JP3037457B2 - Drying and incineration of hydrated solids - Google Patents
Drying and incineration of hydrated solidsInfo
- Publication number
- JP3037457B2 JP3037457B2 JP9856991A JP9856991A JP3037457B2 JP 3037457 B2 JP3037457 B2 JP 3037457B2 JP 9856991 A JP9856991 A JP 9856991A JP 9856991 A JP9856991 A JP 9856991A JP 3037457 B2 JP3037457 B2 JP 3037457B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized
- dryer
- incinerator
- heat medium
- drying
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Landscapes
- Gasification And Melting Of Waste (AREA)
- Drying Of Solid Materials (AREA)
- Processing Of Solid Wastes (AREA)
- Treatment Of Sludge (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、たとえば石炭、褐炭、
活性炭、下水汚泥、特殊産業排水よりなる汚泥あるいは
都市ゴミ等の含水固形物の乾燥・焼却方法に関する。The present invention relates to, for example, coal, lignite,
The present invention relates to a method for drying and incinerating sludge comprising activated carbon, sewage sludge, special industrial wastewater, or hydrated solids such as municipal waste.
【０００２】[0002]
【従来の技術】従来より、この種の汚泥等の含水固形分
の焼却方法について大別すると、汚泥を予備乾燥させて
これを焼却炉へ供給するものと、予備乾燥させることな
く直接的に汚泥を焼却するものとに分けられる。前者の
予備乾燥方式による場合には、焼却前に水分を蒸発させ
るため、焼却炉内で水分の蒸発のために燃焼温度を上げ
る必要がなくなり、焼却炉体が小さくて済むとともに、
設備費や消費助燃料費が低減され、しかも発生ガス量が
多いため排熱回収用の熱交換器の容量が少なくて済むと
いう利点がある。しかし、予備乾燥するための乾燥機を
内蔵または別個に設置する必要があり、その設備費およ
び処理費が嵩むという難点があった。また、たとえば焼
却炉より発生する熱風を用いた廃熱ボイラー、あるいは
焼却炉に取付けられたボイラーより発生する蒸気もしく
は高温熱媒体によって汚泥を予備乾燥する場合には、乾
燥操作として間接加熱型となるため、前記乾燥機および
ボイラーのそれぞれに大きな伝熱面を設けなければなら
ず、その設備費が極めて高いなどの問題を有していた。2. Description of the Related Art Conventionally, methods for incinerating this kind of water-containing solids such as sludge are roughly classified into two types: sludge preliminarily dried and supplied to an incinerator, and sludge directly without predrying. Is incinerated. In the case of the former pre-drying method, since the water is evaporated before incineration, there is no need to raise the combustion temperature for evaporating the water in the incinerator, and the incinerator body can be small,
There is an advantage that the equipment cost and auxiliary fuel cost are reduced, and the amount of generated gas is large, so that the capacity of the heat exchanger for exhaust heat recovery can be reduced. However, it is necessary to incorporate a dryer for pre-drying or to install the dryer separately, and there is a problem that the equipment cost and the processing cost increase. Further, for example, when pre-drying sludge with a waste heat boiler using hot air generated from an incinerator or steam or a high-temperature heat medium generated from a boiler attached to an incinerator, an indirect heating type is used as a drying operation. Therefore, a large heat transfer surface must be provided in each of the dryer and the boiler, and there is a problem that the equipment cost is extremely high.
【０００３】そのため、本願出願人は、先の特開昭５７
−５６０９６号公報において、流動焼却炉からの排ガス
中の高温焼却灰をサイクロンで捕集し、この高温焼却灰
をパドルミキサー等の混合乾燥機に導き、湿潤汚泥と混
合することにより、前記高温焼却灰の保有熱を利用して
水分を蒸発させる方法を開示した。[0003] For this reason, the applicant of the present application has disclosed in
In JP-A-56096, high-temperature incineration ash in flue gas from a fluidized incinerator is collected by a cyclone, and the high-temperature incineration ash is guided to a mixing dryer such as a paddle mixer and mixed with wet sludge to thereby form the high-temperature incineration. A method for evaporating water by using the heat of ash has been disclosed.
