JPH04110020A - Exhaust gas purifying method - Google Patents
Exhaust gas purifying methodInfo
- Publication number
- JPH04110020A JPH04110020A JP2226749A JP22674990A JPH04110020A JP H04110020 A JPH04110020 A JP H04110020A JP 2226749 A JP2226749 A JP 2226749A JP 22674990 A JP22674990 A JP 22674990A JP H04110020 A JPH04110020 A JP H04110020A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- desulfurization
- desulfurizing agent
- water
- temp
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims description 29
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 59
- 230000023556 desulfurization Effects 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 44
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000003546 flue gas Substances 0.000 claims abstract description 5
- 238000007664 blowing Methods 0.000 claims abstract description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 17
- 239000000920 calcium hydroxide Substances 0.000 claims description 17
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 17
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 17
- 238000000746 purification Methods 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 150000002681 magnesium compounds Chemical class 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 23
- 239000000428 dust Substances 0.000 abstract description 14
- 230000002378 acidificating effect Effects 0.000 abstract description 5
- 239000002341 toxic gas Substances 0.000 abstract description 2
- 239000010408 film Substances 0.000 abstract 1
- 239000010409 thin film Substances 0.000 abstract 1
- 239000002245 particle Substances 0.000 description 6
- 229910052749 magnesium Inorganic materials 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 238000005507 spraying Methods 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 231100000676 disease causative agent Toxicity 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 239000004572 hydraulic lime Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000011164 primary particle Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 230000004580 weight loss Effects 0.000 description 1
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は、消石灰およびマグネシウムを含んだ消石灰を
脱硫剤とする脱硫装置において、高温領域での脱硫剤の
高比表面積化および低温領域での加湿により脱硫率を改
善する方法および装置に関するものである。Detailed Description of the Invention [Industrial Field of Application] The present invention is directed to a desulfurization device using slaked lime and slaked lime containing magnesium as a desulfurization agent. The present invention relates to a method and apparatus for improving desulfurization efficiency through humidification.
［従来の技術〕
火力発電所における重油焚、石炭焚ボイラから排出され
る排ガス中には、硫黄化合物（ＳＯｘ）やＨＣｌなどの
酸性有害物質、が通常、１００〜３゜０００ｐｐｍの開
会で含まれており、酸性雨や光化学スモッグの原因物質
とされるため、その効果的な処理手段が望まれている。[Prior art] The exhaust gas emitted from heavy oil-fired and coal-fired boilers in thermal power plants usually contains acidic harmful substances such as sulfur compounds (SOx) and HCl at an opening concentration of 100 to 3,000 ppm. Since it is said to be a causative agent of acid rain and photochemical smog, effective treatment methods are desired.
従来から湿式法（例えば石灰石−石膏法）または乾式法
（活性炭法）が実施されているが、湿式法は有害物質の
除去率が高い反面、廃水処理が困難で、排ガスを再加熱
する必要があり、設備費や運転費が高く、乾式法では高
い除去率が得られないという問題があった。Conventionally, wet methods (e.g. limestone-gypsum method) or dry methods (activated carbon method) have been used, but while the wet method has a high removal rate of harmful substances, it is difficult to treat wastewater and requires reheating of exhaust gas. However, there were problems in that the equipment costs and operating costs were high, and a high removal rate could not be obtained with the dry method.
このため、無排水の低コストプロセスで高い除去率が得
られる脱硫方法の開発が望まれている。Therefore, it is desired to develop a desulfurization method that can obtain a high removal rate with a wastewater-free, low-cost process.
ボイラなどの排ガスの脱硫法としては、上記方法のほか
に、消石灰やそのスラリを排ガス中に噴霧する半乾式法
や火炉内あるいは煙道内の高温ガス中に石灰石を直接分
散させて酸性有害物質を除去する乾式法が提案されてお
り、設備費や運転費が安いという特徴を有しているが、
いずれの方法も除去率が低いという問題がある。In addition to the above-mentioned methods, desulfurization methods for exhaust gas from boilers include a semi-dry method in which slaked lime or its slurry is sprayed into the exhaust gas, and a method in which limestone is directly dispersed in the high-temperature gas in the furnace or flue to remove acidic harmful substances. A dry method for removal has been proposed, and has the feature of low equipment and operating costs.
