JP7730106B2 - Fluidized bed sludge incinerator and automatic combustion control method for fluidized bed sludge incinerator - Google Patents
Fluidized bed sludge incinerator and automatic combustion control method for fluidized bed sludge incineratorInfo
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Description
本発明は、汚泥を燃焼する流動床式汚泥焼却炉及び流動床式汚泥焼却炉の自動燃焼制御方法に関する。 The present invention relates to a fluidized bed sludge incinerator that burns sludge and an automatic combustion control method for a fluidized bed sludge incinerator.
下水処理場においては、下水汚泥を燃やすために流動床式汚泥焼却炉などの汚泥焼却炉を設けている。流動床式汚泥焼却炉は、流動媒体として砂を使用した砂層部（流動層）と、燃焼室であるフリーボード部とを有する筒状の焼却炉本体を備えている多段燃焼式の焼却炉であり、汚泥を乾燥、ガス化、燃焼というプロセスで処理している。 Sewage treatment plants are equipped with sludge incinerators, such as fluidized bed incinerators, to burn sewage sludge. Fluidized bed incinerators are multi-stage combustion furnaces with a cylindrical furnace body that has a sand layer (fluidized bed) that uses sand as a fluidizing medium and a freeboard section that serves as a combustion chamber. The sludge is treated through a process of drying, gasification, and combustion.
下水汚泥は窒素成分に富んでいることからその燃焼排ガスには温暖化効果の高いＮ２Ｏを含むため、焼却炉から排出されるＮ２Ｏを極力少なくすることが望まれている。
また、焼却炉の燃焼状態によっては、煙突から一酸化炭素等の有害未燃物の排出が増大することがあり、一酸化炭素の排出量を抑制する必要がある。
Since sewage sludge is rich in nitrogen components, its combustion exhaust gas contains N 2 O, which has a strong global warming effect, and therefore it is desirable to minimize the amount of N 2 O emitted from incinerators.
Furthermore, depending on the combustion conditions of the incinerator, the amount of harmful unburned matter such as carbon monoxide emitted from the chimney may increase, making it necessary to suppress the amount of carbon monoxide emitted.
特許文献１には、焼却炉本体から排出される燃焼ガスのＮ２Ｏ濃度を測定するＮ２Ｏ濃度センサと、Ｎ２Ｏ濃度センサの測定値に基づいて前記燃焼空気量を調整する制御装置と、を備え、燃焼空気量に基づいて砂層の流動範囲を制限するようにした流動床式汚泥焼却炉が記載されている。 Patent Document 1 describes a fluidized bed sludge incinerator that is equipped with an N2O concentration sensor that measures the N2O concentration of the combustion gas discharged from the incinerator body, and a control device that adjusts the amount of combustion air based on the measurement value of the N2O concentration sensor, and that limits the fluidization range of the sand layer based on the amount of combustion air.
特許文献２には、炉床温度を測定する炉床温度計を流動状態監視手段として用い、その測定値が適正範囲を逸脱した場合、流動不良が発生したと判断し、流動空気量を増加させて流動状態を回復させ、前記測定値が適正範囲に戻った場合には再び流動空気量を減少させ安定運転を継続させるようにした流動床式汚泥焼却炉の燃焼制御方法が記載されている。 Patent Document 2 describes a combustion control method for a fluidized bed sludge incinerator. This method uses a hearth thermometer that measures the hearth temperature as a fluidization state monitoring means, and if the measured value falls outside an appropriate range, it determines that poor fluidization has occurred and increases the amount of fluidizing air to restore the fluidization state. If the measured value returns to the appropriate range, the amount of fluidizing air is reduced again to continue stable operation.
燃焼制御には従来ＣＯ濃度計を用いているが、特許文献１の方法では、Ｎ２Ｏ濃度計が燃焼制御のために必要となる。
特許文献２では、炉床温度計を用い、その測定値の変化率により流動状態の良／不良を判断する方法や、複数の炉床温度計を用い、その温度差により流動状態の良／不良を判断することが提案されているが、焼却物性状の変化により炉床温度全体が上下する場合には、流動状態の悪化を検出することができないという問題がある。
流動床式汚泥焼却炉では砂層流動状態悪化の現象が生じて運転が不安定になることが大きな問題となっている。
これはＮ２Ｏ濃度を低減させようとして一次空気量を減少させ過ぎたのが理由である。
本発明は砂層の流動状態を砂層の各所に設けた砂層温度測定器で測定された温度の温度差に基づいて制御し、排ガス中のＮ２Ｏ濃度を低減することを目的とする。
Conventionally, a CO concentration meter is used for combustion control, but the method of Patent Document 1 requires an N 2 O concentration meter for combustion control.
Patent Document 2 proposes a method of using a hearth thermometer to determine whether the fluidity state is good or bad based on the rate of change of the measured value, or a method of using multiple hearth thermometers to determine whether the fluidity state is good or bad based on the temperature difference between them.However, there is a problem in that if the overall hearth temperature fluctuates due to changes in the properties of the incineration material, it is not possible to detect a deterioration in the fluidity state.
In fluidized bed sludge incinerators, the deterioration of the sand layer fluidity and the resulting unstable operation are major problems.
This is because the amount of primary air was reduced too much in an attempt to reduce the N 2 O concentration.
The present invention aims to reduce the N 2 O concentration in exhaust gas by controlling the fluidization state of a sand layer based on the temperature difference measured by sand layer temperature measuring devices installed at various points in the sand layer.
上記課題を解決するべく発明者らが鋭意検討した結果、出願人は、砂層に砂層温度測定器を複数個設けたとき、この複数個の砂層温度測定器が示す砂層温度の最高温度と最低温度との温度差に上限値と下限値とを設けて、温度差が上限値を超えた場合及び温度差が下限値を下回った場合に砂層部に供給される一次空気量を制御することにより、上記課題を解決することができることを見出して、本発明を完成した。 After extensive research to solve the above problems, the inventors discovered that the above problems could be solved by installing multiple sand layer temperature measuring devices in the sand layer, setting upper and lower limits for the temperature difference between the highest and lowest sand layer temperatures indicated by the multiple sand layer temperature measuring devices, and controlling the amount of primary air supplied to the sand layer when the temperature difference exceeds the upper limit and falls below the lower limit, thereby completing the present invention.
