JP2005125261A - Method and device for removing mercury in boiler exhaust gas - Google Patents
Method and device for removing mercury in boiler exhaust gas Download PDFInfo
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本発明は、石炭焚きボイラの排ガスに含まれる水銀を除去する方法及び装置に関する。更に詳しくは、少なくとも排ガスの脱硫工程若しくは排ガスの集塵工程を有する、石炭焚きボイラの排ガスを処理する工程において、塩素化合物を用いて排ガス中の水銀を除去する方法及び装置に関する。 The present invention relates to a method and apparatus for removing mercury contained in exhaust gas from a coal fired boiler. More particularly, the present invention relates to a method and apparatus for removing mercury in exhaust gas using a chlorine compound in a process of treating exhaust gas from a coal fired boiler, which has at least a desulfurization process of exhaust gas or a dust collection process of exhaust gas.
発電プラントなどで、微粉炭を燃焼する石炭焚きボイラに用いる石炭には、各種微量金属が含まれるので、これら金属若しくは金属化合物はボイラ排ガス中にも含まれて排出される。特に、水銀は着目物質の中のひとつで、その排ガス中含有量の０．０１〜０．００１ｐｐｍレベルの濃度が問題視される。 Since coal used in a coal-fired boiler that burns pulverized coal in a power plant or the like contains various trace metals, these metals or metal compounds are also contained in the boiler exhaust gas and discharged. In particular, mercury is one of the substances of interest, and the concentration of 0.01 to 0.001 ppm level of the content in exhaust gas is regarded as a problem.
通常このようなボイラ設備では、排ガスの処理装置として、脱硫装置や集塵装置をそなえているので、それにより排ガス中の５〜７割の水銀は除去されるが、３〜５割は排ガス中に含まれて排出してしまう。よって対策が必要である。排ガス中の水銀は遊離の金属水銀として存在するか、一部石炭に本来的に含まれる塩素と化合して水銀塩（塩化水銀）の形で存在するが、前記脱硫装置での水への溶解性や集塵装置でのアッシュへの吸着性は、水銀塩（塩化水銀）の形の方が、格段に大きい。従って、遊離の水銀を塩化水銀へ変化させることが、水銀除去率を高める有効な手段である。 Usually, such a boiler facility is equipped with a desulfurization device and a dust collector as an exhaust gas treatment device, thereby removing 50 to 70% of mercury in the exhaust gas, but 30 to 50% is in the exhaust gas. It is contained and discharged. Therefore, countermeasures are necessary. Mercury in the exhaust gas exists as free metallic mercury or some forms of mercury salt (mercury chloride) combined with chlorine originally contained in coal, but dissolved in water in the desulfurization unit In the form of mercury salt (mercury chloride), the ash and the adsorptivity to ash in the dust collector are much greater. Therefore, changing free mercury to mercury chloride is an effective means of increasing the mercury removal rate.
特許文献１では、石炭類をボイラのような燃焼装置で燃焼する際、該石炭類に予め塩素化合物を添加して燃焼させ、次いで該燃焼装置の後流に設置された集塵装置で排ガス中のばい塵を除去、回収する方法を開示している。 In Patent Document 1, when coal is burned in a combustion device such as a boiler, a chlorine compound is previously added to the coal for combustion, and then in the exhaust gas by a dust collector installed downstream of the combustion device. A method for removing and collecting soot and dust is disclosed.
この方法は、ボイラ火炉に直接塩素化合物を投入することになるので、一つには、ボイラ火炉壁、過熱器、節炭器など火炉内電熱面の極力腐蝕から防護すべき部位に、高濃度の塩素化合物を触れさせる事になり、ボイラ保守の寿命を短縮する。更に、火炉内における、１４００℃近辺の高温の条件下では、例えば、有利水銀と塩酸とから塩化水銀が生成する平衡反応で、その平衡が生成系の方へほとんど移動せず、有利水銀のほうが、安定な熱的条件となるので、水銀塩の生成条件としては適していない。 In this method, chlorine compounds are directly fed into the boiler furnace. For one reason, high concentrations are applied to parts that should be protected from corrosion on the electric surface of the furnace, such as boiler furnace walls, superheaters, and economizers. This will shorten the life of boiler maintenance. Furthermore, under conditions of high temperature around 1400 ° C. in the furnace, for example, an equilibrium reaction in which mercury chloride is generated from advantageous mercury and hydrochloric acid, the equilibrium hardly moves toward the production system. Since it is a stable thermal condition, it is not suitable as a mercury salt production condition.
