JPH03196816A - Treatment of waste combustion gas - Google Patents
Treatment of waste combustion gasInfo
- Publication number
- JPH03196816A JPH03196816A JP1337926A JP33792689A JPH03196816A JP H03196816 A JPH03196816 A JP H03196816A JP 1337926 A JP1337926 A JP 1337926A JP 33792689 A JP33792689 A JP 33792689A JP H03196816 A JPH03196816 A JP H03196816A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- desulfurization
- waste gas
- combustion
- furnace
- 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.)
- Granted
Links
- 239000000567 combustion gas Substances 0.000 title 1
- 239000002699 waste material Substances 0.000 title 1
- 238000002485 combustion reaction Methods 0.000 claims abstract description 36
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 26
- 229910001868 water Inorganic materials 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000004202 carbamide Substances 0.000 claims abstract description 11
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims abstract description 7
- 150000001342 alkaline earth metals Chemical class 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 34
- 230000023556 desulfurization Effects 0.000 claims description 34
- 238000000034 method Methods 0.000 claims description 13
- 238000001816 cooling Methods 0.000 abstract description 17
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 14
- 229910052815 sulfur oxide Inorganic materials 0.000 abstract description 6
- 230000003009 desulfurizing effect Effects 0.000 abstract description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 abstract description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract description 4
- 235000010216 calcium carbonate Nutrition 0.000 abstract description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 abstract description 2
- 239000002912 waste gas Substances 0.000 abstract 7
- 239000007789 gas Substances 0.000 description 59
- 238000006243 chemical reaction Methods 0.000 description 35
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 3
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- -1 CaCO) Substances 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 230000003042 antagnostic effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 235000014380 magnesium carbonate Nutrition 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
この発明は、各種のボイラ、各種加熱炉さらには、ごみ
焼成炉などの燃焼炉内に排ガス処理剤を投入して、燃焼
炉から出る排ガス中の硫黄酸化物（ＳＯｘ）を効果的に
除去すると同時に、窒素酸化物（ＮＯＸ）をも効果的に
除去する燃焼排ガス処理方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention is applicable to various boilers, various heating furnaces, and even combustion furnaces such as garbage incineration furnaces by introducing an exhaust gas treatment agent into the combustion furnaces to treat the exhaust gases coming out of the combustion furnaces. The present invention relates to a combustion exhaust gas treatment method that effectively removes sulfur oxides (SOx) and also effectively removes nitrogen oxides (NOX).
し従来技術および発明の課題］
従来より、乾式脱硫法の代表例として、Ｃａ系脱硫剤お
よび／またはＭｇ系脱硫剤を燃焼装置の火炉内へ直接吹
き込んで脱硫を行なう、いわゆる「炉内脱硫法」が知ら
れている。[Prior Art and Problems of the Invention] Conventionally, as a typical example of the dry desulfurization method, the so-called "in-furnace desulfurization method" is used, in which desulfurization is performed by directly injecting a Ca-based desulfurization agent and/or an Mg-based desulfurization agent into the furnace of a combustion device. "It has been known.
しかし、この方法は、脱硫剤を多量に使用する必要があ
る上に、低い脱硫性能しか得られないため、未だ実用化
されるに至っていない。However, this method requires the use of a large amount of desulfurization agent and only provides low desulfurization performance, so it has not yet been put into practical use.
この発明の目的は、上記の如き実情に鑑み、燃焼炉排ガ
ス中の硫黄酸化物と窒素酸化物とを同時にかつ効果的に
除去することができる燃焼排ガス処理方法を提供するこ
とにある。In view of the above-mentioned circumstances, an object of the present invention is to provide a combustion exhaust gas treatment method that can simultaneously and effectively remove sulfur oxides and nitrogen oxides from combustion furnace exhaust gas.
［課題の解決手段〕
この発明による燃焼排ガス処理方法は、燃焼炉の６００
〜９００℃の温度領域の排ガスにアルカリ土類金属系脱
硫剤と尿素ないしその誘導体との混合物より成る排ガス
処理剤を噴射投入し、燃焼炉の後流で１００〜４００℃
の温度領域の排ガスに水を噴射することを特徴とするも
のである。[Means for solving the problem] The combustion exhaust gas treatment method according to the present invention
An exhaust gas treatment agent consisting of a mixture of an alkaline earth metal desulfurization agent and urea or its derivatives is injected into the exhaust gas in the temperature range of ~900℃, and the temperature is raised to 100~400℃ downstream of the combustion furnace.
