JPH0683777B2 - Wet Flue Gas Desulfurization Method - Google Patents
Wet Flue Gas Desulfurization MethodInfo
- Publication number
- JPH0683777B2 JPH0683777B2 JP61142908A JP14290886A JPH0683777B2 JP H0683777 B2 JPH0683777 B2 JP H0683777B2 JP 61142908 A JP61142908 A JP 61142908A JP 14290886 A JP14290886 A JP 14290886A JP H0683777 B2 JPH0683777 B2 JP H0683777B2
- Authority
- JP
- Japan
- Prior art keywords
- slurry
- absorption
- gypsum
- limestone
- particles
- 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 - Lifetime
Links
- 238000006477 desulfuration reaction Methods 0.000 title claims description 15
- 230000023556 desulfurization Effects 0.000 title claims description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 11
- 239000003546 flue gas Substances 0.000 title claims description 11
- 238000000034 method Methods 0.000 title claims description 11
- 239000002002 slurry Substances 0.000 claims description 66
- 238000010521 absorption reaction Methods 0.000 claims description 59
- 239000010440 gypsum Substances 0.000 claims description 53
- 229910052602 gypsum Inorganic materials 0.000 claims description 53
- 235000019738 Limestone Nutrition 0.000 claims description 46
- 239000006028 limestone Substances 0.000 claims description 46
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims description 42
- 235000010261 calcium sulphite Nutrition 0.000 claims description 42
- 239000007789 gas Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 6
- 230000002745 absorbent Effects 0.000 claims description 4
- 239000002250 absorbent Substances 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims 1
- 239000002245 particle Substances 0.000 description 61
- 239000003595 mist Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241001648319 Toronia toru Species 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000001678 irradiating effect Effects 0.000 description 1
- 238000009533 lab test Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は湿式石灰石・石膏法による排煙脱硫方法に関し
吸収スラリーに超音波を照射することによつてSO2吸収
能を高め、効率良く石膏を回収することを可能とした排
煙脱硫方法に関する。The present invention relates to a method for flue gas desulfurization by the wet limestone / gypsum method, which increases the SO 2 absorption capacity by irradiating the absorbing slurry with ultrasonic waves to efficiently and efficiently store gypsum. The present invention relates to a flue gas desulfurization method that enables the recovery of
第３図によつて従来技術（実開昭59−10833号公報）を
説明する。排煙脱硫装置の吸収塔201で燃焼排ガス202を
洗浄する。亜硫酸カルシウム粒子と石膏粒子と石灰石粒
子を懸濁した吸収スラリーを保有する吸収塔タンク203
から吸収塔循環ポンプ204によつてスプレーパイプ205か
ら吸収スラリーをスプレーすることにより、排ガス中の
SO2を吸収する。排ガス中に散布された吸収スラリーは
ミスト状になつて排ガスと接触し同伴されるので、ミス
トエリミネーター206でミストを除去し、浄化ガス207と
して系外へ放出する。ミストエリミネーター206は石膏
粒子、石灰石粒子、亜硫酸カルシウム粒子、フライアッ
シュ粒子などが付着して閉塞し易いので、洗浄ノズル20
8から水を散布して洗浄する。A conventional technique (Japanese Utility Model Laid-Open No. 59-10833) will be described with reference to FIG. The combustion exhaust gas 202 is washed in the absorption tower 201 of the flue gas desulfurization device. Absorption tower tank 203 holding an absorption slurry in which calcium sulfite particles, gypsum particles and limestone particles are suspended.
By spraying the absorption slurry from the spray pipe 205 by using the absorption tower circulation pump 204,
Absorbs SO 2 . Since the absorbing slurry dispersed in the exhaust gas becomes mist-like and comes into contact with the exhaust gas and is entrained therein, the mist is removed by the mist eliminator 206, and the purified gas 207 is released to the outside of the system. Since the mist eliminator 206 is apt to be clogged with gypsum particles, limestone particles, calcium sulfite particles, fly ash particles, etc., the cleaning nozzle 20
Spray with water from 8 and wash.
