JPS6239325B2 - - Google Patents
Info
- Publication number
- JPS6239325B2 JPS6239325B2 JP58069240A JP6924083A JPS6239325B2 JP S6239325 B2 JPS6239325 B2 JP S6239325B2 JP 58069240 A JP58069240 A JP 58069240A JP 6924083 A JP6924083 A JP 6924083A JP S6239325 B2 JPS6239325 B2 JP S6239325B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- oxygen concentration
- flow rate
- air
- signal
- 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
Links
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 51
- 239000001301 oxygen Substances 0.000 claims description 51
- 229910052760 oxygen Inorganic materials 0.000 claims description 51
- 238000002485 combustion reaction Methods 0.000 claims description 38
- 239000007789 gas Substances 0.000 claims description 24
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 73
- 238000000034 method Methods 0.000 description 13
- 239000000463 material Substances 0.000 description 10
- 239000010802 sludge Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- 229910017464 nitrogen compound Inorganic materials 0.000 description 2
- 150000002830 nitrogen compounds Chemical class 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N5/00—Systems for controlling combustion
- F23N5/003—Systems for controlling combustion using detectors sensitive to combustion gas properties
- F23N5/006—Systems for controlling combustion using detectors sensitive to combustion gas properties the detector being sensitive to oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N1/00—Regulating fuel supply
- F23N1/02—Regulating fuel supply conjointly with air supply
- F23N1/022—Regulating fuel supply conjointly with air supply using electronic means
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N2237/00—Controlling
- F23N2237/16—Controlling secondary air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N2237/00—Controlling
- F23N2237/18—Controlling fluidized bed burners
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N5/00—Systems for controlling combustion
- F23N5/18—Systems for controlling combustion using detectors sensitive to rate of flow of air or fuel
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Regulation And Control Of Combustion (AREA)
- Incineration Of Waste (AREA)
Description
【発明の詳細な説明】
本発明は流動床燃焼炉に関し、特に一次空気量
と二次空気量とを適切な値に制御して、排ガス中
の窒素酸化物NOxの発生を抑制し、かつ完全燃
焼を行うための流動床燃焼炉に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a fluidized bed combustion furnace, and in particular controls the amount of primary air and the amount of secondary air to appropriate values to suppress the generation of nitrogen oxides (NOx) in exhaust gas and to completely This invention relates to a fluidized bed combustion furnace for combustion.
流動床燃焼は、空気分散機構上に砂などを充填
し、下方から空気を吹き込んで流動化させた炉床
において、油、石炭、ごみ、汚泥或いは各種廃棄
物を700〜900℃前後の低温で燃焼させるものであ
り、通常の石炭ボイラや石油ボイラの燃焼温度
（約1300℃以上）よりも低温で燃焼するためサー
マル窒素酸化物の発生量が極めて少ない燃焼方法
とされている。しかし被焼却物中に含まれている
窒素化合物による窒素酸化物NOxの発生につい
ては何らかの対策が望まれていた。 Fluidized bed combustion involves burning oil, coal, garbage, sludge, or various wastes at a low temperature of around 700 to 900 degrees Celsius in a hearth that is made by filling an air dispersion mechanism with sand, etc., and fluidizing it by blowing air in from below. It is a combustion method that generates very little thermal nitrogen oxide because it burns at a lower temperature than the combustion temperature of normal coal and oil boilers (approximately 1,300 degrees Celsius or higher). However, some kind of countermeasure has been desired for the generation of nitrogen oxides (NOx) caused by nitrogen compounds contained in the incinerated materials.
