JPH0833827A - Flue gas desulfurizer - Google Patents
Flue gas desulfurizerInfo
- Publication number
- JPH0833827A JPH0833827A JP6172758A JP17275894A JPH0833827A JP H0833827 A JPH0833827 A JP H0833827A JP 6172758 A JP6172758 A JP 6172758A JP 17275894 A JP17275894 A JP 17275894A JP H0833827 A JPH0833827 A JP H0833827A
- Authority
- JP
- Japan
- Prior art keywords
- flue gas
- mist
- absorption
- flue
- scattered
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 49
- 239000003546 flue gas Substances 0.000 title claims description 49
- 239000003595 mist Substances 0.000 claims abstract description 69
- 239000007921 spray Substances 0.000 claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 239000002250 absorbent Substances 0.000 claims abstract description 4
- 230000002745 absorbent Effects 0.000 claims abstract description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 79
- 230000023556 desulfurization Effects 0.000 claims description 79
- 239000007788 liquid Substances 0.000 claims description 73
- 239000007789 gas Substances 0.000 claims description 53
- 238000010521 absorption reaction Methods 0.000 claims description 50
- 238000002485 combustion reaction Methods 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 238000005507 spraying Methods 0.000 claims description 8
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 8
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 6
- 150000001339 alkali metal compounds Chemical class 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 239000011575 calcium Substances 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 239000000567 combustion gas Substances 0.000 abstract 3
- 239000002699 waste material Substances 0.000 abstract 3
- 230000003009 desulfurizing effect Effects 0.000 abstract 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 15
- 239000010440 gypsum Substances 0.000 description 11
- 229910052602 gypsum Inorganic materials 0.000 description 11
- 238000000034 method Methods 0.000 description 11
- 235000019738 Limestone Nutrition 0.000 description 6
- 239000012717 electrostatic precipitator Substances 0.000 description 6
- 239000006028 limestone Substances 0.000 description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical group [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 4
- 235000010261 calcium sulphite Nutrition 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- 235000012255 calcium oxide Nutrition 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000003100 immobilizing effect Effects 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
- Separating Particles In Gases By Inertia (AREA)
- Filtering Of Dispersed Particles In Gases (AREA)
- Chimneys And Flues (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、燃焼排ガスの煙道内に
吸収液を噴霧して行う排煙脱硫装置に関し、特に噴霧し
た吸収液の捕集に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flue gas desulfurization apparatus for spraying an absorbing liquid into a flue of combustion exhaust gas, and more particularly to collecting the sprayed absorbing liquid.
【０００２】[0002]
【従来の技術】化石燃料を燃料とする火力発電プラント
の燃焼装置からの燃料排ガスに含まれる硫黄酸化物を除
去する排煙脱硫装置には、湿式石灰石−石膏法として知
られている湿式法がある。この排煙脱硫装置は過去１５
年の実績で証明されているように高性能で負荷変化など
に対しても信頼性が高く、国内、国外ともに火力発電プ
ラントの排ガス処理装置として広く採用されている。し
かし、この排煙脱硫装置は吸収塔の出口ガスを再加熱す
ることと排水処理することが必要であり、イニシャルコ
ストも比較的高い。現在の環境問題を解決するには開発
途上国でも脱硫装置を設置する必要性が高くなってお
り、コスト的に開発途上国にマッチングした脱硫装置の
出現が望まれている。2. Description of the Related Art A flue gas desulfurization device for removing sulfur oxides contained in fuel exhaust gas from a combustion device of a thermal power plant using fossil fuel as a fuel is a wet process known as a wet limestone-gypsum process. is there. This flue gas desulfurization system has been used in the past 15
As proved by the results of the year, it has high performance and high reliability against load changes, and is widely adopted as an exhaust gas treatment device for thermal power plants both domestically and internationally. However, this flue gas desulfurization apparatus requires reheating the outlet gas of the absorption tower and waste water treatment, and the initial cost is relatively high. In order to solve the present environmental problems, it is more necessary to install a desulfurization device even in developing countries, and the desulfurization device that matches the developing countries in terms of cost is desired to appear.
【０００３】この目的のためにボイラ火炉内に微粒石灰
石を噴霧して脱硫を行い、さらに燃焼排ガスに同伴して
くる未反応の生石灰の脱硫活性を高めるために煙道に水
を噴霧して調湿する方法が提案されている。しかし、こ
の脱硫装置における脱硫性能を高めるためには硫黄酸化
物に対して２倍から３倍の化学当量の石灰石を供給する
必要がある。また、この脱硫装置の煙道での脱硫反応生
成物は亜硫酸カルシウムである。この亜硫酸塩は後流に
設置する電気集塵器で石炭灰と共に捕集されるが、化学
的には不安定であり石炭灰を固定化処理する際に未だ解
決されていない問題点もある。For this purpose, fine limestone is sprayed into a boiler furnace for desulfurization, and further, water is sprayed to the flue to increase the desulfurization activity of unreacted quicklime accompanying the combustion exhaust gas. Wetting methods have been proposed. However, in order to improve the desulfurization performance in this desulfurization device, it is necessary to supply limestone in a chemical equivalent of 2 to 3 times the sulfur oxide. The desulfurization reaction product in the flue of this desulfurization device is calcium sulfite. This sulfite is collected together with the coal ash by an electrostatic precipitator installed in the downstream, but it is chemically unstable and there is a problem that has not yet been solved when immobilizing the coal ash.