This system is characterized by injecting water into exhaust gas in a temperature range of .
上記において、アルカリ土類金属系脱硫剤としては、た
とえばＣａ ＣＯ） 、Ｃａ （ＯＨ）２、ＣａＯなど
のＣａ系脱硫剤や、ドロマイト（Ｍｇ ＣＯ３・Ｃａ
Ｃ０３）などが用いられる。排ガス処理剤の形態は、特
に限定されないが、好ましくは粉体状、スラリー状など
である。In the above, examples of alkaline earth metal desulfurization agents include Ca-based desulfurization agents such as CaCO), Ca(OH)2, and CaO, and dolomite (MgCO3・Ca
C03) etc. are used. The form of the exhaust gas treatment agent is not particularly limited, but is preferably in the form of powder, slurry, or the like.
噴射される水は、好ましくは加熱された状態にあり、噴
射の結果Ｗｒ、！ｉＦＪ化水滴となされる。The water to be injected is preferably in a heated state and the result of the injection is Wr,! It is made into iFJ water droplets.
拮ガス処理剤の投入を行なう領域は６００〜９００℃の
温度領域であり、水噴射を行なう領域は１００〜４００
℃蒸気の温度領域である。The area where the antagonistic gas treatment agent is introduced is a temperature range of 600 to 900°C, and the area where water is sprayed is a temperature range of 100 to 400°C.
°C is the temperature range of steam.
［作 用］
この発明の方法によれば、まず、燃焼炉の６００〜９０
０℃の温度領域の排ガスにアルカリ土類金属系脱硫剤と
尿素ないしその誘導体との混合物より成る排ガス処理剤
を噴射投入することによって、炉内において排ガスの脱
硫および脱硝が同時に行なわれる。[Function] According to the method of the present invention, first, the combustion furnace has 600 to 90
By injecting an exhaust gas treating agent consisting of a mixture of an alkaline earth metal desulfurizing agent and urea or its derivatives into the exhaust gas at a temperature of 0° C., the exhaust gas is simultaneously desulfurized and denitrated in the furnace.
ついで、燃焼炉の後流で１００〜４００℃の温度領域の
排ガスに水を噴射することによって、排ガス中の湿分を
増加せしめると共に排ガス温度を降ドせしめる。この結
果、低温領域で２段目の脱硫が行なわれる。Next, by injecting water into the exhaust gas in the temperature range of 100 to 400° C. downstream of the combustion furnace, the moisture content in the exhaust gas is increased and the temperature of the exhaust gas is lowered. As a result, the second stage of desulfurization is performed in the low temperature region.
こうして、燃焼プロセス全体を一種の反応器と考えて、
その高温領域で炉内脱硫および脱硝反応を行なわしめる
と共に、その後流の低温領域において２段目の脱硫作用
を生起せしめることによって、少量の薬剤使用量で脱硫
率９０％以上および脱硝率８５％以上という高い反応効
率が得られる。Thus, considering the entire combustion process as a kind of reactor,
By performing in-furnace desulfurization and denitrification reactions in the high-temperature region, and generating a second stage of desulfurization in the downstream low-temperature region, the desulfurization rate is 90% or more and the denitrification rate is 85% or more with a small amount of chemicals used. A high reaction efficiency can be obtained.
［夫 施 例］ ａ）プロセスの説明 以下、この発明の実施例を、図面を参照して説明する。[Example of husband giving] a) Process description Embodiments of the invention will be described below with reference to the drawings.
第１図はこの発明の方法を実施するための実験装置およ
びそのプロセスフローを示す。第１図において、この実
験装置は、排ガスの流れ方向に、微粉炭の燃焼炉（１）
と、脱硫脱硝反応用の反応室（３）と、排ガスの排熱に
よる空気加熱用のエアーヒータ（４）と、排ガス冷却用
の冷却塔（６）と、排ガス除塵用のバグフィルタ（７）
とを主たる構成要素として成る。FIG. 1 shows an experimental apparatus for carrying out the method of the present invention and its process flow. In Fig. 1, this experimental device has a pulverized coal combustion furnace (1) in the direction of flow of exhaust gas.
, a reaction chamber (3) for desulfurization and denitrification reaction, an air heater (4) for heating air using the exhaust heat of exhaust gas, a cooling tower (6) for cooling exhaust gas, and a bag filter (7) for removing dust from exhaust gas.
