JP2008001816A - Combustion-controlling method in coke oven - Google Patents
Combustion-controlling method in coke oven Download PDFInfo
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本発明は、装入炭の装入量、水分等の装入諸元、および目標火落時間から、燃焼室に与える燃料ガスの流量およびカロリーを計算設定するコークス炉の燃焼制御方法に関するものであり、特に装入炭の水分量変化に対する応答性の良いコークス炉の燃焼制御方法に関するものである。 The present invention relates to a combustion control method for a coke oven that calculates and sets the flow rate and calories of fuel gas applied to a combustion chamber from the amount of charged coal, the charging specifications such as moisture, and the target fire time. In particular, the present invention relates to a method for controlling the combustion of a coke oven with good responsiveness to changes in the moisture content of the charged coal.
図２は、コークス炉操業における火落時間と燃焼室温度の一般的な関係を示した図である。燃焼室温度と火落時間との関係は、右下がりの曲線で表され、燃焼室温度が高くなるに従って、火落時間は短くなる。コークス炉操業においては、一般的に、まず炉団全体の生産量が決まり、そこから１日当たり何回乾留のサイクルを回せばよいかという、いわゆる炉の稼働率が決まる。そして、そこから乾留後の置き時間を差し引いて、目標となる火落時間が決まる。 FIG. 2 is a diagram showing a general relationship between the burning time and the combustion chamber temperature in coke oven operation. The relationship between the combustion chamber temperature and the fire drop time is represented by a downward-sloping curve, and the fire drop time becomes shorter as the combustion chamber temperature becomes higher. In the coke oven operation, generally, the production amount of the entire furnace group is determined first, and then the so-called furnace operating rate, which is the number of cycles of dry distillation per day, is determined. Then, the target fire time is determined by subtracting the time after dry distillation from there.
次に、図２に示す燃焼室温度と火落時間との関係より、目標とする燃焼室温度が決まることになる。しかしながら、実際の燃焼室温度は、装炭量変化、水分率変化、燃焼室温度制御系のパフォーマンス、さらには炉の経年変化等により、バラツキを持つ。この燃焼室温度のバラツキは、火落時間のバラツキを招き、最悪の場合は稼働率を達成できなくなってしまう。このため、コークス炉操業においては、極力燃焼室温度のバラツキを低減する必要がある。 Next, the target combustion chamber temperature is determined from the relationship between the combustion chamber temperature and the fire drop time shown in FIG. However, the actual combustion chamber temperature varies due to changes in the amount of coal, moisture content, combustion chamber temperature control system performance, furnace aging, and the like. This variation in the temperature of the combustion chamber causes a variation in the burning time, and in the worst case, the operating rate cannot be achieved. For this reason, in coke oven operation, it is necessary to reduce variations in the combustion chamber temperature as much as possible.
燃焼室温度のバラツキを低減するため、これまで種々の技術が提案されてきており、例えば特許文献１に開示されているコークス炉における燃焼制御方法がある。図３は、特許文献１に開示された全体制御系を示した図である。 In order to reduce the variation in the temperature of the combustion chamber, various techniques have been proposed so far. For example, there is a combustion control method in a coke oven disclosed in Patent Document 1. FIG. 3 is a diagram showing an overall control system disclosed in Patent Document 1. As shown in FIG.
この方法は、装入炭の装入量、水分、粒度、揮発分等の装入諸元、目標火落時間、および目標置時間から目標燃焼室温度を計算により決定し、実測燃焼室温度を検出して前記目標燃焼室温度との偏差を求め、前記偏差から燃料ガスの流量およびカロリーを計算設定し、最適燃焼となるようにドラフト量を計算設定すると共に、炉からの燃焼排ガス分析を行い、最適燃焼が行われていない場合、前記ドラフト量を調整せしめ、実績燃焼室温度、実績火落時間、置時間および対応する装入諸元によって前記燃焼室温度をバイアス修正することを特徴とするものである。
しかしながら、上述した特許文献１では、目標燃焼室温度を操作した後で、下位の供給熱量制御系が働いて初めて、炉本体への操作量となる燃料ガスの流量およびカロリーが算出されるという２段構造となっており、降雨等に起因する水分変化の情報が間接的にしか燃焼制御に反映されないという問題があった。すなわち、下位の供給熱量制御系では、炉団平均としての燃焼室温度実績と目標燃焼室温度の偏差を見ながらフィードバックを行うが、炉団平均としての燃焼室温度は、数時間〜１日オーダーの応答遅れを伴っており、このフィードバック構造では、どうしても迅速に水分変化への対応アクションをとれないというものである。 However, in Patent Document 1 described above, after the target combustion chamber temperature is manipulated, the flow rate and calorie of the fuel gas, which is the manipulated variable to the furnace body, are calculated only after the subordinate supply heat quantity control system operates. It has a stage structure, and there has been a problem that information on moisture change caused by rainfall or the like is only indirectly reflected in the combustion control. That is, in the lower supply heat quantity control system, feedback is performed while seeing the deviation between the combustion chamber temperature results as the average of the furnace group and the target combustion chamber temperature, but the combustion chamber temperature as the average of the furnace group is on the order of several hours to one day. In this feedback structure, it is impossible to take action to respond to moisture changes quickly.
