JP3276273B2 - Superheated steam production equipment using waste incineration heat - Google Patents
Superheated steam production equipment using waste incineration heatInfo
- Publication number
- JP3276273B2 JP3276273B2 JP26246595A JP26246595A JP3276273B2 JP 3276273 B2 JP3276273 B2 JP 3276273B2 JP 26246595 A JP26246595 A JP 26246595A JP 26246595 A JP26246595 A JP 26246595A JP 3276273 B2 JP3276273 B2 JP 3276273B2
- Authority
- JP
- Japan
- Prior art keywords
- steam
- char
- combustion
- pyrolysis
- gas
- 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
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Landscapes
- Incineration Of Waste (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Gasification And Melting Of Waste (AREA)
Description
【0001】[0001]
【発明の属する技術分野】本発明は、都市ごみや産業廃
棄物等を焼却し、その燃焼排ガスの熱により蒸気を製造
して、例えば該蒸気を発電プラント等に用いる過熱蒸気
製造に関する発明である。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to the production of superheated steam by incinerating municipal refuse or industrial waste, producing steam by the heat of the combustion exhaust gas, and using the steam in a power plant or the like. .
【0002】[0002]
【従来の技術】従来より都市ごみ等の廃棄物を焼却する
焼却装置には流動床焼却装置が多く用いられ、かかる装
置は流動床焼却炉内の分散板(例えば多孔板)上に収容
された砂等の流動媒体に分散板下方より空気または焼却
排ガス等を吹き込むことにより流動媒体を流動化すると
ともに加熱し、そのようにして形成された流動床内に都
市ごみ等の廃棄物を投入して燃焼させる。この燃焼によ
り発生した燃焼ガスは、燃焼ガス出口ラインを経てボイ
ラに至り、該ボイラ内で温水との熱接触により蒸気を発
生させ、該蒸気を発電プラント等のタービン駆動源とし
て用いるものである。2. Description of the Related Art Conventionally, fluidized bed incinerators are often used as incinerators for incinerating waste such as municipal solid waste, and such apparatuses are accommodated on a dispersion plate (for example, a perforated plate) in a fluidized bed incinerator. The fluidized medium is fluidized and heated by blowing air or incineration exhaust gas etc. from below the dispersion plate into the fluidized medium such as sand, and waste such as municipal solid waste is thrown into the fluidized bed thus formed. Burn. The combustion gas generated by the combustion reaches a boiler via a combustion gas outlet line, generates steam by thermal contact with hot water in the boiler, and uses the steam as a turbine drive source of a power plant or the like.
【0003】[0003]
【発明が解決しようとする課題】さてかかる都市ごみ等
の廃棄物中には塩ビプラスチック等の含塩素有機化合物
が混入しており、可燃分中にC1として約0.2〜0.
5%含有されている。そして都市ごみ等の廃棄物中に混
入した塩ビプラスチック等に含まれる塩素は、燃焼によ
ってHC1となり(通常、都市ごみ燃焼排ガス中のHC
1は約500〜1000ppm)、焼却炉の後流に設置さ
れた蒸気発生用ボイラのチューブに作用してこれを腐食
させる。特にチューブ表面温度が約350℃以上では温
度の増加とともに高温腐食が顕著となる。このため、従
来、チューブ表面温度は350℃以下にする必要があ
り、製造される蒸気の温度は約300℃が限界であっ
た。その結果、従来のごみ焼却による発電効率は約15
%以下であって、塩素を殆ど含有しない重油やLNG等
を燃料とし、ボイラチューブ温度を500〜600℃に
できるプラントの発電効率約40%に比べて著しく低
く、その改善が強く望まれていた。The waste such as municipal solid waste contains a chlorine-containing organic compound such as PVC plastic, and the flammable component has a C1 content of about 0.2 to 0.1%.
Contains 5%. Chlorine contained in PVC plastic and the like mixed into waste such as municipal waste becomes HC1 by combustion (usually, HC1 contained in flue gas from municipal waste combustion).
(1 is about 500 to 1000 ppm), which acts on the tube of the steam generation boiler installed downstream of the incinerator to corrode it. In particular, when the tube surface temperature is about 350 ° C. or higher, high-temperature corrosion becomes remarkable as the temperature increases. For this reason, conventionally, the tube surface temperature had to be 350 ° C. or less, and the temperature of the produced steam was limited to about 300 ° C. As a result, the power generation efficiency of conventional waste incineration is about 15
% Or less, and using fuel such as heavy oil or LNG containing almost no chlorine as fuel, which is remarkably lower than the power generation efficiency of a plant capable of setting the boiler tube temperature to 500 to 600 ° C. of about 40%, and its improvement has been strongly desired. .
【0004】本発明者らはかかる技術的課題に鑑み、先
の出願において(出願番号:特願平6−324843
号、特願平7−140484号)、前記焼却炉としての
流動床内で、温度300〜700℃で処理したところ、
該流動床からの未分解残渣および流動媒体から成るチャ
ー混合物からは実質的に塩素を含有しない未分解残渣が
得られることを見出した。すなわち、廃棄物中に含まれ
ていた塩素は、実質的に全て熱分解ガスに含まれて、熱
分解ガス出口ラインに排出されることを見出した。[0004] In view of such technical problems, the present inventors have filed an earlier application (Application No .: Japanese Patent Application No. 6-324843).
, In a fluidized bed as the incinerator, at a temperature of 300 to 700 ° C.
It has been found that a char mixture consisting of the uncracked residue from the fluidized bed and the fluidized medium results in a substantially chlorine-free uncracked residue. That is, it was found that substantially all chlorine contained in the waste was contained in the pyrolysis gas and was discharged to the pyrolysis gas outlet line.
【0005】そして、かかる知見に基づき、焼却装置側
には、温度300℃以上の空間内に廃棄物を供給して熱
分解反応を行なわせ、その反応により発生した熱分解ガ
スと未分解残渣および流動媒体から成るチャー混合物と
不燃物とを互いに分離する第1の流動床(以下熱分解手
段という)とともに、前記チャー混合物を空気または燃
焼排ガスによって上方に吹き飛ばしながら前記未分解残
渣を完全燃焼させる第2の流動床(以下チャー燃焼手段
という)を設け、一方ボイラ側には第1及び第2のボイ
ラを実質的に直列に接続し、低段側のボイラで前記熱分
解ガスの熱を利用して約400℃以下、具体的には30
0℃前後の温水または蒸気を製造(以下第1の蒸気製造
手段という)し、次に該300℃前後の温水または蒸気
を第2のボイラに導入して前記チャー燃焼手段より得ら
れた燃焼ガスの熱により略500℃若しくはそれ以上の
過熱蒸気を製造(以下第2の蒸気製造手段という)する
ようにした過熱蒸気製造が提案されている。[0005] Based on such knowledge, the incinerator side supplies waste into a space having a temperature of 300 ° C or higher to cause a pyrolysis reaction, and generates a pyrolysis gas generated by the reaction, undecomposed residues and A first fluidized bed (hereinafter referred to as a pyrolysis means) for separating a char mixture composed of a fluidized medium and an incombustible substance from each other, and a method for completely burning the undecomposed residue while blowing the char mixture upward by air or combustion exhaust gas. 2 fluidized beds (hereinafter referred to as char combustion means), while the first and second boilers are connected in series on the boiler side, and the heat of the pyrolysis gas is utilized in the lower stage boiler. About 400 ° C or less, specifically 30
Hot water or steam at about 0 ° C. is produced (hereinafter referred to as first steam producing means), and then the hot water or steam at about 300 ° C. is introduced into a second boiler to obtain combustion gas obtained from the char burning means. Has been proposed to produce superheated steam of about 500 ° C. or higher by the heat of the superheated steam (hereinafter referred to as second steam production means).
【0006】本発明は、かかる先願技術を更に発展さ
せ、塩素によるボイラチューブの高温腐食を防止しなが
ら高温・高圧の過熱蒸気を効率的に得ることのできる過
熱蒸気の製造にかかる発明を提供する事にある。本発明
の他の目的は前記チャー燃焼手段におけるチャー燃焼と
熱分解手段における熱分解を効率良く行い、先願技術に
おいて比較して更に効率良く塩素の低減ともに且つ高温
度の過熱蒸気を得ることの出来る過熱蒸気の製造にかか
る発明を提供する事にある。The present invention further develops such prior art and provides an invention relating to the production of superheated steam capable of efficiently obtaining high temperature and high pressure superheated steam while preventing high temperature corrosion of the boiler tube due to chlorine. To do. Another object of the present invention is to efficiently perform the char combustion in the char combustion means and the pyrolysis in the pyrolysis means, and to more efficiently reduce chlorine and obtain superheated steam at a high temperature as compared with the prior art. It is an object of the present invention to provide a superheated steam that can be produced.