上記課題を解決する本願発明の実施形態は以下に記載するとおりである。
（１）砂層部と前記砂層部の上側に形成されたフリーボード部とを有し、投入された汚泥を燃焼させる流動床式汚泥焼却炉であって、
前記砂層部に設けられ、砂層の複数箇所の温度を測定する複数個の温度測定器と、
前記温度測定器によって測定された砂層の温度の最高温度と最低温度との温度差を計算し、その温度差の値に基づいて前記砂層部に供給される一次空気量を決定し、前記砂層部に供給される一次空気量を制御する制御装置であって、前記温度差が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御する制御装置と、
を有することを特徴とする流動床式汚泥焼却炉。
（２）前記制御装置が、前記温度差が前記所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％増加させ、前記温度差が前記所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％減少させるように制御する制御装置であることを特徴とする上記（１）に記載の流動床式汚泥焼却炉。
（３）前記所定の上限値を１５℃以上の値に設定し、前記所定の下限値を１５℃未満の値に設定することを特徴とする上記（２）に記載の流動床式汚泥焼却炉。
（４）砂層部と前記砂層部の上側に形成されたフリーボード部とを有し、投入された汚泥を燃焼させる流動床式汚泥焼却炉であって、
前記砂層部に設けられ、砂層の複数箇所の温度を測定する複数個の温度測定器と、
前記温度測定器によって測定された砂層の温度の最高温度と最低温度との温度差と前記温度差の変化速度を計算し、その温度差の変化速度の値に基づいて前記砂層部に供給される一次空気量を決定し、前記砂層部に供給される一次空気量を制御する制御装置であって、前記温度差の変化速度が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差の変化速度が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御する制御装置と、
を有することを特徴とする流動床式汚泥焼却炉。
（５）前記制御装置が、前記温度差の変化速度が前記所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％増加させ、前記温度差の変化速度が前記所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％減少させるように制御する制御装置であることを特徴とする上記（４）に記載の流動床式汚泥焼却炉。
（６）前記所定の上限値を１５℃／ｈ以上の値に設定し、前記所定の下限値を１５℃／ｈ未満の値に設定することを特徴とする上記（５）に記載の流動床式汚泥焼却炉。
（７）前記流動床式汚泥焼却炉の焼却炉本体の炉出口から排出された排ガス中のＣＯ濃度を測定するＣＯ濃度測定器を設け、
前記制御装置が、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を減少させ、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を増加させるように制御する制御装置であることを特徴とする上記（１）～（６）のいずれかに記載の流動床式汚泥焼却炉。
（８）前記制御装置が、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％減少させ、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％増加させるように制御する制御装置であることを特徴とする上記（７）に記載の流動床式汚泥焼却炉。
（９）前記所定のＣＯ濃度上限値が１０～２０ＰＰＭであり、前記所定のＣＯ濃度下限値が０～１０ＰＰＭであることを特徴とする上記（７）又は（８）に記載の流動床式汚泥焼却炉。
（１０）砂層部と前記砂層部の上側に形成されたフリーボード部とを有し、投入された汚泥を燃焼させる流動床式汚泥焼却炉の自動燃焼制御方法であって、
前記砂層部に、異なる位置の砂層の温度を測定する複数個の温度測定器を設け、前記複数箇所によって測定された砂層の温度の最高温度と最低温度との温度差を計算し、前記温度差が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御することを特徴とする、流動床式汚泥焼却炉の自動燃焼制御方法。
（１１）前記温度差が前記所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％増加させ、前記温度差が前記所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％減少させるように制御することを特徴とする上記（１０）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１２）前記所定の上限値を１５℃以上の値に設定し、前記所定の下限値を１５℃未満の値に設定することを特徴とする上記（１１）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１３）砂層部と前記砂層部の上側に形成されたフリーボード部とを有し、投入された汚泥を燃焼させる流動床式汚泥焼却炉の自動燃焼制御方法であって、
前記砂層部に、異なる位置の砂層の温度を測定する複数個の温度測定器を設け、前記温度測定器によって測定された砂層の温度の最高温度と最低温度との温度差と前記温度差の変化速度を計算し、前記温度差の変化速度が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差の変化速度が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御することを特徴とする、流動床式汚泥焼却炉の自動燃焼制御方法。
（１４）前記温度差の変化速度が前記所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％増加させ、前記温度差の変化速度が前記所定下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％減少させるように制御することを特徴とする上記（１３）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１５）前記所定の上限値を１５℃／ｈ以上の値に設定し、前記所定の下限値を１５℃／ｈ未満の値に設定することを特徴とする上記（１４）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１６）前記流動床式汚泥焼却炉の焼却炉本体の炉出口から排出された排ガス中のＣＯ濃度をＣＯ濃度測定器で測定し、
前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を減少させ、
前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を増加させることを特徴とする上記（１０）～（１５）のいずれかに記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１７）前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を１～５％減少させ、
前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％増加させることを特徴とする上記（１６）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
（１８）前記所定のＣＯ濃度上限値が１０～２０ＰＰＭであり、前記所定のＣＯ濃度下限値が０～１０ＰＰＭであることを特徴とする上記（１６）又は（１７）に記載の流動床式汚泥焼却炉の自動燃焼制御方法。
The embodiments of the present invention that solve the above problems are as follows.
(1) A fluidized bed sludge incinerator having a sand layer and a freeboard formed above the sand layer, in which sludge is burned,
a plurality of temperature measuring devices provided in the sand layer portion for measuring the temperature of a plurality of locations in the sand layer;
a control device that calculates the temperature difference between the maximum and minimum temperatures of the sand layer measured by the temperature measuring device, determines the amount of primary air to be supplied to the sand layer section based on the value of the temperature difference, and controls the amount of primary air to be supplied to the sand layer section, so that when the temperature difference exceeds a predetermined upper limit value, the amount of primary air to be supplied to the sand layer section is increased, and when the temperature difference falls below a predetermined lower limit value, the amount of primary air to be supplied to the sand layer section is decreased;
A fluidized bed sludge incinerator comprising:
(2) A fluidized bed sludge incinerator as described in (1) above, characterized in that the control device is a control device that controls the amount of primary air supplied to the sand layer to increase by 1 to 5% when the temperature difference exceeds the predetermined upper limit value, and controls the amount of primary air supplied to the sand layer to decrease by 1 to 5% when the temperature difference falls below the predetermined lower limit value.
(3) A fluidized bed sludge incinerator according to (2) above, characterized in that the predetermined upper limit is set to a value of 15°C or higher, and the predetermined lower limit is set to a value below 15°C.
(4) A fluidized bed sludge incinerator having a sand layer and a freeboard formed above the sand layer, in which sludge is burned,
a plurality of temperature measuring devices provided in the sand layer portion for measuring the temperature of a plurality of locations in the sand layer;
a control device that calculates the temperature difference between the maximum and minimum temperatures of the sand layer measured by the temperature measuring device and the rate of change of said temperature difference, determines the amount of primary air to be supplied to said sand layer section based on the value of the rate of change of said temperature difference, and controls the amount of primary air to be supplied to said sand layer section, so that when the rate of change of said temperature difference exceeds a predetermined upper limit value, the amount of primary air to be supplied to said sand layer section is increased, and when the rate of change of said temperature difference falls below a predetermined lower limit value, the control device controls so that the amount of primary air to be supplied to said sand layer section is decreased;
A fluidized bed sludge incinerator comprising:
(5) A fluidized bed sludge incinerator as described in (4) above, characterized in that the control device is a control device that controls the amount of primary air supplied to the sand layer to increase by 1 to 5% when the rate of change of the temperature difference exceeds the specified upper limit value, and controls the amount of primary air supplied to the sand layer to decrease by 1 to 5% when the rate of change of the temperature difference falls below the specified lower limit value.
(6) A fluidized bed sludge incinerator according to (5) above, characterized in that the predetermined upper limit is set to a value of 15°C/h or more, and the predetermined lower limit is set to a value less than 15°C/h.
(7) A CO concentration measuring device is provided to measure the CO concentration in the exhaust gas discharged from the furnace outlet of the incinerator body of the fluidized bed sludge incinerator;
The fluidized bed sludge incinerator according to any one of (1) to (6) above, characterized in that the control device is a control device that controls so as to reduce the amount of primary air supplied to the sand layer when the CO concentration in the exhaust gas measured by the CO concentration meter exceeds a predetermined CO concentration upper limit value, and to increase the amount of primary air supplied to the sand layer when the CO concentration in the exhaust gas measured by the CO concentration meter falls below a predetermined CO concentration lower limit value.
(8) The fluidized bed sludge incinerator described in (7) above, characterized in that the control device is a control device that controls so that when the CO concentration in the exhaust gas measured by the CO concentration meter exceeds a predetermined CO concentration upper limit value, the amount of primary air supplied to the sand layer is reduced by 1 to 5%, and when the CO concentration in the exhaust gas measured by the CO concentration meter falls below a predetermined CO concentration lower limit value, the amount of primary air supplied to the sand layer is increased by 1 to 5%.
(9) The fluidized bed sludge incinerator according to (7) or (8), characterized in that the predetermined CO concentration upper limit value is 10 to 20 ppm and the predetermined CO concentration lower limit value is 0 to 10 ppm.
(10) An automatic combustion control method for a fluidized bed sludge incinerator that has a sand layer and a freeboard formed above the sand layer and burns introduced sludge, comprising:
A method for automatic combustion control of a fluidized bed sludge incinerator, characterized in that a plurality of temperature measuring devices are provided in the sand layer section to measure the temperature of the sand layer at different positions, the temperature difference between the highest and lowest temperatures of the sand layer measured at the plurality of positions is calculated, and when the temperature difference exceeds a predetermined upper limit value, the amount of primary air supplied to the sand layer section is increased, and when the temperature difference falls below a predetermined lower limit value, the amount of primary air supplied to the sand layer section is decreased.
(11) An automatic combustion control method for a fluidized bed sludge incinerator described in (10) above, characterized in that when the temperature difference exceeds the predetermined upper limit value, the amount of primary air supplied to the sand layer is increased by 1 to 5%, and when the temperature difference falls below the predetermined lower limit value, the amount of primary air supplied to the sand layer is decreased by 1 to 5%.
