JP2000218292A - Method and device for treating sludge - Google Patents
Method and device for treating sludgeInfo
- Publication number
- JP2000218292A JP2000218292A JP11024046A JP2404699A JP2000218292A JP 2000218292 A JP2000218292 A JP 2000218292A JP 11024046 A JP11024046 A JP 11024046A JP 2404699 A JP2404699 A JP 2404699A JP 2000218292 A JP2000218292 A JP 2000218292A
- Authority
- JP
- Japan
- Prior art keywords
- incinerator
- sludge
- ash
- dewatered cake
- dewatering
- 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.)
- Granted
Links
Landscapes
- Gasification And Melting Of Waste (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、汚泥を脱水して焼
却処理する汚泥処理方法及び装置に関し、例えば下水処
理場から排出される汚泥を処理する汚泥処理方法及び装
置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a sludge treatment method and apparatus for dewatering and incinerating sludge, for example, a sludge treatment method and apparatus for treating sludge discharged from a sewage treatment plant.
【０００２】[0002]
【従来の技術】下水処理場から排出される汚泥の処理方
法として、従来から、汚泥を脱水機で脱水したうえで、
焼却炉で焼却処理する方法が用いられている。焼却炉及
び後続の排ガス等の処理設備をコンパクトにするために
は、脱水した脱水ケーキの含水率をできるだけ少なくす
ることが好ましい。2. Description of the Related Art As a method of treating sludge discharged from a sewage treatment plant, conventionally, sludge is dehydrated by a dehydrator and then dewatered.
A method of incineration in an incinerator is used. In order to make the incinerator and the subsequent equipment for treating exhaust gas etc. compact, it is preferable to reduce the water content of the dewatered dewatered cake as much as possible.
【０００３】[0003]
【発明が解決しようとする課題】汚泥中の有機物等の可
燃物の含有率が高くなると、汚泥の発熱量が増し、焼却
時の焼却炉の炉内温度が上がって、焼却炉への熱的負荷
が増し、汚泥の一部が融解して炉内の壁面にこびりつい
たりする問題が起こる。従来は、炉内に直接水や空気を
注入することで、炉内の温度上昇を抑えていた。しかし
ながら、このように炉内に水や空気を注入すると、排ガ
スのガス量が増加するため、排ガス処理設備が大型化し
てしまうという問題があった。When the content of combustible substances such as organic substances in sludge increases, the calorific value of the sludge increases, and the temperature in the incinerator at the time of incineration increases. The load increases, causing a problem that a part of the sludge is melted and sticks to the wall in the furnace. Conventionally, the temperature rise in the furnace has been suppressed by directly injecting water or air into the furnace. However, when water or air is injected into the furnace in this way, the amount of exhaust gas increases, and thus there is a problem that the exhaust gas treatment equipment becomes large.
【０００４】この問題点に鑑みて、本発明は、排ガスの
ガス量を増加させることなく焼却炉内の温度上昇を抑
え、焼却炉、後続の排ガス処理設備をコンパクトにする
ことが可能な汚泥処理方法及び装置を提供することを課
題とする。[0004] In view of this problem, the present invention suppresses the temperature rise in an incinerator without increasing the amount of exhaust gas, and enables sludge treatment capable of reducing the size of the incinerator and subsequent exhaust gas treatment equipment. It is an object to provide a method and an apparatus.
【０００５】[0005]
【課題を解決するための手段】上記課題を解決するた
め、本発明の汚泥処理方法は、汚泥を脱水して脱水ケー
キ化する脱水工程と、脱水ケーキを焼却炉で焼却処理す
る焼却工程とを備えている汚泥処理方法において、汚泥
あるいは脱水ケーキとに焼却処理後の焼却灰とを混合し
て焼却炉に投入される脱水ケーキの発熱量を調整する調
整工程をさらに備えていることを特徴とする。Means for Solving the Problems To solve the above problems, the sludge treatment method of the present invention comprises a dewatering step of dewatering sludge to form a dewatered cake and an incineration step of incinerating the dewatered cake in an incinerator. The sludge treatment method provided, further comprising an adjusting step of mixing the sludge or dewatered cake with the incinerated ash after the incineration treatment and adjusting the calorific value of the dewatered cake fed into the incinerator. I do.
【０００６】一方、本発明の汚泥処理装置は、汚泥を脱
水して脱水ケーキ化する脱水機と、この脱水ケーキを焼
却処理する焼却炉とを備えている汚泥処理装置におい
て、汚泥あるいは脱水ケーキに焼却処理後の焼却灰を投
入して混合する投入機と、投入機による投入量を脱水ケ
ーキの発熱量に応じて調整する制御装置と、をさらに備
えていることを特徴とする。On the other hand, a sludge treatment apparatus of the present invention is a sludge treatment apparatus comprising a dehydrator for dewatering sludge to form a dewatered cake and an incinerator for incinerating the dewatered cake. It is further characterized by further comprising a charging device for charging and mixing the incinerated ash after the incineration treatment, and a control device for adjusting a charging amount by the charging device in accordance with a calorific value of the dewatered cake.