【０００４】[0004]
【発明が解決しようとする課題】しかしながら、前述特
開昭５７−５６０９６号公報の焼却方法においても、熱
媒体と汚泥とを直接接触させる機械的な攪拌混合を行っ
ているため、たとえば熱媒体として珪砂などの硬度の高
いものを使用した場合には、攪拌翼が激しく摩耗し、交
換のための維持管理費が嵩むなどの問題がある。また、
攪拌機構により湿潤物質を乾燥する場合には、しばしば
塊状となる傾向にあるため、前記乾燥機に加え粉砕機を
必要とする場合が多く、その設備費が必要になるととも
に、前記粉砕機においても前記乾燥機と同様に汚泥中に
混入している土砂によって粉砕機のロールあるいはイン
ペラが激しく摩耗されるため、交換のための維持費が嵩
むなどの問題がある。However, in the incineration method disclosed in Japanese Patent Application Laid-Open No. 57-56096, mechanical stirring and mixing in which the heat medium and the sludge are brought into direct contact are performed. When a material having a high hardness such as silica sand is used, there is a problem that the stirring blade is severely worn and maintenance cost for replacement is increased. Also,
When the wet substance is dried by the stirring mechanism, it often tends to be agglomerated, so that in many cases, a pulverizer is required in addition to the dryer. As in the case of the dryer, the rolls or impellers of the crusher are severely worn by the earth and sand mixed in the sludge, so that there is a problem that maintenance costs for replacement are increased.
【０００５】さらに、供給汚泥物の中には乾燥すれば、
発火ないしは爆発し易いものが含まれる場合があるた
め、機械的な攪拌混合による乾燥方式では、攪拌の際
に、熱媒体との衝突による火花または摩擦による加熱な
どに触発されて発火や爆発が起こる危険性がある。そこ
で、本発明の主たる目的は、基本的に間接加熱型乾燥
機、廃熱ボイラー、混合乾燥機および粉砕機等の諸設備
を不要とし、設備費およびその維持費の低減を図るとと
もに、発火や爆発の危険性を無くし、安定的な操業が可
能な含水固形物の焼却方法を提供するものである。[0005] Furthermore, if the supplied sludge is dried,
Since there is a case where something that easily ignites or explodes may be included, in the drying method using mechanical stirring and mixing, ignition or explosion occurs due to sparks due to collision with a heat medium or heating due to friction during stirring. There is a risk. Therefore, a main object of the present invention is to basically eliminate the need for various equipment such as an indirect heating dryer, a waste heat boiler, a mixing dryer and a crusher, reduce the equipment cost and the maintenance cost thereof, and reduce ignition and ignition costs. An object of the present invention is to provide a method for incineration of hydrated solid matter, which eliminates the danger of explosion and enables stable operation.
【０００６】[0006]
【課題を解決するための手段】前記課題は、熱媒体が流
動化している流動乾燥機に含水固形物を投入し、流動化
している熱媒体との接触により前記含水固形物の乾燥を
行った後、この乾燥された固形物を前記熱媒体とともに
高速流動焼却炉に送給し、この高速流動焼却炉において
前記固形物の焼却を行うとともに、高速流動焼却炉の排
ガス中の前記熱媒体を前記高速流動焼却炉へ返送して循
環させるとともに、その一部を前記流動乾燥機へ循環さ
せることで解決できる。The object of the present invention is to solve the problem that a heat medium flows.
Add water-containing solids to fluidized dryer
After drying of the water-containing solids by contact with the heating medium that, this dried solid feed in fast fluidized incinerator with the heating medium feeds, of the solids in the fast fluidized incinerator performs incineration, with the heat medium in the exhaust gas of the fast fluidized incinerator circulating and return to the fast fluidized incinerator, can be solved by circulating a part to the fluidized bed dryer.
【０００７】また、発火または爆発し易い含水固形物の
場合には、流動乾燥機の流動用気体として、湿潤空気ま
たは過熱蒸気を用いるものである。In the case of a hydrated solid which easily ignites or explodes, humid air or superheated steam is used as a flowing gas for a fluidized dryer.
【０００８】[0008]
【作用】本発明においては、流動乾燥機により事前に含
水固形分の水分が除去されるため、水分の蒸発のために
焼却炉内の燃焼温度を上げる必要がなくなり、焼却炉体
が小さくて済むとともに、設備費や消費助燃料費が低減
され、熱回収効率が向上する。また、廃熱ボイラー、そ
の他の間接加熱型乾燥機に比べて大きな伝熱面が不用と
なり設備費およびその運転のための維持費が低減する。According to the present invention, since the water content of the water-containing solid is removed in advance by the fluidized drier, there is no need to raise the combustion temperature in the incinerator for evaporating the water, and the incinerator body can be small. At the same time, equipment costs and auxiliary fuel costs are reduced, and heat recovery efficiency is improved. Further, compared with a waste heat boiler and other indirect heating type dryers, a large heat transfer surface is not required, and equipment costs and maintenance costs for the operation thereof are reduced.