一方SO2吸収剤である石灰石スラリーを石灰石供給管209
から供給し吸収されたSO2と反応させて亜硫酸カルシウ
ムとするが、排ガス中に含まれる酸素によつて亜硫酸カ
ルシウムの一部が酸化し石膏となる。又、吸収スラリー
のSO2吸収能を高める為にSO2吸収量より過剰の石灰石を
供給するので、結局、吸収塔タンク203に保有される吸
収スラリーは亜硫酸カルシウム粒子と石膏粒子と石灰石
粒子を混合した水性スラリーとなつている。Meanwhile limestone slurry limestone supplied is SO 2 absorber tube 209
It is made to react with SO 2 supplied and absorbed from to form calcium sulfite, but part of the calcium sulfite is oxidized by the oxygen contained in the exhaust gas to form gypsum. Further, since limestone is supplied in excess of the SO 2 absorption amount in order to enhance the SO 2 absorption capacity of the absorption slurry, the absorption slurry held in the absorption tower tank 203 eventually mixes calcium sulfite particles, gypsum particles and limestone particles. It becomes an aqueous slurry.
石膏を副生品として回収する為に、吸収スラリーをバル
ブ211から抜出して分離器212へ導き、石膏スラリー213
と亜硫酸カルシウム・石灰石スラリー214に分離し亜硫
酸カルシウム・石灰石スラリー214は吸収塔タンク203へ
戻すと共に石膏スラリー213は石膏スラリータンク215を
経由して副生石膏分離機（図示せず）へ送られる。In order to collect the gypsum as a by-product, the absorption slurry is extracted from the valve 211 and guided to the separator 212, where the gypsum slurry 213
Then, the calcium sulfite / limestone slurry 214 is separated, the calcium sulfite / limestone slurry 214 is returned to the absorption tower tank 203, and the gypsum slurry 213 is sent to a by-product gypsum separator (not shown) via the gypsum slurry tank 215.
吸収スラリーから石膏スラリーを分離する分離器212に
は次のような問題がある。The separator 212 for separating the gypsum slurry from the absorption slurry has the following problems.
（１）亜硫酸カルシウム粒子及び石灰石粒子が凝集する
性質を有している為、石膏粒子を包含してしまい、ハイ
ドロサイクロンやシックナーの従来の分離方式では石膏
スラリーと亜硫酸カルシウム・石灰石スラリーに２分別
することは困難である。(1) Since calcium sulfite particles and limestone particles have the property of aggregating, gypsum particles are included, and in the conventional separation method of hydrocyclone or thickener, gypsum slurry and calcium sulfite / limestone slurry are separated into two parts. Is difficult.
（２）亜硫酸カルシウムが吸収塔タンクへ戻される為吸
収塔タンク内の吸収スラリー中の亜硫酸カルシウム粒子
が石膏粒子より多くなり、マスバランス上明らかなよう
に連続的に安定して石膏を回収することは出来ない。即
ち亜硫酸カルシウムの一部を酸化して石膏にする割合
（酸化率）を高めないと安定して石膏を回収することは
出来ない。(2) Since calcium sulfite is returned to the absorption tower tank, the amount of calcium sulfite particles in the absorption slurry in the absorption tower tank is larger than that of gypsum particles, and gypsum can be recovered continuously and stably as is clear from the mass balance. I can't. That is, gypsum cannot be stably recovered unless the ratio (oxidation rate) of a part of calcium sulfite to be converted to gypsum is increased.
本発明は上記の問題点を解消するために吸収スラリーに
超音波振動を与えることによつて、凝集した亜硫酸カル
シウム粒子と石灰石粒子を分散させ、石膏粒子との分離
を容易にすると共に亜硫酸カルシウム粒子と石灰石粒子
の反応性を活性化して酸化率の向上と脱硫性能を向上さ
せた湿式排煙脱硫方法を提供しようとするものである。The present invention disperses aggregated calcium sulfite particles and limestone particles by applying ultrasonic vibration to the absorption slurry in order to solve the above problems, and facilitates separation of gypsum particles and calcium sulfite particles. Another object of the present invention is to provide a wet flue gas desulfurization method in which the reactivity of limestone particles is activated to improve the oxidation rate and the desulfurization performance.
