JPH0585807B2 - - Google Patents
Info
- Publication number
- JPH0585807B2 JPH0585807B2 JP2083713A JP8371390A JPH0585807B2 JP H0585807 B2 JPH0585807 B2 JP H0585807B2 JP 2083713 A JP2083713 A JP 2083713A JP 8371390 A JP8371390 A JP 8371390A JP H0585807 B2 JPH0585807 B2 JP H0585807B2
- Authority
- JP
- Japan
- Prior art keywords
- furnace
- swirling flow
- powder
- combustion
- combusted
- 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 - Lifetime
Links
Landscapes
- Incineration Of Waste (AREA)
- Treatment Of Sludge (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Description
〔産業上の利用分野〕
本発明はし尿、下水汚泥あるいはごみ等の可燃
性廃棄物を旋回流炉で焼却または溶融する方法に
関する。
〔従来の技術と発明が解決しようとする課題〕
旋回流炉は従来から石炭等の固体燃料を高温燃
焼させるスラグタツプ炉として知られており、近
年は汚泥等の減容、無害化のための溶融等にも応
用されている。
旋回流炉は燃焼用空気で炉内に強い旋回流を起
こし、そこに被燃焼粉体を吹き込んで燃焼させる
とともに、灰分を溶融させる場合は炉内壁に捕捉
して流下排出させた後冷却固化させてスラグとす
るもので、被燃焼粉体と燃焼用空気の接触が極め
て良好で、高温、高速の燃焼が可能である。
しかしながら、従来は安定燃焼が得られない、
スラグの回収率が安定しないなどの問題があり、
運転が必ずしも容易ではなかつた。
本発明者等は、種々検討、実験した結果、旋回
流炉に供給する被燃焼粉体の粒径が適当でないこ
と、および旋回流炉に供給される被燃焼粉体の量
の変動が原因になつていることを知り、効率的な
旋回溶融のためには、より大きくかつ広い粒径分
布のものが適していること、また合わせて、被燃
焼物を重量式計量によつて定量供給することが必
要であることを見出して本発明に至つた。
本発明は、旋回流炉において、安定燃焼させて
炉温を保持できるとともに、排ガス中のNOxお
よびダストの発生を抑制でき、高いスラグ回収率
を達成できる焼却溶融方法を提供することを目的
とする。
〔課題を解決するための手段〕
本発明の旋回流炉における焼却、溶融方法で
は、被燃焼粉体を次の粒径分布に調整して旋回流
炉に供給する。
平均径（メジアン径）：0.2〜0.6mm
１mm以上：10重量％以下
0.1mm以下：５〜30重量％
ここで、被燃焼粉体としては、し尿、工場排
水、下水処理によつて発生する汚泥あるいはごみ
等の可燃性廃棄物をあげることができるが、特に
下水汚泥が適している。これらは、水分10％程度
以下に歓送された状態で、旋回流炉に供給される
ことが望ましい。
これら被燃焼粉体は、旋回流炉内で十分燃焼で
きる範囲である粒径１mm程度以下にほぼ全体が粉
砕されたあと炉に供給されるが、その粒径分布
は、平均径（メジアン径）が0.2〜0.6mmで、かつ
１mm以上のものが10重量％以下、0.1mm以下のも
のが５〜30重量％とされることが必要である。こ
の際、平均径が0.6mmより大きく、又１mm以上の
粉体が10重量％を越えると、未燃分が発生し易く
なり、燃焼が不安定になつて炉内温度の制御が不
安定になり、さらに未燃のままスラグに排出され
てスラグをポーラス化するなどスラグ品質不良の
原因となる。一方、平均径が0.2mmより小さく、
又0.1mm以下の粉体が30重量％を越えて多くなる
と、旋回流炉から排煙に同伴されて飛散するダス
トが多くなつてスラグ化率が低下する。
また、この種の高温燃焼炉では一般にNOxの
発生を抑制するために、炉内で供給空気比を0.8
〜0.9程度に制限して１次燃焼を行い、次いで２
次燃焼を行なう２段燃焼が普通であるが、炉に供
給する粉体中に微細粒子が多くなると１次炉すな
わち旋回流炉内での燃焼が進行し過ぎて１次炉温
が上昇し、２段燃焼の制御が難しくなる。他方、
安定燃焼のためには、炉に投入されてすぐ着火燃
焼する微細粒子を一定量含んでいることが必要で
あり、0.1mm以下の粉体が５重量％より少ないと、
この着火性が悪くなり、１次炉の炉温が低下する
