JPH06218227A - Method and device for desulfurizing stack gas - Google Patents
Method and device for desulfurizing stack gasInfo
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- JPH06218227A JPH06218227A JP5031298A JP3129893A JPH06218227A JP H06218227 A JPH06218227 A JP H06218227A JP 5031298 A JP5031298 A JP 5031298A JP 3129893 A JP3129893 A JP 3129893A JP H06218227 A JPH06218227 A JP H06218227A
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Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、亜硫酸ガスを含有する
排煙を湿式石灰法により脱硫処理する方法及び装置の改
良に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an improved method and apparatus for desulfurizing flue gas containing sulfurous acid gas by a wet lime method.
【０００２】[0002]
【従来の技術】従来から、カルシウム化合物含有スラリ
ーを吸収剤とし、石こう化反応を行なわせるために酸化
用空気をこのスラリー中に吹き込む排煙脱硫方法が知ら
れている。ところで、従来法のように単に空気をスラリ
ー中に吹き込む場合、空気噴霧ノズルの先端から、同ノ
ズル内側に向けて同ノズル内壁に硬質のスケールが発生
する。このスケールの発生は吹き込まれる空気が水分未
飽和状態であるため、空気ノズル先端部分で同ノズル内
に付着するスラリー飛沫などの乾燥が原因と考えられ
る。空気ノズル先端でスケールによる閉塞やノズル断面
での通気断面の低下は、空気供給源に必要以上の圧力を
必要とするとともにスラリー滞留タンク断面方向の空気
吹き込み量の不均一を生じ、所期の酸化性能の確保がで
きなくなるなどの不都合が生じていた。2. Description of the Related Art Conventionally, a flue gas desulfurization method has been known in which a calcium compound-containing slurry is used as an absorbent, and oxidizing air is blown into the slurry to carry out a gypsum reaction. By the way, when air is simply blown into the slurry as in the conventional method, a hard scale is generated on the inner wall of the nozzle from the tip of the air atomizing nozzle toward the inside of the nozzle. It is considered that the generation of this scale is caused by the drying of slurry droplets adhering to the inside of the air nozzle because the air blown in is in a water unsaturated state. The scale clogging at the tip of the air nozzle and the reduction of the ventilation cross section at the nozzle cross section require more pressure than necessary for the air supply source and cause uneven air blowing in the cross section direction of the slurry retention tank, resulting in the desired oxidation. There was an inconvenience that performance could not be secured.
【０００３】特開昭６２−８３０２４号公報には、酸化
空気の水蒸気分圧を、前記スラリー温度の露点における
水蒸気分圧以上にするために、酸化空気中に水蒸気を混
合する方法が記載されている。Japanese Unexamined Patent Publication (Kokai) No. 62-83024 describes a method of mixing steam into oxidizing air in order to make the steam partial pressure of oxidizing air equal to or higher than the steam partial pressure at the dew point of the slurry temperature. There is.
【０００４】[0004]
【発明が解決しようとする課題】上記の特開昭６２−８
３０２４号公報記載の方法は、酸化空気を吹き込むノズ
ル部のスケーリングを防止することを目的とするもので
あるが、つぎのような問題点を有している。 （１） 高価な水蒸気を多量に使用する。 （２） 水蒸気混合後の空気は温度が高く、空気配管や
スラリー槽内の空気噴霧ノズル部での熱放散のみでは、
水蒸気飽和温度まで低下せず、スケールが生成する。 （３） スケール生成を無くすためには、空気を強制的
に冷やさなければならず、空気冷却器を新たに設置する
必要がある。DISCLOSURE OF THE INVENTION Problems to be Solved by the Invention
The method described in Japanese Patent No. 3024 aims to prevent scaling of the nozzle portion blowing in oxidizing air, but has the following problems. (1) Use a large amount of expensive steam. (2) The temperature of the air after steam mixing is high, and the heat dissipation at the air spray nozzles in the air pipes and slurry tanks is not enough.
The scale does not fall to the water vapor saturation temperature. (3) In order to eliminate the scale generation, the air must be forcibly cooled and an air cooler must be newly installed.