【０００４】そこで、最近注目されているのが前述の湿
式石灰石−石膏法の脱硫方式を煙道で行う方式である。
この方式は湿式脱硫法の高い吸収反応性を有効に使用し
て、できるだけ脱硫反応部をコンパクト化することでイ
ニシャルコスト低減を行うことにある。脱硫反応部をコ
ンパクト化するには吸収反応部での排ガス流速を高める
必要がある。脱硫性能は排ガス流速が大きいほど高めら
れる傾向にあるが、高速の排ガス流に吸収液を噴霧する
と細かな吸収液ミストが飛散し、煙道の後流に飛散して
くる問題がある。Therefore, what has recently been attracting attention is a method in which the desulfurization method of the wet limestone-gypsum method described above is performed by a flue.
This method is intended to effectively use the high absorption reactivity of the wet desulfurization method and to reduce the initial cost by making the desulfurization reaction section as compact as possible. In order to make the desulfurization reaction section compact, it is necessary to increase the exhaust gas flow rate in the absorption reaction section. The desulfurization performance tends to be enhanced as the exhaust gas flow velocity increases, but when the absorbing liquid is sprayed on the high-speed exhaust gas flow, there is a problem that fine absorbing liquid mist is scattered and scattered in the wake of the flue.
【０００５】[0005]
【発明が解決しようとする課題】前述したように、湿式
石灰石−石膏法の脱硫方式を煙道で行う方式は、脱硫性
能を高めるために高速の排ガス流に吸収液を噴霧する
と、細かな吸収液ミストが飛散し、煙道の後流に飛散し
てくる問題がある。そこで、本発明の目的はできるだけ
吸収反応部をコンパクトにするために燃焼排ガスの流れ
を高速化し、しかも飛散ミストを捕集することができる
排煙脱硫装置を提供することである。As described above, the wet limestone-gypsum desulfurization method is performed by a flue, and if the absorbing solution is sprayed into a high-speed exhaust gas stream in order to enhance desulfurization performance, fine absorption is performed. There is a problem that liquid mist is scattered and scattered in the wake of the flue. Therefore, an object of the present invention is to provide a flue gas desulfurization device capable of accelerating the flow of combustion exhaust gas in order to make the absorption reaction part as compact as possible and collecting the scattered mist.
【０００６】[0006]
【課題を解決するための手段】本発明の前記目的は次の
構成によって達成される。すなわち、アルカリ金属化合
物の水スラリーからなる吸収液を燃焼装置から排出され
る燃焼排ガス煙道内に噴霧して燃焼排ガス中の硫黄酸化
物を除く排煙脱硫装置において、燃焼排ガス煙道内に該
煙道と略同一流路断面積を有し、吸収液スプレノズルを
設けた吸収反応部と、該吸収反応部の後流側に該飛散ミ
スト粗取部と、該飛散ミスト粗取部の後流側にミスト捕
集部を設け、さらに前記吸収液スプレノズルに吸収液を
供給するための吸収液タンクを設けた排煙脱硫装置であ
る。本発明の排煙脱硫装置において、飛散ミスト粗取部
の内部であって、飛散ミスト粗取部を構成する壁面の接
線方向に水を供給する構成とすること、また、吸収液タ
ンクには吸収反応部と飛散ミスト粗取部とで捕集された
吸収液の回収路を設けること、吸収液タンクには空気導
入用の配管を設けること、吸収反応部には、飛散ミスト
粗取部への飛散ミスト量を調整できる吸収液スプレノズ
ルの噴霧吸収液量制御手段を設けることなどの構成を採
用することができる。The above object of the present invention can be achieved by the following constitutions. That is, in the flue gas desulfurization device that removes the sulfur oxides in the flue gas by spraying an absorbing liquid consisting of a water slurry of an alkali metal compound into the flue gas flue gas discharged from the combustion device, And an absorption reaction part having an absorption liquid spray nozzle, a scattering mist rough collecting part on the downstream side of the absorption reaction part, and a scattering mist rough collecting part on the downstream side. It is a flue gas desulfurization apparatus provided with a mist collecting part and further with an absorbing liquid tank for supplying the absorbing liquid to the absorbing liquid spray nozzle. In the flue gas desulfurization apparatus of the present invention, the inside of the scattered mist rough collecting section is configured to supply water in the tangential direction of the wall surface forming the scattered mist rough collecting section, and the absorbing liquid tank absorbs the water. Provide a recovery passageway for the absorption liquid collected by the reaction section and the scattered mist rough collecting section, provide a pipe for introducing air in the absorbing solution tank, and connect the absorption reaction section to the scattered mist rough collecting section. It is possible to adopt a configuration such as providing a spray absorption liquid amount control means for the absorption liquid spray nozzle capable of adjusting the amount of scattered mist.