The main components are:
まず、微粉炭は燃焼炉（１）の燃焼バーナで燃焼させら
れる。燃焼炉（１）における微粉炭の燃焼量は最大で１
０ｋｇ／時であるが、助燃用プロパンの燃焼による低負
荷の石炭燃焼すなわち混焼が可能であり、この混焼によ
って、反応室（３）における温度制御、ＮＯｘ発生量の
抑制、さらにはＳＯ２ガスの注入による排ガス中のＳ０
２ガス濃度の調整が可能なようになっている。First, pulverized coal is burned in a combustion burner of a combustion furnace (1). The maximum amount of pulverized coal burned in the combustion furnace (1) is 1
0 kg/hour, but low-load coal combustion, i.e., co-combustion, is possible by combustion of propane for auxiliary combustion.This co-combustion allows temperature control in the reaction chamber (3), suppression of NOx generation, and even injection of SO2 gas. S0 in exhaust gas due to
The concentration of the two gases can be adjusted.
燃焼炉（１）で発生した排ガスは、燃焼炉（１）の後流
側に設けられている脱硫および脱硝のための反応室（３
）に入る。反応室（３）の内径は３３０ｍｍ、高さは４
ｍである。反応室（３）はその周面に設けられた電気ヒ
ータ（２）で所定温度に制御できるようになっている。The exhaust gas generated in the combustion furnace (1) is sent to a reaction chamber (3) for desulfurization and denitration, which is provided on the downstream side of the combustion furnace (1).
)to go into. The inner diameter of the reaction chamber (3) is 330 mm, and the height is 4
It is m. The temperature of the reaction chamber (3) can be controlled to a predetermined temperature by an electric heater (2) provided on its circumferential surface.
排ガス処理剤、すなわち脱硫剤と尿素ないしその誘導体
との混合物は、粉体の形態にある場合には、反応室（３
）のトップの部分へ空気流にのせて注入される。排ガス
処理剤がスラリーの形態にある場合もやはり反応室（３
）のトップの部分へ注入される。この排ガス処理剤の注
入によって、反応室（３）内で排ガス中のＳＯ□の吸収
反応とＮＯｘの還元反応が起こる。特にＮ。When the exhaust gas treatment agent, that is, the mixture of the desulfurization agent and urea or its derivatives, is in the form of a powder, it is placed in the reaction chamber (3).
) is injected into the top part of the air stream. When the exhaust gas treatment agent is in the form of a slurry, the reaction chamber (3
) is injected into the top part of the tube. By injecting this exhaust gas treatment agent, an absorption reaction of SO□ and a reduction reaction of NOx in the exhaust gas occur in the reaction chamber (3). Especially N.
Ｘの還元反応は、反応室後流でのＮＯｘ低減効果が認め
られなかったことから、反応室（３）において完結する
ようである。他方、Ｓ０２の吸収反応は、反応室（３）
から冷却塔（Ｂ）の出口まで（冷却塔内で水噴射を行な
わない場合はさらに後流まで）、やはり認められなかっ
た。この現象は、反応室（３）の出口とバグフィルタ（
７）の出口に設置した排ガス中の０２、ＳＯ２、ＮＯｘ
の各濃度を測定するガス分析計（８）による分析の結果
、確認された。なお、各部所の温度はそれぞれ温度計（
９）によって測定し、また排ガス流量はバグフィルタ（
７）の出口に設置した流量計（ｌＯ）によって測定した
。The reduction reaction of X appears to be completed in the reaction chamber (3) since no NOx reduction effect was observed downstream of the reaction chamber. On the other hand, the absorption reaction of S02 is carried out in the reaction chamber (3).
It was also not observed from the cooling tower (B) to the outlet (if water injection is not performed in the cooling tower, further to the downstream). This phenomenon occurs between the outlet of the reaction chamber (3) and the bag filter (
7) 02, SO2, NOx in exhaust gas installed at the outlet of
This was confirmed as a result of analysis using a gas analyzer (8) that measures each concentration of . In addition, the temperature of each part can be measured using a thermometer (
9), and the exhaust gas flow rate is measured using a bag filter (
7) was measured with a flow meter (lO) installed at the outlet.
以上の事象から、排ガス中の８０２の吸収反応およびＮ
Ｏｘの還元反応は、いずれも６００〜９００℃の温度領
域で生起するものと推定される。From the above phenomena, the absorption reaction of 802 in exhaust gas and N
It is estimated that all Ox reduction reactions occur in a temperature range of 600 to 900°C.