【0007】[0007]
【課題を解決するための手段】請求項1及び2記載の発
明は、温度300℃以上、好ましくは温度300〜70
0℃の空間内に廃棄物を供給して熱分解反応を行なわ
せ、その反応により発生した熱分解ガスと未分解残渣お
よび流動媒体から成るチャー混合物と不燃物とを互いに
分離する例えば流動床等の熱分解手段と、空気または燃
焼排ガスによって前記チャー混合物を上方に吹き飛ばし
ながら前記未分解残渣を完全燃焼させる例えば流動床や
熱分解炉等のチャー燃焼手段と、前記熱分解ガスを灰溶
融炉に導入し、該灰溶融炉内に空気若しくは酸素富化空
気を前記熱分解ガスと共に導入して該熱分解ガス燃焼熱
により灰分を溶融する灰溶融手段と、前記熱分解ガスを
直接若しくは灰溶融手段通過後再燃焼させて、その熱を
利用して好ましくは約400℃以下、具体的には略30
0〜350℃以下の温水または蒸気を製造する第1の蒸
気製造手段と、前記チャー燃焼手段により得られた燃焼
ガスの熱により前記第1の蒸気製造手段で製造された温
水または蒸気を過熱蒸気とする第2の蒸気製造手段とを
含み、前記熱分解手段とチャー燃焼手段間を接続するチ
ャー通路中に、チャー逆流防止手段を配置したことを特
徴とするものである。According to the first and second aspects of the present invention, a temperature of 300.degree. C. or more, preferably 300 to 70.degree.
A waste material is supplied into a space at 0 ° C. to cause a pyrolysis reaction, and a pyrolysis gas generated by the reaction, a char mixture comprising an undecomposed residue and a fluid medium, and an incombustible material are separated from each other, for example, a fluidized bed. A pyrolysis means, a char combustion means such as a fluidized bed or a pyrolysis furnace for completely burning the undecomposed residue while blowing the char mixture upward by air or combustion exhaust gas, and ash melting the pyrolysis gas.
Air or oxygen-enriched air in the ash melting furnace.
Gas is introduced together with the pyrolysis gas to produce a heat of combustion of the pyrolysis gas.
Ash melting means for melting the ash component, and recombusting the pyrolysis gas directly or after passing through the ash melting means , and utilizing the heat, preferably about 400 ° C. or less, specifically about 30 ° C.
First steam producing means for producing hot water or steam at a temperature of 0 to 350 ° C. or lower; and superheated steam produced by the first steam producing means by the heat of the combustion gas obtained by the char burning means. A second steam producing means, wherein a char backflow preventing means is arranged in a char passage connecting between the pyrolysis means and the char burning means.
【0008】そしてこのような逆流防止手段は、例えば
図2に示すような、前記熱分解手段側へのチャー混合物
界面をチャー燃焼手段側のチャ−混合物界面より大に設
定することによりガスの逆流防止機能をもたせた例えば
シールポットのような、圧力差形成手段により構成して
も良く、又前記逆流防止手段を、図3に示すように、前
記熱分解手段側よりチャー燃焼手段側へ強制的にチャー
の搬送を行う機械的搬送手段で構成し、好ましくは該機
械的搬送手段の入口側より出口側に向け、上向きに傾斜
させ、重力差を持たせて配置して構成してもよい。[0008] Such a backflow preventing means is provided, for example, by setting the interface of the char mixture to the pyrolysis means side larger than that of the char combustion means side as shown in FIG. It may be constituted by a pressure difference forming means such as a seal pot having a preventing function, and the backflow preventing means is forcibly moved from the pyrolysis means side to the char combustion means side as shown in FIG. Alternatively, the mechanical transfer means may be configured to transfer the char, and preferably to be inclined upward from the inlet side to the outlet side of the mechanical transfer means so as to have a gravity difference.
【0009】かかる発明によれば前記いずれの請求項に
おいても熱分解手段で分離されたチャー混合物には塩素
が実質的に含まれないので、これを第2の蒸気製造手段
の過熱源として用い500℃以上の過熱蒸気を得るよう
に構成しても、機器の高温腐食は生じない。According to the invention, the char mixture separated by the thermal decomposition means contains substantially no chlorine in any of the above claims, and is used as a superheat source of the second steam production means. Even if it is configured to obtain superheated steam of not less than ° C, high-temperature corrosion of equipment does not occur.
【0010】また第1の蒸気製造手段の加熱源には、塩
素を含む熱分解ガスを用いるも、該熱を利用して約40
0℃以下、具体的には略300〜350℃以下の温水ま
たは蒸気を製造を製造するものである為に、高温腐食の
温度以下の温度しか加熱しないために、ボイラチューブ
等の腐食の恐れはない。A pyrolysis gas containing chlorine is used as a heating source of the first steam producing means.
Since it is intended to manufacture hot water or steam at a temperature of 0 ° C. or less, specifically, about 300 to 350 ° C. or less, only a temperature lower than a high temperature corrosion temperature is heated. Absent.
【0011】さて前記のようにチャー燃焼手段は、完全
燃焼を可能にする為に、流動床の背高を高くする必要が
あり、この為該燃焼手段内の圧力が高くなり、この為流
動媒体等が燃焼手段側より熱分解手段側へ逆流の恐れが
ある。そこで前記熱分解手段とチャー燃焼手段間を接続
するチャー通路中に、チャー逆流防止手段50を配し、
前記チャー燃焼手段におけるチャー燃焼と熱分解手段に
おける熱分解を効率良く行っている。As described above, in the char combustion means, it is necessary to increase the height of the fluidized bed in order to enable complete combustion, so that the pressure in the combustion means increases, and thus the fluid medium And the like may flow backward from the combustion means side to the thermal decomposition means side. Therefore, in the char passage connecting the pyrolysis means and the char combustion means, a char backflow prevention means 50 is arranged,
The char combustion in the char combustion means and the pyrolysis in the pyrolysis means are efficiently performed.
【0012】そしてこのような逆流防止手段は、例えば
図2に示すような例えばシールポットのような、圧力差
形成手段により前記熱分解手段側の圧力をP2、チャー
燃焼手段側の圧力をP1とした場合に、ΔH・ρ>P1−
P2になるように(ΔH・ρ:熱分解炉側の圧力とチャ
ー燃焼手段側の圧力の差)構成すれば良い。The backflow preventing means is configured such that the pressure on the pyrolysis means side is P 2 and the pressure on the char combustion means side is P 2 by a pressure difference forming means such as a seal pot as shown in FIG. When it is set to 1 , ΔH · ρ> P 1 −
As will become P 2 (ΔH · ρ: the difference in pressure of the pressure and char combustion means side of the pyrolysis furnace side) may be formed.
【0013】又、図3に示すように、機械的搬送手段で
逆流防止手段を構成する場合は、機械的搬送手段の入口
側より出口側に向け、上向きに傾斜させ、重力差を持た
せて配置して構成するのが良く、これにより機械的搬送
手段内が流動媒体により圧密化され、流動媒体でのガス
シール効果が増大する。又機械的搬送手段を用いること
により定量性も増大するが、コスト的又耐摩耗性の面で
はシールポットが優れている。As shown in FIG. 3, when the backflow prevention means is constituted by the mechanical transport means, the mechanical transport means is inclined upward from the inlet side to the outlet side so as to have a gravity difference. It is preferable to arrange and configure, so that the inside of the mechanical conveying means is compacted by the flowing medium, and the gas sealing effect in the flowing medium is increased. In addition, although the quantitative property is increased by using the mechanical transfer means, the seal pot is excellent in cost and abrasion resistance.
【0014】請求項3記載の発明においては、前記第1
若しくは第2の蒸気製造手段で加熱された蒸気若しくは
前記いずれかの製造手段に導入される温水若しくは蒸気
の一部を、前記燃焼手段の高温域側に配した熱交換手段
に適宜導入することを特徴とするものである。即ち、前
記燃焼手段では空気または燃焼排ガスによってチャー混
合物を上方に吹き飛ばしながら未分解残渣を分解させる
ので、その燃焼ガス中には高温の流動媒体が含まれる。
そこで本発明においては、その高温の流動媒体を利用し
て、前記チャー燃焼手段の高温域側に熱交換手段を配設
して、前記第1若しくは第2の蒸気製造手段で加熱され
た蒸気若しくは前記いずれかの製造手段に導入される温
水若しくは蒸気の一部と熱交換する事により、後記する
作用を営むことが出来る。In the third aspect of the present invention, the first
Alternatively, the steam heated by the second steam manufacturing means or a portion of the hot water or steam introduced into any of the manufacturing means may be appropriately introduced into the heat exchange means arranged on the high temperature side of the combustion means. It is a feature. That is, since the combustion means decomposes the undecomposed residue while blowing the char mixture upward by air or combustion exhaust gas, the combustion gas contains a high-temperature fluid medium.
Therefore, in the present invention, utilizing the high-temperature fluid medium, a heat exchange means is arranged on the high-temperature side of the char combustion means, and the steam or the steam heated by the first or second steam production means is used. By performing heat exchange with a part of the hot water or steam introduced into any of the above-mentioned production means, the following operation can be performed.
