JP2007029918A - NOx REDUCTION METHOD FOR EXHAUST GAS OF PLASMA TYPE ASH MELTING FURNACE - Google Patents
NOx REDUCTION METHOD FOR EXHAUST GAS OF PLASMA TYPE ASH MELTING FURNACE Download PDFInfo
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Abstract
Description
本発明は、ノントランスファ方式のプラズマトーチを加熱源に用いた灰溶融炉から排出されるガス中の高濃度NOxを、還元剤としてアンモニアを用いて選択的に還元し、後流に設置する排ガス処理システムヘの浄化負荷を低減することを企図したものである。 The present invention selectively removes high concentration NOx in a gas discharged from an ash melting furnace using a non-transfer type plasma torch as a heating source using ammonia as a reducing agent and installs it in the downstream. It is intended to reduce the purification load on the processing system.
一般に、ノントランスファ方式のプラズマトーチの作動ガスには空気が用いられる。プラズマトーチ内では、作動ガスである空気が3000℃を超える高温まで昇温されるため、空気中の窒素が酸素により酸化され、30000ppmを越える高濃度のNOxが生成される。この高濃度NOxを分解するために高度な排ガス処理技術が求められる。そのため、湿式の排ガス処理や、高濃度硝酸系窒素を処理できる排水処理装置や、多量の脱硝触媒を用いなくてはならなかった。
本発明は、上記の問題点に鑑み、ノントランスファ方式のプラズマ溶融炉から排出されるNOx含有排ガスを排ガス処理装置へ導入する前にNOx濃度を低減しておくことで、排ガス処理装置への浄化負荷を低減させ、一般的な燃焼排ガス処理装置にて上記排ガスを浄化するものである。 In view of the above problems, the present invention reduces the NOx concentration before introducing NOx-containing exhaust gas discharged from a non-transfer type plasma melting furnace into the exhaust gas treatment device, thereby purifying the exhaust gas treatment device. The load is reduced and the exhaust gas is purified by a general combustion exhaust gas treatment device.
請求項1による発明は、
ノントランスファ方式のプラズマ溶融炉から排出されるNOx含有排ガスを無触媒還元脱硝処理に付すに当たり、還元剤を希釈媒体にて希釈し、得られた希釈還元剤を排ガスに添加し、無触媒反応ゾーンまたは無触媒反応器内における還元剤濃度を還元剤の可燃範囲以下にすることを特徴とする、ノントランスファ方式のプラズマ溶融炉排ガスの高濃度NOx低減方法である。
The invention according to
When the NOx-containing exhaust gas discharged from the non-transfer type plasma melting furnace is subjected to non-catalytic reduction and denitration treatment, the reducing agent is diluted with a diluent medium, and the resulting diluted reducing agent is added to the exhaust gas to provide a non-catalytic reaction zone. Alternatively, the present invention is a method for reducing the high concentration NOx of non-transfer type plasma melting furnace exhaust gas, characterized in that the reducing agent concentration in the non-catalyst reactor is set below the flammable range of the reducing agent.