(12) An automatic combustion control method for a fluidized bed sludge incinerator described in (11) above, characterized in that the predetermined upper limit value is set to a value of 15°C or higher, and the predetermined lower limit value is set to a value below 15°C.
(13) An automatic combustion control method for a fluidized bed sludge incinerator that has a sand layer and a freeboard formed above the sand layer and burns introduced sludge, comprising:
a temperature difference between the highest and lowest temperatures of the sand layer measured by the temperature measuring devices and the rate of change of said temperature difference; and if the rate of change of said temperature difference exceeds a predetermined upper limit, the amount of primary air supplied to said sand layer is increased; and if the rate of change of said temperature difference falls below a predetermined lower limit, the amount of primary air supplied to said sand layer is decreased.
(14) An automatic combustion control method for a fluidized bed sludge incinerator described in (13) above, characterized in that when the rate of change of the temperature difference exceeds the predetermined upper limit value, the amount of primary air supplied to the sand layer is increased by 1 to 5%, and when the rate of change of the temperature difference falls below the predetermined lower limit value, the amount of primary air supplied to the sand layer is decreased by 1 to 5%.
(15) An automatic combustion control method for a fluidized bed sludge incinerator described in (14) above, characterized in that the predetermined upper limit value is set to a value of 15°C/h or more, and the predetermined lower limit value is set to a value less than 15°C/h.
(16) The CO concentration in the exhaust gas discharged from the furnace outlet of the incinerator body of the fluidized bed sludge incinerator is measured with a CO concentration meter;
When the CO concentration in the exhaust gas measured by the CO concentration measuring device exceeds a predetermined CO concentration upper limit value, the amount of primary air supplied to the sand layer portion is reduced,
The automatic combustion control method for a fluidized bed sludge incinerator according to any one of (10) to (15) above, characterized in that when the CO concentration in the exhaust gas measured by the CO concentration measuring device falls below a predetermined CO concentration lower limit value, the amount of primary air supplied to the sand layer is increased.
(17) When the CO concentration in the exhaust gas exceeds a predetermined CO concentration upper limit value, the amount of primary air supplied to the sand layer is reduced by 1 to 5%;
The automatic combustion control method for a fluidized bed sludge incinerator according to (16) above, characterized in that when the CO concentration in the exhaust gas falls below a predetermined CO concentration lower limit, the amount of primary air supplied to the sand layer is increased by 1 to 5%.
(18) The automatic combustion control method for a fluidized bed sludge incinerator according to (16) or (17), characterized in that the predetermined CO concentration upper limit value is 10 to 20 PPM, and the predetermined CO concentration lower limit value is 0 to 10 PPM.
本発明によれば、砂層の流動状態を砂層の各所に設けた砂層温度測定器で測定された温度の温度差に基づいて制御することによって排ガス中のＮ２Ｏ濃度を低減することができる。 According to the present invention, the N 2 O concentration in the exhaust gas can be reduced by controlling the fluidization state of the sand layer based on the temperature difference measured by sand layer temperature measuring devices installed at various points in the sand layer.
以下、本発明の実施形態の流動床式汚泥焼却炉、及びその自動燃焼制御方法について図面を参照して詳細に説明する。 The fluidized bed sludge incinerator and its automatic combustion control method according to an embodiment of the present invention will be described in detail below with reference to the drawings.
図１は本発明の一実施形態の流動床式汚泥焼却炉１の概略構成図である。流動床式汚泥焼却炉１は、流動砂１７を熱媒体として汚泥Ｍとともに気泡流動層を形成して燃焼する焼却炉である。
流動床式汚泥焼却炉１の焼却炉本体３は、下部に設けられた砂層部Ｓ（流動層）と砂層部Ｓより上方に設けられたフリーボード部Ｆと、を有しており、焼却炉本体３の側壁に形成された汚泥投入口６と、焼却炉本体３の頂部に設けた炉出口４と、焼却炉本体３の下部に設けられて流動用の空気を供給する一次空気供給部７と、一次空気供給部７の上方に設けられてフリーボード部Ｆに二次空気を供給する二次空気供給部９と、複数の砂層温度測定器１０と、複数のフリーボード温度測定器１１と、砂層温度測定器１０又は砂層温度測定器１０及びフリーボード温度測定器１１の測定値に基づいて一次空気供給部７に供給される一次空気の供給量を制御する制御装置２７と、を備えている。
1 is a schematic diagram of a fluidized bed sludge incinerator 1 according to one embodiment of the present invention. The fluidized bed sludge incinerator 1 is an incinerator that uses fluidized sand 17 as a heat medium to form a bubbling fluidized bed together with sludge M and combusts the sludge.
The incinerator body 3 of the fluidized bed sludge incinerator 1 has a sand layer section S (fluidized bed) located at the bottom and a freeboard section F located above the sand layer section S, and is equipped with a sludge inlet 6 formed in the side wall of the incinerator body 3, a furnace outlet 4 located at the top of the incinerator body 3, a primary air supply section 7 located at the bottom of the incinerator body 3 and supplying air for fluidization, a secondary air supply section 9 located above the primary air supply section 7 and supplying secondary air to the freeboard section F, multiple sand layer temperature measuring devices 10, multiple freeboard temperature measuring devices 11, and a control device 27 that controls the amount of primary air supplied to the primary air supply section 7 based on the measurements of the sand layer temperature measuring device 10 or the sand layer temperature measuring device 10 and the freeboard temperature measuring device 11.
砂層温度測定器１０の設置個数は、例えば、図２Ａ、Ｂに示す様に、砂層温度測定器１０を砂層の垂直方向に距離を置いて上下二段に設け、下段には図２Ａに示す様に周方向に９０度角度をずらして４個設け、上段には図２Ｂに示すように下段の設置位置から周方向に４５度角度をずらして４個設ける。また、本実施形態ではフリーボード温度測定器１１は例えば砂層直上に周方向に１２０度ずらして３個設けている。
焼却炉本体３の壁際は温度が低く、内壁から１５０～２００ｍｍを超えると砂層の温度が測定できるので、熱電対等の温度測定器は内壁から３００ｍｍくらいの所の温度を測定するように配置することが好ましい。
2A and 2B, the sand layer temperature measuring devices 10 are installed in two tiers, upper and lower, spaced apart in the vertical direction of the sand layer, with four devices installed in the lower tier, offset by 90 degrees in the circumferential direction as shown in Fig. 2A, and four devices installed in the upper tier, offset by 45 degrees in the circumferential direction from the installation position of the lower tier, as shown in Fig. 2B. In this embodiment, three freeboard temperature measuring devices 11 are installed directly above the sand layer, offset by 120 degrees in the circumferential direction, for example.
The temperature is low near the walls of the incinerator body 3, and the temperature of the sand layer can be measured more than 150 to 200 mm from the inner wall, so it is preferable to position a thermocouple or other temperature measuring device to measure the temperature about 300 mm from the inner wall.
流動床式汚泥焼却炉１は、汚泥Ｍを砂層部Ｓに投入する汚泥供給装置５を有しており、汚泥Ｍは、汚泥供給装置５から焼却炉本体３の内部の砂層部Ｓに投入される。
流動床式汚泥焼却炉１は、燃焼用空気を供給する流動ブロワ２１、燃焼用空気を予熱する空気予熱器１５、空気予熱器１５から流出する予熱された燃焼用空気の供給を受けると共に冷却ブロワ２３から外気の供給を受ける空気冷却器２５、焼却炉本体３に供給される全空気供給量を調節する全空気量調節弁３１、焼却炉本体３に供給される二次空気供給量を調節する二次空気量調節弁３２、砂層温度測定器１０、フリーボード温度測定器１１を備えている。
The fluidized bed sludge incinerator 1 has a sludge supply device 5 that charges sludge M into the sand layer S, and the sludge M is charged from the sludge supply device 5 into the sand layer S inside the incinerator body 3.
The fluidized bed sludge incinerator 1 is equipped with a fluidized bed blower 21 that supplies combustion air, an air preheater 15 that preheats the combustion air, an air cooler 25 that receives the preheated combustion air flowing out from the air preheater 15 and also receives a supply of outside air from a cooling blower 23, a total air volume control valve 31 that adjusts the total amount of air supplied to the incinerator body 3, a secondary air volume control valve 32 that adjusts the amount of secondary air supplied to the incinerator body 3, a sand layer temperature measuring instrument 10, and a freeboard temperature measuring instrument 11.