ここで従来の流動床燃焼における燃料の窒素酸
化物の低減方法について概説すると、例えば特公
昭55−24005号公報に開示された方法では、流動
床焼却炉へ供給する空気を一次空気と二次空気と
に分割し、炉床に供給される一次空気の量を汚泥
プラス補助燃料の燃焼に必要な理論空気量の１倍
未満となるようにし、流動床表面における雰囲気
を還元性となし、さらに流動床上方のフリーボー
ドに供給される二次空気によつて完全燃焼を行う
ものである。この方法によれば流動床上部の雰囲
気が還元性に維持され、その領域で熱分解する被
焼却物中の窒素化合物からの窒素分は窒素酸化物
NOxとはならず、かなりの窒素酸化物NOxが発
生するのを抑制する効果があるものとされてい
る。しかし、その方法は同公報にも記載されてい
るように、汚泥の流動床燃焼にしか適用できない
ものである。即ち、流動床へ供給される被焼却物
を燃焼するに必要な理論空気量が変化すると、一
次空気の量が過剰になることがあるからである。
従つて流動床への供給量が極めて安定して、かつ
その成分も一定である汚泥の焼却にしか適用でき
ないものとされている。また特公昭55−24005号
公報記載の方法の上述の欠点を解消するため、特
公昭47−5790号公報では特公昭55−24005号公報
の方法の想定し得る最も極端な状況の下で流動床
燃焼を行つている。即ち一次空気の量を流動床が
適切な流動化を行い得る最低の空気量とし、完全
燃焼に必要な残余の空気量を二次空気としてフリ
ーボードへ供給するものである。流動床燃焼であ
る以上一次空気量と二次空気量との関係だけで、
この特公昭47−5790号公報の方法以上に窒素酸化
物NOxの低減効果を得ることは難しい。しかし
一般に燃焼炉は窒素酸化物NOxの発生量だけに
着目して運転されるものではなく、単に物を燃焼
するだけの焼却炉であつても単位時間当りに所定
の量だけの物を焼却処理しなければならないもの
であるし、またボイラや温水熱交換器が付設され
た焼却設備にあつては、ボイラや温水熱交換器の
負荷が要求するだけの物を燃焼しなければならな
いものである。従つて特公昭47−5790号公報の方
法をそのまま現状の流動床燃焼炉に適用するには
限界がある。 To give an overview of conventional methods for reducing nitrogen oxides in fuel in fluidized bed combustion, for example, in the method disclosed in Japanese Patent Publication No. 55-24005, the air supplied to the fluidized bed incinerator is mixed with primary air and secondary air. The amount of primary air supplied to the hearth is less than 1 times the theoretical air amount required for combustion of sludge plus auxiliary fuel, the atmosphere at the surface of the fluidized bed is reduced, and Complete combustion is achieved by secondary air supplied to the freeboard above the floor. According to this method, the atmosphere at the top of the fluidized bed is maintained in a reducing state, and the nitrogen content from the nitrogen compounds in the incinerated material that thermally decomposes in that area is converted into nitrogen oxides.
It does not become NOx, but is said to have the effect of suppressing the generation of a considerable amount of nitrogen oxide NOx. However, as described in the same publication, this method can only be applied to fluidized bed combustion of sludge. That is, if the theoretical amount of air required to burn the material to be incinerated supplied to the fluidized bed changes, the amount of primary air may become excessive.
Therefore, it is said that this method can only be applied to the incineration of sludge in which the amount of supply to the fluidized bed is extremely stable and the components thereof are constant. In addition, in order to eliminate the above-mentioned drawbacks of the method described in Japanese Patent Publication No. 55-24005, Japanese Patent Publication No. 47-5790 describes the method of Japanese Patent Publication No. 55-24005 using a fluidized bed under the most extreme conditions imaginable. It is burning. That is, the amount of primary air is set to the minimum amount that allows the fluidized bed to perform appropriate fluidization, and the remaining amount of air necessary for complete combustion is supplied to the freeboard as secondary air. Since it is fluidized bed combustion, just the relationship between the primary air amount and the secondary air amount,
It is difficult to obtain a greater effect of reducing nitrogen oxide NOx than the method disclosed in Japanese Patent Publication No. 47-5790. However, in general, combustion furnaces are not operated with a focus only on the amount of nitrogen oxides (NOx) produced; even if the incinerator simply burns materials, it incinerates only a predetermined amount of materials per unit time. In addition, in the case of incineration equipment equipped with a boiler or hot water heat exchanger, it is necessary to burn as much material as the load of the boiler or hot water heat exchanger requires. . Therefore, there are limits to the application of the method disclosed in Japanese Patent Publication No. 47-5790 to current fluidized bed combustion furnaces.
上記の２つの方法の限界を打破する方法とし
て、特公昭58−17366号公報の方法では、流動床
の上部にアンモニアガスを供給することを提案し
ている。確かにこのアンモニアガスを添加する方
法を強力な窒素酸化物NOx低減化方法ではある
が流動床燃焼に際し、常時アンモニアガスを消費
することとなるので、負荷価値が極めて高い場合
の流動床燃焼には採用することができても多くの
場合には採用できないものとされている。本発明
はこのような実情に鑑みてなされたものであつ
て、本発明の流動床燃焼炉は石油、石炭、ごみ、
汚泥或いはさまざまな廃棄物等をどのような状態
であつても窒素酸化物NOxの発生量を抑制して
燃焼し得るものであり、また本発明の流動床燃焼
炉は排ガス中の窒素酸化物NOxのみならず一酸
化炭素ガスCO或いは有視煙の排出を極力低減せ
しめるものである。 As a method to overcome the limitations of the above two methods, the method of Japanese Patent Publication No. 17366/1983 proposes supplying ammonia gas to the upper part of the fluidized bed. It is true that the method of adding ammonia gas is a powerful method for reducing nitrogen oxides and NOx, but since ammonia gas is constantly consumed during fluidized bed combustion, it is not suitable for fluidized bed combustion when the load value is extremely high. Even if it can be adopted, in many cases it cannot be adopted. The present invention has been made in view of these circumstances, and the fluidized bed combustion furnace of the present invention can be used to burn petroleum, coal, garbage,
The fluidized bed combustion furnace of the present invention can burn sludge or various wastes under any condition while suppressing the amount of nitrogen oxides NOx generated. Not only that, but also the emission of carbon monoxide gas CO or visible smoke is reduced as much as possible.