不都合が生じる。
被燃焼粉体は、通常空気移送あるいは炉排ガス
流により公知の旋回流炉内の旋回流に吹き込まれ
るが、解砕機で粉砕された被燃焼粉体の密度は変
動することがあるので、従来行なわれていたテー
ブルフイーダー等による容量式の定量供給では供
給の精度が悪く、炉内での燃焼が不安定になる。
このような不都合に対処するには、前記粒度分
布に調整された被燃焼粉体を、重量式計量して旋
回流炉に一定量を供給すると良い。
ここで重量式計量とは、単位時間当たりに旋回
流炉に供給される粉体の重量を計量する方法であ
る。
このような重量式計量を行える装置としては、
ホツパ減量式のもの、スケール付きテーブルフイ
ーダーなどがある。
一次炉の運転条件は被燃焼粉体の種類によつて
も異なるが、例えば、下水汚泥の溶融の場合は一
般に以下のとおりである。
炉温度 1350〜1450℃
旋回流速 10〜100ｍ／sec
炉負荷：（50〜300）×104Kcal／m3・Ｈ
空気比
１次炉 0.8〜0.9（−）
２次炉 0.2〜0.5（−）
全空気比 1.1〜1.3（−）
〔実施例〕
第１図に示した装置を用い、被燃焼粉体の粒度
を変えて旋回流炉による処理を行つた。
第１図の装置では、乾燥処理された被燃焼物は
乾燥汚泥貯留槽１に一時貯えられた後、スクリユ
ーフイーダ２によつて解砕機３に送られる。つい
でこの被燃焼物はコンベアー４によつて解砕汚泥
貯留槽５に送られて一時貯留された後、重量式の
計量フイーダー６によつて計量されて、ブロアー
７に接続された加圧移送ライン８を介して旋回流
炉９の一次炉９ａに空気圧送される。この炉９
は、第２図に示すように、竪形旋回流炉で、上部
に１次空気送入口１０…および乾燥汚泥送入口１
１…、下部に廃ガスおよび溶融スラグ抜出し口１
３を有している。そして、廃ガスは続いく２次燃
焼室（二次炉）９ｂで供給口１４から送入される
２次空気により２次燃焼後排出される構造となつ
ている。
この実施例では、下水汚泥を水分10％以下に乾
燥したあと、種々の粒径分布に粉砕し、それらを
旋回流炉９に圧送して焼却溶融処理を行なつた。
１次炉９ａの温度は通常1400±50℃とされ、２
次炉９ｂの温度もほぼこれと同じ温度に保つた。
乾燥汚泥の供給量は100〜150Kg／Hr（供給精度±
10％以内）、燃焼空気量は800〜900Nm3／Ｈ、旋
回流速は20〜50ｍ／secであつた。１次炉９ａと
２次炉９ｂにおける空気比はそれぞれ0.8〜0.9，
0.2〜0.5であつた。
結果を第１表に示す。
[Industrial Field of Application] The present invention relates to a method for incinerating or melting combustible waste such as human waste, sewage sludge or garbage in a swirling flow furnace. [Prior art and problems to be solved by the invention] Swirling flow furnaces have traditionally been known as slag tap furnaces that burn solid fuels such as coal at high temperatures. It is also applied to A swirling flow furnace uses combustion air to create a strong swirling flow inside the furnace, and the powder to be burned is blown into it and combusted.In addition, when melting ash, it is captured on the inner wall of the furnace and discharged downstream, after which it is cooled and solidified. The powder is heated to form slag, which allows for extremely good contact between the powder to be combusted and the combustion air, allowing for high-temperature, high-speed combustion. However, with conventional methods, stable combustion cannot be obtained.