【０００７】汚泥あるいは脱水ケーキに焼却処理後の焼
却灰を投入して混合することにより、投入後の汚泥ある
いは脱水ケーキの灰分が増加する一方、可燃物含有量、
含水率はともに低下する。その結果、単位重量、単位体
積あたりの発熱量も低下する。つまり、焼却灰の投入量
を制御することで最終的に得られる焼却灰混合脱水ケー
キの発熱量を調整することが可能である。こうして焼却
する焼却灰混合脱水ケーキの発熱量を調整することで焼
却炉の温度が上昇しないよう制御できる。灰分は焼却時
の燃焼反応には関与しないので、排ガスは焼却灰の混合
の有無に関らず増加することがなく、排ガス処理設備を
大型化する必要がない。また、灰分混入による体積増加
の影響は少ないので、焼却炉もコンパクト化できる。[0007] By injecting and mixing the incinerated ash after the incineration treatment into the sludge or dewatered cake, the ash content of the sludge or the dewatered cake after input increases, while the combustible material content,
Both moisture contents decrease. As a result, the calorific value per unit weight and unit volume also decreases. That is, by controlling the amount of incinerated ash, it is possible to adjust the calorific value of the finally obtained incinerated ash mixed dewatered cake. By adjusting the calorific value of the incinerated ash mixed dewatering cake to be incinerated in this way, it is possible to control the temperature of the incinerator so as not to rise. Since the ash does not participate in the combustion reaction at the time of incineration, the exhaust gas does not increase irrespective of the presence or absence of incineration ash, and there is no need to increase the size of the exhaust gas treatment facility. In addition, since the effect of volume increase due to ash mixing is small, the incinerator can be made compact.
【０００８】この調整工程は、脱水工程に先立って行な
っても、脱水工程と焼却工程の間に行なってもよい。つ
まり、投入機は、脱水機の手前に配置されていても、脱
水機と焼却炉の間に配置されていてもよい。脱水の前に
汚泥に焼却灰を投入すると、汚泥と焼却灰の混合が容易
であり、さらに、脱水効率を高めることができるので、
より好ましい。This adjusting step may be performed prior to the dewatering step or between the dewatering step and the incineration step. That is, the charging machine may be arranged before the dehydrator or between the dehydrator and the incinerator. If incineration ash is added to sludge before dehydration, mixing of sludge and incineration ash is easy, and furthermore, dehydration efficiency can be increased.
More preferred.
【０００９】この発熱量の調整は、焼却炉の温度と脱水
ケーキの含水率を基にして焼却炉の炉内温度が目標温度
となるように行なうことが好ましい。焼却炉の温度は、
炉内温度計により随時測定が可能であり、脱水ケーキの
含水率はサンプリングにより測定が可能である。炉の温
度と脱水ケーキの含水率から脱水ケーキの組成を推定
し、焼却炉の炉内温度が目標温度となる発熱量になる組
成に調整することが可能である。It is preferable that the heating value be adjusted based on the temperature of the incinerator and the water content of the dewatered cake so that the temperature in the incinerator reaches the target temperature. The temperature of the incinerator is
It can be measured at any time by a furnace thermometer, and the moisture content of the dehydrated cake can be measured by sampling. It is possible to estimate the composition of the dewatered cake from the temperature of the furnace and the moisture content of the dewatered cake, and to adjust the composition so that the in-furnace temperature of the incinerator becomes a calorific value that becomes the target temperature.
【００１０】[0010]
【発明の実施の形態】以下、添付図面を参照して本発明
の好適な実施の形態について詳細に説明する。図１は、
本発明に係る汚泥処理装置の全体フロー図である。Preferred embodiments of the present invention will be described below in detail with reference to the accompanying drawings. FIG.
It is the whole flow figure of the sludge treatment device concerning the present invention.
