JPH06126127A - Method and apparatus for simultaneous treatment of dust collection and desulfurization - Google Patents
Method and apparatus for simultaneous treatment of dust collection and desulfurizationInfo
- Publication number
- JPH06126127A JPH06126127A JP4276899A JP27689992A JPH06126127A JP H06126127 A JPH06126127 A JP H06126127A JP 4276899 A JP4276899 A JP 4276899A JP 27689992 A JP27689992 A JP 27689992A JP H06126127 A JPH06126127 A JP H06126127A
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- JP
- Japan
- Prior art keywords
- desulfurization
- exhaust gas
- ash
- slurry
- coal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、大気汚染公害防止装置
に係わり、特に燃焼排ガス中の硫黄酸化物（ＳＯ2およ
びＳＯ3、以下ＳＯｘと記す。）を、コンパクトでシン
プルな形状を有し、かつ運転経費をも軽減でき、さらに
排ガス中の灰などの固形物を同時に処理できる脱硫方法
と装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an air pollution pollution control device, and in particular, it has a compact and simple shape of sulfur oxides (SO 2 and SO 3 , hereinafter referred to as SOx) in combustion exhaust gas. The present invention also relates to a desulfurization method and apparatus capable of reducing operating costs and simultaneously treating solid matter such as ash in exhaust gas.
【０００２】[0002]
【従来の技術】大気汚染公害防止の観点から、発電用ボ
イラなどの硫黄分を比較的多く含む石油や石炭などの化
石燃料を燃焼させる大型装置においては、排ガスからの
ＳＯｘを除去低減するため湿式の排煙脱硫装置が多く取
り付けられている。図３は、湿式排煙脱硫装置のうち最
も多く設置されている石灰石−石膏法湿式排煙脱硫装置
のシステムフローである。2. Description of the Related Art From the viewpoint of preventing air pollution and pollution, in a large-scale apparatus for burning fossil fuel such as oil or coal containing a relatively large amount of sulfur such as a boiler for power generation, a wet type is used to remove SOx from exhaust gas. Many flue gas desulfurizers are installed. FIG. 3 is a system flow of the limestone-gypsum method wet flue gas desulfurization apparatus installed most in the wet flue gas desulfurization apparatus.
【０００３】図３に示す石灰石−石膏法湿式排煙脱硫装
置はボイラ１から排出された１２０〜１５０℃の排ガス
は電気集塵器２により脱塵され、ガス／ガスヒータ３で
約９０℃に冷却された後、脱硫吸収塔４に導入され、排
ガス中のＳＯｘは石灰（ＣａＣＯ3）を含むスラリと気
液接触により石膏（ＣａＳＯ4）として除去回収され
る。ＳＯｘ分が取り除かれた脱硫吸収塔出口排ガス２２
は、デミスタ１５およびミストエリミネータ１６で水分
除去された後、前述ガス／ガスヒータ３で加熱され、煙
突１７から大気に放出させるシステムである。また、電
気集塵器２により回収される灰分は灰回収装置１８に回
収される。In the limestone-gypsum method wet flue gas desulfurization apparatus shown in FIG. 3, the exhaust gas of 120 to 150 ° C. discharged from the boiler 1 is dedusted by the electrostatic precipitator 2 and cooled to about 90 ° C. by the gas / gas heater 3. After being treated, it is introduced into the desulfurization absorption tower 4, and SOx in the exhaust gas is removed and recovered as gypsum (CaSO 4 ) by gas-liquid contact with the slurry containing lime (CaCO 3 ). Desulfurization absorption tower outlet exhaust gas 22 from which SOx components have been removed
Is a system in which water is removed by the demister 15 and the mist eliminator 16 and then heated by the gas / gas heater 3 described above and released from the chimney 17 to the atmosphere. Further, the ash collected by the electrostatic precipitator 2 is collected by the ash collecting device 18.
【０００４】吸収塔タンク５内の石灰スラリは、循環ポ
ンプ８により脱硫吸収塔４内でスプレされ、排ガスと気
液反応を起こすようにしている。石灰スラリの前記循環
系には工業用水１３と石灰１４が供給され、さらに、石
灰スラリ混合器１２から新規石灰スラリが供給される。
また、吸収塔タンク５に設置されている撹拌インペラ６
は石灰スラリを混合均一化するもので、酸化用インペラ
７はＳＯｘと石灰の反応で生じた亜硫酸カルシウム（Ｃ
ａＳＯ3）を硫酸カルシウム、すなわち石膏（ＣａＳ
Ｏ4）に酸化するため空気供給器１９より導入される空
気を分散均一するものである。生成した石膏含有スラリ
は吸収塔タンク５からシックナ９に導かれて濃縮され
る。次いで石膏含有スラリは遠心分離器１０で水分を除
去された後、生成石膏１１として回収され、石膏ボード
など建築材料に利用される。こうした石灰−石膏法湿式
排煙脱硫装置は脱硫率が９５％以上と高いことおよび副
製石膏を建築部材に利用できるメリットもあり、大気汚
染防止に大いに役立っている。The lime slurry in the absorption tower tank 5 is sprayed in the desulfurization absorption tower 4 by the circulation pump 8 to cause a gas-liquid reaction with the exhaust gas. Industrial water 13 and lime 14 are supplied to the circulation system of the lime slurry, and new lime slurry is further supplied from the lime slurry mixer 12.