【０００５】本発明は上記の諸点に鑑みなされたもの
で、水蒸気混合後の酸化用空気に、さらに水を混合する
ことにより、水蒸気使用量を低減か、水蒸気を使用しな
いことにより、ノズル部のスケーリングを確実に防止す
るようにした排煙脱硫方法及び装置を提供することを目
的とする。The present invention has been made in view of the above points, and the amount of steam used is reduced by further mixing water with the oxidizing air after mixing the steam, or the steam is not used. An object of the present invention is to provide a flue gas desulfurization method and apparatus that reliably prevent scaling.
【０００６】[0006]
【課題を解決するための手段】上記の目的を達成するた
めに、本発明の排煙脱硫方法は、カルシウム化合物含有
スラリーを排煙脱硫用吸収剤とし、石こう化反応を行な
わせるために酸化用空気を前記スラリーに吹き込むとと
もに、この吹込空気中の水蒸気分圧を前記スラリーの露
点における水蒸気分圧以上にするために水蒸気をこの吹
込空気に混合する排煙脱硫方法において、吹込空気に水
蒸気を混合した後、さらに、吹込空気に水を混合して吹
込空気を増湿冷却することを特徴としている。上記の方
法において、吹込空気に水を余剰に混合し、余剰水及び
水蒸気の凝縮水を、吹込空気とともに多孔ノズルからカ
ルシウム化合物含有スラリー中に均一に吹き込むことが
望ましい。また、本発明の排煙脱硫装置は、カルシウム
化合物含有スラリーを排煙脱硫用吸収剤とし、石こう化
反応を行なわせるために酸化用空気を前記スラリーに吹
き込む排煙脱硫装置において、酸化空気ブロワー９から
吸収塔１内下部の空気噴霧ノズル７間を空気母管１４で
接続し、該空気噴霧ノズル７を空気母管１４に突込み、
余剰水により空気母管１４内に液面をつくり、空気とと
もに余剰水を吹き込むようにしたことを特徴としてい
る。In order to achieve the above-mentioned object, the flue gas desulfurization method of the present invention uses a slurry containing a calcium compound as an flue gas desulfurization absorbent, which is used for oxidation in order to carry out a gypsum reaction. In the flue gas desulfurization method in which air is blown into the slurry and steam is mixed with the blown air so that the steam partial pressure in the blown air is equal to or higher than the steam partial pressure at the dew point of the slurry, the blown air is mixed with the steam. After that, the blow air is further mixed with water to humidify and cool the blow air. In the above-mentioned method, it is desirable to excessively mix water with the blowing air and uniformly blow the condensed water of the excess water and the steam into the calcium compound-containing slurry from the porous nozzle together with the blowing air. Further, the flue gas desulfurization apparatus of the present invention is a flue gas desulfurization apparatus in which a calcium compound-containing slurry is used as a flue gas desulfurization absorbent, and oxidizing air is blown into the slurry to carry out a gypsum reaction. To connect the air spray nozzles 7 in the lower part of the absorption tower 1 with an air mother pipe 14, and push the air spray nozzle 7 into the air mother pipe 14.
A feature is that a liquid level is created in the air mother pipe 14 by the excess water and the excess water is blown together with the air.
【０００７】図３は、本発明の方法における酸化用空
気、すなわち、水蒸気混合後の酸化用空気にさらに水を
混合した酸化用空気の温度と湿度との関係を示し、図４
は、従来の方法における酸化用空気、すなわち、水蒸気
のみを混合した酸化用空気の温度と湿度との関係を示し
ている。FIG. 3 shows the relationship between the temperature and the humidity of the oxidizing air in the method of the present invention, that is, the oxidizing air obtained by further mixing water with the oxidizing air after mixing with steam.
Shows the relationship between the temperature and the humidity of the oxidizing air in the conventional method, that is, the oxidizing air in which only steam is mixed.