Both methods have the problem of low removal rates.
消石灰や生石灰を排ガス中に噴霧して排ガス中のＳＯ２
と反応させ、これを集塵装置で除去する方法の代表的な
フローシートを第４図に示す、ボイラ１からの排ガスは
エアヒータ２で温度を下げられ、脱硫塔３に導かれる。SO2 in exhaust gas is removed by spraying slaked lime or quicklime into exhaust gas.
FIG. 4 shows a typical flow sheet of a method for reacting with the oxidation gas and removing it using a dust collector. The exhaust gas from the boiler 1 is lowered in temperature by the air heater 2, and is led to the desulfurization tower 3.
消石灰などの脱硫剤Ａは煙道４または脱硫塔３内に噴霧
して供給され、この時水Ｂも供給されることにより排ガ
スの温度を下げ、湿度を上げる。この除水Ｂは脱硫剤Ａ
と別に供給しても、脱硫剤Ａをスラリとして同時に供給
してもよい。反応した脱硫剤Ａは排ガス中の灰とともに
集塵器５で捕集され、廃棄される。このような方法にお
いて、酸性有害物質の除去率は排ガス中の水分く相対湿
度）が支配的であるとされている。すなわち除去率を上
げるためには、排ガスの温度を下げ、水分を上げること
が必要である。水分濃度を上げるために、水や消石灰ス
ラリを噴霧する方法が提案されているが、このようなガ
ス中の水分濃度を上げる方法では除去率の向上は十分で
はない、除去率が低い場合は、集塵器によって捕集され
た未反応の脱硫剤を含む粒子に水や蒸気を添加し、表面
に形成された反応生成物の殻を破壊した後この一部を再
び排ガス中に噴霧することによって除去率を向上する方
法も提案されている（例えば、米国特許第３４３１２８
９号明細書、特開昭６１−３５８２７号）、シかし、集
塵器で捕集された未反応の脱硫剤を含む粒子をリサイク
ルする場合、集塵器で処理しなければならない粒子量が
増加し、集塵器の処理容量を増やさなければならなくな
る。また、リサイクルのための設備も必要になるため、
設備費や運転費も高くなるという問題があった。A desulfurizing agent A such as slaked lime is supplied by spraying into the flue 4 or the desulfurizing tower 3, and water B is also supplied at this time to lower the temperature of the exhaust gas and increase the humidity. This water removal B is desulfurization agent A
The desulfurizing agent A may be supplied separately or simultaneously as a slurry. The reacted desulfurizing agent A is collected together with the ash in the exhaust gas by the dust collector 5 and discarded. In such a method, the removal rate of acidic harmful substances is said to be dominated by moisture (relative humidity) in the exhaust gas. That is, in order to increase the removal rate, it is necessary to lower the temperature of the exhaust gas and increase the moisture content. Spraying water or slaked lime slurry has been proposed to increase the moisture concentration, but such methods of increasing the moisture concentration in the gas do not sufficiently improve the removal rate, and if the removal rate is low, By adding water or steam to particles containing unreacted desulfurization agent collected by a dust collector, and destroying the shell of reaction products formed on the surface, a part of this is sprayed back into the exhaust gas. Methods to improve the removal rate have also been proposed (e.g., U.S. Pat. No. 3,431,28
9 specification, JP-A No. 61-35827), when recycling particles containing unreacted desulfurization agent collected by a dust collector, the amount of particles that must be treated by the dust collector will increase, making it necessary to increase the processing capacity of the dust collector. In addition, equipment for recycling will also be required.
There was a problem that equipment costs and operating costs also increased.