In addition, the stirring impeller 6 installed in the absorption tower tank 5
Is for mixing and homogenizing lime slurry, and the impeller 7 for oxidation is calcium sulfite (C
aSO 3 ) to calcium sulfate, that is, gypsum (CaS
The air introduced from the air supplier 19 for being oxidized to O 4 ) is dispersed and uniform. The generated gypsum-containing slurry is guided from the absorption tower tank 5 to the thickener 9 and concentrated. Next, the gypsum-containing slurry is dewatered by the centrifuge 10 and then recovered as the produced gypsum 11 to be used as a building material such as a gypsum board. Such a lime-gypsum method wet flue gas desulfurization device has a high desulfurization rate of 95% or more and has the advantage of using by-product gypsum as a construction member, and thus is very useful for preventing air pollution.
【０００５】しかしながら、現状のプラントシステムの
問題点は、使用機器数の増大、装置の大型化およびシス
テムの複雑化に伴う装置費用の高騰並びに動力用電力や
使用水などのユーティリティの増加に伴い多大な費用が
必要なことにある。すなわち設備費や運転経費が高いと
いう問題がある。そのため、経済上および敷地面積上問
題のあるところでは排煙脱硫装置が設置し難いのが実状
である。さらに、最近クローズアップしている地球規模
の環境汚染問題のうち酸性雨を解決するためには、開発
途上国でも設置しうる廉価でコンパクトかつ運転経費の
かからない脱硫装置の提供が必要になっている。However, the problems of the present plant system are great as the number of equipment used increases, the size of the device increases, the cost of the device increases due to the complexity of the system, and the utilities such as power and water used increase. There is a great expense. That is, there is a problem that equipment costs and operating costs are high. Therefore, it is difficult to install the flue gas desulfurization equipment in places where there are problems in terms of economy and site area. Furthermore, in order to solve acid rain, which is one of the most recent global environmental pollution problems, it is necessary to provide desulfurization equipment that can be installed in developing countries at low cost, is compact and does not require operating costs. .
【０００６】脱硫装置に用いる用水量を低減する方法と
して、脱塵された排ガスを冷却し、その凝縮水を利用す
る方法（特開昭５９−１６５２６号公報、特開昭６３−
４８３５号公報等）が考えられており、この手法で用水
量は低減できるが、従来と同等の脱塵灰処理装置や脱硫
用石灰とその供給装置が必要である。As a method for reducing the amount of water used in a desulfurization apparatus, a method of cooling dedusted exhaust gas and utilizing the condensed water thereof (Japanese Patent Laid-Open Nos. 59-16526 and 63-63).
No. 4835) is considered, and the amount of water used can be reduced by this method, but a dedusting ash treatment device, a desulfurization lime and its supply device equivalent to the conventional one are required.
【０００７】[0007]
【発明が解決しようとする課題】本発明の目的は、従来
技術の湿式排煙脱硫装置で問題となっている設備費用や
運転費用を軽減したコパクトでシンプルな湿式排煙脱硫
方法と装置を提供することにある。さらに、従来電気集
塵器で除去していた排ガス中のアッシュも同時に処理で
きる方法と装置を提供することにある。SUMMARY OF THE INVENTION It is an object of the present invention to provide a compact and simple wet flue gas desulfurization method and apparatus which reduce facility costs and operating costs, which are problems in the conventional wet flue gas desulfurization apparatus. To do. Another object of the present invention is to provide a method and an apparatus capable of simultaneously treating ash in exhaust gas, which has been conventionally removed by an electrostatic precipitator.
【０００８】[0008]
【課題を解決するための手段】本発明の上記目的は次の
構成によって達成できる。すなわち、燃焼排ガス中の硫
黄酸化物をアルカリ性物質を含む脱硫剤で吸収除去する
湿式排煙脱硫方法において、石炭燃焼灰を含む排ガスを
４０℃以下に冷却して、その凝縮水中に石炭燃焼灰を混
入させ、この石炭燃焼灰と凝縮水とのスラリに脱硫剤を
添加した脱硫吸収液により排ガス中の硫黄酸化物を分離
除去する脱塵脱硫同時処理方法である。ここで、前記脱
塵脱硫同時処理方法において、石炭燃焼灰と凝縮水との
スラリに脱硫剤を添加した脱硫吸収液から固形石炭灰物
質を沈降分離させ、脱硫吸収液には主に上澄み液を用い
ることができる。The above object of the present invention can be achieved by the following constitution. That is, in a wet flue gas desulfurization method of absorbing and removing sulfur oxides in combustion exhaust gas with a desulfurizing agent containing an alkaline substance, the exhaust gas containing coal combustion ash is cooled to 40 ° C. or lower, and coal combustion ash is condensed in the condensed water. It is a simultaneous desulfurization and desulfurization treatment method in which sulfur oxides in exhaust gas are separated and removed by a desulfurization absorption liquid which is mixed with a desulfurization agent added to the slurry of coal combustion ash and condensed water. Here, in the desulfurization desulfurization simultaneous treatment method, the solid coal ash material is precipitated and separated from the desulfurization absorption liquid obtained by adding a desulfurization agent to the slurry of coal combustion ash and condensed water, and the supernatant liquid is mainly contained in the desulfurization absorption liquid. Can be used.