【０００９】流動乾燥機においては、流動用気体により
熱媒体が激しく運動しており、通常は投入される含水固
形物は前記熱媒体との衝突・摩擦により乾燥とともに粉
砕もなされる。前記流動層における混合攪拌により含水
固形物が粉砕されない場合には、流動乾燥機の流動層に
粉砕媒体を別途投入し含水固形物の粉砕を行うこともで
きる。In a fluidized-bed dryer, a heating medium is violently moved by a flowing gas, and usually, a hydrated solid material is dried and crushed by collision and friction with the heating medium. When the hydrated solid is not pulverized due to the mixing and stirring in the fluidized bed, a pulverizing medium may be separately added to the fluidized bed of the fluidized dryer to pulverize the hydrated solid.
【００１０】含水固形物に乾燥により発火・爆発し易い
物質が混入している場合には、流動乾燥機に供給する流
動用気体を湿潤空気または過熱蒸気を用いることで乾燥
機内を一定の湿度状態に保持し得るため、発火・爆発を
防止することができる。[0010] When a substance which easily ignites or explodes due to drying is mixed in the hydrated solid, the flowing gas supplied to the fluidized dryer is moist air or superheated steam to keep the inside of the dryer at a constant humidity. Can be prevented, so that ignition and explosion can be prevented.
【００１１】なお、前記流動乾燥機に供給される流動用
気体は、流動乾燥機の排ガスを循環利用することとすれ
ば、より維持費の低減が図れる。[0011] If the fluid gas supplied to the fluidized dryer is circulated using the exhaust gas of the fluidized dryer, the maintenance cost can be further reduced.
【００１２】以上のように、本発明では、含水固形物は
流動乾燥機と高速流動焼却炉とを巧妙に組み合わせたこ
とにより、効率の良い安定した操業を行うことができ
る。なお、本発明に係る焼却システムの流動乾燥機を熱
分解炉として使用することもできる。As described above, according to the present invention, efficient and stable operation of the hydrated solid can be performed by using a fluidized dryer and a high-speed fluidized incinerator. In addition, the fluidized dryer of the incineration system according to the present invention can be used as a pyrolysis furnace.
【００１３】[0013]
【実施例】以下、本発明を図１に示す具体例に基づき詳
説する。本発明における焼却システムは、高速高速流動
焼却炉１と流動乾燥機１１とが並列的に配設されてお
り、両者が連係した一連の乾燥・焼却工程プロセスが構
成されている。前記高速流動焼却炉１は、その下部に流
動用空気導入口２が設けられるとともに、前記流動用空
気導入口２の若干上方に焼却炉内での燃焼を完全にする
ための二次空気導入口３が設けられ、通常粒子の終末速
度付近で運転されている。また、後述する流動乾燥機１
１において乾燥された処理原料を熱媒体とともに供給す
るために前記流動乾燥機１１と連絡する原料移送管４、
および後述する主サイクロン７からの熱媒体を循環させ
るための戻り管５が接続されている。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described below in detail with reference to a specific example shown in FIG. In the incineration system according to the present invention, a high-speed and high-speed fluidized-bed incinerator 1 and a fluidized-bed dryer 11 are arranged in parallel, and a series of drying and incineration step processes in which both are linked to each other are configured. The high-speed fluidized incinerator 1 is provided with a flowing air inlet 2 at a lower portion thereof, and a secondary air inlet slightly above the flowing air inlet 2 for complete combustion in the incinerator. 3 are usually operated near the end velocity of the particles. In addition, a fluid dryer 1 described below.
A raw material transfer pipe 4 communicating with the fluidized drier 11 to supply the processing raw material dried in 1 with a heat medium;
Further, a return pipe 5 for circulating a heat medium from a main cyclone 7 described later is connected.
【００１４】また、図２に示されるように、処理原料が
細粒になり飛散する場合には、流動乾燥機１１に取付け
られた副サイクロン１３で熱媒体とともに処理原料も多
く捕集されるため、この細粒化された処理原料を前記高
速流動焼却炉１に移送するための原料副移送管１４Ｂを
設ける。前記高速流動焼却炉１の上部には、主サイクロ
ン７と連通する排ガス管６が設けられており、この排ガ
ス管６を通って前記主サイクロン７に導入する排ガス中
から熱媒体が捕集され、捕集された熱媒体が前記戻り管
５により高速流動焼却炉１の流動層に再び供給される循
環路が形成されている。前記戻り管５の中間にはシール
バルブ８が形成されるとともに、その下流側に分配器９
が設けられており、この分配器９から分岐して、熱媒体
の一部を流動乾燥機１１に熱媒体を循環させるための戻
り枝管１０が設けられている。なお、前記主サイクロン
７により分離されたガスは、排ガス処理設備２４に送ら
れ、ここで熱交換器による熱回収が図られるなどして、
ダストコレクタースクラバー、ブロアーを経て外気に放
出される。Further, as shown in FIG. 2, when the processing raw material becomes fine particles and scatters, a large amount of the processing raw material is collected together with the heat medium by the auxiliary cyclone 13 attached to the fluidized dryer 11. A raw material sub-transfer pipe 14B for transferring the finely divided processing raw material to the high-speed fluidized incinerator 1 is provided. An exhaust gas pipe 6 communicating with the main cyclone 7 is provided at an upper part of the high-speed fluidized incinerator 1, and a heat medium is collected from exhaust gas introduced into the main cyclone 7 through the exhaust gas pipe 6, A circulation path is formed in which the collected heat medium is again supplied to the fluidized bed of the high-speed fluidized-bed incinerator 1 by the return pipe 5. A seal valve 8 is formed in the middle of the return pipe 5 and a distributor 9 is provided downstream thereof.