そこで、脱硫剤粒子を排ガス中に分散させて脱硫率を向
上させるため、例えば、特開昭６０−２１６８３２号記
載の方法が提案されている。これによれば、１０μｍ以
下の一次粒子から成る高濃度脱硫剤分散ガスを煙道に導
入することによって脱硫率が２〜３倍程度向上する。Therefore, in order to improve the desulfurization rate by dispersing desulfurizing agent particles in the exhaust gas, a method described, for example, in JP-A-60-216832 has been proposed. According to this, by introducing a highly concentrated desulfurizing agent-dispersed gas consisting of primary particles of 10 μm or less into the flue, the desulfurization rate can be improved by about 2 to 3 times.
［発明が解決しようとする課題］
しかし、前記特開昭６０−２１６８３２号公報記載の方
法でも専用の粒子分散装置が必要になるため設備が複雑
化するという問題点があった。[Problems to be Solved by the Invention] However, the method described in Japanese Patent Application Laid-Open No. 60-216832 also requires a dedicated particle dispersion device, which poses a problem in that the equipment becomes complicated.
そこで、本発明の目的は消石灰を含む脱硫剤を用いて、
しかも簡易なシステムで高い脱硫率を得る排ガス浄化方
法を提供することにある。Therefore, the purpose of the present invention is to use a desulfurizing agent containing slaked lime,
Moreover, it is an object of the present invention to provide an exhaust gas purification method that achieves a high desulfurization rate with a simple system.
［課題を解決するための手段］ 本発明の目的は次の構成により達成される。[Means to solve the problem] The object of the present invention is achieved by the following configuration.
すなわち、燃焼装置から排出される排ガスに消石灰また
はマグネシウム化合物含有消石灰を含む脱硫剤を用いて
水分を吹き込みながら脱硫反応を行わせる排ガス処理法
において。That is, in an exhaust gas treatment method in which a desulfurization reaction is carried out while blowing moisture into exhaust gas discharged from a combustion device using a desulfurization agent containing slaked lime or slaked lime containing a magnesium compound.
脱硫剤の導入位置の温度が、４００℃から７００℃の範
囲にありかっ、水分吹き込み位置の温度が３０℃から２
００℃の範囲にある排ガス浄化方法、
である。The temperature at the introduction point of the desulfurizing agent is in the range of 400℃ to 700℃, and the temperature at the moisture injection point is in the range of 30℃ to 2℃.
A method for purifying exhaust gas in the range of 00°C.
［作用］
脱硫剤を４００℃〜７００℃の範囲の煙道ガスに供給す
ると
（Ｃａ、Ｍ−ｇ）（ＯＨＬ−（Ｃａ、Ｍｇ）Ｏ＋Ｈ２０
という反応により水分が除去される。この後、水および
水蒸気を３０℃〜２００℃という低温で導入することに
よって下式のような水和反応を起こさせる。[Effect] When the desulfurization agent is supplied to the flue gas in the range of 400°C to 700°C, (Ca, M-g) (OHL-(Ca, Mg)O+H20
Water is removed by this reaction. Thereafter, water and steam are introduced at a low temperature of 30°C to 200°C to cause a hydration reaction as shown in the following formula.
（Ｃａ、Ｍｇ）Ｏ＋ＨｚＯ−（Ｃａ 、Ｍｇ）（ＯＨ）
ａ上記処理によって該脱硫剤が高比表面積化されること
は公知であるが、この際、水蒸気に液状の水を添加する
ことにより上記の脱硫剤表面に薄い水の層が形成され、
脱硫剤の高比表面積化との相乗効果で脱硫率が改善され
る。(Ca, Mg)O+HzO-(Ca,Mg)(OH)
a It is known that the specific surface area of the desulfurizing agent is increased by the above treatment, but at this time, by adding liquid water to the steam, a thin layer of water is formed on the surface of the desulfurizing agent,
The desulfurization rate is improved by the synergistic effect with the high specific surface area of the desulfurization agent.
［実施例］
本発明は、下記の実施例によって、さらに詳細に説明さ
れるが、下記の例で制限されるものではない。[Examples] The present invention will be explained in more detail by the following examples, but is not limited thereto.