【０００７】また、本発明の前記目的は次の構成によっ
て達成される。すなわち、前記排煙脱硫装置に、さらに
その吸収反応部の前流側の煙道から直接ミスト捕集部後
流側の煙道に燃焼排ガスの一部を導く排ガス流路を設け
た排煙脱硫装置、または、カルシウム系化合物の微粉末
を燃焼装置の火炉内に噴霧し、さらにアルカリ金属化合
物の水スラリーからなる吸収液を燃焼装置から排出され
る燃焼排ガス煙道内に噴霧して燃焼排ガス中の硫黄酸化
物を除く排煙脱硫装置において、燃焼排ガス煙道内に該
煙道と略同一流路断面積を有し、吸収液スプレノズルを
設けた吸収反応部と、該吸収反応部の後流側に該飛散ミ
スト粗取部と、該飛散ミスト粗取部の後流側にミスト捕
集部を設け、さらに前記吸収液スプレノズルに吸収液を
供給するための吸収液タンクを設けた排煙脱硫装置であ
る。The above object of the present invention can be achieved by the following constitution. That is, the flue gas desulfurization device further comprises an exhaust gas passage for guiding a part of combustion exhaust gas from the flue gas upstream of the absorption reaction section to the flue gas downstream of the mist collecting section. Device, or fine powder of calcium-based compound is sprayed into the furnace of the combustion device, and the absorption liquid consisting of water slurry of alkali metal compound is further sprayed into the combustion exhaust gas flue discharged from the combustion device to In a flue gas desulfurization device excluding sulfur oxides, the flue gas flue gas has a flow passage cross-sectional area substantially the same as that of the flue gas, an absorption reaction section provided with an absorption liquid spray nozzle, and a wake side of the absorption reaction section. In the flue gas desulfurization device, the scattered mist rough collecting section, the mist collecting section is provided on the downstream side of the scattered mist rough collecting section, and the absorbing solution tank for supplying the absorbing solution to the absorbing solution spray nozzle is further provided. is there.
【０００８】[0008]
【作用】現在汎用されいる湿式排煙脱硫装置では、その
燃焼排ガス流速は吸収塔構造により異なるが、２から４
ｍ／ｓ近傍で運用している。そして、吸収液をスプレで
微粒化し、燃焼排ガスとの接触効率を高めて脱硫性能を
上げるには、吸収液滴径は４００から２０００ミクロン
に微粒化して噴霧される。燃焼排ガス流速を前述の数値
より高めると噴霧された微粒状の吸収液液滴の大部分は
後流側に飛散してくる。現在、脱硫用ミスト捕集器は種
々開発されてきているが、ミスト負荷量やガス流速に限
界があり、高ミスト負荷に対してはミスト捕集部の前段
に飛散ミストの粗取りを行うことが不可欠である。本発
明では積極的に飛散ミストを多くしてサイクロンなどの
飛散ミスト粗取部でのミストの粗取りと飛散ミスト粗取
部での脱硫性能を高めることで吸収反応部での脱硫と合
わせて全体の脱硫性能を高めている。In the currently widely used wet flue gas desulfurization equipment, the flue gas flow velocity varies from 2 to 4 depending on the structure of the absorption tower.
It operates near m / s. Then, in order to atomize the absorption liquid by spraying and improve the contact efficiency with the combustion exhaust gas to improve the desulfurization performance, the absorption droplet diameter is atomized from 400 to 2000 microns and sprayed. When the flue gas flow velocity is increased above the above-mentioned value, most of the sprayed fine droplets of the absorbing liquid are scattered to the wake side. Currently, various desulfurization mist collectors have been developed, but there is a limit to the amount of mist load and gas flow rate, and for high mist load, rough mist collection of scattered mist should be performed before the mist collector. Is essential. In the present invention, the amount of scattered mist is positively increased to increase the desulfurization performance in the rough mist collecting part and the scattered mist rough collecting part in the scattered mist rough collecting part, and the desulfurization in the absorption reaction part is combined with the whole. The desulfurization performance of is improved.