従って、本発明は上記従来の技術の問題点に鑑み、火炉内伝熱面の腐蝕を防止しつつ、石炭含有の水銀に由来する石炭焚きボイラの排ガス中の水銀を、向上した除去率にて除去する方法及び装置の提供を目標とする。 Therefore, in view of the above-mentioned problems of the conventional technology, the present invention prevents mercury on the heat transfer surface in the furnace while reducing the mercury in the exhaust gas of the coal fired boiler derived from coal-containing mercury with an improved removal rate. The goal is to provide a method and apparatus for removal.
本発明のボイラ排ガス中の水銀除去方法は、少なくとも排ガスの脱硫工程若しくは排ガスの集塵工程を有する、石炭焚きボイラの排ガスを処理する工程において、ボイラ下流側で、１００〜３５０℃の温度域を保つ排ガス処理経路中に、排ガス中の全塩素濃度が３５０ｐｐｍを超えない範囲で、塩素化合物を投入することを特徴とする。 The method for removing mercury in boiler exhaust gas according to the present invention includes at least a desulfurization process for exhaust gas or a dust collection process for exhaust gas, and a process for treating exhaust gas from a coal-fired boiler at a temperature range of 100 to 350 ° C. on the downstream side of the boiler. In the exhaust gas treatment path to be maintained, a chlorine compound is introduced in a range where the total chlorine concentration in the exhaust gas does not exceed 350 ppm.
前記したように、高温域で塩素化合物を投入することは、ボイラシステムにおける高度な保守性を必要とする部位に塩素化合物を触れさせることになること、高温域では成果物としたい塩化水銀が、むしろ解離して、遊離の水銀となることから、中温域の１００〜３５０℃の温度域に保たれており、一定の反応時間を保つことができて、生成した塩化水銀が、経路中の排ガスの処理手段で除去可能な場所に投入することとした。 As described above, when a chlorine compound is introduced in a high temperature range, the chlorine compound is brought into contact with a site requiring high maintainability in the boiler system, and in the high temperature range, mercury chloride to be a product is obtained. Rather, since it is dissociated and becomes free mercury, it is kept in a temperature range of 100 to 350 ° C. in the middle temperature range, and can maintain a certain reaction time, and the generated mercury chloride is exhaust gas in the path. It was decided to put it in a place where it can be removed by the above processing means.
温度域の選択についての下限域の１００℃は、これに満たない低温では、経路中の滞留時間内で、完全な塩素化が進行せず、上限域の３５０℃をこえると、前記したように、反応平衡が不利な方向へ移動すること、しかも腐蝕性が高くなることによる。しかし、好ましくは１００〜３００℃の範囲がよい。 The lower limit of 100 ° C. for the selection of the temperature range is as follows. At a low temperature less than this, complete chlorination does not proceed within the residence time in the path, and the upper limit range of 350 ° C. is exceeded. This is because the reaction equilibrium moves in an unfavorable direction and the corrosivity becomes high. However, the range of 100 to 300 ° C. is preferable.
排ガス中の全塩素濃度については、３５０ｐｐｍを越えると、特に腐蝕性が目立ち、装置の保守上からこのましくない。また下限については、特に限定しないが、１０ｐｐｍ未満では、系内の全水銀に対する塩素化反応の反応率が低く満足な除去効果が得られない。ここで全塩素濃度とは、燃料石炭中に含まれて、入る塩素量と系内に添加する塩素量との総和から求められる塩素濃度である。 When the total chlorine concentration in the exhaust gas exceeds 350 ppm, the corrosiveness is particularly noticeable, which is not preferable from the viewpoint of maintenance of the apparatus. Further, the lower limit is not particularly limited, but if it is less than 10 ppm, the reaction rate of the chlorination reaction with respect to the total mercury in the system is low, and a satisfactory removal effect cannot be obtained. Here, the total chlorine concentration is a chlorine concentration obtained from the sum of the amount of chlorine contained in the fuel coal and added to the system.
