JP2001038147A - Treatment of stack gas - Google Patents
Treatment of stack gasInfo
- Publication number
- JP2001038147A JP2001038147A JP11218396A JP21839699A JP2001038147A JP 2001038147 A JP2001038147 A JP 2001038147A JP 11218396 A JP11218396 A JP 11218396A JP 21839699 A JP21839699 A JP 21839699A JP 2001038147 A JP2001038147 A JP 2001038147A
- Authority
- JP
- Japan
- Prior art keywords
- oxidizing agent
- exhaust gas
- mist
- mercury
- desulfurization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、排煙処理方法、即
ち排煙処理システム内の水銀除去方法に関し、詳しく
は、膨大な排出量の排ガスを脱硫するシステムにおい
て、排ガス中から金属水銀蒸気を除去する方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flue gas treatment method, that is, a method for removing mercury in a flue gas treatment system. More specifically, in a system for desulfurizing an enormous amount of flue gas, metallic mercury vapor is removed from the flue gas. It relates to the method of removing.
【０００２】[0002]
【従来の技術】石炭や重質油焚き排ガス中には水銀等の
有害微量物質が存在しており、現状の排煙処理システム
においては除去が困難である。水銀は、主に排ガス中に
金属水銀（Ｈｇ）と塩化水銀（ＨｇＣｌ2）で存在する
と考えられている。ＨｇＣｌ2は、水に容易に吸収され
るため、脱硫吸収塔などで除去することができる。しか
し、Ｈｇは水への溶解度が極めて低いために、脱硫吸収
塔で吸収されず、金属水銀蒸気として、煙突より排出さ
れるおそれがある。現在、このように煙突より排出され
るおそれのあるＨｇについては、存在したとしても、そ
の量は微量であり、環境への影響は小さい。しかし、理
想的には、このようなおそれがないことが好ましい。2. Description of the Related Art Toxic trace substances such as mercury are present in coal or heavy oil-burning exhaust gas, and it is difficult to remove them with the current flue gas treatment system. Mercury is considered to exist mainly in exhaust gas as metallic mercury (Hg) and mercury chloride (HgCl 2 ). HgCl 2 is easily absorbed by water and can be removed by a desulfurization absorption tower or the like. However, since Hg has extremely low solubility in water, Hg is not absorbed in the desulfurization absorption tower, and may be discharged from the chimney as metal mercury vapor. At present, even if there is such Hg that may be discharged from the chimney, the amount thereof is very small, and the effect on the environment is small. However, ideally, it is preferable that there is no such a fear.
【０００３】そのため、Ｈｇ除去技術として、活性炭吸
着法や、次亜塩素酸ソーダ吸収法などが用いられてい
る。活性炭吸着法としては、排ガス中に活性炭粉末を吹
き込んでバグフィルターで回収する方法等が既に実用化
されている。しかし、主にゴミ焼却排ガスを対象とし
て、発電所排ガス等の大容量ガスに適した例はない。ま
た、次亜塩素酸ソーダ吸収法として、例えば、特開平１
０−２１６４７６号には、冷却塔の冷却水あるいは脱硫
吸収塔の吸収液、または、湿式電気集じん機の供給水あ
るいは循環水に、次亜塩素酸ソーダなどの添加剤を直接
添加する方法が記載されている。しかし、どの場合も、
排ガス処理プラントの主要機器に添加剤を加えるもので
あり、添加剤によって、その本質的な機能が阻害される
懸念がある。例えば、冷却塔は低ｐＨであることから酸
化剤が大量に必要になる、吸収塔では水銀以外の過酸化
物質が生成する、湿式電気集じん機では亜硫酸が酸化さ
れ酸性が強くなるなどが考えられる。また、主にゴミ焼
却排ガスを対象としており、発電所排ガス等の大容量ガ
スに適していない。[0003] Therefore, activated carbon adsorption, sodium hypochlorite absorption, and the like are used as Hg removal techniques. As the activated carbon adsorption method, a method of blowing activated carbon powder into exhaust gas and collecting the activated carbon powder with a bag filter has already been put to practical use. However, there is no example suitable for large-capacity gas such as power plant exhaust gas, mainly for waste incineration exhaust gas. As a sodium hypochlorite absorption method, for example,
No. 0-216476 discloses a method in which an additive such as sodium hypochlorite is directly added to cooling water of a cooling tower, absorption liquid of a desulfurization absorption tower, or feed water or circulating water of a wet-type electrostatic precipitator. Has been described. But in each case,
An additive is added to the main equipment of an exhaust gas treatment plant, and there is a concern that the additive may inhibit its essential function. For example, a cooling tower requires a large amount of an oxidizing agent because of its low pH, an absorption tower generates peroxides other than mercury, and a wet electric precipitator oxidizes sulfurous acid and increases acidity. Can be In addition, it mainly targets garbage incineration exhaust gas, and is not suitable for large-capacity gas such as power plant exhaust gas.