反応室（３）を出た排ガスはエアヒータ（４）を通過し
、冷却空気により排熱が回収されて冷却された後、熱交
換器（５）で冷却水によってさらに冷却される。The exhaust gas leaving the reaction chamber (3) passes through the air heater (4), and after being cooled by recovering exhaust heat with cooling air, it is further cooled by cooling water in the heat exchanger (5).
この発明では、燃焼炉の後流でさらに付加的脱硫を行な
うために、っぎの操作を行なう。すなわち、熱交換器（
５）において、排ガスを冷却するのに用いられた冷却水
は、熱交換器（５）を通過する間に排ガスの排熱によっ
て加熱されている。この加熱状態の水は冷却塔（６）の
上部から噴射ノズルで塔内へ吹き込まれる。その結果、
冷却塔（６）内において、冷却水は加熱状態にあるため
その噴射によってフラッシュ蒸発作用を起こして、微細
化水滴となされる。こうして生じた微細化水滴は、粗大
水滴が冷却塔（６）内で壁面に付着し、この付着水によ
って脱硫剤含有灰分が同壁面に付着して固化し、さらに
この固化物が成長して塔の閉塞を招くことを防止すると
共に、排ガスと水滴の良好な混合を促進する働きをする
。この微細化水滴は、排ガスとの混合の結果、排ガス中
の湿分を増加せしめると共に、排ガス温度を降下せしめ
る。In this invention, the following operation is performed in order to further perform additional desulfurization downstream of the combustion furnace. That is, the heat exchanger (
In 5), the cooling water used to cool the exhaust gas is heated by the exhaust heat of the exhaust gas while passing through the heat exchanger (5). This heated water is blown from the top of the cooling tower (6) into the tower through an injection nozzle. the result,
In the cooling tower (6), since the cooling water is in a heated state, its injection causes a flash evaporation effect and is turned into fine water droplets. The fine water droplets generated in this way are coarse water droplets that adhere to the wall surface in the cooling tower (6), and the adhering water causes desulfurizing agent-containing ash to adhere to the wall surface and solidify, and this solidified material grows and grows into the tower. This function not only prevents clogging of water but also promotes good mixing of exhaust gas and water droplets. As a result of mixing with the exhaust gas, these fine water droplets increase the moisture content in the exhaust gas and lower the exhaust gas temperature.
冷却塔（６）内では、排ガス中の灰分に含まれる未反応
のＣａＯが噴射された水分と反応して、Ｃａ （ＯＨ）
２となり、これがＳ０２を吸収する作用が生起する。こ
うして、冷却塔（６）において２段目の脱硫反応が進行
する。In the cooling tower (6), unreacted CaO contained in the ash in the exhaust gas reacts with the injected moisture to form Ca (OH).
2, which causes an effect of absorbing S02. In this way, the second stage desulfurization reaction proceeds in the cooling tower (6).
ここで、反応室（３）および冷却塔（６）で起こると考
えられるＳ０２の吸収反応を纏めると、つぎのようにな
る。Here, the absorption reactions of S02 that are thought to occur in the reaction chamber (3) and the cooling tower (6) are summarized as follows.
■ 反応室（３）内の６００〜９００℃の温度領域で生
起する反応：
ＣａＣＯ３→ＣａＯ＋Ｃ０２↑
Ｃａ Ｏ＋ Ｓ ０２ ＋ １ ／ ２０２ →Ｃａ
Ｓ Ｏ４■ 冷却塔（６）内の１００〜４００℃の温度
領域で生起する反応：
Ｃａ Ｏ十Ｈ２０−Ｃａ （ＯＨ） ２Ｃａ（ＯＨ）２
＋ＳＯ２→ＣａＳＯ３・Ｈ２Ｏすなわち、高温領域では
ＣａＳＯ４が生じ、低温領域ではＣａ Ｓ Ｏ３が生じ
る。また、■の一連の反応は冷却塔（６）内だけで完結
するものではなく、さらに後流のバグフィルタ（７）の
フィルタ表面においても継続されているようである。な
お、上記■■の反応で生じたＣ ａ Ｓ ０４、Ｃａ
Ｓ Ｏ３、および未反応のＣａＣ０，、、ＣａＯは、い
ずれも石炭燃焼灰との混合物として、バグフィルタ（７
）で捕集・回収された。■ Reactions that occur in the temperature range of 600 to 900°C in the reaction chamber (3): CaCO3 → CaO + C02↑ Ca O+ S 02 + 1 / 202 → Ca
S O4 ■ Reaction that occurs in the temperature range of 100 to 400 °C in the cooling tower (6): Ca O + H20 - Ca (OH) 2Ca (OH)2
+SO2→CaSO3·H2O That is, CaSO4 is produced in the high temperature region, and CaSO3 is produced in the low temperature region. Furthermore, the series of reactions (2) are not completed only within the cooling tower (6), but also seem to continue on the filter surface of the downstream bag filter (7). In addition, Ca S 04, Ca
S O3 and unreacted CaC0, , CaO are both passed through a bag filter (7
) was collected and recovered.
