JPH0741143B2 - Exhaust gas treatment method - Google Patents
Exhaust gas treatment methodInfo
- Publication number
- JPH0741143B2 JPH0741143B2 JP62308887A JP30888787A JPH0741143B2 JP H0741143 B2 JPH0741143 B2 JP H0741143B2 JP 62308887 A JP62308887 A JP 62308887A JP 30888787 A JP30888787 A JP 30888787A JP H0741143 B2 JPH0741143 B2 JP H0741143B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- temperature
- radiation
- irradiation
- reactor
- 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.)
- Expired - Fee Related
Links
- 238000000034 method Methods 0.000 title claims description 61
- 238000011282 treatment Methods 0.000 title claims description 21
- 230000005855 radiation Effects 0.000 claims description 31
- 239000000428 dust Substances 0.000 claims description 28
- 239000000498 cooling water Substances 0.000 claims description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 25
- 239000012717 electrostatic precipitator Substances 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 15
- 229910021529 ammonia Inorganic materials 0.000 claims description 12
- 229920006395 saturated elastomer Polymers 0.000 claims description 11
- 238000010894 electron beam technology Methods 0.000 claims description 9
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 7
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 7
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 7
- 239000006227 byproduct Substances 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 2
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 claims 2
- 239000001166 ammonium sulphate Substances 0.000 claims 1
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 230000006698 induction Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 description 131
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 238000006477 desulfuration reaction Methods 0.000 description 16
- 230000023556 desulfurization Effects 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 12
- 238000001816 cooling Methods 0.000 description 9
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 230000033228 biological regulation Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 230000020169 heat generation Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 231100000987 absorbed dose Toxicity 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000005909 Kieselgur Substances 0.000 description 1
- 206010037660 Pyrexia Diseases 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000001464 adherent effect Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000000137 annealing Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002341 toxic gas Substances 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
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は放射線照射による排ガス処理法の改善に関し、
さらに詳しくは、アンモニア添加と放射線照射とを併用
することにより高濃度のSOx、もしくはさらにその他の
有害ガス成分のNOxを含む排ガスの浄化法における脱硫
もしくはさらに脱硝効率の改善に関する。TECHNICAL FIELD The present invention relates to improvement of an exhaust gas treatment method by irradiation with radiation,
More particularly, to ammonia added and irradiation and by using high concentrations of SO x, or even improved desulfurization or more denitration efficiency in the purification method of the exhaust gas containing NO x and other harmful gas components.
（従来の技術） 本明細書で脱硫とは排ガス中に含まれる各種形態の硫黄
酸化物（通常SOxと略記される）の除去を意味し、脱硝
とは排ガス中に含まれる各種形態の窒素酸化物（通常NO
xと略記される）の除去を意味する。工場や発電所では
毎日絶え間なく大量の燃焼排ガスが発生している。これ
ら排ガスの中には量の違いにあっても、例外なくSOxお
よびNOxの少なくとも一方が含まれている。SOxおよびNO
xは通常有害ガス成分として排ガス中に含まれている。
したがって、排ガスを大気に放出する前にこれを脱硫・
脱硝処理することは大気汚染防止上不可欠のことであ
る。(Prior Art) In the present specification, desulfurization means removal of various forms of sulfur oxides (usually abbreviated as SO x ) contained in exhaust gas, and denitration means various forms of nitrogen contained in exhaust gas. Oxide (usually NO
abbreviated as x ). Every day in factories and power plants, a large amount of combustion exhaust gas is generated. These exhaust gases contain at least one of SO x and NO x without exception even if the amount is different. SO x and NO
x is usually contained in the exhaust gas as a harmful gas component.
Therefore, it is necessary to desulfurize the exhaust gas before releasing it into the atmosphere.
Denitration treatment is indispensable for preventing air pollution.
（発明が解決しようとする問題点） 従来各種の脱硫・脱硝法が考案されて実施されている
が、水や特定の化学物質を多量に使う湿式法が多く、こ
のため副生する多量の排水やスラリーの処理がまた別の
困難な問題を生じている。特に有害ガス成分の含有比率
が高い、高濃度のSOx、もしくはさらにNOxを含む排ガス
の処理においては副生する排水やスラリーの量が厖大と
なるため、これらの処理が別の困難な問題を生じるため
排ガス処理技術の現状は必ずしも満足できるものではな
い。(Problems to be solved by the invention) Conventionally, various desulfurization / denitration methods have been devised and implemented, but many wet methods use a large amount of water or a specific chemical substance, and thus a large amount of wastewater produced as a by-product. Processing of slurries presents another difficult problem. Especially in the treatment of exhaust gas containing a high concentration of harmful gas components and high concentration of SO x , or NO x , the amount of waste water and slurry produced as by-products becomes enormous, which makes these treatments another difficult problem. However, the present situation of exhaust gas treatment technology is not always satisfactory.
（問題点を解決するための手段） 上記欠点のない方法として研究開発された放射線照射に
よる排ガス処理法は乾式法であって、排気ガス中にppm
オーダーで含まれている有毒ガス成分を直接固体粒子に
変えることのできる方法であるため、二次的な排水やス
ラリーが生じないばかりでなく、SOxおよびNOx（SOx単
独の場合もあるが、説明上は両者併存について行う）
を、商品価値のある化学肥料の形で回収できるため、SO
xおよびNOxの濃度が高ければコスト的に一層有利になる
場合もあるという利点がある。アンモニア添加放射線照
射排ガス処理法の典型的な工程概略図を第４図に示す。
ボイラー１で発生したSOxおよび／またはNOxを含む排ガ
ス（通常130℃以上の高温である）は排ガス導管２を経
て冷却塔３に導かれる。ここで排ガスは、冷却水供給管
４によりスプレーされる冷却水により反応器中央部のガ
ス温が50〜80℃となるように冷却された後、排ガス導管
５を経て反応器７内に導かれる。導管５の途中でアンモ
ニア添加装置６によりアンモニアを加えられる。反応器
に導入された排ガスは放射線発生装置９からの放射線を
照射される。排ガス中のSOxおよび／またはNOxは硫安お
よび／または硝安に変化するので、これらを集塵機で回
収し、浄化した排ガスを導管あるいは煙突15を経て大気
に放出する。(Means for solving the problem) The exhaust gas treatment method by irradiation of radiation, which has been researched and developed as a method without the above-mentioned drawbacks, is a dry method, and ppm in the exhaust gas is
Since it is a method that can directly convert the toxic gas components contained in the order to solid particles, it does not generate secondary drainage and slurry, but also SO x and NO x (SO x alone may be used. However, for the sake of explanation, we will do both.