用いる塩素化合物は、前記温度範囲で水銀と反応性を示すものなら特に限定はないが、塩酸、塩素などの揮発性物質、塩化ナトリウム、塩化カリウム、塩化カルシウム、などの金属塩、塩化アンモニュウムなどのアンモニュウム塩、有機アミンの塩酸塩、塩化メチル、クロルベンゼンなどの有機塩化物が例として揚げることができる。 The chlorine compound to be used is not particularly limited as long as it is reactive with mercury in the above temperature range, but volatile substances such as hydrochloric acid and chlorine, metal salts such as sodium chloride, potassium chloride and calcium chloride, ammonium chloride and the like. Organic chlorides such as ammonium salts, hydrochlorides of organic amines, methyl chloride, chlorobenzene can be used as examples.
投入する時の形態は、ガス状、水溶液状、微粉状などを、物質によって選択することができる。 The form at the time of charging can be selected from substances such as gas, aqueous solution, and fine powder.
更に、本発明のボイラ排ガス中の水銀除去方法は、前記塩素化合物を投入する排ガス処理経路が、排ガスの脱硫装置入り口であることを特徴とする。 Further, the method for removing mercury in boiler exhaust gas according to the present invention is characterized in that the exhaust gas treatment path into which the chlorine compound is introduced is an exhaust gas desulfurization apparatus inlet.
これにより、脱硫装置内で塩化水銀が反応生成するとともに、該塩化水銀は脱硫装置に加えられる脱硫剤中に溶解して、除去される。 Thereby, mercury chloride reacts and generates in the desulfurization apparatus, and the mercury chloride is dissolved and removed in the desulfurization agent added to the desulfurization apparatus.
更に、本発明のボイラ排ガス中の水銀除去方法は、前記塩素化合物を投入する排ガス処理経路が、排ガスの脱硫装置空間であって、前記塩素化合物を湿式脱硫装置の脱硫剤溶液中に溶解して投入することを特徴とする。 Further, in the method for removing mercury in boiler exhaust gas of the present invention, the exhaust gas treatment path into which the chlorine compound is introduced is an exhaust gas desulfurization device space, and the chlorine compound is dissolved in a desulfurization agent solution of a wet desulfurization device. It is characterized by charging.
更に、本発明のボイラ排ガス中の水銀除去方法は、前記塩素化合物を投入する排ガス処理経路が、排ガスの集塵装置入り口であることを特徴とする。 Further, the method for removing mercury in boiler exhaust gas according to the present invention is characterized in that the exhaust gas treatment path into which the chlorine compound is introduced is an exhaust gas dust collector entrance.
これにより、集塵装置内で塩化水銀が反応生成するとともに、該塩化水銀は集塵装置内に滞留するフライアッシュに吸着されて、除去される。 Thereby, mercury chloride reacts and is generated in the dust collector, and the mercury chloride is adsorbed and removed by the fly ash staying in the dust collector.
更に、本発明の他の側面であるボイラ排ガス中の水銀除去装置は、少なくとも排ガスの脱硫装置若しくは排ガスの集塵装置を有する、石炭焚きボイラの排ガスを処理する装置において、ボイラ下流側で、１００〜３００℃の温度域を保つ排ガス処理経路中に接続され、排ガス中の全塩素濃度が３５０ｐｐｍを超えない範囲で、塩素化合物を投入する塩素化合物投入手段を有することを特徴とする。 Furthermore, a mercury removing apparatus for boiler exhaust gas according to another aspect of the present invention is an apparatus for treating exhaust gas from a coal-fired boiler having at least an exhaust gas desulfurization apparatus or an exhaust gas dust collector. It is connected to an exhaust gas treatment path maintaining a temperature range of ˜300 ° C., and has a chlorine compound charging means for charging a chlorine compound in a range where the total chlorine concentration in the exhaust gas does not exceed 350 ppm.