【０００９】また、本発明の上記目的は次の構成によっ
ても達成できる。すなわち、燃焼排ガス中の硫黄酸化物
をアルカリ性物質を含む脱硫剤で吸収除去する湿式排煙
脱硫装置において、石炭燃焼灰を含む排ガスを４０℃以
下に冷却させる排ガス冷却凝縮器と、排ガス冷却凝縮器
で得られる凝縮水と石炭燃焼灰を導入し、アルカリ性物
質を含む脱硫剤と混合して脱硫用スラリとする吸収塔タ
ンクと、該吸収塔タンク内の脱硫用スラリを噴霧して排
ガスと接触させる吸収塔を備えた脱塵脱硫同時処理装置
である。ここで、前記脱塵脱硫同時処理装置において、
吸収塔タンク下部に不要な石炭灰を沈降させ、吸収塔内
に噴霧させる上澄み脱硫用スラリと分離させる不要石炭
灰沈降分離装置を備えることができる。The above object of the present invention can also be achieved by the following configuration. That is, in a wet flue gas desulfurization apparatus for absorbing and removing sulfur oxides in combustion exhaust gas with a desulfurizing agent containing an alkaline substance, an exhaust gas cooling condenser for cooling exhaust gas containing coal combustion ash to 40 ° C. or less, and an exhaust gas cooling condenser Introduce the condensed water and coal combustion ash obtained in step 1, and mix with a desulfurizing agent containing an alkaline substance to form a desulfurization slurry, and the desulfurization slurry in the absorption tower tank is sprayed and brought into contact with exhaust gas. It is a dedusting desulfurization simultaneous treatment apparatus equipped with an absorption tower. Here, in the dedusting desulfurization simultaneous treatment apparatus,
An unnecessary coal ash settling / separating device for separating unnecessary coal ash in the lower part of the absorption tower tank and separating it from the supernatant desulfurization slurry sprayed in the absorption tower can be provided.
【００１０】[0010]
【作用】石炭を燃焼させた排ガス中には、約１０％の水
分を含んでいる。水分１０％のガスの露点すなわち水凝
縮温度は約５０℃である。したがって、ボイラ排ガスを
４０℃以下に冷却すると多量の凝縮水が生成する。従来
型の湿式脱硫装置の場合には排ガス量８００，０００Ｎ
ｍ3／ｈのボイラの場合、４０℃冷却で約２５ｔｏｎ／
ｈ、３０℃冷却で約４１ｔｏｎ／ｈの水が生成するの
で、５０℃以上の冷却で運転される。そのため、排ガス
中の水分は活用しておらず、むしろ蒸発分や系の不純物
の濃縮防止を考慮して約１５０ｔｏｎ／ｈの河川水や工
業用水を供給している。ボイラ排ガスを露点以下に冷却
した際、生じた水に石灰を混合し、その石灰スラリと排
ガスを気液反応させることによってＳＯｘを除去すると
低温運転であることから水分の蒸発量が少なく、凝縮水
は再利用できるので工業用水の供給を求めることができ
る。Function: The exhaust gas from burning coal contains about 10% of water. The dew point of water containing 10% of water, that is, the water condensation temperature is about 50 ° C. Therefore, when the boiler exhaust gas is cooled to 40 ° C. or less, a large amount of condensed water is generated. Exhaust gas amount of 800,000N in case of conventional wet desulfurization equipment
For boiler m 3 / h, approximately at 40 ° C. Cooling 25Ton /
Since about 41 ton / h of water is produced by cooling at 30 ° C. for 30 hours, the cooling is performed at 50 ° C. or higher. Therefore, the water in the exhaust gas is not used, rather, about 150 ton / h of river water or industrial water is supplied in consideration of the prevention of concentration of evaporated components and impurities in the system. When the boiler exhaust gas is cooled below the dew point, lime is mixed with the generated water, and SOx is removed by gas-liquid reaction between the lime slurry and the exhaust gas, so the amount of water evaporation is small because of low temperature operation, and the condensed water Since it can be reused, a supply of industrial water can be sought.