【０００８】図３及び図４は、下記を基本条件としてい
る。 空気圧縮機入口空気 温度：３５℃ 湿度：６０％ 空気圧縮機出口空気 圧力：６５００mmＨ2 Ｏ スラリー中の噴出空気 温度：スラリー温度５２℃ 空気露点温度５５℃ 圧力：大気圧（実際は大気圧より若干高いが、便宜上大
気圧とした。） 供給水蒸気 温度：１５０℃ 圧力：４kg／cm GThe basic conditions shown in FIGS. 3 and 4 are as follows. Air compressor inlet air Temperature: 35 ° C Humidity: 60% Air compressor outlet air Pressure: 6500mmH 2 O Jet air in slurry Temperature: Slurry temperature 52 ° C Air dew point temperature 55 ° C Pressure: Atmospheric pressure (actually slightly higher than atmospheric pressure However, atmospheric pressure is used for convenience.) Supply steam temperature: 150 ° C Pressure: 4 kg / cm G
【０００９】図４に示すように、酸化用空気の圧縮機吹
込状態のＡ点（温度：３５℃、湿度：６０％）を圧縮機
により昇圧する。昇圧されることにより、断熱圧縮等に
より空気はＢ点まで昇温される（温度：９４℃）。この
空気を、吹込部スラリー温度の露点における水蒸気分圧
以上の水蒸気分圧を有するようにするため、水蒸気を混
合し、Ｃ点の状態とする（温度：１００℃、湿度：０．
１１５〔水蒸気kg／乾き空気kg〕）。Ｃ点の空気をＤ点
の水蒸気飽和温度まで温度を低下させ、スラリー中に噴
霧する。なお、Ｂ点の空気を予め冷却し、温度を低下さ
せた後、水蒸気を混合する方法もある。スラリー温度Ｅ
点より温度、湿度共高い空気の状態であるＤ点の空気
は、スラリー温度近くまで冷却される間に、水蒸気が凝
縮し、噴霧ノズル内面に水分が供給され、洗われること
により、スケール付着を防止する。As shown in FIG. 4, point A (temperature: 35 ° C., humidity: 60%) when the oxidizing air is blown into the compressor is boosted by the compressor. By increasing the pressure, the temperature of the air is raised to point B due to adiabatic compression (temperature: 94 ° C.). In order to make this air have a water vapor partial pressure that is equal to or higher than the water vapor partial pressure at the dew point of the temperature of the blowing part slurry, water vapor is mixed and brought to the state of point C (temperature: 100 ° C., humidity: 0.
115 (water vapor kg / dry air kg)). The temperature of the air at point C is lowered to the water vapor saturation temperature at point D, and sprayed into the slurry. There is also a method in which the air at the point B is cooled in advance, the temperature is lowered, and then steam is mixed. Slurry temperature E
The air at the point D, which is in a state where the temperature and humidity are both higher than the point, condenses water vapor while the temperature is close to the slurry temperature, water is supplied to the inner surface of the spray nozzle, and the scale is attached. To prevent.
【００１０】従来の水蒸気のみを酸化用空気に混合する
場合は以上のとおりである。しかし、Ｂ点（湿度：０．
０２２〔水蒸気kg／乾き空気kg〕）の空気を、Ｃ点（湿
度：０．１１５〔水蒸気kg／乾き空気kg〕）の状態にす
るのに、水蒸気混合量は０．０９３〔水蒸気kg／乾き空
気kg〕必要であり、また、Ｃ点（温度：１００℃）の空
気をＤ点（温度：５５℃）の状態にするには、冷却器が
必要である。The above is the case where only the conventional steam is mixed with the oxidizing air. However, point B (humidity: 0.
022 [water vapor kg / dry air kg]) is brought to the state of point C (humidity: 0.115 [water vapor kg / dry air kg]), and the amount of water vapor is 0.093 [water vapor kg / dry air]. Air kg] is required, and a cooler is required to bring the air at the point C (temperature: 100 ° C.) to the state at the point D (temperature: 55 ° C.).