There is provided a return branch pipe 10 which branches off from the distributor 9 and circulates a part of the heat medium to the fluidized dryer 11. The gas separated by the main cyclone 7 is sent to an exhaust gas treatment facility 24, where heat is recovered by a heat exchanger.
It is released to the outside air via a dust collector scrubber and a blower.
【００１５】一方、流動乾燥機１１は、前述した高速流
動焼却炉１との原料移送管４および熱媒体の戻り枝管１
０が接続されている。さらに流動乾燥機１１の下部に
は、流動化のための気体を供給する流動用気体導入管１
８が設けられるとともに、その胴部中間には処理原料を
投入する原料投入管１５が設けられている。また、流動
乾燥機１１の上部には排ガス管１２が接続され副サイク
ロン１３と連通しており、前記副サイクロン１３により
捕集された熱媒体が戻り管１４により流動乾燥機１１の
下部の流動層形成部分に再び供給される熱媒体の循環路
が形成されている。On the other hand, the fluidized drier 11 is provided with a raw material transfer pipe 4 for the high-speed fluidized incinerator 1 and a return branch pipe 1 for the heat medium.
0 is connected. Further, at the lower part of the fluidizing dryer 11, a fluidizing gas introducing pipe 1 for supplying fluidizing fluid is provided.
8 is provided, and a material input pipe 15 for inputting a processing material is provided in the middle of the body. An exhaust gas pipe 12 is connected to the upper part of the fluidized dryer 11 and communicates with the sub-cyclone 13. The heat medium collected by the sub-cyclone 13 is returned to the fluidized bed at the lower part of the fluidized dryer 11 by the return pipe 14. A circulation path of the heat medium to be supplied again to the formation portion is formed.
【００１６】前述したように、処理原料が細粒になり飛
散する場合には、図２に示されるように、前記副サイク
ロン１３からの戻り管に分配器９Ａを設け、前述した原
料副移送管１４Ｂと、熱媒体を再び流動乾燥機１１に循
環させるための戻り管１４Ａとに分岐し、副サイクロン
１３によって捕集される原料を前記副移送管１４Ｂを通
じて高速流動焼却炉１に送給する。なお、８Ｂは、前述
主サイクロン７の場合と同様のシールバルブである。前
記副サイクロン１３により分離されたガスは、循環ダク
ト１６により清浄塔１７に送られ、ここで洗浄された
後、連通する前記流動用気体導入管１８を経て、ブロワ
ー１９および加熱器２０により圧縮・加熱されて熱媒体
の流動用気体として流動乾燥機１１に供給される。前記
清浄塔１７においては、ポンプ２２および冷却器２１を
経て冷却水が循環する循環路が形成されており、前記清
浄塔１７に導入されるガスの温度を下げて、ここで蒸発
する水分を凝縮させることにより流動乾燥機１１に送る
気体を湿潤化している。ここで発生する余剰水分につい
ては水パージライン２６を経て外部に排水される。ま
た、流動用気体導入管１８の中間から分岐するガスパー
ジライン２５は、分解ガスをガスタービン等に利用する
場合や脱臭装置へガスを送る必要がある場合に使用され
る。As described above, when the processing raw material becomes fine particles and scatters, as shown in FIG. 2, a distributor 9A is provided in the return pipe from the sub cyclone 13, and the raw material sub-transfer pipe is provided. 14B and a return pipe 14A for circulating the heat medium to the fluidized dryer 11 again, and feed the raw material collected by the sub cyclone 13 to the high-speed fluidized incinerator 1 through the sub-transfer pipe 14B. 8B is a seal valve similar to that of the main cyclone 7 described above. The gas separated by the sub-cyclone 13 is sent to a cleaning tower 17 by a circulation duct 16, washed there, and then compressed and blown by a blower 19 and a heater 20 through the flowing gas introduction pipe 18 communicating therewith. The fluid is heated and supplied to the fluidized dryer 11 as a fluid for flowing the heat medium. In the cleaning tower 17, a circulation path for circulating cooling water via a pump 22 and a cooler 21 is formed, and the temperature of the gas introduced into the cleaning tower 17 is lowered to condense the water evaporating there. This wets the gas sent to the fluidized dryer 11. The excess water generated here is drained to the outside via a water purge line 26. The gas purge line 25 branched from the middle of the flowing gas introduction pipe 18 is used when the decomposition gas is used for a gas turbine or the like or when it is necessary to send the gas to a deodorizing device.