Can be recovered in the form of chemical fertilizers with commercial value,
If the x and NO x concentrations are high, there is an advantage that the cost may be more advantageous. A typical process schematic diagram of the ammonia-added radiation irradiation exhaust gas treatment method is shown in FIG.
Exhaust gas containing SO x and / or NO x generated in the boiler 1 (usually at a high temperature of 130 ° C. or higher) is guided to the cooling tower 3 via the exhaust gas conduit 2. Here, the exhaust gas is cooled by the cooling water sprayed by the cooling water supply pipe 4 so that the gas temperature in the central part of the reactor becomes 50 to 80 ° C., and then introduced into the reactor 7 through the exhaust gas conduit 5. . Ammonia can be added by the ammonia addition device 6 in the middle of the conduit 5. The exhaust gas introduced into the reactor is irradiated with the radiation from the radiation generator 9. Since SO x and / or NO x in the exhaust gas changes to ammonium sulfate and / or ammonium nitrate, these are collected by a dust collector, and the purified exhaust gas is discharged to the atmosphere via the conduit or the chimney 15.
第４図で述べた排ガス温度調整法は、本発明者等による
先行特許（日本特許第1,171,144号）に記載の方法であ
る。この先行特許の特徴は、放射線照射区域（反応器）
の中央部のガス温度を50〜80℃の範囲に調整することで
ある。これはSOx・NOx共に約200ppmと低濃度のデータに
基づくものであった。本発明者等は更にテストを重ねた
結果、石炭燃焼排ガスのように高SOx,NOx濃度の排ガス
では、反応器中央部のガス温度を50〜80℃に調整して
も、後述のSOx・NOxのNH3との反応による発熱が大きい
ため反応器出口のガス温度が高くなり、SOx・NOxの除去
率が向上しないことが明らかとなった。The exhaust gas temperature adjusting method described in FIG. 4 is the method described in the prior patent (Japanese Patent No. 1,171,144) by the present inventors. The feature of this prior patent is that the irradiation area (reactor)
Is to adjust the gas temperature in the central part of the range of 50 to 80 ° C. This was based on the low concentration data of both SO x and NO x of about 200 ppm. As a result of further tests conducted by the present inventors, in the case of exhaust gas with high SO x and NO x concentrations such as coal combustion exhaust gas, even if the gas temperature in the central part of the reactor is adjusted to 50 to 80 ° C., the SO It was clarified that the gas temperature at the outlet of the reactor was high because the heat generated by the reaction of x · NO x with NH 3 was large, and the removal rate of SO x · NO x was not improved.
また、反応器中央部のガス温度を50〜80℃とするため、
反応器入口ガス温度は、50℃以下にすることが必要とな
るケースがある。この場合、冷却塔への入口排ガスが例
えば150℃、8.5Vol％水分の排ガスについて、冷却塔で
水スプレーして蒸発潜熱を利用して、ガス温度を下げて
いくと、約53℃で湿度が飽和となる。これを更に50℃に
下げるには、水の顕熱を利用することになる。しかし、
これは水分飽和温度以下にするため、ドレン水が発生
し、この方法が乾式ではなくなる。このように単に50〜
80℃にすることは乾式法でなくなるケースもあることが
明らかとなった。Also, in order to set the gas temperature in the central part of the reactor to 50 to 80 ° C,
In some cases, the reactor inlet gas temperature needs to be 50 ° C or lower. In this case, when the inlet exhaust gas to the cooling tower is, for example, 150 ° C. and 8.5 Vol% moisture exhaust gas, water is sprayed in the cooling tower and the latent heat of vaporization is used to reduce the gas temperature. It becomes saturated. To further reduce this to 50 ° C, sensible heat of water will be used. But,
Since this is below the water saturation temperature, drain water is generated and this method is not dry. Just like this
It has become clear that there are cases in which raising the temperature to 80 ° C is not the dry method.
本発明における高濃度SOxを含む排ガスとは、アンモニ
ア添加、放射線照射排ガス処理法により、反応器入口ガ
ス温度を、約50℃にしても、反応器出口温度が約90℃を
越えるようになる、高濃度SOx、もしくはさらにその他
の有害ガス成分のNOxを含む排ガスを意味する。Exhaust gas containing a high concentration of SO x in the present invention, ammonia addition, by the radiation irradiation exhaust gas treatment method, even if the reactor inlet gas temperature is about 50 ℃, the reactor outlet temperature exceeds about 90 ℃ Exhaust gas containing high concentration SO x , or NO x which is another harmful gas component.
前記のアンモニア添加放射線照射排ガス処理法によるSO
xおよびNOx除去の原理は次の通りである。SO by the above-mentioned ammonia-added radiation irradiation exhaust gas treatment method
The principle of x and NO x removal is as follows.
排ガスに放射線を照射すると、排ガス中に存在する酸素
分子および水分子から酸化力の非常に強い活性種である
OH,O、HO2等が生じる。これら活性種は極めて短時間でS
OxおよびNOxをそれぞれ酸化し、H2SHO4およびHNO3を形
成する。次いで、このようにして形成されたH2SO4およ
びHNO3は、排ガス中に添加されたアンモニアと反応して
(NH4)2SO4（硫安）とNH4NO3（硝安）とをそれぞれ形成
する。上記の硫安および硝安形成反応の過程で起る代表
的な反応を式で示すと次の通りである。When exhaust gas is irradiated with radiation, it is an active species with a very strong oxidizing power from oxygen molecules and water molecules present in the exhaust gas.
OH, O, HO 2 etc. are generated. These active species are S
The O x and NO x and oxidation respectively, to form a H 2 SHO 4 and HNO 3. The H 2 SO 4 and HNO 3 thus formed then react with the ammonia added in the exhaust gas.
