JPS58174227A - Method for controlling charging amount of ammonia in denitration apparatus - Google Patents
Method for controlling charging amount of ammonia in denitration apparatusInfo
- Publication number
- JPS58174227A JPS58174227A JP57056047A JP5604782A JPS58174227A JP S58174227 A JPS58174227 A JP S58174227A JP 57056047 A JP57056047 A JP 57056047A JP 5604782 A JP5604782 A JP 5604782A JP S58174227 A JPS58174227 A JP S58174227A
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- amount
- ammonia
- signal
- denitrification
- flow rate
- Prior art date
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Abstract
Description
【発明の詳細な説明】
本発明は排ガス中の窒素酸化物をアンモニア接触還元法
を用いて脱硝する脱硝装置のアンモニア注入量制御方法
に係り、特に負荷変動の激しい燃焼装置に用いて好適な
脱硝装置のアンモニア注入量制御方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an ammonia injection amount control method for a denitrification device that denitrates nitrogen oxides in exhaust gas using an ammonia catalytic reduction method. The present invention relates to a method for controlling the amount of ammonia injected into an apparatus.
排ガス中の窒素酸化物（以下、これをＮＯｘと称す。）
の脱硝方法の一つであるアンモニア接触還元法は、乾式
であることおよび装置が簡単であること等により火力発
電用の大型ボイラなどに多く用いられている。Nitrogen oxides in exhaust gas (hereinafter referred to as NOx)
The ammonia catalytic reduction method, which is one of the denitrification methods, is often used in large boilers for thermal power generation because it is a dry method and the equipment is simple.
この脱硝方法では、その脱硝性能がアンモニアの注入量
に大ぎく依存し【おり、装置を安定して運転するためＫ
はアンモニアの注入量の制御が重要なｉｔ題となってい
る。即ち、アンモニアの注入量が少ないと当然脱硝性能
は低下し、又、アンモニアの注入量が多過ぎるとアンモ
ニアが未反応のまま脱硝装置の触媒層から流出して排ガ
ス中の三酸化硫黄（ＳＯ，）と反応し、後流に設けられ
た空気予熱器に硫安として堆積し、又は白煙の原因とな
る。In this denitrification method, the denitrification performance is highly dependent on the amount of ammonia injected, and in order to operate the equipment stably,
Controlling the amount of ammonia injected is an important issue. In other words, if the amount of ammonia injected is small, the denitrification performance will naturally decrease, and if the amount of ammonia injected is too large, the ammonia will flow out from the catalyst layer of the denitrification device unreacted, resulting in sulfur trioxide (SO, ) and deposits as ammonium sulfate in the air preheater installed downstream, or causes white smoke.
従来、アンモニア注入量の制御には種々の方法が提案さ
れているが、これらの方法な原理的に別けると次の２つ
の方法に爆着する。Conventionally, various methods have been proposed for controlling the amount of ammonia injection, but these methods can be divided into the following two methods in principle.
（１）脱硝装置入口における排ガスの条件による制御
この方法は、脱硝反応が
ＮＨ，＋ＮＯ＋１／４０□→Ｎｌ＋２／３Ｈ，０の反応
式から明らかなようにアンモニアと一酸化窒素とが等モ
ルで反応することから、排ガス流量や全ＮＯｘ濃度など
から脱硝装置に流入するＮ Ｏ。(1) Control based on exhaust gas conditions at the inlet of the denitrification equipment In this method, ammonia and nitrogen monoxide react in equal moles, as is clear from the reaction formula: NH, +NO + 1/40□→Nl + 2/3H,0. Therefore, NO flowing into the denitrification equipment from the exhaust gas flow rate and total NOx concentration.
量を算出してアンモニアの必要量を決定する方法である
。This method determines the required amount of ammonia by calculating the amount.
（２）脱硝装置出口における排ガスの条件による制御 この方法は、原理的には脱硝装置の出口のＮＯ。(2) Control based on exhaust gas conditions at the outlet of the denitrification equipment In principle, this method uses NO at the outlet of the denitration equipment.
濃度を測定し、これを直接又は脱硝率に変換してアンモ
ニア注入糸にフィードバックさせて注入量を制御しよう
とするものである。The purpose is to control the injection amount by measuring the concentration and feeding it back to the ammonia injection thread either directly or by converting it into a denitrification rate.