【００１７】操業に当たっては、前記高速流動焼却炉１
と流動乾燥機１１とを同時運転した状態で、流動乾燥機
１１の原料投入管１５より水分を含有する焼却原料をそ
のまま投入する。流動乾燥機１１の下部では供給される
流動用気体により熱媒体が流動化しており、投入される
焼却原料は前記高温の熱媒体と激しく攪拌混合されるこ
とにより熱媒体と接触し、原料中の水分が熱媒体の熱を
奪い蒸発し乾燥する。前記焼却原料は、熱媒体の流動化
による攪拌により粉砕されるが、好ましくは熱媒体の粒
径を１００μｍ以上とすることにより塊状化を防止する
ことができる。それでもなお、塊を形成する場合には、
小石、セラミックボール、ステンレスボール等の粉砕媒
体を流動層にさらに投入することにより、流動層の底部
を噴流層型とし焼却原料の粉砕を確実に行うことができ
る。ここで粉砕・乾燥された焼却原料は熱媒体ととも
に、原料移送管４を経て、また図２に示される焼却シス
テムの場合には原料移送管４および原料副移送管１４Ｂ
を経て、高速流動焼却炉１に移動する。In operation, the high-speed fluidized incinerator 1
In a state where the fluidized-bed dryer 11 and the fluidized-bed dryer 11 are operated at the same time, the incinerated raw material containing water is directly supplied from the raw-material supply pipe 15 of the fluidized-bed dryer 11. In the lower part of the fluidized dryer 11, the heating medium is fluidized by the supplied flowing gas, and the incinerated raw material to be charged comes in contact with the heating medium by being vigorously stirred and mixed with the high-temperature heating medium, and Moisture deprives the heat medium of heat and evaporates to dryness. The incinerated raw material is pulverized by stirring by fluidization of the heating medium. Preferably, the particle size of the heating medium is set to 100 μm or more to prevent agglomeration. Nevertheless, when forming a lump,
By further adding a pulverizing medium such as pebbles, ceramic balls, and stainless balls to the fluidized bed, the bottom of the fluidized bed can be made into a spouted bed type, and the incineration raw material can be reliably pulverized. The incinerated raw material pulverized and dried here passes through a raw material transfer pipe 4 together with a heat medium. In the case of the incineration system shown in FIG. 2, the raw material transfer pipe 4 and the raw material sub-transfer pipe 14B
After that, it moves to the high-speed fluidized incinerator 1.
【００１８】高速流動焼却炉１に移動した焼却原料は、
流動用気体導入口２より導入される流動用気体により激
しく流動している熱媒体と再び混合攪拌されるととも
に、二次空気導入口３からの燃焼空気により完全に燃焼
される。なお、高速流動焼却炉１内の熱媒体の挙動は、
最初に熱媒体をどの程度入れるかによって異なるが、全
体粒子濃度を１０〜２５kg/m3 程度の密度とすることで
充分である。また、主サイクロン７で捕集される熱媒体
を再度高速流動焼却炉１および流動乾燥機１１に分けて
循環するが、高速流動焼却炉１への循環量は炉温度を下
げることがない量とし、また流動乾燥機１１への循環量
は含水原料の乾燥に適した量とすることが重要である。
これは、循環流動層の運転条件、主として流速と粒子の
保有量および熱媒体の粒子の大きさ等を選定するととも
に、焼却炉の圧力損失とホールドアップ量との関係を把
握し制御することにより容易に成し得る。The incinerated raw material moved to the high-speed fluidized incinerator 1 is
The gas for flow introduced from the gas inlet for flow 2 is mixed and stirred again with the heat medium which is flowing violently, and is completely burned by the combustion air from the secondary air inlet 3. The behavior of the heat medium in the high-speed fluidized incinerator 1 is as follows.
Although it depends on how much the heat medium is initially charged, it is sufficient to set the total particle concentration to a density of about 10 to 25 kg / m 3 . Further, the heat medium collected by the main cyclone 7 is circulated again to the high-speed fluidized incinerator 1 and the fluidized dryer 11 again, and the circulation amount to the high-speed fluidized incinerator 1 is an amount that does not lower the furnace temperature. It is important that the circulation amount to the fluidized dryer 11 be an amount suitable for drying the water-containing raw material.
This is achieved by selecting the operating conditions of the circulating fluidized bed, mainly the flow velocity and the amount of retained particles, the size of the particles of the heat medium, etc., and grasping and controlling the relationship between the pressure loss of the incinerator and the hold-up amount. Easy to do.