【００１１】これに対して、図３に示す本発明の方法に
おいては、Ｂ点の空気は、Ｃ′点（温度：９９℃、湿
度：０．０９１〔水蒸気kg／乾き空気kg〕）にするため
の水蒸気の混合でよく、従来技術（図４）で必要な水蒸
気量：０．０９３kg／乾き空気kgに対し、本発明の方法
では０．０６９kg／乾き空気kgでよく、２５％の水蒸気
使用量の低減が図れる。また、図３のＣ′点の水蒸気混
合後の空気に水を混合するので、断熱冷却線に沿って空
気は増湿冷却され、Ｄ点の水蒸気飽和温度が容易に得ら
れ、空気冷却器等が不要である。On the other hand, in the method of the present invention shown in FIG. 3, the air at the point B is at the point C '(temperature: 99 ° C., humidity: 0.091 [water vapor kg / dry air kg]). The amount of water vapor required in the prior art (FIG. 4) is 0.093 kg / kg of dry air, whereas 0.069 kg / kg of dry air is sufficient in the method of the present invention, and 25% of water vapor is used. The amount can be reduced. Further, since water is mixed with the air after steam mixing at the point C'in FIG. 3, the air is humidified and cooled along the adiabatic cooling line, and the steam saturation temperature at the point D can be easily obtained. Is unnecessary.
【００１２】また、水の混合量は、増湿冷却を確実にす
るため、増湿水分量以上に供給することが望ましく、こ
の余剰水は多孔ノズルからスラリー中に均一に噴霧され
るため、水蒸気の凝縮による水分の洗浄効果と相俟っ
て、スケール付着の防止をより一層確実に行なえる。な
お、余剰水を多孔噴霧ノズルから均一に噴霧させる構成
としては、図２に示すように、空気噴霧ノズル７を空気
母管１４内に突込み、余剰水１５により母管１４内に液
面をつくり、空気とともに余剰水１５を吹き込む構成が
有効であることを確認している。The amount of water mixed is preferably more than the amount of moisture for humidification in order to ensure the humidification cooling, and this excess water is uniformly sprayed into the slurry from the multi-hole nozzle, so steam Combined with the effect of cleaning water due to condensation of water, it is possible to prevent scale adhesion even more reliably. As a configuration for uniformly spraying excess water from the multi-hole spray nozzle, as shown in FIG. 2, the air spray nozzle 7 is thrust into the air mother pipe 14 and the surplus water 15 creates a liquid surface in the mother pipe 14. It has been confirmed that the structure in which the excess water 15 is blown together with the air is effective.
【００１３】[0013]
【実施例】以下、本発明を実施例及び比較例に基づいて
さらに詳細に説明するが、本発明は下記実施例に何ら限
定されるものではなく、その要旨を変更しない範囲にお
いて適宜変更して実施することが可能なものである。The present invention will be described in more detail based on the following examples and comparative examples. However, the present invention is not limited to the following examples, and may be appropriately modified within the scope of the invention. It can be implemented.
【００１４】比較例１ 図５に示す従来方法を実施する装置を用いて排煙脱硫処
理を行なった。亜硫酸ガス１０００ppm を含む排ガス２
を、８０００m N ／H 吸収塔１に導入し、石灰石供給ラ
イン８から供給された石灰石によりpH５．２、カルシウ
ム化合物スラリー濃度１５wt％（石こう：１４．８wt
％、亜硫酸カルシウム０．０５wt％、石灰石０．１５wt
％）に調整された温度５０℃の吸収塔スラリーを、下部
液溜槽４から吸収塔循環ポンプ５によりスプレーノズル
６から吸収塔スラリーを噴霧させ、排ガス中の亜硫酸ガ
スを除去し、清浄な排ガス３として吸収塔１から排出さ
せた。Comparative Example 1 Flue gas desulfurization treatment was carried out using an apparatus for carrying out the conventional method shown in FIG. Exhaust gas containing sulfurous acid gas 1000ppm 2
Was introduced into the absorption tower 1 of 8000 m N / H, pH was 5.2 and the concentration of calcium compound slurry was 15 wt% (gypsum: 14.8 wt%) by the limestone supplied from the limestone supply line 8.
%, Calcium sulfite 0.05 wt%, limestone 0.15 wt
%) Adjusted to 50 ° C., the absorption tower slurry is sprayed from the lower liquid storage tank 4 from the spray nozzle 6 by the absorption tower circulation pump 5 to remove the sulfurous acid gas in the exhaust gas, and the clean exhaust gas 3 Was discharged from the absorption tower 1.