本発明は、上記事情に鑑みてなされたものであり、火落時間が降雨等に起因する水分変化に影響を受けないコークス炉の燃焼制御方法を提供することを目的とする。 The present invention has been made in view of the above circumstances, and an object of the present invention is to provide a combustion control method for a coke oven that is not affected by moisture change caused by rainfall or the like.
本発明の請求項１に係る発明は、装入炭の装入量、水分等の装入諸元、および目標火落時間から、燃焼室に与える供給熱量を計算し設定するコークス炉の燃焼制御方法において、前記供給熱量の計算値に、現在の装炭量および水分率に基づく水分補償熱量を加えて設定値とすることを特徴とするコークス炉の燃焼制御方法である。 The invention according to claim 1 of the present invention is a combustion control of a coke oven that calculates and sets the amount of heat supplied to the combustion chamber from the charging amount of charging coal, the charging parameters such as moisture, and the target fire time. In the method, a combustion control method for a coke oven is characterized in that a set value is obtained by adding a moisture compensation heat amount based on a current coal loading amount and a moisture content to the calculated value of the supplied heat amount.
また本発明の請求項２に係る発明は、請求項１に記載のコークス炉の燃焼制御方法において、前記水分補償熱量を、以下の計算式にて求めることを特徴とするコークス炉の燃焼制御方法である。 The invention according to claim 2 of the present invention is the coke oven combustion control method according to claim 1, wherein the moisture compensation calorie is obtained by the following calculation formula. It is.
本発明は、装入炭の装入量、水分から、燃焼室温度目標値を経由することなく直接に炉団への供給熱量を補正するようにしたので、下位の供給熱量制御系のパフォーマンス、特に燃焼室温度の炉団平均の持つ応答遅れの影響を受けることなく、炉団平均水分変動への対応を迅速に行うことが出来るようになった。 In the present invention, the amount of heat supplied to the furnace group is corrected directly from the charge amount and water content of the charge coal without going through the combustion chamber temperature target value. In particular, it has become possible to quickly cope with fluctuations in the average moisture content of the furnace group without being affected by the response delay of the furnace group average of the combustion chamber temperature.
以下に本発明を実施するための最良の形態について、図面および数式を参照して以下に説明を行う。図１は、本発明に係る制御系全体例を示す図である。 The best mode for carrying out the present invention will be described below with reference to the drawings and mathematical expressions. FIG. 1 is a diagram showing an example of the entire control system according to the present invention.
装炭情報のうち、装炭量および水分率をもとに、直接燃料ガスの流量およびカロリーの補正分を算出する。水分率や装炭量が変化、つまり水分量が変化した場合は、少なくともその蒸発潜熱の変化分は陽にかつ直に算出可能である。 Based on the amount of charcoal and the moisture content, the fuel gas flow rate and calorie correction are directly calculated. When the moisture content or the amount of coal is changed, that is, when the amount of moisture is changed, at least the change in latent heat of vaporization can be calculated directly and directly.
すなわち、100℃の水1kgを蒸発させるには539Kcal(=2256KJ)の熱量が必要なことが一般に知られている。従って、求まった蒸発潜熱変化分を元に直にガスカロリー変更すれば、迅速な対応が可能となる。 That is, it is generally known that an amount of heat of 539 Kcal (= 2256 KJ) is required to evaporate 1 kg of water at 100 ° C. Accordingly, if the gas calorie is changed directly based on the obtained change in the latent heat of vaporization, a quick response is possible.