制御装置２７は、例えばＣＰＵ（Ｃｅｎｔｒａｌ Ｐｒｏｃｅｓｓｉｎｇ Ｕｎｉｔ、中央処理装置）が、記憶部からプログラムを読み出して実行することで構成される。
図１に示したものでは、制御装置２７は複数の砂層温度測定器１０からのデータ、又は、複数の砂層温度測定器１０及びフリーボード温度測定器１１からのデータに基づいて、砂層の流動状態を把握し、制御信号を流動ブロワ２１、全空気量調節弁３１、二次空気量調節弁３２に送って、一次空気量を調整し、砂層の流動状態を流動不良が起きず、かつ、Ｎ２Ｏを低減することができる最適な流動状態を保つ。
The control device 27 is configured by, for example, a CPU (Central Processing Unit) reading and executing a program from a storage unit.
In the example shown in Figure 1, the control device 27 grasps the fluidity state of the sand layer based on data from multiple sand layer temperature measuring devices 10, or data from multiple sand layer temperature measuring devices 10 and freeboard temperature measuring device 11, and sends control signals to the fluidization blower 21, total air volume control valve 31, and secondary air volume control valve 32 to adjust the amount of primary air and maintain the sand layer in an optimal fluidity state that does not cause poor fluidity and can reduce N2O .
流動ブロワ２１から供給される燃焼用空気が導入される配管は、上流側に配置されている全空気供給配管２８と、全空気供給配管２８の下流側で分岐する一次空気供給配管２９及び二次空気供給配管３０と、を有している。流動ブロワ２１は、全空気供給配管２８を介して一次空気供給配管２９及び二次空気供給配管３０に空気を供給する。 The piping through which combustion air is supplied from the fluidized bed blower 21 includes an upstream total air supply piping 28, and a primary air supply piping 29 and a secondary air supply piping 30 that branch off downstream from the total air supply piping 28. The fluidized bed blower 21 supplies air to the primary air supply piping 29 and secondary air supply piping 30 via the total air supply piping 28.
一次空気供給配管２９は砂層部Ｓに一次空気を供給し、二次空気供給配管３０は、フリーボード部Ｆに二次空気を供給する。全空気供給配管２８を流れる全空気（砂層部Ｓ及びフリーボード部Ｆに供給される全ての空気）の流量（全空気量）は、一次空気の流量（一次空気量）とフリーボード部Ｆに供給される二次空気の流量（二次空気量）との合計である。全空気量は、炉出口温度が８２５～８７５℃となる様に決定する。 The primary air supply pipe 29 supplies primary air to the sand layer section S, and the secondary air supply pipe 30 supplies secondary air to the freeboard section F. The flow rate (total air volume) of all air (all air supplied to the sand layer section S and freeboard section F) flowing through the total air supply pipe 28 is the sum of the flow rate of primary air (primary air volume) and the flow rate of secondary air (secondary air volume) supplied to the freeboard section F. The total air volume is determined so that the furnace outlet temperature is between 825 and 875°C.
図４は炉出口温度と炉出口から排出されたガス中のＮ２Ｏ濃度との関係を示した図である。図４に示すように、炉出口温度が８２５℃以上でＮ２Ｏ値が低下することから、全空気量は炉出口温度が８２５℃以上となるように決定する。
また、炉出口温度が８７５℃を超えると、空気予熱器が損傷する恐れがあり、また、炉から発生する飛灰が溶融固化してしまって排ガスダクトの閉塞をもたらす恐れがある。
このため、全空気量は炉出口温度が８７５℃を超えないように決定する。
Fig. 4 shows the relationship between the furnace outlet temperature and the N2O concentration in the gas discharged from the furnace outlet. As shown in Fig. 4, the N2O value decreases when the furnace outlet temperature is 825°C or higher, so the total air amount is determined so that the furnace outlet temperature is 825°C or higher.
Furthermore, if the furnace outlet temperature exceeds 875°C, the air preheater may be damaged, and the fly ash generated from the furnace may melt and solidify, causing blockage of the exhaust gas duct.
Therefore, the total amount of air is determined so that the furnace outlet temperature does not exceed 875°C.
また、図５は煙突出口におけるＮ２Ｏ濃度値とセラミックフィルター出口におけるＣＯ濃度値との相関を見たものであるが、図５に示されているように、煙突出口におけるＮ２Ｏ濃度値とセラミックフィルター出口におけるＣＯ濃度値とには高い相関がある（相関係数０．８２）。
従って、ＣＯ濃度を下げる制御をすることによってＮ２Ｏ濃度も低下させることができる。
上記のように、煙突出口におけるＮ２Ｏ濃度値とセラミックフィルター出口におけるＣＯ濃度値とに高い相関があることから、本発明においては、ＣＯ濃度計によってＣＯ濃度値を観察し、このＣＯ濃度値を制御することによってＮ２Ｏ濃度値を制御する。
Furthermore, Figure 5 shows the correlation between the N2O concentration value at the chimney outlet and the CO concentration value at the ceramic filter outlet. As shown in Figure 5, there is a high correlation between the N2O concentration value at the chimney outlet and the CO concentration value at the ceramic filter outlet (correlation coefficient 0.82).
Therefore, by controlling the CO concentration to be lower, the N 2 O concentration can also be lowered.
As described above, since there is a high correlation between the N 2 O concentration value at the chimney outlet and the CO concentration value at the ceramic filter outlet, in the present invention, the CO concentration value is observed using a CO concentration meter, and the N 2 O concentration value is controlled by controlling this CO concentration value.
全空気供給配管２８には、全空気量を調整する全空気量調節弁３１が設けられている。二次空気供給配管３０には、二次空気量を調整する二次空気量調節弁３２が設けられている。二次空気量調節弁３２が調整されることにより、二次空気量が調整され、その結果、一次空気量が調整される。二次空気量調節弁３２によって二次空気量が調整された場合においても、全空気量調節弁３１が操作されない限り、全空気量は変化しない。全空気量調節弁３１及び二次空気量調節弁３２は、制御装置２７によって制御される。 The total air supply pipe 28 is provided with a total air volume control valve 31 that adjusts the total air volume. The secondary air supply pipe 30 is provided with a secondary air volume control valve 32 that adjusts the secondary air volume. Adjusting the secondary air volume control valve 32 adjusts the secondary air volume, and as a result, the primary air volume. Even when the secondary air volume is adjusted by the secondary air volume control valve 32, the total air volume will not change unless the total air volume control valve 31 is operated. The total air volume control valve 31 and secondary air volume control valve 32 are controlled by the control device 27.
空気予熱器１５は、全空気供給配管２８を流れる全空気を予熱する。空気予熱器１５は、例えば、焼却炉本体３から排出される排ガスから熱を回収して空気を予熱する。空気予熱器１５を出た排ガスはセラミックフィルター３３、洗煙処理塔３４で処理された後、誘引通風機（ＩＤＦ）３５を介して煙突３６に送られる。 The air preheater 15 preheats all the air flowing through the total air supply pipe 28. The air preheater 15 preheats the air by recovering heat from, for example, the exhaust gas discharged from the incinerator main body 3. The exhaust gas leaving the air preheater 15 is treated in a ceramic filter 33 and a smoke washing treatment tower 34, and then sent to the chimney 36 via an induced draft fan (IDF) 35.
流動床式汚泥焼却炉１は、砂層部Ｓの温度Ｔｓを測定する砂層温度測定器１０と、砂層直上の温度Ｔｆを測定するフリーボード温度測定器１１と、炉出口４から排出された直後の煙道１２を流れる排ガスの温度Ｔｏを検出する排ガス温度測定器１３と、煙道１２を流れる排ガスのＣＯ濃度を測定するＣＯ濃度測定器１４と、を備えている。
これら測定器１０、１１、１３、１４は制御装置２７と電気的に接続されている。制御装置２７は、これら測定器によって測定された測定値に基づいて、全空気量調節弁３１及び二次空気量調節弁３２を制御する。
The fluidized bed sludge incinerator 1 is equipped with a sand layer temperature measuring device 10 that measures the temperature Ts of the sand layer S, a freeboard temperature measuring device 11 that measures the temperature Tf directly above the sand layer, an exhaust gas temperature measuring device 13 that detects the temperature To of the exhaust gas flowing through the flue 12 immediately after it is discharged from the furnace outlet 4, and a CO concentration measuring device 14 that measures the CO concentration of the exhaust gas flowing through the flue 12.