【００１５】また、吸収された亜硫酸ガスは、亜硫酸塩
として吸収塔スラリーに含まれているため、これを硫酸
塩（石こう）にするための酸化用空気は、酸化空気ブロ
ワー９で２００m N ／H を０．６５atg まで加圧し、ア
フタークーラー１１で５０℃迄冷却した後、温度１５０
℃、圧力４kg／cm Gの水蒸気１７kg／H を、水蒸気供給
ライン１０から酸化用空気ラインに混合し、吸収塔下部
液溜槽４の空気噴霧ノズル７から吸収塔スラリー中に噴
出させた。この状態での運転を１週間実施したが、空気
噴霧ノズル内面にはスケール付着は認められなかった。Further, since the absorbed sulfurous acid gas is contained in the absorption tower slurry as a sulfite, the oxidizing air for converting the sulfurous acid gas into the sulfate (gypsum) is 200 m N / H by the oxidizing air blower 9. Is pressurized to 0.65 atg, cooled to 50 ° C with the aftercooler 11, and then heated to 150 ° C.
17 kg / H 2 of steam at 4 ° C. and a pressure of 4 kg / cm G was mixed from the steam supply line 10 to the oxidation air line and jetted into the absorption tower slurry from the air atomizing nozzle 7 of the lower absorption tower liquid tank 4. The operation in this state was carried out for one week, but no scale adhesion was observed on the inner surface of the air spray nozzle.
【００１６】一方、酸化空気ブロワー７出口部のアフタ
ークーラー１１に、冷却水を入れず、空気温度８０℃の
状態で水蒸気１７kg／H を混合し、１週間の運転を実施
したところ、図６に示すように、スケール１３が噴霧ノ
ズル７内面に発生し、空気流路が狭められ、供給空気量
の低下原因になった。On the other hand, the aftercooler 11 at the outlet of the oxidizing air blower 7 was mixed with 17 kg / H of water vapor at a temperature of 80 ° C. without cooling water, and was operated for one week. As shown, the scale 13 was generated on the inner surface of the spray nozzle 7, and the air passage was narrowed, which caused a decrease in the supply air amount.
【００１７】実施例１ 図１に示す装置を用い、比較例１に対し、酸化用空気の
吸収塔スラリーへの吹込方法を変えて実施した例を以下
に示す。酸化用空気２００m N ／H をブロワー９で０．
６５atg 迄昇圧し、８０℃まで昇温された部分に、水蒸
気１４kg／H を混合した後、工業用水供給ライン１２か
ら更に工業用水１０kg／H を混合し、吸収塔１下部液溜
槽４の空気噴霧ノズル７から吸収塔スラリー中に噴出さ
せた。この状態での運転を１週間実施したが、空気噴霧
ノズル７内面には、スケール付着は認められなかった。Example 1 An example in which the apparatus shown in FIG. 1 was used and the method of blowing the oxidizing air into the absorption tower slurry was changed from that of Comparative Example 1 is shown below. Oxidizing air of 200 m N / H was blown with a blower 9.
After mixing 14 kg / H of steam to the portion heated up to 65 atg and heated to 80 ° C., 10 kg / H of industrial water was further mixed from the industrial water supply line 12, and air was sprayed in the lower liquid storage tank 4 of the absorption tower 1. It was ejected from the nozzle 7 into the absorption tower slurry. The operation in this state was carried out for one week, but no scale adhesion was observed on the inner surface of the air spray nozzle 7.
【００１８】また、工業用水及び水蒸気共に酸化用空気
中に混合せず、１週間運転した結果、噴霧ノズル７内面
にスケールが生成されていたが、スケールを除去せず、
そのままの状態で、工業用水及び水蒸気を前記と同じ量
で１日運転した結果、スケールは完全に除去されてお
り、本発明の方法はスケール除去にも効果があることが
確認できた。Further, neither industrial water nor steam was mixed in the oxidizing air, and after operating for 1 week, scale was generated on the inner surface of the spray nozzle 7. However, scale was not removed,
As a result of operating the industrial water and steam in the same amount for one day as they were, the scale was completely removed, and it was confirmed that the method of the present invention is also effective for scale removal.
【００１９】以上の実施例１での空気噴霧ノズル部での
圧力は１．４５ata 、吸収塔スラリー温度は５０℃であ
り、スラリー温度５０℃での飽和水蒸気分圧は９２．５
mmHgであることから、露点での水蒸気量は、In Example 1 above, the pressure at the air atomizing nozzle was 1.45ata, the absorption tower slurry temperature was 50 ° C., and the saturated steam partial pressure at the slurry temperature 50 ° C. was 92.5.