塩素化合物投入手段は投入物質の形態によるが、例えば水溶液として添加する場合、予め調整した塩化物水溶液を保留する塩化物タンク、該タンクより前記経路に定量的に圧入可能なポンプを備え、その圧入口を投入箇所に配管で接続された塩素化合物投入手段であることができる。また、ガス状の場合は、投入物質の装填されたガスボンベ、流量を調節できる弁を備え、その圧入口を投入箇所に配管で接続された塩素化合物投入手段であることができる。更に、系内の全塩素濃度を検出して、その値により、流量を制御可能な制御装置を備えても良い。 The chlorine compound charging means depends on the form of the charged substance. For example, when adding as an aqueous solution, the chlorine compound charging means includes a chloride tank for holding a previously prepared chloride aqueous solution, and a pump capable of quantitatively press-fitting into the path from the tank. It can be a chlorine compound charging means in which the inlet is connected to the charging point by piping. Further, in the case of a gaseous state, it can be a chlorine compound charging means provided with a gas cylinder charged with an input substance, a valve capable of adjusting the flow rate, and having a pressure inlet connected to the input position by piping. Furthermore, you may provide the control apparatus which can detect the total chlorine concentration in a system, and can control a flow volume by the value.
更に、本発明のボイラ排ガス中の水銀除去装置は、前記塩素化合物投入手段が、排ガスの脱硫装置入り口に接続されていることを特徴とする。 Furthermore, the mercury removing apparatus for boiler exhaust gas according to the present invention is characterized in that the chlorine compound charging means is connected to an exhaust gas desulfurization apparatus inlet.
更に、本発明のボイラ排ガス中の水銀除去装置は、前記塩素化合物を投入する排ガス処理経路が、排ガスの脱硫装置空間であって、前記塩素化合物を湿式脱硫装置の脱硫剤溶液中に溶解して投入することを可能とする塩素化合物投入手段を有することを特徴とする。 Further, in the apparatus for removing mercury in boiler exhaust gas according to the present invention, the exhaust gas treatment path into which the chlorine compound is introduced is an exhaust gas desulfurization device space, and the chlorine compound is dissolved in a desulfurization agent solution of a wet desulfurization device. It is characterized by having a chlorine compound charging means that can be charged.
更に、本発明のボイラ排ガス中の水銀除去装置は、前記塩素化合物投入手段が、排ガスの集塵装置入り口に接続されていることを特徴とする。 Furthermore, the mercury removing apparatus for boiler exhaust gas according to the present invention is characterized in that the chlorine compound charging means is connected to an exhaust gas dust collector inlet.
以上説明したように、本発明の効果は、以下のようにまとめることができる。
（１）適切な温度域を選んで塩素化合物を投入するようにしたため、遊離水銀から塩化銀の生成の平衡反応において、塩化水銀の生成系の側へ平衡が移動し、遊離水銀として残存しない。生成反応率が高い。加えて火炉中の伝熱面の腐蝕問題をさけることができる。
（２）更に、塩素化合物の濃度範囲を適切に選んだため、塩化銀の生成反応率が高く、同時に腐蝕トラブルを低く押さえることができる。
（３）前記構成と合わせて、脱塵工程（装置）、脱硫工程（装置）が塩化水銀の除去工程を果たし、全体として水銀除去率の向上した方法及び装置を提供している。
As described above, the effects of the present invention can be summarized as follows.
(1) Since an appropriate temperature range is selected and a chlorine compound is introduced, in the equilibrium reaction for producing silver chloride from free mercury, the equilibrium moves to the side of the mercury chloride producing system and does not remain as free mercury. The production reaction rate is high. In addition, the corrosion problem of the heat transfer surface in the furnace can be avoided.
(2) Furthermore, since the concentration range of the chlorine compound is appropriately selected, the silver chloride production reaction rate is high, and at the same time, corrosion troubles can be kept low.