【０００４】[0004]
【発明が解決しようとする課題】そこで、本発明は、発
電所排ガス等の大容量ガスに含有する水銀、特に金属水
銀蒸気を除去することが可能な排煙処理システム内の水
銀除去方法を提供することを目的とする。SUMMARY OF THE INVENTION Therefore, the present invention provides a method for removing mercury contained in a large-capacity gas such as exhaust gas from a power plant, particularly a method for removing mercury in a flue gas treatment system capable of removing metallic mercury vapor. The purpose is to do.
【０００５】[0005]
【課題を解決するための手段】上記の目的を達成するた
めに、本発明の排煙処理システム内の水銀除去方法は、
水銀及び亜硫酸ガスを含む排ガスを脱硫吸収塔によって
脱硫処理した後、ミストエリミネータによって脱硫排ガ
スからミストを除去回収する排煙処理システムにおい
て、上記ミストエリミネータ上流で脱硫排ガス中に酸化
剤を供給することを特徴とする。ミストエリミネータ上
流で脱硫排ガス中に酸化剤を供給することにより、従来
の水銀除去方法に比べて酸化剤の供給量が１／１０から
１／２０で済み、また、他の機器類が酸化剤によって汚
染されずに、脱硫排ガス中から水銀を除去することがで
きる。In order to achieve the above object, a method for removing mercury in a flue gas treatment system according to the present invention comprises:
In a flue gas treatment system that removes and recovers mist from desulfurized exhaust gas using a mist eliminator after desulfurizing an exhaust gas containing mercury and sulfur dioxide gas using a desulfurization absorption tower, supplying an oxidizing agent to the desulfurized exhaust gas upstream of the mist eliminator. Features. By supplying the oxidizing agent to the desulfurization flue gas upstream of the mist eliminator, the amount of oxidizing agent to be supplied can be reduced to 1/10 to 1/20 of that of the conventional mercury removal method. Mercury can be removed from the desulfurization exhaust gas without being contaminated.
【０００６】上記ミストエリミネータとしては、垂直置
ミストエリミネータを用いることが好ましい。本発明で
は、上記ミストを除去回収した溶液に、上記酸化剤をさ
らに過剰添加し、酸化剤として循環使用することができ
る。また、本発明では、上記ミストを除去回収した溶液
に、上記酸化剤をさらに過剰添加し、その溶液の一部を
抜き出して、脱硫排水処理に用いることができる。上記
酸化剤は、上記脱硫排ガスの流れに対して並流または向
流に供給することができる。また、上記酸化剤を溶液に
して脱硫排ガス中に噴霧することによって、酸化剤を脱
硫排ガス中に供給することができる。It is preferable to use a vertical mist eliminator as the mist eliminator. In the present invention, the oxidizing agent can be further added to the solution from which the mist has been removed and recovered, and can be recycled as the oxidizing agent. Further, in the present invention, the oxidizing agent is further excessively added to the solution from which the mist has been removed and recovered, and a part of the solution is extracted to be used for desulfurization wastewater treatment. The oxidizing agent can be supplied cocurrently or countercurrently to the flow of the desulfurization exhaust gas. Further, the oxidizing agent can be supplied into the desulfurized exhaust gas by spraying the oxidant in a solution into the desulfurized exhaust gas.