こうして、浄化処理せられた排ガスは流量計（１０）を
経て系外へ排出される。The purified exhaust gas is discharged to the outside of the system through the flow meter (10).
ｂ）脱硫脱硝試験
以下の比較例および実施例における主な実験条件は下記
のとおりであった。b) Desulfurization and denitrification test The main experimental conditions in the following comparative examples and examples were as follows.
燃料供給速度：プロパン０．６４Ｎｍ’ ／時十石炭３
．４２ｋｇ／時の混焼
空気比：１．８１（排ガス中の酸素濃度９．４％）
排ガス量： ７４Ｎｍ’ ／時
ＳＯｘ濃度：８００ｐｐｍ（純Ｓ０２ガス添加による濃
度調整）
ＮＯｘ濃度：２６０ｐｐｍ
反応温度ニア８０℃
ガス滞留時間＝４，５秒（反応室内）
比較例
排ガス中に、排ガス処理剤として粒径１．７μのＣａＣ
Ｏ３微粉末と粉状の尿素との混合物（Ｃａ ＣＯ３９：
尿素１）を反応室（３）へ噴射供給した。そして、燃焼
炉（１）内で発生するＳＯ□量（モル量）と反応室（３
）に投入したＣａｆｆ１（モル量）の比、すなわちＣａ
／ Ｓモル当量比を変えつつ、反応室（３）の出口お
よびバグフィルタ（７）の出口での各ガス分析計（８）
を用いて、排ガス中のＮＯｘ濃度およびＳ０２濃度をΔ
Ｐ１定し、Ｃａ ／ Ｓモル当量比と脱硝率および脱硫
率との関係を調べた。これらの測定結果をそれぞれ第２
図中の曲線（Ａ）および第３図中の曲線（Ｂ）に示す。Fuel supply rate: Propane 0.64Nm' / hour 1 coal 3
．． 42kg/hour co-combustion air ratio: 1.81 (oxygen concentration in exhaust gas 9.4%) Exhaust gas amount: 74Nm'/hour SOx concentration: 800ppm (concentration adjustment by adding pure S02 gas) NOx concentration: 260ppm Reaction temperature near 80 °C Gas residence time = 4.5 seconds (in the reaction chamber) Comparative example CaC with a particle size of 1.7μ was added as an exhaust gas treatment agent in the exhaust gas.
A mixture of O3 fine powder and powdered urea (Ca CO39:
Urea 1) was injected into the reaction chamber (3). The SO□ amount (molar amount) generated in the combustion furnace (1) and the reaction chamber (3
), that is, the ratio of Caff1 (molar amount) added to Ca
/S molar equivalent ratio, each gas analyzer (8) at the outlet of the reaction chamber (3) and the outlet of the bag filter (7).
Using Δ
P1 was determined, and the relationship between the Ca/S molar equivalent ratio and the denitrification rate and desulfurization rate was investigated. Each of these measurement results is
This is shown in curve (A) in the figure and curve (B) in FIG.
脱硝性能を示す第２図の曲線（Ａ）から明らかなように
、Ｃａ／Ｓモル当量比−３の時に脱硝率８５％が得られ
、反応室（３）の出口およびバグフィルタ（７）の出口
での各ＮＯｘ濃度はいずれも４０’ｐｐｍ程度まで低下
した。なお、尿素の供給量を増大して、Ｃａ／Ｓモル当
量比を３以上に上げても、脱硝効果はそれ以上には向上
しなかった。As is clear from the curve (A) in Figure 2 showing the denitrification performance, a denitrification rate of 85% was obtained when the Ca/S molar equivalent ratio was -3, and the denitrification rate at the outlet of the reaction chamber (3) and the bag filter (7) Each NOx concentration at the outlet decreased to about 40'ppm. Note that even if the supply amount of urea was increased to raise the Ca/S molar equivalent ratio to 3 or more, the denitrification effect did not improve any further.