【００１１】この装置は、汚泥を脱水する脱水機１と、
汚泥中の可燃物を焼却して減量処理する焼却炉２と、焼
却炉排ガスを処理する排ガス処理設備３と、処理済の排
ガスを大気中に放出する煙突４と、排ガスから焼却灰を
回収する灰回収設備５を備えている。脱水機１と焼却炉
２、焼却炉２と排ガス処理設備３、排ガス処理設備３と
煙突４、排ガス処理設備３と灰回収設備５とはそれぞれ
ラインＬ２、Ｌ３、Ｌ４、Ｌ５により接続されており、
脱水機１に汚泥を投入するラインＬ１には、この汚泥に
灰回収設備５で回収された焼却灰の一部を混合するライ
ンＬ６が接続されている。This apparatus comprises a dehydrator 1 for dewatering sludge,
Incinerator 2 for incinerating combustibles in sludge for weight reduction, exhaust gas treatment equipment 3 for treating incinerator exhaust gas, chimney 4 for releasing treated exhaust gas into the atmosphere, and collecting incineration ash from exhaust gas An ash recovery facility 5 is provided. The dehydrator 1 and the incinerator 2, the incinerator 2 and the exhaust gas treatment equipment 3, the exhaust gas treatment equipment 3 and the chimney 4, the exhaust gas treatment equipment 3 and the ash recovery equipment 5 are connected by lines L2, L3, L4 and L5, respectively. ,
A line L <b> 6 for mixing a part of the incinerated ash recovered by the ash recovery facility 5 with the sludge is connected to a line L <b> 1 for charging the sludge into the dehydrator 1.
【００１２】ここで、脱水機１には、フィルタープレス
脱水装置、ベルトプレス脱水装置、遠心脱水装置などが
好適に使用可能である。また、焼却炉２には、各種の焼
却炉が使用可能であるが、流動床式や循環流動層式の焼
却炉が好適である。排ガス処理設備３は、排熱ボイラー
や空気予熱器などの熱回収設備や急冷塔、脱硝・脱硫設
備、集塵機などを組み合わせて構成される。Here, as the dewatering machine 1, a filter press dewatering device, a belt press dewatering device, a centrifugal dewatering device, or the like can be suitably used. Although various types of incinerators can be used as the incinerator 2, a fluidized bed type or a circulating fluidized bed type incinerator is preferable. The exhaust gas treatment equipment 3 is configured by combining heat recovery equipment such as an exhaust heat boiler and an air preheater, a quenching tower, denitration / desulfurization equipment, and a dust collector.
【００１３】次に、図１、図２を用いて、本装置の動
作、すなわち、本発明に係る汚泥処理方法について説明
する。図２は、本装置における物質収支を示している。Next, the operation of the present apparatus, that is, the sludge treatment method according to the present invention will be described with reference to FIGS. FIG. 2 shows a material balance in the present apparatus.
【００１４】下水処理場等で発生した水分を大量に含む
汚泥Ｍs(kg)がラインＬ１を介して脱水機１へと供給さ
れる。この汚泥の組成は、図２（ａ）に示されるよう
に、水分含有量がγs、可燃分率がＶs、灰分の分率がＡ
sである。したがって、可燃分の単位重量あたりの発熱
量をＱv(kcal/kg)とすると、この汚泥の単位重量あたり
の発熱量はＱvＶs(kcal/kg)となる。この下水汚泥に後
続の焼却処理によって処理され、灰回収設備５で回収さ
れた焼却灰をラインＬ６を介してＭa(kg)混入する。つ
まり、ラインＬ６がラインＬ１への投入機として機能す
る。この混入割合の設定については後述する。投入焼却
灰の組成は、図２（ｂ）に示されるように、全て不燃性
の灰分からなる。したがって、その発熱量は０(kcal/k
g)である。こうして下水汚泥と投入焼却灰が混合された
脱水前汚泥の組成は、図２（ｃ）に示されるように、水
分と可燃分の比率がそれぞれγsＭs／（Ｍs＋Ｍa）、Ｖ
sＭs／（Ｍs＋Ｍa）となり減少する一方、灰分は、（Ａ
sＭs＋Ｍa）／（Ｍs＋Ｍa）となって増加する。この結
果、単位重量あたりの発熱量も｛ＱvＶsＭs／（Ｍs＋Ｍ
a）｝(kcal/kg)と低下する。Sludge Ms (kg) containing a large amount of water generated in a sewage treatment plant or the like is supplied to the dehydrator 1 through a line L1. As shown in FIG. 2 (a), the composition of this sludge has a water content of γs, a combustible fraction of Vs, and an ash fraction of A.
s. Therefore, if the calorific value per unit weight of combustibles is Qv (kcal / kg), the calorific value per unit weight of this sludge is QvVs (kcal / kg). The sewage sludge is treated by a subsequent incineration treatment, and the incinerated ash recovered by the ash recovery equipment 5 is mixed with Ma (kg) through the line L6. That is, the line L6 functions as a charging machine for the line L1. The setting of the mixing ratio will be described later. As shown in FIG. 2 (b), the composition of the input incineration ash is composed entirely of non-combustible ash. Therefore, the calorific value is 0 (kcal / k
g). As shown in FIG. 2 (c), the composition of the pre-dewatering sludge in which the sewage sludge and the incinerated ash are mixed has a ratio of moisture and combustible content of γsMs / (Ms + Ma) and V, respectively.
sMs / (Ms + Ma) and the ash content is (A
sMs + Ma) / (Ms + Ma) and increases. As a result, the calorific value per unit weight is also ΔQvVsMs / (Ms + M
a) It decreases to｝ (kcal / kg).
