に炉に投入し、従来の直下脱臭法との比較を第２
表に示す。Table 1 (Example 2) IOT/day with outer diameter 23 Hm/m and number of stages 8, water content 78χ9 calorific value 4300 kcal/k in vertical multi-stage furnace
g-ds+7) After deodorizing the entire sludge by extraction? 0
Heat is recovered from the combustion exhaust gas of 0 to soo'c to 300C by heat exchange, and the heat-recovered eoo'c air is directly supplied to the dryer to dry the sludge moisture to 301C. After drying, the air at 150°C containing a large amount of moisture was cooled to 40°C and dehumidified. A portion of the air after dehumidification is supplied to the furnace, the shortage is filled with air, and the mixed air is directly used as a heat source for the dryer. Specific example 1 is the sludge after drying.
was placed in the furnace in the same way, and compared with the conventional direct deodorization method.
Shown in the table.

第２表 〔発明の効果〕 以上の通り、本発明によれば、１税臭に当って単純な構
成により経／／ｆ的に、しかも高い効率をもって脱臭を
行うことができ、さらに熱回収を行うことにより系全体
の省エネルギー化を達成できる。Table 2 [Effects of the Invention] As described above, according to the present invention, it is possible to deodorize one odor with a simple structure and with high efficiency, and also to recover heat. By doing so, it is possible to achieve energy savings for the entire system.

【図面の簡単な説明】[Brief explanation of drawings]

第１図は竪型多段焼却炉による石灰ケーキと高分子凝集
ケーキとの焼却υ１ガスの臭気濃度の比較を示す相関図
、第２図および第３図は本発明の具体例を示す概略図で
ある。 ■・・・炉本体　２　、、、、汚泥 ３　、、、、乾燥器　６−、、、高温燃焼排ガス７　、
、、、滞留室　８．、、、、熱交換器１５、、、、循環
路　１Ｂ、、、、廃熱ボイラー特許出願人　岩　崎　臣
　良Figure 1 is a correlation diagram showing a comparison of the odor concentration of incinerated υ1 gas between lime cake and polymer agglomerated cake in a vertical multistage incinerator, and Figures 2 and 3 are schematic diagrams showing specific examples of the present invention. be. ■... Furnace main body 2, ..., sludge 3, ..., dryer 6-, ..., high-temperature combustion exhaust gas 7,
,,,retention chamber 8. , Heat exchanger 15, Circulation path 1B, Waste heat boiler patent applicant Yoshi Iwasaki

Claims (2)

【特許請求の範囲】[Claims] （１）汚泥類を竪型多段炉で焼却するとともに前記多段
炉の燃焼段から高温の燃焼ガスを全量抜き出し、これを
十分な滞留時間をもって高温酸化脱臭を行い、その後熱
回収設備へ導き熱回収をなし、その回収熱を汚泥類の予
備乾燥用熱源とすることを特徴とする汚泥類の焼却方法
。(1) The sludge is incinerated in a vertical multi-stage furnace, and the entire amount of high-temperature combustion gas is extracted from the combustion stage of the multi-stage furnace, subjected to high-temperature oxidation and deodorization with sufficient residence time, and then guided to heat recovery equipment for heat recovery. A method for incinerating sludge, characterized in that the recovered heat is used as a heat source for preliminary drying of sludge. （２）汚泥類を竪型多段炉で焼却するとともに前記多段
炉の焼却段における高温の燃焼ガスの一部を乾燥段に通
気して乾燥を行い、乾燥排ガスの実質的に全量を燃焼段
の下部または冷却段上部に返送することを連続的に行い
、前記燃焼ガスの残量を抜き出し、これを十分な滞留時
間をもって高温酸化脱臭を行い、その後熱回収設備へ導
き熱回収をなし、その回収熱を汚泥類の予備乾燥用熱コ
；（とすることを特徴とする汚泥類の焼却方法。(2) The sludge is incinerated in a vertical multi-stage furnace, and a part of the high-temperature combustion gas in the incineration stage of the multi-stage furnace is vented to the drying stage for drying, and substantially all of the dry exhaust gas is transferred to the combustion stage. The residual amount of the combustion gas is extracted by continuously returning it to the lower part or the upper part of the cooling stage, and it is subjected to high-temperature oxidation and deodorization with sufficient residence time, and then guided to a heat recovery equipment for heat recovery. A method for incinerating sludge, characterized in that heat is applied to a heating device for pre-drying sludge.
JP58205401A 1983-10-31 1983-10-31 Incinerating method of sludge Pending JPS6096825A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP58205401A JPS6096825A (en) 1983-10-31 1983-10-31 Incinerating method of sludge

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP58205401A JPS6096825A (en) 1983-10-31 1983-10-31 Incinerating method of sludge

Publications (1)

Publication Number Publication Date
JPS6096825A true JPS6096825A (en) 1985-05-30

Family

ID=16506218

Family Applications (1)

Application Number Title Priority Date Filing Date
JP58205401A Pending JPS6096825A (en) 1983-10-31 1983-10-31 Incinerating method of sludge

Country Status (1)

Country Link
JP (1) JPS6096825A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02192506A (en) * 1989-01-21 1990-07-30 Ngk Insulators Ltd Combustion control method for multistage incinerator
US7695701B2 (en) 2008-03-07 2010-04-13 Du Pont Process for treating acid gas in staged furnaces with inter-stage heat recovery
JP4755250B2 (en) * 2005-06-21 2011-08-24 中国科学院工程熱物理研究所 Combined dryer, wet sludge incineration apparatus with combined dryer, and method thereof

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS454000Y1 (en) * 1969-06-19 1970-02-24
JPS56133522A (en) * 1980-03-22 1981-10-19 Kawasaki Heavy Ind Ltd Method and device for burning of sludge in multistage incinerator

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS454000Y1 (en) * 1969-06-19 1970-02-24
JPS56133522A (en) * 1980-03-22 1981-10-19 Kawasaki Heavy Ind Ltd Method and device for burning of sludge in multistage incinerator

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02192506A (en) * 1989-01-21 1990-07-30 Ngk Insulators Ltd Combustion control method for multistage incinerator
JP4755250B2 (en) * 2005-06-21 2011-08-24 中国科学院工程熱物理研究所 Combined dryer, wet sludge incineration apparatus with combined dryer, and method thereof
US7695701B2 (en) 2008-03-07 2010-04-13 Du Pont Process for treating acid gas in staged furnaces with inter-stage heat recovery

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