【0015】即ち、前記第1の蒸気製造手段に導入され
る温水を前記熱交換手段に導入してある程度の昇温を図
ることにより、熱交換手段−第1の蒸気製造手段−第2
の蒸気製造手段と、実質的に直列の3段階昇温を図るこ
とが出来、多量且つ十分加熱された過熱蒸気を得ること
が出来る。又、前記第2の蒸気製造手段に導入される温
水又は蒸気を前記第1の蒸気製造手段とともに、前記熱
交換手段にパラレルに導入することにより、第2の蒸気
製造手段の加熱量を多くする事が出来、多量の過熱蒸気
を得ることが出来る。That is, hot water introduced into the first steam producing means is introduced into the heat exchanging means to raise the temperature to a certain extent, whereby heat exchanging means-first steam producing means-second steam producing means
The temperature can be raised in three stages substantially in series with the steam production means of the above, and a large amount of sufficiently heated superheated steam can be obtained. Further, the amount of heating of the second steam producing means is increased by introducing the hot water or steam introduced into the second steam producing means together with the first steam producing means into the heat exchange means in parallel. And a large amount of superheated steam can be obtained.
【0016】又前記チャー燃焼手段の高温域側に熱交換
手段を配設する事は、800〜1300℃前後と無用に
高くなり、そのまま出口ラインに流すと通常の金属ライ
ンでは温度的に持たないが、これを800〜950℃に
落とすことにより通常の耐熱金属ラインの利用が可能と
なる。又前記のように800〜950℃に落としても第
2の蒸気製造手段における蒸気温度を500〜600℃
に維持する上で何の支障もない。The provision of the heat exchange means on the high temperature side of the char combustion means is unnecessarily high, around 800 to 1300 ° C., and if it flows directly to the outlet line, it does not have the temperature in the ordinary metal line. However, by dropping the temperature to 800 to 950 ° C., a normal heat-resistant metal line can be used. Further, even if the temperature is lowered to 800 to 950 ° C. as described above, the steam temperature in the second steam producing means is set to 500 to 600 ° C.
There is no hindrance in maintaining it.
【0017】請求項4記載の発明は、上記燃焼手段の出
口側に接続され該燃焼手段より燃焼ガスと上記流動媒体
とを分離する分離手段を含み、前記第1若しくは第2の
蒸気製造手段で加熱された蒸気若しくは前記いずれかの
製造手段に導入される温水若しくは蒸気の一部を、適宜
前記分離手段の流動媒体出口側に導入し、該流動媒体と
の熱接触により加熱することを特徴とするものである。
かかる発明によれば、前記チャー燃焼手段の出口側に燃
焼ガスと前記流動媒体とを分離する分離手段を設けた為
に、言換えれば800〜950℃前後の高温の流動媒体
を熱分解手段とチャー燃焼手段夫々に戻入することによ
り、目的とする温度の流動床形成や温度管理が容易にな
る。According to a fourth aspect of the present invention, there is provided a separator connected to an outlet side of the combustion means for separating the combustion gas and the fluid medium from the combustion means. The heated steam or a part of the hot water or steam introduced into any one of the production means is appropriately introduced to the fluid medium outlet side of the separation means, and heated by thermal contact with the fluid medium. Is what you do.
According to this invention, since the separation means for separating the combustion gas and the fluid medium is provided on the outlet side of the char combustion means, in other words, the high temperature fluid medium of about 800 to 950 ° C. is used as the thermal decomposition means. By returning each of the char combustion means, formation of a fluidized bed at a desired temperature and temperature control become easy.
【0018】そして本発明においては、前記分離手段の
流動媒体出口側に熱交換手段を配置し、前記第1若しく
は第2の蒸気製造手段で加熱された蒸気若しくは前記い
ずれかの製造手段に導入される温水若しくは蒸気の一部
を、適宜該流動媒体との熱接触により加熱することによ
り、請求項3記載の発明と同様な作用を営むことが出来
る。この場合、前記チャー燃焼手段の高温域側に熱交換
手段(以下第1熱交換手段という)と前記分離手段の流
動媒体出口側にも熱交換手段(以下第2熱交換手段とい
う)を配置してもよい。又、第1の熱交換手段−第1の
蒸気製造手段−第2の蒸気製造手段−第2熱交換手段と
配置することにより、実質的に直列の4段階昇温を図る
ことが出来、極めて高い十分加熱された過熱蒸気を得る
ことが出来る。In the present invention, a heat exchange means is arranged on the fluid medium outlet side of the separation means, and is introduced into the steam heated by the first or second steam production means or any one of the production means. By heating a portion of the hot water or steam by appropriate thermal contact with the fluid medium, the same effect as the invention of claim 3 can be achieved. In this case, heat exchange means (hereinafter referred to as first heat exchange means) is disposed on the high temperature side of the char combustion means, and heat exchange means (hereinafter referred to as second heat exchange means) is disposed also on the fluid medium outlet side of the separation means. You may. Further, by arranging the first heat exchanging means, the first steam producing means, the second steam producing means, and the second heat exchanging means, it is possible to substantially increase the temperature in four stages in series. High and sufficiently heated superheated steam can be obtained.
【0019】又、後記実施例に示すように(第1の熱交
換手段と第1の蒸気製造手段を並列に)−第2の蒸気製
造手段−第2熱交換手段とを直列に配置することによ
り、実質的に並列/直列の3段階昇温を図ることが出
来、多量且つ十分加熱された過熱蒸気を得ることが出来
る。又第1の熱交換手段と第2の熱交換手段をいずれか
を選択的に用いても良い。又、前記熱交換手段にはスー
パヒータ若しくはボイラを用いるのがよい。Further, as shown in the embodiment described later, the first heat exchange means and the first steam production means are arranged in parallel, the second steam production means and the second heat exchange means are arranged in series. Accordingly, the temperature can be raised substantially in three stages of parallel / series, and a large amount and sufficiently heated superheated steam can be obtained. Either the first heat exchange means or the second heat exchange means may be selectively used. It is preferable to use a superheater or a boiler as the heat exchange means.
【0020】[0020]
【発明の実施の形態】以下図面を参照して本発明の実施
形態を説明する。但し、この実施形態に記載されている
構成部品の寸法、材質、形状、その相対的配置等は特に
特定的な記載がないかぎりは、この発明の範囲をそれに
限定する趣旨ではなく、単なる説明例にすぎない。図1
は本発明の実施例に係る廃棄物の焼却熱を利用した過熱
蒸気製造装置を示し、図中、1は流動床からなる熱分解
炉で、多孔板等の分散板3上に流動砂等の流動媒体2が
収納されており、廃棄物供給ライン4及び砂循環ライン
5より流動砂と都市ごみ等の廃棄物が投入され、空気ま
たは燃焼排ガス入口ライン6より供給された空気または
燃焼排ガスにより温度300℃以上の流動床空間を生成
し、廃棄物の熱分解反応を行なわせ、その反応により発
生した熱分解ガスは熱分解ガス出口ライン7より、又未
分解残渣および流動砂から成るチャー混合物は逆流防止
手段50を介してチャー混合物取り出しライン9より、
不燃物は不燃物取り出しライン8より、夫々互いに分離
して取り出す。尚前記空気または燃焼排ガス入口ライン
6より熱分解炉1に供給される空気または燃焼排ガス
は、300〜700℃の範囲で熱分解を効率的に行うた
めに、酸素の少ない(5%程度)且つ温度が100〜3
00℃の温度を維持している燃焼排ガス、具体的には第
1のボイラ24の出口ライン25より取り出された燃焼
排ガスを用いるのが良い。Embodiments of the present invention will be described below with reference to the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the components described in this embodiment are not intended to limit the scope of the present invention unless otherwise specified, and are merely illustrative examples. It's just FIG.
1 shows an apparatus for producing superheated steam using the heat of incineration of wastes according to an embodiment of the present invention. In the drawing, reference numeral 1 denotes a pyrolysis furnace comprising a fluidized bed, wherein fluidized sand or the like is dispersed on a dispersion plate 3 such as a perforated plate. Fluid medium and waste such as municipal solid waste are supplied from a waste supply line 4 and a sand circulation line 5, and the temperature is controlled by air or flue gas supplied from air or flue gas inlet line 6. A fluidized bed space of 300 ° C. or higher is generated to cause a pyrolysis reaction of the waste, and the pyrolysis gas generated by the reaction is supplied to a pyrolysis gas outlet line 7. From the char mixture removal line 9 via the backflow prevention means 50,
The incombustibles are separated from each other and taken out from the incombustibles take-out line 8. The air or the flue gas supplied to the pyrolysis furnace 1 from the air or flue gas inlet line 6 contains a small amount of oxygen (about 5%) in order to efficiently perform pyrolysis in the range of 300 to 700 ° C. The temperature is 100-3
It is preferable to use the combustion exhaust gas maintaining the temperature of 00 ° C., specifically, the combustion exhaust gas taken out from the outlet line 25 of the first boiler 24.
【0021】熱分解ガス出口ライン7より取り出された
熱分解ガスは、灰溶融炉31及び熱分解ガス燃焼炉34
を経て第1のボイラ24に導入される。即ち、前記灰溶
融炉31は、旋回流により砂混合熱分解ガス灰を旋回分
離させながら、該溶融炉31内に空気若しくは酸素富化
空気を前記熱分解ガスと共に、導入して該熱分解ガス燃
焼熱により1300℃として灰分を溶融して、該溶融し
た灰分を溶融灰出口ライン32を介して水貯溜部32A
に落下させ、数mm程度の水冷スラッグを生成し、該ス
ラッグを建築用骨材として利用する。The pyrolysis gas extracted from the pyrolysis gas outlet line 7 is supplied to the ash melting furnace 31 and the pyrolysis gas combustion furnace 34.