(NH 4 ) 2 SO 4 (ammonium sulfate) and NH 4 NO 3 (ammonium nitrate) are formed, respectively. A typical reaction that occurs in the process of the above ammonium sulfate and ammonium nitrate formation reaction is shown by a formula as follows.
SO2＋2OH→H2SO4 ……（２） H2SO4＋2NH3→(NH4)2SO4 ……（３） NO＋HO2→HNO3 ……（４） HNO3＋NH3→NH4NO3 ……（５） アンモニア添加放射線照射排ガス処理法（以下「アン添
照射法」という。）は、総体的にみて発熱反応である。
発熱の原因は二つに大別できる。一つは照射した放射線
エネルギーが排ガスに吸収されて熱エネルギーに変るこ
とによる発熱である。これは排ガスの温度を高める要因
の一つとなる。排ガスの吸収線量をＤ（Mrad）、排ガス
の流量をＱ（Nm3/h）、排ガス密度を とするとき、放射線エネルギーの吸収によって生じる発
熱量Ｃ（kcal/h）は次の式によって与えられる。 SO 2 + 2OH → H 2 SO 4 …… (2) H 2 SO 4 ＋ 2NH 3 → (NH 4 ) 2 SO 4 …… (3) NO + HO 2 → HNO 3 …… (4) HNO 3 + NH 3 → NH 4 NO 3 (5) The ammonia-added radiation irradiation exhaust gas treatment method (hereinafter referred to as the "Anne addition irradiation method") is an exothermic reaction as a whole.
There are two main causes of fever. One is heat generation due to the absorbed radiation energy being absorbed by the exhaust gas and converted into heat energy. This is one of the factors that increase the temperature of exhaust gas. The absorbed dose of exhaust gas is D (Mrad), the flow rate of exhaust gas is Q (Nm 3 / h), and the exhaust gas density is Then, the calorific value C (kcal / h) generated by the absorption of radiation energy is given by the following equation.
もう一つの発熱原因は脱硫反応〔すなわち、上記（２）
および（３）式による反応〕および脱硝反応〔すなわ
ち、上記（４）および（５）式による反応〕による反応
熱の発生である。ガスの流量Ｑは上記と同じであるとし
て、未処理排ガス中のSOx濃度を〔SOx〕（ppm）、脱硫
率をηSOx、未処理排ガス中のNOx濃度を〔NOx〕（pp
m）、脱硝率をηNOxとするとき、脱硫による発熱量Ａ
（kcal/h）および脱硝による発熱量Ｂ（kcal/h）は、そ
れぞれ次の式で与えられる。 Another cause of heat generation is desulfurization reaction [that is, (2) above.
And the reaction according to the equation (3)] and the denitration reaction [that is, the reaction according to the equations (4) and (5)]. As gas flow rate Q are as defined above, the SO x concentration in the untreated flue gas [SO x] (ppm), the desulfurization rate eta SOx, the concentration of NO x untreated flue gas [NO x] (pp
m) and the NOx removal rate is η NOx , the calorific value A due to desulfurization
(Kcal / h) and the calorific value B (kcal / h) due to denitration are given by the following equations, respectively.
Ａ＝Ｑ×〔SOgx〕×ηSO2×10-6×103×1/22.4×131.02
（kcal/h） ……（７） Ｂ＝Ｑ×〔NOx〕×ηNOx×10-6×103×1/22.4×68.93
（kcal/h） ……（８） したがって、排ガスの比熱をｃ（kcal/kg℃）とすると
き、アン添照射法による排ガス温度の上昇ΔＴ（℃）は
次の式で与えられる。A = Q × [SO gx ] × η SO2 × 10 -6 × 10 3 × 1/2 2.4 × 13 1.02
(Kcal / h) (7) B = Q × [NO x ] × η NOx × 10 −6 × 10 3 × 1 / 22.4 × 68.93
(Kcal / h) (8) Therefore, when the specific heat of the exhaust gas is c (kcal / kg ° C), the increase ΔT (° C) of the exhaust gas temperature by the Anne-addition irradiation method is given by the following formula.
上の各式を用い、 ｃ＝0.27（kcal/kg℃） と仮定して、具体的に排ガス処理の一例を示すと次の通
りである。 Using the above equations, Assuming that c = 0.27 (kcal / kg ° C.), a specific example of exhaust gas treatment is as follows.
たとえば300MWの発電能力をもつ発電所について考える
と、排ガスの流量は概略1,000,000Nm3/hと推定される。
この排ガスのSO2濃度を2,000ppm、NOx濃度を300ppmと仮
定し、排ガスに照射する電子線の量を吸収線量で1.8Mra
dとすると、アン添照射法によってこの排ガスを処理し
たときの排ガスの温度上昇は次のようにする。For example, considering a power plant with a power generation capacity of 300 MW, the flow rate of exhaust gas is estimated to be approximately 1,000,000 Nm 3 / h.
Assuming that the SO 2 concentration of this exhaust gas is 2,000 ppm and the NO x concentration is 300 ppm, the amount of electron beam irradiated to the exhaust gas is 1.8 Mra in absorbed dose.
Assuming d, the temperature rise of the exhaust gas when the exhaust gas is treated by the Annealing irradiation method is as follows.
（６）式より Ｃ＝2.39×1.8×1,000,000×1.3＝5,592,600 （kcal/hr） （７）式より Ａ＝1,000,000×2,000×1.0×10-6×103× 1/22.4×131.02＝11,698,214（Kcal/hr） （８）式より Ｂ＝1,000,000×300×1.0×10-6×103× 1/22.4×68.93＝923,170（kcal/h） したがって（９）式より すなわち、高SOx,NOx含有排ガス処理の場合、上記の例
では、約52℃の温度上昇となる。そこで、反応器入口ガ
ス温度を53℃に調整し、反応器中央部のガス温を とした。すると出口ガス温度は105℃と高温となるため
に除去率は、向上しなかった。つまり、反応器中央部の
ガス温度より反応器下流のガス温度の方がより重要であ
ることが明らかとなった。From formula (6) C = 2.39 x 1.8 x 1,000,000 x 1.3 = 5,592,600 (kcal / hr) From formula (7) A = 1,000,000 x 2,000 x 1.0 x 10 -6 x 10 3 x 1 / 22.4 x 131.02 = 11,698,214 (Kcal / hr) From equation (8) B = 1,000,000 × 300 × 1.0 × 10 -6 × 10 3 × 1 / 22.4 × 68.93 = 923,170 (kcal / h) Therefore, from equation (9) That is, the high SO x, if of the NO x containing exhaust gas treatment, in the above example, the temperature increase of about 52 ° C.. Therefore, the gas temperature at the reactor inlet was adjusted to 53 ° C and the gas temperature in the center of the reactor was adjusted. And Then, the outlet gas temperature was as high as 105 ° C, and the removal rate was not improved. That is, it became clear that the gas temperature downstream of the reactor is more important than the gas temperature at the center of the reactor.