【０００７】[0007]
【発明の実施の形態】図１は、本発明の排煙処理システ
ム内の水銀除去方法の実施の形態を説明する工程フロー
図である。図１に示すように、発電所から排出される大
容量の排ガス１は、集じん器２で脱塵処理された後、脱
硫吸収塔３に導入される。ここで、集じん器２は、排ガ
ス１を脱硫吸収塔３に導入する前に、排ガス１から粗集
じんできるものであればよく、特に限定されるものでは
ない。また、脱流吸収塔３は、一般に排煙処理で用いら
れている２塔式脱硫装置などでよく、特に限定されるも
のではない。脱硫吸収塔３内において、排ガス１は石灰
スラリー循環液などの吸収液と接触してＳＯｘが吸収、
除去される。また、排ガス１中に含まれる水銀のうち塩
化水銀（ＨｇＣｌ2）も上記吸収液に溶解、除去され
る。しかし、水銀のうち金属水銀（Ｈｇ）は、水への溶
解度が低いため、吸収液で除去されず、金属水銀蒸気と
して脱硫排ガスに含有し、脱硫吸収塔３を通過する。そ
して、Ｈｇ蒸気を含有した脱硫排ガスは、水平ダクト４
に導入される。FIG. 1 is a process flow chart illustrating an embodiment of a method for removing mercury in a flue gas treatment system of the present invention. As shown in FIG. 1, a large-capacity exhaust gas 1 discharged from a power plant is subjected to a dust removal treatment in a dust collector 2 and then introduced into a desulfurization absorption tower 3. Here, the dust collector 2 is not particularly limited as long as it can roughly collect dust from the exhaust gas 1 before introducing the exhaust gas 1 into the desulfurization absorption tower 3. Further, the outflow absorption tower 3 may be a two-tower type desulfurization apparatus generally used in flue gas treatment, and is not particularly limited. In the desulfurization absorption tower 3, the exhaust gas 1 comes into contact with an absorption liquid such as a lime slurry circulating liquid to absorb SOx.
Removed. In addition, mercury chloride (HgCl 2 ) among the mercury contained in the exhaust gas 1 is dissolved and removed in the absorbing solution. However, among mercury, metallic mercury (Hg) is not removed by the absorbing solution because of its low solubility in water, is contained in desulfurized exhaust gas as metallic mercury vapor, and passes through the desulfurizing absorption tower 3. The desulfurization exhaust gas containing Hg vapor is supplied to the horizontal duct 4
Will be introduced.