These measuring devices 10, 11, 13, and 14 are electrically connected to a control device 27. The control device 27 controls a total air amount control valve 31 and a secondary air amount control valve 32 based on the values measured by these measuring devices.
次に、汚泥燃焼のプロセスを説明する。
以下では、砂層温度測定器１０を図２に示すように８個設けた場合について説明する。
汚泥Ｍは図示しない脱水プロセスによって脱水され、汚泥供給装置５により焼却炉本体３に供給される。また、燃焼用空気が流動ブロワ２１の吐出圧により全空気供給配管２８に導入された後、空気予熱器１５で加熱され、砂層部Ｓ及びフリーボード部Ｆに供給される。
燃焼用空気により加熱された砂層部Ｓの砂粒は、燃焼用空気と発生する燃焼ガスによって、供給された汚泥Ｍとともに流動し、汚泥Ｍは流動しながら燃焼する。さらに、燃焼ガスはフリーボード部Ｆの内部を上昇しながら、二次空気供給配管３０を介して供給される二次空気によって燃焼が完結される。燃焼後の排ガスは炉出口４を介して煙道１２に導入され、排ガス処理装置へ排出される。
Next, the sludge combustion process will be explained.
In the following, a case where eight sand layer temperature measuring devices 10 are provided as shown in FIG. 2 will be described.
The sludge M is dewatered by a dewatering process (not shown) and supplied to the incinerator body 3 by the sludge supply device 5. Combustion air is introduced into the total air supply piping 28 by the discharge pressure of the fluidization blower 21, heated by the air preheater 15, and supplied to the sand layer section S and the freeboard section F.
The sand grains in the sand layer S, heated by the combustion air, are fluidized together with the supplied sludge M by the combustion air and the generated combustion gas, and the sludge M burns while fluidizing. Furthermore, the combustion gas rises inside the freeboard section F, and the combustion is completed by secondary air supplied through the secondary air supply pipe 30. The exhaust gas after combustion is introduced into the flue 12 through the furnace outlet 4 and discharged to the exhaust gas treatment device.
次に本実施態様における、流動床式汚泥焼却炉１の制御方法について説明する。
まず、本実施形態の流動床式汚泥焼却炉１を起動し、運転を安定させるまでの流動床式汚泥焼却炉１の立ち上げ工程について説明する。
流動床式汚泥焼却炉１の立ち上げ工程では、焼却炉本体３に汚泥Ｍ及び一次空気（燃焼用空気）を供給する。即ち、流動床式汚泥焼却炉１の立ち上げ工程においては、二次空気は使用しない。汚泥Ｍ及び一次空気の供給後、流動床式汚泥焼却炉１の各部温度が上昇し、流動床式汚泥焼却炉１の各部温度が安定した状態になった場合に流動床式汚泥焼却炉１の立ち上げ工程は終了する。
Next, a method for controlling the fluidized bed sludge incinerator 1 in this embodiment will be described.
First, the start-up process of the fluidized bed sludge incinerator 1 of this embodiment from start-up to stabilization of operation will be described.
In the start-up process of the fluidized bed sludge incinerator 1, sludge M and primary air (air for combustion) are supplied to the incinerator body 3. In other words, secondary air is not used in the start-up process of the fluidized bed sludge incinerator 1. After the supply of sludge M and primary air, the temperatures of each part of the fluidized bed sludge incinerator 1 rise, and when the temperatures of each part of the fluidized bed sludge incinerator 1 have stabilized, the start-up process of the fluidized bed sludge incinerator 1 is completed.
次に、流動床式汚泥焼却炉１の立ち上げ工程後の流動床式汚泥焼却炉１の制御方法について説明する。
定常運転時には、一次空気量が少ない方が、排ガス中のＮ２Ｏ濃度が少なくなる。従って、Ｎ２Ｏ濃度を少なくするには、一次空気量を可能な限り少なくする必要がある。
しかしながら、一次空気量が少なすぎると流動状態が悪くなり、効率の良い燃焼焼却処理ができない。さらに悪化すると流動が停止して、焼却が出来なくなる。
そこで、燃焼に影響が出ない最低限度にまで一次空気量を減らすことが本発明の制御方法の目的である。
Next, a method for controlling the fluidized bed sludge incinerator 1 after the start-up process of the fluidized bed sludge incinerator 1 will be described.
During steady-state operation, the smaller the amount of primary air, the lower the N 2 O concentration in the exhaust gas. Therefore, in order to reduce the N 2 O concentration, it is necessary to make the amount of primary air as small as possible.
However, if the amount of primary air is too small, the fluidity will be poor and efficient combustion and incineration will be impossible. If it gets worse, the fluidity will stop and incineration will become impossible.
Therefore, the object of the control method of the present invention is to reduce the amount of primary air to the minimum level that does not affect combustion.
本発明においては一次空気量の増減によって排ガス中のＣＯ濃度を制御することによってＮ２Ｏ濃度を制御するとともに、効率の良い燃焼焼却処理を行う。このため、流動床式汚泥焼却炉１の運転試験を行って、砂層の温度の最高温度と最低温度との温度差がどのような数値（下限値）を下回るとＣＯ濃度（Ｎ２Ｏ濃度）が所定の値を超えるのか、及び、前記温度差がどのような数値（上限値）を超えると流動状態が悪くなり、効率の良い燃焼焼却処理ができなくなるかを予め運転試験を行って把握し、砂層温度差の上限値及び下限値を設定しておく。 In the present invention, the CO concentration in the exhaust gas is controlled by increasing or decreasing the amount of primary air, thereby controlling the N2O concentration and achieving efficient combustion incineration. For this reason, an operational test of the fluidized bed sludge incinerator 1 is conducted in advance to determine the numerical value (lower limit) below which the CO concentration ( N2O concentration) exceeds a predetermined value for the temperature difference between the maximum and minimum temperatures of the sand layer, and the numerical value (upper limit) above which the fluidization state deteriorates and efficient combustion incineration cannot be achieved, and then the upper and lower limits of the sand layer temperature difference are set.
また、同様に、流動床式汚泥焼却炉１の運転試験を行って、砂層の温度の最高温度と最低温度との温度差の変化速度の値がどのような数値（下限値）を下回るとＣＯ濃度（Ｎ２Ｏ濃度）が所定の値を超えるのか、及び、前記温度差の変化速度がどのような数値（上限値）を超えると流動状態が悪くなり、効率の良い燃焼焼却処理ができなくなるかを予め運転試験を行って把握し、砂層温度差の変化速度の上限値及び下限値を設定しておく。 Similarly, an operating test of the fluidized bed sludge incinerator 1 is conducted in advance to determine the value (lower limit) below which the CO concentration ( N2O concentration) exceeds a predetermined value for the rate of change of the temperature difference between the highest and lowest temperatures of the sand layer, and the value (upper limit) above which the rate of change of the temperature difference deteriorates and efficient combustion incineration processing becomes impossible, and then the upper and lower limits for the rate of change of the temperature difference in the sand layer are set.
本発明に於いては、流動床式汚泥焼却炉１の砂層に砂層温度測定器１０を複数個設ける。そして、この複数ある砂層温度測定器１０が示す砂層温度の最高温度と最低温度との温度差を算出する。
そして、本発明の第一の態様においては、この温度差に基づいて一次空気量の制御を行う。
具体的には、砂層の温度差が１５℃～３０℃となった場合には砂層の流動が不足しているため、一次空気量を１～５％増加させように制御する。
一方、砂層の温度差が０～１５℃となった場合には砂層の流動が活発すぎるため、一次空気量を１～５％減少させるように制御をする。
上記の制御を行うことにより、排ガス中のＮ２Ｏ濃度を低く保ちつつ焼却炉を安定して運転することができる。
In the present invention, a plurality of sand layer temperature measuring devices 10 are provided in the sand layer of the fluidized bed sludge incinerator 1. Then, the temperature difference between the maximum and minimum sand layer temperatures indicated by the plurality of sand layer temperature measuring devices 10 is calculated.