上舵（ＩＬ（２）のいずれの方法も、脱硝装置の運転条
件が一定している場合には脱硝性能は安定に維持されて
いる。しかし、例えばボイラの負荷が上昇すると、処理
すべき排ガス量は約２倍、排ガス温度は約５０℃、ＮＯ
，９度は２倍というように大幅に変化し、この変化は数
１０分という短時間内に発生するものであり、このよう
に短時間に大幅な反応条件の変化が生じた場合、前記（
１）の方法では、触媒へのアンモニア吸着量が変化し、
この結果脱硝装置出口のＮＯ，濃度が一時的に＾くなる
現象が発生するという欠点があった。これを第１図（鳳
）、（ｂ）に示す。図（、）は横軸に時間Ｔ、縦軸に負
荷の大きさＬがとっである。又、図（ｂ）は横軸に時間
、縦軸に脱硝装置出口のＮ０ｘＩＩＩＷＩＤがとっであ
る。図（ａ）、（ｂ）の時間軸は揃えて記載されている
。第１図から、負荷の上昇変化が始まると直ちに脱硝装
置出口のＮＯ，濃度が急く高くなり、その後徐々に一定
値戻る。したがって、この間脱硝率が低下すると（・５
欠点が発生する。In both methods of upper rudder (IL (2)), the denitrification performance is maintained stably when the operating conditions of the denitrification equipment are constant. However, for example, when the load on the boiler increases, the exhaust gas to be treated The amount is about double, the exhaust gas temperature is about 50℃, NO
, 9 degrees changes significantly, doubling, and this change occurs within a short period of several tens of minutes.When a significant change in reaction conditions occurs in such a short period of time,
In method 1), the amount of ammonia adsorbed on the catalyst changes,
As a result, there was a drawback in that the NO concentration at the outlet of the denitration equipment temporarily decreased. This is shown in Figure 1 (Otori) and (b). In the figure (,), the horizontal axis represents time T, and the vertical axis represents load size L. In addition, in FIG. 3(b), the horizontal axis represents time, and the vertical axis represents N0xIIIWID at the outlet of the denitrification device. The time axes in Figures (a) and (b) are aligned. From FIG. 1, as soon as the load starts to increase, the NO concentration at the outlet of the denitrification device increases rapidly, and then gradually returns to a constant value. Therefore, if the denitrification rate decreases during this period (・5
Defects occur.
又、前記（２）の方法では、短時間で大幅な変化に対し
て脱硝性能を追従させるためには、前述のフィードバッ
クの量を大きく選定すればよいのであるが、そうすやと
発振現象が発生してアンモニア注入量が一定しないばか
りか、アンモニア注入量がオーバーシュートして大量の
未反応アンモニアが触媒層から流出してしまうという欠
点があった。In addition, in the method (2) above, in order to make the denitrification performance follow large changes in a short time, it is sufficient to select a large amount of feedback, but this will cause the oscillation phenomenon. Not only is the ammonia injection amount not constant, but the ammonia injection amount overshoots and a large amount of unreacted ammonia flows out of the catalyst layer.
本発明の目的は、前記従来方法による欠点を除ｔ、負荷
の変動に伴う急激な反応条件の変化に対する脱硝性能の
追従性が良好であり、かつ、触、媒層から流出する未反
応アンモニアの量を少なくすることができる脱硝装置の
アンモニア注入量の制御方法を提供するにある。It is an object of the present invention to eliminate the drawbacks of the conventional methods, to provide good followability of denitrification performance to rapid changes in reaction conditions due to load fluctuations, and to eliminate unreacted ammonia flowing out from the catalyst and catalyst layers. An object of the present invention is to provide a method for controlling the amount of ammonia injected into a denitrification device, which can reduce the amount of ammonia injected.
この目的を達成するため、本発明は、脱硝装置の出口側
のＮＯ，量をある値に設定しておき、脱硝装置入口側の
ＮＯ，量と前記設定値とで脱硝反応に要するアンモニア
注入量に応じた信号をつくり、この信号に脱硝装置の触
媒に吸着するアンモニアの補充すべき量又は減ずべき量
に応じた信号を加算し、この加算の結果得た信号により
アンモニア注入量の制御を行うよ５Ｋｌたことを特徴と
する。In order to achieve this object, the present invention sets the amount of NO on the outlet side of the denitrification device to a certain value, and the amount of ammonia injection required for the denitrification reaction based on the amount of NO on the inlet side of the denitrification device and the set value. A signal corresponding to the amount of ammonia adsorbed on the catalyst of the denitration equipment is added to this signal, and a signal corresponding to the amount of ammonia that should be reduced is added to the signal, and the amount of ammonia injection is controlled using the signal obtained as a result of this addition. It is characterized by having completed 5Kl.
