JP2005299993A - Incineration facility, or gasification facility, and its operating method - Google Patents

Incineration facility, or gasification facility, and its operating method Download PDF

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JP2005299993A
JP2005299993A JP2004115272A JP2004115272A JP2005299993A JP 2005299993 A JP2005299993 A JP 2005299993A JP 2004115272 A JP2004115272 A JP 2004115272A JP 2004115272 A JP2004115272 A JP 2004115272A JP 2005299993 A JP2005299993 A JP 2005299993A
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fluid medium
facility
gasification
fluidized bed
incineration
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JP4365256B2 (en
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Hidekazu Endo
英和 遠藤
Ikuo Nakanishi
郁郎 仲西
Toshiharu Oshima
俊治 大島
Yasuyuki Yamamoto
保行 山本
Tsutomu Higo
勉 肥後
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Ebara Corp
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Ebara Corp
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  • Incineration Of Waste (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)

Abstract

<P>PROBLEM TO BE SOLVED: To provide an incineration facility, or a gasification facility, and its operating method wherein a salt concentration of sand which is a bed material of a fluidized bed can be prevented from rising and maintained constant, and the facility can be operated at a low running cost by washing sand with an increased salt concentration by water, reducing the salt concentration, and reusing it. <P>SOLUTION: The incineration facility or the gasification facility provided with a fluidized bed incinerator 1 or a fluidized bed gasification furnace wherein combustibles are dropped and incinerated or gasified on a fluidized bed with a fluidized bed material is provided with a bed material extracting means for periodically extracting the bed material with the increased salt concentration, a bed material washing means (a sand washing device 12) for washing the extracted bed material by water, and a bed material returning means for returning the washed bed material into the fluidized bed incinerator 1 or the fluidized bed gasification furnace. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

本発明は、流動床焼却炉又は流動床ガス化炉を備えた焼却設備又はガス化設備、及びその運転方法に関し、特に流動媒体を有効に利用することに特徴を有する焼却設備又はガス化設備、及びそれらの運転方法に関するものである。   The present invention relates to an incineration facility or a gasification facility equipped with a fluidized bed incinerator or a fluidized bed gasification furnace, and an operating method thereof, in particular, an incineration facility or a gasification facility characterized by effectively using a fluidized medium, And their operating methods.

炉内の流動媒体（主に硅砂等の砂）を空気によって流動させる流動床焼却炉は一般廃棄物や産業廃棄物等の幅広い可燃物の焼却に用いられている。また、流動床焼却炉をベースとした流動床ガス化炉で廃棄物等の可燃物をガス化し、そのガスから有価物を得たり、ガス化した後に溶融炉に導いて高温燃焼により灰分を溶融スラグ化するガス化溶融炉も同様である。これらの可燃物は固形物や泥状物、液状物等様々な形態のものがあり、それらの成分の中には、設備の運転に悪影響を及ぼすものもある。   Fluidized bed incinerators that fluidize fluid media in the furnace (mainly sand such as dredged sand) with air are used for incineration of a wide range of combustible materials such as general waste and industrial waste. In addition, combustible materials such as waste are gasified in a fluidized bed gasifier based on a fluidized bed incinerator, and valuable materials are obtained from the gas. The same applies to gasification melting furnaces that slag. These combustible materials have various forms such as solids, mud materials, and liquid materials, and some of these components may adversely affect the operation of equipment.

特に産業廃棄物の塩を含む食品廃棄物や中和廃液のように、Ｎａ、Ｋ、Ｃｌ、Ｓその他の成分を含む廃棄物を焼却又はガス化処理した場合、反応後に残った成分が塩として蓄積して塩濃度が高くなる。流動床は、焼却炉では５５０℃〜９００℃、ガス化炉では５００℃〜６００℃程度で運転されることが多い。そして塩の種類や流動床温度によっては、塩が溶けて流動媒体をベタつかせたり、更には流動媒体を溶かしたりするため、流動媒体粒子どうしが付着して塊を形成したり、流動の動きがベタつくようになったりし、流動を阻害する場合がある。そして、塩の流動床中の濃度が高くなるほど、このような状態となり易い傾向が強い。従って塩濃度を一定以下に抑える必要がある。   In particular, when waste containing Na, K, Cl, S or other components, such as food waste containing industrial waste salts or neutralized waste liquid, is incinerated or gasified, the components remaining after the reaction are converted into salts. Accumulate and increase salt concentration. The fluidized bed is often operated at about 550 ° C. to 900 ° C. in an incinerator and about 500 ° C. to 600 ° C. in a gasifier. Depending on the type of salt and the fluidized bed temperature, the salt dissolves to make the fluid medium sticky, and further the fluid medium dissolves, so that the fluid medium particles adhere to each other to form a lump, It may become sticky and hinder flow. And the tendency for such a state to become easy is strong, so that the density | concentration in the fluidized bed of salt becomes high. Therefore, it is necessary to keep the salt concentration below a certain level.

塩の濃度が高いとちょっとしたきっかけで、最悪の場合は流動媒体が流動しなくなる。この場合、設備を停止し冷却してから流動媒体やその塊を全て除去し、即ち塩濃度の高い流動媒体を入れ替えなければならなくなり、運転再開までに数日を要してまう。流動床炉では、一般的に焼却物やガス化物に含まれる不燃物が流動床中に残って蓄積してゆくのを防ぐため炉内から流動媒体を不燃物と共に抜き出し、分級して不燃物を排除して流動媒体は炉に戻すという流動媒体循環を行なっている。この通常は炉に戻す流動媒体の一部を抜き出し、その代りに新しい流動媒体を補充することにより、流動媒体中の塩濃度を一定に保つことで対応するが、抜き出した流動媒体は廃棄物となるため、供給砂といランニングコストがかかる上に使用済みの塩を含む流動媒体という廃棄物が増えてしまうという問題があり、公知となっている流動媒体経路を有する流動床焼却装置（例えば特許文献１参照）では運転上の大きな負担であった。   If the salt concentration is high, the flow medium will not be able to flow in the worst case. In this case, the facility must be stopped and cooled to remove all of the fluid medium and its clumps, that is, the fluid medium having a high salt concentration must be replaced, and it takes several days to resume operation. In a fluidized bed furnace, in general, in order to prevent incombustibles contained in incineration and gasification products from remaining in the fluidized bed and accumulating, the fluidized medium is extracted from the furnace together with the incombustibles and classified to remove the incombustibles. A fluid medium circulation is performed in which the fluid medium is removed and returned to the furnace. This is usually handled by extracting a part of the fluid medium to be returned to the furnace and replacing it with a new fluid medium to keep the salt concentration in the fluid medium constant. Therefore, there is a problem in that the running cost of the supply sand is increased, and there is a problem that the waste of the fluid medium containing the used salt increases, and a fluidized bed incinerator having a known fluid medium path (for example, patent document) 1) was a heavy driving burden.

図１は従来の流動床焼却炉を備えた焼却設備の、流動媒体である砂の流れを図解的に示したものである。なお、流動床ガス化炉の場合も同様である。図１において、流動床焼却炉１は流動床２を具備する。流動床２はその底部から押込空気（流動化空気）１１０を供給することにより、流動媒体である砂が流動するようになっている。流動床焼却炉１には流動床２上に廃棄物を供給する廃棄物供給装置３及び液状の廃棄物を供給する液状廃棄物供給装置４が設けられている。これら廃棄物供給装置３及び液状廃棄物供給装置４から固形状及び液状の廃棄物を流動床２上に投入することにより、これらの廃棄物が焼却され、排ガス出口５から排ガス１０１が排出される。   FIG. 1 schematically shows the flow of sand as a fluidized medium in an incinerator equipped with a conventional fluidized bed incinerator. The same applies to the fluidized bed gasifier. In FIG. 1, a fluidized bed incinerator 1 includes a fluidized bed 2. The fluidized bed 2 is supplied with forced air (fluidized air) 110 from the bottom thereof so that sand as a fluidized medium flows. The fluidized bed incinerator 1 is provided with a waste supply device 3 for supplying waste on the fluidized bed 2 and a liquid waste supply device 4 for supplying liquid waste. By putting solid and liquid wastes from the waste supply device 3 and the liquid waste supply device 4 onto the fluidized bed 2, these wastes are incinerated and the exhaust gas 101 is discharged from the exhaust gas outlet 5. .