本発明は燃焼排ガスを吸収スラリーと気液接触させて排
ガス中の硫黄酸化物を吸収する吸収工程と、該吸収工程
から流出する吸収スラリーに吸収剤である石灰石を加え
て混合する吸収スラリー調整工程と、調整された吸収ス
ラリーを前記吸収工程に循環するとともに、循環する吸
収スラリーの一部を抜き出して分離工程に導き、沈降す
る石膏スラリーと浮上する石灰石・亜硫酸カルシウムス
ラリーに分離して石膏スラリーは石膏回収工程へ、石灰
石・亜硫酸カルシウムスラリーは前記吸収スラリー調整
工程へそれぞれ移送する湿式排煙脱硫方法において、前
記分離工程で吸収スラリーに対して超音波を照射するこ
とを特徴とする湿式排煙脱硫方法である。The present invention is an absorption step of adsorbing sulfur oxides in exhaust gas by bringing combustion exhaust gas into gas-liquid contact with the absorption slurry, and an absorption slurry adjusting step of adding limestone as an absorbent to the absorption slurry flowing out of the absorption step and mixing. And, while circulating the adjusted absorption slurry in the absorption step, a part of the circulating absorption slurry is extracted and guided to a separation step, and the gypsum slurry is separated into a gypsum slurry that sediments and a limestone / calcium sulfite slurry that floats. In the wet flue gas desulfurization method, in which the limestone / calcium sulfite slurry is transferred to the gypsum recovery step, respectively, to the absorption slurry adjustment step, in the separation step, the absorption slurry is irradiated with ultrasonic waves. Is the way.
本発明は亜硫酸カルシウム粒子と石灰石粒子と石膏粒子
が混在する吸収スラリーに対して超音波振動を与えるこ
とにより、石膏スラリーの分離特性を向上させ更に超音
波照射で亜硫酸カルシウム粒子と石灰石粒子の反応活性
を向上させ、石膏への酸化率とSO2吸収能を高める様に
した脱硫方法を見い出したことにある。The present invention, by applying ultrasonic vibration to the absorbing slurry in which calcium sulfite particles, limestone particles and gypsum particles are mixed, the separation characteristics of the gypsum slurry are improved and further the reaction activity of calcium sulfite particles and limestone particles by ultrasonic irradiation. To find a desulfurization method that improves the oxidation rate of gypsum and the SO 2 absorption capacity.
本発明の重要な要素を占める超音波振動による石膏粒子
と亜硫酸カルシウム・石灰石粒子の分離効果を第２図に
より説明する。平均40μの石膏粒子約100g/kg H2Oと平
均10μの亜硫酸カルシウム・石灰石粒子約15g/kg H2Oを
含む吸収スラリーを分離器に供給し、オーバーフローと
アンダーフローの流体流量がほゞ等しくなる様に常に調
整し乍ら、吸収スラリーの分離器への供給量を変化させ
た。即ち、分離器への供給スラリー流量を変えることは
オーバーフロー流量が変わることであり、（常にアンダ
ーフロー流量もオーバーフロー流量とほゞ等しくなる様
に変えた。）オーバーフロー液の分離器内での平均上昇
速度の変化として捕えることが出来る訳である。The effect of separating gypsum particles and calcium sulfite / limestone particles by ultrasonic vibration, which is an important element of the present invention, will be described with reference to FIG. An absorbent slurry containing an average of 40μ gypsum particles of about 100g / kg H 2 O and an average of 10μ of calcium sulfite / limestone particles of about 15g / kg H 2 O was supplied to the separator, and the overflow and underflow fluid flow rates were almost equal. The amount of the absorption slurry supplied to the separator was changed while always adjusting so that In other words, changing the flow rate of slurry supplied to the separator changes the overflow flow rate, and (always changes the underflow flow rate to be almost equal to the overflow flow rate). The average rise of overflow liquid in the separator It can be captured as a change in speed.