Since it is mmHg, the amount of water vapor at the dew point is
【００２０】２００〔m N ／H 〕×９２．５〔mmHg〕÷
（１．４５×７６０−９２．５〔mmHg〕）×１８〔kg／
kg・mol 〕÷２２．４〔m N ／kg・mol 〕＝１５〔kg／
H 〕 であり、比較例１では露点以上の水蒸気混合量で、実施
例１では露点以下の水蒸気量で工業用水にて露点以上と
したものである。なお、実施例１では工業用水を酸化用
空気に混合する場合について説明したが、工業用水に限
ることなく、他の水を使用することも可能である。200 [m N /H]×92.5 [mmHg] ÷
(1.45 x 760-92.5 [mmHg]) x 18 [kg /
kg ・ mol] ÷ 22.4 [m N / kg ・ mol] = 15 [kg /
H 2], in Comparative Example 1, the amount of water vapor mixed above the dew point was used, and in Example 1, the amount of water vapor below the dew point was set above the dew point of industrial water. In addition, although the case where the industrial water is mixed with the oxidizing air has been described in the first embodiment, the water is not limited to the industrial water, and other water may be used.
【００２１】[0021]
【発明の効果】本発明は上記のように構成されているの
で、つぎのような効果を奏する。 （１） 水蒸気混合後の酸化用空気に、さらに水を混合
し、この空気を増湿冷却するので、混合水蒸気量の低減
を図ることができる。 （２） 水蒸気飽和温度の空気を容易に得ることがで
き、従来方式におけるような空気冷却器が不要である。 （３） 請求項２の場合は、混合した水の余剰分が多孔
ノズルから均一に噴出されるので、水蒸気の凝縮水によ
る洗浄効果と相俟って、スケール付着の防止をより一層
確実に行うことができる。 （４） 請求項３の場合は、混合した水の余剰分が多孔
ノズルから均一に噴出されるので、ノズルのスケール付
着の防止を確実に行うことができるとともに、水蒸気を
使用することもなく実施できるため、ランニングコスト
の大幅削減が達成される。Since the present invention is configured as described above, it has the following effects. (1) Since the oxidizing air after the steam mixing is further mixed with water and the air is humidified and cooled, the amount of mixed steam can be reduced. (2) Air having a water vapor saturation temperature can be easily obtained, and an air cooler as in the conventional method is unnecessary. (3) In the case of claim 2, since the excess amount of the mixed water is uniformly ejected from the multi-hole nozzle, combined with the cleaning effect of the condensed water of the steam, the scale adhesion is prevented more reliably. be able to. (4) In the case of claim 3, since the excess amount of the mixed water is uniformly ejected from the multi-hole nozzle, it is possible to reliably prevent the scale from adhering to the nozzle, and to carry out without using steam. Therefore, the running cost can be significantly reduced.
【図面の簡単な説明】[Brief description of drawings]
【図１】本発明の排煙脱硫方法を実施する装置の一例
（実施例１）を示す系統的説明図である。FIG. 1 is a systematic explanatory view showing an example (Example 1) of an apparatus for carrying out the flue gas desulfurization method of the present invention.
【図２】本発明の排煙脱硫装置における空気噴霧ノズル
まわりの一例を示すもので、下部液溜槽に接続した空気
母管、空気噴霧ノズル及び余剰水の関係を示す断面説明
図である。FIG. 2 is a cross-sectional explanatory view showing an example of an area around an air spray nozzle in a flue gas desulfurization apparatus of the present invention, showing a relationship between an air mother pipe connected to a lower liquid reservoir, an air spray nozzle, and excess water.
【図３】本発明の方法における酸化用空気、すなわち、
水蒸気混合後の空気に水を混合した空気の温度と湿度と
の関係を示すグラフである。FIG. 3 is the oxidizing air in the method of the present invention, ie,
It is a graph which shows the relationship between the temperature and humidity of the air which mixed water with the air after steam mixing.