There are problems such as unstable slag recovery rate,
Driving wasn't always easy. As a result of various studies and experiments, the inventors of the present invention found that the particle size of the powder to be combusted supplied to the swirling flow furnace was not appropriate and that the cause was fluctuations in the amount of powder to be combusted supplied to the swirling flow furnace. In order to achieve efficient swirl melting, larger particles with a wider particle size distribution are suitable, and in addition, the material to be combusted should be supplied quantitatively by gravimetric metering. The present invention was achieved by discovering that the following is necessary. An object of the present invention is to provide an incineration and melting method that can maintain furnace temperature through stable combustion in a swirling flow furnace, suppress the generation of NOx and dust in exhaust gas, and achieve a high slag recovery rate. . [Means for Solving the Problems] In the incineration and melting method in a swirling flow furnace of the present invention, the powder to be combusted is adjusted to the following particle size distribution and then supplied to the swirling flow furnace. Average diameter (median diameter): 0.2 to 0.6 mm 1 mm or more: 10% by weight or less 0.1 mm or less: 5 to 30% by weight Here, the powder to be burned includes human waste, industrial wastewater, and sludge generated from sewage treatment. Alternatively, combustible waste such as garbage can be mentioned, but sewage sludge is particularly suitable. It is desirable that these materials be supplied to the swirling flow furnace with a moisture content of approximately 10% or less. These powders to be combusted are almost entirely pulverized to a particle size of approximately 1 mm or less, which is the range for sufficient combustion in the swirling flow furnace, and then supplied to the furnace.The particle size distribution is determined by the average diameter (median diameter) is 0.2 to 0.6 mm, and 1 mm or more should be 10% by weight or less, and 0.1 mm or less should be 5 to 30% by weight. At this time, if the average diameter is larger than 0.6 mm and the powder with a diameter of 1 mm or more exceeds 10% by weight, unburned particles are likely to be generated, combustion becomes unstable, and the control of the temperature inside the furnace becomes unstable. Furthermore, the unburned slag is discharged into the slag, causing the slag to become porous, resulting in poor slag quality. On the other hand, the average diameter is smaller than 0.2mm,
Moreover, if the amount of powder of 0.1 mm or less exceeds 30% by weight, more dust will be scattered by the flue gas from the swirling flow furnace, and the slagging rate will decrease. In addition, in order to suppress the generation of NOx in this type of high-temperature combustion furnace, the air supply ratio within the furnace is generally reduced to 0.8.
The primary combustion is limited to ~0.9, and then the secondary
Two-stage combustion with secondary combustion is common, but if there are too many fine particles in the powder supplied to the furnace, the combustion in the primary furnace, that is, the swirling flow furnace, will progress too much and the temperature of the primary furnace will rise. Control of two-stage combustion becomes difficult. On the other hand,
For stable combustion, it is necessary to contain a certain amount of fine particles that ignite and burn as soon as they are put into the furnace, and if the powder is less than 5% by weight,
The ignitability deteriorates, causing the inconvenience of lowering the furnace temperature of the primary furnace. The powder to be combusted is normally blown into a swirling flow in a known swirling flow furnace by air transfer or a flow of furnace exhaust gas, but since the density of the powder to be combusted crushed by a crusher may vary, this method is not conventionally carried out. The volumetric quantitative supply using a table feeder, etc., which was previously used, has poor supply accuracy and combustion in the furnace becomes unstable. To deal with this inconvenience, it is preferable to gravimetrically weigh the powder to be combusted, which has been adjusted to have the particle size distribution, and supply a fixed amount to the swirling flow furnace. Here, gravimetric weighing is a method of measuring the weight of powder supplied to a swirling flow furnace per unit time. Devices that can perform this type of gravimetric weighing include:
There are hoppa weight-reducing types and table feeders with scales. The operating conditions of the primary furnace vary depending on the type of powder to be combusted, but for example, in the case of melting sewage sludge, they are generally as follows. Furnace temperature 1350~1450℃ Swirling flow rate 10~100m/sec Furnace load: (50~300) x 10 4 Kcal/m 3・H Air ratio Primary furnace 0.8~0.9 (-) Secondary furnace 0.2~0.5 (-) Total air ratio 1.1 to 1.3 (-) [Example] Using the apparatus shown in FIG. 1, the powder to be combusted was treated in a swirling flow furnace while changing the particle size. In the apparatus shown in FIG. 1, the dried combustible material is temporarily stored in a dry sludge storage tank 1, and then sent to a crusher 3 by a screw feeder 2. Next, this combustible material is sent to a crushed sludge storage tank 5 by a conveyor 4 and temporarily stored therein, and then weighed by a gravimetric metering feeder 6 and transferred to a pressurized transfer line connected to a blower 7. 8 to the primary furnace 9a of the swirling flow furnace 9. This furnace 9
As shown in Fig. 2, this is a vertical swirling flow furnace with a primary air inlet 10 and a dry sludge inlet 1 at the top.
1..., exhaust gas and molten slag outlet 1 at the bottom
It has 3. The waste gas is then discharged after secondary combustion by secondary air introduced from the supply port 14 in the subsequent secondary combustion chamber (secondary furnace) 9b. In this example, sewage sludge was dried to a moisture content of 10% or less, then ground into various particle size distributions, and then forced into a swirling flow furnace 9 for incineration and melting treatment. The temperature of the primary furnace 9a is normally 1400±50℃,
The temperature of the next furnace 9b was also maintained at approximately the same temperature.