And is introduced into the first boiler 24. That is, the ash melting furnace 31 introduces air or oxygen-enriched air together with the pyrolysis gas into the melting furnace 31 while swirling and separating the sand-mixed pyrolysis gas ash by a swirling flow. The ash is melted at 1300 ° C. by the heat of combustion, and the melted ash is melted through a molten ash outlet line 32 into a water storage section 32A.
To produce a water-cooled slag of about several mm, which is used as building aggregate.
【0022】又、前記灰溶融炉31には後記するガス出
口ライン17に設けた高温フィルタ40より分離した灰
分がダストライン29及びサイクロンの砂出口ライン1
8に設けた灰分離器41(スクリーン)より分離した灰
分がダストライン29aを介して夫々導入され、これら
も溶融分離される。そして、灰分を除去した熱分解ガス
は出口ライン33を介して熱分解ガス燃焼炉に導入し、
空気供給ラインより供給された空気により完全燃焼を行
い、その出口ライン35/23を介して第1ボイラ24
に導入する。In the ash melting furnace 31, ash separated from a high-temperature filter 40 provided in a gas outlet line 17 to be described later is mixed with a dust line 29 and a sand outlet line 1 of a cyclone.
The ash separated from the ash separator 41 (screen) provided at 8 is respectively introduced through the dust line 29a, and these are also melted and separated. Then, the pyrolysis gas from which the ash has been removed is introduced into the pyrolysis gas combustion furnace through the outlet line 33,
Complete combustion is performed by the air supplied from the air supply line, and the first boiler 24 is
To be introduced.
【0023】又、前記熱分解炉1により得られた熱分解
ガスの一部を灰溶融炉31の上流側で、分岐ライン7a
を介して熱分解炉1の分散板3下方の入口側に供給する
ものであるために、言換えれば350℃〜400℃の高
温の可燃性ガスを熱分解炉1に循環供給する事が出来る
ために、熱分解ガスが空気又は燃焼排ガス中のN2、C
O2,H2O等の不活性ガスでの希釈を最小限に抑えて、
単位容積当りの発熱量を高くし、灰溶融に必要な燃焼温
度1300℃に容易にすることが可能となるとともに、
温度変動を抑制して安定した熱分解が可能となる。A part of the pyrolysis gas obtained by the pyrolysis furnace 1 is supplied to a branch line 7a on the upstream side of the ash melting furnace 31.
In other words, high-temperature flammable gas of 350 ° C. to 400 ° C. can be circulated and supplied to the thermal decomposition furnace 1 because the gas is supplied to the inlet side below the dispersion plate 3 of the thermal decomposition furnace 1 through Therefore, the pyrolysis gas is N 2 , C in air or flue gas.
Minimizing dilution with an inert gas such as O 2 , H 2 O,
The calorific value per unit volume can be increased, and the combustion temperature required for ash melting can be easily increased to 1300 ° C.
Stable thermal decomposition becomes possible by suppressing temperature fluctuation.
【0024】図2は前記チャー混合物取り出しライン9
上に配設された逆流防止手段50の一実施態様を示し、
前記熱分解炉1側へのチャー圧力をチャー燃焼炉10側
への圧力より大に設定することにより逆流防止機能をも
たせたシールポット59を形成する。即ち、熱分解炉1
の隔壁55よりオーバーフローしたチャー混合物は逆流
防止手段50に流入し、そして逆流防止手段50はチャ
ー混合物取り出しライン9を隔壁52を介して上下2つ
に折返し、熱分解炉1側と連通する第一の流動層通路5
0aと、チャー燃焼炉10側と連通する第二の流動層通
路50bを隣接して形成すると共に、折返した底部にシ
ールポット59(前記2つの通路の折返し部であって、
共通する流動砂収納部を有するもの)を形成すると共
に、該シールポット59の底部に分散板53を配すると
共に、該分散板下部の空気導入空間を仕切り板51にて
左右2つの導入空間54a、54bに仕切り、第一及び
第二の流動層通路50a、50bに夫々独立した流速の
空気若しくは排ガスがライン58より導入可能に構成し
ている。FIG. 2 shows the char mixture removal line 9.
Shows one embodiment of the backflow prevention means 50 disposed above,
By setting the char pressure to the pyrolysis furnace 1 side higher than the pressure to the char combustion furnace 10 side, a seal pot 59 having a backflow prevention function is formed. That is, the pyrolysis furnace 1
The char mixture which has overflowed from the partition wall 55 flows into the backflow prevention means 50, and the backflow prevention means 50 folds the char mixture take-out line 9 up and down through the partition wall 52 and communicates with the pyrolysis furnace 1 side. Fluidized bed passage 5
0a and a second fluidized bed passage 50b communicating with the char combustion furnace 10 side are formed adjacent to each other, and a seal pot 59 (a folded portion of the two passages,
And a dispersing plate 53 is disposed at the bottom of the seal pot 59, and the air introducing space below the dispersing plate is divided into two left and right introducing spaces 54a by the partition plate 51. , 54b, so that air or exhaust gas having independent flow rates can be introduced into the first and second fluidized bed passages 50a, 50b through a line 58.
【0025】そして前記第一及び第二の流動層通路50
a、50bの通路高さは、前記熱分解炉1側の圧力をP
2、チャー燃焼炉10側の圧力をP1とした場合に、 ΔH・ρ>P1−P2 ΔH:(第一流動層通路50a高さH1−第二の流動層
通路50b高さH2) ρ:流動層密度(比重) の式を満足になるように構成すれば良く、そして更に仕
切り板51にて左右2つの導入空間54a、bに仕切っ
た導入空間54a、bの流速を異ならせ、チャー燃焼炉
10側の第二の流動層通路50a、bの流速を早く、熱
分解炉1側の第一流動層通路50aの流速を遅くするこ
とにより、前記逆流防止効果が一層高まる。The first and second fluidized bed passages 50
The passage heights of a and 50b are determined by setting the pressure on the pyrolysis furnace 1 side to P
2, the pressure of the char combustion furnace 10 side when the P 1, ΔH · ρ> P 1 -P 2 ΔH :( first fluidized bed passages 50a height H 1 - second fluidized bed passage 50b height H 2 ) ρ: fluidized bed density (specific gravity) should be satisfied, and if the flow rates of the introduction spaces 54a, b divided into two left and right introduction spaces 54a, b by the partition plate 51 are different. By increasing the flow velocity of the second fluidized bed passages 50a and 50b on the side of the char combustion furnace 10 and decreasing the flow velocity of the first fluidized bed passage 50a on the pyrolysis furnace 1 side, the backflow prevention effect is further enhanced.
【0026】又、図3に示すように、機械的搬送手段5
0Bで逆流防止手段50を構成しても良い。例えば、チ
ャー混合物取り出しライン9の途中位置、若しくはチャ
ー燃焼路のチャー混合物導入口側にスクリューフィーダ
61を設けると共に、該スクリューフィーダの入口側よ
り出口側に向け、上向きに傾斜させ、重力差を持たせて
配置して構成する。これにより機械的搬送手段50B内
が流動砂により圧密化され、流動砂でのガスシール効果
が増大する。Further, as shown in FIG.
0B may constitute the backflow prevention means 50. For example, a screw feeder 61 is provided in the middle of the char mixture take-out line 9 or at the char mixture inlet side of the char combustion path, and the screw feeder is inclined upward from the inlet side to the outlet side to have a gravity difference. It is arranged and configured. As a result, the inside of the mechanical transfer means 50B is compacted by the fluidized sand, and the gas sealing effect with the fluidized sand is increased.
【0027】10は塔式の流動床炉からなるチャー燃焼
炉で、底部に配した分散板11上にチャー混合物取り出
しライン9より逆流防止手段50を介して供給されたチ
ャー混合物、及び砂循環ライン19より循環された流動
砂が収納される。Reference numeral 10 denotes a char combustion furnace consisting of a tower type fluidized bed furnace. The char mixture supplied from a char mixture take-out line 9 through a backflow prevention means 50 onto a dispersion plate 11 disposed at the bottom, and a sand circulation line. The fluid sand circulated from 19 is stored.
【0028】そして前記分散板11下方の空気供給ライ
ン12より更にチャー燃焼炉10中域の空気供給ライン
13より夫々空気が供給されて未分解残渣の燃焼を行
い、約1500℃前後の燃焼ガスを生成すると共に、ラ
イン26’よりそのチャー燃焼炉10中の上方域に水冷
壁ボイラ又はスーパヒートを配設し、950〜1300
℃前後と無用に高くなった燃焼ガスを800〜950℃
に落とすと共に、第1ボイラに供給するボイラ水の一部
を加熱する。該ボイラ水の加熱温度は300℃前後にな
る。尚前記のように燃焼ガス温度を800〜950℃に
落としても第2のボイラ20における蒸気温度を500
〜600℃に維持する上で何の支障もない。Air is further supplied from the air supply line 12 below the dispersion plate 11 to the air supply line 13 in the middle region of the char combustion furnace 10 to burn undecomposed residues, and the combustion gas at about 1500 ° C. A water-cooled wall boiler or a superheat is disposed in the upper region of the char combustion furnace 10 through a line 26 ', and 950 to 1300
Combustion gas that has risen unnecessarily to around 800 ° C
And a part of the boiler water supplied to the first boiler is heated. The heating temperature of the boiler water is about 300 ° C. As described above, even if the combustion gas temperature is lowered to 800 to 950 ° C., the steam temperature in the second
There is no problem in maintaining the temperature at -600 ° C.