【０００８】水平ダクト４では、先ず、脱硫排ガス中
に、酸化剤１０を供給する。本発明で用いられる酸化剤
１０としては、例えば、次亜塩素酸ソーダ、塩素酸ソー
ダ、過マンガン酸カリウム、塩化銅、塩化マンガン、塩
化鉄、過酸化水素、キレート剤、活性炭、活性コーク
ス、イオウ、アルミナ、シリカ、珪酸アルミニウム、硫
化鉄、硫化鉛、塩化カルシウム、石炭灰などの１種また
は２種以上の混合物がある。最も好ましくは、次亜塩素
酸ソーダである。脱硫排ガスへの酸化剤供給方法は、脱
硫排ガスに酸化剤１０が十分行き渡るように供給される
方法であれば、特に限定されるものではない。例えば、
図１に示すように、上記酸化剤１０を溶液にし、ノズル
７等によって脱硫排ガスへ連続的に噴霧して供給する。
ノズル７の方向は特に限定されないが、排ガスの流れに
対して並流または向流に噴霧する。好ましくは、図１に
示すように、排ガスの流れに対して向流に噴霧する。噴
霧されることによって、脱硫排ガス中のＨｇは酸化さ
れ、ＨｇＣｌ2等の水に溶け易い形態となり、数百μｍ
粒径のミスト（液滴）が形成される。In the horizontal duct 4, first, the oxidizing agent 10 is supplied to the desulfurization exhaust gas. Examples of the oxidizing agent 10 used in the present invention include sodium hypochlorite, sodium chlorate, potassium permanganate, copper chloride, manganese chloride, iron chloride, hydrogen peroxide, chelating agent, activated carbon, activated coke, and sulfur. , Alumina, silica, aluminum silicate, iron sulfide, lead sulfide, calcium chloride, coal ash and the like. Most preferably, it is sodium hypochlorite. The method of supplying the oxidizing agent to the desulfurized exhaust gas is not particularly limited as long as the oxidizing agent 10 is supplied to the desulfurized exhaust gas so as to be sufficiently distributed. For example,
As shown in FIG. 1, the oxidizing agent 10 is made into a solution, and is continuously sprayed and supplied to the desulfurization exhaust gas by a nozzle 7 or the like.
Although the direction of the nozzle 7 is not particularly limited, the nozzle 7 is sprayed cocurrently or countercurrently to the flow of the exhaust gas. Preferably, as shown in FIG. 1, it sprays in a countercurrent to the flow of the exhaust gas. By being sprayed, Hg in the desulfurization exhaust gas is oxidized and becomes easily soluble in water such as HgCl 2.
A mist (droplets) having a particle size is formed.
【０００９】酸化剤１０の供給量は、Ｌ／Ｇ（単位：１
／ｈ）と表し、Ｌは酸化剤溶液の容積（単位：ｍ3）
を、Ｇは脱硫排ガスの流量（単位：ｍ3／ｈ）を表す。
上記酸化剤１０の供給量は、0.01〜1.0［１／ｈ］が好
ましく、0.01〜0.05［１／ｈ］がさらに好ましい。0.01
［１／ｈ］未満の場合、排ガスに酸化剤１０が十分に行
き渡らず、水銀除去率は低くなる。1.0［１／ｈ］を超
えると、供給量を増加しても水銀除去率の向上しなくな
るため、実用的でない。本発明によれば、酸化剤１０の
供給量は、吸収液に酸化剤を添加する従来の水銀除去方
法と比較して、約１／１０から１／２０で済み、コスト
や設備などの点で多くのメリットがある。The supply amount of the oxidizing agent 10 is L / G (unit: 1).
/ H), where L is the volume of the oxidizing agent solution (unit: m 3 )
And G represents the flow rate (unit: m 3 / h) of the desulfurization exhaust gas.
The supply amount of the oxidizing agent 10 is preferably 0.01 to 1.0 [1 / h], and more preferably 0.01 to 0.05 [1 / h]. 0.01
If it is less than [1 / h], the oxidizing agent 10 does not sufficiently spread to the exhaust gas, and the mercury removal rate is low. If it exceeds 1.0 [1 / h], the mercury removal rate will not be improved even if the supply amount is increased, which is not practical. According to the present invention, the supply amount of the oxidizing agent 10 is about 1/10 to 1/20 as compared with the conventional mercury removing method in which the oxidizing agent is added to the absorbing solution, and the cost and equipment are reduced. There are many benefits.