【０００９】燃焼の種類にもよって異なるが、石炭火力
などの燃焼排ガスには硫黄酸化物（主にＳＯ2ガス）が
３００から４０００ｐｐｍ含まれている。またボイラ内
で発生した窒素酸化物は２００から５００ｐｐｍ程度含
まれている。通常は窒素酸化物はアンモニアを還元剤と
して触媒上で窒素ガスに還元される。窒素酸化物を除去
した燃焼排ガスは次に電気集塵器に導入され、ばいじん
が除去されて脱硫装置に導入される。本発明の排煙脱硫
装置では燃焼排ガス流速を４から１０ｍ／ｓ近傍とする
ことができる。したがって、吸収反応部の容積は従来の
湿式排煙脱硫装置の１／２程度にコンパクト化できる。
燃焼排ガス流速が１０ｍ／ｓ近傍になると７００ミクロ
ン程度の吸収液の微粒子まで後流に飛散する。飛散した
ミストはサイクロンなどの飛散ミスト粗取部に導入さ
れ、特に飛散ミストの中でも大きな粒子が捕集される。
飛散ミスト粗取部で捕集されない微粒子はミスト捕集部
で捕集される。Although it depends on the type of combustion, the combustion exhaust gas from coal-fired power generation contains 300 to 4000 ppm of sulfur oxides (mainly SO 2 gas). In addition, the nitrogen oxides generated in the boiler are contained in an amount of about 200 to 500 ppm. Normally, nitrogen oxides are reduced to nitrogen gas on the catalyst using ammonia as a reducing agent. The combustion exhaust gas from which the nitrogen oxides have been removed is then introduced into the electrostatic precipitator, dust and soot are removed, and then introduced into the desulfurizer. In the flue gas desulfurization apparatus of the present invention, the combustion exhaust gas flow velocity can be set to about 4 to 10 m / s. Therefore, the volume of the absorption reaction section can be reduced to about half that of the conventional wet flue gas desulfurization apparatus.
When the flow rate of combustion exhaust gas is close to 10 m / s, even fine particles of the absorbing liquid of about 700 microns are scattered in the wake. The scattered mist is introduced into a scattered mist rough collecting section such as a cyclone, and particularly large particles are collected in the scattered mist.
Fine particles that are not collected by the scattered mist rough collecting section are collected by the mist collecting section.
【００１０】また、湿式石灰石−石膏法では特有の問題
がある。それは吸収液の一部が飛散ミスト粗取部の内壁
に付着し、石膏化することである。これを防止するには
飛散ミスト粗取部の内壁を常時洗浄することで解決でき
る。噴霧吸収液に吸収された硫黄酸化物の大部分は亜硫
酸カルシウムとして固定されるので吸収液タンク内に導
き、該タンクの液溜め部に空気をバブリングしながら導
入することにより亜硫酸カルシウムを化学的に安定な硫
酸カルシウム（石膏）に酸化して系外に抜き出すことが
できる。また、湿式石灰石−石膏法では吸収液の一部が
蒸発し、排ガスに同伴するので処理後の排ガスを再加熱
する必要がある。この再加熱をするために吸収反応部に
導入する直前の高温燃焼排ガスの一部をバイパスさせ、
脱硫処理後のガスと混合させることで、処理後の排ガス
用の加熱装置を新たに備える必要はない。The wet limestone-gypsum method has its own problems. That is, a part of the absorbing liquid adheres to the inner wall of the scattered mist rough collecting part and becomes gypsum. To prevent this, the inner wall of the scattered mist rough collecting part can be constantly cleaned. Most of the sulfur oxides absorbed in the sprayed absorbent are fixed as calcium sulfite, so they are introduced into the absorbent tank, and calcium sulfite is chemically introduced by introducing air into the liquid reservoir of the tank while bubbling. It can be oxidized to stable calcium sulfate (gypsum) and extracted from the system. Further, in the wet limestone-gypsum method, a part of the absorbing liquid evaporates and is entrained in the exhaust gas, so it is necessary to reheat the exhaust gas after treatment. In order to perform this reheating, a part of the high temperature combustion exhaust gas immediately before being introduced into the absorption reaction section is bypassed,
By mixing with the gas after the desulfurization treatment, it is not necessary to additionally provide a heating device for the exhaust gas after the treatment.