【0029】そして前記燃焼炉で燃焼炉で燃焼されない
小型の不燃物は不燃物取り出しライン14より取り出さ
れる。そして前記のように高温化された砂混合の燃焼ガ
スは、砂/燃焼ガス出口ライン15より気・固分離装置
例えばサイクロン16に導入され、ここで流動砂と燃焼
ガスを分離し、燃焼ガスはガス出口ライン17より第2
ボイラ20に導入される。Small incombustibles that are not burned in the combustion furnace in the combustion furnace are taken out from the incombustibles take-out line 14. Then, the combustion gas of the sand mixture, which has been heated as described above, is introduced into a gas / solid separation device, for example, a cyclone 16 through a sand / combustion gas outlet line 15, where the combustion gas is separated from the flowing sand. Second from gas outlet line 17
It is introduced into the boiler 20.
【0030】砂出口ライン18より取り出された流動砂
は、灰分分離器41(スクリーン)で灰分を分離した
後、出口ライン18Aより、整流板及び回転弁からなる
分配調整弁を介して砂循環ライン19より燃焼炉10
と、砂循環ライン5より熱分解炉1に夫々供給される。The fluidized sand taken out from the sand outlet line 18 is separated into ash by an ash separator 41 (screen), and then is discharged from the outlet line 18A via a distribution regulating valve comprising a straightening plate and a rotary valve to a sand circulation line. From 19, combustion furnace 10
Is supplied to the pyrolysis furnace 1 from the sand circulation line 5.
【0031】又灰分分離器41(スクリーン)で分離さ
れた灰分は、ダストライン29a/29を介して灰溶融
炉31に導入される。又前記燃焼炉10と第2ボイラ2
0間の燃焼ガスライン17には、スーパーヒータからな
る熱交換器37と高温フィルタ40が直列に配設され、
例えば900℃前後に加熱された燃焼ガスが熱交換器3
7で、第2ボイラ20で加熱後の過熱蒸気と熱交換さ
れ、加熱温度を600℃前後に落として高温フィルタ4
0に導入される。そして該高温フィルタ40で燃焼ガス
中の灰分の分離を行った後、ライン141を介して第2
ボイラ20に導入される。The ash separated by the ash separator 41 (screen) is introduced into the ash melting furnace 31 through the dust lines 29a / 29. Further, the combustion furnace 10 and the second boiler 2
A heat exchanger 37 composed of a super heater and a high temperature filter 40 are arranged in series in the combustion gas line 17 between 0,
For example, the combustion gas heated to about 900 ° C.
7, the heat is exchanged with the superheated steam after heating in the second boiler 20, and the heating temperature is lowered to about 600 ° C.
0 is introduced. After the ash in the combustion gas is separated by the high-temperature filter 40, the second
It is introduced into the boiler 20.
【0032】そして前記高温フィルタ40で分離された
灰分は、ダストライン29を介して灰溶融炉31に導入
される。20は第2ボイラ及び24は第1ボイラで、第
1ボイラ24では熱分解ガス出口ライン7より取り出さ
れた熱分解ガスが、空気入口ライン21より取込んだ空
気により再燃焼されて第2ボイラガス出口より排出され
た燃焼排ガスと共に、第1のボイラ24に導入され、ボ
イラ水入口26より取込んだボイラ水を300℃前後に
加熱し、第1ボイラ蒸気出口27より第2ボイラ20に
蒸気を供給する。The ash separated by the high temperature filter 40 is introduced into an ash melting furnace 31 through a dust line 29. Reference numeral 20 denotes a second boiler and reference numeral 24 denotes a first boiler. In the first boiler 24, the pyrolysis gas taken out from the pyrolysis gas outlet line 7 is reburned by the air taken in from the air inlet line 21 to produce a second boiler gas. The boiler water introduced into the first boiler 24 together with the combustion exhaust gas discharged from the outlet and taken in from the boiler water inlet 26 is heated to about 300 ° C., and steam is sent from the first boiler steam outlet 27 to the second boiler 20. Supply.
【0033】第2ボイラ20では前記第1ボイラ24の
第1ボイラ蒸気出口ライン27より取り出した蒸気及び
水冷壁ボイラ36により加熱され分岐蒸気ライン27’
を介してとりだされた蒸気を導入して、前記燃焼ガス出
口ライン17を介して供給された燃焼ガスで加熱し、5
00〜600℃前後の過熱蒸気を製造し、第2ボイラ蒸
気出口28より取り出す。In the second boiler 20, steam extracted from the first boiler steam outlet line 27 of the first boiler 24 and heated by the water-cooled wall boiler 36 are branched steam lines 27 '.
Through the combustion gas supplied through the combustion gas outlet line 17, and
A superheated steam of about 00 to 600 ° C. is produced and taken out from the second boiler steam outlet 28.
【0034】次に前記実施例の作用について詳述する。
熱分解炉1に供給される都市ごみ等の廃棄物中には塩ビ
プラスチック等の含塩素有機化合物が混入しており、可
燃分中にC1として約0.2〜0.5%含有されてい
る。そして、廃棄物供給ライン4から都市ごみ、砂循環
ライン5から高温の循環砂を、それぞれ熱分解炉1に供
給し、下部の空気または燃焼排ガス入口ライン6から空
気または燃焼排ガスを供給して流動砂2を流動させた流
動床内で、温度300〜700℃で処理することによ
り、チャー混合物取り出しライン9からは実質的に塩素
を含有しない未分解残渣が得られる。すなわち、廃棄物
中に含まれていた塩素は、実質的に全て熱分解ガスに含
まれて、熱分解ガス出口ライン7に排出されることにな
る。なお、熱分解炉1内の熱分解反応で分離された大型
の不燃物は、不燃物取り出しライン8から炉外に取り出
される。Next, the operation of the above embodiment will be described in detail.
Chlorine-containing organic compounds such as PVC plastics are mixed in the waste such as municipal waste supplied to the pyrolysis furnace 1, and the combustibles contain about 0.2 to 0.5% as C1. . Then, municipal solid waste from the waste supply line 4 and high-temperature circulating sand from the sand circulation line 5 are supplied to the pyrolysis furnace 1, respectively, and air or combustion exhaust gas is supplied from the lower air or combustion exhaust gas inlet line 6 to flow. By treating at a temperature of 300 to 700 ° C. in the fluidized bed in which the sand 2 is fluidized, an undecomposed residue substantially free of chlorine is obtained from the char mixture removal line 9. That is, substantially all of the chlorine contained in the waste is contained in the pyrolysis gas and discharged to the pyrolysis gas outlet line 7. The large-sized incombustibles separated by the thermal decomposition reaction in the thermal decomposition furnace 1 are taken out of the furnace through an incombustibles take-out line 8.
【0035】熱分解炉1の熱分解出口ライン7から取り
出された上記熱分解ガスには、低カロリーガス、油分、
タールおよびHC1が含まれているが、これを灰溶融炉
31及び熱分解燃焼炉で完全燃焼させた後、第2ボイラ
ガス出口ライン22よりの燃焼排ガスとともに第1ボイ
ラガス入口23から第1ボイラ24に供給する。The pyrolysis gas extracted from the pyrolysis outlet line 7 of the pyrolysis furnace 1 includes low calorie gas, oil,
Tar and HC1, which are completely burned in the ash melting furnace 31 and the pyrolysis combustion furnace, and then together with the combustion exhaust gas from the second boiler gas outlet line 22 from the first boiler gas inlet 23 to the first boiler 24. Supply.
【0036】従って、第1ボイラ24に導入される熱分
解ガス中に灰分等が混入されることなく長期に亙って安
定して蒸気製造が可能になるとともに、又第1ボイラ2
4に導入される熱分解ガス温度を略850〜900℃
(最大950℃前後)程度に高く設定できるために、該
ボイラ24で製造される300℃前後の蒸気を多量に製
造できる。Accordingly, it is possible to stably produce steam over a long period of time without incorporation of ash or the like into the pyrolysis gas introduced into the first boiler 24.
The temperature of the pyrolysis gas introduced into 4 is approximately 850-900 ° C
(Up to around 950 ° C.), a large amount of steam at around 300 ° C. produced by the boiler 24 can be produced.
【0037】第1ボイラガス入口23のガスにはHC1
が約500〜1000ppm含まれているので、ボイラ水
の流量を調整して第1ボイラ24のチューブ表面温度は
従来並みの約350℃以下として、高温腐食を抑制す
る。このため、第1ボイラ24では高温の過熱蒸気は得
られないが、約300℃までは加熱できるので、これを
更に第2ボイラ20で加熱すれば、約500〜600℃
の高温の過熱蒸気を得ることができる。The gas at the first boiler gas inlet 23 is HC1
Is contained at about 500 to 1000 ppm, so that the flow rate of the boiler water is adjusted to keep the tube surface temperature of the first boiler 24 at about 350 ° C. or less, which is the same as the conventional one, thereby suppressing high-temperature corrosion. For this reason, high-temperature superheated steam cannot be obtained in the first boiler 24, but can be heated up to about 300 ° C., and if this is further heated in the second boiler 20, about 500 to 600 ° C.