【００１９】ところで、褐炭、あるいはプラスチック等
の燃焼においては、分解ガスを利用する場合には、前記
流動乾燥機１１を分解炉として用いることができ、分解
ガスはガスパージライン２５より取り出して、別途処理
してガスタービンや特殊ボイラー等に供給される。ま
た、本焼却システムの場合には、還元雰囲気で運転でき
るので、毒性のある産業廃棄物、具体的にはダイオキシ
ンを発生し易い塩化化合物を含むスラッジ、あるいは燃
焼して塩素系有害物が発生する固形廃棄物等を焼却する
場合には、先ず還元雰囲気によって一次燃焼を行った
後、その後に設ける高温焼却炉により分解することがで
きる。By the way, in the combustion of lignite or plastic, when using a decomposed gas, the fluidized dryer 11 can be used as a decomposing furnace, and the decomposed gas is taken out from the gas purge line 25 and treated separately. And supplied to gas turbines and special boilers. In addition, in the case of this incineration system, since it can be operated in a reducing atmosphere, toxic industrial waste, specifically, sludge containing chloride compounds that easily generate dioxin, or chlorine-based harmful substances are generated by combustion. In the case of incineration of solid waste or the like, after first performing primary combustion in a reducing atmosphere, it can be decomposed by a high-temperature incinerator provided thereafter.
【００２０】また、この種の焼却装置が取り扱うスラッ
ジの中には腐食性がある場合がある。この場合には、従
来用いていたボイラー、混合乾燥機等の乾燥機の場合に
は耐用年数が短かったが、本発明における乾燥機として
耐火物で構成される流動乾燥機を用いているため、長寿
命化を図ることができる。Further, some sludge handled by this kind of incinerator may be corrosive. In this case, in the case of a conventionally used boiler, a dryer such as a mixing dryer, the service life was short, but since a fluid dryer composed of a refractory is used as the dryer in the present invention, The service life can be extended.
【００２１】（実施例１） 直径３００mm、高さ８ｍの高速高速流動焼却炉１に直径
５００mm×高さ１．８ｍの形状の主サイクロン７を取付
けるとともに、直径２５０mm、高さ４ｍの流動乾燥機１
１に直径３００mm×１．１ｍの形状の副サイクロン１３
を取付け、産業排水より得られた水分７８％、発熱量４
１００kcal/kgd.s. のスラッジについて表１に示す運転
条件の下で焼却を行った。Example 1 A high-speed high-speed fluidized-bed incinerator 1 having a diameter of 300 mm and a height of 8 m was provided with a main cyclone 7 having a shape of 500 mm in diameter and 1.8 m in height, and a fluidized dryer having a diameter of 250 mm and 4 m in height. 1
1 is a sub cyclone 13 having a diameter of 300 mm x 1.1 m.
Attached, water 78% obtained from industrial wastewater, calorific value 4
Sludge of 100 kcal / kgd.s. Was incinerated under the operating conditions shown in Table 1.
【００２２】[0022]
【表１】 [Table 1]
【００２３】以上の条件の下での焼却の結果、下記の知
見を得ることができた。乾燥しないで汚泥の焼却を行
う従来法の場合には、重油0.1 kg/kg dry solidの助燃
が必要であったが、本発明法による焼却法の場合には焼
却スタート時を除いてほとんど助燃なしの通常の運転状
態で運転することができた。臭気の最も少ない間接加
熱型乾燥機を別途設置する従来法の場合には、その運転
に過熱蒸気量を６５０kg/hr 必要としていたが、本発明
法の場合には、運転経費の少ない流動乾燥機を用いるた
め大幅に運転経費を節減することができる。表１に示
される条件では、にわか質の汚泥が混入していたため、
流動乾燥機の下層に直径１０〜４０mmのボール状の塊が
発生した。これを取り除くため、粉砕媒体として直径２
〜５mmの小石を２０kg投入した結果、前記粉砕媒体は円
錐部で激しく攪乱運動し前記塊を粉砕することができ、
塊状汚泥による閉塞を起こすことなく運転することがで
きた。As a result of incineration under the above conditions, the following findings were obtained. In the case of the conventional method, in which sludge was incinerated without drying, it was necessary to supplement 0.1 kg / kg dry solid of heavy oil. It was possible to drive in the normal operation state of. In the case of the conventional method in which an indirect heating type dryer with the lowest odor is separately installed, the amount of superheated steam was required to be 650 kg / hr for the operation. Because of the use, the operating cost can be greatly reduced. Under the conditions shown in Table 1, fluffy sludge was mixed in.
A ball-shaped lump having a diameter of 10 to 40 mm was generated in the lower layer of the fluidized dryer. In order to remove this, the diameter 2
As a result of inputting 20 kg of pebble of ~ 5 mm, the crushing medium can be vigorously disturbed in the conical portion and crush the lumps,
Operation was possible without blockage due to massive sludge.