【００１１】[0011]
【実施例】まず、本発明の脱硫装置の構成の一実施例を
図１により説明する。図１においてボイラ１では石炭燃
料が燃焼される。燃焼排ガス２は脱硝装置３で窒素酸化
物が除去され、窒素酸化物が除去された燃焼排ガス４は
空気予熱器５に導かれ、熱回収の後、電気集塵器６に導
入される。電気集塵器６では大部分の粒子が除去され、
燃焼排ガス７は脱硫装置８に導入される。脱硫装置８で
は液溜めタンク９からのカルシウムあるいはマグネシウ
ムを含む化合物の水スラリーからなる吸収液１０をスプ
レノズル１１から噴霧する。脱硫装置８中では吸収液１
０は燃焼排ガスと微粒化状態で混合され、脱硫反応が行
われる。ここで、本実施例の脱硫装置８は、装置的に従
来の本格的な湿式排煙脱硫装置の吸収塔のようにスペー
スの大きい塔を用いる必要はなく、例えば図２に示すよ
うな煙道の排ガス流路断面積とほぼ同一の流路断面積を
有する装置である。なお、従来の本格的な湿式排煙脱硫
装置の吸収塔のようにスペースの大きい塔を用いること
が制限されることはない。DESCRIPTION OF THE PREFERRED EMBODIMENTS First, one embodiment of the structure of the desulfurization apparatus of the present invention will be described with reference to FIG. In FIG. 1, the boiler 1 burns coal fuel. Nitrogen oxides are removed from the combustion exhaust gas 2 by the denitration device 3, and the combustion exhaust gas 4 from which the nitrogen oxides are removed is guided to the air preheater 5 and, after recovering the heat, is introduced into the electrostatic precipitator 6. In the electrostatic precipitator 6, most particles are removed,
The combustion exhaust gas 7 is introduced into the desulfurization device 8. In the desulfurization device 8, the absorption liquid 10 composed of the water slurry of the compound containing calcium or magnesium from the liquid storage tank 9 is sprayed from the spray nozzle 11. Absorbing liquid 1 in desulfurizer 8
0 is mixed with combustion exhaust gas in the atomized state, and desulfurization reaction is performed. Here, the desulfurization apparatus 8 of the present embodiment does not need to use a tower having a large space as in the absorption tower of a conventional full-scale wet flue gas desulfurization apparatus, and for example, a flue shown in FIG. The device has a flow passage cross-sectional area that is substantially the same as the exhaust gas flow passage cross-sectional area. It should be noted that the use of a tower having a large space like the absorption tower of a conventional full-scale wet flue gas desulfurization apparatus is not limited.
【００１２】噴霧吸収液１０の一部は脱硫装置８から液
溜めタンク９に戻されるが、燃焼排ガスに同伴する吸収
液はサイクロン１３に導かれる。サイクロン１３では燃
焼排ガスに同伴してくる吸収液のミストの大部分を捕集
する。サイクロン１３には、その内壁を洗浄するために
補給水１５が供給される。サイクロン１３で捕集された
吸収液および補給水１５は液溜めタンク９に回収され
る。サイクロン１３の出口の燃焼排ガス１４はミスト捕
集器１６に導入され、ここで飛散ミストがさらに除去さ
れる。ミスト捕集器１６には洗浄を目的の補給水１５の
一部を供給する。処理された燃焼排ガス１７は脱硫装置
８の直前の煙道から脱硫装置８を迂回して供給される高
温の燃焼排ガス７と混合されて処理された燃焼排ガス１
７の温度を高め、煙突１８から大気に放出される。液溜
めタンク９には亜硫酸カルシウムを酸化するために空気
１８および石灰石２０を供給する。液溜めタンク９の吸
収液は脱硫装置８、サイクロン１３およびミスト捕集器
１６間を循環する。また、液溜めタンク９の吸収液の一
部が抜き出し液１９として抜き出され、遠心分離器２２
に供給され、ここで石膏２３を回収する。石膏を回収し
た上澄み液は液溜めタンク９に戻される。A part of the spray absorption liquid 10 is returned from the desulfurization device 8 to the liquid storage tank 9, but the absorption liquid entrained in the combustion exhaust gas is guided to the cyclone 13. The cyclone 13 collects most of the mist of the absorbing liquid that accompanies the combustion exhaust gas. Make-up water 15 is supplied to the cyclone 13 for cleaning the inner wall thereof. The absorbing liquid and makeup water 15 collected by the cyclone 13 are collected in the liquid storage tank 9. The combustion exhaust gas 14 at the exit of the cyclone 13 is introduced into the mist collector 16, where the scattered mist is further removed. A part of the makeup water 15 for cleaning is supplied to the mist collector 16. The treated flue gas 17 is mixed with the high temperature flue gas 7 supplied from the flue immediately before the desulfurization device 8 bypassing the desulfurization device 8 and treated.
The temperature of 7 is raised and released from the chimney 18 to the atmosphere. Air 18 and limestone 20 are supplied to the liquid storage tank 9 to oxidize calcium sulfite. The absorption liquid in the liquid storage tank 9 circulates between the desulfurization device 8, the cyclone 13 and the mist collector 16. Further, a part of the absorption liquid in the liquid storage tank 9 is extracted as the extraction liquid 19, and the centrifugal separator 22
And the gypsum 23 is collected here. The supernatant liquid from which the gypsum has been collected is returned to the liquid storage tank 9.