High temperature superheated steam can be obtained.
【0038】熱分解炉1でチャー混合物取り出しライン
9から取り出されたチャー混合物は流動砂と未分解残渣
から成り、実質的に塩素を含有しないチャー混合物を、
逆流防止手段50を介して燃焼炉10では燃焼炉10の
下部に供給し、空気供給ライン12から分散板11を介
して供給される空気によって燃焼させる。The char mixture taken out of the char mixture take-out line 9 in the pyrolysis furnace 1 is composed of fluidized sand and uncracked residue, and is substantially free of chlorine.
In the combustion furnace 10, the air is supplied to the lower part of the combustion furnace 10 via the backflow prevention means 50, and is burned by air supplied from the air supply line 12 through the distribution plate 11.
【0039】尚、チャー燃焼炉10は、高温の燃焼を可
能にする為に、流動床の背高を高くする必要があり、こ
の為該チャー燃焼炉10内の圧力が高くなり、この為流
動砂等が燃焼炉10側より熱分解炉1側へ逆流の恐れが
あるが、本発明においては前記熱分解炉1とチャー燃焼
炉10間を接続するチャー混合物取り出しライン9中
に、チャー逆流防止手段50を配し、前記チャー燃焼炉
10よりの逆流を防止し、チャー燃焼と熱分解炉1にお
ける熱分解を効率良く行っている。In the char combustion furnace 10, it is necessary to increase the height of the fluidized bed in order to enable high-temperature combustion. Therefore, the pressure in the char combustion furnace 10 increases, and the There is a possibility that sand or the like may flow backward from the combustion furnace 10 to the pyrolysis furnace 1. In the present invention, however, the backflow prevention of the char mixture is performed in the char mixture take-out line 9 connecting the pyrolysis furnace 1 and the char combustion furnace 10. Means 50 are disposed to prevent backflow from the char combustion furnace 10 and to efficiently perform char combustion and pyrolysis in the pyrolysis furnace 1.
【0040】この場合、空気供給ライン12から供給す
る空気量を調整して、流動砂を上方に吹き飛ばしながら
未分解残渣を燃焼させる。完全燃焼のために空気供給ラ
イン13から更に空気を供給することもある。燃焼炉1
0の温度は燃焼発熱反応によって上昇する。この温度値
は、チャー混合物取り出しライン9から供給される未分
解残渣の発熱量と空気供給ライン12、13の空気およ
び砂循環ライン19の砂の量と温度によって決まるが、
950〜1300℃前後の高温になる場合がある。そこ
で水冷壁ボイラ36により分岐管26より導入されたボ
イラ水と熱交換することにより砂混合燃焼ガス800〜
950℃にすることは容易である。ガラスや缶類等の溶
融により小型化された不燃物は不燃物取り出しライン1
4から抜き出す。In this case, the amount of air supplied from the air supply line 12 is adjusted, and the undecomposed residue is burned while blowing the fluidized sand upward. Further air may be supplied from the air supply line 13 for complete combustion. Combustion furnace 1
The temperature of 0 rises due to the exothermic combustion reaction. This temperature value is determined by the calorific value of the undecomposed residue supplied from the char mixture removal line 9, the amount of air in the air supply lines 12, 13 and the amount and temperature of the sand in the sand circulation line 19,
The temperature may be as high as about 950 to 1300 ° C. Then, heat exchange with the boiler water introduced from the branch pipe 26 is performed by the water-cooled wall boiler 36, so that the sand mixed combustion gas 800 to
It is easy to reach 950 ° C. Incombustibles that have been miniaturized by melting glass and cans, etc.
Pull out from 4.
【0041】燃焼炉10で生成し800〜950℃の高
温でかつ塩素を実質的に含有しない燃焼ガスは、砂とと
もに砂・燃焼ガス出口ライン15を経てサイクロン16
に導入され、流動砂は砂出口ライン18から、排ガスは
ガス出口ライン17からそれぞれ分離して取り出され
る。そして砂出口ライン18から取り出された800〜
950℃の高温の流動砂は灰分離器41により灰分が分
離された後、その一部は砂循環ライン5を経て熱分解炉
1へ戻され、熱分解炉1内部の温度を所定温度に保持す
るために用いられる。また残りは砂循環ライン19を経
て燃焼炉10に戻される。The combustion gas generated in the combustion furnace 10 at a high temperature of 800 to 950 ° C. and substantially containing no chlorine passes through the sand / combustion gas outlet line 15 together with the sand and the cyclone 16.
The fluidized sand is taken out from the sand outlet line 18 and the exhaust gas is taken out separately from the gas outlet line 17. And 800-taken out from the sand exit line 18
After the ash content of the 950 ° C. high-temperature fluidized sand is separated by the ash separator 41, a part of the ash is returned to the pyrolysis furnace 1 through the sand circulation line 5, and the temperature inside the pyrolysis furnace 1 is maintained at a predetermined temperature. Used to The remainder is returned to the combustion furnace 10 via the sand circulation line 19.
【0042】従って本実施例によれば前記サイクロン1
6の砂出口ライン18側に流動砂と灰分の分離を行う灰
分分離器41とを設けた為に、熱分解炉1とチャー燃焼
炉10夫々に戻入する流動媒体に灰分等が混入されるこ
となく、安定した熱分解とチャー燃焼が長期に亙って達
成出来る。一方前記灰分は前記した灰分溶融分離器31
に導入する事により、前記溶融灰を利用して骨材等の製
造が可能となるとともに、前記灰分は高温であるために
その熱を利用して分離された熱分解ガスの再加熱を行う
ことも可能である。Therefore, according to the present embodiment, the cyclone 1
6. Since the ash separator 41 for separating the ash from the fluidized sand is provided on the side of the sand outlet line 18 of 6, the ash and the like are mixed in the fluid medium returning to the pyrolysis furnace 1 and the char combustion furnace 10, respectively. And stable pyrolysis and char combustion can be achieved over a long period of time. On the other hand, the ash is separated from the ash melt separator 31 described above.
By introducing the molten ash, it becomes possible to produce aggregates and the like by using the molten ash, and since the ash is high in temperature, the separated pyrolysis gas is reheated by utilizing its heat. Is also possible.
【0043】一方、上記サイクロン16のガス出口ライ
ン17から取り出された800〜950℃の高温燃焼ガ
スは、熱交換器37で予冷した後、高温フィルタ40に
導入して、該フィルタ40で燃焼ガス中の灰分の分離を
行う為に、第2のボイラ20に導入される燃焼ガス中に
灰分等が混入されることなく長期に亙って安定して蒸気
製造が可能になるとともに、又前記燃焼ガス中の未燃焼
塩素化合物の燃焼を行う為に、いわゆるダイオキシンの
除去を確実に行う事ができる。On the other hand, the 800-950 ° C. high-temperature combustion gas taken out from the gas outlet line 17 of the cyclone 16 is pre-cooled by the heat exchanger 37, introduced into the high-temperature filter 40, and In order to separate ash therein, it is possible to stably produce steam over a long period of time without mixing ash or the like into the combustion gas introduced into the second boiler 20, and to perform the above combustion. Since the unburned chlorine compounds in the gas are burned, so-called dioxin can be reliably removed.
【0044】そして、前記高温フィルタ40の入口側に
熱交換器37を配し、前記第2ボイラ20の加熱された
過熱蒸気を熱交換器37に導入して前記高温フィルタ4
0に導入される燃焼ガスの予冷を行う事により、高温フ
ィルタ40に加わる負荷を大幅に低減できる。又前記熱
交換器37に第2ボイラ20で加熱後の過熱蒸気を導入
することにより、一層加熱された過熱蒸気を得ることも
出来、特に第2ボイラ20には第1ボイラ24と水冷壁
ボイラ36の蒸気を導入するために、過熱容量不足にな
ることもあるが、本実施例では又前記熱交換器37に第
2ボイラ20で加熱後の過熱蒸気を導入する為に熱容量
不足を解消して十分加熱された過熱蒸気を得ることが出
来る。Then, a heat exchanger 37 is arranged on the inlet side of the high-temperature filter 40, and the superheated steam heated from the second boiler 20 is introduced into the heat exchanger 37, and
By pre-cooling the combustion gas introduced to zero, the load applied to the high temperature filter 40 can be significantly reduced. Further, by introducing the superheated steam heated by the second boiler 20 into the heat exchanger 37, it is possible to obtain a superheated steam which is further heated. In particular, the second boiler 20 includes the first boiler 24 and the water-cooled wall boiler. Although the superheat capacity may be insufficient due to the introduction of the steam of 36, the present embodiment also solves the heat capacity shortage by introducing the superheated steam heated by the second boiler 20 into the heat exchanger 37. Thus, it is possible to obtain a sufficiently heated superheated steam.