(3) In combination with the above configuration, the dedusting process (apparatus) and the desulfurization process (apparatus) perform the mercury chloride removal process, thereby providing a method and apparatus with an improved mercury removal rate as a whole.
以下、図面を参照して本発明の好適な実施例を例示的に詳しく説明する。但しこの実施例に記載されている構成部品の寸法、材質、形状、その相対的配置等は特に特定的な記載がない限りは、この発明の範囲をそれに限定する趣旨ではなく、単なる説明例に過ぎない。 Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the components described in this embodiment are not intended to limit the scope of the present invention unless otherwise specified, but are merely illustrative examples. Not too much.
図１は本発明の水銀除去工程の第一の実施例を示すプロセスフローシートである。 FIG. 1 is a process flow sheet showing a first embodiment of the mercury removing process of the present invention.
図１において、ボイラ１は石炭を例えば微粉状で供給して、燃焼させるボイラであり燃焼ガスは、不図示の火炉水管、過熱器、節炭器などの伝熱面を過熱したあと排ガスとなって、排ガス処理経路に排出され、脱硫装置４で硫黄分が脱硫剤５によって除去され、エアヒータ７でボイラ１用の燃焼用空気をおよそ余熱し、集塵装置８で排ガス中のフライアッシュが除去された後、煙突９によって大気中に放出される。 In FIG. 1, a boiler 1 is a boiler that supplies coal, for example, in the form of fine powder and burns it. The combustion gas becomes exhaust gas after overheating a heat transfer surface such as a furnace water pipe, a superheater, and a economizer not shown. The sulfur is removed by the desulfurization agent 5 by the desulfurization device 4, the combustion air for the boiler 1 is preheated by the air heater 7, and the fly ash in the exhaust gas is removed by the dust collector 8. And then released into the atmosphere by the chimney 9.
実施例１の装置では、本発明に関わる塩素化合物投入手段２が、脱硫装置４の上流側入口付近に配管にて接続されている。塩素化合物投入手段２は、不図示の塩酸水溶液タンクと定量圧送ポンプを備え、該ポンプのサクション側は塩酸水溶液タンクの塩酸水溶液出口へ、デリベリ側は脱硫装置４の上流側入口付近に配管接続されている。実施例１の場合、塩素化合物３は塩酸（水溶液）である。塩酸水溶液は予め既定濃度に調整されてタンクに仕込まれ、塩酸水溶液は前記構成の塩素化合物投入手段２によって、脱硫装置内に定量供給される。脱硫装置内の平均排ガス温度は３００〜３５０℃である。本例の場合、脱硫装置の出口にて、適時にサンプリングし、全塩素濃度を検出し、その値によって、供給量を調節し、１５０ｐｐｍ前後とする。 In the apparatus of Example 1, the chlorine compound charging means 2 according to the present invention is connected by piping near the upstream inlet of the desulfurization apparatus 4. The chlorine compound charging means 2 includes a hydrochloric acid aqueous solution tank (not shown) and a constant pressure pump, and the suction side of the pump is connected to the hydrochloric acid aqueous solution outlet of the hydrochloric acid aqueous solution tank, and the delivery side is connected to the upstream side of the desulfurization apparatus 4 near the upstream side. ing. In the case of Example 1, the chlorine compound 3 is hydrochloric acid (aqueous solution). The aqueous hydrochloric acid solution is adjusted in advance to a predetermined concentration and charged into the tank, and the aqueous hydrochloric acid solution is supplied in a fixed amount into the desulfurization apparatus by the chlorine compound charging means 2 having the above-described configuration. The average exhaust gas temperature in the desulfurization apparatus is 300 to 350 ° C. In the case of this example, at the outlet of the desulfurization apparatus, sampling is performed in a timely manner, the total chlorine concentration is detected, and the supply amount is adjusted according to the value to be about 150 ppm.