また、今回実施の高SOx,NOx排ガステストの結果、脱硫
反応として新たに次式で表わされる熱化学反応が存在す
ることが確認された。In addition, as a result of the high SO x , NO x exhaust gas test conducted this time, it was confirmed that a thermochemical reaction newly represented by the following formula exists as a desulfurization reaction.
SOx＋2NH3＋H2O＋1/2O２→(NH4)2SO4 ……（10） この新たに確認された反応は、反応器下流の電気集塵機
（ESP）および／またはバグフィルター内で大きく進行
することおよびその温度依存性が大きく、低温ほど進行
することが明らかとなった。本発明者等は、これらの新
たな結果に基づき、本願排ガス処理法の実用的な温度コ
ントロール法を発明するに至った。SO x + 2NH 3 + H 2 O + 1 / 2O 2 → (NH 4 ) 2 SO 4 (10) This newly confirmed reaction greatly progresses in the electrostatic precipitator (ESP) and / or bag filter downstream of the reactor. It was found that the temperature dependence and the temperature dependence were large, and that the lower the temperature, the higher the progress. Based on these new results, the present inventors have invented a practical temperature control method for the exhaust gas treatment method of the present application.
第１図に従って本発明を説明する。ボイラー１で発生し
た高濃度SOxおよび／またはNOxを含む排ガス（通常130
℃以上の高温である）は、排ガス導管２を経て冷却塔３
に導かれる。ここで排ガスは、冷却水管４によりスプレ
ーされる冷却水により、排ガス湿度が飽和になる温度以
上で100℃以下の範囲の温度に冷却された後、排ガス導
管５を経て反応器７に導かれる。導管５の途中でアンモ
ニア添加装置６によりアンモニアを加えられる。反応器
に導入された排ガスは放射線発生装置９からの放射線を
照射される。反応器内の照射区域よりも手前（上流）の
位置に固定した冷却水供給管８′により冷却水をスプレ
ーする。排ガス中のSOxおよび／またはNOxは硫安および
／または硝安に変化するので、これらを集塵機で回収
し、浄化した排ガスを導管あるいは煙突13を経て大気に
放出する。The present invention will be described with reference to FIG. Exhaust gas containing high concentration SO x and / or NO x generated in boiler 1 (usually 130
(High temperature of ℃ or more) passes through the exhaust gas conduit 2 and the cooling tower 3
Be led to. Here, the exhaust gas is cooled by the cooling water sprayed by the cooling water pipe 4 to a temperature in the range of 100 ° C. or higher to a temperature at which the exhaust gas humidity is saturated, and then introduced into the reactor 7 via the exhaust gas conduit 5. Ammonia can be added by the ammonia addition device 6 in the middle of the conduit 5. The exhaust gas introduced into the reactor is irradiated with the radiation from the radiation generator 9. Cooling water is sprayed by a cooling water supply pipe 8'fixed at a position (upstream) in front of the irradiation area in the reactor. Since SO x and / or NO x in the exhaust gas changes to ammonium sulfate and / or ammonium nitrate, these are collected by a dust collector, and the purified exhaust gas is discharged to the atmosphere via the conduit or the chimney 13.
この冷却水供給管８′により冷却水をスプレーするの
は、スプレー水の蒸発潜熱を利用して、前述の放射線エ
ネルギーの吸収と脱硫・脱硝反応による発熱に伴う温度
上昇を防ぎ、集塵機出口のガス温を調整するためであ
る。The cooling water is sprayed by the cooling water supply pipe 8'by utilizing the latent heat of vaporization of the spray water to prevent the temperature rise due to the absorption of radiation energy and the heat generation due to the desulfurization / denitration reaction, and the gas at the dust collector outlet. This is to adjust the temperature.
本発明で使用する集塵機としては、バグフィルター単独
または電気集塵機（ESP）単独または電気集塵機（ESP）
とバグフィルターの組合せの集塵機である。ESPとバグ
フィルターの組合せの場合にはバグフィルター出口のガ
ス温度を、排ガス湿度が飽和になる温度以上で100℃以
下となるように冷却水をスプレーするのが望ましく、ま
たESP単独の場合には、ESP出口ガス温度を、排ガス湿度
が飽和になる温度以上の90℃以下になるように冷却水を
スプレーするのが望ましい。As the dust collector used in the present invention, a bag filter alone or an electrostatic precipitator (ESP) alone or an electrostatic precipitator (ESP)
It is a dust collector that is a combination of a bag filter and a bag filter. In the case of a combination of ESP and bag filter, it is desirable to spray cooling water so that the gas temperature at the bag filter outlet is 100 ° C or less above the temperature at which the exhaust gas humidity becomes saturated, and in the case of ESP alone It is desirable to spray the cooling water so that the ESP outlet gas temperature is 90 ° C or lower, which is higher than the temperature at which the exhaust gas humidity becomes saturated.
第２図に本発明の他の実施態様を示す。第２図の方法
は、第１図に示した方法に改良を加えたものである。第
１図と異なる点は、冷却水のスプレー位置を放射線照射
前から後に変更したことである。これは後述の実施例に
示すように、照射後に水スプレーを移して実施したとこ
ろ、SOx,NOxの除去率、特に脱硝率が向上した結果に基
づくものである。FIG. 2 shows another embodiment of the present invention. The method of FIG. 2 is an improvement of the method shown in FIG. The difference from FIG. 1 is that the spray position of the cooling water is changed from before irradiation to after irradiation. This is based on the result that when the water spray was transferred after the irradiation and the removal rate of SO x and NO x , in particular, the denitration rate was improved, as shown in Examples described later.