【００２４】（実施例２） さらに、実施例１に示す焼却設備によりプラスチック類
を主体とする分別都市ゴミを表２に示す処理条件の下で
焼却した。Example 2 Separated city waste mainly composed of plastics was incinerated by the incineration equipment shown in Example 1 under the processing conditions shown in Table 2.
【００２５】[0025]
【表２】 [Table 2]
【００２６】前記プラスチック類を含む都市ゴミの分解
に際しても、本発明は好適に適用し得ることが確認され
た。It has been confirmed that the present invention can be suitably applied to the decomposition of municipal waste containing the plastics.
【００２７】[0027]
【発明の効果】以上詳説のとおり、本発明によれば、含
水固形物の乾燥・焼却に係り、設備費および維持費を大
幅に低減し得るとともに、発火・爆発の危険のある物質
に対しても安全に適用することができる。また、その乾
燥工程においても塊状となるのを防止することができ
る。As described in detail above, according to the present invention, the drying and incineration of water-containing solids can greatly reduce equipment costs and maintenance costs, and reduce the risk of ignition or explosion of substances. Can also be applied safely. In addition, it is possible to prevent lumps in the drying step.
【図１】本発明に係る焼却システムの概念図である。FIG. 1 is a conceptual diagram of an incineration system according to the present invention.
【図２】図１に示す焼却システムの一部改良に係る焼却
システム概念図である。FIG. 2 is a conceptual diagram of an incineration system according to a partial improvement of the incineration system shown in FIG.
１…高速流動焼却炉、２…流動用空気導入口、３…二次
空気導入口、４…原料移送管、５…戻り管、６…排ガス
管、７…主サイクロン、８…シールバルブ、９…分配
器、１０…戻り枝管、１１…流動乾燥機、１３…副サイ
クロン、１４Ａ…戻り管、１４Ｂ…原料副移送管、１６
…循環ダクト、１７…清浄塔、１８…流動用気体導入
管、２０…加熱器、２１…冷却器、２５…ガスパージラ
イン、２６…水パージラインDESCRIPTION OF SYMBOLS 1 ... High-speed fluidized incinerator, 2 ... Fluid air inlet, 3 ... Secondary air inlet, 4 ... Raw material transfer pipe, 5 ... Return pipe, 6 ... Exhaust gas pipe, 7 ... Main cyclone, 8 ... Seal valve, 9 ... distributor, 10 ... return branch pipe, 11 ... fluid dryer, 13 ... sub cyclone, 14A ... return pipe, 14B ... raw material sub-transfer pipe, 16
... circulation duct, 17 ... clean tower, 18 ... flow gas introduction pipe, 20 ... heater, 21 ... cooler, 25 ... gas purge line, 26 ... water purge line
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｆ２３Ｇ 5/04 ＺＡＢ Ｆ２３Ｇ 5/30 ＺＡＢＣ 5/30 ＺＡＢ Ｂ０９Ｂ 3/00 ３０３Ｊ (58)調査した分野(Int.Cl.7，ＤＢ名) F23G 7/00 104 F23G 7/00 ZAB B09B 3/00 C02F 11/06 C02F 11/12 F23G 5/04 ZAB F23G 5/30 ZAB ──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 7 identification code FI F23G 5/04 ZAB F23G 5/30 ZABC 5/30 ZAB B09B 3/00 303J (58) Investigated fields (Int. Cl. 7 , DB name) F23G 7/00 104 F23G 7/00 ZAB B09B 3/00 C02F 11/06 C02F 11/12 F23G 5/04 ZAB F23G 5/30 ZAB
Claims (5)
固形物を投入し、流動化している熱媒体との接触により
前記含水固形物の乾燥を行った後、この乾燥された固形
物を前記熱媒体とともに高速流動焼却炉に送給し、 この高速流動焼却炉において前記固形物の焼却を行うと
ともに、 高速流動焼却炉の排ガス中の前記熱媒体を前記高速流動
焼却炉へ返送して循環させるとともに、その一部を前記
流動乾燥機へ循環させることを特徴とする含水固形物の
乾燥・焼却方法。1. A heat medium hydrous solid was placed in a fluidized dryer is fluidized, after drying of the water-containing solids by contact with the heat medium having fluidized, is the dry solid feeds feed stuff in fast fluidized incinerator with the heating medium, performs incineration of the solids in the fast fluidized incinerator, returns the heat medium in the exhaust gas of the fast fluidized incinerator to said fast fluidized incinerator And circulating a part thereof to the fluidized dryer.