【００１３】図２は上記脱硫装置の詳細図を示す一例で
ある。電気集塵器６からの燃焼排ガス７は脱硫装置８に
導入される。脱硫装置８には液溜めタンク（図示せず）
から吸収液１０が供給され、スプレノズル１１から微粒
化状態で燃焼排ガス７中に噴霧される。燃焼排ガス７に
同伴する吸収液ミストはサイクロン１３に導入され、サ
イクロン１３の出口にはミスト捕集器１６を設置する。
サイクロン１３とミスト捕集器１６には洗浄を目的とす
る補給水（図示せず）を供給する。FIG. 2 is an example showing a detailed view of the desulfurization apparatus. The combustion exhaust gas 7 from the electrostatic precipitator 6 is introduced into the desulfurization device 8. The desulfurization device 8 has a liquid storage tank (not shown)
The absorbing liquid 10 is supplied from the spray nozzle 11 and is sprayed from the spray nozzle 11 into the combustion exhaust gas 7 in the atomized state. The absorbing liquid mist that accompanies the combustion exhaust gas 7 is introduced into the cyclone 13, and a mist collector 16 is installed at the outlet of the cyclone 13.
Make-up water (not shown) for cleaning is supplied to the cyclone 13 and the mist collector 16.
【００１４】図３には脱硫装置８での脱硫性能について
調べた結果の一例を示す。燃焼排ガス７を５ｍ／ｓの流
速で流しておき、この状態の燃焼排ガスに吸収液１０と
して石膏１５％、炭酸カルシウム２５ミリモル／リット
ルを含むスラリを噴霧したときの脱硫率を示す。燃焼排
ガス７中のＳＯ2濃度を５００、１０００、１５００ｐ
ｐｍに調製した。脱硫率は吸収液量Ｌ（リットル／時
間）と燃焼排ガス流量Ｇ（立方メートル／時間）の比を
Ｌ／Ｇとすると、Ｌ／Ｇを大きくすることにより脱硫率
を高めることができる。また、脱硫率は燃焼排ガス７中
のＳＯ2濃度が高くなると低下する傾向を示した。FIG. 3 shows an example of the results obtained by examining the desulfurization performance of the desulfurization unit 8. The desulfurization rate is shown when the combustion exhaust gas 7 was allowed to flow at a flow rate of 5 m / s and a slurry containing 15% of gypsum and 25 mmol / liter of calcium carbonate was sprayed as the absorption liquid 10 on the combustion exhaust gas in this state. SO 2 concentration in combustion exhaust gas 7 is 500, 1000, 1500 p
pm. The desulfurization rate can be increased by increasing L / G, where L / G is the ratio of the absorption liquid amount L (liter / hour) to the combustion exhaust gas flow rate G (cubic meter / hour). Further, the desulfurization rate tended to decrease as the SO 2 concentration in the combustion exhaust gas 7 increased.
【００１５】図４はサイクロン１３に飛散する吸収液ミ
スト量を測定した結果を示す一例である。サイクロン１
３への吸収液ミスト飛散量は燃焼排ガス７の流速を高め
ると急激に増加する傾向がある。またスプレノズル１１
から吸収液１０を燃焼排ガス７の流れと逆向きに噴霧す
ると、例えば燃焼排ガス７の流速が５ｍ／ｓの時、図４
の同一排ガス流速時の吸収液ミスト量の１／５に低減で
きた。FIG. 4 is an example showing the result of measuring the amount of the absorbing liquid mist scattered on the cyclone 13. Cyclone 1
The amount of the absorbed liquid mist scattered to 3 tends to increase sharply when the flow velocity of the combustion exhaust gas 7 is increased. Also spray nozzle 11
When the absorption liquid 10 is sprayed in the opposite direction to the flow of the combustion exhaust gas 7 from, for example, when the flow velocity of the combustion exhaust gas 7 is 5 m / s,
It was possible to reduce to 1/5 of the amount of mist of absorbing liquid at the same exhaust gas flow rate.
【００１６】図５にはサイクロン１３に飛散する吸収液
ミスト量とサイクロン１３での脱硫率の測定結果を示し
た。サイクロン１３に導入した燃焼排ガス７中のＳＯ2
濃度は１００ｐｐｍとした。脱硫率は吸収液ミスト量が
多くなるほど高くなる傾向がある。したがって、本発明
の脱硫装置８の構成を計画する際にはサイクロン１３へ
の吸収液ミスト飛散量を調整することで、脱硫率の調整
が可能と言える。FIG. 5 shows the measurement results of the amount of the absorbing liquid mist scattered on the cyclone 13 and the desulfurization rate of the cyclone 13. SO 2 in the combustion exhaust gas 7 introduced into the cyclone 13
The concentration was 100 ppm. The desulfurization rate tends to increase as the amount of mist of the absorbing solution increases. Therefore, it can be said that the desulfurization rate can be adjusted by adjusting the amount of the absorbed liquid mist scattered to the cyclone 13 when planning the configuration of the desulfurization device 8 of the present invention.