【００１０】酸化剤溶液の濃度は、0.001〜0.1ｍｏｌ／
リットルが好ましく、0.001〜0.02ｍｏｌ／リットルが
さらに好ましい。0.001ｍｏｌ／リットル未満の場合、
必要量の酸化剤を供給するためには、溶液の量が増加す
るため、効率的でない。0.1ｍｏｌ／リットルを超える
と、供給量を増加しても水銀除去率は向上しなくなるた
め、実用的でない。また、酸化剤溶液のｐＨは、5〜9が
好ましく、5〜7がさらに好ましい。ｐＨ5未満の場合、
酸性が強すぎて酸化剤が分解する恐れがあり、好ましく
ない。ｐＨ9を超えると、水銀除去率が低下するため好
ましくない。The concentration of the oxidizing agent solution is 0.001 to 0.1 mol /
Liter is preferable, and 0.001 to 0.02 mol / liter is more preferable. If less than 0.001 mol / liter,
It is not efficient to supply the required amount of oxidant because the amount of solution increases. If it exceeds 0.1 mol / liter, the mercury removal rate will not improve even if the supply amount is increased, so that it is not practical. Further, the pH of the oxidizing agent solution is preferably from 5 to 9, and more preferably from 5 to 7. If the pH is less than 5,
The acidity is so strong that the oxidizing agent may be decomposed, which is not preferable. If the pH exceeds 9, the mercury removal rate decreases, which is not preferable.
【００１１】噴霧されることによって、脱硫排ガス中の
Ｈｇは酸化され、ＨｇＣｌ2等の水に溶け易い形態とな
ると同時に、脱硫排ガス中に依然含有するＳＯ2も、酸
化剤１０によって酸化吸収される。このため、高度脱硫
が達成できるという利点がある。Ｈｇ及びＳＯ2は、噴
霧によって形成された数百μｍ粒径のミストに含有され
る。上記ミストは、水平ダクト４の高効率ミストエリミ
ネータ８によって脱硫排ガスから分離され、捕集され
る。ミストエリミネータ８は、くの字型に折れ曲がった
板が３０〜４５ｍｍ間隔で連続的に並んで設置されてお
り、その間隙を排ガス１が通過することによって、ミス
トが板に付着し、排ガスからミストを除去する。付着し
たミストは、板を伝わりながら下方に流れ、回収され
る。ミストエリミネータ８は、一般に、約１０〜２０μ
ｍ粒径のミストまで取り除くことができる高効率ミスト
エリミネータ８であれば、特に限定されるものではな
い。よって、Ｈｇ及びＳＯ2含有のミストは、数百μｍ
粒径であるため、ミストエリミネータ８によって確実に
捕集することができる。By spraying, Hg in the desulfurized exhaust gas is oxidized and becomes a form easily soluble in water such as HgCl 2 , and SO 2 still contained in the desulfurized exhaust gas is also oxidized and absorbed by the oxidizing agent 10. . For this reason, there is an advantage that advanced desulfurization can be achieved. Hg and SO 2 are contained in a mist with a particle size of several hundred μm formed by spraying. The mist is separated from the desulfurization exhaust gas by the high-efficiency mist eliminator 8 of the horizontal duct 4 and collected. The mist eliminator 8 is provided with plates bent in a U-shape and arranged continuously at intervals of 30 to 45 mm. When the exhaust gas 1 passes through the gap, the mist adheres to the plate, and the mist is removed from the exhaust gas. Is removed. The adhering mist flows downward along the plate and is collected. The mist eliminator 8 is generally about 10 to 20 μm.
There is no particular limitation as long as it is a high-efficiency mist eliminator 8 that can remove mist having an m particle size. Therefore, the mist containing Hg and SO 2 is several hundred μm
Because of the particle size, the mist can be reliably collected by the mist eliminator 8.