【００１１】一方、脱硫処理前のボイラ排ガス、すなわ
ち電気集塵器の前流のボイラ排ガスを４０℃以下に冷却
し、凝縮水を得ると、その中にアッシュなどの固形物も
混入することになる。石炭の燃焼灰はアルカリ成分を含
んでいるので排ガス中のＳＯｘを一部脱硫することがで
き、回収石炭燃焼灰を脱硫剤の一部として用いると、石
灰量を低減できるので脱硫への石炭灰の利用はメリット
がある。On the other hand, when the boiler exhaust gas before desulfurization treatment, that is, the boiler exhaust gas in the upstream of the electrostatic precipitator is cooled to 40 ° C. or less and condensed water is obtained, solid matter such as ash is also mixed therein. Become. Since the combustion ash of coal contains an alkaline component, it is possible to partially desulfurize SOx in the exhaust gas. If the recovered coal combustion ash is used as a part of the desulfurizing agent, the amount of lime can be reduced. There are advantages to using.
【００１２】排ガスの冷却温度を４０℃以下にしたの
は、石炭を燃焼した場合の排ガス中の水分量（約１０
％）と脱硫反応に必要な石灰石スラリの水分量より定め
たもので、これ以上の温度では、凝縮水分量が少なく、
適正な脱硫反応を生じさせることはできない。系の不純
物濃度やスラリの粘度を低くするためには、３０℃以下
に冷却し、より多量の水分を得ることが望ましい。The cooling temperature of the exhaust gas is set to 40 ° C. or lower because the amount of water in the exhaust gas when coal is burned (about 10
%) And the water content of the limestone slurry required for the desulfurization reaction. At temperatures above this, the condensed water content is low,
A proper desulfurization reaction cannot occur. In order to reduce the concentration of impurities in the system and the viscosity of the slurry, it is desirable to cool to 30 ° C. or lower to obtain a larger amount of water.
【００１３】脱硫反応で生じたＣａＳＯ3のＣａＳＯ4へ
の酸化は、従来通り空気酸化によればよい。石炭燃焼灰
中の有効なアルカリ成分は、中性から酸性液中に溶解し
ていき、それ以外の酸化物（ＳｉＯ2、Ａｌ2Ｏ3、Ｆｅ2
Ｏ3など）は、脱硫反応や構成材料の腐食に対しては影
響を及ぼさないが、硬さが高いため、高流速になる領域
では構成材料を摩耗させることがある。こうした摩耗を
低減するためには、摩耗有害物質をタンク内などで沈降
分離できる装置を設置すればよい。The oxidation of CaSO 3 produced by the desulfurization reaction to CaSO 4 may be carried out by air oxidation as is conventional. Effective alkali components in coal combustion ash are dissolved in neutral to acidic liquids and other oxides (SiO 2 , Al 2 O 3 , Fe 2
O 3 and the like do not affect the desulfurization reaction and the corrosion of the constituent materials, but since the hardness is high, the constituent materials may be abraded in the high flow velocity region. In order to reduce such wear, a device capable of settling and separating the wear harmful substances in a tank or the like may be installed.
【００１４】[0014]
【実施例】本発明の具体的実施例を以下図面をもって説
明する。図１には、本実施例になる石炭焚きボイラ排ガ
スの脱塵脱硫同時処理装置のシステムフローを示す。ボ
イラ１から出た１００〜２００℃の排ガスを排ガス冷却
凝縮器２０により４０℃以下に冷却し、石炭アッシュを
含んだ凝縮水を得る。その凝縮水は、ポンプ（図示せ
ず）などで脱硫吸収塔４へ送る。また、排ガス冷却凝縮
器２０により冷却された水分のほとんどが除去された排
ガスも、脱硫吸収塔４に供給され、脱硫吸収塔４で石灰
１４を添加されたアッシュスラリ液と気液接触により、
排ガス中のＳＯｘを石膏として分離回収するようにした
ものである。アッシュおよび生成石膏は、吸収塔タンク
５の底部に沈殿させ、図３に示す石膏シックナ９と同様
の方法により回収し、遠心分離器１０などで水分を除去
した後、灰および石膏回収装置（図示せず）で灰含有石
膏２４を回収する。また、吸収塔タンク５内のスラリ液
は循環ポンプ８により脱硫吸収塔４に循環供給され、塔
内に噴霧される。酸化用インペラ７はＳＯｘと石灰の反
応で生じた亜硫酸カルシウム（ＣａＳＯ3）を硫酸カル
シウム、すなわち石膏（ＣａＳＯ4）に酸化するため空
気供給器１９より導入される空気を分散均一するもので
ある。脱硫吸収塔４のデミスタ１５とミストエリミネー
タ１６でさらに脱塵されたクリーンな排ガス２２は、排
ガス冷却凝縮器２０で熱交換された後、煙突１７から排
出される。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Specific embodiments of the present invention will be described below with reference to the drawings. FIG. 1 shows a system flow of a simultaneous dust removal and desulfurization treatment apparatus for coal-fired boiler exhaust gas according to this embodiment. The exhaust gas of 100 to 200 ° C. emitted from the boiler 1 is cooled to 40 ° C. or lower by the exhaust gas cooling condenser 20 to obtain condensed water containing coal ash. The condensed water is sent to the desulfurization absorption tower 4 by a pump (not shown) or the like. In addition, the exhaust gas cooled by the exhaust gas cooling condenser 20 and from which most of the water has been removed is also supplied to the desulfurization absorption tower 4, and by the gas-liquid contact with the ash slurry liquid to which the lime 14 has been added in the desulfurization absorption tower 4,
SOx in the exhaust gas is separated and collected as gypsum. The ash and the generated gypsum are settled on the bottom of the absorption tower tank 5, collected by the same method as the gypsum thickener 9 shown in FIG. 3, and after removing water with a centrifuge 10 or the like, an ash and gypsum recovery device (see FIG. The ash-containing gypsum 24 is recovered (not shown). Further, the slurry liquid in the absorption tower tank 5 is circulated and supplied to the desulfurization absorption tower 4 by the circulation pump 8 and sprayed into the tower. The oxidizing impeller 7 is for uniformly dispersing the air introduced from the air supplier 19 in order to oxidize calcium sulfite (CaSO 3 ) generated by the reaction of SOx and lime into calcium sulfate, that is, gypsum (CaSO 4 ). The clean exhaust gas 22 further dedusted by the demister 15 and the mist eliminator 16 of the desulfurization absorption tower 4 is heat-exchanged by the exhaust gas cooling condenser 20 and then discharged from the chimney 17.