脱硫性能を示す第３図の曲線（Ｂ）から明らかなように
、Ｃａ ／ Ｓモル当量比−３の時に脱硫率は８５％で
あり、反応室（３）の出口およびバグフィルタ（７）の
出口での各５０２ａ度はそれぞれ１２０ｐｐｍであった
。As is clear from the curve (B) in Figure 3 showing the desulfurization performance, the desulfurization rate is 85% when the Ca/S molar equivalent ratio is -3, and the desulfurization rate is 85% at the outlet of the reaction chamber (3) and the bag filter (7). Each 502a degree at the outlet was 120 ppm.
実施例
比較例の上記条件と同じ条件で、比較例の上記操作に加
えて、熱交換器（５）を出た加熱状態の冷却水１２ｇ／
時を冷却塔（６）内に頂部のノズルから吹き込んだ。こ
の時、エアーヒータ（４）の出口の排ガス温度は４３０
℃、水噴射の後流すなわち冷却塔（６）の出口の温度は
１６０℃、バグフィルタ（７）の出口の温度は１２０℃
であった。Under the same conditions as the above-mentioned conditions of the embodiment and comparative example, in addition to the above-mentioned operations of the comparative example, 12g/12g of the heated cooling water exiting the heat exchanger (5) was added.
Time was blown into the cooling tower (6) through a nozzle at the top. At this time, the exhaust gas temperature at the outlet of the air heater (4) is 430
℃, the temperature at the wake of the water injection, i.e. the outlet of the cooling tower (6), is 160℃, and the temperature at the outlet of the bag filter (7) is 120℃.
Met.
比較例と同様にして、排ガス中のＳＯ２濃度をＭ１定し
、Ｃａ ／ Ｓモル当量比と脱硫率との関係を調べた。In the same manner as in the comparative example, the SO2 concentration in the exhaust gas was determined as M1, and the relationship between the Ca/S molar equivalent ratio and the desulfurization rate was investigated.
これらの測定結果をそれぞれ第３図中の曲線（Ｃ）に示
す。The results of these measurements are shown in curves (C) in FIG. 3, respectively.
上記水の吹き込みによって、排ガス中の湿分が増加せら
れると共に排ガス温度が降下さぜられ、上記■の反応が
進行し、２段目の脱硫が行なわれる。その結果、脱硫性
能を示す第３図の曲線（Ｃ）から明らかなように、Ｃａ
／ Ｓモル当量比−２の時に脱硫率９５％が得られ、
バグフィルタ（７）の出口でのＳＯ２濃度は４０ｐｐｍ
であった。これに対し、水噴射の前流すなわち反応室（
３）の出口におけるＳＯ□濃度は２４０ｐｐｍであった
。By blowing water, the moisture content in the exhaust gas is increased and the temperature of the exhaust gas is lowered, so that the reaction (2) proceeds and the second stage of desulfurization is performed. As a result, as is clear from the curve (C) in Figure 3 showing the desulfurization performance, Ca
A desulfurization rate of 95% was obtained when the /S molar equivalent ratio was −2,
SO2 concentration at the outlet of bag filter (7) is 40 ppm
Met. In contrast, the upstream of the water jet, i.e., the reaction chamber (
The SO□ concentration at the outlet of 3) was 240 ppm.
また、ＮＯｘ濃度は、反応室（３〉の出口およびバグフ
ィルタ（７）の出口とも１１００ｐｐであった。このこ
とは、脱硝に関しては第２図の曲線（Ａ）の性能が支配
的であり、脱硝効率をさらに向上させるには尿素の含量
を増加させる必要があることを示している。In addition, the NOx concentration was 1100 pp at both the outlet of the reaction chamber (3>) and the outlet of the bag filter (7).This means that the performance of curve (A) in Fig. 2 is dominant in terms of denitrification. This indicates that it is necessary to increase the urea content to further improve the denitrification efficiency.