【００１２】また、ミストエリミネータ８の上流で酸化
剤１０を供給し、ミストエリミネータ８によって酸化剤
１０を確実に捕集できることから、ダクト４の上流に設
置された脱硫吸収塔３と下流に設置された熱交換器５
は、酸化剤１０によって汚染されることがない。よっ
て、その他機器の本来の機能を阻害する懸念がないとい
う利点がある。なお、図１に示すように、脱硫排ガスは
ダクト４内を水平方向に流れ、ミストエリミネータ８を
垂直に置く垂直置ミストエリミネータによって、ミスト
を捕集している。しかし、本発明は、上記垂直置ミスト
エリミネータに限定されるものではない。例えば、脱硫
吸収塔の上部にミストエリミネータが設置される場合、
脱硫排ガスはミストエリミネータ内を下から上へと流
れ、ミストエリミネータ８を水平もしくは斜めに傾けて
置くことによって、垂直置と同様に、ミストを捕集する
ことができる。ただし、脱硫吸収塔の上部にミストエリ
ミネータが設置された場合は、酸化剤１０をミストエリ
ミネータ８の上流で供給することによって、下部の脱硫
吸収塔に酸化剤１０が混入し、吸収液を汚染することが
考えられる。この場合、酸化剤１０の汚染防止をする設
備を別途設置する、または、吸収液に酸化剤１０が含ま
れていることに対応できる脱硫吸収塔にする必要があ
る。Further, since the oxidizing agent 10 is supplied upstream of the mist eliminator 8 and the oxidizing agent 10 can be reliably collected by the mist eliminator 8, the oxidizing agent 10 is installed downstream of the desulfurization absorption tower 3 installed upstream of the duct 4. Heat exchanger 5
Is not contaminated by the oxidizing agent 10. Therefore, there is an advantage that there is no concern that the original function of the device is obstructed. In addition, as shown in FIG. 1, the desulfurization exhaust gas flows in the duct 4 in the horizontal direction, and mist is collected by a vertical mist eliminator in which the mist eliminator 8 is placed vertically. However, the present invention is not limited to the vertical mist eliminator. For example, when a mist eliminator is installed at the top of the desulfurization absorption tower,
The desulfurization exhaust gas flows from the bottom to the top in the mist eliminator, and the mist can be collected by placing the mist eliminator 8 horizontally or obliquely in the same manner as in the vertical placement. However, when the mist eliminator is installed in the upper part of the desulfurization absorption tower, the oxidizer 10 is supplied to the upper part of the mist eliminator 8 so that the oxidizer 10 is mixed in the lower desulfurization absorption tower and contaminates the absorbent. It is possible. In this case, it is necessary to separately install a facility for preventing the oxidizing agent 10 from being contaminated, or to provide a desulfurization absorption tower capable of coping with the oxidizing agent 10 being contained in the absorbing solution.
【００１３】高効率ミストエリミネータ８によってＨｇ
が除去された排ガスは、再加熱器５に導入され、空気と
間接的に熱交換して空気を予熱するとともに、排ガスは
冷却され、煙突６から排出される。一方、捕集されたミ
ストは、酸化剤１０をさらに添加することによって補給
し、酸化剤含有溶液として再びノズル７へ循環し、脱硫
排ガスに噴霧することによって、循環利用することがで
きる。また、ノズル７へ循環する前に酸化剤含有溶液の
一部を抜き出して、排水処理設備９に送る。排水処理設
備９は、脱硫吸収塔３の脱硫排水を処理するためのもの
であり、酸化剤含有溶液は、脱硫排水のＣＯＤ処理用の
薬剤として再利用することができる。酸化剤含有溶液に
含まれるＨｇは、脱硫排水に含まれるＨｇと同様に、Ｈ
ｇＣｌ2で存在するため、脱硫排水のＨｇＣｌ2処理系を
使用することが可能である。よって、上記のように排水
処理設備９に送ることにより、処理設備を新設する必要
がないという利点がある。The high efficiency mist eliminator 8 allows Hg
The exhaust gas from which is removed is introduced into the reheater 5, indirectly exchanges heat with the air to preheat the air, and the exhaust gas is cooled and discharged from the chimney 6. On the other hand, the collected mist can be replenished by further adding the oxidizing agent 10, circulated again to the nozzle 7 as an oxidizing agent-containing solution, and sprayed on the desulfurization exhaust gas to be circulated and used. Before circulating to the nozzle 7, a part of the oxidant-containing solution is extracted and sent to the wastewater treatment facility 9. The wastewater treatment equipment 9 is for treating the desulfurization wastewater of the desulfurization absorption tower 3, and the oxidant-containing solution can be reused as a chemical for COD treatment of the desulfurization wastewater. Hg contained in the oxidizing agent-containing solution is H
Since it is present in gCl 2 , it is possible to use a HgCl 2 treatment system for desulfurization effluent. Therefore, there is an advantage that there is no need to newly install a treatment facility by sending the wastewater to the wastewater treatment facility 9 as described above.