【００１５】この脱水前汚泥は脱水機１に導かれ、Ｗ(k
g)の水が脱水される。なお、デカンタ型などの連続処理
が可能な遠心脱水機を用いる場合は、脱水機１内で汚泥
が攪拌されるので、汚泥と焼却灰を別ラインで脱水機１
に投入しても両者を脱水機１内で混合することができ
る。つまり、脱水機１が投入機を兼ねることになる。脱
水前あるいは脱水時に汚泥に焼却灰を混合することによ
り、脱水効率を高めることも可能となる。The pre-dewatering sludge is led to the dewatering machine 1 and is subjected to W (k
g) water is dehydrated. When a centrifugal dehydrator capable of continuous processing, such as a decanter type, is used, the sludge is stirred in the dehydrator 1, so that the sludge and the incinerated ash are separated on a separate line.
Can be mixed in the dehydrator 1. That is, the dehydrator 1 also functions as a charging machine. By mixing incineration ash with sludge before or during dehydration, it is also possible to increase dehydration efficiency.
【００１６】図２（ｄ）はこうして脱水処理された後の
汚泥、すなわち、脱水ケーキの組成を示している。得ら
れる脱水ケーキの重量をＭc(kg)とすると、Ｍc＝Ｍs＋
Ｍa−Ｗが成立し、水分比（含水率）は、（γsＭs−
Ｗ）／Ｍcと脱水前に比べて減少する一方、可燃分、灰
分はそれぞれＶsＭs／Ｍc、（ＡsＭs＋Ｍa）／Ｍcと脱
水前に比べて増加する。この結果、単位重量あたりの発
熱量も（ＱvＶsＭs／Ｍc）(kcal/kg)と脱水前より増加
するが、投入焼却灰量を増加させるに従って、脱水ケー
キの単位重量当たりの発熱量は元の下水汚泥よりも低下
する。したがって、前述した焼却灰の添加量Ｍaを調整
することで、発熱量を調整することが可能である。FIG. 2D shows the composition of the sludge, that is, the dewatered cake after the dewatering treatment. Assuming that the weight of the obtained dehydrated cake is Mc (kg), Mc = Ms +
Ma-W holds, and the water ratio (moisture content) is (γsMs−
W) / Mc, as compared to before dehydration, while the combustibles and ash increase to VsMs / Mc, (AsMs + Ma) / Mc, respectively, before dehydration. As a result, the calorific value per unit weight also increases to (QvVsMs / Mc) (kcal / kg) before dehydration, but as the amount of incinerated ash increases, the calorific value per unit weight of the dewatered cake becomes the original sewage. Lower than sludge. Therefore, the heat value can be adjusted by adjusting the addition amount Ma of the incineration ash described above.
【００１７】この脱水ケーキを焼却炉２へ投入して８０
０〜９００℃程度で燃焼させて焼却処理する。脱水ケー
キの発熱量を調整することで、炉内温度を調整すること
が可能である。さらに、炉内温度が目標温度となるよ
う、焼却灰の添加量Ｍaをフィードバック制御して調整
してもよい。The dehydrated cake is put into the incinerator 2 and
It is burned at about 0 to 900 ° C. and incinerated. By adjusting the calorific value of the dehydrated cake, it is possible to adjust the furnace temperature. Further, the addition amount Ma of the incinerated ash may be adjusted by feedback control so that the furnace temperature becomes the target temperature.
【００１８】焼却炉２内では、脱水ケーキを図２（ｅ）
に示されるようにＡ(kg)の空気を付加して燃焼させるこ
とで、同図（ｆ）及び（ｇ）にそれぞれ示されるよう
に、｛（１−Ａs）Ｍs＋Ａ−Ｗ｝(kg)の排ガスと、（Ａ
sＭs＋Ｍa）(kg)のダスト（焼却灰）が生成される。こ
の排ガスとダストはラインＬ３を介して排ガス処理設備
３に送られ、排ガスは同設備で処理されたうえで、ライ
ンＬ４を介して煙突４から大気中へと放出される。一
方、焼却灰は排ガス処理設備３で分離されてラインＬ５
を介して灰回収設備５へと送られ、このうちＭa(kg)が
前述したようにラインＬ６を介して戻される。In the incinerator 2, the dewatered cake is placed in the incinerator 2 as shown in FIG.