請求項2による発明は、
無触媒反応ゾーンまたは無触媒反応器の前流において排ガスに冷却用ガスを投入して無触媒反応ゾーンまたは無触媒反応器内の温度をコントロールし、および/または、無触媒反応ゾーンまたは無触媒反応器内において排ガスに希釈還元剤を添加することで無触媒反応ゾーンまたは無触媒反応器内の温度をコントロールする、請求項1記載の方法である。
The invention according to
Control the temperature in the non-catalytic reaction zone or non-catalytic reactor by introducing a cooling gas into the exhaust gas in the upstream of the non-catalytic reaction zone or non-catalytic reactor, and / or the non-catalytic reaction zone or non-catalytic reaction The method according to
請求項3による発明は、
無触媒反応ゾーンまたは無触媒反応器内における排ガス温度が800〜900℃である請求項1記載の方法である。
The invention according to
The method according to
請求項4による発明は、
希釈媒体が空気、水蒸気または不活性ガスである請求項1記載の方法である。
The invention according to claim 4
The method of
請求項5による発明は、
処理前のNOx含有排ガス中の酸素濃度が15〜30vol%である請求項1記載の方法である。
The invention according to claim 5
The method according to
請求項6による発明は、
処理前のNOx含有排ガス中のNOx濃度が10000〜30000ppmである請求項1記載の方法である。
The invention according to claim 6
The method according to
請求項7による発明は、
還元剤がアンモニアであり、希釈還元剤中の還元剤濃度が1〜25vol%であり、および/または、無触媒反応ゾーンまたは無触媒反応器内における平均還元剤が0.4〜10vol%である請求項1記載の方法である。
The invention according to claim 7
The reducing agent is ammonia, the reducing agent concentration in the diluted reducing agent is 1 to 25 vol%, and / or the average reducing agent in the noncatalytic reaction zone or the noncatalytic reactor is 0.4 to 10 vol%. The method of
請求項8による発明は、
還元剤が尿素であり、尿素の分解で生じるアンモニアの希釈還元剤中濃度が1〜25vol%であり、および/または、無触媒反応ゾーンまたは無触媒反応器内における平均還元剤が0.4〜10vol%である請求項1記載の方法である。
The invention according to claim 8 provides:
The reducing agent is urea, the concentration of ammonia produced by decomposition of urea is 1 to 25 vol%, and / or the average reducing agent in the non-catalytic reaction zone or the non-catalytic reactor is 0.4 to The method according to
本発明方法によれば、希釈還元剤を用いることで、ノントランスファ方式のプラズマトーチを加熱源に用いた灰溶融炉から排出されるガス中の高濃度NOxを高脱硝率で除去することができ、これにより後流に設置する排ガス処理システムヘの浄化負荷を低減することができる。 According to the method of the present invention, by using a dilute reducing agent, it is possible to remove high-concentration NOx in gas discharged from an ash melting furnace using a non-transfer type plasma torch as a heating source with a high denitration rate. Thus, the purification load on the exhaust gas treatment system installed downstream can be reduced.
つぎに、本発明を具体的に説明するために、本発明の実施例およびこれとの比較を示すための比較例をいくつか挙げる。 Next, in order to specifically explain the present invention, some examples of the present invention and comparative examples for showing comparison with the examples will be given.
実施例1
空気を作動ガスに用いるノントランスフア式プラズマトーチからは、30000ppmを越えるNOxを含む高温の空気が排出される。この排ガスを3秒程度滞留させることができる無触媒脱硝反応器を設け、排ガスを反応器へ流入する前に空気希釈することで排ガス温度を800〜900℃の範囲で調整し、反応器入ロから希釈していないアンモニアと、空気にて約10倍に空気希釈したアンモニアを注入し、反応器出口NOx濃度を計測する試験を行った。この結果、好条件では、99%を超える脱硝効果を得た。この結果を図1に示す。
Example 1
High-temperature air containing NOx exceeding 30000 ppm is discharged from a non-transfer type plasma torch that uses air as a working gas. A non-catalytic denitration reactor capable of retaining this exhaust gas for about 3 seconds is provided, and the exhaust gas temperature is adjusted in the range of 800 to 900 ° C. by diluting the exhaust gas before flowing into the reactor. The test was performed by injecting undiluted ammonia and air diluted about 10 times with air and measuring the NOx concentration at the outlet of the reactor. As a result, under favorable conditions, a denitration effect exceeding 99% was obtained. The result is shown in FIG.
この試験結果より、下記のことが判明した。 From the test results, the following was found.
○無触媒脱硝を高効率に進めるためには、アンモニアの可燃濃度範囲を下回る濃度に希釈する必要がある。 ○ In order to promote non-catalytic denitration with high efficiency, it is necessary to dilute to a concentration below the flammable concentration range of ammonia.
○反応時のガス温度が低いと、脱硝反応が進みにくい。 ○ If the gas temperature during the reaction is low, the denitration reaction is difficult to proceed.
○反応時のガス温度が高いと、アンモニアの可燃範囲が広がり、燃焼反応が進むため、脱硝反応が進みにくい。 ○ If the gas temperature during the reaction is high, the flammable range of ammonia is expanded and the combustion reaction proceeds, so the denitration reaction is difficult to proceed.