以下、本発明を図示の実施例に基づいて説明する。Hereinafter, the present invention will be explained based on illustrated embodiments.
ここで、実施例の構成の説明に先立ち、触媒へのアンモ
ニア吸着量について述べる。前述のように、脱硝反応は
アンモニア（ＮＨ，）と−酸化窒素（ＮＯ）との等モル
反応であるため、触媒量を反応がほぼ定置的に進行し得
る緻に選定しておき、脱硝装置に流入するＮ０Ｘｔとこ
の脱硝装置に求められる性能とから算出されるアンモニ
アの必要量を注入する、方法が、未反応のアンモニアの
流出な最小限度に抑えるだめの方法であるといえる。Here, prior to explaining the structure of the example, the amount of ammonia adsorbed on the catalyst will be described. As mentioned above, the denitrification reaction is an equimolar reaction between ammonia (NH, ) and -nitrogen oxide (NO), so the amount of catalyst is carefully selected so that the reaction can proceed almost stationarily, and the denitrification equipment It can be said that the method of injecting the required amount of ammonia calculated from the NOXt flowing into the reactor and the performance required of this denitrification equipment is the best way to minimize the outflow of unreacted ammonia.
そして、このような方法の欠点である応答速度の悪い点
を改善すれば本発明の目的を達成することができる。こ
のような観点から、急激な反応条件の変化における脱硝
率の一時的低下（第１図）が発生する原因な考察し、そ
の原因を除けば応答速度を改善することができるのであ
る。The object of the present invention can be achieved by improving the poor response speed, which is a drawback of such a method. From this point of view, the cause of the temporary decrease in the denitrification rate (Fig. 1) caused by a sudden change in reaction conditions can be considered, and the response speed can be improved by eliminating the cause.
そこで、種々研究の結米紡記の原因は触媒へのアンモニ
ア吸着量に関係することが判明した。第２図は種々の温
度における触媒へのアンモニア吸着量（Ｑ）と脱硝率に
関連する値（Ａ）との関係を示したものである。ここで
、脱硝率に関連する値Ａとは次のような数式で表わされ
る値である。Therefore, various studies have revealed that the cause of rice grain formation is related to the amount of ammonia adsorbed on the catalyst. FIG. 2 shows the relationship between the amount of ammonia adsorbed on the catalyst (Q) and the value related to the denitrification rate (A) at various temperatures. Here, the value A related to the denitrification rate is a value expressed by the following formula.
ドＩ
Ａ ＝ｖ Ｉｎ ｌｘ
ただし、Ｆは排ガス流量、Ｖは触媒量、Ｘは脱鋼車であ
る。I A = v In lx where F is the exhaust gas flow rate, V is the catalyst amount, and X is the steel-free vehicle.
第２図から明らかなように、同一温度においては両者は
比例関係にある。したがって、次式が成立する。As is clear from FIG. 2, there is a proportional relationship between the two at the same temperature. Therefore, the following equation holds.
ただし、Ｋは定数、Ｇ （Ｔ）は温度Ｔの関数である。However, K is a constant and G (T) is a function of temperature T.
この（１）式は、排ガス量Ｆの増加や温度′ｒの低下の
場合、アンモニア吸着量Ｑを増加してやらなければ脱硝
性能は一定に維持できないことを示している。換言すれ
ば、負荷の変動に伴う反応条件の変化に脱硝性能を追従
させるためには、定常の性能を維持するためのアンモニ
ア注入量に上記の増加すべきアンモニア吸着量を追加し
てやればよいということになる。これは、アンモニア吸
着量が過剰である場合も同じであり、その場合はアひ
ンモニア注入量を低減してやればよいことになる１゜以
下、増加についての場合のみ説明する。Equation (1) shows that when the exhaust gas amount F increases or the temperature 'r decreases, the denitrification performance cannot be maintained constant unless the ammonia adsorption amount Q is increased. In other words, in order to make the denitrification performance follow changes in reaction conditions due to changes in load, it is sufficient to add the above amount of ammonia adsorption that should be increased to the amount of ammonia injected to maintain steady performance. become. This also applies when the amount of adsorbed ammonia is excessive, and in that case, only the case of an increase of 1° or less, in which case it is sufficient to reduce the amount of ahimmonia injected, will be explained.