【0045】更に高温フィルタ40と灰分分離器41に
より分離された灰分は灰分溶融分離炉31に導入するこ
とにより、前記溶融灰を利用して骨材等の製造が可能と
なる。又前記灰分はいずれも高温であるためにその熱を
利用して分離された熱分解ガスの再加熱を行うことも可
能である。Further, the ash separated by the high temperature filter 40 and the ash separator 41 is introduced into the ash melting / separating furnace 31, so that the molten ash can be used to produce aggregates and the like. Since the ash content is high in temperature, it is possible to reheat the separated pyrolysis gas by using the heat.
【0046】第2ボイラ20で第2ボイラ20に導入さ
れ、第1ボイラ24で製造された蒸気を更に加熱して過
熱蒸気とするために用いられる。ガス出口ライン17を
経て来た排ガスは実質的に塩素を含有していないので、
第2ボイラ20のボイラチューブ表面温度を350℃以
上としても高温腐食は大幅に軽減される。したがってチ
ューブ内の蒸気温度を約500〜600℃、100Kg
f/cm2とすることができ、第2ボイラ蒸気出口28
からは安定して高温の過熱蒸気が得られる。The steam introduced into the second boiler 20 by the second boiler 20 is used to further heat the steam produced by the first boiler 24 to become superheated steam. Since the exhaust gas coming through the gas outlet line 17 does not substantially contain chlorine,
Even when the surface temperature of the boiler tube of the second boiler 20 is set to 350 ° C. or more, high-temperature corrosion is greatly reduced. Therefore, the steam temperature in the tube is about 500-600 ° C, 100Kg
f / cm 2 and the second boiler steam outlet 28
, Stable high-temperature superheated steam is obtained.
【0047】前記熱分解炉1で熱分解炉1の温度を所定
温度300℃以上に維持するには、空気または燃焼排ガ
ス入口ライン6から供給される流動気体の酸素量を調
節、言換えれば第1ボイラ24よりの排ガスを多く供給
するとともに、サイクロン16よりの砂出口ライン18
から取り出される高温約800〜950℃の砂の一部を
砂循環ライン5から供給して熱源とすることが好まし
い。そのためには、燃焼炉10の燃焼炉10ではガスの
空搭速度(炉内のガス流量/炉の断面積)を3〜6m/s
として、チャー混合物取り出しライン9から供給された
砂を吹き飛ばしながら未分解残渣を燃焼し、砂はサイク
ロン16で燃焼ガスと分離して熱分解炉1と燃焼炉10
に循環供給する高速循環型流動床が適している。In order to maintain the temperature of the pyrolysis furnace 1 at a predetermined temperature of 300 ° C. or higher in the pyrolysis furnace 1, the amount of oxygen in the air or the flowing gas supplied from the flue gas inlet line 6 is adjusted, in other words, A large amount of exhaust gas from one boiler 24 is supplied and a sand outlet line 18 from the cyclone 16
It is preferable that a part of the sand having a high temperature of about 800 to 950 ° C. taken out from the sand is supplied from the sand circulation line 5 to be used as a heat source. For this purpose, in the combustion furnace 10 of the combustion furnace 10, the empty space velocity of the gas (gas flow rate in the furnace / cross-sectional area of the furnace) is 3 to 6 m / s.
As a result, the undecomposed residue is burned while blowing off the sand supplied from the char mixture take-out line 9, and the sand is separated from the combustion gas by the cyclone 16 and the pyrolysis furnace 1 and the combustion furnace 10 are separated.
A high-speed circulating fluidized bed is suitable for circulating feed.
【0048】そして本発明をより効率的に実施するに
は、チャー混合物取り出しライン9から取り出される実
質的に塩素を含有しないチャー混合物の量をできるだけ
多くし好ましくは原料中可燃物の40%以上、燃焼炉1
0で発生する熱量を多くして、第2ボイラ20における
回収熱量を多くすることが望ましい。この結果発電効率
が30%以上が可能となる。そこで本実施例において
は、ごみ中の塩素を実質的に分離除去しチャーの回収率
を40%以上にできる条件として、熱分解炉1の温度を
300〜700℃、好ましくは350〜450℃とする
ことが望ましい。In order to carry out the present invention more efficiently, the amount of the substantially chlorine-free char mixture taken out from the char mixture take-out line 9 is made as large as possible, preferably 40% or more of the combustible material in the raw material, Combustion furnace 1
It is desirable to increase the amount of heat generated at 0 and increase the amount of heat recovered in the second boiler 20. As a result, the power generation efficiency can be 30% or more. Therefore, in the present embodiment, the temperature of the pyrolysis furnace 1 is set at 300 to 700 ° C., preferably 350 to 450 ° C., as conditions under which the chlorine in the refuse can be substantially separated and removed and the char recovery rate can be 40% or more. It is desirable to do.
【0049】[0049]
【発明の効果】以上記載した如く本発明によれば、塩素
によるボイラチューブの高温腐食を防止しながら高温・
高圧の過熱蒸気を効率的に得ることができる。又本発明
によれば前記先願技術に比較して、更に効率良く熱分解
とチャー燃焼を可能にすると共に、且つ高温度の過熱蒸
気を得ることが出来る。等の種々の著効を有す。As described above, according to the present invention, it is possible to prevent high temperature corrosion of a boiler tube by chlorine while preventing high temperature corrosion.
High-pressure superheated steam can be obtained efficiently. Further, according to the present invention, it is possible to more efficiently perform pyrolysis and char combustion and obtain a high-temperature superheated steam, as compared with the prior art. And so on.
【図1】図1は本発明に対応する実施例に係る廃棄物の
焼却熱を利用した過熱蒸気製造装置を示す系統図であ
る。FIG. 1 is a system diagram showing an apparatus for producing superheated steam using waste heat of incineration according to an embodiment corresponding to the present invention.
【図2】図2は図1に示す逆流防止手段を、逆流防止機
能をもたせた圧力差形成手段により構成した概略図であ
る。FIG. 2 is a schematic diagram in which the backflow prevention means shown in FIG. 1 is constituted by a pressure difference forming means having a backflow prevention function.
【図3】図3は図1に示す逆流防止手段を、前記熱分解
手段側よりチャー燃焼手段側へ強制的にチャーの搬送を
行う機械的搬送手段で構成した概略図である。FIG. 3 is a schematic diagram in which the backflow prevention means shown in FIG. 1 is constituted by mechanical transport means for forcibly transporting char from the pyrolysis means side to the char combustion means side.
1 熱分解炉(熱分解手段) 2 砂等の流動媒体 10 燃焼炉(チャー燃焼手段) 11 分散板 16 サイクロン(分離手段) 20 第2ボイラ(第2の蒸気製造手段) 24 第1ボイラ(第1の蒸気製造手段) 31 灰溶融炉 34 熱分解ガス燃焼炉 36 水冷壁ボイラ(チャー燃焼手段の高温域側に
配した熱交換手段) 37 熱交換器 40 高温フィルタ 50、50A、50B 逆流防止手段 50a 第一流動層通路 50b 第二の流動層通路 59 シールポット 61 スクリューフィーダDESCRIPTION OF SYMBOLS 1 Pyrolysis furnace (pyrolysis means) 2 Fluid medium such as sand 10 Combustion furnace (char combustion means) 11 Dispersion plate 16 Cyclone (separation means) 20 Second boiler (second steam production means) 24 First boiler (first 1 steam production means) 31 ash melting furnace 34 pyrolysis gas combustion furnace 36 water-cooled wall boiler (heat exchange means arranged on the high temperature side of char combustion means) 37 heat exchanger 40 high temperature filter 50, 50A, 50B backflow prevention means 50a first fluidized bed passage 50b second fluidized bed passage 59 seal pot 61 screw feeder
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 FI F23C 10/20 F23G 5/16 ZABE F23G 5/00 115 5/30 ZABE ZAB ZABK 5/16 ZAB ZABM 5/30 ZAB 5/32 ZAB 5/46 ZABA ZABB 5/32 ZAB 7/00 103A 5/46 ZAB ZAB F23J 1/00 ZABB 7/00 103 F23C 11/02 ZAB ZAB 312 F23J 1/00 ZAB 313 (72)発明者 貝原 裕二 横浜市中区錦町12番地 三菱重工業株式 会社横浜製作所内 (72)発明者 佐藤 鉄雄 横浜市中区錦町12番地 三菱重工業株式 会社横浜製作所内 (56)参考文献 特開 平5−346204(JP,A) 特開 昭58−95104(JP,A) 特開 昭51−36201(JP,A) 特開 平1−252806(JP,A) 特開 平7−35322(JP,A) 特開 平5−141636(JP,A) (58)調査した分野(Int.Cl.7,DB名) F23G 5/027 F22B 1/18 F22G 1/16 F23C 10/00 F23C 10/18 F23C 10/20 F23G 5/00 F23G 5/16 F23G 5/30 F23G 5/32 F23G 5/46 F23G 7/00 F23J 1/00 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 Identification code FI F23C 10/20 F23G 5/16 ZABE F23G 5/00 115 5/30 ZABE ZAB ZABK 5/16 ZAB ZABM 5/30 ZAB 5/32 ZAB 5/46 ZABA ZABB 5/32 ZAB 7/00 103A 5/46 ZAB ZAB F23J 1/00 ZABB 7/00 103 F23C 11/02 ZAB ZAB 312 F23J 1/00 ZAB 313 (72) Inventor Yuji Kaihara Yokohama 12 Nishiki-cho, Naka-ku Mitsubishi Heavy Industries, Ltd. Yokohama Works (72) Inventor Tetsuo Sato 12 Nishiki-cho, Naka-ku, Yokohama-shi Mitsubishi Heavy Industries, Ltd. Yokohama Works (56) References JP-A-5-346204 (JP, A) JP-A-58-95104 (JP, A) JP-A-51-36201 (JP, A) JP-A-1-252806 (JP, A) JP-A-7-35322 (JP, A) JP-A-5-141636 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) F23G 5/027 F22B 1/18 F22G 1 / 16 F23C 10/00 F23C 10/18 F23C 10/20 F23G 5/00 F23G 5/16 F23G 5/30 F23G 5/32 F23G 5/46 F23G 7/00 F23J 1/00
Claims (4)
給して熱分解反応を行なわせ、その反応により発生した
熱分解ガスと未分解残渣および流動媒体から成るチャー
混合物と不燃物とを互いに分離する熱分解手段と、 空気または燃焼排ガスによって前記チャー混合物を上方
に吹き飛ばしながら前記未分解残渣を完全燃焼させるチ
ャー燃焼手段と、前記熱分解ガスを灰溶融炉に導入し、該灰溶融炉内に空
気若しくは酸素富化空気を前記熱分解ガスと共に導入し
て該熱分解ガス燃焼熱により灰分を溶融する灰溶融手段
と、 前記熱分解ガスを直接若しくは灰溶融手段通過後再燃焼
させて、その熱を利用して約400℃以下の温水または
蒸気を製造する第1の蒸気製造手段と、 前記チャー燃焼手段により得られた燃焼ガスの熱により
前記第1の蒸気製造手段で製造された温水または蒸気を
過熱蒸気とする第2の蒸気製造手段とを含み、 前記熱分解手段とチャー燃焼手段間を接続するチャー通
路中に、チャー逆流防止手段を配するとともに、前記逆
流防止手段が、前記熱分解手段側のチャー混合物界面を
チャー燃焼手段側のチャ−混合物界面より大に設定する
ことによりガスの逆流防止機能をもたせた圧力差形成手
段により構成した事を特徴とする廃棄物の焼却熱を利用
した過熱蒸気製造装置。(1) providing waste in a space having a temperature of 300 ° C. or more;
To cause the thermal decomposition reaction, which is generated by the reaction
Char consisting of pyrolysis gas, uncracked residue and flowing medium
Pyrolysis means for separating the mixture and the incombustible material from each other; and raising the char mixture by air or flue gas
To completely burn the undecomposed residue while blowing it away
Combustion means,The pyrolysis gas is introduced into an ash melting furnace, and the inside of the ash melting furnace is emptied.