○ガス温度が高い場合、アンモニアの燃焼反応が進み、未反応残留アンモニアのリークがなくなる。 ○ When the gas temperature is high, the combustion reaction of ammonia proceeds and there is no leakage of unreacted residual ammonia.
○空気希釈アンモニアを高速で崖入し、撹拌が重要である。 ○ Stirring is important because the air-diluted ammonia enters the cliff at high speed.
つぎに、本発明による、ノントランスファ方式のプラズマ溶融炉排ガスのNOx低減方法を、従来技術と比較して示す。 Next, a method for reducing NOx of the non-transfer type plasma melting furnace exhaust gas according to the present invention will be described in comparison with the prior art.
本発明方法および従来法における脱硝性能データと性能比較データを図1〜図3に示す。なお、それぞれのテスト条件は表lの通りである。 Denitration performance data and performance comparison data in the method of the present invention and the conventional method are shown in FIGS. Each test condition is as shown in Table 1.
ノントランスファ方式のプラズマ溶融炉を用いる選択的無触媒還元では、従来法に比べて、100℃程度低い温度で高い脱硝性能が得られる。その理由として、排ガス中のNOx濃度の違いが考えられる。ノントランスファ方式のプラズマ溶融法では10000〜30000ppmのNOxが発生する。これに比べてボイラー排ガスやごみ焼却排ガスではNOx濃度は100〜200ppmであり、当然選択的無触媒還元法のために投入するNH3 も多く必要で、NOxとNH3 の接触効率が高くなることが考えられる。
ボイラー排ガスやごみ焼却排ガスにおいて、従来行われていた選択的無触媒還元法は、そのほとんどが焼却炉内へのアンモニアや尿素の吹込みからなり、炉内温度800〜900℃程度でアンモニア比1〜1.5で脱硝率は40〜50%であった。脱硝率を高めようとすると高アンモニア比での反応が必要になり、リークアンモニアが急激に増加する。特に炉内吹込みの場合には、偏流や高温火炎等の影響で高い脱硝性能が得られない。 In the case of boiler exhaust gas and waste incineration exhaust gas, the selective non-catalytic reduction methods that have been conventionally carried out consist mainly of injecting ammonia or urea into the incinerator, with an in-furnace temperature of about 800 to 900 ° C. and an ammonia ratio of 1 The NOx removal rate was 40 to 50% at ˜1.5. In order to increase the denitration rate, a reaction at a high ammonia ratio is required, and the leaked ammonia increases rapidly. In particular, in the case of in-furnace blowing, high denitration performance cannot be obtained due to the influence of drift or high-temperature flame.
ノントランスファ方式のプラズマ灰溶融炉排ガス処理では、炉内温度が1400〜1500℃程度で、炉内吹込みによる選択的無触媒還元は不可能である(アンモニアの燃焼が早くて脱硝効率が低い)。幸い、ノントランスファ方式プラズマ灰溶融炉排ガス処理では排ガス量がボイラーやごみ焼却の排ガス量に比べて少ないことから、脱硝反応室を炉と分離した形で設け、脱硝反応室前流で空気吹込みによる排ガス温度調整を行うとともに、還元剤であるアンモニアを吹込み、これを空気で希釈し、NOxとアンモニアの混合性を高めた。 In the non-transfer type plasma ash melting furnace exhaust gas treatment, the furnace temperature is about 1400-1500 ° C., and selective non-catalytic reduction by in-furnace blowing is impossible (ammonia combustion is fast and denitration efficiency is low) . Fortunately, in the non-transfer type plasma ash melting furnace exhaust gas treatment, the amount of exhaust gas is small compared to the amount of exhaust gas from boilers and waste incineration, so a denitration reaction chamber is separated from the furnace, and air is blown in the upstream of the denitration reaction chamber The temperature of the exhaust gas was adjusted, and ammonia as a reducing agent was blown in, and this was diluted with air to improve the mixing ability of NOx and ammonia.