超音波照射なしの場合は、第２図中黒塗り印を破線で結
んだ通り、亜硫酸カルシウム・石灰石粒子が凝集してい
る為、石膏粒子と同等の挙動を示し、オーバーフロー液
の上昇速度が4m/h以下ではオーバーフロー液は清澄液に
なつてしまつている。第２図より明らかに石膏粒子と亜
硫酸カルシウム・石灰石粒子とは凝集した状態にあつて
ほゞ同じ沈降速度を有している為、各々の粒子を分離す
ることは困難であつた。In the case of no ultrasonic irradiation, the calcium sulfite / limestone particles are aggregated as shown by connecting the black marks in Fig. 2 with a broken line, so the behavior is the same as gypsum particles, and the rising speed of the overflow liquid is 4 m. Below / h, the overflow liquid has become a clear liquid. As is clear from FIG. 2, it is difficult to separate the gypsum particles and the calcium sulfite / limestone particles in the aggregated state because they have almost the same settling speed.
ところが超音波を照射すると、白印を実線で結んだ通り
亜硫酸カルシウム・石灰石粒子と石膏粒子は分離し易く
なる。更に分離された亜硫酸カルシウム・石灰石粒子は
その粒子表面が分散時に活性化される為、亜硫酸カルシ
ウムは酸化され易くなつて好ましい石膏になり又、石灰
石は中和能力が向上するのでSO2吸収性能が向上する。However, when ultrasonic waves are applied, the calcium sulfite / limestone particles and the gypsum particles are easily separated as indicated by the solid line connecting the white marks. Further, since the separated calcium sulfite / limestone particles have their particle surfaces activated during dispersion, calcium sulfite is easily oxidized and becomes a preferable gypsum, and limestone has an improved neutralizing ability, so that SO 2 absorption performance is improved. improves.
脱硫率と酸化率に及ぼす超音波の効果は表−１の通りで
あつた。The effects of ultrasonic waves on the desulfurization rate and oxidation rate are shown in Table 1.
尚第２図のデータ及び表−１のデータは、第１図に示す
フローからなる小型ラボ試験装置（排ガス量200m3N/h石
炭焚き排ガス処理湿式石灰石・石膏法脱硫装置）に於い
て得られたもので分離器は容積10l、超音波は400W出
力、周波数28KHzの条件で照射したものである。 The data shown in Fig. 2 and the data shown in Table-1 were obtained with a small-scale laboratory test device (exhaust gas amount of 200 m 3 N / h coal-fired exhaust gas treatment wet limestone / gypsum method desulfurization device) consisting of the flow shown in Fig. 1. The separator was irradiated with a volume of 10 liters, ultrasonic waves of 400 W output and a frequency of 28 KHz.
第１図によつて本発明の実施態様を説明する。 An embodiment of the present invention will be described with reference to FIG.
排煙脱硫装置の吸収塔101で燃焼排ガス102を洗浄する所
の石膏粒子と亜硫酸カルシウム粒子と石灰石粒子を懸濁
した吸収スラリーを保有する吸収塔タンク103から吸収
塔循環ポンプ104によつてスプレーパイプ105から吸収ス
ラリーをスプレーすることにより、排ガス中のSO2は吸
収される。排ガス中に散布された吸収スラリーはミスト
状になつて排ガスに同伴するのでミストエリミネーター
106でミストを除去し、浄化ガス107として系外へ放出す
る。ミストエリミネーター106は石灰石・亜硫酸カルシ
ウム、石膏、フライアッシュの各粒子が付着して閉塞し
易いので洗浄ノズル108から水を散布して洗浄する。Spray pipe from absorption tower tank 103 holding absorption slurry in which gypsum particles, calcium sulfite particles and limestone particles are suspended in a place where flue gas 102 is washed in absorption tower 101 of flue gas desulfurization apparatus by absorption tower circulation pump 104 By spraying the absorption slurry from 105, SO 2 in the exhaust gas is absorbed. The absorbing slurry dispersed in the exhaust gas becomes a mist and accompanies the exhaust gas, so the mist eliminator
The mist is removed at 106, and the purified gas 107 is discharged to the outside of the system. Since the particles of limestone / calcium sulfite, gypsum, and fly ash are easily attached to the mist eliminator 106, the mist eliminator 106 is sprayed with water from the cleaning nozzle 108 for cleaning.
一方SO2吸収剤である石灰石スラリーを石灰石供給管109
から供給し吸収されたSO2と反応させて亜硫酸カルシウ
ムとする。吸収スラリーのSO2吸収能を高める為にSO2吸
収量より過剰の石灰石を供給するので吸収スラリー中に
は石灰石粒子が常に存在する。On the other hand, the limestone slurry which is the SO 2 absorbent is supplied to the limestone supply pipe 109.