今、アンモニア吸着量の不足分なΔＱとすると、このΔ
Ｑは前記（１）式から次のように表される。Now, if ΔQ is the insufficient amount of ammonia adsorption, then this Δ
Q is expressed as follows from the above equation (1).
ここで、Ｘ、は脱硝率の設定値、Ｘは実測された脱硝率
、Ｃ０は脱硝装置出口のＮＯｘ濃度の設定値、Ｃは実測
された脱硝装置出口のＮＯ，濃度である。Here, X is the set value of the denitrification rate, X is the actually measured denitrification rate, C0 is the set value of the NOx concentration at the outlet of the denitrification device, and C is the actually measured NO concentration at the outlet of the denitrification device.
この（２）、（３）式から、アンモニア吸着量の不足蓋
ΔＱは、脱硝率の設定値Ｘ、と実測値Ｘ。From these equations (2) and (3), the insufficient cap ΔQ of the ammonia adsorption amount is the set value X of the denitrification rate and the actual measured value X.
又は出口のＮＯ，濃度の設定値Ｃ０と実測値Ｃとの比の
対数、排ガス流量および温度により算出することができ
る。Alternatively, it can be calculated using the NO at the outlet, the logarithm of the ratio between the concentration setting value C0 and the actual measurement value C, the exhaust gas flow rate, and the temperature.
したがって、排ガスｆｔ、ｔ、入口のＮＯｘ濃度に基づ
いてアンモニア注入量を制御する入口制御系に上記アン
モニア吸着不足量の追加系を組合せてやれば、反応条件
の急変があってもこれに充分追従してゆくことができる
アンモニア注入量制御を、゛。Therefore, if the above-mentioned additional system for ammonia adsorption deficiency is combined with the inlet control system that controls the ammonia injection amount based on the exhaust gas ft, t, and the NOx concentration at the inlet, even if there is a sudden change in the reaction conditions, it will be able to sufficiently follow it. The amount of ammonia injection can be controlled.
竹い得るということになる。即ち、このようなアンモニ
ア注入量の制御は、反応に必要なアンモニア量と触媒性
能を一定に維持するために必要なアンモニア量とを別々
に制御する構成であるといえる。This means that you can get bamboo. That is, such control of the ammonia injection amount can be said to be a configuration in which the amount of ammonia required for the reaction and the amount of ammonia required to maintain constant catalyst performance are separately controlled.
次に第３図に示す本発明の制御方法を実施するための制
御装置の一実施例について説明する。Next, an embodiment of a control device for carrying out the control method of the present invention shown in FIG. 3 will be described.
図で１は脱硝反応を行５ための脱硝装置、２は脱硝装置
１０入口側の煙道、３は出口側の煙道であり、煙道２に
は脱硝されていない排ガスが、煙道３には脱硝された排
ガスがそれぞれ矢印Ｊ方向に流れる。４は脱硝装置１の
入口側煙道２に注入されるべきアンモニアの供給源、５
はアンモニア供給源４からのアンモニア流量を制御する
制御弁、６はアンモニアの流量検出装置である。制御弁
５はこの制御装置からの出力信号により操作されてアン
モニア注入量を制御する。７は脱硝装置ｌの入口側の排
ガス内のＮＯｘ濃度を分析し、これに応じた信号すを出
力する入口ＮＯｘ分析装置、８は同じく入口側の排ガス
の流量を検出し、これに応じた信号ｆを出力する排ガス
流量検出装置、９は同じく入口側の排ガスの温度を検出
し、これに応じた信号ｔを出力する温度検出装置、１ｏ
は脱硝装置１の出口側の排ガス内のＮＯ，濃度を分析し
、これに応じた信号Ｃを出力する出ロＮＯ，分析装置で
ある。In the figure, 1 is a denitrification device for carrying out the denitrification reaction 5, 2 is a flue on the inlet side of the denitrification device 10, and 3 is a flue on the outlet side. The denitrified exhaust gas flows in the direction of arrow J, respectively. 4 is an ammonia supply source to be injected into the inlet flue 2 of the denitrification device 1;
6 is a control valve that controls the flow rate of ammonia from the ammonia supply source 4, and 6 is an ammonia flow rate detection device. The control valve 5 is operated by an output signal from this control device to control the amount of ammonia injected. 7 is an inlet NOx analyzer that analyzes the NOx concentration in the exhaust gas on the inlet side of the denitrification equipment l and outputs a signal in accordance with this, and 8 also detects the flow rate of exhaust gas in the inlet side and outputs a signal in accordance with this. 9 is an exhaust gas flow rate detection device that outputs f, and 9 is a temperature detection device that also detects the temperature of the exhaust gas on the inlet side and outputs a signal t in accordance with this, 1o
1 is an output NO analyzer that analyzes the NO concentration in the exhaust gas on the outlet side of the denitrification device 1 and outputs a signal C corresponding to the NO concentration.