ボイラー炉やごみ焼却炉では炉内幅および高さが数mもあるので混合性を高めるのは困難であるが、ノントランスファー式プラズマ灰溶融炉排ガス処理装置では、脱硝反応室は炉内と分離しているので排ガス自身の偏流も少なく、脱硝反応室の幅および高さは1m未満であり、希釈空気による混合性がよい。また、ノントランスファー式プラズマ灰溶融炉排ガス処理の場合には、NOx濃度が高い分、投入するアンモニア量も多く、このアンモニアが脱硝反応前に燃焼・酸化されると計算上200〜300℃程度の排ガス温度の上昇を招き、反応操作のコントロールができない。投入アンモニアを希釈して燃焼・酸化を抑
え、脱硝反応を優先させてやることにより、発熱反応が緩やかになり、反応操作のコントロール可能になる。
It is difficult to improve the mixing properties of boiler furnaces and waste incinerators because the furnace width and height are several meters, but in non-transfer type plasma ash melting furnace exhaust gas treatment equipment, the denitration reaction chamber is separated from the inside of the furnace. Therefore, the drift of the exhaust gas itself is small, the width and height of the denitration reaction chamber are less than 1 m, and the mixing property by dilution air is good. Further, in the case of non-transfer type plasma ash melting furnace exhaust gas treatment, the amount of ammonia to be added is large due to the high NOx concentration. If this ammonia is burned and oxidized before the denitration reaction, it is calculated to be about 200 to 300 ° C. The exhaust gas temperature rises and the reaction operation cannot be controlled. By diluting the input ammonia to suppress combustion / oxidation and giving priority to the denitration reaction, the exothermic reaction becomes moderate and the reaction operation can be controlled.
実施例2
空気希釈されたアンモニアを還元剤として用い、無触媒反応ゾーン(反応器)内におけるアンモニア濃度(空気希釈)10vol%、モル比(NH /NOx)0.9〜1.0、反応温度850℃、反応時間約1.5秒で、無触媒脱硝反応を行った。この場合の還元剤濃度と脱硝率の関係を図4のグラフに示す。
Example 2
Using ammonia diluted in air as a reducing agent, ammonia concentration (air dilution) in a non-catalytic reaction zone (reactor) 10 vol%, molar ratio (NH / NOx) A non-catalytic denitration reaction was performed at 0.9 to 1.0, a reaction temperature of 850 ° C., and a reaction time of about 1.5 seconds. The relationship between the reducing agent concentration and the denitration rate in this case is shown in the graph of FIG.
実施例3
還元剤として尿素を用い、尿素の分解により生じたアンモニアの、無触媒反応ゾーン(反応器)内における濃度(空気希釈)10vol%、モル比(NH /NOx)0.9〜1.0、反応温度850℃、反応時間約1.5秒で、無触媒脱硝反応を行った。この場合の還元剤濃度と脱硝率の関係を図4のグラフに示す。
Example 3
Using urea as a reducing agent, the concentration of ammonia produced by the decomposition of urea in the non-catalytic reaction zone (reactor) (air dilution) 10 vol%, molar ratio (NH / NOx) A non-catalytic denitration reaction was performed at 0.9 to 1.0, a reaction temperature of 850 ° C., and a reaction time of about 1.5 seconds. The relationship between the reducing agent concentration and the denitration rate in this case is shown in the graph of FIG.
実施例4
空気希釈されたアンモニア(濃度:8vol%)を還元剤として用い、反応温度850℃で無触媒脱硝反応を行った。この場合の無触媒反応ゾーン(反応器)内におけるNOx含有排ガス滞留時間と脱硝率の関係を図5のグラフに示す。
Example 4
Non-catalytic denitration reaction was performed at a reaction temperature of 850 ° C. using ammonia diluted in air (concentration: 8 vol%) as a reducing agent. The relationship between the NOx-containing exhaust gas residence time and the denitration rate in the non-catalytic reaction zone (reactor) in this case is shown in the graph of FIG.
Claims (8)
The reducing agent is urea, the concentration of ammonia produced by decomposition of urea is 1 to 25 vol%, and / or the average reducing agent in the non-catalytic reaction zone or the non-catalytic reactor is 0.4 to The method according to claim 1, which is 10 vol%.
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