本発明の流動床燃焼炉は基本的には上述の特公
昭55−24005号公報記載の発明と同様に流動床燃
焼炉へ供給する空気を一次空気と二次空気とに分
割することによつて燃料の窒素酸化物NOxの発
生を抑制しようとするものである。 The fluidized bed combustion furnace of the present invention is basically similar to the invention described in Japanese Patent Publication No. 55-24005 mentioned above, by dividing the air supplied to the fluidized bed combustion furnace into primary air and secondary air. This is an attempt to suppress the generation of nitrogen oxides (NOx) in fuel.
本発明は、燃焼用空気を流動床下部から供給す
る一次空気とフリーボードへ供給する二次空気と
に分割して炉内へ供給する流動床燃焼炉におい
て、一次空気の流量を計測する第１の流量計と、
二次空気の流量を計測する第２の流量計と、排ガ
ス中の酸素濃度を計測する酸素濃度計と、該第１
及び第２の流量計と酸素濃度計からの出力信号に
基づいて流動床表面における酸素濃度状態を演算
する第１の演算部と、該第１の演算部から出力さ
れた酸素濃度状態と予め設定された流動床表面に
おける酸素濃度状態との偏差に基づいて一次空気
の流量を調節する操作信号を出力する第１の調節
部と、該酸素濃度計からの出力信号が予め設定さ
れた設定値となるべく二次空気の流量を調節する
操作信号を出力する第２の調節部とを具備する流
動床燃焼炉である。 The present invention provides a fluidized bed combustion furnace in which combustion air is divided into primary air supplied from the lower part of the fluidized bed and secondary air supplied to a freeboard and supplied into the furnace. a flow meter,
a second flow meter that measures the flow rate of secondary air; an oxygen concentration meter that measures the oxygen concentration in the exhaust gas;
and a first calculation unit that calculates the oxygen concentration state at the surface of the fluidized bed based on output signals from the second flowmeter and the oxygen concentration meter, and a preset oxygen concentration state output from the first calculation unit. a first adjusting section that outputs an operation signal for adjusting the flow rate of the primary air based on the deviation from the oxygen concentration state at the surface of the fluidized bed, and the output signal from the oxygen concentration meter is set to a preset value; The present invention is a fluidized bed combustion furnace, preferably comprising a second adjustment section that outputs an operating signal for adjusting the flow rate of secondary air.
次に、図面を用いて本発明の流動床燃焼炉につ
いて具体的に説明する。 Next, the fluidized bed combustion furnace of the present invention will be specifically explained using the drawings.
第１図は本発明の流動床燃焼炉の一実施例を示
す概略図である。流動床燃焼炉の本体１は空気箱
２、流動床３、フリーボード４から成り空気箱２
と流動床３との間には空気箱２からの空気を分散
して流動床３へ導く空気分散板５が設けられてい
る。都市ごみ、石炭などの可燃性物質を含有する
被焼却物はスクリユーフイーダ６によつて流動床
３へ供給される。流動床燃焼炉の本体１へ供給さ
れる空気は流動床３の下部から供給される一次空
気とフリーボード４へ供給される二次空気とに分
割されている。一次空気は押込フアン７によつて
上昇された空気が管路８によつて空気箱２へ導入
されることにより供給され、他方二次空気はフア
ン９によつて吸引された空気がフリーボード４の
複数位置に吹出口をもつ管路１０によつてフリー
ボード４へ導入されることにより供給されてい
る。一方排ガスはフリーボード４に開口が接続さ
れた排ガスダクト１１を介して図示しない誘引フ
アンに吸引されて、同様に図示しない煙突から大
気中へ放出される。一次空気の管路８には一次空
気の流量を計測する第１の流量計１２と一次空気
の流量を調節する調節弁１３とが設けられ、同様
に二次空気の管路１０にも二次空気の流量を計測
する第２の流量計１４と二次空気の流量を調節す
る調節弁１５が設けられている。さらに排ガスダ
クト１１には排ガス中の酸素濃度を計測する酸素
濃度計１６が設けられている。 FIG. 1 is a schematic diagram showing an embodiment of a fluidized bed combustion furnace of the present invention. The main body 1 of the fluidized bed combustion furnace consists of an air box 2, a fluidized bed 3, and a free board 4.