【図４】従来の方法における酸化用空気、すなわち、水
蒸気のみを混合した酸化用空気の温度と湿度との関係を
示すグラフである。FIG. 4 is a graph showing a relationship between temperature and humidity of oxidizing air in the conventional method, that is, oxidizing air in which only steam is mixed.
【図５】比較例１（従来方式）で用いた装置の系統的説
明図である。FIG. 5 is a systematic explanatory diagram of an apparatus used in Comparative Example 1 (conventional method).
【図６】比較例１における空気噴霧ノズル内の状態を示
す断面説明図である。FIG. 6 is a cross-sectional explanatory view showing a state inside the air spray nozzle in Comparative Example 1.
１ 吸収塔 ２ 排ガス ３ 排ガス ４ 下部液溜槽 ５ 吸収塔循環ポンプ ６ スプレーノズル ７ 空気噴霧ノズル ８ 石灰石供給ライン ９ 酸化空気ブロワー １０ 水蒸気供給ライン １１ アフタークーラー １２ 工業用水供給ライン １３ スケール １４ 空気母管 １５ 余剰水 1 Absorption Tower 2 Exhaust Gas 3 Exhaust Gas 4 Lower Liquid Reservoir 5 Absorption Tower Circulation Pump 6 Spray Nozzle 7 Air Spray Nozzle 8 Limestone Supply Line 9 Oxidized Air Blower 10 Steam Supply Line 11 Aftercooler 12 Industrial Water Supply Line 13 Scale 14 Air Mother Pipe 15 Surplus water
Claims (3)
硫用吸収剤とし、石こう化反応を行なわせるために酸化
用空気を前記スラリーに吹き込むとともに、この吹込空
気中の水蒸気分圧を前記スラリーの露点における水蒸気
分圧以上にするために水蒸気をこの吹込空気に混合する
排煙脱硫方法において、 吹込空気に水蒸気を混合した後、さらに、吹込空気に水
を混合して吹込空気を増湿冷却することを特徴とする排
煙脱硫方法。1. A calcium compound-containing slurry is used as an absorbent for flue gas desulfurization, and oxidizing air is blown into the slurry to carry out a gypsum reaction, and the partial pressure of water vapor in the blown air at the dew point of the slurry is measured. In the flue gas desulfurization method in which steam is mixed with the blown air so as to have a partial pressure of steam or higher, after mixing the blown air with the steam, water is further mixed with the blown air to humidify and cool the blown air. Characteristic flue gas desulfurization method.
び水蒸気の凝縮水を、吹込空気とともに多孔ノズルから
カルシウム化合物含有スラリー中に均一に吹き込むこと
を特徴とする請求項１記載の排煙脱硫方法。2. The exhaust according to claim 1, wherein excess water is mixed with the blown air, and the condensed water of the excess water and the steam is blown into the calcium compound-containing slurry uniformly from the porous nozzle together with the blown air. Smoke desulfurization method.
硫用吸収剤とし、石こう化反応を行なわせるために酸化
用空気を前記スラリーに吹き込む排煙脱硫装置におい
て、 酸化空気ブロワー（９）から吸収塔（１）内下部の空気
噴霧ノズル（７）間を空気母管（１４）で接続し、該空
気噴霧ノズル（７）を空気母管（１４）に突込み、余剰
水により空気母管（１４）内に液面をつくり、空気とと
もに余剰水を吹き込むようにしたことを特徴とする排煙
脱硫装置。3. A flue gas desulfurization apparatus in which a calcium compound-containing slurry is used as an flue gas desulfurization absorbent, and oxidizing air is blown into the slurry to carry out a gypsum reaction, from an oxidizing air blower (9) to an absorption tower ( 1) An air mother pipe (14) is connected between the air spray nozzles (7) at the inner and lower parts, the air atomizer nozzle (7) is thrust into the air mother pipe (14), and the excess water causes the inside of the air mother pipe (14). A flue gas desulfurization device characterized in that a liquid level is created on the inside of the equipment to blow excess water together with air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5031298A JP2549050B2 (en) | 1993-01-27 | 1993-01-27 | Flue gas desulfurization method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5031298A JP2549050B2 (en) | 1993-01-27 | 1993-01-27 | Flue gas desulfurization method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06218227A true JPH06218227A (en) | 1994-08-09 |
| JP2549050B2 JP2549050B2 (en) | 1996-10-30 |
Family
ID=12327390