In the first aspect of the present invention, the amount of primary air is controlled based on this temperature difference.
Specifically, when the temperature difference in the sand layer is between 15°C and 30°C, the flow of the sand layer is insufficient, so the amount of primary air is controlled to be increased by 1 to 5%.
On the other hand, when the temperature difference in the sand layer is 0 to 15°C, the flow of the sand layer is too vigorous, so the amount of primary air is controlled to be reduced by 1 to 5%.
By carrying out the above control, the incinerator can be operated stably while maintaining a low N 2 O concentration in the exhaust gas.
上記の制御を行うためには、一次空気量を増加させる制御を開始するための温度差を流動床式汚泥焼却炉１の特性に応じて、１５℃～３０℃の間の所定の温度（例えば２５℃）を上限値（閾値）として設定しておく。
また、一次空気量を減少させる制御を開始するための温度差を流動床式汚泥焼却炉１の特性に応じて、０℃～１５℃の間の所定の温度（例えば５℃）を下限値（閾値）として設定しておく。
In order to perform the above control, the temperature difference for starting control to increase the amount of primary air is set to a predetermined temperature (e.g., 25°C) between 15°C and 30°C as the upper limit (threshold) depending on the characteristics of the fluidized bed sludge incinerator 1.
In addition, the temperature difference for starting control to reduce the amount of primary air is set as a lower limit (threshold) to a predetermined temperature between 0°C and 15°C (for example, 5°C) depending on the characteristics of the fluidized bed sludge incinerator 1.
また、本発明の第二の態様においては、この温度差の変化速度に基づいて一次空気量の制御を行う。
具体的には、砂層の温度差の変化速度が１５℃／ｈ～３０℃／ｈとなった場合には砂層の流動が不足しているため、一次空気量を１～５％増加させように制御する。
一方、砂層の温度差の変化速度が０℃／ｈ～１５℃／ｈとなった場合には砂層の流動が活発すぎるため、一次空気量を１～５％減少させるように制御する。
上記の制御を行うことにより、排ガス中のＮ２Ｏ濃度を低く保ちつつ焼却炉を安定して運転することができる。
In a second aspect of the present invention, the amount of primary air is controlled based on the rate of change of this temperature difference.
Specifically, when the rate of change of the temperature difference in the sand layer reaches 15°C/h to 30°C/h, the flow of the sand layer is insufficient, so the amount of primary air is controlled to be increased by 1 to 5%.
On the other hand, when the rate of change of the temperature difference in the sand layer is between 0°C/h and 15°C/h, the flow of the sand layer is too vigorous, so the amount of primary air is controlled to be reduced by 1 to 5%.
By carrying out the above control, the incinerator can be operated stably while maintaining a low N 2 O concentration in the exhaust gas.
上記の制御を行うためには、一次空気量を増加させる制御を開始するための温度差の変化速度を流動床式汚泥焼却炉１の特性に応じて、１５℃／ｈ～３０℃／ｈの間の所定の温度（例えば２５℃）を上限値（閾値）として設定しておく。
また、一次空気量を減少させる制御を開始するための温度差の変化速度を流動床式汚泥焼却炉１の特性に応じて、０℃／ｈ～１５℃／ｈの間の所定の温度（例えば５０℃）を下限値（閾値）として設定しておく。
In order to perform the above control, the rate of change of the temperature difference for starting control to increase the amount of primary air is set as an upper limit (threshold) to a predetermined temperature (e.g., 25°C) between 15°C/h and 30°C/h depending on the characteristics of the fluidized bed sludge incinerator 1.
In addition, the rate of change of the temperature difference for starting control to reduce the amount of primary air is set as a lower limit (threshold) to a predetermined temperature (e.g., 50°C) between 0°C/h and 15°C/h depending on the characteristics of the fluidized bed sludge incinerator 1.
制御装置２７の動作について以下説明する。
まず、８個の砂層温度測定器１０が示す温度値Ｔｓの最大温度値と最小温度値のデータを所定時間間隔（例えば１分毎）で入手し、その温度差（ΔＴ）を算出する。
次に所定時間(ｔ分：例えば１０分)経過したときに、ｔ分前の温度差（ΔＴ０）とｔ分経過後の温度差（ΔＴｔ）の変化速度（変化率）［（ΔＴ０－ΔＴｔ）／ｔ］を算出する。
そして、現在の温度差が許容範囲であるのか、温度差の変化速度がプラス（＋）であるのかマイナス（－）であるのか、その変化速度の絶対値の大きさがどの程度か、その変化速度の状態がどの程度続いているのか等のデータを、蓄積したデータベースと照らし合わせて一次空気量の増減の必要性の有無を決定する。
制御装置２７は全空気量調節弁３１、二次空気量調節弁３２、又は流動ブロワ２１に信号を送って一次空気量を増減させる。
The operation of the control device 27 will now be described.
First, the maximum and minimum temperature values Ts indicated by the eight sand layer temperature measuring devices 10 are obtained at predetermined time intervals (for example, every minute), and the temperature difference (ΔT) is calculated.
Next, when a predetermined time (t minutes: for example, 10 minutes) has passed, the rate of change (rate of change) [(ΔT 0 - ΔT t )/t] between the temperature difference (ΔT 0 ) before t minutes and the temperature difference (ΔT t ) after t minutes have passed is calculated.
The system then compares data such as whether the current temperature difference is within the allowable range, whether the rate of change of the temperature difference is positive (+) or negative (-), how large the absolute value of the rate of change is, and how long that rate of change has continued against the accumulated database to determine whether or not it is necessary to increase or decrease the amount of primary air.
The control device 27 sends a signal to the total air flow control valve 31, the secondary air flow control valve 32, or the flow blower 21 to increase or decrease the amount of primary air.
［実施例１］
図１に示す流動床式汚泥焼却炉１であって、内径：５．０ｍ、フリーボード高さ：８．５ｍの流動床式汚泥焼却炉１を用いて運転試験を行った。流動砂には珪砂を使用し、静止砂層高さは１．０ｍとした。汚泥の含水率は７５％であり、供給量は６ｔ／ｈとした。
この流動床式汚泥焼却炉１を用いて運転試験を行い図３に示す［空気量－砂層温度差、砂層温度差変化速度］のグラフを得た。
なお、実施例では砂層の温度差の上限値を２５℃と設定し、温度差の変化速度の下限値を０℃／ｈとした。
[Example 1]
An operation test was carried out using the fluidized bed sludge incinerator 1 shown in Figure 1, which had an inner diameter of 5.0 m and a freeboard height of 8.5 m. Silica sand was used as the fluidizing sand, and the static sand layer height was 1.0 m. The moisture content of the sludge was 75%, and the supply rate was 6 t/h.
An operational test was carried out using this fluidized bed sludge incinerator 1, and the graph of [air volume vs. sand layer temperature difference, sand layer temperature difference change rate] shown in FIG. 3 was obtained.
In the example, the upper limit of the temperature difference of the sand layer was set to 25°C, and the lower limit of the rate of change of the temperature difference was set to 0°C/h.
図３において複数ある砂層温度の最大値と最小値の差が２５℃に達し（図３中短い矢印の位置参照）、一次空気量を３％増加した結果、図３の〇において上記温度差が減少でき、流動不良現象が消え、流動床式汚泥焼却炉１の運転が安定化した。
また、砂層温度差の変化速度を利用した１例では、図３の◎において（図３中の◎で示した長い矢印の位置参照）、変化速度が０℃／ｈ以下となったため、一次空気量を３％減少させた。その結果、砂層温度差が大きくなった現象が確認できた。
In Figure 3, the difference between the maximum and minimum temperatures of the multiple sand layers reached 25°C (see the position of the short arrow in Figure 3). As a result of increasing the amount of primary air by 3%, the temperature difference was reduced as indicated by the circle in Figure 3, the poor fluidization phenomenon disappeared, and the operation of the fluidized bed sludge incinerator 1 became stable.
In one example using the rate of change in the sand layer temperature difference, the rate of change was below 0°C/h at the double circle in Figure 3 (see the position of the long arrow marked with a double circle in Figure 3), so the amount of primary air was reduced by 3%. As a result, it was confirmed that the sand layer temperature difference increased.