１１は入口ＮＯｘ分析装ｆｉｌ１７の出力信号すと信号
Ｃ，とな入力して必要な演算を行う演算器である。Reference numeral 11 denotes an arithmetic unit which inputs the output signal of the inlet NOx analyzer fil17 and the signal C, and performs necessary calculations.
ここで、信号Ｃ０は前記（３）式における脱硝装＠１の
出ＩＩ＠Ｎｏｒ＠度の設定値Ｃ０に応じた信号である。Here, the signal C0 is a signal corresponding to the set value C0 of the output II@Nor@degree of the denitrification device@1 in the equation (3).
演算器１１からは脱硝装置１の性能を維持するのに必要
な信号Ｘが出力される。１２は排ガス流量検出装置８か
らの出力信号ｆと演算器１１からの出力信号Ｘとを乗算
する乗算器であり、反応に必要なアンモニア量に応じた
信号ａ、が出力される。１３はある定められた関数を有
する関数発生器であり、温度検出装［９からの信号ｔが
入力されると、これに対応した前記（３）式における値
Ｇ （１’ ）に応じた信号ｇ（ｔ）を出力する。１４
は出ロＮＯ，分析装置１０の出力信号Ｃと前記出口側Ｎ
０ｘｌｌＩｉ度の設定値Ｃ０に応じた信号Ｃ０とを入力
して必要な演算を行う演算器であり、この演算器１４に
より前記（３）式の値１３ が算出され、曹
この普に応じた信号１４−か出力される。１５はＣ・
信号ｆ、信号ｇ （ｔ）、信号ｊ％−Ｅ−１信号ｋを入
Ｃ・
力し、これらを乗算する乗算器である。ここで、信号に
は前記（３）式のに／Ｖに相当する籠に応じた信号であ
る。乗算器１５からは触媒性能を一定に維持するために
必要なアンモニア吸着不足量４Ｑに応じた信号ａ、が出
力される。１６は信号ａ。The arithmetic unit 11 outputs a signal X necessary to maintain the performance of the denitrification device 1. A multiplier 12 multiplies the output signal f from the exhaust gas flow rate detection device 8 and the output signal X from the calculator 11, and outputs a signal a corresponding to the amount of ammonia required for the reaction. Reference numeral 13 denotes a function generator having a certain predetermined function, and when the signal t from the temperature detection device [9 is input, it generates a signal corresponding to the value G (1') in the equation (3) above. Output g(t). 14
is the output side NO, the output signal C of the analyzer 10 and the exit side N
This is an arithmetic unit that performs necessary calculations by inputting a signal C0 corresponding to a set value C0 of 0xllIi degrees, and this arithmetic unit 14 calculates the value 13 of the above formula (3), 14- is output. 15 is a multiplier which inputs the C signal f, the signal g(t), the signal j%-E-1 signal k, and multiplies them. Here, the signal is a signal corresponding to the cage corresponding to /V in the above equation (3). The multiplier 15 outputs a signal a corresponding to the ammonia adsorption deficiency 4Q necessary to maintain the catalyst performance constant. 16 is signal a.
と信号ａ、とを加算する加算器であり、加算器１６から
は制御弁５を制御する制御信号路が出力される。１７は
加算器１６の制御信号ルを入力し、この信号ルに応じて
制御弁５の開閉制御を行う比例制御装置である。The adder 16 is an adder that adds the signals a and a, and a control signal path for controlling the control valve 5 is output from the adder 16. 17 is a proportional control device which inputs the control signal of the adder 16 and controls the opening and closing of the control valve 5 in accordance with this signal.