塩化水銀はほとんどが、脱硫装置内で脱硫剤中の水に溶解して、除去されるが、その後の排ガス中に残存する塩化水銀は集塵装置のフライアッシュに吸着されて除去され、煙突から排出する排出ガス中の水銀濃度は検出限界以下である。また排ガス処理装置内での顕著な腐蝕現象は見出せなかった。 Most of the mercury chloride is dissolved in the water in the desulfurizing agent in the desulfurizer and removed, but the mercury chloride remaining in the exhaust gas after that is adsorbed and removed by the fly ash of the dust collector and removed from the chimney. The mercury concentration in the exhaust gas is below the detection limit. In addition, no significant corrosion phenomenon was found in the exhaust gas treatment apparatus.
図２は本発明の水銀除去工程の第二の実施例を示すプロセスフローシートである。 FIG. 2 is a process flow sheet showing a second embodiment of the mercury removing process of the present invention.
図２において、ボイラ１は石炭を例えば微粉状で供給して、燃焼させるボイラであり燃焼ガスは、不図示の火炉水管、過熱器、節炭器などの伝熱面を過熱したあと排ガスとなって、排ガス処理経路に排出され、脱硫装置４で硫黄分が脱硫剤５によって除去され、エアヒータ７でボイラ１用の燃焼用空気をおよそ余熱し、集塵装置８で排ガス中のフライアッシュが除去された後、煙突９によって大気中に放出される。 In FIG. 2, a boiler 1 is a boiler that supplies coal in the form of fine powder, for example, and burns it. The combustion gas becomes exhaust gas after overheating a heat transfer surface such as a furnace water pipe, a superheater, and a economizer not shown. The sulfur is removed by the desulfurization agent 5 by the desulfurization device 4, the combustion air for the boiler 1 is preheated by the air heater 7, and the fly ash in the exhaust gas is removed by the dust collector 8. And then released into the atmosphere by the chimney 9.
実施例２の装置では、本発明に関わる塩素化合物投入手段２が、脱硫装置４に接続されている不図示の攪拌器を備えた脱硫剤タンクに配管にて接続されている。塩素化合物投入手段２は、不図示の塩化アンモニュウム水溶液タンクと定量圧送ポンプを備え、該ポンプのサクション側は塩化アンモニュウム水溶液タンクの塩化アンモニュウム水溶液タンク出口へ、デリベリ側は脱硫タンク上部に配管接続されている。実施例２の場合、塩素化合物３は塩化アンモニュウム水溶液である。塩化アンモニュウム水溶液は予め既定濃度に調整されてタンクに仕込まれ、塩化アンモニュウム水溶液は前記構成の塩素化合物投入手段２によって、脱硫剤タンク内に定量供給される。そこで攪拌機によって脱硫剤に均一に混合される。混合された塩化アンモニュウムは脱硫剤とともに脱硫装置４内に導入されて、水銀を塩素化する。脱硫装置内の平均排ガス温度は３００〜３５０℃である。本例の場合、脱硫装置の出口にて、適時にサンプリングし、全塩素濃度を検出し、その値によって、塩化アンモニュウムの供給量を調節し、２００ｐｐｍ前後とする。 In the apparatus of Example 2, the chlorine compound charging means 2 according to the present invention is connected by piping to a desulfurization agent tank provided with a stirrer (not shown) connected to the desulfurization apparatus 4. The chlorine compound charging means 2 includes an ammonium chloride aqueous solution tank (not shown) and a metering pump. The suction side of the pump is connected to the ammonium chloride aqueous solution tank outlet of the ammonium chloride aqueous solution tank, and the delivery side is connected to the upper part of the desulfurization tank. Yes. In the case of Example 2, the chlorine compound 3 is an ammonium chloride aqueous solution. The aqueous ammonium chloride solution is adjusted in advance to a predetermined concentration and charged into the tank, and the aqueous ammonium chloride solution is quantitatively supplied into the desulfurizing agent tank by the chlorine compound charging means 2 having the above-described configuration. Therefore, it is uniformly mixed with the desulfurizing agent by a stirrer. The mixed ammonium chloride is introduced into the desulfurization apparatus 4 together with the desulfurizing agent to chlorinate mercury. The average exhaust gas temperature in the desulfurization apparatus is 300 to 350 ° C. In the case of this example, at the outlet of the desulfurization apparatus, sampling is performed in a timely manner, the total chlorine concentration is detected, and the supply amount of ammonium chloride is adjusted according to the value to be around 200 ppm.