By adding and burning the air of A (kg) as shown in FIG. 2 (f) and (g), as shown in FIGS. 3 (f) and 3 (g), {(1-As) Ms + A−W} (kg) Exhaust gas and (A
sMs + Ma) (kg) dust (incineration ash) is generated. The exhaust gas and the dust are sent to the exhaust gas treatment equipment 3 via the line L3, and the exhaust gas is treated by the equipment and then discharged from the chimney 4 to the atmosphere via the line L4. On the other hand, the incinerated ash is separated in the exhaust gas treatment equipment 3 and
To the ash recovery facility 5, of which Ma (kg) is returned via the line L6 as described above.
【００１９】排ガス処理設備３に送られる排ガスの量
は、投入された焼却灰の量とは無関係であり、焼却灰を
投入したことによって増加することはない。そして、脱
水した水の量だけ減少しているので、排ガス体積が低減
され、処理設備をコンパクト化することが可能である。
一方、ダストは焼却灰の添加によって増加するが、ダス
トの体積は排ガスの体積に比べると極端に小さいので、
その増加量に伴う処理設備への負荷増加は大きくない。
そして、本装置においては、焼却灰の一部が循環するだ
けであるため、外部から添加剤を添加するのと異なり、
添加剤の保管施設等が不要で添加剤のコストもかからな
いので、低コストで実現できる。The amount of the exhaust gas sent to the exhaust gas treatment equipment 3 is irrelevant to the amount of the incinerated ash, and does not increase by the incineration ash. Since the amount of dewatered water is reduced, the volume of exhaust gas is reduced, and the processing equipment can be made compact.
On the other hand, dust increases with the addition of incineration ash, but since the volume of dust is extremely small compared to the volume of exhaust gas,
The increase in the load on the processing equipment accompanying the increase is not large.
And, in this device, since only part of the incineration ash circulates, unlike adding additives from the outside,
Since there is no need for a storage facility for the additive and no cost for the additive, the present invention can be realized at low cost.
【００２０】ここで、焼却炉２の温度調整のための焼却
灰の添加量制御について図３を参照して詳細に説明す
る。図３は、焼却炉に投入された汚泥の灰分、含水率に
対する炉頂温度（循環流動層式焼却炉内の頂部部分の温
度）となる自燃限界線を示す線図である。Here, the control of the amount of incineration ash added for adjusting the temperature of the incinerator 2 will be described in detail with reference to FIG. FIG. 3 is a diagram showing a self-combustion limit line that indicates the furnace top temperature (the temperature of the top part in the circulating fluidized bed incinerator) with respect to the ash content and the water content of the sludge fed into the incinerator.
【００２１】脱水ケーキの可燃分の単位重量あたりの発
熱量はほぼ一定であり、焼却炉２の熱容量は既知である
から、所定の焼却炉２においては、燃焼させる脱水ケー
キの組成がわかれば、補助燃料を使用せず、可燃分を完
全燃焼させた時の炉内温度を算出することができる。ま
た、脱水ケーキの含水率、可燃分率、灰分率をそれぞれ
γc、Ｖc、Ａcとすると、γc＋Ｖc＋Ａc＝１が成立する
ので、いずれか２つがわかれば、他の１つは算出でき
る。図３は、ある循環流動層式焼却炉において、所定量
の汚泥を投入して補助燃料を供給することなく完全燃焼
させた場合に、この焼却炉の炉頂部分の温度が一定とな
る含水率と灰分率の関係を求めて線図として表したもの
である。焼却炉の炉内容積９７ｍ3、脱水ケーキの投入
量は１００ｔ／日、可燃分の高位発熱量は約５６００kc
al/kgとして計算した。Since the calorific value per unit weight of the combustible content of the dewatered cake is substantially constant and the heat capacity of the incinerator 2 is known, in a given incinerator 2, if the composition of the dewatered cake to be burned is known, It is possible to calculate the furnace temperature when combustible components are completely burned without using auxiliary fuel. If the moisture content, combustible content, and ash content of the dehydrated cake are γc, Vc, and Ac, respectively, γc + Vc + Ac = 1 holds, so if one of them is known, the other one can be calculated. Fig. 3 shows the moisture content at which the temperature at the top of the incinerator becomes constant when a certain amount of sludge is injected and completely burned without supplying auxiliary fuel in a certain circulating fluidized bed incinerator. And the relationship between the ash content and the ash content is obtained and represented as a diagram. The incinerator has a furnace volume of 97m 3 , the amount of dewatered cake charged is 100t / day, and the high calorific value of the combustible is about 5600kc
Calculated as al / kg.