第２図に示す方法の向上効果の理由として、第１図の方
法では反応器中にスプレーされた微小水滴は、反応器内
で蒸発し、その蒸発潜熱により排ガス温度を低下させる
が、それらの水滴は反応器内の放射線照射区域を排ガス
と共に通過する際に、照射された放射線の一部を直接吸
収する。このようにして水滴に吸収された放射線エネル
ギーは、水滴中で熱に変り、単にこの水滴の蒸発のため
に消費され、本来の照射目的である排ガス中での活性種
の生成に寄与しないためと考えられる。The reason for the improvement effect of the method shown in FIG. 2 is that in the method shown in FIG. 1, the fine water droplets sprayed in the reactor evaporate in the reactor and the exhaust gas temperature is lowered due to the latent heat of vaporization. The water droplets directly absorb a portion of the applied radiation as they pass through the irradiation area in the reactor with the exhaust gas. The radiation energy absorbed in the water droplets in this way is converted into heat in the water droplets, and is simply consumed for evaporation of the water droplets, and does not contribute to the generation of active species in the exhaust gas, which is the original purpose of irradiation. Conceivable.
冷却水のスプレーを行なう方向は、排ガスの流れる方向
と同一の方向（並流方式）でも十分よい効果が得られる
ことが確認されたが、第２図に示すように、排ガスの流
れと逆方向（向流方式）にすることによって、さらによ
い効果が得られることがわかった。向流方式にした場
合、スプレーと排ガスとが衝突する部分にガス流の乱れ
が生じ、水滴の気化を促進する効果があるためと考えら
れる。It has been confirmed that the spraying of cooling water can be performed sufficiently in the same direction as the exhaust gas flow direction (cocurrent flow method), but as shown in Fig. 2, the direction opposite to the exhaust gas flow direction is obtained. It was found that a better effect can be obtained by using the (countercurrent method). It is considered that when the counterflow method is used, the gas flow is disturbed at the portion where the spray and the exhaust gas collide with each other, which has the effect of promoting vaporization of water droplets.
第３図には第２図とは別の、本発明の他の好ましい実施
態様を示す。第３図に示す方法は、ガス−ガスヒーター
14により高温の未処理ガスと比較的低温の処理済ガスの
間で熱交換させるものであり、本発明のガス処理全体で
の冷却水量の低減および大気に放出される処理済ガスの
高温化による拡散効果が可能である。FIG. 3 shows another preferred embodiment of the present invention different from FIG. The method shown in FIG. 3 is a gas-gas heater.
14 is for heat exchange between a high temperature untreated gas and a relatively low temperature treated gas, which is caused by a reduction in the amount of cooling water in the entire gas treatment of the present invention and a high temperature of the treated gas released to the atmosphere. Diffusion effect is possible.
上記に排ガス温度の調整手段として、冷却水を使用して
いるが、冷却水の代用として、常温空気または冷却空気
の添加による方法も可能である。Although the cooling water is used as the means for adjusting the exhaust gas temperature in the above, a method of adding normal temperature air or cooling air can be used as a substitute for the cooling water.
なお、以下に本方法で使用する集塵機について述べる。
生成する硫安および硝安は、付着性、凝集性、吸湿性に
富んだ極めて微細な粉体粒子であり、バグフィルターの
ような過集塵方式では粉体量が多いとき、過抵抗が
比較的短時間に増大するので過面積を大きくすること
または粒子同志のフィルター上での付着凝集を防ぐた
め、バグフィルター上流の排ガスにケイソウ土、クレー
等の過助材を添加して過面の閉塞を防ぐなどにより
使用するが、除塵効率の高い集塵方式である。The dust collector used in this method will be described below.
The ammonium sulfate and ammonium nitrate that are produced are extremely fine powder particles that are highly adherent, cohesive, and hygroscopic.In a dust collection method such as a bag filter, when the amount of powder is large, the overresistance is relatively short. Since it increases with time, in order to increase the excess area or prevent the adhesion and agglomeration of particles on the filter, an excess amount of diatomaceous earth, clay, etc. is added to the exhaust gas upstream of the bag filter to prevent clogging of the excess surface. This is a dust collection method with high dust removal efficiency.
ESP単独の場合、バグフィルターのような閉塞問題はな
く使用可能である。しかし煤塵規制が、例えば10mg/Nm3
以下と特別に厳しい条件では、ESP内ガス流速を下げて
（例えば0.3m/s）対応するため設備が大きくなる場合が
ある。ESP alone can be used without the problem of blockage like a bug filter. However, the dust regulation is, for example, 10 mg / Nm 3
Under particularly severe conditions such as the following, the equipment may become large in order to reduce the gas flow rate in the ESP (for example, 0.3 m / s).
ESPとバグフィルター組合せ集塵の場合、厳しい煤塵規
制に対応できかつ閉塞問題もない方法である。すなわ
ち、後流にバグフィルターがあるのでESPは比較的速い
ガス流速（１〜3m/s）を採用でき、かつ後流のバグフィ
ルターはガス中の粉体含有料が小さくなっているため
過抵抗が短時間に増大することはない。従って過面積
を大きくする必要がなく、ESP.バグフィルターどちらも
コンパクトとなり経済的で好ましい集塵方式である。In the case of combined dust collection with ESP and bag filter, it is a method that can comply with strict soot dust regulations and does not have a blocking problem. That is, since there is a bag filter in the wake, ESP can adopt a relatively high gas flow rate (1 to 3 m / s), and the bag filter in the wake has an excessive resistance because the powder content in the gas is small. Does not increase in a short time. Therefore, there is no need to increase the excess area, and both ESP and bag filters are compact and economical and a preferred dust collection method.
以上のように本方法ではESP単独、バグフィルター単
独、ESPとバグフィルターの組合せ集塵が使用可能であ
り、どの方法を採用するかは入口SO2,NOx濃度、脱硫
率、脱硝率および煤塵規制値等により決定される。As described above, ESP alone, bag filter alone, and combined dust collection of ESP and bag filter can be used in this method.Which method is adopted depends on the inlet SO 2 , NO x concentration, desulfurization rate, denitrification rate, and soot dust. It is determined by the regulation value.