塩化水銀はほとんどが、脱硫装置内で脱硫剤中の水に溶解して、除去されるが、その後の排ガス中に残存する塩化水銀は集塵装置のフライアッシュに吸着されて除去され、煙突から排出する排出ガス中の水銀濃度は検出限界以下である。また排ガス処理装置内での顕著な腐蝕現象は見出せなかった。 Most of the mercury chloride is dissolved in the water in the desulfurizing agent in the desulfurizer and removed, but the mercury chloride remaining in the exhaust gas after that is adsorbed and removed by the fly ash of the dust collector and removed from the chimney. The mercury concentration in the exhaust gas is below the detection limit. In addition, no significant corrosion phenomenon was found in the exhaust gas treatment apparatus.
図３は本発明の水銀除去工程の第三の実施例を示すプロセスフローシートである。 FIG. 3 is a process flow sheet showing a third embodiment of the mercury removing process of the present invention.
図３において、ボイラ１は石炭を例えば微粉状で供給して、燃焼させるボイラであり燃焼ガスは、不図示の火炉水管、過熱器、節炭器などの伝熱面を過熱したあと排ガスとなって、排ガス処理経路に排出され、脱硫装置４で硫黄分が脱硫剤５によって除去され、エアヒータ７でボイラ１用の燃焼用空気をおよそ余熱し、集塵装置８で排ガス中のフライアッシュが除去された後、煙突９によって大気中に放出される。 In FIG. 3, a boiler 1 is a boiler that supplies coal, for example, in the form of fine powder and burns it. The combustion gas becomes exhaust gas after overheating a heat transfer surface such as a furnace water pipe, a superheater, and a economizer not shown. The sulfur is removed by the desulfurization agent 5 by the desulfurization device 4, the combustion air for the boiler 1 is preheated by the air heater 7, and the fly ash in the exhaust gas is removed by the dust collector 8. And then released into the atmosphere by the chimney 9.
実施例３の装置では、本発明に関わる塩素化合物投入手段２が、集塵装置８の上流側入口付近に配管にて接続されている。塩素化合物投入手段２は、不図示の空気で希釈された希塩酸ガスボンベと流量を調節できる弁を備え、該弁を経由してボンベが集塵器上流側入口に接続された構成となっている。実施例３の場合、塩素化合物３は希釈された塩酸ガスである。塩酸ガスは予め既定濃度に希釈されボンベに充填され、希塩酸ガスは前記構成の塩素化合物投入手段２によって、集塵装置８内に定量供給される。集塵装置内の平均排ガス温度は１７０〜１５０℃である。本例の場合、集塵装置の出口にて、適時にサンプリングし、全塩素濃度を検出し、その値によって、供給量を調節し、１００ｐｐｍ前後とする。 In the apparatus of the third embodiment, the chlorine compound charging means 2 according to the present invention is connected by piping near the upstream side inlet of the dust collector 8. The chlorine compound charging means 2 includes a dilute hydrochloric acid gas cylinder diluted with air (not shown) and a valve capable of adjusting the flow rate, and the cylinder is connected to the upstream side of the dust collector via the valve. In the case of Example 3, the chlorine compound 3 is diluted hydrochloric acid gas. The hydrochloric acid gas is previously diluted to a predetermined concentration and filled in a cylinder, and the diluted hydrochloric acid gas is quantitatively supplied into the dust collector 8 by the chlorine compound charging means 2 having the above-described configuration. The average exhaust gas temperature in the dust collector is 170 to 150 ° C. In the case of this example, at the outlet of the dust collector, sampling is performed in a timely manner, the total chlorine concentration is detected, and the supply amount is adjusted according to the value to be about 100 ppm.