実施例１
脱硫剤として消石灰を用い、石炭焚ボイラの排ガスを脱
硫処理する場合について、本発明法による装置を適用し
た例を用いて説明する。Example 1 A case of desulfurizing exhaust gas from a coal-fired boiler using slaked lime as a desulfurizing agent will be described using an example in which an apparatus according to the present invention is applied.
第１図において、ボイラ１からの排ガスは脱硫剤を加え
られた後エアヒータ２で温度を下げられ、脱硫反応塔３
に導かれる。本実施例ではガス温度４００℃の部位に上
記脱硫剤を添加した。脱硫反応塔３内でノズル４より水
を噴霧し、脱硫剤に水を添加する。このような処理がな
された脱硫剤は、排カス中のＳＯ２などの酸性有毒ガス
と反応し、反応した脱硫剤は排ガス中の灰とともに集塵
器５で捕集され、廃棄される。In Fig. 1, the exhaust gas from the boiler 1 is added with a desulfurization agent, and then the temperature is lowered by the air heater 2, and the temperature is lowered by the desulfurization reaction tower 3.
guided by. In this example, the above desulfurization agent was added to the region where the gas temperature was 400°C. Water is sprayed from a nozzle 4 in the desulfurization reaction tower 3, and water is added to the desulfurization agent. The desulfurizing agent subjected to such treatment reacts with acidic toxic gas such as SO2 in the exhaust gas, and the reacted desulfurizing agent is collected together with the ash in the exhaust gas by the dust collector 5 and discarded.
この装置を用いて、Ａ炭（石炭中の硫黄分１゜０％）を
燃焼したときの脱硫性能を測定した。ただし、脱硫剤は
消石灰を用い、消石灰を排ガス中に含まれるＳＯ２に対
しモル比で２倍（以下、Ｃａ 、′Ｓ ＝ ２と略す）
添加した。また、脱硫反応塔３内では排ガスに対し重量
比で５％の水を添加した。水導入時の塔内湯度は７０℃
であった。なお、脱硫反応塔３に供給される直前の脱硫
剤をサンプリングし、１１０℃の雰囲気下で脱硫剤の重
量が恒量になるまで乾燥し、その時の重量減少から水分
量を測定したところ０．５％であった。Using this device, the desulfurization performance was measured when coal A (sulfur content in coal: 1.0%) was burned. However, slaked lime is used as the desulfurization agent, and the molar ratio of slaked lime to SO2 contained in the exhaust gas is twice (hereinafter abbreviated as Ca, 'S = 2).
Added. Furthermore, in the desulfurization reaction tower 3, 5% water by weight was added to the exhaust gas. The temperature inside the tower when water is introduced is 70℃
Met. In addition, the desulfurization agent was sampled just before being supplied to the desulfurization reaction tower 3, and dried in an atmosphere of 110°C until the weight of the desulfurization agent became constant.The water content was measured from the weight loss at that time, and it was found to be 0.5. %Met.
ボイラ１出口および集塵器５出口において、ガス中の水
分を除去した後、ＳＯ２濃度を測定したところそれぞれ
８２０ｐｐｍおよび９０ｐｐｍであった。すなわち、排
ガス中のＳ０２の内８９％が除去されたことになる。After removing moisture from the gas at the boiler 1 outlet and dust collector 5 outlet, SO2 concentrations were measured and found to be 820 ppm and 90 ppm, respectively. That is, 89% of S02 in the exhaust gas was removed.
実施例２
実施例１と同一の装置を用いて、脱硫剤導入部分の温度
が７００℃の場合について脱硫率を測定した。他の条件
は実施例１と同一である。この時は、集塵器５の出口に
おけるＳ０２の濃度は８５ｐｐｍであり、脱硫率９０％
が得られた。Example 2 Using the same apparatus as in Example 1, the desulfurization rate was measured when the temperature of the desulfurizing agent introduction portion was 700°C. Other conditions are the same as in Example 1. At this time, the concentration of S02 at the outlet of the dust collector 5 is 85 ppm, and the desulfurization rate is 90%.
was gotten.