また、上記の制御を行った場合でも、何らかの事情により煙突から排出される排ガス中のＣＯ濃度が高くなる（即ちＮ２Ｏ濃度が高くなる）場合がある。
この場合には、排ガス中のＣＯ濃度に予め所定のＣＯ濃度上限値を設定しておき、ＣＯ濃度測定器１４で測定した排ガス中のＣＯ濃度が前記ＣＯ濃度上限値を超えた場合には、前記砂層部Ｓに供給される一次空気量を１～５％減少させる制御を行う。
Furthermore, even if the above control is performed, there may be cases where the CO concentration in the exhaust gas discharged from the chimney becomes high (that is, the N 2 O concentration becomes high) for some reason.
In this case, a predetermined upper limit value for the CO concentration in the exhaust gas is set in advance, and when the CO concentration in the exhaust gas measured by the CO concentration measuring device 14 exceeds the upper limit value, the amount of primary air supplied to the sand layer section S is controlled to be reduced by 1 to 5%.
また、排ガス中のＣＯ濃度を過度に低減させるような操業状態も好ましくない。
そこで、排ガス中のＣＯ濃度に下限値を設定しておき、ＣＯ濃度測定器１４で測定した排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、砂層部Ｓに供給される一次空気量を１～５％増加させるように制御を行う。
Ｎ２Ｏ濃度の規制値は３０ＰＰＭである。このため、運転に際しての管理上限値は安全面から余裕をみて、例えば２０ＰＰＭ未満で管理することとし、このＮ２Ｏ濃度に対応するＣＯ濃度（図５の相関図から２４ＰＰＭ）をＣＯ濃度の上限値に設定しても良い。
Moreover, an operating state that excessively reduces the CO concentration in the exhaust gas is also undesirable.
Therefore, a lower limit is set for the CO concentration in the exhaust gas, and when the CO concentration in the exhaust gas measured by the CO concentration measuring device 14 falls below the predetermined CO concentration lower limit, the amount of primary air supplied to the sand layer section S is controlled to be increased by 1 to 5%.
The regulated value for N2O concentration is 30 PPM. Therefore, the upper limit of the control value during operation may be set to, for example, less than 20 PPM to allow for a margin of safety, and the CO concentration corresponding to this N2O concentration (24 PPM from the correlation diagram in Figure 5) may be set as the upper limit of the CO concentration.
本発明の実施形態においては煙道１２に排ガス中のＣＯ濃度を測定するＣＯ濃度測定器１４を設け、Ｎ２Ｏ濃度測定器は特に設けない。
前記したように、ＣＯ濃度とＮ２Ｏ濃度とは高い相関がある。また、ＣＯ濃度測定器１４はＮ２Ｏ濃度測定器より安価で、広く普及している。そこで、Ｎ２Ｏ濃度測定器を用いてＮ２Ｏ濃度を測定することなく、ＣＯ濃度測定器１４を用いてＣＯ濃度を測定することにより、Ｎ２Ｏ濃度の状況を把握することができる。従って、ＣＯ濃度測定器１４の計測値を制御に用いることで操業を調整し、また、排ガス値を公表する必要がある等の、Ｎ２Ｏ濃度値をデータとして作製する必要がある場合には、ＣＯ濃度から、ＣＯ濃度―Ｎ２Ｏ濃度の相関データに基づいてＮ２Ｏ濃度を算出することができる。
In this embodiment of the present invention, a CO concentration measuring device 14 for measuring the CO concentration in the flue gas is provided in the flue 12, but no N 2 O concentration measuring device is particularly provided.
As described above, there is a high correlation between the CO concentration and the N 2 O concentration. Furthermore, the CO concentration measuring instrument 14 is cheaper than the N 2 O concentration measuring instrument and is widely used. Therefore, the N 2 O concentration status can be grasped by measuring the CO concentration using the CO concentration measuring instrument 14 without measuring the N 2 O concentration using the N 2 O concentration measuring instrument. Therefore, when it is necessary to adjust operations by using the measurement value of the CO concentration measuring instrument 14 for control, or to prepare N 2 O concentration values as data, such as when it is necessary to publish exhaust gas values, the N 2 O concentration can be calculated from the CO concentration based on the correlation data between the CO concentration and the N 2 O concentration.
以下に、排ガス中のＣＯ濃度の上限値及び下限値を設定して、一次空気量を増減させることにより、Ｎ２Ｏ濃度及び流動床式汚泥焼却炉１の流動状態を制御した例を示す。 An example will be shown below in which the N 2 O concentration and the fluidization state of the fluidized bed sludge incinerator 1 are controlled by setting upper and lower limits for the CO concentration in the exhaust gas and increasing or decreasing the amount of primary air.
［実施例２］
実施例１と同じ流動床式汚泥焼却炉１を用いて運転試験を行った。
砂層温度の最高温度と最低温度の差（以下、砂層温度差）を６℃、一次空気量を８，４００Ｎｍ３／ｈとしたところ、セラミックフィルター出口で測定している排ガス中のＣＯ濃度が２４ＰＰＭに上昇した。この時、煙突出口で測定している排ガス中のＮ２Ｏ濃度も許容値（管理上限値）２０ＰＰＭに達した。そのため、一次空気量を８，４００Ｎｍ３／ｈから８，０００Ｎｍ３／ｈに５．０％減少させて前記ＣＯ濃度を１６ＰＰＭに低下させた。
その結果、前記Ｎ２Ｏ濃度は１０ＰＰＭまで低下し、砂層温度差も流動状態良好な範囲内の１０℃となり、前記焼却炉を好適に安定運転することができた。
[Example 2]
An operation test was carried out using the same fluidized bed sludge incinerator 1 as in Example 1.
When the difference between the maximum and minimum sand layer temperatures (hereinafter referred to as the sand layer temperature difference) was set to 6°C and the primary air volume was set to 8,400 Nm3 /h, the CO concentration in the exhaust gas measured at the ceramic filter outlet rose to 24 PPM. At this time, the N2O concentration in the exhaust gas measured at the chimney outlet also reached the allowable value (upper control limit) of 20 PPM. Therefore, the primary air volume was reduced by 5.0% from 8,400 Nm3 /h to 8,000 Nm3 /h, lowering the CO concentration to 16 PPM.
As a result, the N 2 O concentration was reduced to 10 ppm, the temperature difference in the sand layer was reduced to 10° C., which is within the range for a good fluidity state, and the incinerator was able to be operated in a stable manner.
[実施例３]
実施例１と同じ流動床式汚泥焼却炉１を用いて運転試験を行った。
砂層温度差を２０℃、一次空気量を７，８００Ｎｍ３／ｈで運転した。この時、セラミックフィルター出口で測定している排ガス中のＣＯ濃度は１６ＰＰＭであり、煙突出口で測定している排ガス中のＮ２Ｏ濃度は許容値（管理上限値：２０ＰＰＭ）以下の１０ＰＰＭであったが、一次空気量不足のため、砂層の流動状態が不十分であった。
そこで前記Ｎ２Ｏ濃度の許容値２０ＰＰＭに対応する前記ＣＯ濃度を超えない範囲で一次空気量を増やし、砂層の流動状態の改善を図った。一次空気量を７，８００Ｎｍ３／ｈから８，２００Ｎｍ３／ｈに５．０％増加させ、前記ＣＯ濃度を２０ＰＰＭとした。
その結果、前記Ｎ２Ｏ濃度も許容値以下の１５ＰＰＭに抑えることができ、砂層温度差も８℃となって砂層流動状態が改善し、前記焼却炉を好適に安定運転することができた。
実施例２、３の結果を表１に示す。
[Example 3]
An operation test was carried out using the same fluidized bed sludge incinerator 1 as in Example 1.
The plant was operated with a sand layer temperature difference of 20°C and a primary air flow rate of 7,800 Nm3 /h. At this time, the CO concentration in the exhaust gas measured at the ceramic filter outlet was 16 PPM, and the N2O concentration in the exhaust gas measured at the chimney outlet was 10 PPM, below the allowable value (upper control limit: 20 PPM). However, the fluidization of the sand layer was insufficient due to the insufficient primary air flow rate.
Therefore, the flow rate of the primary air was increased within a range that did not exceed the CO concentration corresponding to the N2O concentration tolerance of 20 PPM, in order to improve the fluidity of the sand layer. The primary air rate was increased by 5.0% from 7,800 Nm3 /h to 8,200 Nm3 /h, and the CO concentration was set to 20 PPM.