例えば、水分補償熱量の計算方法として、以下の式（１）を用いるようにすればよい。 For example, the following equation (1) may be used as a method for calculating the moisture compensation heat quantity.
上式、基準となる水分率を定め、計測された装入炭の水分率により、プラスのカロリー補正、マイナスのカロリー補正を直接施すものである。パラメータa1は、前記蒸発潜熱を代表する、調整可能なパラメータである539Kcal/Kg(=2256KJ/Kg)の値を用いれば、100%の補償となる。 The above formula, the moisture content used as a reference, is determined, and positive calorie correction and negative calorie correction are directly performed based on the measured moisture content of the charged coal. If the value of 539 Kcal / Kg (= 2256 KJ / Kg), which is an adjustable parameter representing the latent heat of vaporization, is used as the parameter a 1 , the compensation is 100%.
すなわち、装炭量×水分率＝水分値の基準値からの変動分に、蒸発潜熱係数を乗じて、水分変動による必要熱量変化を直接計算する。また、パラメータa2は水分率の変化分、言い換えると水分変化速度に対して、上乗せして補償するかどうかを決める係数である。水分変化速度が正の場合、今後とも水分が増えることが想定されるので、前倒しのアクションをとることが可能となる。 That is, the required amount of heat change due to moisture fluctuation is directly calculated by multiplying the fluctuation amount from the reference value of coal loading x moisture content = moisture value by the latent heat of vaporization coefficient. Parameter a 2 is a coefficient that determines whether or not to compensate for the change in moisture content, in other words, the rate of moisture change. When the moisture change rate is positive, it is assumed that moisture will increase in the future, so it is possible to take an action ahead of schedule.
これにより、下位の供給熱量計算部に頼ることなく、直接的に燃料ガスのカロリーを変化させられるので、炉団の昇温遅れ等の影響を受けることなく迅速に水分変化に対応することができる。 As a result, the calorie of the fuel gas can be changed directly without relying on the subordinate supply calorie calculation unit, so that it is possible to respond quickly to moisture changes without being affected by a delay in the temperature rise of the furnace group. .
特許文献１で示した従来の燃焼制御方法における水分変動対応は、まず(1)目標温度補正を行い、その後(2)燃料ガスカロリー補正（実績を目標に近づけるフィードバック制御）を行うというように、２段階を踏んでおり、応答が数時間〜半日オーダーとなっていた。 In the conventional combustion control method shown in Patent Document 1, the moisture fluctuation is dealt with by first (1) correcting the target temperature and then (2) correcting the fuel gas calorie (feedback control that brings the actual results closer to the target). There were two steps and the response was on the order of several hours to half a day.
上記２段階の内、特に、(2)のフィードバック制御部分がネックとなっている。何故なら、コークス炉は熱容量が非常に大きく、補正をしてから結果が出るのに、半日〜１日オーダーの時間が掛かるからである。本発明では、(1)温度目標を介することなく、最初からガスカロリー補正をするので、即対応ができる。 Among the above two stages, the feedback control part (2) is particularly a bottleneck. This is because the coke oven has a very large heat capacity, and it takes a half day to an order of one day to obtain the result after correction. In the present invention, (1) gas calorie correction is performed from the beginning without going through the temperature target, so that it is possible to respond immediately.
もちろん、本発明のブロック構造を保ったまま、他の水分補償熱量計算を用いても構わないが、燃焼室温度という間接指標を経由しないで、コークス炉に操作を加えられることが肝要である。 Of course, another moisture compensation calorie calculation may be used while maintaining the block structure of the present invention, but it is important that the coke oven is operated without passing through the indirect index of the combustion chamber temperature.
なお、本発明で提案した方法は、プロセスコンピュータ等の計算機によって、自動的に炉に働きかけることはもちろん、ガイダンスシステム等によりオペレータを介して燃料ガスカロリーを変えるようにしても良い。 In the method proposed in the present invention, the fuel gas calorie may be changed via an operator by a guidance system or the like as well as by automatically operating the furnace by a computer such as a process computer.