実施例３
実施例１と同一の装置を用いて、水導入部分の温度が３
０．５０．１５０．２００および２５０℃の場合につい
て相対湿度と脱硫率との関係を測定した。他の条件は実
施例１と同一である。この結果を第２図に示す。湿度と
脱硫率との関係は比例的であることがわかる。この関係
から、相対湿度が重要であるが、実施条件から判断する
と３０℃〜２００℃が水導入部の温度として望ましいと
いえる。Example 3 Using the same equipment as in Example 1, the temperature of the water introduction part was 3.
The relationship between relative humidity and desulfurization rate was measured for the cases of 0.50.150.200°C and 250°C. Other conditions are the same as in Example 1. The results are shown in FIG. It can be seen that the relationship between humidity and desulfurization rate is proportional. From this relationship, relative humidity is important, but judging from the implementation conditions, it can be said that a temperature of 30°C to 200°C is desirable as the temperature of the water introduction part.
実施例４
実施例１と同一の装置を用いて、同一条件下でＣａ：Ｍ
ｇ＝１ ： １ （モル比）の水酸化物脱硫剤による脱
硫率を測定しな。Example 4 Using the same equipment as in Example 1 and under the same conditions, Ca:M
Measure the desulfurization rate using a hydroxide desulfurization agent with a molar ratio of g=1:1.
脱硫剤は排ガス中に含まれるＳ Ｏ２に対しモル比で２
倍（以下、（Ｃａ、Ｍｇ）／Ｓ＝２と略す）添加した。The desulfurization agent has a molar ratio of 2 to SO2 contained in the exhaust gas.
(hereinafter abbreviated as (Ca, Mg)/S=2) was added.
この時は、集塵器５の出口におけるＳＯ２濃度は８０ｐ
ｐｍであり、脱硫率９０％が得られた。At this time, the SO2 concentration at the outlet of the dust collector 5 is 80p.
pm, and a desulfurization rate of 90% was obtained.
実施例５
実施例１と同一の装置を用いて、水噴霧を煙道ガス上流
方向に向かって行った場合の脱硫率を測定した。噴霧角
は、０〜１８０°に変化させて行った６結果は第３図に
示す通りで、Ｏ〜５０°までは改善効果が顕著であるこ
とがわかった。Example 5 Using the same equipment as in Example 1, the desulfurization rate was measured when water spray was performed in the upstream direction of the flue gas. The results obtained by varying the spray angle from 0 to 180 degrees are shown in FIG. 3, and it was found that the improvement effect was significant from 0 to 50 degrees.
比較例Ｉ
Ａ炭について実施例１および５と同じ条件で脱硫率を測
定した。ただし、水は排ガスに対して重量比で５％を煙
道中に噴霧して添加した。その結果、脱硫率４９％であ
った０本発明法による脱硫装置に比較して脱硫率が低く
なっている。Comparative Example I The desulfurization rate of coal A was measured under the same conditions as in Examples 1 and 5. However, water was added by spraying into the flue at a weight ratio of 5% to the exhaust gas. As a result, the desulfurization rate was lower than that of the desulfurization apparatus according to the method of the present invention, which had a desulfurization rate of 49%.
比較例２
第４図に示した従来技術に基づく装置を用いて、Ａ炭に
ついて実施例４と同じ条件で脱硫率を測定した。ただし
、水は排ガスに対して重量比で５％を煙道中に噴霧して
添加した。その結果、脱硫率４８％であった。本発明法
による脱硫装置に比較して脱硫率が低くなっている。Comparative Example 2 The desulfurization rate of coal A was measured under the same conditions as in Example 4 using an apparatus based on the conventional technology shown in FIG. However, water was added by spraying into the flue at a weight ratio of 5% to the exhaust gas. As a result, the desulfurization rate was 48%. The desulfurization rate is lower than that of the desulfurization apparatus according to the present invention.
［発明の効果］
本発明により、消石灰粒子の高比表面積化および表面へ
の水膜の形成により高い脱硫率を得ることができる。[Effects of the Invention] According to the present invention, a high desulfurization rate can be obtained by increasing the specific surface area of slaked lime particles and forming a water film on the surface.