【００１５】ボイラ排ガスを４０℃以下に冷却する排ガ
ス冷却凝縮器２０の冷却源は、いずれの方法でもよい
が、エネルギー効率および省エネを考慮すると、図１で
示したように、高温部ではボイラ用空気またはボイラ給
水２１の加熱に用い、中温部で脱硫出口排ガス２２の加
熱に用い、最終段では、海水または工業用水２３などで
冷却するのが望ましい。また、上述したボイラ排ガス冷
却手段の少なくとも一つ以上を組み合わせて用いること
ができる。The exhaust gas cooling condenser 20 for cooling the exhaust gas of the boiler to 40 ° C. or lower may be cooled by any method, but in consideration of energy efficiency and energy saving, as shown in FIG. It is desirable to use it for heating the air or boiler feed water 21, use it for heating the desulfurization outlet exhaust gas 22 in the middle temperature section, and cool it with seawater or industrial water 23 in the final stage. Further, at least one of the above-mentioned boiler exhaust gas cooling means can be used in combination.
【００１６】図１では脱硫吸収塔４の構造をスラリ落
下、ガス上昇の対向流気液接触法としているが、この
他、スプレタイプ、スラリ液内バブリングタイプ、濡れ
壁タイプ等いずれの方法を用いて排ガスと脱硫用スラリ
とを接触させてもよい。どの方式を採るかは、敷地面
積、効率およびアッシュ成分により決定すればよい。本
実施例の脱硫用スラリは、アッシュを多量に含むため構
成材料を摩耗させるので、これを防ぐために、流速をで
きるだけ低く抑えられる方式や図１のように不要アッシ
ュ沈降分離装置２６により、摩耗成分をタンク内で沈降
分離させ、タンク内上澄み液に石灰を混入させる方式が
好ましい。この方法も本実施例の特徴部分である。In FIG. 1, the structure of the desulfurization absorption tower 4 is a countercurrent gas-liquid contact method of slurry falling and gas rising, but other methods such as spray type, slurry liquid bubbling type and wet wall type may be used. The exhaust gas and the desulfurizing slurry may be brought into contact with each other. Which method to use may be determined by the site area, efficiency and ash component. Since the desulfurization slurry of this embodiment contains a large amount of ash, the constituent materials are abraded. Therefore, in order to prevent this, the method of keeping the flow velocity as low as possible and the unnecessary ash sedimentation separation device 26 as shown in FIG. It is preferable to settle in the tank and settle in the tank, and mix lime with the supernatant in the tank. This method is also a characteristic part of this embodiment.
【００１７】本実施例の脱塵脱硫同時処理装置の各構成
部分の作用を以下に説明する。排ガス冷却凝縮器２０は
石炭焚きボイラ排ガスを、ボイラ燃焼用空気、ボイラ給
水、脱硫出口排ガスおよび海水や工業用水の一種または
複数種を用いて４０℃以下に冷却し、排ガス中のアッシ
ュと共に水分を凝縮させる作用を有する。該凝縮器２０
により排ガス中の余熱を低温まで回収できるのでボイラ
効率が約１％上昇する。排ガス冷却凝縮器２０を脱硫出
口排ガス２２と熱交換させるのは脱硫出口排ガス２２を
昇温させて煙突からの飛散を容易にするためである。The operation of each component of the desulfurization / desulfurization simultaneous treatment apparatus of this embodiment will be described below. The exhaust gas cooling condenser 20 cools the coal-fired boiler exhaust gas to 40 ° C. or lower by using one or more kinds of boiler combustion air, boiler feed water, desulfurization outlet exhaust gas, and seawater or industrial water, and removes moisture along with ash in the exhaust gas. Has a function of condensing. The condenser 20
As a result, the residual heat in the exhaust gas can be recovered to a low temperature, and the boiler efficiency will increase by about 1%. The exhaust gas cooling condenser 20 is heat-exchanged with the desulfurization outlet exhaust gas 22 in order to raise the temperature of the desulfurization outlet exhaust gas 22 and facilitate scattering from the chimney.