【００２２】図中で示す線は、それぞれ炉頂温度
が８００℃、８５０℃、９００℃となる線を示してお
り、灰分率あるいは含水率が高くなるほど、すなわち、
可燃分率が低くなるほど炉頂温度は低下することがわか
る。そして、の各曲線において、灰分率と含水率
は、 γc＝ａＡc2＋ｂＡc＋ｃ の関係を満たすことがわかった。この式は焼却炉の炉形
状、運転条件と炉頂温度等により、自燃限界となる汚泥
成分を数点算出し、これらの点の近似曲線を最小二乗法
により求めたものである。つまり、ａ、ｂ、ｃは定数と
なる。The lines shown in the figure indicate the lines where the furnace top temperature is 800 ° C., 850 ° C., and 900 ° C., respectively, and the higher the ash content or the water content, that is,
It can be seen that the lower the combustible fraction, the lower the furnace top temperature. In each of the curves, it was found that the ash content and the water content satisfied the relationship of γc = aAc 2 + bAc + c. This equation is obtained by calculating several points of the sludge component which becomes the self-burning limit based on the furnace shape, operating conditions, furnace top temperature and the like of the incinerator, and obtaining an approximate curve of these points by the least square method. That is, a, b, and c are constants.
【００２３】次に、ある脱水ケーキを燃焼させたときの
炉頂温度が目標より高いときに、炉頂温度を目標温度に
調整するために必要な脱水ケーキ１ｋｇに対して添加す
べき焼却灰の量Ｍa1（kg）の算出について説明する。調
整前の脱水ケーキの含水率、可燃分率、灰分率をそれぞ
れγc1、Ｖc1、Ａc1、調整後の脱水ケーキの含水率、可
燃分率、灰分率をそれぞれγct、Ｖct、Ａctとすると、 γct＝ａＡct2＋ｂＡct＋ｃ …（１） を満たすａ、ｂ、ｃは既知である。調整前の脱水ケーキ
１ｋｇに対して灰分１００％の焼却灰Ｍa1（ｋｇ）を添
加するのであるから、 γct＝γc1／（１＋Ｍa1） …（２ａ） Ｖct＝Ｖc1／（１＋Ｍa1） …（２ｂ） Ａct＝（Ａc1＋Ｍa1）／（１＋Ｍa1） …（２ｃ） がそれぞれ成立する。（２ａ）（２ｃ）式を（１）式に
代入して整理すると、 ＡＭa12＋ＢＭa1＋Ｃ＝０ …（３） ただし、Ａ＝ａ＋ｂ＋ｃ Ｂ＝２ａＡc1＋ｂ（１＋Ａc1）＋２ｃ−γc1 Ｃ＝ａＡc12＋ｂＡc1＋ｃ−γc1 が成立し、（３）式からＭa1を求めることができる。Next, when the furnace top temperature at the time of burning a certain dewatered cake is higher than the target, the incineration ash to be added to 1 kg of the dewatered cake required to adjust the furnace top temperature to the target temperature is obtained. The calculation of the amount Ma1 (kg) will be described. If the moisture content, combustible content, and ash content of the dewatered cake before adjustment are γc1, Vc1, and Ac1, respectively, and the water content, flammable content, and ash content of the dehydrated cake after adjustment are γct, Vct, and Act, respectively, γct = aAct 2 + bAct + c (1) a, b, and c that satisfy the following are known. Since incinerated ash Ma1 (kg) with 100% ash is added to 1 kg of the dewatered cake before adjustment, γct = γc1 / (1 + Ma1) (2a) Vct = Vc1 / (1 + Ma1) (2b) Act = (Ac1 + Ma1) / (1 + Ma1) (2c) holds. Rearranging (2a) to (2c) Formula (1) are substituted into equation, AMa1 2 + BMa1 + C = 0 ... (3) provided that, A = a + b + c B = 2aAc1 + b (1 + Ac1) + 2c-γc1 C = aAc1 2 + bAc1 + c-γc1 is This holds, and Ma1 can be obtained from equation (3).
【００２４】具体的には、図３の線図において、の曲
線においては、ａ＝０．００１５、ｂ＝−０．８１、ｃ
＝０．７７となる。ここで、調整前の脱水ケーキの灰
分、含水率がそれぞれ５％、７０％（Ｐ点）であったと
すると、（３）式のＡ、Ｂ、Ｃはそれぞれ−０．０３
４、−０．００１３、０．０３４であり、Ma1＝０．９
８となる。この結果、調整後の脱水ケーキの灰分、含水
率は図に占めされるようにそれぞれ５２．１％、３５．
３％（Ｑ点）となる。Specifically, in the curve of FIG. 3, a = 0.0015, b = -0.81, c
= 0.77. Here, assuming that the ash content and the water content of the dewatered cake before adjustment are 5% and 70% (point P), respectively, A, B, and C in the expression (3) are −0.03.