As a result, the N 2 O concentration was suppressed to 15 ppm, which is below the allowable value, and the temperature difference in the sand layer was reduced to 8° C., improving the sand layer fluidity, and enabling the incinerator to be operated in a stable manner.
The results of Examples 2 and 3 are shown in Table 1.
以上、本発明の実施形態を、図面を参照して詳述してきたが、具体的な構成はこの実施形態に限られるものではなく、この発明の要旨を逸脱しない範囲の設計変更等も含まれる。 The above describes an embodiment of the present invention in detail with reference to the drawings, but the specific configuration is not limited to this embodiment and includes design modifications and the like that do not deviate from the gist of the present invention.
１ 流動床式汚泥焼却炉
３ 焼却炉本体
４ 炉出口
５ 汚泥供給装置
６ 汚泥投入口
７ 一次空気供給部
９ 二次空気供給部
１０ 砂層温度測定器
１１ フリーボード温度測定器
１２ 煙道
１３ 排ガス温度測定器
１４ ＣＯ濃度測定器
１５ 空気予熱器
１７ 流動砂
１９ 空気供給ノズル
２１ 流動ブロワ
２３ 冷却ブロワ
２５ 空気冷却器
２７ 制御装置
２８ 全空気供給配管
２９ 一次空気供給配管
３０ 二次空気供給配管
３１ 全空気量調節弁
３２ 二次空気量調節弁
３３ セラミックフィルター
３４ 洗煙処理塔
３５ 誘引通風機
３６ 煙突
Ｆ フリーボード部
Ｍ 汚泥
Ｓ 砂層部
REFERENCE SIGNS LIST 1 Fluidized bed sludge incinerator 3 Incinerator body 4 Furnace outlet 5 Sludge supply device 6 Sludge inlet 7 Primary air supply section 9 Secondary air supply section 10 Sand layer temperature measuring device 11 Freeboard temperature measuring device 12 Flue duct 13 Exhaust gas temperature measuring device 14 CO concentration measuring device 15 Air preheater 17 Fluidized sand 19 Air supply nozzle 21 Fluidized blower 23 Cooling blower 25 Air cooler 27 Control device 28 Total air supply piping 29 Primary air supply piping 30 Secondary air supply piping 31 Total air volume control valve 32 Secondary air volume control valve 33 Ceramic filter 34 Smoke washing treatment tower 35 Induced draft fan 36 Chimney F Freeboard section M Sludge S Sand layer section
Claims (12)
前記砂層部に設けられ、砂層の複数箇所の温度を測定する複数個の温度測定器と、
前記温度測定器によって測定された砂層の温度の最高温度と最低温度との温度差と前記温度差の変化速度を計算し、その温度差の変化速度の値に基づいて前記砂層部に供給される一次空気量を決定し、前記砂層部に供給される一次空気量を制御する制御装置であって、前記温度差の変化速度が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差の変化速度が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御する制御装置と、
を有することを特徴とする流動床式汚泥焼却炉。 A fluidized bed sludge incinerator having a sand layer and a freeboard formed above the sand layer, in which sludge is burned,
a plurality of temperature measuring devices provided in the sand layer portion for measuring the temperature of a plurality of locations in the sand layer;
a control device that calculates the temperature difference between the maximum and minimum temperatures of the sand layer measured by the temperature measuring device and the rate of change of said temperature difference, determines the amount of primary air to be supplied to said sand layer section based on the value of the rate of change of said temperature difference, and controls the amount of primary air to be supplied to said sand layer section, so that when the rate of change of said temperature difference exceeds a predetermined upper limit value, the amount of primary air to be supplied to said sand layer section is increased, and when the rate of change of said temperature difference falls below a predetermined lower limit value, the control device controls so that the amount of primary air to be supplied to said sand layer section is decreased;
A fluidized bed sludge incinerator comprising:
前記制御装置が、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を減少させ、前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を増加させるように制御する制御装置であることを特徴とする請求項１～３のいずれかに記載の流動床式汚泥焼却炉。 a CO concentration measuring device for measuring the CO concentration in the exhaust gas discharged from the furnace outlet of the incinerator body of the fluidized bed sludge incinerator;
The fluidized bed sludge incinerator according to any one of claims 1 to 3, characterized in that the control device is a control device that controls so as to reduce the amount of primary air supplied to the sand layer when the CO concentration in the exhaust gas measured by the CO concentration meter exceeds a predetermined CO concentration upper limit value, and to increase the amount of primary air supplied to the sand layer when the CO concentration in the exhaust gas measured by the CO concentration meter falls below a predetermined CO concentration lower limit value.
前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％増加させるように制御する制御装置であることを特徴とする請求項４に記載の流動床式汚泥焼却炉。 the control device reduces the amount of primary air supplied to the sand layer by 1 to 5% when the CO concentration in the exhaust gas measured by the CO concentration measuring device exceeds a predetermined CO concentration upper limit value;
The fluidized bed sludge incinerator according to claim 4, characterized in that the control device controls the amount of primary air supplied to the sand layer to be increased by 1 to 5% when the CO concentration in the exhaust gas measured by the CO concentration measuring device falls below a predetermined CO concentration lower limit value.
前記砂層部に、異なる位置の砂層の温度を測定する複数個の温度測定器を設け、
前記温度測定器によって測定された砂層の温度の最高温度と最低温度との温度差と前記温度差の変化速度を計算し、前記温度差の変化速度が所定の上限値を超えた場合には、前記砂層部に供給される一次空気量を増加させ、前記温度差の変化速度が所定の下限値を下回った場合には、前記砂層部に供給される一次空気量を減少させるように制御することを特徴とする、流動床式汚泥焼却炉の自動燃焼制御方法。 1. An automatic combustion control method for a fluidized bed sludge incinerator that has a sand layer and a freeboard formed above the sand layer and burns introduced sludge, comprising:
a plurality of temperature measuring devices for measuring the temperature of the sand layer at different positions are provided in the sand layer section;
The method for automatic combustion control of a fluidized bed sludge incinerator comprises calculating the temperature difference between the maximum and minimum temperatures of the sand layer measured by the temperature measuring device and the rate of change of said temperature difference, and controlling the amount of primary air supplied to said sand layer to increase if the rate of change of said temperature difference exceeds a predetermined upper limit value, and decreasing the amount of primary air supplied to said sand layer if the rate of change of said temperature difference falls below a predetermined lower limit value.
前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度上限値を超えた場合には、前記砂層部に供給される一次空気量を減少させ、
前記ＣＯ濃度測定器で測定した前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を増加させることを特徴とする請求項７～９のいずれかに記載の流動床式汚泥焼却炉の自動燃焼制御方法。 The CO concentration in the exhaust gas discharged from the furnace outlet of the incinerator body of the fluidized bed sludge incinerator is measured with a CO concentration measuring device;
When the CO concentration in the exhaust gas measured by the CO concentration measuring device exceeds a predetermined CO concentration upper limit value, the amount of primary air supplied to the sand layer portion is reduced,
The automatic combustion control method for a fluidized bed sludge incinerator according to any one of claims 7 to 9, characterized in that when the CO concentration in the exhaust gas measured by the CO concentration measuring device falls below a predetermined CO concentration lower limit value, the amount of primary air supplied to the sand layer section is increased.
前記排ガス中のＣＯ濃度が所定のＣＯ濃度下限値を下回った場合には、前記砂層部に供給される一次空気量を１～５％増加させることを特徴とする請求項１０に記載の流動床式汚泥焼却炉の自動燃焼制御方法。 When the CO concentration in the exhaust gas exceeds a predetermined CO concentration upper limit value, the amount of primary air supplied to the sand layer is reduced by 1 to 5%;
The automatic combustion control method for a fluidized bed sludge incinerator according to claim 10 , characterized in that when the CO concentration in the exhaust gas falls below a predetermined CO concentration lower limit, the amount of primary air supplied to the sand layer is increased by 1 to 5%.
The automatic combustion control method for a fluidized bed sludge incinerator according to claim 10 or 11 , characterized in that the predetermined CO concentration upper limit value is 10 to 20 PPM, and the predetermined CO concentration lower limit value is 0 to 10 PPM.
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