【００１８】脱硫吸収塔４では、排ガス冷却凝縮器２０
で生成させたアッシュを含む凝縮水スラリに石灰を添加
して排ガスと気液接触させ、排ガス中の硫黄酸化物を石
膏に変化させる。石炭燃焼アッシュ中にはＳｉＯ2、Ａ
ｌ2Ｏ3およびＦｅ2Ｏ3のようにいずれの物質とも反応し
にくい安定な物質もあるが、ＣａＯ、ＭｇＯおよびＮａ
2Ｏなどのアルカリ成分を５〜２０％含んでいるため、
これらのアルカリ成分は脱硫反応に寄与し、石炭灰を利
用することによって石灰の量を低減できる。石炭焚きボ
イラ排ガスを凝縮し、その凝縮水中に約１０００ｐｐｍ
のＳＯｘが全て溶解したと仮定すると約９％の硫酸が生
成する。硫酸または亜硫酸が生成してｐＨが低下すると
ＳＯｘの吸収が悪くなり、実際には多くて０．５％しか
溶解せずｐＨは１前後となる。排ガス冷却凝縮器２０で
ｐＨ１の液が生成すると石炭アッシュ中のアルカリ成分
が反応して中和作用がでてくる。凝縮水が中和されれば
その分脱硫されたことになる。In the desulfurization absorption tower 4, the exhaust gas cooling condenser 20
Lime is added to the condensed water slurry containing the ash generated in step (3) to make gas-liquid contact with the exhaust gas, and the sulfur oxides in the exhaust gas are converted to gypsum. SiO 2 , A in the coal combustion ash
Some stable substances such as l 2 O 3 and Fe 2 O 3 are difficult to react with any substance, but CaO, MgO and Na
Since it contains 5 to 20% of alkaline components such as 2 O,
These alkaline components contribute to the desulfurization reaction, and the amount of lime can be reduced by utilizing the coal ash. Coal-fired boiler exhaust gas is condensed to approximately 1000ppm in the condensed water.
Assuming that all of the SOx are dissolved, about 9% sulfuric acid is produced. When sulfuric acid or sulfurous acid is generated and the pH is lowered, SOx absorption is deteriorated, and in reality, only 0.5% is dissolved and the pH is around 1. When a liquid having a pH of 1 is produced in the exhaust gas cooling condenser 20, the alkaline components in the coal ash react with each other and a neutralizing action appears. If the condensed water is neutralized, it is desulfurized correspondingly.
【００１９】吸収塔タンク５内の不要アッシュ沈降分離
装置２６は摩耗に有害な酸化物を沈降分離する作用を有
する。本実施例では該回収装置２６は吸収塔タンク５の
下部に設けられた傾斜方式としているが、図３に示す従
来型脱硫吸収塔タンク４では、タンク下部中央部に円錐
状の沈殿が生じるので、従来型脱硫吸収塔タンク４下部
に撹拌インペラ（図示せず）を設け、タンク底中央部よ
り不要アッシュを抜き出す方式でもよく、この方式も本
発明の範囲内のものである。The unnecessary ash sedimentation / separation device 26 in the absorption tower tank 5 has a function of sedimenting and separating oxides harmful to wear. In the present embodiment, the recovery device 26 is of a tilt type installed in the lower part of the absorption tower tank 5, but in the conventional desulfurization absorption tower tank 4 shown in FIG. 3, a conical precipitate occurs in the central part of the lower part of the tank. A method may be used in which a stirring impeller (not shown) is provided in the lower portion of the conventional desulfurization absorption tower tank 4 and unnecessary ash is withdrawn from the center of the tank bottom, and this method is also within the scope of the present invention.
【００２０】また、本発明の他の実施例を図２に示す。
本実施例の図１に示すシステムフローと比較して排ガス
冷却凝縮器２０と脱硫吸収塔４を分離型にした所が異な
る。排ガス冷却凝縮器２０で生成させたアッシュを含む
凝縮水スラリ２８は吸収塔タンク５下部の不要アッシュ
沈降分離装置２６に導かれ、また、冷却された排ガスは
脱硫吸収塔４に導かれる。その他の各装置の作用は図１
に示す装置と同じである。Another embodiment of the present invention is shown in FIG.
Compared with the system flow shown in FIG. 1 of this embodiment, the exhaust gas cooling condenser 20 and the desulfurization absorption tower 4 are separated. The condensed water slurry 28 containing ash generated in the exhaust gas cooling condenser 20 is guided to the unnecessary ash sedimentation / separation device 26 below the absorption tower tank 5, and the cooled exhaust gas is guided to the desulfurization absorption tower 4. The operation of other devices is shown in FIG.
It is the same as the device shown in.