An air distribution plate 5 is provided between the air box 2 and the fluidized bed 3 to disperse the air from the air box 2 and guide it to the fluidized bed 3. The materials to be incinerated containing combustible materials such as municipal waste and coal are supplied to the fluidized bed 3 by a screw feeder 6 . The air supplied to the main body 1 of the fluidized bed combustion furnace is divided into primary air supplied from the lower part of the fluidized bed 3 and secondary air supplied to the freeboard 4. The primary air is supplied by the air raised by the push-in fan 7 and introduced into the air box 2 through the conduit 8, while the secondary air is supplied by the air sucked by the fan 9 into the freeboard 4. The air is supplied by being introduced into the freeboard 4 through a conduit 10 having outlets at a plurality of locations. On the other hand, the exhaust gas is sucked into an induction fan (not shown) through an exhaust gas duct 11 having an opening connected to the freeboard 4, and is discharged into the atmosphere from a chimney (also not shown). The primary air conduit 8 is provided with a first flow meter 12 for measuring the flow rate of the primary air and a control valve 13 for regulating the flow rate of the primary air. A second flow meter 14 that measures the flow rate of air and a control valve 15 that adjusts the flow rate of secondary air are provided. Further, the exhaust gas duct 11 is provided with an oxygen concentration meter 16 that measures the oxygen concentration in the exhaust gas.
第１の演算部１７は第１の流量計１２から出力
される一次空気の流量を示す出力信号S1と、第２
の流量計１４から出力される二次空気の流量を示
す出力信号S2と、酸素濃度計１６から出力される
排ガス中の酸素濃度を示す出力信号S3とを入力信
号として、流動床３の表面１８における酸素濃度
状態を演算によつて求めるものである。この演算
部１７における演算は、出力信号S1によつて特定
される一次空気の流量をQ1（Ｎm3）、出力信号S2
によつて特定される二次空気の流量をQ2（Ｎ
m3）及び出力信号S3によつて特定される排ガス中
の酸素濃度をＸ（％）とすれば、
Ｙ＝｛（Q1＋Q2）・Ｘ−21・Q2｝／Q1 ……(1)
なる演算を実行するものであつて、上記(1)式によ
つて求められる演算値Ｙは流動床３の表面１８に
おける酸素濃度状態を示すものである。即ちＹ＝
０であれば一次空気の供給量が理論空気量に等し
いこととなり、Ｙが正の値であれば、一次空気の
供給量が理論空気量よりも大きいことを示し、ま
たＹが負の値であれば一次空気の供給量が理論空
気量よりも小さいことを示すものである。そし
て、Ｙの絶対値の大小はそれぞれの度合の大小に
対応するものである。演算部１７は、このように
して得られる流動床３の表面１８における酸素濃
度状態を示す演算値Ｙを出力信号S4として出力す
るものである。 The first calculation unit 17 outputs an output signal S1 indicating the flow rate of primary air output from the first flowmeter 12, and a second
The output signal S 2 indicating the flow rate of secondary air output from the flow meter 14 of the fluidized bed 3 and the output signal S 3 indicating the oxygen concentration in the exhaust gas output from the oxygen concentration meter 16 are used as input signals. The oxygen concentration state at the surface 18 is determined by calculation. The calculation in this calculation unit 17 calculates the primary air flow rate specified by the output signal S 1 to Q 1 (Nm 3 ), and the output signal S 2
The secondary air flow rate specified by Q 2 (N
m 3 ) and the oxygen concentration in the exhaust gas specified by the output signal S 3 is X (%), then Y = {(Q 1 + Q 2 )・X−21・Q 2 }/Q 1 ... (1), and the calculated value Y determined by the above equation (1) indicates the oxygen concentration state at the surface 18 of the fluidized bed 3. That is, Y=
If it is 0, it means that the primary air supply amount is equal to the theoretical air amount, if Y is a positive value, it means that the primary air supply amount is larger than the theoretical air amount, and if Y is a negative value, it means that the primary air supply amount is greater than the theoretical air amount. If so, it indicates that the supply amount of primary air is smaller than the theoretical air amount. The magnitude of the absolute value of Y corresponds to the magnitude of each degree. The calculation section 17 outputs the calculated value Y indicating the oxygen concentration state at the surface 18 of the fluidized bed 3 obtained in this manner as an output signal S4 .