Gas or oxygen-enriched air with the pyrolysis gas
Melting means for melting ash by the heat of combustion of the pyrolysis gas
When, The pyrolysis gas directly orReburn after passing through ash melting means
Let meUsing the heat, hot water of about 400 ° C or less or
First steam producing means for producing steam, and heat of the combustion gas obtained by the char burning means
Hot water or steam produced by the first steam producing means
A second steam producing means for producing superheated steam, and a char flow connecting the pyrolysis means and the char burning means.
Provide backflow prevention means on the road.And the reverse
Flow preventing means, the interface of the char mixture on the pyrolysis means side
Set larger than the char-mixture interface on the char combustion means side
Pressure difference forming hand with gas backflow prevention function
Composed of stepsUtilizes waste heat of incineration
Superheated steam production equipment.
給して熱分解反応を行なわせ、その反応により発生した
熱分解ガスと未分解残渣および流動媒体から成るチャー
混合物と不燃物とを互いに分離する熱分解手段と、 空気または燃焼排ガスによって前記チャー混合物を上方
に吹き飛ばしながら前記未分解残渣を完全燃焼させるチ
ャー燃焼手段と、 前記熱分解ガスを灰溶融炉に導入し、該灰溶融炉内に空
気若しくは酸素富化空気を前記熱分解ガスと共に導入し
て該熱分解ガス燃焼熱により灰分を溶融する灰溶融手段
と、 前記熱分解ガスを灰溶融手段通過後再燃焼させて、その
熱を利用して約400℃以下の温水または蒸気を製造す
る第1の蒸気製造手段と、 前記チャー燃焼手段により得られた燃焼ガスの熱により
前記第1の蒸気製造手 段で製造された温水または蒸気を
過熱蒸気とする第2の蒸気製造手段とを含み、 前記熱分解手段とチャー燃焼手段間を接続するチャー通
路中に、チャー逆流防止手段を配するとともに、 前記逆
流防止手段が、前記熱分解手段側よりチャー燃焼手段側
へ強制的にチャーの搬送を行う機械的搬送手段で構成
し、該機械的搬送手段の入口側より出口側に向け、上向
きに傾斜させ、重力差を持たせて配置したことを特徴と
する廃棄物の焼却熱を利用した過熱蒸気製造装置。(2)Provide waste in a space with a temperature of 300 ° C or higher.
To cause the thermal decomposition reaction, which is generated by the reaction
Char consisting of pyrolysis gas, uncracked residue and flowing medium
Pyrolysis means for separating the mixture and incombustibles from each other, Up the char mixture by air or flue gas
To completely burn the undecomposed residue while blowing it away
Combustion means, The pyrolysis gas is introduced into an ash melting furnace, and the inside of the ash melting furnace is emptied.
Gas or oxygen-enriched air with the pyrolysis gas
Melting means for melting ash by the heat of combustion of the pyrolysis gas
When, The pyrolysis gasAfter passing through the ash melting meansLet it reburn,That
Using heatAbout 400 ° C or lessProduce hot water or steam
First steam producing means, By the heat of the combustion gas obtained by the char combustion means
The first steam maker Hot water or steam produced in the stage
Second steam producing means for producing superheated steam, Char flow connecting the pyrolysis means and the char combustion means.
In the road, while installing a means for preventing backflow of char, The reverse
The flow prevention means is closer to the char combustion means than the pyrolysis means.
Composed of mechanical transport means for forcibly transporting char
And upward from the inlet side of the mechanical transport means toward the outlet side.
It is characterized by being tilted and placed with a difference in gravity
Superheated steam production equipment that uses the heat of incineration of waste.
加熱された蒸気若しくは前記いずれかの製造手段に導入
される温水若しくは蒸気の一部を、前記チャー燃焼手段
の高温域側に配した熱交換手段に適宜導入することを特
徴とすることを特徴とする請求項1若しくは2記載の廃
棄物の焼却熱を利用した過熱蒸気製造装置。3. The steam heated by the first or second steam producing means or a portion of hot water or steam introduced into any one of the producing means is disposed on a high temperature side of the char combustion means. 3. A superheated steam production apparatus utilizing waste incineration heat according to claim 1 or 2, wherein the apparatus is introduced into the heat exchange means as appropriate.
該チャー燃焼手段より燃焼ガスと前記流動媒体とを分離
する分離手段を含み、 前記第1若しくは第2の蒸気製造手段で加熱された蒸気
若しくは前記いずれかの製造手段に導入される温水若し
くは蒸気の一部を、適宜前記分離手段の流動媒体出口側
に導入し、該流動媒体との熱接触により加熱することを
特徴とする請求項1若しくは2記載の廃棄物の焼却熱を
利用した過熱蒸気製造装置。4. A steam connected to an outlet side of the char combustion means and separating the combustion gas and the fluid medium from the char combustion means, wherein the steam heated by the first or second steam production means is provided. Alternatively, a part of the hot water or steam introduced into any one of the production means is appropriately introduced to the fluid medium outlet side of the separation means, and heated by thermal contact with the fluid medium. Or a superheated steam production apparatus utilizing the heat of incineration of the waste according to 2 .
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP26246595A JP3276273B2 (en) | 1995-09-13 | 1995-09-13 | Superheated steam production equipment using waste incineration heat |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP26246595A JP3276273B2 (en) | 1995-09-13 | 1995-09-13 | Superheated steam production equipment using waste incineration heat |
Publications (2)
Publication Number | Publication Date |
---|---|
JPH0979541A JPH0979541A (en) | 1997-03-28 |
JP3276273B2 true JP3276273B2 (en) | 2002-04-22 |
Family
ID=17376168
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP26246595A Expired - Fee Related JP3276273B2 (en) | 1995-09-13 | 1995-09-13 | Superheated steam production equipment using waste incineration heat |
Country Status (1)
Country | Link |
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JP (1) | JP3276273B2 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR102674375B1 (en) * | 2023-11-07 | 2024-06-11 | 박안수 | Pyrolysis system for plastic wastes |
KR102679681B1 (en) * | 2023-10-18 | 2024-06-27 | 이동석 | Pyrolysis apparatus using plasma |
-
1995
- 1995-09-13 JP JP26246595A patent/JP3276273B2/en not_active Expired - Fee Related
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR102679681B1 (en) * | 2023-10-18 | 2024-06-27 | 이동석 | Pyrolysis apparatus using plasma |
KR102674375B1 (en) * | 2023-11-07 | 2024-06-11 | 박안수 | Pyrolysis system for plastic wastes |
Also Published As
Publication number | Publication date |
---|---|
JPH0979541A (en) | 1997-03-28 |
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