潤空気または過熱蒸気を用いる請求項１記載の含水固形
物の乾燥・焼却方法。2. The method according to claim 1, wherein wet air or superheated steam is used as the fluidizing gas in the fluidized dryer.
動乾燥機の排ガスを循環利用する請求項１記載の含水固
形物の乾燥・焼却方法。3. The method for drying and incinerating a hydrated solid according to claim 1, wherein the exhaust gas of the fluidized dryer is circulated and used as the fluidizing gas in the fluidized dryer.
は別に粉砕媒体を投入し含水固形物の粉砕を行う請求項
１記載の含水固形物の乾燥・焼却方法。4. The method for drying and incinerating a hydrated solid according to claim 1, wherein a crushing medium is added to the fluidized bed of the fluidized dryer in addition to the fluidized heat medium to crush the hydrated solid.
項１記載の含水固形物の乾燥・焼却方法。5. The method according to claim 1, wherein the fluidized dryer is operated as a pyrolysis furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9856991A JP3037457B2 (en) | 1991-04-30 | 1991-04-30 | Drying and incineration of hydrated solids |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9856991A JP3037457B2 (en) | 1991-04-30 | 1991-04-30 | Drying and incineration of hydrated solids |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04327706A JPH04327706A (en) | 1992-11-17 |
| JP3037457B2 true JP3037457B2 (en) | 2000-04-24 |
Family
ID=14223313
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9856991A Expired - Fee Related JP3037457B2 (en) | 1991-04-30 | 1991-04-30 | Drying and incineration of hydrated solids |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3037457B2 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007006218A1 (en) * | 2005-07-08 | 2007-01-18 | Institute Of Engineering Thermophysics, Chinese Academy Of Sciences | A dryer and a method and an equipment for drying and incinerating wet sludge using circulating fluidized bed with the dryer |
| WO2012005164A1 (en) * | 2010-07-08 | 2012-01-12 | 株式会社大川原製作所 | Drying system of dry exhaust gas circulation type equipped with heat pump unit |
| JP2012122623A (en) * | 2010-12-06 | 2012-06-28 | Metawater Co Ltd | Method and apparatus for drying and incinerating sewage sludge |
| EP2703715A4 (en) * | 2011-04-19 | 2015-04-29 | Hokkaido Tokushushiryou Kabushikikaisha | Combustion device, combustion method, and electric power-generating device and electric power-generating method using same |
| CN106322404A (en) * | 2016-09-05 | 2017-01-11 | 上海理工大学 | Sludge and coal fluidization-suspension coupled combustion system based on direct blowing type high-temperature flue gas drying |
| JP7075574B2 (en) * | 2017-05-29 | 2022-05-26 | 国立研究開発法人産業技術総合研究所 | Combustion furnace of organic waste and treatment system of organic waste using the combustion furnace |
-
1991
- 1991-04-30 JP JP9856991A patent/JP3037457B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH04327706A (en) | 1992-11-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0020735B1 (en) | Flash drying sludge derived fuel process | |
| JP3153091B2 (en) | Waste treatment method and gasification and melting and combustion equipment | |
| US3670669A (en) | Process for disposal of combustible waste | |
| CN105948459A (en) | Method using drying and incineration to treat sludge | |
| JP3037457B2 (en) | Drying and incineration of hydrated solids | |
| CN101526220B (en) | Double working substance bicirculating sludge incinerator | |
| JP2664831B2 (en) | Combustible substance moisture content reduction device | |
| JP4306334B2 (en) | Carbide processing method and apparatus | |
| JPH1054525A (en) | Circulation fluidized bed incinerator integral with fluidized bed drier | |
| JP4358095B2 (en) | Method for treating combustible waste and water-containing organic sludge | |
| PL179698B1 (en) | Fluidised bed furnace for performing heat treatment of waste materials | |
| JPS6152883B2 (en) | ||
| KR101005850B1 (en) | Apparatus for Drying and Carbonating Combustibile or organic Waste | |
| CN109563991B (en) | Staged combustion | |
| JP2000283434A (en) | Method and system for treating waste | |
| JP4161462B2 (en) | Waste treatment method and waste treatment system | |
| JPH01208610A (en) | Method for burning combustibles with high water content and apparatus therefor | |
| JPH11337040A (en) | Sludge incineration method | |
| CN109534654A (en) | A kind of sludge treating system and method | |
| JP4300893B2 (en) | Carbide molding method | |
| KR102166297B1 (en) | Stoker type incinerator equipped with waste pre-dryer and waste incinerationg method using the same | |
| JP3270447B2 (en) | Waste treatment method and gasification and melting equipment | |
| JP4089080B2 (en) | Waste treatment method and waste treatment system | |
| JP2002115829A (en) | Method for waste treatment and gasification and melting apparatus | |
| JPH01203813A (en) | Combustion device for highly wet combustible substance |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |