JP3306849B2 - Waste incineration method - Google Patents
Waste incineration methodInfo
- Publication number
- JP3306849B2 JP3306849B2 JP20899498A JP20899498A JP3306849B2 JP 3306849 B2 JP3306849 B2 JP 3306849B2 JP 20899498 A JP20899498 A JP 20899498A JP 20899498 A JP20899498 A JP 20899498A JP 3306849 B2 JP3306849 B2 JP 3306849B2
- Authority
- JP
- Japan
- Prior art keywords
- temperature
- waste
- dust
- combustion gas
- fluidized incinerator
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、下水汚泥等の廃棄
物のエネルギーを効率良く回収しながら焼却することが
できる廃棄物焼却方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a waste incineration method capable of incineration while efficiently recovering energy of waste such as sewage sludge.
【０００２】[0002]
【従来の技術】下水汚泥等の廃棄物をエネルギーを回収
しながら焼却するための従来の代表的なフローが、図３
に示されている。この図３のフローでは、下水汚泥等の
廃棄物を気泡流動焼却炉２１で流動焼却させ、その高温
燃焼ガスを空気予熱器２２に通して一部の熱を回収した
うえ、廃熱ボイラ２３に通して熱回収し、得られた蒸気
で蒸気タービン２４を備えた発電機３０を運転してい
る。また廃熱ボイラ２３を出た２５０℃程度の低温排ガ
スは低温集塵機２５で焼却灰を分離したのち、排煙処理
塔２６で排煙処理され、煙突２７から放出されている。
なお、２８は白煙防止器、２９は復水器である。2. Description of the Related Art A typical conventional flow for incinerating waste such as sewage sludge while recovering energy is shown in FIG.
Is shown in In the flow of FIG. 3, waste such as sewage sludge is fluidized and incinerated in a bubble fluidized incinerator 21, and the high-temperature combustion gas is passed through an air preheater 22 to recover a part of the heat. The generator 30 provided with the steam turbine 24 is operated with the obtained steam. Further, the low-temperature exhaust gas of about 250 ° C. that has exited the waste heat boiler 23 is separated into incinerated ash by the low-temperature dust collector 25, is subjected to the flue gas treatment in the flue gas treatment tower 26, and is discharged from the chimney 27.
In addition, 28 is a white smoke prevention device, and 29 is a condenser.
【０００３】ところがこのような従来の廃棄物焼却方法
では、気泡流動焼却炉２１を出たダスト濃度の高い高温
燃焼ガスが直接空気予熱器２２や廃熱ボイラ２３等に入
るため、これらの伝熱面がダストの付着により汚れ易い
という問題があった。このため伝熱面の総括伝熱係数が
減少し、エネルギーの回収効率が低くなるうえ、伝熱面
積を大きく取らねばならないという問題があった。また
伝熱面に付着したダストを除去するためにボイラにより
得られた蒸気の一部を用いてスートブローを作動させね
ばならず、これによる蒸気ロスが更にエネルギーの回収
効率を引き下げる要因となっていた。However, in such a conventional waste incineration method, high-temperature combustion gas having a high dust concentration exiting the bubble fluidized incinerator 21 directly enters the air preheater 22, the waste heat boiler 23 and the like. There is a problem that the surface is easily stained by the adhesion of dust. For this reason, there has been a problem that the overall heat transfer coefficient of the heat transfer surface decreases, the energy recovery efficiency decreases, and the heat transfer area must be large. In addition, soot blow had to be operated using part of the steam obtained by the boiler in order to remove dust attached to the heat transfer surface, and the steam loss caused by this caused a further reduction in energy recovery efficiency. .
【０００４】この他、廃熱ボイラ２３の高温腐食を抑制
するために、廃熱ボイラ２３で得られる蒸気の温度を３
５０℃よりも高くすることが難しく、また廃熱ボイラ２
３の低温腐食を抑制するために、出口温度を２５０℃よ
りも下げることは難しい。このために廃熱ボイラ２３の
入口と出口のガスの温度差に限界があり、十分な熱回収
が行えないことや発電効率が低くなるという問題があっ
た。In addition, in order to suppress high-temperature corrosion of the waste heat boiler 23, the temperature of steam obtained by the waste heat
It is difficult to raise the temperature above 50 ° C and waste heat boiler 2
In order to suppress the low temperature corrosion of No. 3, it is difficult to lower the outlet temperature below 250 ° C. For this reason, there is a limit to the temperature difference between the gas at the inlet and the outlet of the waste heat boiler 23, and there has been a problem that sufficient heat recovery cannot be performed and power generation efficiency is reduced.
【０００５】[0005]
【発明が解決しようとする課題】本発明は上記した従来
の問題点を解決し、廃熱ボイラ等の伝熱面へのダストの
付着を防止でき、また廃熱ボイラの高温腐食や低温腐食
を防止でき、スートブローによる蒸気ロスも無くするこ
とができ、その結果として従来よりも優れたエネルギー
の回収効率を達成することができる廃棄物焼却方法を提
供するためになされたものである。SUMMARY OF THE INVENTION The present invention solves the above-mentioned conventional problems, prevents dust from adhering to a heat transfer surface of a waste heat boiler or the like, and prevents high-temperature corrosion and low-temperature corrosion of the waste heat boiler. An object of the present invention is to provide a waste incineration method capable of preventing waste, eliminating steam loss due to soot blow, and consequently achieving higher energy recovery efficiency than before.
【０００６】[0006]
【課題を解決するための手段】上記の課題を解決するた
めになされた廃棄物焼却方法は、流動焼却炉に廃棄物と
ともに脱硫剤を投入して抑制燃焼させ、炉内で脱硫され
た抑制燃焼ガスを熱回収器に通して冷却し、６００℃〜
６５０℃の温度で脱塩し、脱塩された抑制燃焼ガスをろ
過式フィルタからなる高温集塵機に通して、ダストが付
着した表面において脱硫、脱塩を進行させ，かつ除塵し
た後に完全燃焼させ、その清浄な完全燃焼ガスを廃熱ボ
イラに通して熱回収することを特徴とするものである。 Waste incineration process has been made to solve the above problems BRIEF SUMMARY OF THE INVENTION may flow incinerator by introducing a desulfurizing agent by suppressing the combustion with waste, which is desulfurized in a furnace suppressed The combustion gas is cooled by passing it through a heat recovery unit.
Demineralize at a temperature of 650 ° C and filter out the desalinated suppressed combustion gas.
Dust is passed through a high-temperature dust collector consisting of
It is characterized in that desulfurization and desalination are advanced on the surface on which it is deposited , and after the dust is removed, it is completely burned, and the clean completely burned gas is passed through a waste heat boiler to recover heat.
【０００７】なお、流動焼却炉としては気泡流動焼却炉
よりも循環流動焼却炉が好ましく、高温集塵機はセラミ
ックフィルタのような高温のろ過式フィルタであること
が好ましい。特に下水汚泥のように高水分の廃棄物を処
理する場合には、循環流動焼却炉が用いられると温度が
均一化し、抑制燃焼を行う際の温度制御が容易となる点
で好ましい。The fluidized incinerator is more preferably a circulating fluidized incinerator than a bubble fluidized incinerator, and the high-temperature dust collector is preferably a high-temperature filter such as a ceramic filter. In particular, when treating high-moisture waste such as sewage sludge, it is preferable to use a circulating fluidized incinerator because the temperature becomes uniform and the temperature control during suppressed combustion becomes easy.
【０００８】本発明によれば、脱硫・脱塩された抑制燃
焼ガスを高温集塵機に通して除塵した後に完全燃焼さ
せ、その清浄な完全燃焼ガスを廃熱ボイラに通して熱回
収するので、廃熱ボイラ等の伝熱面へのダストの付着は
ほとんど生じない。このため伝熱面の総括伝熱係数が大
きくなり、スートブローによる蒸気ロスもなくなるの
で、優れたエネルギーの回収効率を達成することができ
る。しかも流動焼却炉で抑制燃焼を行わせるので、抑制
燃焼ガス量は通常の燃焼ガス量よりも少なくなる。この
ため高温集塵機のろ過面積を小さくすることができ、設
備の小型化を図ることができる。According to the present invention, desulfurized and desalinated suppressed combustion gas is passed through a high-temperature dust collector to remove dust, and then completely burned, and the clean complete combustion gas is passed through a waste heat boiler to recover heat. Dust hardly adheres to the heat transfer surface of a heat boiler or the like. For this reason, the overall heat transfer coefficient of the heat transfer surface is increased, and steam loss due to soot blowing is also eliminated, so that excellent energy recovery efficiency can be achieved. Moreover, since the suppression combustion is performed in the fluidized incinerator, the suppression combustion gas amount is smaller than the normal combustion gas amount. For this reason, the filtration area of the high-temperature dust collector can be reduced, and the size of the equipment can be reduced.
【０００９】[0009]
【発明の実施の形態】以下に本発明の好ましい実施形態
を示す。図１は本発明の前提となる参考形態を示すフロ
ーシートであり、１は廃棄物を焼却するための流動焼却
炉である。この形態では廃棄物は下水汚泥脱水汚泥であ
り、流動焼却炉１は好ましくは循環流動焼却炉である。
この流動焼却炉１には廃棄物とともに脱硫・脱塩剤であ
るCa(OH)2、CaCO3、CaO 等が投入され、空気比λが0.7
〜0.9 程度、温度700 ℃程度の抑制燃焼を行う。脱硫・
脱塩剤は流動焼却炉１の内部を循環しつつ硫黄分や塩素
と反応し、脱硫・脱塩を炉内で行う。循環流動焼却炉を
用れば、抑制燃焼による温度調整が気泡流動炉よりも容
易であり、また攪拌効率も高いためにより優れた脱硫・
脱塩効果を得ることができる。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of the present invention will be described below. FIG. 1 is a flow sheet showing a reference embodiment as a premise of the present invention , and 1 is a fluidized incinerator for incinerating waste. Waste in the form state this is sewage sludge dewatering sludge, flow incinerator 1 is preferably a circulating fluidized incinerator.
In this fluidized incinerator 1, desulfurization / desalting agents such as Ca (OH) 2 , CaCO 3 , CaO and the like are introduced together with the waste, and the air ratio λ is 0.7.
Suppress combustion at ~ 0.9 ° C and 700 ° C. Desulfurization
The desalting agent reacts with sulfur and chlorine while circulating in the fluidized incinerator 1, and performs desulfurization and desalination in the furnace. If a circulating fluidized incinerator is used, temperature control by suppressed combustion is easier than in a bubble fluidized-bed incinerator, and because of its high stirring efficiency, superior desulfurization and
A desalting effect can be obtained.
【００１０】なお、本発明では、脱硫・脱塩された抑制
燃焼ガスはダストを含むため、高温集塵機２に導かれて
除塵される。高温集塵機２としては700 ℃程度の高温で
除塵できるセラミックフィルタや高温バグフィルタのよ
うな高温のろ過式フィルタを用いることが必要である。
これらの高温のろ過式フィルタは集塵効率が高いうえ
に、ダストが付着した表面においても脱硫・脱塩を進行
させることができる利点がある。更にこのような高温集
塵を行えば、ダスト中のダイオキシンが再合成されにく
い利点がある。焼却灰は高温集塵機２から取り出され
る。In the present invention, since the desulfurized and desalted suppressed combustion gas contains dust, it is guided to the high-temperature dust collector 2 to be removed. As the high-temperature dust collector 2, it is necessary to use a high-temperature filtration filter such as a ceramic filter or a high-temperature bag filter capable of removing dust at a high temperature of about 700 ° C.
These high-temperature filtration filters have high dust collection efficiency and have the advantage that desulfurization and desalination can be advanced even on the surface to which dust is attached. Further, if such high-temperature dust collection is performed, there is an advantage that dioxin in the dust is hardly resynthesized. The incinerated ash is taken out of the high-temperature dust collector 2.
【００１１】このようにして高温集塵機２で除塵された
抑制燃焼ガスは、後燃焼炉３で完全燃焼される。このと
き、外部から燃焼用空気と必要に応じて重油等の燃料が
供給される。この後燃焼炉３から出た完全燃焼ガスはダ
ストを含まない850 ℃程度の高温のガスであり、空気予
熱器４で一部の熱を回収され650 ℃程度まで降温された
うえで廃熱ボイラ５に送られる。なお、空気予熱器４に
より650 ℃程度まで予熱された空気は、流動焼却炉１に
吹き込まれる。The suppressed combustion gas thus removed by the high-temperature dust collector 2 is completely burned in the post-burning furnace 3. At this time, combustion air and fuel such as heavy oil are supplied from the outside as needed. Thereafter, the complete combustion gas discharged from the combustion furnace 3 is a high-temperature gas of about 850 ° C. containing no dust, and a part of the heat is recovered by the air preheater 4 and the temperature is lowered to about 650 ° C. Sent to 5. The air preheated to about 650 ° C. by the air preheater 4 is blown into the fluidized incinerator 1.
【００１２】廃熱ボイラ５は空気予熱器４を通過した完
全燃焼ガスを熱源として蒸気を発生させ、蒸気タービン
６を備えた発電機７により発電を行う。上記したよう
に、後燃焼炉３から出た完全燃焼ガスはダストを含まな
い清浄なガスであるから、空気予熱器４及び廃熱ボイラ
５は低ダスト濃度仕様とすることができる。その結果、
熱回収構造の簡素化とガス流速の高速化が可能となり、
総括伝熱係数が大きくなって伝熱面積の小型化を図るこ
とができる。またダスト除去のためのスートブローが不
要となり、エネルギー回収効率を上げることができる。The waste heat boiler 5 generates steam by using the complete combustion gas passing through the air preheater 4 as a heat source, and generates electric power by a generator 7 having a steam turbine 6. As described above, since the complete combustion gas discharged from the post-burning furnace 3 is a clean gas containing no dust, the air preheater 4 and the waste heat boiler 5 can have low dust concentration specifications. as a result,
It is possible to simplify the heat recovery structure and increase the gas flow speed,
The overall heat transfer coefficient increases, and the heat transfer area can be reduced in size. In addition, soot blowing for removing dust is not required, and energy recovery efficiency can be improved.
【００１３】さらにまた、廃熱ボイラ５に入るガスは予
め炉内で脱硫・脱塩が行われたガスであるから、ボイラ
水管の高温腐食が回避できる。このため蒸気温度及び蒸
気圧力を上げることができ、発電効率が向上する。同様
に、廃熱ボイラ５に入るガスは予め炉内で脱硫・脱塩が
行われたガスであるから酸露点が低下し、ボイラ水管の
低温腐食も回避できる。このためボイラ出口の排ガス温
度を従来よりも50℃低温の200 ℃程度とすることがで
き、その結果としてボイラでの回収熱量が増加し、発電
量を増加させることができる。Further, since the gas entering the waste heat boiler 5 is a gas which has been desulfurized and desalted in the furnace in advance, high-temperature corrosion of the boiler water tube can be avoided. Therefore, the steam temperature and the steam pressure can be increased, and the power generation efficiency is improved. Similarly, the gas entering the waste heat boiler 5 is gas that has been desulfurized and desalted in the furnace in advance, so that the acid dew point is lowered, and low temperature corrosion of the boiler water tube can be avoided. For this reason, the temperature of the exhaust gas at the boiler outlet can be reduced to about 200 ° C., which is 50 ° C. lower than the conventional one, and as a result, the amount of heat recovered in the boiler increases, and the amount of power generation can be increased.
【００１４】なお、蒸気タービン６を出た蒸気は復水器
８で空気との熱交換が行われて冷却されて廃熱ボイラ５
に戻る。復水器８により加熱された空気は後燃焼炉３に
送られるとともに、一部は煙突１０に送られて白煙防止
を行う。このように復水器８に、後燃焼炉３の空気予熱
器と白煙防止器との働きを兼用させることにより、発電
以外に使用する蒸気量が削減でき、発電量の増加を図る
ことができる。廃熱ボイラ５を出たガスは排煙処理塔９
で処理され、煙突１０から排出される。The steam that has exited the steam turbine 6 undergoes heat exchange with air in a condenser 8 to be cooled, and the steam is cooled.
Return to The air heated by the condenser 8 is sent to the post-burning furnace 3 and a part is sent to the chimney 10 to prevent white smoke. In this way, by making the condenser 8 also function as the air preheater and the white smoke suppressor of the post-combustion furnace 3, the amount of steam used for other than power generation can be reduced, and the amount of power generation can be increased. it can. The gas discharged from the waste heat boiler 5 is converted into a flue gas treatment tower 9
And discharged from the chimney 10.