第１図は本発明の実施例の装置のフローシート、第２図
は実施例３の実験結果を示す図、第３図は実施例５の実
験結果を示す図、第４図は従来装置のフローシートであ
る。
１・・・ボイラ、２・・・エアヒータ（空気加熱器）、
３・・・脱硫反応塔、５・・・集塵器
出願人 バブコック日立株式会社
代理人 弁理士 松永孝義 はか１名
第
図
第
図
噴
霧
角（０）
５：集塵器Figure 1 is a flow sheet of the apparatus according to the embodiment of the present invention, Figure 2 is a diagram showing the experimental results of Example 3, Figure 3 is a diagram showing the experimental results of Example 5, and Figure 4 is a diagram of the conventional apparatus. It is a flow sheet. 1...Boiler, 2...Air heater (air heater),
3... Desulfurization reaction tower, 5... Dust collector Applicant Babcock Hitachi Co., Ltd. Agent Patent attorney Takayoshi Matsunaga Haka 1 person Figure Figure Spray angle (0) 5: Dust collector
Claims (3)
グネシウム化合物含有消石灰を含む脱硫剤を用いて水分
を吹き込みながら脱硫反応を行わせる排ガス処理法にお
いて、 脱硫剤の導入位置の温度が、４００℃から７００℃の範
囲にあり、かつ、水分吹き込み位置の温度が３０℃から
２００℃の範囲にあることを特徴とする排ガス浄化方法
。(1) In an exhaust gas treatment method in which a desulfurization agent containing slaked lime or slaked lime containing a magnesium compound is used to carry out a desulfurization reaction while blowing moisture into the exhaust gas discharged from a combustion device, the temperature at the point where the desulfurization agent is introduced is 400°C or higher. An exhaust gas purification method characterized in that the temperature is in the range of 700°C and the temperature at the moisture injection position is in the range of 30°C to 200°C.
交換して脱硫反応塔に導き、消石灰またはマグネシウム
化合物含有消石灰を含む脱硫剤と水分により脱硫反応を
行わせる排ガスの浄化装置において、 脱硫剤の導入位置が燃焼装置と脱硫反応塔間の煙道に設
けられた空気加熱器の上流にあり、かつ、水分の吹き込
み位置が空気加熱器下流にあることを特徴とする排ガス
の浄化装置。(2) In the exhaust gas purification device, the exhaust gas discharged from the combustion equipment is exchanged with air using an air heater and guided to the desulfurization reaction tower, where a desulfurization reaction is carried out using moisture and a desulfurization agent containing slaked lime or slaked lime containing a magnesium compound. An exhaust gas purification device characterized in that the introduction position of the agent is upstream of an air heater provided in a flue between a combustion device and a desulfurization reaction tower, and the moisture injection position is downstream of the air heater.
道ガス流の上流方向に対して０から５０゜であることを
特徴とする請求項２記載の排ガス浄化装置。(3) The exhaust gas purification device according to claim 2, wherein the angle between the direction of moisture injection and the flue gas flow is 0 to 50 degrees with respect to the upstream direction of the flue gas flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2226749A JPH04110020A (en) | 1990-08-30 | 1990-08-30 | Exhaust gas purifying method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2226749A JPH04110020A (en) | 1990-08-30 | 1990-08-30 | Exhaust gas purifying method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04110020A true JPH04110020A (en) | 1992-04-10 |
Family
ID=16850010
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2226749A Pending JPH04110020A (en) | 1990-08-30 | 1990-08-30 | Exhaust gas purifying method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04110020A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023007973A1 (en) * | 2021-07-30 | 2023-02-02 | 三菱重工業株式会社 | Exhaust gas treatment apparatus |
-
1990
- 1990-08-30 JP JP2226749A patent/JPH04110020A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023007973A1 (en) * | 2021-07-30 | 2023-02-02 | 三菱重工業株式会社 | Exhaust gas treatment apparatus |
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