It reacts with the SO 2 that was supplied from and absorbed to form calcium sulfite. Limestone particles are always present in the absorption slurry because limestone is supplied in excess of the SO 2 absorption amount in order to increase the SO 2 absorption capacity of the absorption slurry.
又亜硫酸カルシウムは排ガス中の酸素によつて酸化され
石膏となるので吸収塔タンク103に保有されるスラリー
は石膏粒子と亜硫酸カルシウム粒子と石灰石粒子を含
む。Further, since calcium sulfite is oxidized by oxygen in exhaust gas to form gypsum, the slurry held in the absorption tower tank 103 contains gypsum particles, calcium sulfite particles and limestone particles.
吸収スラリーの一部はバルブ111を介して分離器112へ導
かれる。分離器112内へ入つた吸収スラリーに超音波振
動を与えて、凝集している亜硫酸カルシウム・石灰石粒
子を分散させる為に超音波振動子113と超音波発振器114
が設けてある。これによつて10μ前後の亜硫酸カルシウ
ム・石灰石粒子と40μ前後の石膏粒子とが分散するの
で、石膏粒子と亜硫酸カルシウム・石灰石粒子の沈降速
度差を利用した分離が効率良く行われる。A part of the absorption slurry is guided to the separator 112 via the valve 111. Ultrasonic vibration is applied to the absorbing slurry that has entered the separator 112 to disperse the aggregated calcium sulfite / limestone particles.
Is provided. As a result, the calcium sulfite / limestone particles having a particle size of about 10 μ and the gypsum particles having a particle size of about 40 μ are dispersed, so that the separation using the difference in the sedimentation velocity between the gypsum particles and the calcium sulfite / limestone particles is efficiently performed.
亜硫酸カルシウム・石灰石粒子をオーバーフロー側に運
ぶ様に、そして石膏粒子はアンダーフロー側に運ばれる
様に流体の移動速度を調整することによつて、亜硫酸カ
ルシウム・石灰石スラリー115と石膏スラリー116が得ら
れる。Calcium sulfite / limestone slurry 115 and gypsum slurry 116 are obtained by adjusting the fluid moving speed so that the calcium sulfite / limestone particles are carried to the overflow side and the gypsum particles are carried to the underflow side. .
分離器112の底流である石膏スラリー116の抜出し量は吸
収塔タンク103に保有される吸収スラリーのスラリー濃
度検出器117（比重計）からの信号を受けてバルブ118の
開閉によつて調整する。これにより、吸収スラリー中の
石膏粒子をスケール防止の種晶として必要な濃度に管理
することが出来る。石膏スラリー116は石膏スラリータ
ンク119を経由して副生石膏分離機110へ送られる。又、
分離器112の溢流である亜硫酸カルシウム・石灰石スラ
リー115は吸収塔タンク103へ戻される。超音波照射によ
つて活性化された亜硫酸カルシウム粒子及び石灰石粒子
は各々排ガス中の酸素で酸化され易く又、SO2吸収能が
増大する。即ち、SO2吸収性能並びに石膏への酸化性能
が向上する効果が得られるので、物質収支上、吸収され
たSO2が全て石膏として回収出来る様になるすぐれた効
果をもたらす。The withdrawal amount of the gypsum slurry 116 which is the bottom flow of the separator 112 is adjusted by opening and closing the valve 118 in response to a signal from the slurry concentration detector 117 (specific gravity meter) of the absorption slurry held in the absorption tower tank 103. As a result, the gypsum particles in the absorption slurry can be controlled to a necessary concentration as seed crystals for scale prevention. The gypsum slurry 116 is sent to the byproduct gypsum separator 110 via the gypsum slurry tank 119. or,
The calcium sulfite / limestone slurry 115, which is the overflow of the separator 112, is returned to the absorption tower tank 103. The calcium sulfite particles and the limestone particles activated by ultrasonic irradiation are easily oxidized by oxygen in the exhaust gas, and the SO 2 absorption capacity is increased. That is, since the effect of improving the SO 2 absorption performance and the oxidation performance to gypsum can be obtained, an excellent effect that all the absorbed SO 2 can be recovered as gypsum in terms of mass balance is brought about.