通常、炉内の砂１０２は不燃物１０３に同伴して流動床２の底部の抜出しシュート２ａより不燃物排出装置６により抜き出され、振動篩や回転篩等の分級機７によって粒径に従って不燃物１０３と砂１０２に分級される。不燃物１０３は系外で再資源化もしくは廃棄されるが、砂１０２は砂エレベータ８によって運ばれ、経路Ｌ１を通って砂投入装置９まで運ばれ、砂投入装置９によって流動床焼却炉１内に再投入される。点検や工事等で炉内の砂１０２を全て抜き出す場合は、砂投入装置９を停止させて砂１０２をオーバフローさせ経路Ｌ２へと送り、経路Ｌ３の切替ダンパ１０を開いておけば経路Ｌ３を経て砂は砂バンカ１１に移送される。流動床焼却炉１を立ち上げる際は、該砂バンカ１１に貯留されている砂１０２を流動床焼却炉１内へ投入して運転を開始する。   Normally, the sand 102 in the furnace is extracted by the incombustible discharge device 6 from the extraction chute 2a at the bottom of the fluidized bed 2 along with the incombustible material 103, and incombustible according to the particle size by the classifier 7 such as a vibration sieve or a rotary sieve. It is classified into the object 103 and the sand 102. Although the incombustible material 103 is recycled or discarded outside the system, the sand 102 is carried by the sand elevator 8, is carried to the sand throwing device 9 through the path L <b> 1, and inside the fluidized bed incinerator 1 by the sand throwing device 9. Will be re-entered. When all the sand 102 in the furnace is to be extracted for inspection or construction, the sand throwing device 9 is stopped, the sand 102 is overflowed, sent to the path L2, and the path L3 switching damper 10 is opened to pass through the path L3. The sand is transferred to the sand bunker 11. When starting up the fluidized bed incinerator 1, the sand 102 stored in the sand bunker 11 is put into the fluidized bed incinerator 1 and the operation is started.

経路Ｌ２へと砂を送るために、経路Ｌ１から経路Ｌ２を分岐させてダンパで切り替えるようにしてもよい。塩濃度が高くなった砂１０２を系外に排出する場合は、砂投入装置９を停止させ、尚且つ切替ダンパ１０を閉じておけば、経路Ｌ４から系外へ排出される。系外に排出された砂１０２は塩濃度が高いため再利用できないので廃棄され、その分新砂１０３を砂バンカ１１へ投入し、該砂バンカ１１から砂エレベータ８ヘ送ることにより、流動床焼却炉１内へ投入される。
特開平８−３３４２１９号公報 In order to send sand to the path L2, the path L2 may be branched from the path L1 and switched by a damper. When the sand 102 having a high salt concentration is discharged out of the system, the sand throwing device 9 is stopped and the switching damper 10 is closed, and the sand 102 is discharged out of the system from the path L4. Sand 102 discharged out of the system cannot be reused because of its high salt concentration, and is discarded. Accordingly, fresh sand 103 is thrown into the sand bunker 11 and sent from the sand bunker 11 to the sand elevator 8, thereby fluidized bed incinerator. 1 is inserted.
JP-A-8-334219

図１に示す従来の焼却設備では、焼却物に塩が含まれると流動媒体である砂の塩濃度が常時上昇し続ける傾向にあるため、流動床焼却炉１内の砂の一部を頻繁に塩をあまり含まない砂に入れ替えて流動媒体中の塩濃度を一定以下に抑える必要があり、ランニングコストが高くなるという問題があった。また、高い塩濃度の砂を廃棄する量も多くなり、環境への負担も大きくなる。   In the conventional incineration facility shown in FIG. 1, when salt is contained in the incineration product, the salt concentration of the sand that is a fluid medium tends to constantly increase. Therefore, a part of the sand in the fluidized bed incinerator 1 is frequently used. It was necessary to replace the sand containing less salt with the salt concentration in the fluidized medium below a certain level, and there was a problem that the running cost was increased. In addition, the amount of sand having a high salt concentration is increased, which increases the burden on the environment.

本発明は上述の点に鑑みてなされたもので、流動媒体（主に硅砂）の入れ替え無しに流動媒体の塩濃度上昇を抑えて一定以下に保つことができ、低いランニングコストで設備を運転できる焼却設備又はガス化設備、及びその運転方法を提供することを目的とする。   The present invention has been made in view of the above points, and can suppress the increase in the salt concentration of the fluid medium without changing the fluid medium (mainly dredged sand) and keep it below a certain level, and can operate the equipment at a low running cost. It aims at providing incineration equipment or gasification equipment, and its operating method.

上記課題を解決するため請求項１に記載の発明は、可燃物を焼却する流動床炉又はガス化する流動床炉を備えた焼却設備又はガス化設備において、塩濃度が高くなった流動媒体を流動床炉内から抜き出す流動媒体抜き出し手段と、該抜出した流動媒体を水で洗浄する流動媒体洗浄手段と、該洗浄した流動媒体を流動床炉に戻す流動媒体戻し手段を設けたことを特徴とする。   In order to solve the above-mentioned problem, the invention described in claim 1 is directed to a fluidized bed medium having a high salt concentration in a fluidized bed furnace for incinerating combustibles or an incineration facility or a gasification facility equipped with a fluidized bed furnace for gasification. A fluid medium extraction means for extracting from the fluid bed furnace, a fluid medium cleaning means for cleaning the extracted fluid medium with water, and a fluid medium return means for returning the cleaned fluid medium to the fluid bed furnace are provided. To do.

請求項２に記載の発明は、請求項１に記載の焼却設備又はガス化設備において、流動媒体戻し手段は、洗浄した流動媒体を流動床炉に可燃物を供給する可燃物供給装置に搬送するように構成されることを特徴とする。   According to a second aspect of the present invention, in the incineration facility or the gasification facility according to the first aspect, the fluidized medium returning means conveys the cleaned fluidized medium to a combustible material supply device that supplies the combustible material to the fluidized bed furnace. It is comprised so that it may be comprised.

請求項３に記載の発明は、請求項１又は２に記載の焼却設備又はガス化設備において、流動媒体洗浄手段は、流動媒体を攪拌する攪拌手段を具備し、該流動媒体を攪拌しながら水洗浄するように構成されていることを特徴とする。   According to a third aspect of the present invention, in the incineration facility or the gasification facility according to the first or second aspect, the fluid medium cleaning means includes a stirring means for stirring the fluid medium, and water is added while stirring the fluid medium. It is comprised so that it may wash | clean.

請求項４に記載の発明は、請求項１乃至３のいずれか１項に記載の焼却設備又はガス化設備において、流動媒体洗浄手段は、流動媒体を空気により攪拌する攪拌手段を具備し、該流動媒体を攪拌しながら水洗浄するように構成されていることを特徴とする。   The invention according to claim 4 is the incineration facility or the gasification facility according to any one of claims 1 to 3, wherein the fluid medium cleaning means comprises a stirring means for stirring the fluid medium with air, The fluidized medium is configured to be washed with water while stirring.

請求項５に記載の発明は、請求項１乃至４のいずれか１項に記載の焼却設備又はガス化設備において、流動媒体洗浄手段は、洗浄水を循環させる洗浄水循環手段を具備し、洗浄水を循環させながら流動媒体を水洗浄するように構成されていることを特徴とする。   According to a fifth aspect of the present invention, in the incineration facility or the gasification facility according to any one of the first to fourth aspects, the fluidized medium cleaning means comprises a cleaning water circulation means for circulating the cleaning water, and the cleaning water The fluid medium is washed with water while circulating the water.

請求項６に記載の発明は、請求項１乃至５のいずれか１項に記載の焼却設備又はガス化設備において、流動媒体抜出し手段により抜き出す流動媒体の量及び前記流動媒体戻し手段により戻す流動媒体の量を制御し、流動床焼却炉又は流動床ガス化炉の炉床温度を制御する炉床温度制御手段を設けたことを特徴とする。   The invention according to claim 6 is the incineration facility or the gasification facility according to any one of claims 1 to 5, wherein the amount of the fluid medium extracted by the fluid medium extracting means and the fluid medium returned by the fluid medium returning means And a hearth temperature control means for controlling the hearth temperature of the fluidized bed incinerator or fluidized bed gasification furnace.

請求項７に記載の発明は、可燃物を焼却する流動床炉を備えた焼却設備又はガス化する流動床炉を備えた焼却設備又はガス化設備の運転方法において、塩濃度が高くなった流動媒体を抜出して水で洗浄し、該洗浄した流動媒体を流動床炉に戻すことを特徴とする。   The invention according to claim 7 is a method of operating an incineration facility equipped with a fluidized bed furnace for incinerating combustibles or an incineration facility equipped with a fluidized bed furnace for gasification or an operation method of a gasification facility. The medium is extracted and washed with water, and the washed fluid medium is returned to the fluidized bed furnace.

請求項８に記載の発明は、請求項７に記載の焼却設備又はガス化設備の運転方法において、洗浄した流動媒体を可燃物供給装置により搬送して流動床炉に投入することを特徴とする。   The invention according to claim 8 is the operation method of the incineration facility or gasification facility according to claim 7, wherein the washed fluid medium is transported by a combustible material supply device and put into a fluidized bed furnace. .

請求項９に記載の発明は、請求項７又は８に記載の焼却設備又はガス化設備の運転方法において、流動媒体を水で洗浄する際、機械的に該流動媒体の攪拌を行うことを特徴とする。   The invention according to claim 9 is the operation method of the incineration facility or gasification facility according to claim 7 or 8, wherein the fluidized medium is mechanically stirred when the fluidized medium is washed with water. And

請求項１０に記載の発明は、請求項７乃至９のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、流動媒体を水で洗浄する際、空気により該流動媒体の攪拌を行うことを特徴とする。もっと詳しくは、流動媒体を含む洗浄水の底部から空気を吹き込みその空気が洗浄水中を上昇等の動きにより洗浄水を振騰攪拌する。   According to a tenth aspect of the present invention, in the method for operating an incineration facility or a gasification facility according to any one of the seventh to ninth aspects, when the fluidized medium is washed with water, the fluidized medium is agitated by air. It is characterized by performing. More specifically, air is blown from the bottom of the washing water containing the fluid medium, and the air is stirred and shaken by a movement such as rising in the washing water.

請求項１１に記載の発明は、請求項７乃至１０のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、流動媒体を水で洗浄する際、洗浄水を循環させて該流動媒体を洗浄することを特徴とする。   The invention according to claim 11 is the operating method of the incineration facility or the gasification facility according to any one of claims 7 to 10, wherein when the fluid medium is washed with water, the washing water is circulated to cause the flow. The medium is washed.

請求項１２に記載の発明は、請求項７乃至１１のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、流動媒体の抜き出し量及び洗浄した流動媒体の投入量によって炉床温度の制御を行うことを特徴とする。   A twelfth aspect of the present invention is the operation method of the incineration facility or the gasification facility according to any one of the seventh to eleventh aspects, wherein the hearth temperature depends on the amount of fluid medium extracted and the amount of washed fluid medium charged. It is characterized by controlling.

請求項１及び請求項７に記載の発明によれば、塩濃度が高くなった流動媒体を抜き出して水で洗浄し、該洗浄した流動媒体を流動床焼却炉又は流動床ガス化炉に戻すから、流動床の流動媒体の塩濃度を低い一定値に保つことができ、流動媒体粒子どうしが付着して塊となり、流動を阻害するという問題がなくなり、設備の安定した連続運転を低いランニングコストで実現できる。また、塩濃度の高くなった流動媒体を水洗浄して再利用するので、高い塩濃度の流動媒体を廃棄することが少なくなり、環境への負担が軽減できる。   According to the first and seventh aspects of the present invention, the fluid medium having a high salt concentration is extracted and washed with water, and the washed fluid medium is returned to the fluidized bed incinerator or fluidized bed gasifier. , The salt concentration of the fluidized medium in the fluidized bed can be kept at a low constant value, and the problem that the fluidized medium particles adhere to each other and become agglomerates and obstruct the flow is eliminated. realizable. In addition, since the fluid medium with a high salt concentration is washed with water and reused, the fluid medium with a high salt concentration is less discarded, and the burden on the environment can be reduced.

請求項２及び請求項８に記載の発明によれば、洗浄した流動媒体を可燃物に混ぜて流動床焼却炉又は流動床ガス化炉に投入するので、洗浄した流動媒体を流動床焼却炉又は流動床ガス化炉に戻すための専用の設備を設ける必要がない。また、砂だけを流動床焼却炉に送ろうとすると、激しい摩耗が搬送機器に生じたり、大きな搬送動力を必要とするが、汚泥や固形物等と共に供給してやることで、摩耗が緩和されたり動力が軽減されたり、或いは一度に多量の砂が入って炉床温度も低下するのを防ぐことができる。   According to the second and eighth aspects of the invention, the cleaned fluidized medium is mixed with the combustible material and charged into the fluidized bed incinerator or fluidized bed gasification furnace. There is no need to provide a dedicated facility for returning to the fluidized bed gasifier. In addition, if only sand is sent to the fluidized bed incinerator, severe wear may occur in the transfer equipment, or a large amount of transfer power is required. It can be reduced, or it can be prevented that a large amount of sand enters at a time and the hearth temperature decreases.

請求項３及び請求項９に記載の発明によれば、流動媒体を攪拌しながら水洗浄するので、まんべんなく洗浄水に曝すことができ、攪拌の際に砂どうしが衝突しあうことで物理作用も働いて塩濃度の高い或いは溶解度の低い塩に対しても流動媒体を効率よく洗浄できる。   According to the inventions of claims 3 and 9, since the fluidized medium is washed with water while stirring, it can be exposed to the washing water evenly, and the physical action is also caused by sand colliding with each other during stirring. The working fluid medium can be efficiently washed even for salts with high salt concentration or low solubility.

請求項４及び請求項１０に記載の発明によれば、流動媒体を空気により攪拌しながら水洗浄するので、塩濃度の高い或いは溶解度の低い塩に対しても流動媒体を効率よく洗浄できる。   According to the fourth and tenth aspects of the present invention, since the fluid medium is washed with water while stirring with air, the fluid medium can be efficiently washed even for a salt having a high salt concentration or a low solubility.

請求項５及び請求項１１に記載の発明によれば、洗浄水を循環させて該流動媒体を洗浄するので、洗浄水を何度も連続使用することになり、洗浄水の使用量を低減できるだけでなく、排水処理しなければならない排水洗浄水の量も低減できる。   According to the fifth and eleventh aspects of the present invention, since the washing medium is circulated by washing the circulating water, the washing water is continuously used over and over, so that the amount of washing water used can be reduced. In addition, the amount of waste water washing water that must be treated can be reduced.

請求項６及び請求項１２に記載の発明によれば、流動媒体の抜出し量及び洗浄した流動媒体の投入量によって炉床温度の制御ができるので、可燃物のカロリーの変動により炉床温度が上昇した場合も容易に炉床温度を制御できる。また、流動媒体の抜出し量及び洗浄した流動媒体の投入量によって炉床温度を制御することにより、例えば流動床に水を注入して炉床温度を制御する炉床温度制御に比べて炉床全体を均一に、且つ緩やかに制御することが容易となる。   According to the invention described in claim 6 and claim 12, since the hearth temperature can be controlled by the amount of fluid medium extracted and the amount of fluidized fluid that has been washed, the hearth temperature rises due to changes in the calories of combustible materials. In this case, the hearth temperature can be easily controlled. In addition, by controlling the hearth temperature according to the amount of fluid medium extracted and the amount of washed fluid medium charged, for example, the whole hearth temperature is controlled compared to the hearth temperature control in which water is injected into the fluidized bed to control the hearth temperature. Can be controlled uniformly and gently.

以下、本発明の実施の形態例を図面に基づいて説明する。   Embodiments of the present invention will be described below with reference to the drawings.

図２（ａ）は本発明に係る流動床焼却炉を備えた焼却設備の流動媒体である砂の流を図解的に示す図である。なお、流動床ガス化炉を備えたガス化設備の場合も同様である。また、図２において、図１と同一符号を付した部分は同一又は相当部分を示す。また、他の図においても同様とする。本焼却設備では、流動媒体である砂を洗浄する流動媒体洗浄装置１２を備えている。該流動媒体洗浄装置１２には経路Ｌ４から砂１０２が投入されると共に洗浄水１０４が供給されるようになっている。また、洗浄水１０４は循環して再利用するようになっており、塩濃度が所定以上になった洗浄水１０５は排水処理設備（図示せず）に送られ、排水処理されるようになっていいる。   FIG. 2 (a) is a diagram schematically showing the flow of sand that is a fluid medium of an incineration facility equipped with a fluidized bed incinerator according to the present invention. The same applies to a gasification facility equipped with a fluidized bed gasification furnace. In FIG. 2, the parts denoted by the same reference numerals as those in FIG. 1 indicate the same or corresponding parts. The same applies to other drawings. The incineration facility includes a fluid medium cleaning device 12 that cleans sand that is a fluid medium. The fluid medium cleaning device 12 is supplied with sand 102 from a path L4 and supplied with cleaning water 104. In addition, the cleaning water 104 is circulated and reused, and the cleaning water 105 having a salt concentration exceeding a predetermined level is sent to a wastewater treatment facility (not shown) for wastewater treatment. Yes.

流動床２の砂１０２の塩濃度が高くなったら、砂投入装置９を停止させ、切替ダンパ１０を閉じることにより、高い塩濃度の砂１０２は経路Ｌ４を通って流動媒体洗浄装置１２に投入され水洗浄される。水洗浄後の砂１０６は経路Ｌ５を通って、洗浄砂投入装置１３に供給され、流動床焼却炉１内に供給される。このように、水洗浄後の砂１０６を経路Ｌ５を通して専用の洗浄砂投入装置１３に供給し、洗浄砂投入装置１３から流動床焼却炉１内に投入する。流動床の塩濃度の監視は定期的に砂１０２のサンプリングと分析で行うことが望ましい。なお、流動床２から排出される不燃物中の砂塊の大きさや量によってもある程度塩濃度を推測することができる。即ち、塩濃度が低ければ砂塊の大きさは小さく量も少ないが、塩濃度が高くなれば砂塊は大きく量も多くなる。この場合、カメラ等の撮像手段で流動床２から排出される砂塊を監視することにより、塩濃度の高低判断をしてもよい。なお、ここにおいて、図２（ｂ）に示すように、洗浄工程を２段に分けて供給する新たな洗浄水１０４によって仕上洗浄するようにしてやれば、洗浄砂中に残る塩濃度を下げて且つ排水処理に送る排水（洗浄水１０５）中の温濃度を上げて、排水量を大幅に削減できる。勿論これは２段に限定されるものではなく、３段以上の多段にすることで効果は上がる。   When the salt concentration of the sand 102 of the fluidized bed 2 becomes high, the sand throwing device 9 is stopped and the switching damper 10 is closed, whereby the sand 102 with a high salt concentration is thrown into the fluid medium washing device 12 through the path L4. Washed with water. The sand 106 after the water cleaning is supplied to the cleaning sand charging device 13 through the path L5 and supplied into the fluidized bed incinerator 1. In this way, the sand 106 after the water cleaning is supplied to the dedicated cleaning sand charging device 13 through the path L5, and is charged into the fluidized bed incinerator 1 from the cleaning sand charging device 13. It is desirable to monitor the salt concentration of the fluidized bed periodically by sampling and analyzing the sand 102. It should be noted that the salt concentration can be estimated to some extent by the size and amount of the sand lump in the incombustible material discharged from the fluidized bed 2. That is, if the salt concentration is low, the size of the sand lump is small and the amount is small, but if the salt concentration is high, the sand lump is large and the amount is large. In this case, the level of the salt concentration may be determined by monitoring the sand lump discharged from the fluidized bed 2 with an imaging means such as a camera. Here, as shown in FIG. 2 (b), if the washing process is finished and washed with new washing water 104 that is supplied in two stages, the salt concentration remaining in the washing sand is reduced and By increasing the temperature concentration in the wastewater (wash water 105) sent to the wastewater treatment, the amount of wastewater can be greatly reduced. Of course, this is not limited to two stages, and the effect is enhanced by using three or more stages.

図３は本発明に係る流動床焼却炉を備えた他焼却設備の流動媒体である砂の流れを図解的に示す図である。なお、流動床ガス化炉を備えたガス化設備の場合も同様である。図示するようにここでは、流動媒体洗浄装置１２で水洗浄された砂１０６は経路Ｌ５を通って、廃棄物供給装置３に供給され、該廃棄物供給装置３で廃棄物に混入されて流動床焼却炉１内に供給される。このように、水洗浄後の砂１０６を経路Ｌ５を通して廃棄物供給装置３に供給することにより、実施例１の場合のように専用の洗浄砂投入装置１３を設ける必要がなく、洗浄後の砂１０６を流動床焼却炉１内に戻すことができる。   FIG. 3 is a diagram schematically showing the flow of sand which is a fluid medium of another incineration facility equipped with a fluidized bed incinerator according to the present invention. The same applies to a gasification facility equipped with a fluidized bed gasification furnace. As shown in the drawing, here, the sand 106 washed with water by the fluid medium cleaning device 12 is supplied to the waste supply device 3 through the path L5, and is mixed with the waste by the waste supply device 3 to be fluidized bed. It is supplied into the incinerator 1. In this way, by supplying the sand 106 after water washing to the waste supply device 3 through the path L5, it is not necessary to provide the dedicated washing sand charging device 13 as in the case of the first embodiment, and the sand after washing is removed. 106 can be returned to the fluidized bed incinerator 1.

図４は本発明に係る流動床焼却炉を備えた他焼却設備の流動媒体である砂の流れを図解的に示す図である。なお、流動床ガス化炉を備えたガス化設備の場合も同様である。図示するようにここでは、流動床焼却炉１に廃棄物供給装置３と液状廃棄物供給装置４の他に汚泥供給装置１４を設け、廃棄物の性状によりその供給装置を切り替え、即ち廃棄物の投入経路を変える構成を採用している。ここでは、砂に性状が類似する汚泥を供給する汚泥供給装置１４に経路Ｌ５を通して水洗浄後の砂１０６を供給している。該砂１０６は汚泥供給装置１３で汚泥に混入され流動床焼却炉１内に供給される。このように、水洗浄後の砂１０６を汚泥供給装置１３に供給することにより、実施例２の場合と同様、専用の洗浄砂投入装置１３を設ける必要がなく、流動床焼却炉１内に戻すことができる。汚泥と混じることで流動性がよくなり、機器の摩耗や動力低減も可能である。   FIG. 4 is a diagram schematically showing the flow of sand which is a fluid medium of another incineration facility equipped with a fluidized bed incinerator according to the present invention. The same applies to a gasification facility equipped with a fluidized bed gasification furnace. As shown in the figure, the fluidized bed incinerator 1 is provided with a sludge supply device 14 in addition to the waste supply device 3 and the liquid waste supply device 4, and the supply device is switched depending on the properties of the waste. A configuration that changes the input route is adopted. Here, the sand 106 after water washing is supplied to the sludge supply device 14 that supplies sludge having properties similar to those of sand through the path L5. The sand 106 is mixed with sludge by the sludge supply device 13 and supplied into the fluidized bed incinerator 1. Thus, by supplying the sand 106 after water cleaning to the sludge supply device 13, it is not necessary to provide a dedicated cleaning sand charging device 13 as in the case of the second embodiment, and it is returned to the fluidized bed incinerator 1. be able to. Mixing with sludge improves fluidity, and can reduce equipment wear and power.

また、流動媒体洗浄装置１２で水洗浄後の砂１０６を砂エレベータ８を利用して流動床焼却炉１内に戻す場合は、水洗浄後の砂１０６を乾燥させる必要があり、乾燥装置等を必要とするが、上記のように液状廃棄物供給装置４、廃棄物供給装置３、汚泥供給装置１４に供給し、ここで液状廃棄物、廃棄物、汚泥と混合して流動床焼却炉１内に供給することにより、このような専用の乾燥装置等の設備を必要としない。また、廃棄物の形態が液状、固形状、汚泥状と異なる場合は、汚泥のように性状の近い廃棄物と混ぜることが望ましい。   Further, when the sand 106 after water washing is returned to the fluidized bed incinerator 1 by using the sand elevator 8 in the fluid medium washing device 12, it is necessary to dry the sand 106 after water washing. Although it is necessary, it supplies to the liquid waste supply apparatus 4, the waste supply apparatus 3, and the sludge supply apparatus 14 as mentioned above, and mixes with a liquid waste, a waste, and sludge here, and is in a fluidized bed incinerator 1. Therefore, the equipment such as a dedicated drying device is not required. In addition, when the form of waste is different from liquid, solid, or sludge, it is desirable to mix it with waste having similar properties such as sludge.

図５は砂洗浄装置の構成例を示す図で、図５（ａ）は平面図、図５（ｂ）は側断面である。図示するように、本砂洗浄装置２０は箱状の容器２１内に複数本（図では２本）の攪拌空気用パイプ２２を配置すると共に、排水用パイプ２３を取付けた構成である。攪拌空気用パイプ２２には図示を省略するが、直径数ｍｍ程度の孔が複数個設けられている。また、攪拌空気用パイプ２２には開閉バルブ２４が設けられ、排水用パイプ２３にも開閉バルブ２５が設けられ、更に洗浄水の流入口には砂１０２の流出を防ぐため、砂粒径より細かいメッシュの網が設けられている。   FIG. 5 is a diagram showing a configuration example of the sand cleaning apparatus, FIG. 5 (a) is a plan view, and FIG. 5 (b) is a side cross section. As shown in the figure, the sand cleaning device 20 has a configuration in which a plurality of (two in the figure) stirring air pipes 22 are arranged in a box-like container 21 and a drainage pipe 23 is attached. Although not shown, the stirring air pipe 22 is provided with a plurality of holes having a diameter of several millimeters. In addition, the agitation air pipe 22 is provided with an opening / closing valve 24, the drainage pipe 23 is also provided with an opening / closing valve 25, and further to prevent the sand 102 from flowing out at the inlet of the washing water, it is finer than the sand particle size. A mesh net is provided.

上記構成の本砂洗浄装置２０において、図示しない砂供給手段により容器２１内に流動床焼却炉１から排出された塩濃度の高い砂１０２を図５（ｂ）に示すように容器に対し半分のレベル程度入れて、更に図示しない洗浄水供給手段により洗浄水１０４で満たす。この状態で、開閉バルブ２４を開き、攪拌空気用パイプ２２に空気１０７を送り込むと該攪拌空気用パイプ２２に設けられた複数の孔から洗浄水中に空気１０７が噴出し、砂１０２が攪拌され洗浄される。空気１０７は圧縮機による圧縮空気を用いてもよいし、流動床焼却炉１の流動床２底部に圧縮空気を押込む押込空気ラインから分岐させた圧縮空気を用いてもよい。なお、攪拌空気用パイプ２２は容器２１に固定せず攪拌状況を確認しながら砂１０２の層への挿入位置を変えられるようにすると便利である。洗浄の終了した水は排水用パイプ２３の開閉バルブ２５を開いて排出し、再利用することが可能である。排水用パイプ２３の洗浄水流入口には上記のように砂粒径より細かいメッシュの網が設けられているので、この排水用パイプ２３を通って砂１０２が流出することはない。なお、流動床では細い粒径のものは炉に戻しても飛散してしまうため、メッシュより細いものが排水と共に、流出しても支障はない。   In the sand cleaning apparatus 20 having the above-described configuration, the sand 102 having a high salt concentration discharged from the fluidized bed incinerator 1 into the container 21 by sand supply means (not shown) is half of the container as shown in FIG. After the level is reached, it is further filled with cleaning water 104 by a cleaning water supply means (not shown). In this state, when the opening / closing valve 24 is opened and the air 107 is sent to the stirring air pipe 22, the air 107 is jetted into the cleaning water from a plurality of holes provided in the stirring air pipe 22, and the sand 102 is stirred and washed. Is done. The air 107 may be compressed air by a compressor, or may be compressed air branched from a pushing air line that pushes compressed air into the bottom of the fluidized bed 2 of the fluidized bed incinerator 1. It is convenient that the stirring air pipe 22 is not fixed to the container 21 and the insertion position of the sand 102 into the layer of the sand 102 can be changed while confirming the stirring state. The washed water can be discharged by opening the open / close valve 25 of the drain pipe 23 and reused. Since the mesh of finer mesh than the sand particle size is provided at the washing water inlet of the drain pipe 23 as described above, the sand 102 does not flow out through the drain pipe 23. In the fluidized bed, those with a small particle size will scatter even if they are returned to the furnace.

図６は砂洗浄装置の他の構成例を示す図である。本砂洗浄装置３０は汎用の小型コンクリートミキサー３１を備えている。該小型コンクリートミキサー３１を矢印Ａに示すように回転させながら、流動床焼却炉１から排出された塩濃度の高い砂１０２と洗浄水１０４を供給しながら、砂１０２を洗浄する。なお、小型コンクリートミキサー３１に替えてトロンメル（回転篩）、洗浄する砂１０２の量によってはコンクリートミキサー車等を用いて攪拌洗浄を行ってもよい。   FIG. 6 is a view showing another configuration example of the sand cleaning apparatus. The sand cleaning apparatus 30 includes a general-purpose small concrete mixer 31. While rotating the small concrete mixer 31 as indicated by the arrow A, the sand 102 is washed while supplying the sand 102 and the washing water 104 having a high salt concentration discharged from the fluidized bed incinerator 1. It should be noted that instead of the small concrete mixer 31, stirring and washing may be performed using a trommel (rotary sieve) or a concrete mixer truck depending on the amount of sand 102 to be washed.

水洗浄の終了した砂は図２に示すように、専用の洗浄砂投入装置１３により流動床焼却炉１内へ再投入される。厨芥や汚泥のようにある程度水分を含んだ廃棄物を焼却処理する場合は、図３に示すように廃棄物供給装置３を介して、廃棄物に混ぜて流動床焼却炉１内へ再投入される。このように廃棄物と混ぜて再投入すれば洗浄済の砂を再投入するための専用の設備を設置する必要がない。廃棄物が複数種類あり、投入経路が異なる場合は、図４に示すように、汚泥のような性状が近い廃棄物と混ぜることが望ましい。   As shown in FIG. 2, the sand that has been washed with water is re-introduced into the fluidized bed incinerator 1 by a dedicated cleaning sand input device 13. In the case of incinerating waste that contains water to some extent, such as dredging and sludge, it is re-introduced into the fluidized bed incinerator 1 through the waste supply device 3 and mixed with the waste as shown in FIG. The In this way, if it is mixed with waste and re-introduced, it is not necessary to install a dedicated facility for re-injecting the washed sand. When there are a plurality of types of waste and the input routes are different, as shown in FIG. 4, it is desirable to mix with waste having similar properties such as sludge.

また、流動床炉では、流動床温度が燃焼やガス化の反応温度となるため、反応に適した温度に極力安定保持することが望ましいが、流動床焼却炉１内に投入する廃棄物のカロリーの変動により、流動床２の温度が変動する。温度が上昇した場合、砂の抜き出し量を増やして洗浄後の砂１０６を連続的に投入することにより炉床温度をコントロールすることも可能である。流動床２に水を注入することでも炉床温度をコントロールすることが可能であるが、注水の場合は局所的に温度が下がったり温度が下がり過ぎたりして温度コントロールが難しい場合がある、或いはしぶきが耐火物壁面にかかってスポーリングにより耐火物を傷める可能性があるが、水分を含んだ洗浄後の砂１０６を少量ずつ連続的に投入すれば、炉床温度が比較的均一に且つ緩慢にコントロールできるので制御し易いという利点がある。   In a fluidized bed furnace, since the fluidized bed temperature is the reaction temperature for combustion and gasification, it is desirable to keep it as stable as possible at a temperature suitable for the reaction. However, the calorie of the waste put into the fluidized bed incinerator 1 , The temperature of the fluidized bed 2 varies. When the temperature rises, it is possible to control the hearth temperature by increasing the amount of sand extracted and continuously feeding the washed sand 106. It is possible to control the hearth temperature by injecting water into the fluidized bed 2, but in the case of water injection, the temperature may be locally lowered or too low, making temperature control difficult, or Splashing may hit the refractory wall and damage the refractory due to spalling. However, if sand 106 after washing containing moisture is continuously added little by little, the hearth temperature is relatively uniform and slow. Therefore, there is an advantage that it is easy to control.

また、一般的に、流動層（流動床２の流動媒体層）温度は低温になるに従い層内での燃焼又はガス化反応が緩慢になるため、僅かなきっかけで層内温度が低下しはじめるとそのまま下がり続けて運転不能に陥る虞がある。一方、層内温度を高温にしすぎると層内反応速度が速くなるため燃焼変動が激化し一酸化炭素発生量（すなわち、有機性ハロゲン発生量）が発生し易くなるなどの虞があると共に、クリンカーが発生し易くなる虞がある。従って、流動層温度を適切な温度範囲に維持することが重要である。ここで、最適な流動層温度の運転範囲は、各々の処理物や炉の特性によって、最適な範囲があることも考慮して決定することになる。   Also, generally, as the temperature of the fluidized bed (fluidized bed 2 of the fluidized bed 2) becomes lower, the combustion or gasification reaction in the bed becomes slow, and therefore the temperature in the bed begins to decrease with a slight trigger. There is a risk that it will continue to fall and become inoperable. On the other hand, if the temperature in the layer is too high, the reaction rate in the layer increases, so that fluctuations in combustion increase and carbon monoxide generation amount (that is, organic halogen generation amount) is likely to occur. May occur easily. Therefore, it is important to maintain the fluidized bed temperature in an appropriate temperature range. Here, the operation range of the optimum fluidized bed temperature is determined in consideration of the existence of the optimum range depending on the characteristics of each processed product and the furnace.

流動層温度を最適に制御するための具体的方法としては、タイマーを用いて間欠的に不燃物を流動層から排出するための流動媒体循環量を調整する方法がある。停止タイマーと起動タイマーを用い、停止タイマーの設定時間Ｔ１が経過した段階で、別途設けられた起動タイマーの設定時間Ｔ２だけ、高温の熱媒体として流動媒体を流動層炉から抜き出すための装置を起動させる。これを繰り返す。この装置は、図では不燃物排出装置（コンベヤ）６であり、連続運転の排出能力Ｑｋｇ／ｈに対して、実際の流動媒体排出量はＱ×Ｔ２÷（Ｔ１＋Ｔ２）ｋｇ／ｈとなる。勿論、停止タイマーと起動タイマーによる調節ではなく、インバータや可変速減速機等を使っての、コンベヤ回転数又はコンベヤ速度変更によってこのコンベヤ排出能力を調整することでもよい。   As a specific method for optimally controlling the fluidized bed temperature, there is a method of adjusting the circulating amount of the fluidized medium for intermittently discharging the incombustible material from the fluidized bed using a timer. Using the stop timer and start timer, when the stop timer set time T1 has elapsed, the device for starting the fluidized medium as a high-temperature heat medium from the fluidized bed furnace is started for the set start timer time T2 provided separately. Let Repeat this. This device is a non-combustible material discharge device (conveyor) 6 in the figure, and the actual fluid discharge amount is Q × T2 ÷ (T1 + T2) kg / h with respect to the discharge capacity Qkg / h of continuous operation. Of course, the conveyor discharge capacity may be adjusted by changing the conveyor rotation speed or the conveyor speed using an inverter, a variable speed reducer, or the like, instead of the adjustment by the stop timer and the start timer.

これにより、流動媒体は不燃物とともに流動層から冷やされながら抜き出され、該不燃物が分別された後に流動床焼却炉１に返送される流動媒体循環を行なうが、この一連の過程で流動媒体が冷えて戻った分流動層の熱バランスで放出熱となる。このため、流動媒体循環の量を調節することでそれに伴う放出熱量を調節することができる。流動媒体の循環量を増やすことでより低い流動床温度で熱収支がバランスする。即ち、低い流動床温度となる。逆に流動媒体の循環量を減らすことにより高い流動床温度で熱収支がバランスする。即ち、高い流動床温度となる。   Thereby, the fluidized medium is extracted while being cooled from the fluidized bed together with the incombustible material, and the fluidized medium is circulated and returned to the fluidized bed incinerator 1 after the incombustible material is separated. Heat is released due to the heat balance of the fluidized bed. For this reason, by adjusting the amount of circulating fluid medium, the amount of heat released can be adjusted. Increasing the circulation rate of the fluidized medium balances the heat balance at a lower fluidized bed temperature. That is, the fluidized bed temperature is low. Conversely, the heat balance is balanced at a high fluidized bed temperature by reducing the circulation rate of the fluidized medium. That is, the fluidized bed temperature is high.

このように流動媒体の抜き出しの実行と停止を繰り返すことで、適切な流動層温度に維持することが可能となる。流動層内に注水を行なわずとも、廃棄物の投入量を適切に制御し、且つ／又は、上述した流動媒体循環量調節を使用した流動層温度の制御方法とを組み合わせることで、流動層温度を適切な範囲内に維持することが可能である。   By repeating the execution and stoppage of the fluidized medium in this way, it becomes possible to maintain an appropriate fluidized bed temperature. Even if water injection is not performed in the fluidized bed, the fluidized bed temperature can be controlled by appropriately controlling the input amount of waste and / or the fluidized bed temperature control method using the fluidized medium circulation rate adjustment described above. Can be maintained within an appropriate range.

（実施例１、実施例４の結果）
図２に示す構成の焼却設備で流動床２は６００〜６５０℃で運転している。これにおいて、砂洗浄装置１２に図５に示す構成の洗浄装置を用いて流動床焼却炉から排出された砂の洗浄を行い、塩測定を行った。ここでは、分級機７で４ｍｍ未満のものを砂として分級した。傾向として砂中塩濃度（Ｎａ＋Ｋ）がある一定濃度以上になると流動不良が起こりやすくなるため（１０ｃｍ以下の砂の塊が通常の倍以上排出されるようになる）、毎日サンプリング、分析を行い、適正な管理値を定め、該管理値以下で管理するようした。 (Results of Example 1 and Example 4)
The fluidized bed 2 is operated at 600 to 650 ° C. in the incineration facility having the configuration shown in FIG. In this case, the sand discharged from the fluidized bed incinerator was washed in the sand washing device 12 using the washing device having the configuration shown in FIG. 5, and the salt was measured. Here, the classifier 7 classified the sand as less than 4 mm. As a tendency, when the salt concentration in the sand (Na + K) exceeds a certain level, poor flow is likely to occur (a lump of sand of 10 cm or less will be discharged more than usual), so sampling and analysis are performed every day, Appropriate control values were determined and managed below the control values.

塩濃度が高くなった砂１０２を抜き出して砂洗浄装置２０の容積１ｍ3の容器２１に０．５ｍ3程度入れ、更に洗浄水１０４を満たし、空気を用いて３分間攪拌洗浄を行った。圧縮空気を使用し、砂が飛散しないように開閉バルブ２４の開度を調整して行った。洗浄水１０４を交換して合計３回洗浄を行い、洗浄前、１回洗浄、２回洗浄、３回洗浄のそれぞれの砂の塩濃度（Ｎａ及びＫ）の分析を行った結果を図７に示す。洗浄前（洗浄回数０回）Ｎａ＋Ｋで３．６５％あった塩濃度が３回洗浄後には１％以下の０．８９％となり高い洗浄効果が確認できた。また、１回洗浄後でも１．３１％となり十分低い値となることが確認できた（図７参照）。 By extracting sand 102 salt concentration was higher placed 0.5 m 3 degrees to the vessel 21 of volume 1 m 3 of sand cleaning device 20, still filled with wash water 104, the mixture was stirred 3 min wash using air. Compressed air was used and the opening / closing valve 24 was adjusted to prevent sand from scattering. Washing water 104 was changed and washing was performed three times in total, and the results of the analysis of the salt concentration (Na and K) of each sand before washing, once washing, twice washing and three times washing are shown in FIG. Show. Before washing (0 washing times), the salt concentration of 3.65% with Na + K was 0.89%, which is 1% or less after 3 washings, and a high washing effect was confirmed. In addition, it was confirmed that the value was 1.31% even after the first washing, which was a sufficiently low value (see FIG. 7).

砂バンカ１１と流動床２に保持する砂約３０ｍ3において、１回０．５ｍ3の砂を１日数回洗浄し流動床焼却炉１に戻すと、砂中塩濃度（Ｎａ＋Ｋ）を管理値以下に維持することができ、新砂１０３の投入量を最低限に抑えた上で流動床焼却炉１の安定連続運転ができた。 In about 30m 3 of sand held in the sand bunker 11 and fluidized bed 2, once 0.5m 3 of sand is washed several times a day and returned to the fluidized bed incinerator 1, the salt concentration (Na + K) in the sand is below the control value. Thus, the fluidized bed incinerator 1 can be stably operated continuously while keeping the amount of fresh sand 103 charged to a minimum.

また、流動床焼却炉１に投入する廃棄物のカロリー変動により炉床温度が上昇した場合も、砂の抜き出し量及び洗浄した砂の投入量をコントロールすることにより廃棄物の処理量（焼却量又はガス化量）が大きく低下することなく安定した運転をすることができた。   In addition, even when the hearth temperature rises due to calorie fluctuation of waste to be introduced into the fluidized bed incinerator 1, the amount of waste treated (incineration amount or incineration amount) can be controlled by controlling the amount of sand extracted and the amount of washed sand input. Stable operation was possible without significant reduction in gasification.

（実施例２、実施例３の結果）
図３、図４に示す構成の焼却設備で、洗浄した砂１０６を廃棄物供給装置３、汚泥供給装置１４に供給し、廃棄物、汚泥に混ぜて流動床焼却炉１に再投入した場合も上記と同様の結果が得られた。 (Results of Example 2 and Example 3)
In the incinerator having the configuration shown in FIGS. 3 and 4, the washed sand 106 is supplied to the waste supply device 3 and the sludge supply device 14, mixed with the waste and sludge, and re-entered into the fluidized bed incinerator 1. Similar results were obtained.

（実施例５の結果）
砂洗浄装置に図６に示す小型コンクリートミキサー３１を備えた砂洗浄装置を用い、砂を機械的に攪拌して洗浄した場合も上記と同様の結果が得られた。 (Result of Example 5)
The same results as described above were obtained when the sand washer was mechanically stirred and washed using the sand washer equipped with the small concrete mixer 31 shown in FIG.

洗浄水を循環させて洗浄水の再利用を行いながら砂の洗浄を行った場合も上記と同様の結果が得られた。   Similar results were obtained when the sand was washed while circulating the wash water and reusing the wash water.

なお、上記実施形態例は焼却設備を例として説明したが、本発明は焼却設備に限定されるものではなく、ガス化設備においても同様である。但しガス化の流動床は５００℃〜６００℃程度と低目に設定するのが普通で、流動床自体では塩濃度が上昇しても溶融点に至らずクリンカの生成はないが炉外に抜き出すシュート２ａにおいて、焼却炉と異なり可燃物が混じることがあり、流動媒体よりも高温化してここでクリンカが生じ易い。クリンカの抑制のため、塩濃度上昇を抑えることが好ましいため、本発明が有効である。   In addition, although the said embodiment demonstrated the incineration equipment as an example, this invention is not limited to incineration equipment, The same is applied also to gasification equipment. However, the fluidized bed for gasification is usually set to a low temperature of about 500 ° C. to 600 ° C. The fluidized bed itself does not reach the melting point even if the salt concentration is increased and does not generate clinker, but is extracted outside the furnace. In the chute 2a, combustible materials may be mixed unlike the incinerator, and the temperature is higher than that of the fluidized medium, and clinker is easily generated here. In order to suppress the clinker, it is preferable to suppress an increase in salt concentration, and thus the present invention is effective.

以上本発明の実施形態を説明したが、本発明は上記実施形態に限定されるものではなく、特許請求の範囲、及び明細書と図面に記載された技術的思想の範囲内において種々の変形が可能である。
Although the embodiments of the present invention have been described above, the present invention is not limited to the above-described embodiments, and various modifications can be made within the scope of the technical idea described in the claims and the specification and drawings. Is possible.

従来の流動床焼却炉を備えた焼却設備の流動媒体である砂の流れを図解的に示す図である。It is a figure which shows the flow of the sand which is a fluid medium of the incineration equipment provided with the conventional fluidized-bed incinerator schematically. 本発明に係る流動床焼却炉を備えた焼却設備の流動媒体である砂の流れを図解的に示す図である。（実施例１）It is a figure which shows the flow of the sand which is a fluid medium of the incineration equipment provided with the fluidized-bed incinerator concerning this invention schematically. (Example 1) 本発明に係る流動床焼却炉を備えた焼却設備の流動媒体である砂の流れを図解的に示す図である。（実施例２）It is a figure which shows the flow of the sand which is a fluid medium of the incineration equipment provided with the fluidized-bed incinerator concerning this invention schematically. (Example 2) 本発明に係る流動床焼却炉を備えた焼却設備の流動媒体である砂の流れを図解的に示す図である。（実施例３）It is a figure which shows the flow of the sand which is a fluid medium of the incineration equipment provided with the fluidized-bed incinerator concerning this invention schematically. Example 3 砂洗浄装置の構成例を示す図である。It is a figure which shows the structural example of a sand cleaning apparatus. 砂洗浄装置の構成例を示す図である。It is a figure which shows the structural example of a sand cleaning apparatus. 実施例１、実施例４の結果を示す図である。It is a figure which shows the result of Example 1 and Example 4. FIG.

符号の説明Explanation of symbols

１ 流動床焼却炉
２ 流動床
３ 廃棄物供給装置
４ 液状廃棄物供給装置
５ 排ガス出口
６ 不燃物排出装置
７ 分級機
８ 砂エレベータ
９ 砂投入装置
１０ 切替ダンパ
１１ 砂バンカ
１２ 流動媒体洗浄装置
１３ 洗浄砂投入装置
１４ 汚泥投入装置
２０ 砂洗浄装置
２１ 容器
２２ 攪拌空気用パイプ
２３ 排水パイプ
２４ 開閉バルブ
３０ 砂洗浄装置
３１ 汎用小型コンクリートミキサ DESCRIPTION OF SYMBOLS 1 Fluidized bed incinerator 2 Fluidized bed 3 Waste supply device 4 Liquid waste supply device 5 Exhaust gas outlet 6 Incombustible material discharge device 7 Classifier 8 Sand elevator 9 Sand input device 10 Switching damper 11 Sand bunker 12 Fluid medium washing device 13 Washing Sand input device 14 Sludge input device 20 Sand cleaning device 21 Container 22 Pipe for stirring air 23 Drain pipe 24 Opening / closing valve 30 Sand cleaning device 31 General-purpose small concrete mixer

Claims (12)