次に、この制御装置の動作を述べる。まず、入口ＮＯ，
分析装置７により入口側ＮＯｘ濃度が、又、排ガス流量
検出装置８により入口側排ガス流量が検出され、これに
応じた信号すおよび信号ｆに基づいて反応に必要なアン
モニア量が演算され、これに応じた信号１．を得る。一
方、これとは別に、排ガス流量検出装置８、温度検出装
置９、出ロＮＯ，分析装置１０によりそれぞれ入口側排
ガス流量、入口側排ガス温度、出口側ＮＯｘ濃度が検出
され、これらに応じた信号ｆ１信号１、信号Ｃに基づい
て（３）弐に該当する変動時のアンモニア吸着不足量が
演算され、これに応じた信号ａ。Next, the operation of this control device will be described. First, entrance NO.
The analyzer 7 detects the NOx concentration on the inlet side, and the exhaust gas flow rate detector 8 detects the exhaust gas flow rate on the inlet side, and the amount of ammonia required for the reaction is calculated based on the corresponding signals S and F. Corresponding signal 1. get. On the other hand, apart from this, the exhaust gas flow rate on the inlet side, the exhaust gas temperature on the inlet side, and the NOx concentration on the outlet side are detected by the exhaust gas flow rate detection device 8, temperature detection device 9, outlet NOx, and analysis device 10, respectively, and signals corresponding to these are detected. Based on f1 signal 1 and signal C, the amount of ammonia adsorption deficiency at the time of fluctuation corresponding to (3) 2 is calculated, and signal a corresponding to this is calculated.
を得る。煙道２に注入すべきアンモニアの量は、反応に
必要なアンモニア量とアンモニア吸着不足鎗とを加えた
量であるから、これに応じた信号ａ。get. Since the amount of ammonia to be injected into the flue 2 is the sum of the amount of ammonia required for the reaction and the amount of ammonia adsorption deficiency, the signal a corresponding to the amount of ammonia.
と信吟ａ、とを加算器１６で加算することにより、必要
とする制御信号ルを得、この制御信号ｒＬＫより比例制
御装置１７を介して制御弁５を制御するものである。The necessary control signal rLK is obtained by adding the signals rLK and shingin a in an adder 16, and the control valve 5 is controlled by this control signal rLK via a proportional control device 17.
このようＫ、この実施例では反応に必要なアンモニア量
とは別に、触媒へのアンモニア吸着量の通、不足を演算
し、両者を加算してアンモニア注入量としたので、急激
な反応条件の変化に対する脱硝性能の追従性が良好とな
り、前記従来の制御方法で問題となっていた発振や未反
応のアンモニアの触媒層からの、−出を防ぐことができ
る。In this example, in addition to the amount of ammonia required for the reaction, the amount of ammonia adsorbed on the catalyst was calculated, and the amount of ammonia injected was calculated by adding the two, so that the reaction conditions could change rapidly. The followability of the denitrification performance against the denitrification performance improves, and it is possible to prevent oscillation and the release of unreacted ammonia from the catalyst layer, which were problems in the conventional control method.
次に、第４図に示す本発明の制御方法を実施するための
制御装置の他の実施例について説明する。Next, another embodiment of the control device for carrying out the control method of the present invention shown in FIG. 4 will be described.
図で［３図に示す実施例と同一部分には同一符号を付し
て説明を省略する。１８は演算器である。演算器１８に
は、さきの実施例における演算器１４と異なり、出口Ｎ
Ｏｘ分析装置１０の出力信号Ｃ１入口ＮＯｘ分析装置７
の出力信号す、前記（２）式における脱硝率設定値Ｘ、
に応じた信号Ｘ、が入力れ、これに応じた信号 １１１
ニニｌ−が出力される。In the figure, the same parts as those in the embodiment shown in FIG. 18 is a computing unit. Unlike the calculator 14 in the previous embodiment, the calculator 18 has an outlet N.
Output signal C1 of Ox analyzer 10 Inlet NOx analyzer 7
The output signal is the denitrification rate set value X in the above equation (2),
A signal X corresponding to this is input, and a signal corresponding to this 111
Nini l- is output.
１−ｘ。1-x.