【００１７】本発明の上記図１または図２に示す実施例
を前述のボイラ１の火炉内に微粒石灰石を噴霧して脱硫
を行い、燃焼排ガスに同伴してくる未反応の生石灰の脱
硫活性を高めるために煙道に水を噴霧して調湿する脱硫
反応の組み合わせた乾式排煙脱硫装置と組み合わせても
良い。すなわち、排ガス煙道に水を噴霧する代わりに液
溜めタンク９から吸収液１０を噴霧し、さらにサイクロ
ン１３とミスト捕集器１６とを順次設ける装置である。
この方法によると、ボイラ１の火炉内に噴霧する微粒石
灰石量を低減することができる等の効果がある。The embodiment shown in FIG. 1 or FIG. 2 of the present invention is desulfurized by spraying fine limestone into the furnace of the boiler 1 described above, and the desulfurization activity of unreacted quicklime accompanying the combustion exhaust gas is measured. It may be combined with a dry flue gas desulfurization device in which a desulfurization reaction in which water is sprayed on the flue to control the humidity is combined in order to raise the temperature. That is, instead of spraying water on the exhaust gas flue, the absorption liquid 10 is sprayed from the liquid storage tank 9, and the cyclone 13 and the mist collector 16 are sequentially provided.
According to this method, it is possible to reduce the amount of fine limestone sprayed in the furnace of the boiler 1.
【００１８】[0018]
【発明の効果】本発明によれば、噴霧吸収液の飛散ミス
トの粗取りと脱硫性能を行った後にミストを捕集するこ
とで、燃焼排ガス流速を高めて脱硫性能を向上させ、し
かも脱硫装置本体のコンパクト化を行うにとができる。EFFECTS OF THE INVENTION According to the present invention, by roughly collecting scattered mist of spray absorbing liquid and performing desulfurization performance, the mist is collected to increase the flow rate of combustion exhaust gas and improve desulfurization performance, and moreover, the desulfurization apparatus. It is possible to make the body compact.
【図１】 本発明の一実施例の排煙脱硫装置の全体構成
図である。FIG. 1 is an overall configuration diagram of a flue gas desulfurization apparatus according to an embodiment of the present invention.
【図２】 本発明の一実施例の排煙脱硫装置の詳細図の
一例である。FIG. 2 is an example of a detailed view of a flue gas desulfurization apparatus according to an embodiment of the present invention.
【図３】 本発明の一実施例の吸収反応部での吸収液量
と燃焼排ガス流量の比と脱硫率との関係図である。FIG. 3 is a relationship diagram of a desulfurization rate and a ratio of an absorption liquid amount to a combustion exhaust gas flow rate in an absorption reaction section of an example of the present invention.
【図４】 本発明の一実施例の燃焼排ガス流速とサイク
ロンに飛散する吸収液ミスト量の関係図である。FIG. 4 is a diagram showing a relationship between a combustion exhaust gas flow rate and an amount of absorbing liquid mist scattered in a cyclone according to an embodiment of the present invention.
【図５】 本発明の一実施例のサイクロンでの吸収液ミ
スト量と脱硫率の関係図である。FIG. 5 is a diagram showing the relationship between the amount of absorbing liquid mist and the desulfurization rate in a cyclone according to an example of the present invention.
１…ボイラ、２…燃焼排ガス、３…脱硝装置、４、７、
１４…燃焼排ガス、５…空気予熱器、６…電気集塵器、
８…脱硫装置、９…液溜めタンク、１０…吸収液、１１
…スプレノズル、１３…サイクロン、１５…補給水、１
６…ミスト捕集器、１８…煙突、１９…抜き出し液、２
０…石灰石、２２…遠心分離器、２３…石膏1 ... Boiler, 2 ... Combustion exhaust gas, 3 ... Denitration device, 4, 7,
14 ... Combustion exhaust gas, 5 ... Air preheater, 6 ... Electrostatic precipitator,
8 ... Desulfurization device, 9 ... Liquid storage tank, 10 ... Absorption liquid, 11
… Spray nozzle, 13… Cyclone, 15… Makeup water, 1
6 ... Mist collector, 18 ... Chimney, 19 ... Extraction liquid, 2
0 ... Limestone, 22 ... Centrifuge, 23 ... Gypsum
───────────────────────────────────────────────────── 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 46/00 Ｅ 9441−4Ｄ 53/18 ＺＡＢ Ｅ 53/34 ＺＡＢ Ｆ２３Ｊ 15/00 Ｆ２３Ｊ 15/00 Ｂ (72)発明者 宮寺 博 茨城県日立市久慈町4026番地 株式会社日 立製作所日立研究所内 (72)発明者 野沢 滋 広島県呉市宝町６番９号 バブコック日立 株式会社呉工場内─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Internal reference number FI Technical display location B01D 46/00 E 9441-4D 53/18 ZAB E 53/34 ZAB F23J 15/00 F23J 15/00 B (72) Hiroshi Miyadera, 4026 Kuji Town, Hitachi City, Ibaraki Prefecture, Hitachi Research Laboratory, Hitachi, Ltd. (72) Shigeru Nozawa, 6-9 Takaracho, Kure City, Hiroshima Prefecture Babcock Hitachi Ltd., Kure Factory
Claims (7)
る吸収液を燃焼装置から排出される燃焼排ガス煙道内に
噴霧して燃焼排ガス中の硫黄酸化物を除く排煙脱硫装置
において、 燃焼排ガス煙道内に該煙道と略同一流路断面積を有し、
吸収液スプレノズルを設けた吸収反応部と、該吸収反応
部の後流側に該飛散ミスト粗取部と、該飛散ミスト粗取
部の後流側にミスト捕集部を設け、さらに前記吸収液ス
プレノズルに吸収液を供給するための吸収液タンクを設
けたことを特徴とする排煙脱硫装置。1. A flue gas desulfurization device for removing sulfur oxides in flue gas by spraying an absorbing liquid consisting of a water slurry of an alkali metal compound into the flue gas flue gas discharged from a combustion device. Has a flow passage cross-sectional area substantially the same as that of the flue,
An absorption reaction part provided with an absorption liquid spray nozzle, a scattered mist rough collecting part on the downstream side of the absorption reaction part, and a mist collecting part on the downstream side of the scattered mist rough collecting part, and the absorption liquid An flue gas desulfurization device, characterized in that an absorbing liquid tank for supplying the absorbing liquid to the spray nozzle is provided.