第１の調節部１９は、第１の演算部１７からの
出力信号S4に基づいて一次空気の流量を制御する
ための操作信号を出力する機能を有するものであ
つて、炉床部酸素濃度調節計１９ａ、制御幅制限
演算器１９ｂ、一次空気流量基準設定器１９ｃ及
び一次空気流量調節計１９ｄとから成るものであ
る。炉床部酸素濃度調節計１９ａは、予め設定さ
れた流動床３の表面１８における酸素濃度状態
Y0と演算部１７からの出力信号S4によつて特定
される酸素濃度状態Ｙとの偏差ΔＹ（ΔＹ＝Y0
−Ｙ）が「０」となるように出力信号S5を出力す
る調節計である。また制御幅制限演算器１９ｂは
信号S5と、一次空気流量基準設定器１９ｃに予め
設定された基準一次空気流量Q0に対応する信号
S6とを入力し、次の式(2)の演算を行い信号S7を出
力するものである。 The first adjustment section 19 has a function of outputting an operation signal for controlling the flow rate of primary air based on the output signal S4 from the first calculation section 17, and has a function of outputting an operation signal for controlling the flow rate of the primary air. It consists of a controller 19a, a control width limit calculator 19b, a primary air flow rate reference setting device 19c, and a primary air flow rate controller 19d. The hearth oxygen concentration controller 19a monitors a preset oxygen concentration state at the surface 18 of the fluidized bed 3.
Deviation ΔY (ΔY= Y 0
This is a controller that outputs an output signal S5 so that -Y) becomes "0". The control width limit calculator 19b also outputs a signal S5 and a signal corresponding to the reference primary air flow rate Q0 preset in the primary air flow rate reference setting device 19c.
S6 is input, the following equation (2) is calculated, and a signal S7 is output.
S7＝S6＋２α（S5−0.5） ……(2)
ここでαは、砂の流動化に必要な最低流量
（Gmf）を確保し、制御不調或いは酸素濃度計不
調時において、プラントの暴走を防ぐための基準
設定値信号S6に対する許容幅である。 S 7 = S 6 + 2α (S 5 -0.5) ... (2) Here, α is the minimum flow rate (Gmf) required for sand fluidization, and the plant's flow rate in the event of control failure or oxygen concentration meter malfunction. This is the allowable range for the reference set value signal S6 to prevent runaway.
このことを第２図によつて説明すれば、信号S5
の０から１までに対応して信号S7が信号S6を基準
にして±αの範囲で変化するものである。そして
この信号S7の下限値は（S6−α）で規定されるも
のである。前記最低流量（Gmf）に相当する値以
上に確保されているものである。さらに一次空気
流量調節計１９ｄは前記信号S7を設定値とし、第
１の流量計１２からの信号S1を入力し、信号S1が
信号S7に等しくなるように、一次空気流量を制御
する調節弁１３を操作する信号S8を出力する調節
計である。 To explain this using FIG. 2, the signal S 5
The signal S 7 changes within a range of ±α with respect to the signal S 6 from 0 to 1. The lower limit value of this signal S7 is defined by ( S6 -α). A value equal to or higher than the minimum flow rate (Gmf) is ensured. Further, the primary air flow rate controller 19d uses the signal S7 as a set value, inputs the signal S1 from the first flowmeter 12, and controls the primary air flow rate so that the signal S1 becomes equal to the signal S7 . This is a controller that outputs a signal S8 to operate the control valve 13.