さらに、実施例により本発明を説明する。Furthermore, the present invention will be described with reference to examples.
実施例１ 第１図に示す方式の実験装置を用い、ボイラー１の燃焼
排ガスが導管２を経て冷却塔３に導入されるときの温度
が150℃となるように調節した。集塵機としては、ESPと
バグフィルターの組合せ集塵機を使用した。その時の排
ガスのSOx濃度は2,000ppm、NOx濃度は350ppm、水分濃度
8.5％であった。冷却塔にて水スプレーすることによ
り、冷却塔出口における排ガスの温度が70℃となるよう
にした。次に導管５を通過する排ガスに容量で4,350ppm
（１モル）のアンモニアガスを吹き込み混合させ、この
排ガスが8,000Nm3/hの流量で反応器７を通過するように
した。電子線加速器からの電子線を1.8Mrad照射し、冷
却水スプレー管８′から冷却水をスプレー添加し、集塵
機出口（バグフィルター出口）の排ガス温度を65〜100
℃に変化させた。全実験時間を通じてほぼ上記の条件が
維持されるようにし、連続的に８時間実験を行なった。
この間に生成する固形副生物をESPおよびバグフィルタ
ーで回収した。定常状態が安定に維持されているときに
ESP入口、出口およびバグフィルター出口のガス温度な
らびに数回サンプリングを行ない排ガス中のSOx濃度、
およびNOx濃度を測定してその平均値を求めた。第５図
および第６図にそれらの結果を示す。Example 1 Using the experimental apparatus of the system shown in FIG. 1, the temperature at which the combustion exhaust gas from the boiler 1 was introduced into the cooling tower 3 via the conduit 2 was adjusted to 150 ° C. As the dust collector, a combined dust collector of ESP and bag filter was used. SO x concentration in the exhaust gas at that time 2,000 ppm, NO x concentration 350 ppm, moisture concentration
It was 8.5%. By spraying with water in the cooling tower, the temperature of the exhaust gas at the outlet of the cooling tower was adjusted to 70 ° C. Next, the exhaust gas passing through the conduit 5 has a capacity of 4,350 ppm
(1 mol) of ammonia gas was blown in and mixed, and this exhaust gas was allowed to pass through the reactor 7 at a flow rate of 8,000 Nm 3 / h. Irradiate the electron beam from the electron beam accelerator with 1.8 Mrad, spray the cooling water from the cooling water spray pipe 8 ', and set the exhaust gas temperature at the dust collector outlet (bag filter outlet) to 65-100.
Changed to ° C. The above conditions were maintained for the entire experiment time, and the experiment was continuously performed for 8 hours.
The solid by-product generated during this time was collected by ESP and a bag filter. When steady state is maintained stable
ESP inlet, outlet and bag filter outlet gas temperature and SO x concentration in exhaust gas after sampling several times,
The NO x concentration was measured and the average value was calculated. The results are shown in FIGS. 5 and 6.
なお、各サンプリング点の排ガス湿度が飽和になる温度
は約56℃である。The temperature at which the exhaust gas humidity at each sampling point becomes saturated is approximately 56 ° C.
実施例２ 冷却水を第２図の18に示すような照射区域のすぐ下流の
位置でスプレーしたこと以外は実施例１と全く同じ条件
で実験を行なった。照射した電子線の量も1.8Mradで実
施例１の場合と同じである。生成した固形副生物をESP
およびバグフィルターで分離した。排ガスのサンプルを
実施例１の場合と同様に採取し、SOx濃度およびNOx濃度
を測定した。結果として、脱硝率は実施例１に比し約５
〜10％向上した。脱硫率は、実施例１とほとんど同様で
あった。Example 2 An experiment was conducted under exactly the same conditions as in Example 1 except that cooling water was sprayed at a position immediately downstream of the irradiation area as shown in FIG. The amount of electron beam irradiated was 1.8 Mrad, which is the same as in the first embodiment. ESP generated solid by-product
And separated with a bag filter. Samples of gas were collected in the same manner as in Example 1, it was measured SO x concentration and NO x concentration. As a result, the denitration rate was about 5 as compared with Example 1.
~ 10% improved. The desulfurization rate was almost the same as in Example 1.
実施例３ 集塵機としてバグフィルター単独を使用したこと以外は
実施例１と同条件でテストを実施し、バグフィルター出
口でガス温度の測定およびSOx,NOx濃度を測定した。結
果は、ESPとバグフィルター組合せの場合のバグフィル
ター出口の結果とほとんど同様であった（第５図、第６
図参照）。Example 3 A test was conducted under the same conditions as in Example 1 except that a bag filter alone was used as the dust collector, and the gas temperature and the SO x and NO x concentrations were measured at the bag filter outlet. The results were almost the same as the results at the bag filter exit in the case of the ESP and bag filter combination (Figs. 5 and 6).
See figure).
第５図より脱硫率は、ガス温度の影響を強くうけ、低温
ほど向上することまた集塵機でも大きく進行することが
わかる。ESPとバグフィルター組合せ集塵およびバグフ
ィルター単独集塵の場合は100℃以下が望ましいこと、E
SP単独では90℃以下が望ましいことが認められる。いず
れの場合も低温ほど良いが、その下限温度として、本方
式の乾式化のため、排ガス湿度が飽和になる温度以上が
好ましい。実施例の場合の下限温度は約56℃である。ま
た、第５図より本方式の脱硫反応は100℃以下で大きく
進行することから、反応器入口ガス温も100℃を越えな
いことが望ましい。反応器入口ガス温度の下限は、前述
のように乾式化のため、排ガス湿度が飽和になる温度以
上が好ましい。It can be seen from FIG. 5 that the desulfurization rate is strongly influenced by the gas temperature and improves as the temperature lowers, and also that the desulfurization rate greatly progresses. For combination of ESP and bag filter dust collection and bag filter single dust collection, 100 ° C or less is desirable.