The supply amount of dried sludge is 100 to 150Kg/Hr (supply accuracy ±
(within 10%), the amount of combustion air was 800 to 900 Nm 3 /H, and the swirling flow velocity was 20 to 50 m/sec. The air ratio in the primary furnace 9a and secondary furnace 9b is 0.8 to 0.9, respectively.
It was between 0.2 and 0.5. The results are shown in Table 1.
以上のように、被燃焼物を所定の粒度に調整す
る本発明の方法によれば、炉内での安定燃焼が可
能で炉温の保持が容易になる。特にそのような粒
度に調整した被燃焼物を重量計量で旋回流炉に供
給すると、炉内での燃焼の安定性がさらに向上す
る。
特に、２段燃焼の制御も安定し、高燃焼率を得
るとともに、排ガス中のNOxの発生を抑制する
ことができる。
又、未燃分を少なくし、かつ排煙に同伴される
ダストの飛散を最小限に防止できるので、スラグ
化回収率を高くすることができる。
As described above, according to the method of the present invention for adjusting the particle size of the combustible material to a predetermined particle size, stable combustion in the furnace is possible and the furnace temperature can be easily maintained. In particular, when the combustion material adjusted to such a particle size is fed to the swirling flow furnace by weight measurement, the stability of combustion within the furnace is further improved. In particular, the control of the two-stage combustion is stable, a high combustion rate can be obtained, and the generation of NOx in the exhaust gas can be suppressed. Moreover, since the unburned content can be reduced and the scattering of dust entrained in exhaust smoke can be minimized, the slagging recovery rate can be increased.
第１図は本発明の焼却溶融方法を実施する装置
の一例を示す概略構成図、第２図は同装置で用い
た旋回流炉を示す断面図である。
６……計量フイーダ、８……空気移送ライン、
９……旋回流炉。
FIG. 1 is a schematic configuration diagram showing an example of an apparatus for carrying out the incineration melting method of the present invention, and FIG. 2 is a sectional view showing a swirling flow furnace used in the apparatus. 6...Weighing feeder, 8...Air transfer line,
9...Swirling flow furnace.
Claims (1)
にあたり、平均径（メジアン径）が0.2〜0.6mmで
あり、かつ１mm以上が10重量％以下、0.1mm以下
が５〜30重量％となるように被燃焼粉体の粒度分
布を調整して旋回流炉に供給することを特徴とす
る旋回流炉における焼却溶融方法。 ２ 前記被燃焼粉体を重量式計量して旋回流炉に
定量供給することを特徴とする請求項１記載の旋
回流炉における焼却溶融方法。[Claims] 1. When incinerating or melting the powder to be combusted in a swirling flow furnace, the average diameter (median diameter) is 0.2 to 0.6 mm, and 1 mm or more is 10% by weight or less, and 0.1 mm or less is 5% by weight or less. 1. A method for incineration and melting in a swirling flow furnace, characterized in that the particle size distribution of powder to be combusted is adjusted to 30% by weight and then supplied to the swirling flow furnace. 2. The incineration and melting method in a swirling flow furnace according to claim 1, characterized in that the powder to be burned is weighed gravimetrically and fed in a quantitative manner to the swirling flow furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2083713A JPH03282109A (en) | 1990-03-30 | 1990-03-30 | Method of incineration and melting in swirl flow furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2083713A JPH03282109A (en) | 1990-03-30 | 1990-03-30 | Method of incineration and melting in swirl flow furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03282109A JPH03282109A (en) | 1991-12-12 |
| JPH0585807B2 true JPH0585807B2 (en) | 1993-12-08 |
Family
ID=13810147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2083713A Granted JPH03282109A (en) | 1990-03-30 | 1990-03-30 | Method of incineration and melting in swirl flow furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH03282109A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3600262B2 (en) | 1994-03-04 | 2004-12-15 | 月島機械株式会社 | Measuring device for slag flow rate and furnace equipment using the same |
| US5694480A (en) * | 1995-08-30 | 1997-12-02 | Tsukishima Kikai Co., Ltd. | Molten slag flow rate measuring device and furnace facilities using the same |
| US11293635B2 (en) | 2017-09-01 | 2022-04-05 | Alberto Carlos Pereira Filho | Reactor for a process of advanced combustion for burning biomass and waste |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0650172B2 (en) * | 1985-03-19 | 1994-06-29 | 月島機械株式会社 | Combustion method for solid substances containing incombustibles in swirl flow melting equipment |
-
1990
- 1990-03-30 JP JP2083713A patent/JPH03282109A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03282109A (en) | 1991-12-12 |
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