第２の調節部２０は排ガス酸素濃度調節計２０
ａと二次空気流量調節計２０ｂとから成り、酸素
濃度計１６からの出力信号S3を入力し、排ガス中
の酸素濃度を予め設定された値となるように二次
空気流量を調節するための操作信号をを出力する
調節計である。この第２の調節部２０において、
先ず信号S3が排ガス酸素濃度調節計２０ａへ入力
され、予め設定された排ガス中の酸素濃度値に対
応する設定値SV0に信号S3が等しくなるように排
ガス酸素濃度調節計２０ａから信号S9が出力され
る。二次空気流量調節計２０ｂは排ガス酸素濃度
調節計２０ａからの信号S9を設定値として入力
し、さらに第２の流量計１４からの信号S2を入力
し、信号S2が信号S9と等しくなるように二次空気
流量を制御する調節弁１５を操作する信号S10を
出力する調節計である。なお前記炉床部酸素濃度
調節計１９ａ及び排ガス酸素濃度調節計２０ａに
おける制御動作としては比例積分微分（PID）動
作を行うのがよく、また一次空気流量調節計１９
ｄと二次空気流量調節計２０ｂとの制御動作は流
動床燃焼設備にボイラが付設されている場合には
比例（Ｐ）動作がよく、他方ボイラが付設されて
いない場合には比例積分（PI）動作とするのが望
ましい。第１図に示した本発明の流動床燃焼炉で
は、流動床３の表面１８における酸素濃度状態を
予め設定した酸素濃度状態に制御できるものであ
り、即ちこの予め設定する酸素濃度状態を環元性
の範囲にしておけば二次空気からの酸素の影響を
受ける直前での燃焼ガス（近似的には流動床の表
面での燃焼ガス）の雰囲気を常時還元性に維持す
べく一次空気の供給量が調節されるものである。
従つて流動床３で発生する窒素酸化物NOxは一
酸化炭素ガスCOの作用によつて還元される排ガ
ス中の窒素酸化物NOxの量は著しく低減される
こととなる。 The second adjustment section 20 is an exhaust gas oxygen concentration controller 20
a and a secondary air flow rate controller 20b, which inputs the output signal S3 from the oxygen concentration meter 16 and adjusts the secondary air flow rate so that the oxygen concentration in the exhaust gas becomes a preset value. This is a controller that outputs operation signals. In this second adjustment section 20,
First, the signal S3 is input to the exhaust gas oxygen concentration controller 20a, and the signal S3 is inputted from the exhaust gas oxygen concentration controller 20a so that the signal S3 becomes equal to the set value SV0 corresponding to the preset oxygen concentration value in the exhaust gas. 9 is output. The secondary air flow rate controller 20b inputs the signal S 9 from the exhaust gas oxygen concentration controller 20a as a set value, and further inputs the signal S 2 from the second flow meter 14, so that the signal S 2 is the same as the signal S 9 . This is a controller that outputs a signal S10 that operates a control valve 15 that controls the secondary air flow rate so that the secondary air flow rate becomes equal. The control operations in the hearth oxygen concentration controller 19a and the exhaust gas oxygen concentration controller 20a are preferably proportional-integral-differential (PID) operations, and the primary air flow rate controller 19
d and the secondary air flow rate controller 20b, proportional (P) operation is best when a boiler is attached to the fluidized bed combustion equipment, whereas proportional integral (PI) operation is preferred when a boiler is not attached. ) is preferable. In the fluidized bed combustion furnace of the present invention shown in FIG. 1, the oxygen concentration state at the surface 18 of the fluidized bed 3 can be controlled to a preset oxygen concentration state. If the temperature range is within the range of The amount is regulated.
Therefore, the nitrogen oxides NOx generated in the fluidized bed 3 are reduced by the action of the carbon monoxide gas CO, and the amount of nitrogen oxides NOx in the exhaust gas is significantly reduced.
また本発明では第２の調節部２０によつて排ガ
ス中の酸素濃度が一定の値となるべく、二次空気
の流量を制御するものであるから燃焼ガス中の可
燃成分を効果的に燃焼し、有視煙の発生を抑制す
ることとなる。 Furthermore, in the present invention, since the flow rate of the secondary air is controlled by the second adjustment section 20 so that the oxygen concentration in the exhaust gas becomes a constant value, the combustible components in the combustion gas are effectively combusted. This will suppress the generation of visible smoke.
本発明は、燃焼用空気を流動床下部から供給す
る一次空気とフリーボードへ供給する二次空気と
に分割して炉内へ供給する流動床燃焼炉におい
て、一次空気の流量を計測する第１の流量計と、
二次空気の流量を計測する第２の流量計と、排ガ
ス中の酸素濃度を計測する酸素濃度計と、該第１
及び第２の流量計と酸素濃度計からの出力信号に
基づいて流動床表面における酸素濃度状態を演算
する第１の演算部と、該第１の演算部から出力さ
れた酸素濃度状態と予め設定された流動床表面に
おける酸素濃度状態との偏差に基づいて一次空気
の流量を調節する操作信号を出力する第１の調節
部と、該酸素濃度計からの出力信号が予め設定さ
れた設定値となるべく二次空気の流量を調節する
操作信号を出力する第２の調節部とを具備する流
動床燃焼炉である。 The present invention provides a fluidized bed combustion furnace in which combustion air is divided into primary air supplied from the lower part of the fluidized bed and secondary air supplied to a freeboard and supplied into the furnace. a flow meter,
a second flow meter that measures the flow rate of secondary air; an oxygen concentration meter that measures the oxygen concentration in the exhaust gas;
and a first calculation unit that calculates the oxygen concentration state at the surface of the fluidized bed based on output signals from the second flowmeter and the oxygen concentration meter, and a preset oxygen concentration state output from the first calculation unit. a first adjusting section that outputs an operation signal for adjusting the flow rate of the primary air based on the deviation from the oxygen concentration state at the surface of the fluidized bed, and the output signal from the oxygen concentration meter is set to a preset value; The present invention is a fluidized bed combustion furnace, preferably comprising a second adjustment section that outputs an operating signal for adjusting the flow rate of secondary air.