又、乗算器１２にはさぎの実施例と異なり、排ガス流量
検出装置８の出力信号ｆ、入ロＮＯ，分析装置７の出力
信号ｂ１前記脱硝率設定値Ｘ、に応じた信号Ｘ、が入力
され、乗算が行われて信号ａ８が出力される。乗算器１
５には、さぎの実施例における入力信号 Ｉｎ−の代り
に信号、、１−ｘＣ・
１−ｘ。Also, unlike the Sagi embodiment, the multiplier 12 receives the output signal f of the exhaust gas flow rate detection device 8, the input NO, the output signal b1 of the analyzer 7, and the signal , multiplication is performed, and signal a8 is output. Multiplier 1
5, the input signal In- in the rabbit embodiment is replaced by a signal, , 1-xC.
1-x.
が入力され、前記（２）式の演算を行って信号ａ。is input, and the above equation (2) is calculated to obtain the signal a.
が出力される。本実施例の動作はさぎの実施例の動作に
準するものであるので、説明は省略する。is output. Since the operation of this embodiment is similar to that of the rabbit embodiment, the explanation will be omitted.
このように、本実施はさぎの実施例と同じ効果を有する
ばかりでな（、さぎの実施例における演算器の１つを省
略することができる。In this way, this embodiment not only has the same effect as the rabbit embodiment (but also allows one of the arithmetic units in the rabbit embodiment to be omitted).
なお、以上の実施例においては排ガス流量の信号な排ガ
ス流量を直接検出することにより得ているが、ボイラ負
荷や過剰空気緻を検出することにより得ることもできる
。In the above embodiments, the signal of the exhaust gas flow rate is obtained by directly detecting the exhaust gas flow rate, but it can also be obtained by detecting the boiler load or excess air density.
又、各演算手段としてマイクロコンビ二一夕を用いれば
、制御装置を小型、高信頼度のものとすることができる
。Further, by using a microcombiner as each calculation means, the control device can be made small and highly reliable.
以上説明したように、本発明では、反応に必要なアンモ
ニア量とは別に、触媒へのアンモニア吸着量の通、不足
を演算し、両者な加算してこれをアンモニアの注入量と
したので、急激な反応条件の変化に対しても脱硝性能の
追従性が良好となり、又、未反応アンモニアの触媒ｌ−
からの流出を防ぐことができる。As explained above, in the present invention, in addition to the amount of ammonia required for the reaction, the amount of ammonia adsorbed on the catalyst is calculated, and the amount of ammonia adsorbed to the catalyst is calculated, and the two are added together to determine the amount of ammonia injected. The denitrification performance has good followability even with changes in reaction conditions, and the catalyst l-
It is possible to prevent leakage from.
第１図（ＩＩ）、（ｂ）は従来の制御方法を用いた場合
の負荷の変動と脱＃［置出Ｄ １１１ Ｎ Ｏ，ｘ量と
の関係を説明するための説明図、第２図はアンモニア吸
着量と脱硝効率との関係な説明するための説明図、第３
図は本発明のアンモニア注入量制御方法を実施する制御
装置の一実施例の系統図、第４図は本発明のアンモニア
注入量制御方法を実施する制御装置の他の実施例の系統
図である。
ｌ・・・・・・脱硝装置、４・・・・・・アンモニア供
給源、５・・・・・・制御弁、７・・・・・・入口ＮＯ
，分析鋏置、８・・・・・・排ガス流量検出装置、９・
・・・・・温度検出装置、１０・・・・・・出口ＮＯｘ
分析装置、１１．１４．１Ｂ・・・・・・演算器、１２
．１５・・・・・・乗算器、１３・・・・・・関数発生
器、１６・・・・・・加算器。
第１図（Ｏ）
第１図（ｂ）
第２図Figures 1 (II) and (b) are explanatory diagrams for explaining the relationship between load fluctuations and the amount of desulfurization [output D 111 N O,x] when using the conventional control method; is an explanatory diagram to explain the relationship between ammonia adsorption amount and denitrification efficiency, Part 3
The figure is a system diagram of one embodiment of a control device that implements the ammonia injection amount control method of the present invention, and FIG. 4 is a system diagram of another embodiment of a control device that implements the ammonia injection amount control method of the present invention. . 1... Denitrification device, 4... Ammonia supply source, 5... Control valve, 7... Inlet NO.
, analysis scissors holder, 8...exhaust gas flow rate detection device, 9.