本発明は上記構成を採用することにより、特に、吸収ス
ラリーに対する超音波照射により、石膏粒子とともに凝
縮している亜硫酸カルシウム・石灰石粒子を分離活性化
し、亜硫酸カルシウムを酸化して石膏を生成する酸化率
を向上させるとともに、石灰石の脱硫能力を向上せし
め、他方、亜硫酸カルシウムと石灰石粒子から分離され
る石膏粒子の分離効率を向上させることができた。The present invention, by adopting the above configuration, in particular, by ultrasonic irradiation to the absorption slurry, the calcium sulfite / limestone particles condensed with the gypsum particles are activated separately, and the oxidation rate of oxidizing calcium sulfite to produce gypsum. It was possible to improve the desulfurization ability of limestone and to improve the separation efficiency of gypsum particles separated from calcium sulfite and limestone particles.
第１図は本発明の構成を示す湿式排煙脱硫方法のフロー
図 第２図は本発明による超音波照射効果を示すグラフ 第３図は従来の湿式排煙脱硫方法のフロー図である。FIG. 1 is a flow chart of a wet flue gas desulfurization method showing the constitution of the present invention. FIG. 2 is a graph showing an ultrasonic irradiation effect according to the present invention. FIG. 3 is a flow chart of a conventional wet flue gas desulfurization method.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 高品 徹 広島県広島市西区観音新町４丁目６番22号 三菱重工業株式会社広島研究所内 (56)参考文献 特開 昭54−61070（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Toru Honshin 4-6-22 Kannon Shinmachi, Nishi-ku, Hiroshima City, Hiroshima Prefecture Mitsubishi Heavy Industries Ltd. Hiroshima Research Laboratory (56) Reference JP-A-54-61070 (JP, A) )
Claims (1)
て排ガス中の硫黄酸化物を吸収する吸収工程と、該吸収
工程から流出する吸収スラリーに吸収剤である石灰石を
加えて混合する吸収スラリー調整工程と、調整された吸
収スラリーを前記吸収工程に循環するとともに、循環す
る吸収スラリーの一部を抜き出して分離工程に導き、沈
降する石膏スラリーと浮上する石灰石・亜硫酸カルシウ
ムスラリーに分離して石膏スラリーは石膏回収工程へ、
石灰石・亜硫酸カルシウムスラリーは前記吸収スラリー
調整工程へそれぞれ移送する湿式排煙脱硫方法におい
て、前記分離工程で吸収スラリーに対して超音波を照射
することを特徴とする湿式排煙脱硫方法。1. An absorption step of adsorbing sulfur oxides in exhaust gas by bringing combustion exhaust gas into gas-liquid contact with the absorption slurry, and an absorption slurry in which limestone as an absorbent is added to and mixed with the absorption slurry flowing out of the absorption step. In the adjusting step, the adjusted absorption slurry is circulated in the absorption step, and a part of the circulating absorption slurry is extracted and guided to a separation step, which is separated into a gypsum slurry that sinks and a limestone / calcium sulfite slurry that floats and gypsum. Slurry goes to gypsum recovery process,
In the wet flue gas desulfurization method of transferring the limestone / calcium sulfite slurry to the absorption slurry preparation step, ultrasonic waves are applied to the absorption slurry in the separation step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61142908A JPH0683777B2 (en) | 1986-06-20 | 1986-06-20 | Wet Flue Gas Desulfurization Method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61142908A JPH0683777B2 (en) | 1986-06-20 | 1986-06-20 | Wet Flue Gas Desulfurization Method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS631426A JPS631426A (en) | 1988-01-06 |
| JPH0683777B2 true JPH0683777B2 (en) | 1994-10-26 |
Family
ID=15326411
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61142908A Expired - Lifetime JPH0683777B2 (en) | 1986-06-20 | 1986-06-20 | Wet Flue Gas Desulfurization Method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0683777B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0722676B2 (en) * | 1986-09-16 | 1995-03-15 | 三菱重工業株式会社 | Flue gas desulfurization method |
-
1986
- 1986-06-20 JP JP61142908A patent/JPH0683777B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS631426A (en) | 1988-01-06 |
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