【００２１】[0021]
【発明の効果】本発明によれば、石炭アッシュのアルカ
リ成分を脱硫の一部に利用することから石灰の量を低減
でき、また脱硫用スラリには排ガス中の水分を用いるこ
とから用水が不要となる。さらに脱塵脱硫同時処理であ
ることから電気集塵器が不要でまた灰の処理が従来のよ
うに乾式でなく湿式であるため飛散や人体への進入の問
題も解決できる。According to the present invention, the amount of lime can be reduced by utilizing the alkaline component of coal ash as a part of desulfurization, and the desulfurization slurry does not require water because the moisture in the exhaust gas is used. Becomes Furthermore, since it is a simultaneous desulfurization and desulfurization treatment, an electric precipitator is not required, and since the ash treatment is wet rather than dry as in the past, the problems of scattering and entering the human body can be solved.
【図１】 本発明の一実施例になる脱塵脱硫同時処理装
置のシステムフローを示す図である。FIG. 1 is a diagram showing a system flow of a desulfurization / desulfurization simultaneous treatment apparatus according to an embodiment of the present invention.
【図２】 本発明の他の実施例になる脱塵脱硫同時処理
装置のシステムフローを示す図である。FIG. 2 is a diagram showing a system flow of a simultaneous dedusting / desulfurization treatment apparatus according to another embodiment of the present invention.
【図３】 従来技術になる石灰−石膏法湿式排煙脱硫装
置のシステムフローを示す図である。FIG. 3 is a diagram showing a system flow of a conventional lime-gypsum method wet flue gas desulfurization apparatus.
１…ボイラ、４…脱硫吸収塔、５…吸収塔タンク、７…
酸化用インペラ、８…循環ポンプ、１０…遠心分離器、
１４…石灰、１５…デミスタ、１６…ミストエリミネー
タ、１９…空気供給器、２０…排ガス冷却凝縮器、２１
…ボイラ用空気又はボイラ給水、２２…脱硫出口排ガ
ス、２３…冷却用海水等、２４…灰および石膏回収装
置、２６…不要アッシュ沈降分離装置1 ... Boiler, 4 ... Desulfurization absorption tower, 5 ... Absorption tower tank, 7 ...
Oxidation impeller, 8 ... Circulation pump, 10 ... Centrifuge,
14 ... Lime, 15 ... Demister, 16 ... Mist eliminator, 19 ... Air supplier, 20 ... Exhaust gas cooling condenser, 21
... Boiler air or boiler feed water, 22 ... Desulfurization outlet exhaust gas, 23 ... Cooling seawater, etc., 24 ... Ash and gypsum recovery device, 26 ... Unnecessary ash sedimentation separation device
Claims (4)
物質を含む脱硫剤で吸収除去する湿式排煙脱硫方法にお
いて、石炭燃焼灰を含む排ガスを４０℃以下に冷却し
て、その凝縮水中に石炭燃焼灰を混入させ、この石炭燃
焼灰と凝縮水とのスラリに脱硫剤を添加した脱硫吸収液
により排ガス中の硫黄酸化物を分離除去することを特徴
とする脱塵脱硫同時処理方法。1. A wet flue gas desulfurization method for absorbing and removing sulfur oxides in combustion exhaust gas with a desulfurizing agent containing an alkaline substance, wherein exhaust gas containing coal combustion ash is cooled to 40 ° C. or lower, and coal is condensed in the condensed water. A method for simultaneous desulfurization and desulfurization, which comprises mixing combustion ash and separating and removing sulfur oxides in exhaust gas by a desulfurization absorption liquid obtained by adding a desulfurization agent to a slurry of the coal combustion ash and condensed water.
を添加した脱硫吸収液から固形石炭灰物質を沈降分離さ
せ、脱硫吸収液には主に上澄み液を用いることを特徴と
する請求項１記載の脱塵脱硫同時処理方法。2. A solid coal ash material is settled and separated from a desulfurization absorption liquid obtained by adding a desulfurization agent to a slurry of coal combustion ash and condensed water, and a supernatant liquid is mainly used as the desulfurization absorption liquid. Item 1. A dedusting desulfurization simultaneous treatment method according to Item 1.