...Temperature detection device, 10...Outlet NOx
Analyzer, 11.14.1B... Arithmetic unit, 12
．． 15... Multiplier, 13... Function generator, 16... Adder. Figure 1 (O) Figure 1 (b) Figure 2
Claims (1)
物を除′去する脱硝装置において、設定された前記脱硝
装置出口＠窒素酸化物量と前記脱硝装置入口側窒素酸化
物量とＫより脱硝反応Ｋｌ’するアンモニア注入量に応
じた信号を発生するとともに、この信号に前記触媒に吸
着するアンモニアの調整量に応じた信号を加算し、この
加算された信号でアンモニア注入量を制御することを特
徴とする脱硝装置のアンモニア注入量制御方法。1. In a denitrification device that removes nitrogen oxides from exhaust gas by adsorbing ammonia on a catalyst, the denitrification reaction Kl is determined from the set amount of nitrogen oxides at the outlet of the denitrification device, the amount of nitrogen oxides at the entrance of the denitrification device, and K. A signal corresponding to the amount of ammonia to be injected is generated, a signal corresponding to the adjusted amount of ammonia adsorbed on the catalyst is added to this signal, and the amount of ammonia to be injected is controlled by this added signal. Ammonia injection amount control method for denitrification equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57056047A JPS58174227A (en) | 1982-04-06 | 1982-04-06 | Method for controlling charging amount of ammonia in denitration apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57056047A JPS58174227A (en) | 1982-04-06 | 1982-04-06 | Method for controlling charging amount of ammonia in denitration apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58174227A true JPS58174227A (en) | 1983-10-13 |
| JPH0411248B2 JPH0411248B2 (en) | 1992-02-27 |
Family
ID=13016165
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57056047A Granted JPS58174227A (en) | 1982-04-06 | 1982-04-06 | Method for controlling charging amount of ammonia in denitration apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58174227A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04265124A (en) * | 1991-02-21 | 1992-09-21 | Sumitomo Chem Eng Kk | Denitration method |
| JPH04346819A (en) * | 1991-05-23 | 1992-12-02 | Niigata Eng Co Ltd | Denitration control device and method |
| JP2003010645A (en) * | 2001-07-03 | 2003-01-14 | Babcock Hitachi Kk | Method and apparatus for controlling ammonia injection amount to nitrogen oxide removal apparatus and ammonia injection amount correcting apparatus to be employed therefor |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001303934A (en) * | 1998-06-23 | 2001-10-31 | Toyota Motor Corp | Exhaust emission control device for internal combustion engine |
| JP2002177741A (en) * | 2000-12-18 | 2002-06-25 | Miura Co Ltd | Method of controlling denitration apparatus in boiler |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5433864A (en) * | 1977-08-22 | 1979-03-12 | Hitachi Ltd | Process and device for controlling reducing agent for use in denitration plant |
| JPS551858A (en) * | 1978-06-21 | 1980-01-09 | Mitsubishi Chem Ind Ltd | Reduction and denitrification by ammonia |
| JPS56163741A (en) * | 1980-05-20 | 1981-12-16 | Kawasaki Heavy Ind Ltd | Method for controlling feed rate or nh3 in dry denitration apparatus |
-
1982
- 1982-04-06 JP JP57056047A patent/JPS58174227A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5433864A (en) * | 1977-08-22 | 1979-03-12 | Hitachi Ltd | Process and device for controlling reducing agent for use in denitration plant |
| JPS551858A (en) * | 1978-06-21 | 1980-01-09 | Mitsubishi Chem Ind Ltd | Reduction and denitrification by ammonia |
| JPS56163741A (en) * | 1980-05-20 | 1981-12-16 | Kawasaki Heavy Ind Ltd | Method for controlling feed rate or nh3 in dry denitration apparatus |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04265124A (en) * | 1991-02-21 | 1992-09-21 | Sumitomo Chem Eng Kk | Denitration method |
| JPH04346819A (en) * | 1991-05-23 | 1992-12-02 | Niigata Eng Co Ltd | Denitration control device and method |
| JP2003010645A (en) * | 2001-07-03 | 2003-01-14 | Babcock Hitachi Kk | Method and apparatus for controlling ammonia injection amount to nitrogen oxide removal apparatus and ammonia injection amount correcting apparatus to be employed therefor |
| JP4627611B2 (en) * | 2001-07-03 | 2011-02-09 | バブコック日立株式会社 | Ammonia injection amount control method and apparatus for denitration apparatus and ammonia injection amount correction device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0411248B2 (en) | 1992-02-27 |
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