図４は、本発明に係る燃焼制御方法を適用した場合と適用しなかった場合の比較例を示す図である。実コークス炉を対象にした長期オンライン試験の結果であり、図４（ａ）は本発明を適用しない場合、すなわちオペレータによるマニュアル運転の結果、（ｂ）は本発明を適用した場合の結果を示している。それぞれ、縦軸は火落ち温度偏差、横軸は目標火落ち時間からの乖離を正規化して示している。 FIG. 4 is a diagram showing a comparative example when the combustion control method according to the present invention is applied and when it is not applied. FIG. 4A shows the result of a long-term online test for an actual coke oven. FIG. 4A shows the result when the present invention is not applied, that is, the result of manual operation by an operator, and FIG. 4B shows the result when the present invention is applied. ing. In each case, the vertical axis represents the fire drop temperature deviation, and the horizontal axis represents the deviation from the target fire drop time.
図４（ｂ）の本発明を適用した場合では、目標火落ち時間(0.00)を中心にしたバラツキの小さい分布を示しているのに対して、（ａ）の本発明を適用しない場合では、目標火落ち時間を超え、かつバラツキの多い分布になっていることが分かる。本発明を適用した場合には、目標火落ち時間を確実に守れており、このことは目標とした生産量が達成できたコークス炉操業であることを示している。さらに、平均値としての乾留熱量が大幅に低減できてもいる。 In the case where the present invention of FIG. 4B is applied, a distribution with a small variation centered on the target fire drop time (0.00) is shown, whereas in the case where the present invention of FIG. 4A is not applied, It can be seen that the distribution exceeds the target burn-out time and has many variations. When the present invention is applied, the target burn-out time can be surely observed, which indicates that the coke oven operation has achieved the target production amount. Furthermore, the heat of dry distillation as an average value can be significantly reduced.
Claims (2)
前記供給熱量の計算値に、現在の装炭量および水分率に基づく水分補償熱量を加えて設定値とすることを特徴とするコークス炉の燃焼制御方法。 In the combustion control method of the coke oven that calculates and sets the amount of heat supplied to the combustion chamber from the charging amount of charging coal, the charging specifications such as moisture content, and the target fire time,
A combustion control method for a coke oven, wherein a set value is obtained by adding a moisture compensation heat amount based on a current coal charge amount and a moisture content to the calculated value of the supplied heat amount.
前記水分補償熱量を、以下の計算式にて求めることを特徴とするコークス炉の燃焼制御方法。
A method for controlling combustion in a coke oven, wherein the moisture compensation heat quantity is obtained by the following formula.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012153882A (en) * | 2011-01-04 | 2012-08-16 | Jfe Steel Corp | Method for calculating gas cock opening, method for operating coke oven and method for producing coke |
| JP2013133462A (en) * | 2011-12-27 | 2013-07-08 | Jfe Steel Corp | Determination method of carbonization chamber wall state of coke oven and device for the same |
| KR101435272B1 (en) | 2012-09-27 | 2014-08-27 | 현대제철 주식회사 | Method for predicting consume calorie of coke oven |
| KR20220008018A (en) * | 2020-07-13 | 2022-01-20 | 주식회사 포스코 | Appratus and method for operating coke oven |
| CN114644934A (en) * | 2022-04-18 | 2022-06-21 | 武汉钢铁有限公司 | Coke oven heating method matched with coking process of coal as fired |
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2006
- 2006-06-23 JP JP2006173232A patent/JP2008001816A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012153882A (en) * | 2011-01-04 | 2012-08-16 | Jfe Steel Corp | Method for calculating gas cock opening, method for operating coke oven and method for producing coke |
| JP2013133462A (en) * | 2011-12-27 | 2013-07-08 | Jfe Steel Corp | Determination method of carbonization chamber wall state of coke oven and device for the same |
| KR101435272B1 (en) | 2012-09-27 | 2014-08-27 | 현대제철 주식회사 | Method for predicting consume calorie of coke oven |
| KR20220008018A (en) * | 2020-07-13 | 2022-01-20 | 주식회사 포스코 | Appratus and method for operating coke oven |
| KR102412477B1 (en) | 2020-07-13 | 2022-06-22 | 주식회사 포스코 | Appratus and method for operating coke oven |
| CN114644934A (en) * | 2022-04-18 | 2022-06-21 | 武汉钢铁有限公司 | Coke oven heating method matched with coking process of coal as fired |
| CN114644934B (en) * | 2022-04-18 | 2023-08-18 | 武汉钢铁有限公司 | Coke oven heating method matched with coking process of coal entering furnace |
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