従つて本発明の流動床燃焼炉によれば、流動床
部に高価な酸素濃度計を設けることなく流動床表
面の酸素濃度状態を把握し、所定の酸素濃度状態
に維持できるから排ガス中の窒素酸化物NOxの
量を低減することができる。さらに排ガス中の酸
素濃度を独立して制御しているので、常時有視煙
の発生を抑止できる完全燃焼運転をすることが可
能となる。 Therefore, according to the fluidized bed combustion furnace of the present invention, the oxygen concentration state on the surface of the fluidized bed can be determined without installing an expensive oxygen concentration meter in the fluidized bed section, and the oxygen concentration state can be maintained at a predetermined oxygen concentration state. The amount of oxide NOx can be reduced. Furthermore, since the oxygen concentration in the exhaust gas is controlled independently, it is possible to perform complete combustion operation that can suppress the generation of visible smoke at all times.
特に従来の低窒素酸化物NOx流動床燃焼炉で
は前記の如く汚泥のように極めて均質な被焼却物
しか適用できなかつたものが、本発明にあつて
は、都市ごみのように発熱量が不均質でかつその
変化が予測し得ないものであつても、窒素酸化物
NOxの発生を抑制しつつ燃焼できるものであ
る。 In particular, in the conventional low nitrogen oxide NOx fluidized bed combustion furnace, only extremely homogeneous incineration materials such as sludge can be used, but in the present invention, it can be applied to incineration materials that have a low calorific value such as municipal waste. Nitrogen oxides, even if they are homogeneous and their changes are unpredictable.
It can burn while suppressing the generation of NOx.
第１図は本発明の実施例である流動床燃焼炉の
概略図であり、第２図は調節計の作動の説明図で
ある。
１……炉本体、２……空気箱、３……流動床、
４……フリーボード、５……空気分散板、６……
スクリユーフイーダ、７……押込フアン、８……
管路、９……フアン、１０……管路、１１……排
ガスダクト、１２……第１の流量計、１３……調
節弁、１４……第２の流量計、１５……調節弁、
１６……酸素濃度計、１７……第１の演算部、１
８……流動床の表面、１９……第１の調節部、１
９ａ……炉床部酸素濃度調節計、１９ｂ……制御
幅制限演算器、１９ｃ……一次空気流量基準設定
器、１９ｄ……一次空気流量調節計、２０……第
２の調節部、２０ａ……排ガス酸素濃度調節計、
２０ｂ……二次空気流量調節計、S1〜S10……信
号。
FIG. 1 is a schematic diagram of a fluidized bed combustion furnace according to an embodiment of the present invention, and FIG. 2 is an explanatory diagram of the operation of a controller. 1...furnace body, 2...air box, 3...fluidized bed,
4...Free board, 5...Air dispersion plate, 6...
Screw feeder, 7... push fan, 8...
Pipe line, 9... Fan, 10... Pipe line, 11... Exhaust gas duct, 12... First flow meter, 13... Control valve, 14... Second flow meter, 15... Control valve,
16...Oxygen concentration meter, 17...First calculation section, 1
8...Surface of the fluidized bed, 19...First adjustment section, 1
9a...Heart oxygen concentration controller, 19b...Control width limit calculator, 19c...Primary air flow rate reference setter, 19d...Primary air flow rate controller, 20...Second adjustment section, 20a... ...Exhaust gas oxygen concentration controller,
20b...Secondary air flow rate controller, S1 to S10 ...Signal.