物質を含む脱硫剤で吸収除去する湿式排煙脱硫装置にお
いて、石炭燃焼灰を含む排ガスを４０℃以下に冷却させ
る排ガス冷却凝縮器と、排ガス冷却凝縮器で得られる凝
縮水と石炭燃焼灰を導入し、アルカリ性物質を含む脱硫
剤と混合して脱硫用スラリとする吸収塔タンクと、該吸
収塔タンク内の脱硫用スラリを噴霧して排ガスと接触さ
せる吸収塔を備えたことを特徴とする脱塵脱硫同時処理
装置。3. An exhaust gas cooling condenser for cooling exhaust gas containing coal combustion ash to 40 ° C. or lower in a wet flue gas desulfurization apparatus for absorbing and removing sulfur oxides in combustion exhaust gas with a desulfurizing agent containing an alkaline substance, and an exhaust gas. Introducing condensed water and coal combustion ash obtained in a cooling condenser, an absorption tower tank that mixes with a desulfurizing agent containing an alkaline substance to form a desulfurization slurry, and an exhaust gas by spraying the desulfurization slurry in the absorption tower tank An apparatus for simultaneous dedusting and desulfurization, which is equipped with an absorption tower to be brought into contact with
させ、吸収塔内に噴霧させる上澄み脱硫用スラリと分離
させる不要石炭灰沈降分離装置を備えたことを特徴とす
る請求項３記載の脱塵脱硫同時処理装置。4. An unnecessary coal ash sedimentation separation device for separating unnecessary coal ash in the lower part of the absorption tower tank and separating it from the supernatant desulfurization slurry sprayed in the absorption tower. Dedusting and desulfurization simultaneous treatment equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4276899A JPH06126127A (en) | 1992-10-15 | 1992-10-15 | Method and apparatus for simultaneous treatment of dust collection and desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4276899A JPH06126127A (en) | 1992-10-15 | 1992-10-15 | Method and apparatus for simultaneous treatment of dust collection and desulfurization |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06126127A true JPH06126127A (en) | 1994-05-10 |
Family
ID=17575943
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4276899A Pending JPH06126127A (en) | 1992-10-15 | 1992-10-15 | Method and apparatus for simultaneous treatment of dust collection and desulfurization |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06126127A (en) |
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| WO2001012299A1 (en) * | 1999-08-12 | 2001-02-22 | Ebara Corporation | Method and apparatus for treating exhaust gas |
| WO2010150424A1 (en) * | 2009-06-26 | 2010-12-29 | 三菱重工業株式会社 | Flue-gas desulfurization system using river water and method of removing humus |
| JP2012196611A (en) * | 2011-03-18 | 2012-10-18 | Babcock Hitachi Kk | Flue gas desulfurization apparatus and flue gas desulfurization method |
| JP2013202432A (en) * | 2012-03-27 | 2013-10-07 | Taiheiyo Cement Corp | Method for disposing of fluidized bed boiler ash and disposer |
| CN104848193A (en) * | 2015-05-28 | 2015-08-19 | 苏州斯洛莱自动化设备有限公司 | Industrial environment-friendly boiler |
| CN106422730A (en) * | 2016-08-31 | 2017-02-22 | 张明鑫 | Double wet method flue gas desulphurization and dust removal treatment process |
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| JP2019118893A (en) * | 2018-01-09 | 2019-07-22 | 株式会社タクマ | Method for removal of acid gas in flue gas, and device therefor |
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-
1992
- 1992-10-15 JP JP4276899A patent/JPH06126127A/en active Pending
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|---|---|---|---|---|
| US6773555B1 (en) | 1999-08-12 | 2004-08-10 | Ebara Corporation | Method for treating exhaust gas |
| WO2001012299A1 (en) * | 1999-08-12 | 2001-02-22 | Ebara Corporation | Method and apparatus for treating exhaust gas |
| WO2010150424A1 (en) * | 2009-06-26 | 2010-12-29 | 三菱重工業株式会社 | Flue-gas desulfurization system using river water and method of removing humus |
| US8298321B2 (en) | 2009-06-26 | 2012-10-30 | Mitsubishi Heavy Industries, Ltd. | River water utilizing flue gas desulfurization system and humic substance removing method |
| JP2012196611A (en) * | 2011-03-18 | 2012-10-18 | Babcock Hitachi Kk | Flue gas desulfurization apparatus and flue gas desulfurization method |
| JP2013202432A (en) * | 2012-03-27 | 2013-10-07 | Taiheiyo Cement Corp | Method for disposing of fluidized bed boiler ash and disposer |
| US10376835B2 (en) | 2013-06-10 | 2019-08-13 | Ihi Corporation | Device for removing impurities from water-containing gas and impurities removal system |
| CN104848193A (en) * | 2015-05-28 | 2015-08-19 | 苏州斯洛莱自动化设备有限公司 | Industrial environment-friendly boiler |
| CN106422730B (en) * | 2016-08-31 | 2018-12-07 | 张明鑫 | Double wet process of FGD dust removal process techniques |
| CN106422730A (en) * | 2016-08-31 | 2017-02-22 | 张明鑫 | Double wet method flue gas desulphurization and dust removal treatment process |
| CN106975357A (en) * | 2017-04-28 | 2017-07-25 | 张久明 | A kind of desulphurization and denitration, flue dust solid matter retracting device and its recycling and control method |
| JP2019118893A (en) * | 2018-01-09 | 2019-07-22 | 株式会社タクマ | Method for removal of acid gas in flue gas, and device therefor |
| WO2020204026A1 (en) | 2019-04-01 | 2020-10-08 | 三菱日立パワーシステムズ株式会社 | Device and method pertaining to gas purification treatment and/or combustion ash neutralization treatment |
| KR20210126746A (en) | 2019-04-01 | 2021-10-20 | 미츠비시 파워 가부시키가이샤 | Apparatus and method for gas purification treatment and/or combustion ash neutralization treatment |
| WO2023238936A1 (en) * | 2022-06-11 | 2023-12-14 | ナノミストテクノロジーズ株式会社 | Exhaust gas treatment apparatus |
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