【００１５】上記したように、この形態によれば従来よ
りも廃熱ボイラ５等の伝熱面積の小型化と発電量の増加
とを図ることができる。具体的には、水分75％の下水脱
水汚泥を焼却する300t/day規模の処理場では、図３の従
来システムの場合には廃熱ボイラ５本体の伝熱面積は71
0m2でスートブローに200kg/h の蒸気を要し、発電量は7
20kW 程度であった。これに対して図１に示したこの形
態によれば、廃熱ボイラ５本体の伝熱面積は540m2でス
ートブローに蒸気を供給する必要は無くなり、発電量は
1000kWにまで増大する。As described above, according to this embodiment , it is possible to reduce the size of the heat transfer area of the waste heat boiler 5 and the like and increase the amount of power generation as compared with the related art. Specifically, in a 300 t / day treatment plant that incinerates sewage dewatered sludge of 75% moisture, the heat transfer area of the waste heat boiler 5 body is 71 in the case of the conventional system of FIG.
In 0 m 2 in soot-blowing it takes steam 200 kg / h, the power generation amount 7
It was about 20kW. On the other hand, this form shown in FIG.
According to the state , the heat transfer area of the waste heat boiler 5 body is 540 m 2 and there is no need to supply steam to the soot blow, and the power generation amount is
Increase to 1000kW.
【００１６】図２は本発明の実施形態を示すものであ
る。先の参考形態では流動焼却炉１の炉内で脱硫と脱塩
を行わせていたが、本発明の実施形態では炉内で脱硫の
み行い、空気予熱器４でガス温度を850 ℃から600 〜65
0 ℃まで降温させてから反応器１１で脱塩を行うように
した点が相違する。その他の点は先に説明した参考形態
と特に変わるところはない。脱硫剤としては例えばCa(O
H)2、CaCO3、CaO 等が使用でき、脱塩剤としては例えば
Ca(OH)2、CaO が使用できる。脱硫と脱塩は好ましい反
応温度が異なるため、このように二段階に分けて反応さ
せることでより確実な脱硫・脱塩が可能となる。この請
求項２の発明の流動焼却炉１も、循環流動焼却炉である
ことが好ましい。FIG. 2 shows an embodiment of the present invention. In the previous embodiment , desulfurization and desalination were performed in the furnace of the fluidized incinerator 1, but in the embodiment of the present invention, only desulfurization was performed in the furnace, and the gas temperature was increased from 850 ° C. to 600 to 600 ° C. by the air preheater 4. 65
The difference is that the temperature is lowered to 0 ° C. before desalting in the reactor 11. The other points are not particularly different from the reference embodiment described above . As a desulfurizing agent, for example, Ca (O
H) 2 , CaCO 3 , CaO and the like can be used.
Ca (OH) 2 and CaO can be used. Since desulfurization and desalination have different preferred reaction temperatures, more reliable desulfurization and desalination can be achieved by performing the reaction in two stages in this manner. The fluidized-bed incinerator 1 according to the second aspect of the present invention is also preferably a circulating fluidized-bed incinerator.
【００１７】[0017]
【発明の効果】以上に説明したように、本発明によれば
廃熱ボイラや空気予熱器等等の伝熱面へのダストの付着
を防止でき、また廃熱ボイラの高温腐食や低温腐食を防
止でき、スートブローによる蒸気ロスも無くすることが
できる。その結果として、本発明によれば従来よりも小
型の設備で従来よりも優れたエネルギーの回収効率を達
成することができる大きい効果がある。As described above, according to the present invention, it is possible to prevent dust from adhering to a heat transfer surface of a waste heat boiler, an air preheater, or the like, and to prevent high temperature corrosion and low temperature corrosion of the waste heat boiler. This can prevent steam loss due to soot blowing. As a result, according to the present invention, there is a great effect that energy recovery efficiency superior to the conventional one can be achieved with a facility smaller than the conventional one.
【図１】本発明の参考形態を示すフローシートである。FIG. 1 is a flow sheet showing a reference embodiment of the present invention.
【図２】本発明の実施形態を示すフローシートである。FIG. 2 is a flow sheet showing an embodiment of the present invention.
【図３】従来例を示すフローシートである。FIG. 3 is a flow sheet showing a conventional example.
１ 流動焼却炉、２ 高温集塵機、３ 後燃焼炉、４
空気予熱器、５ 廃熱ボイラ、６ 蒸気タービン、７
発電機、８ 復水器、９ 排煙処理塔、１０煙突、１１
反応器、２１ 従来の低温集塵機、２６ 排煙処理
塔、２７ 煙突、２８ 白煙防止器、２９ 復水器、３
０ 発電機1 fluidized incinerator, 2 high-temperature dust collector, 3 post-combustion furnace, 4
Air preheater, 5 Waste heat boiler, 6 Steam turbine, 7
Generator, 8 condenser, 9 flue gas treatment tower, 10 chimney, 11
Reactor, 21 conventional low-temperature dust collector, 26 flue gas treatment tower, 27 chimney, 28 white smoke suppressor, 29 condenser, 3
0 generator
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平７−71731（ＪＰ，Ａ) 特開 平10−169935（ＪＰ，Ａ) 特開 平10−103640（ＪＰ，Ａ) 特開 平６−109219（ＪＰ，Ａ) 特開 平３−195809（ＪＰ，Ａ) 特開 平５−172309（ＪＰ，Ａ) 特開 平９−42631（ＪＰ，Ａ) 特開 昭56−113918（ＪＰ，Ａ) 特開 昭58−12927（ＪＰ，Ａ) 特開 昭58−61181（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) F23G 5/027 F23G 5/00 F23G 5/14 F23G 5/46 ────────────────────────────────────────────────── ─── Continuation of the front page (56) References JP-A-7-71731 (JP, A) JP-A-10-169935 (JP, A) JP-A-10-103640 (JP, A) 109219 (JP, A) JP-A-3-195809 (JP, A) JP-A-5-172309 (JP, A) JP-A-9-42631 (JP, A) JP-A-56-113918 (JP, A) JP-A-58-12927 (JP, A) JP-A-58-61181 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) F23G 5/027 F23G 5/00 F23G 5/14 F23G 5/46
Claims (2)
入して抑制燃焼させ、炉内で脱硫された抑制燃焼ガスを
熱回収器に通して冷却し、６００℃〜６５０℃の温度で
脱塩し、脱塩された抑制燃焼ガスをろ過式フィルタから
なる高温集塵機に通して、ダストが付着した表面におい
て脱硫、脱塩を進行させ，かつ除塵した後に完全燃焼さ
せ、その清浄な完全燃焼ガスを廃熱ボイラに通して熱回
収することを特徴とする廃棄物焼却方法。1. A fluidized incinerator is charged with a desulfurizing agent together with waste to suppress combustion, and the suppressed combustion gas desulfurized in the furnace is cooled by passing through a heat recovery unit, and is cooled at a temperature of 600 ° C. to 650 ° C. br /> Demineralized and desalted suppressed combustion gas is filtered from the filter
Made through the high-temperature dust collector, the surface odor dust adhered
A waste incineration method characterized by promoting desulfurization and desalination, removing dust, burning completely , and passing the clean complete combustion gas through a waste heat boiler to recover heat.
項１に記載の廃棄物焼却方法。Wherein according fluidized incinerator is circulating fluidized incinerator
Item 4. The waste incineration method according to Item 1 .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20899498A JP3306849B2 (en) | 1998-07-24 | 1998-07-24 | Waste incineration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20899498A JP3306849B2 (en) | 1998-07-24 | 1998-07-24 | Waste incineration method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000039121A JP2000039121A (en) | 2000-02-08 |
| JP3306849B2 true JP3306849B2 (en) | 2002-07-24 |
Family
ID=16565570
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP20899498A Expired - Fee Related JP3306849B2 (en) | 1998-07-24 | 1998-07-24 | Waste incineration method |
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| Country | Link |
|---|---|
| JP (1) | JP3306849B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4542417B2 (en) * | 2004-11-26 | 2010-09-15 | 新日鉄エンジニアリング株式会社 | Method of treating combustible gas in waste melting furnace |
| JP5692853B2 (en) * | 2011-01-13 | 2015-04-01 | 新日鉄住金エンジニアリング株式会社 | How to dry wood chips |
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|---|---|
| JP2000039121A (en) | 2000-02-08 |
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