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5031298A Expired - Lifetime JP2549050B2 (en) | 1993-01-27 | 1993-01-27 | Flue gas desulfurization method and device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2549050B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002320820A (en) * | 2001-04-26 | 2002-11-05 | Kawasaki Steel Corp | Air header and method for washing its nozzle |
| EP2087933A1 (en) * | 2008-02-07 | 2009-08-12 | Alstom Technology Ltd | A gas sparger for supplying oxidation gas to a wet scrubber |
| KR100914836B1 (en) * | 2009-05-06 | 2009-09-02 | 김윤철 | Device safety for steam trap |
| CN101844036A (en) * | 2010-05-11 | 2010-09-29 | 上海龙净环保科技工程有限公司 | Wet flue gas desulfurization (WFGD) process for gypsum through oxidization in tower by using calcium-based strongly basic substance |
| CN115400563A (en) * | 2022-08-16 | 2022-11-29 | 安徽华电宿州发电有限公司 | Oxidation air system security method in wet desulphurization process |
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|---|---|---|---|---|
| JPS60154157A (en) * | 1984-01-25 | 1985-08-13 | Mitsubishi Heavy Ind Ltd | Method for measuring continuously concentration of caco3 and concentration of caso3 in slurry |
| JPS6283024A (en) * | 1985-10-09 | 1987-04-16 | Mitsubishi Heavy Ind Ltd | Desulfurization method for flue gas |
| JPS62258729A (en) * | 1986-05-02 | 1987-11-11 | Mitsubishi Heavy Ind Ltd | Gas blowing-in method for aeration tank |
-
1993
- 1993-01-27 JP JP5031298A patent/JP2549050B2/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60154157A (en) * | 1984-01-25 | 1985-08-13 | Mitsubishi Heavy Ind Ltd | Method for measuring continuously concentration of caco3 and concentration of caso3 in slurry |
| JPS6283024A (en) * | 1985-10-09 | 1987-04-16 | Mitsubishi Heavy Ind Ltd | Desulfurization method for flue gas |
| JPS62258729A (en) * | 1986-05-02 | 1987-11-11 | Mitsubishi Heavy Ind Ltd | Gas blowing-in method for aeration tank |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002320820A (en) * | 2001-04-26 | 2002-11-05 | Kawasaki Steel Corp | Air header and method for washing its nozzle |
| EP2087933A1 (en) * | 2008-02-07 | 2009-08-12 | Alstom Technology Ltd | A gas sparger for supplying oxidation gas to a wet scrubber |
| WO2009098055A1 (en) * | 2008-02-07 | 2009-08-13 | Alstom Technology Ltd | A gas sparger for supplying oxidation gas to a wet scrubber |
| JP2011511707A (en) * | 2008-02-07 | 2011-04-14 | アルストム テクノロジー リミテッド | Gas sparger for supplying oxidizing gas to wet scrubber |
| US8377174B2 (en) | 2008-02-07 | 2013-02-19 | Alstom Technology Ltd | Gas sparger for supplying oxidation gas to a wet scrubber |
| KR101272141B1 (en) * | 2008-02-07 | 2013-06-05 | 알스톰 테크놀러지 리미티드 | A gas sparger for supplying oxidation gas to a wet scrubber |
| KR100914836B1 (en) * | 2009-05-06 | 2009-09-02 | 김윤철 | Device safety for steam trap |
| CN101844036A (en) * | 2010-05-11 | 2010-09-29 | 上海龙净环保科技工程有限公司 | Wet flue gas desulfurization (WFGD) process for gypsum through oxidization in tower by using calcium-based strongly basic substance |
| CN115400563A (en) * | 2022-08-16 | 2022-11-29 | 安徽华电宿州发电有限公司 | Oxidation air system security method in wet desulphurization process |
| CN115400563B (en) * | 2022-08-16 | 2023-07-14 | 安徽华电宿州发电有限公司 | Security method for oxidation wind system in wet desulfurization process |
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|---|---|
| JP2549050B2 (en) | 1996-10-30 |
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