4, −0.0013, 0.034, and Ma1 = 0.9
It becomes 8. As a result, the ash content and the water content of the dehydrated cake after adjustment were 52.1% and 35.
3% (point Q).
【００２５】実際の制御においては、例えば、炉内温度
計によりオンラインでの測定が容易な焼却炉２の炉頂温
度と、脱水機１出口においてサンプリングにより測定可
能な脱水ケーキの含水率をそれぞれ測定してこれらを基
にして図３の曲線からケーキの灰分率を推定し、（３）
式を用いて最適な焼却灰投入量を求めてこの投入量とな
るよう灰回収設備５からラインＬ６への供給量を制御す
ればよい。さらに、精密に調整する場合は、多少の時間
遅れを伴うことになるが、脱水ケーキあるいは汚泥をサ
ンプリングして灰分率あるいは可燃分率、発熱量を測定
し、これをもとにして投入量を調整してもよい。In actual control, for example, the furnace top temperature of the incinerator 2 which can be easily measured on-line by an in-furnace thermometer, and the water content of the dewatered cake which can be measured by sampling at the outlet of the dehydrator 1 are measured. Then, based on these, the ash content of the cake was estimated from the curve in FIG. 3, and (3)
The optimum amount of incinerated ash input may be obtained using the equation, and the amount of supply from the ash recovery facility 5 to the line L6 may be controlled so as to achieve this input amount. In addition, in the case of precise adjustment, there will be some time delay.However, the dehydrated cake or sludge is sampled, and the ash content or flammable content and the calorific value are measured. It may be adjusted.
【００２６】以上の説明では、脱水機１の手前で汚泥に
焼却灰を投入する装置及び方法について説明してきた
が、図１に点線で示すラインＬ６’を介して脱水機１の
後で脱水ケーキに焼却灰を投入してもよい。この場合
は、脱水ケーキと焼却灰を混合、攪拌する装置を設ける
ことが好ましい。あるいは、焼却炉に直接、必要な量の
焼却灰を投入してもよい。In the above description, the apparatus and the method for putting incinerated ash into sludge before the dewatering machine 1 have been described. However, the dewatered cake is provided after the dewatering machine 1 via a line L6 'shown by a dotted line in FIG. The incineration ash may be put into the furnace. In this case, it is preferable to provide a device for mixing and stirring the dewatered cake and the incinerated ash. Alternatively, the required amount of incineration ash may be directly charged into the incinerator.
【００２７】[0027]
【発明の効果】以上、説明したように、本発明に係る汚
泥処理方法及び装置によれば、汚泥あるいは脱水ケーキ
に焼却灰を混合してその発熱量を調整しているので、可
燃分の多い汚泥を処理する場合でも、炉内温度を低く抑
えることができる。また、排ガス量が増加することがな
いので、後続の排ガス処理設備が大型化することがな
く、コンパクト化できる。As described above, according to the sludge treatment method and apparatus according to the present invention, since the amount of heat generated is adjusted by mixing incineration ash with sludge or dewatered cake, the amount of combustibles is large. Even when treating sludge, the furnace temperature can be kept low. In addition, since the amount of exhaust gas does not increase, the size of the subsequent exhaust gas treatment equipment can be reduced without increasing the size.
【００２８】さらに、脱水前の汚泥に焼却灰を添加すれ
ば、脱水効率が向上して好ましい。Further, it is preferable to add incineration ash to the sludge before dewatering because the dewatering efficiency is improved.
【図１】本発明に係る汚泥処理装置の全体フロー図であ
る。FIG. 1 is an overall flowchart of a sludge treatment apparatus according to the present invention.
【図２】図１の装置における物質収支を示している。FIG. 2 shows the material balance in the device of FIG.
【図３】循環流動層式焼却炉において投入された汚泥の
灰分、含水率に対する炉頂温度を示す線図である。FIG. 3 is a diagram showing furnace top temperature with respect to ash content and water content of sludge fed into a circulating fluidized bed incinerator.
１…脱水機、２…焼却炉、３…排ガス処理設備、４…煙
突、５…灰回収設備、Ｌ１〜Ｌ６…ライン。DESCRIPTION OF SYMBOLS 1 ... Dehydrator, 2 ... Incinerator, 3 ... Exhaust gas treatment equipment, 4 ... Chimney, 5 ... Ash recovery equipment, L1-L6 ... Line.
フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｆ２３Ｇ 7/04 ＺＡＢ Ｆ２３Ｇ 7/04 ＺＡＢ ６０３ ６０３Ａ ６０３Ｚ Ｆ２３Ｋ 1/00 Ｆ２３Ｋ 1/00 Ｚ Ｆターム(参考） 3K061 AB01 AC02 AC03 BA02 BA04 BA10 DA03 DA04 DA11 3K065 AB01 AC02 AC03 BA02 BA04 BA05 CA03 CA04 CA18 4D059 AA03 BB13 BE08 BE16 BE38 BF20 CA06 CA14 DA64 EA01 EA20 EB20 Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat II (reference) F23G 7/04 ZAB F23G 7/04 ZAB 603 603A 603Z F23K 1/00 F23K 1/00 Z F term (reference) 3K061 AB01 AC02 AC03 BA02 BA04 BA10 DA03 DA04 DA11 3K065 AB01 AC02 AC03 BA02 BA04 BA05 CA03 CA04 CA18 4D059 AA03 BB13 BE08 BE16 BE38 BF20 CA06 CA14 DA64 EA01 EA20 EB20
Claims (8)
程と、前記脱水ケーキを焼却炉で焼却処理する焼却工程
とを備えている汚泥処理方法において、 前記汚泥あるいは前記脱水ケーキと焼却処理後の焼却灰
を混合して焼却炉に投入される前記脱水ケーキの発熱量
を調整する調整工程をさらに備えていることを特徴とす
る汚泥処理方法。1. A sludge treatment method comprising: a dewatering step of dewatering sludge to form a dewatered cake; and an incineration step of incinerating the dewatered cake in an incinerator. A sludge treatment method, further comprising an adjusting step of adjusting the calorific value of the dewatered cake to be mixed into the incinerator by mixing the incinerated ash.
ことを特徴とする請求項１記載の汚泥処理方法。2. The sludge treatment method according to claim 1, wherein the adjusting step is performed before the dewatering step.
に行うことを特徴とする請求項１記載の汚泥処理方法。3. The sludge treatment method according to claim 1, wherein the adjusting step is performed between the dewatering step and the incineration step.
記脱水ケーキの含水率を基にして、前記焼却炉の温度が
目標温度となるよう前記焼却灰の混合割合を調整するこ
とにより脱水ケーキの発熱量を調整することを特徴とす
る請求項１〜３のいずれかに記載の汚泥処理方法。4. The dehydrating step includes adjusting a mixing ratio of the incinerated ash based on a temperature of the incinerator and a moisture content of the dewatered cake so that a temperature of the incinerator becomes a target temperature. The sludge treatment method according to any one of claims 1 to 3, wherein the calorific value of the cake is adjusted.
と、前記脱水ケーキを焼却処理する焼却炉とを備えてい
る汚泥処理装置において、 前記汚泥あるいは前記脱水ケーキに焼却処理後の焼却灰
を投入して混合する投入機と、 前記投入機による投入量を前記脱水ケーキの発熱量に応
じて調整する制御装置と、 をさらに備えていることを特徴とする汚泥処理装置。5. A sludge treatment apparatus comprising: a dehydrator for dewatering sludge to form a dewatered cake; and an incinerator for incinerating the dewatered cake, wherein the incineration ash after incineration of the sludge or the dewatered cake is provided. A sludge treatment apparatus, further comprising: a throwing machine for feeding and mixing, and a control device that adjusts a throwing amount by the throwing machine according to a calorific value of the dewatered cake.
されていることを特徴とする請求項５記載の汚泥処理装
置。6. The sludge treatment apparatus according to claim 5, wherein the charging machine is disposed before the dewatering machine.
の間に配置されていることを特徴とする請求項５記載の
汚泥処理装置。7. The sludge treatment apparatus according to claim 5, wherein the charging device is disposed between the dehydrator and the incinerator.
と前記脱水ケーキの含水率を基にして前記焼却炉の炉内
温度が目標温度となるよう前記焼却灰の投入量調整を行
なうことを特徴とする請求項５〜７のいずれかに記載の
汚泥処理装置。8. The controller according to claim 1, wherein the controller adjusts the amount of the incinerated ash based on a temperature in the incinerator and a moisture content of the dewatered cake so that the temperature in the incinerator reaches a target temperature. The sludge treatment apparatus according to any one of claims 5 to 7, wherein
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02404699A JP3678596B2 (en) | 1999-02-01 | 1999-02-01 | Sludge treatment method and apparatus |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02404699A JP3678596B2 (en) | 1999-02-01 | 1999-02-01 | Sludge treatment method and apparatus |
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| Publication Number | Publication Date |
|---|---|
| JP2000218292A true JP2000218292A (en) | 2000-08-08 |
| JP3678596B2 JP3678596B2 (en) | 2005-08-03 |
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ID=12127548
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP02404699A Expired - Fee Related JP3678596B2 (en) | 1999-02-01 | 1999-02-01 | Sludge treatment method and apparatus |
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