可燃物を焼却する流動床炉又はガス化する流動床炉を備えた焼却設備又はガス化設備において、
塩濃度が高くなった前記流動媒体を前記流動床炉内から抜き出す流動媒体抜き出し手段と、該抜き出した流動媒体を水で洗浄する流動媒体洗浄手段と、該洗浄した流動媒体を前記流動床炉に戻す流動媒体戻し手段を設けたことを特徴とする焼却設備又はガス化設備。 In incineration equipment or gasification equipment equipped with a fluidized bed furnace for incinerating combustibles or a fluidized bed furnace for gasification,
Fluid medium extraction means for extracting the fluid medium having a high salt concentration from the fluid bed furnace, fluid medium cleaning means for cleaning the extracted fluid medium with water, and the cleaned fluid medium in the fluid bed furnace. An incineration facility or a gasification facility characterized in that a fluid medium returning means for returning is provided. 請求項１に記載の焼却設備又はガス化設備において、
前記流動媒体戻し手段は、前記洗浄した流動媒体を前記流動床炉に前記可燃物を供給する可燃物供給装置に搬送するように構成されることを特徴とする焼却設備又はガス化設備。 Incineration equipment or gasification equipment according to claim 1,
The incineration equipment or gasification equipment, wherein the fluid medium return means is configured to convey the cleaned fluid medium to a combustible material supply device that supplies the combustible material to the fluidized bed furnace. 請求項１又は２に記載の焼却設備又はガス化設備において、
前記流動媒体洗浄手段は、前記流動媒体を攪拌する攪拌手段を具備し、該流動媒体を攪拌しながら水洗浄するように構成されていることを特徴とする焼却設備又はガス化設備。 In the incineration facility or gasification facility according to claim 1 or 2,
An incineration facility or a gasification facility characterized in that the fluid medium cleaning means includes a stirring means for stirring the fluid medium, and the fluid medium is washed with water while stirring the fluid medium. 請求項１乃至３のいずれか１項に記載の焼却設備又はガス化設備において、
前記流動媒体洗浄手段は、前記流動媒体を空気により攪拌する攪拌手段を具備し、該流動媒体を攪拌しながら水洗浄するように構成されていることを特徴とする焼却設備又はガス化設備。 In the incineration equipment or gasification equipment according to any one of claims 1 to 3,
The incineration facility or gasification facility is characterized in that the fluid medium cleaning means includes an agitation means for agitating the fluid medium with air, and the fluid medium is washed with water while stirring the fluid medium. 請求項１乃至４のいずれか１項に記載の焼却設備又はガス化設備において、
前記流動媒体洗浄手段は、前記洗浄水を循環させる洗浄水循環手段を具備し、洗浄水を循環させながら流動媒体を水洗浄するように構成されていることを特徴とする焼却設備又はガス化設備。 In incineration equipment or gasification equipment given in any 1 paragraph of Claims 1 thru / or 4,
The incineration facility or the gasification facility, wherein the fluid medium cleaning means includes a cleaning water circulation means for circulating the cleaning water, and is configured to wash the fluid medium with water while circulating the cleaning water. 請求項１乃至５のいずれか１項に記載の焼却設備又はガス化設備において、
前記流動媒体抜き出し手段により抜き出す流動媒体の量及び前記流動媒体戻し手段により戻す流動媒体の量を制御し、前記流動床焼却炉又は流動床ガス化炉の炉床温度を制御する炉床温度制御手段を設けたことを特徴とする焼却設備又はガス化設備。 In the incineration facility or gasification facility according to any one of claims 1 to 5,
A hearth temperature control means for controlling the amount of the fluid medium extracted by the fluid medium extraction means and the amount of the fluid medium returned by the fluid medium return means to control the hearth temperature of the fluidized bed incinerator or fluidized bed gasification furnace. Incineration equipment or gasification equipment characterized by providing 可燃物を焼却する流動床炉を備えた焼却設備又はガス化する流動床炉を備えた焼却設備又はガス化設備の運転方法において、
塩濃度が高くなった前記流動媒体を抜出して水で洗浄し、該洗浄した流動媒体を前記流動床炉に戻すことを特徴とする焼却設備又はガス化設備の運転方法。 In an incineration facility equipped with a fluidized bed furnace for incinerating combustibles or an incineration facility equipped with a fluidized bed furnace for gasification or an operation method of a gasification facility,
A method for operating an incineration facility or a gasification facility, wherein the fluid medium having a high salt concentration is extracted and washed with water, and the washed fluid medium is returned to the fluidized bed furnace. 請求項７に記載の焼却設備又はガス化設備の運転方法において、
前記洗浄した流動媒体を前記可燃物供給装置により搬送し前記流動床炉に投入することを特徴とする焼却設備又はガス化設備の運転方法。 In the operation method of the incineration facility or gasification facility according to claim 7,
A method of operating an incineration facility or a gasification facility, wherein the washed fluid medium is transported by the combustible material supply device and charged into the fluidized bed furnace. 請求項７又は８に記載の焼却設備又はガス化設備の運転方法において、
前記流動媒体を水で洗浄する際、機械的に該流動媒体の攪拌を行うことを特徴とする焼却設備又はガス化設備の運転方法。 In the operation method of the incineration facility or gasification facility according to claim 7 or 8,
A method of operating an incineration facility or a gasification facility, wherein the fluidized medium is mechanically stirred when the fluidized medium is washed with water. 請求項７乃至９のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、
前記流動媒体を水で洗浄する際、空気により該流動媒体の攪拌を行うことを特徴とする焼却設備又はガス化設備の運転方法。 In the operation method of the incineration equipment or gasification equipment according to any one of claims 7 to 9,
A method for operating an incineration facility or a gasification facility, wherein the fluid medium is agitated with air when the fluid medium is washed with water. 請求項７乃至１０のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、
前記流動媒体を水で洗浄する際、洗浄水を循環させて該流動媒体を洗浄することを特徴とする焼却設備又はガス化設備の運転方法。 In the operation method of the incineration equipment or gasification equipment according to any one of claims 7 to 10,
A method for operating an incineration facility or a gasification facility, wherein the fluid medium is washed by circulating the washing water when the fluid medium is washed with water. 請求項７乃至１１のいずれか１項に記載の焼却設備又はガス化設備の運転方法において、
前記流動媒体の抜き出し量及び洗浄した流動媒体の投入量によって炉床温度の制御を行うことを特徴とする焼却設備又はガス化設備の運転方法。 In the method for operating an incineration facility or a gasification facility according to any one of claims 7 to 11,
A method for operating an incineration facility or a gasification facility, wherein the hearth temperature is controlled by the amount of the fluid medium extracted and the amount of the washed fluid medium introduced.
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JP2009275975A (en) * 2008-05-14 2009-11-26 Kobelco Eco-Solutions Co Ltd Operating method of fluidized bed pyrolytic furnace
JP2010522148A (en) * 2007-03-19 2010-07-01 アルケマ フランス How to vaporize glycerol
CN102492481A (en) * 2011-12-07 2012-06-13 山东省科学院能源研究所 Method and device for eliminating biomass gasification slagging of fluidized bed
WO2013121087A1 (en) * 2012-02-15 2013-08-22 Metso Power Oy An arrangement for recirculating bed material in connection with a boiler
CN103629673A (en) * 2013-12-12 2014-03-12 安徽今朝环保科技有限公司 Industrial waste salt processing device based on heat exchange of fluidized bed combustion boiler and high-temperature heat pipes
JP2018080247A (en) * 2016-11-16 2018-05-24 株式会社Ihi Gasified gas generation system
CN117682592A (en) * 2024-02-02 2024-03-12 南京宇清环境科技有限公司 Device and method for simultaneously treating high-salt-content high-COD industrial wastewater and industrial solid waste salt

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2010522148A (en) * 2007-03-19 2010-07-01 アルケマ フランス How to vaporize glycerol
JP2009275975A (en) * 2008-05-14 2009-11-26 Kobelco Eco-Solutions Co Ltd Operating method of fluidized bed pyrolytic furnace
CN102492481A (en) * 2011-12-07 2012-06-13 山东省科学院能源研究所 Method and device for eliminating biomass gasification slagging of fluidized bed
CN102492481B (en) * 2011-12-07 2013-11-13 山东省科学院能源研究所 Method and device for eliminating biomass gasification slagging of fluidized bed
WO2013121087A1 (en) * 2012-02-15 2013-08-22 Metso Power Oy An arrangement for recirculating bed material in connection with a boiler
CN103629673A (en) * 2013-12-12 2014-03-12 安徽今朝环保科技有限公司 Industrial waste salt processing device based on heat exchange of fluidized bed combustion boiler and high-temperature heat pipes
JP2018080247A (en) * 2016-11-16 2018-05-24 株式会社Ihi Gasified gas generation system
CN117682592A (en) * 2024-02-02 2024-03-12 南京宇清环境科技有限公司 Device and method for simultaneously treating high-salt-content high-COD industrial wastewater and industrial solid waste salt
CN117682592B (en) * 2024-02-02 2024-06-11 南京宇清环境科技有限公司 Device and method for simultaneously treating high-salt-content high-COD industrial wastewater and industrial solid waste salt

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