It is recognized that it is desirable to use the SP alone at 90 ° C or lower. In either case, the lower the temperature, the better, but the lower limit temperature is preferably a temperature at which the exhaust gas humidity is saturated or higher because of the dry method of this system. In the case of the embodiment, the lower limit temperature is about 56 ° C. Further, as shown in FIG. 5, the desulfurization reaction of this system greatly progresses at 100 ° C. or lower, so it is desirable that the gas temperature at the reactor inlet also does not exceed 100 ° C. The lower limit of the gas temperature at the reactor inlet is preferably equal to or higher than the temperature at which the exhaust gas humidity becomes saturated because of the dry process as described above.
以上照射直前および直後の水スプレー方式について述べ
たが、例えば、処理ガス条件（入口ガス温度、水分濃
度、SOx濃度、NOx濃度、脱硫率、脱硝率等）によって定
まるスプレー水量が多い場合等には、両者併用または照
射中のスプレーとの組合せ等によるコントロールも好ま
しい方式である。Although the water spray method immediately before and immediately after irradiation has been described above, for example, when the amount of spray water determined by the processing gas conditions (inlet gas temperature, water concentration, SO x concentration, NO x concentration, desulfurization rate, denitrification rate, etc.) is large, etc. In addition, a control method by using both of them or a combination with a spray during irradiation is also a preferable method.
第６図は、バグフィルター出口のガス温度と脱硝率との
関係を示すが、脱硝率はガス温度の影響を脱硫率程強く
うけないことが認められる。なお、サンプリング位置に
よる脱硝率の差は見られなかった。FIG. 6 shows the relationship between the gas temperature at the outlet of the bag filter and the denitrification rate. It is recognized that the denitrification rate is less affected by the gas temperature than the desulfurization rate. No difference in the denitration rate depending on the sampling position was observed.
第１図は、冷却水のスプレー添加を照射直前に行なう本
発明方法のアンモニア添加放射線照射排ガス処理法の工
程概略図である。 第２図は、冷却水スプレー添加を照射直後に行なう本発
明方法のアンモニア添加放射線照射排ガス処理法の工程
概略図である。 第３図は、ガス−ガスヒーターにより高温の未処理排ガ
スと比較的低温の処理済排ガスの間で熱交換させ、冷却
水のスプレー添加を照射直後に行なう本発明方法のアン
モニア添加放射線照射排ガス処理法の工程概略図であ
る。 第４図は、先行技術の日本特許第1,171,144号に記載の
アンモニア添加放射線照射排ガス温度調整法の工程概略
図である。 第５図は、EPS入口、EPS出口、バグフィルター出口の夫
々のガス温度と脱硫率との関係を示す。 第６図は、バグフィルター出口のガス温度と脱硝率との
関係を示す。 図中の記号は次のものをそれぞれ表わす。 １……ボイラー、２……排ガス導管 ３……冷却塔、４……冷却水供給管 ５……排ガス導管 ６……アンモニア添加装置 ７……反応器 8,8′……冷却水供給管 ９……放射線発生装置（電子線） 10……排ガス導管、11……集塵機 12……副生品回収系路、13……排ガス導管（煙突） 14……ガス−ガスヒーターFIG. 1 is a process schematic diagram of an ammonia-added radiation irradiation exhaust gas treatment method of the method of the present invention in which spray addition of cooling water is performed immediately before irradiation. FIG. 2 is a schematic view of the steps of the ammonia addition radiation irradiation exhaust gas treatment method of the method of the present invention in which cooling water spray addition is performed immediately after irradiation. FIG. 3 is an ammonia-added radiation irradiation exhaust gas treatment of the method of the present invention in which heat is exchanged between a high-temperature untreated exhaust gas and a relatively low-temperature treated exhaust gas by a gas-gas heater, and cooling water is spray-added immediately after irradiation. It is a process schematic of a method. FIG. 4 is a process schematic diagram of the ammonia addition radiation irradiation exhaust gas temperature adjusting method described in Japanese Patent No. 1,171,144 of the prior art. FIG. 5 shows the relationship between the gas temperature and the desulfurization rate at the EPS inlet, EPS outlet, and bag filter outlet. FIG. 6 shows the relationship between the gas temperature at the bag filter outlet and the denitration rate. The symbols in the figure represent the following respectively. 1 ... Boiler, 2 ... Exhaust gas pipe 3 ... Cooling tower, 4 ... Cooling water supply pipe 5 ... Exhaust gas pipe 6 ... Ammonia addition device 7 ... Reactor 8, 8 '... Cooling water supply pipe 9 …… Radiation generator (electron beam) 10 …… Exhaust gas conduit, 11 …… Dust collector 12 …… By-product collection system path, 13 …… Exhaust gas conduit (chimney) 14 …… Gas-gas heater
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/74 (72)発明者 青木 慎治 東京都大田区羽田旭町11番１号 株式会社 荏原製作所内 (56)参考文献 特開 昭55−97233（ＪＰ，Ａ) 特開 昭50−40463（ＪＰ，Ａ)─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Reference number within the agency FI Technical indication location B01D 53/74 (72) Inventor Shinji Aoki 11-1 Haneda-Asahicho, Ota-ku, Tokyo EBARA CORPORATION In-house (56) Reference JP-A-55-97233 (JP, A) JP-A-50-40463 (JP, A)
Claims (6)
放射線照射区域に誘導すること、照射前、照射中または
照射後の排ガスにアンモニア（NH3）を添加すること、
並びに形成された硫安を含む固形副生物を集塵機で捕集
した後排ガスを大気に放出することからなる排ガス処理
法であって、 反応器入口の排ガス温度を、排ガス湿度が飽和になる温
度以上で100℃以下に調整し、 反応器内で該排ガスに放射線を照射し、 反応器内で放射線の照射前、照射中、照射後の内の少な
くとも１ケ所から排ガスに冷却水をスプレーし、 集塵機としてバグフィルター単独または電気集塵機およ
びバグフィルターの組合せ集塵機を使用し、 バグフィルター出口の排ガス湿度を排ガス湿度が飽和に
なる温度以上で100℃以下の範囲に調整することを特徴
とする排ガス処理法。1. Induction into an exhaust gas radiation irradiation area containing a high concentration of sulfur oxide (SO x ), addition of ammonia (NH 3 ) to the exhaust gas before, during or after irradiation,
In addition, an exhaust gas treatment method comprising collecting the formed solid by-products including ammonium sulfate with a dust collector and then discharging the exhaust gas to the atmosphere, wherein the exhaust gas temperature at the reactor inlet is equal to or higher than a temperature at which exhaust gas humidity becomes saturated. Adjust the temperature to 100 ° C or less, irradiate the exhaust gas with radiation in the reactor, and spray cooling water on the exhaust gas from at least one of the inside of the reactor before, during, and after irradiation of the radiation, and use it as a dust collector. An exhaust gas treatment method characterized by using a bag filter alone or an electric dust collector and a combination of bag filters to adjust the exhaust gas humidity at the bag filter outlet to a range of 100 ° C or higher at a temperature at which the exhaust gas humidity becomes saturated or higher.