Claims (1)
気とフリーボードへ供給する二次空気とに分割し
て炉内へ供給する流動床燃焼炉において、一次空
気の流量を計測する第１の流量計と、二次空気の
流量を計測する第２の流量計と、排ガス中の酸素
濃度を計測する酸素濃度計と、該第１及び第２の
流量計と酸素濃度計からの出力信号に基づいて流
動床表面における酸素濃度状態を演算する第１の
演算部と、該第１の演算部から出力された酸素濃
度状態と予め設定された流動床表面における酸素
濃度状態との偏差に基づいて一次空気の流量を調
節する操作信号を出力する第１の調節部と、該酸
素濃度計からの出力信号が予め設定された設定値
となるべく二次空気の流量を調節する操作信号を
出力する第２の調節部とを具備することを特徴と
する流動床燃焼炉。1. A first flowmeter that measures the flow rate of primary air in a fluidized bed combustion furnace that divides combustion air into primary air supplied from the lower part of the fluidized bed and secondary air supplied to the freeboard and supplies it into the furnace. , a second flow meter that measures the flow rate of the secondary air, an oxygen concentration meter that measures the oxygen concentration in the exhaust gas, and based on output signals from the first and second flow meters and the oxygen concentration meter. a first calculation unit that calculates the oxygen concentration state on the surface of the fluidized bed; and a first calculation unit that calculates the oxygen concentration state on the surface of the fluidized bed; and a first adjustment section that outputs an operation signal for adjusting the flow rate of the secondary air, and a second adjustment section that outputs an operation signal for adjusting the flow rate of the secondary air so that the output signal from the oxygen concentration meter becomes a preset value. A fluidized bed combustion furnace characterized by comprising a control section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58069240A JPS59195019A (en) | 1983-04-21 | 1983-04-21 | Fluidized-bed type combustion furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58069240A JPS59195019A (en) | 1983-04-21 | 1983-04-21 | Fluidized-bed type combustion furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59195019A JPS59195019A (en) | 1984-11-06 |
| JPS6239325B2 true JPS6239325B2 (en) | 1987-08-22 |
Family
ID=13397027
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58069240A Granted JPS59195019A (en) | 1983-04-21 | 1983-04-21 | Fluidized-bed type combustion furnace |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59195019A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0328021U (en) * | 1989-07-28 | 1991-03-20 | ||
| JP2856917B2 (en) * | 1995-01-17 | 1999-02-10 | エルディティ ゲーエムベーハー ウント シーオー．レーザー−ディスプレー−テクノロギー カーゲー | amplifier |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2070688C1 (en) * | 1987-05-01 | 1996-12-20 | Ибара Корпорейшн | Method of combustion control in furnace for burning waste in fluidized bed |
| US5020451A (en) * | 1989-10-05 | 1991-06-04 | Ishikawajima-Harima Heavy Industries Co., Ltd. | Fluidized-bed combustion furnace |
| JP2530502B2 (en) * | 1989-11-08 | 1996-09-04 | 川崎重工業株式会社 | Highly efficient combustion method and apparatus for fluidized bed furnace |
| JP2560005Y2 (en) * | 1991-11-08 | 1998-01-21 | 石川島播磨重工業株式会社 | Pressurized fluidized bed boiler |
| JP2748214B2 (en) * | 1993-05-11 | 1998-05-06 | 川崎重工業株式会社 | Combustion control method in fluidized bed furnace |
| ES2540702B1 (en) * | 2012-09-11 | 2016-05-12 | Fundacion Cidaut | SOLID FUEL BOILER |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4979068A (en) * | 1972-12-05 | 1974-07-30 | ||
| JPS5389281A (en) * | 1977-01-14 | 1978-08-05 | Ishigaki Mech Ind | Control of nox emission in fluidized bed incinerator |
| JPS5556514A (en) * | 1978-10-20 | 1980-04-25 | Takuma Co Ltd | Method of automatic combustion control for refuse incinerating furnace |
| JPS5790512A (en) * | 1980-11-26 | 1982-06-05 | Kubota Ltd | Method and device for controlling fusion incinerator |
-
1983
- 1983-04-21 JP JP58069240A patent/JPS59195019A/en active Granted
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4979068A (en) * | 1972-12-05 | 1974-07-30 | ||
| JPS5389281A (en) * | 1977-01-14 | 1978-08-05 | Ishigaki Mech Ind | Control of nox emission in fluidized bed incinerator |
| JPS5556514A (en) * | 1978-10-20 | 1980-04-25 | Takuma Co Ltd | Method of automatic combustion control for refuse incinerating furnace |
| JPS5790512A (en) * | 1980-11-26 | 1982-06-05 | Kubota Ltd | Method and device for controlling fusion incinerator |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0328021U (en) * | 1989-07-28 | 1991-03-20 | ||
| JP2856917B2 (en) * | 1995-01-17 | 1999-02-10 | エルディティ ゲーエムベーハー ウント シーオー．レーザー−ディスプレー−テクノロギー カーゲー | amplifier |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59195019A (en) | 1984-11-06 |
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