ミスト粗取部を構成する壁面の接線方向に水を供給する
構成としたことを特徴とする請求項１記載の排煙脱硫装
置。2. The flue gas desulfurization apparatus according to claim 1, wherein water is supplied inside the scattered mist rough collecting section in a tangential direction of a wall surface forming the scattered mist rough collecting section. .
ト粗取部とで捕集された吸収液の回収路を設けたことを
特徴とする請求項１記載の排煙脱硫装置。3. The flue gas desulfurization apparatus according to claim 1, wherein the absorbing liquid tank is provided with a recovery passage for the absorbing liquid collected by the absorbing reaction portion and the scattered mist rough collecting portion.
けたことを特徴とする請求項３記載の排煙脱硫装置。4. The flue gas desulfurization apparatus according to claim 3, wherein a pipe for introducing air is provided in the absorbent tank.
飛散ミスト量を調整できる吸収液スプレノズルの噴霧吸
収液量制御手段を設けたことを特徴とする請求項１記載
の排煙脱硫装置。5. The flue gas desulfurization according to claim 1, wherein the absorption reaction part is provided with a spray absorption liquid amount control means of an absorption liquid spray nozzle capable of adjusting the amount of scattered mist to the scattered mist rough collecting part. apparatus.
その吸収反応部の前流側の煙道から直接ミスト捕集部後
流側の煙道に燃焼排ガスの一部を導く排ガス流路を設け
ることを特徴とする排煙脱硫装置。6. The flue gas desulfurization apparatus according to claim 1, further comprising a flue gas flow for directing a part of the flue gas from the flue on the upstream side of the absorption reaction section to the flue on the downstream side of the mist collecting section. A flue gas desulfurization device characterized by providing a passage.
の火炉内に噴霧し、さらにアルカリ金属化合物の水スラ
リーからなる吸収液を燃焼装置から排出される燃焼排ガ
ス煙道内に噴霧して燃焼排ガス中の硫黄酸化物を除く排
煙脱硫装置において、 燃焼排ガス煙道内に該煙道と略同一流路断面積を有し、
吸収液スプレノズルを設けた吸収反応部と、該吸収反応
部の後流側に該飛散ミスト粗取部と、該飛散ミスト粗取
部の後流側にミスト捕集部を設け、さらに前記吸収液ス
プレノズルに吸収液を供給するための吸収液タンクを設
けたことを特徴とする排煙脱硫装置。7. A flue gas produced by spraying a fine powder of a calcium-based compound into a furnace of a combustion apparatus, and further spraying an absorption liquid consisting of an aqueous slurry of an alkali metal compound into a flue gas exhaust channel discharged from the combustion apparatus. In the flue gas desulfurization device excluding the sulfur oxides, the combustion exhaust gas flue has substantially the same flow passage cross-sectional area as the flue,
An absorption reaction part provided with an absorption liquid spray nozzle, a scattered mist rough collecting part on the downstream side of the absorption reaction part, and a mist collecting part on the downstream side of the scattered mist rough collecting part, and the absorption liquid An flue gas desulfurization device, characterized in that an absorbing liquid tank for supplying the absorbing liquid to the spray nozzle is provided.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6172758A JPH0833827A (en) | 1994-07-25 | 1994-07-25 | Flue gas desulfurizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6172758A JPH0833827A (en) | 1994-07-25 | 1994-07-25 | Flue gas desulfurizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0833827A true JPH0833827A (en) | 1996-02-06 |
Family
ID=15947790
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6172758A Pending JPH0833827A (en) | 1994-07-25 | 1994-07-25 | Flue gas desulfurizer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0833827A (en) |
-
1994
- 1994-07-25 JP JP6172758A patent/JPH0833827A/en active Pending
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