［発明の効果］
この発明の方法によれば、まず、燃焼炉の６００〜９０
０℃の温度領域の排ガスにアルカリ土類金属系脱硫剤と
尿素ないしその誘導体との混合物より成る排ガス処理剤
を噴射投入するので、炉内において排ガスの脱硫および
脱硝を同時に行なうことができる。[Effect of the invention] According to the method of this invention, first, the combustion furnace
Since an exhaust gas treating agent consisting of a mixture of an alkaline earth metal desulfurizing agent and urea or its derivatives is injected into the exhaust gas in the temperature range of 0° C., the exhaust gas can be desulfurized and denitrated at the same time in the furnace.
ついで、燃焼炉の後流で１００〜４００℃の温度領域の
排ガスに水を噴射するので１、排ガス中の湿分を増加せ
しめると共に排ガス温度を降下せしめ、この結果低温領
域で２段目の脱硫を行なわしめることができる。Next, water is injected into the exhaust gas in the temperature range of 100 to 400 degrees Celsius downstream of the combustion furnace, which increases the moisture content in the exhaust gas and lowers the exhaust gas temperature.As a result, the second stage of desulfurization occurs in the low temperature region. can be carried out.
こうして、この発明の方法では、燃焼プロセス全体を一
種の反応器と考えて、その高温領域で炉内脱硫および脱
硝反応を行なうと共に、その後流の低温領域において２
段目の脱硫作用を生起せしめることによって、少量の薬
剤使用量で脱硫率９０％以上および脱硝率８５％以上と
いう高い反応効率を得ることができる。In this way, in the method of this invention, the entire combustion process is considered as a kind of reactor, and the in-furnace desulfurization and denitrification reactions are carried out in the high temperature region, and the 2
By causing the desulfurization action in the first stage, high reaction efficiency such as a desulfurization rate of 90% or more and a denitrification rate of 85% or more can be obtained with a small amount of chemicals used.
第１図はこの発明の実施例を示すフローシート、第２図
はＣａ ／ Ｓモル当量比と脱硝率との関係を示すグラ
フ、第３図はＣａ ／ Ｓモル当量比と脱硫率との関係
を示すグラフである。
（１）・・・燃焼炉、（２）・・・電気ヒータ、（３）
・・・反応室、（４）・・・エアーヒータ、（５）・・
・熱交換器、（６）・・・冷却塔、（ア）・・・バグフ
ィルタ、（８）・・ガス分析計、（９）・・・温度計、
（１０）・・・流量計。
以 上Figure 1 is a flow sheet showing an example of the present invention, Figure 2 is a graph showing the relationship between Ca/S molar equivalent ratio and denitrification rate, and Figure 3 is the relationship between Ca/S molar equivalent ratio and desulfurization rate. This is a graph showing. (1)... Combustion furnace, (2)... Electric heater, (3)
...Reaction chamber, (4)...Air heater, (5)...
・Heat exchanger, (6)...Cooling tower, (A)...Bag filter, (8)...Gas analyzer, (9)...Thermometer,
(10)...Flowmeter. that's all
Claims (1)
カリ土類金属系脱硫剤と尿素ないしその誘導体との混合
物より成る排ガス処理剤を噴射投入し、燃焼炉の後流で
１００〜４００℃の温度領域の排ガスに水を噴射するこ
とを特徴とする燃焼排ガス処理方法。An exhaust gas treatment agent consisting of a mixture of an alkaline earth metal desulfurization agent and urea or its derivatives is injected into the exhaust gas in the temperature range of 600 to 900°C from the combustion furnace, and the temperature is increased to 100 to 400°C downstream of the combustion furnace. A combustion exhaust gas treatment method characterized by injecting water into the exhaust gas of a region.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1337926A JPH0696090B2 (en) | 1989-12-25 | 1989-12-25 | Combustion exhaust gas treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1337926A JPH0696090B2 (en) | 1989-12-25 | 1989-12-25 | Combustion exhaust gas treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03196816A true JPH03196816A (en) | 1991-08-28 |
| JPH0696090B2 JPH0696090B2 (en) | 1994-11-30 |
Family
ID=18313304
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1337926A Expired - Lifetime JPH0696090B2 (en) | 1989-12-25 | 1989-12-25 | Combustion exhaust gas treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0696090B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021060160A (en) * | 2019-10-08 | 2021-04-15 | 伊藤レーシングサービス株式会社 | Incinerator |
-
1989
- 1989-12-25 JP JP1337926A patent/JPH0696090B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021060160A (en) * | 2019-10-08 | 2021-04-15 | 伊藤レーシングサービス株式会社 | Incinerator |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0696090B2 (en) | 1994-11-30 |
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