塩化水銀は集塵装置のフライアッシュに吸着されて除去され、煙突から排出する排出ガス中の水銀濃度は検出限界以下である。また排ガス処理装置内での顕著な腐蝕現象は見出せなかった。 Mercury chloride is adsorbed and removed by the fly ash of the dust collector, and the mercury concentration in the exhaust gas discharged from the chimney is below the detection limit. In addition, no significant corrosion phenomenon was found in the exhaust gas treatment apparatus.
本発明により火炉内伝熱面の腐蝕を防止しつつ、石炭含有の水銀に由来する石炭焚きボイラの排ガス中の水銀を、向上した除去率にて除去することが可能となり、大気汚染を防止して、発電などを行うことができ、埋蔵エネルギ源の有効な利用と電気エネルギなどを、環境を害することなく供給することを可能とし、産業上の寄与は大きい。 While preventing corrosion of the heat transfer surface in the furnace according to the present invention, it becomes possible to remove mercury in the exhaust gas of coal-fired boilers derived from coal-containing mercury with an improved removal rate, thereby preventing air pollution. Therefore, it is possible to generate electric power and the like, and it is possible to supply an effective use of an embedded energy source and electric energy without harming the environment, and the industrial contribution is great.
１ ボイラ
２ 塩素化合物投入手段
３ 塩素化合物
４ 脱硫装置
５ 脱硫剤
７ エアヒータ
８ 集塵装置
９ 煙突
DESCRIPTION OF SYMBOLS 1 Boiler 2 Chlorine compound input means 3 Chlorine compound 4 Desulfurization apparatus 5 Desulfurization agent 7 Air heater 8 Dust collector 9 Chimney
Claims (8)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2003365324A JP2005125261A (en) | 2003-10-24 | 2003-10-24 | Method and device for removing mercury in boiler exhaust gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2003365324A JP2005125261A (en) | 2003-10-24 | 2003-10-24 | Method and device for removing mercury in boiler exhaust gas |
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| JP2005125261A true JP2005125261A (en) | 2005-05-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2003365324A Withdrawn JP2005125261A (en) | 2003-10-24 | 2003-10-24 | Method and device for removing mercury in boiler exhaust gas |
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| JP (1) | JP2005125261A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100346865C (en) * | 2006-06-01 | 2007-11-07 | 上海交通大学 | Method for removing mercury for flue gas by using sulfo-halogen compound-supported modified adsorbent |
| DE102012214281A1 (en) | 2011-08-12 | 2013-02-14 | Babcock-Hitachi Kabushiki Kaisha | Desulphurising device for wet type exhaust gases and thermal power plant with same |
| JP2014149148A (en) * | 2014-03-10 | 2014-08-21 | Mitsubishi Heavy Ind Ltd | Mercury removal system and mercury removal method from high-temperature exhaust gas containing mercury |
| CN111397403A (en) * | 2020-03-23 | 2020-07-10 | 华南理工大学 | Boiler flue gas waste heat recovery system and method based on heat exchange absorption tower |
-
2003
- 2003-10-24 JP JP2003365324A patent/JP2005125261A/en not_active Withdrawn
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100346865C (en) * | 2006-06-01 | 2007-11-07 | 上海交通大学 | Method for removing mercury for flue gas by using sulfo-halogen compound-supported modified adsorbent |
| DE102012214281A1 (en) | 2011-08-12 | 2013-02-14 | Babcock-Hitachi Kabushiki Kaisha | Desulphurising device for wet type exhaust gases and thermal power plant with same |
| US9327236B2 (en) | 2011-08-12 | 2016-05-03 | Mitsubishi Hitachi Power Systems, Ltd. | Wet type flue-gas desulfurization method |
| JP2014149148A (en) * | 2014-03-10 | 2014-08-21 | Mitsubishi Heavy Ind Ltd | Mercury removal system and mercury removal method from high-temperature exhaust gas containing mercury |
| CN111397403A (en) * | 2020-03-23 | 2020-07-10 | 华南理工大学 | Boiler flue gas waste heat recovery system and method based on heat exchange absorption tower |
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