水をスプレーし、集塵機出口排ガス温度を調整すること
を特徴とする特許請求の範囲第１項に記載の排ガスの処
理法。2. The method for treating exhaust gas according to claim 1, wherein the exhaust gas before irradiation with radiation is sprayed with cooling water in the reactor to adjust the exhaust gas temperature at the outlet of the dust collector.
る、特許請求の範囲第１項又は第２項に記載の排ガスの
処理法。3. The method for treating exhaust gas according to claim 1 or 2, wherein the radiation is an electron beam from an electron beam accelerator.
を放射線照射区域に誘導すること、照射前、照射中また
は照射後の排ガスにアンモニア（NH3）を添加するこ
と、並びに形成された硫安を含む固形副生物を集塵機で
捕集した後排ガスを大気に放出することからなる排ガス
処理法であって、 反応器入口の排ガス温度を、排ガス湿度が飽和になる温
度以上で100℃以下に調整し、 反応器内で該排ガスに放射線を照射し、 反応器内で放射線の照射前、照射中、照射後の内の少な
くとも１ケ所から排ガスに冷却水をスプレーし、 集塵機として電気集塵機を使用し、 電気集塵機の出口排ガス温度を排ガス湿度が飽和になる
温度以上で90℃以下の範囲に調整することを特徴とする
排ガス処理法。4. Introducing an exhaust gas containing a high concentration of sulfur oxide (SO x ) to a radiation irradiation area, adding ammonia (NH 3 ) to the exhaust gas before irradiation, during irradiation, or after irradiation, and formation thereof. The exhaust gas treatment method consists of collecting solid by-products containing ammonium sulphate with a dust collector and then discharging the exhaust gas to the atmosphere.The exhaust gas temperature at the reactor inlet is 100 ° C above the temperature at which the exhaust gas humidity becomes saturated. Adjust the following, irradiate the exhaust gas with radiation in the reactor, spray cooling water on the exhaust gas from at least one of before, during, and after irradiation of radiation in the reactor, as an electrostatic precipitator Is used to adjust the temperature of the exhaust gas at the outlet of the electrostatic precipitator to a range of not lower than 90 ° C and not lower than the temperature at which the exhaust gas humidity becomes saturated.
水をスプレーし、集塵機出口排ガス温度を調整すること
を特徴とする特許請求の範囲第４項に記載の排ガスの処
理法。5. The method for treating exhaust gas according to claim 4, wherein the exhaust gas before irradiation with radiation is sprayed with cooling water in the reactor to adjust the exhaust gas temperature at the exit of the dust collector.
る、特許請求の範囲第４項又は第５項に記載の排ガスの
処理法。6. The method for treating exhaust gas according to claim 4, wherein the radiation is an electron beam from an electron beam accelerator.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62308887A JPH0741143B2 (en) | 1987-05-30 | 1987-12-07 | Exhaust gas treatment method |
| DE8888108408T DE3877834T2 (en) | 1987-05-30 | 1988-05-26 | METHOD FOR TREATING EXHAUST GAS. |
| EP88108408A EP0294658B1 (en) | 1987-05-30 | 1988-05-26 | Process for treating effluent gas |
| CA000567783A CA1324782C (en) | 1987-05-30 | 1988-05-26 | Process for treating effluent gas |
| US07/199,859 US4882020A (en) | 1987-05-30 | 1988-05-27 | Process for treating effluent gas |
| CN88103234A CN1011858B (en) | 1987-05-30 | 1988-05-30 | Process for treating waste gas |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62-136067 | 1987-05-30 | ||
| JP13606787 | 1987-05-30 | ||
| JP62308887A JPH0741143B2 (en) | 1987-05-30 | 1987-12-07 | Exhaust gas treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01135519A JPH01135519A (en) | 1989-05-29 |
| JPH0741143B2 true JPH0741143B2 (en) | 1995-05-10 |
Family
ID=15166439
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62308887A Expired - Fee Related JPH0741143B2 (en) | 1987-05-30 | 1987-12-07 | Exhaust gas treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0741143B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| PL340879A1 (en) | 1997-12-01 | 2001-03-12 | Ebara Corp | Method of and apparatus for desulphurising flue gas |
| JP2007029819A (en) * | 2005-07-25 | 2007-02-08 | Kawasaki Heavy Ind Ltd | Exhaust gas purification electron beam irradiation device |
| DE102010031063A1 (en) | 2010-07-07 | 2012-01-12 | Robert Bosch Gmbh | A sensor device for a pedal and method for providing information regarding an operation of a pedal |
| DE102010042216A1 (en) | 2010-10-08 | 2011-06-09 | Basf Se | Process for inhibiting the undesired radical polymerization of acrylic acid present in a liquid phase P. |
| CN114849434B (en) * | 2022-05-09 | 2023-06-16 | 福建龙净环保股份有限公司 | Prilling tower system and tail gas treatment device |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5040463A (en) * | 1973-08-15 | 1975-04-14 | ||
| JPS58884B2 (en) * | 1978-12-29 | 1983-01-08 | 株式会社荏原製作所 | Exhaust gas treatment method using radiation irradiation |
-
1987
- 1987-12-07 JP JP62308887A patent/JPH0741143B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01135519A (en) | 1989-05-29 |
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