【００１４】したがって、本発明の排煙処理システム内
の水銀除去方法によれば、ミストエリミネータの上流で
脱硫排ガス中に酸化剤を噴霧するという従来に比べて低
コストの設備によって、理想的な金属水銀蒸気の除去率
を達成することができる。また、金属水銀以外の有害微
量物質であっても、排ガス中に非溶解状態で含有し、酸
化されることによって溶解度が向上する物質（例えば、
ヒ素、セレン等）であれば、本発明によって、排ガス中
から除去することが可能である。Therefore, according to the method for removing mercury in a flue gas treatment system of the present invention, an ideal metal can be obtained by using a low-cost facility for spraying an oxidizing agent into a desulfurization exhaust gas upstream of a mist eliminator. Mercury vapor removal rates can be achieved. Also, even harmful trace substances other than metallic mercury are contained in the exhaust gas in a non-dissolved state, and substances whose solubility is improved by being oxidized (for example,
Arsenic, selenium, etc.) can be removed from the exhaust gas by the present invention.
【００１５】[0015]
【発明の効果】上記したように、本発明によれば、発電
所排ガス等の大容量ガスに含有する水銀、特に金属水銀
蒸気を除去することが可能な排煙処理システム内の水銀
除去方法が提供される。また、本発明によれば、脱硫吸
収塔や下流に設置された機器等が酸化剤によって汚染さ
れず、よって、その他機器の本来の機能を阻害する懸念
がないという利点がある。As described above, according to the present invention, a method for removing mercury in a flue gas treatment system capable of removing mercury contained in large-capacity gas such as power plant exhaust gas, particularly metal mercury vapor, is provided. Provided. Further, according to the present invention, there is an advantage that the desulfurization absorption tower, equipment installed downstream, and the like are not contaminated by the oxidizing agent, and therefore, there is no concern that the original function of the equipment is obstructed.
【図１】本発明の排煙処理システム内の水銀除去方法の
実施の形態を説明する工程フロー図である。FIG. 1 is a process flowchart illustrating an embodiment of a method for removing mercury in a flue gas treatment system of the present invention.
１ 排ガス ２ 集じん器 ３ 脱硫吸収塔 ４ ダクト ５ 再加熱器 ６ 煙突（スタック） ７ ノズル ８ ミストエリミネータ ９ 排水処理設備 １０ 酸化剤 Reference Signs List 1 exhaust gas 2 dust collector 3 desulfurization absorption tower 4 duct 5 reheater 6 chimney (stack) 7 nozzle 8 mist eliminator 9 wastewater treatment equipment 10 oxidizing agent
───────────────────────────────────────────────────── フロントページの続き (72)発明者 越智 英次 東京都千代田区丸の内二丁目５番１号 三 菱重工業株式会社内 Ｆターム(参考） 4D002 AA02 AA29 AC01 BA02 BA05 BA14 BA16 CA01 DA05 DA16 DA37 DA38 DA41 DA52 DA61 EA02 GA01 GA03 GB01 GB06 GB08 GB09 GB12 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Eiji Ochi 2-5-1, Marunouchi, Chiyoda-ku, Tokyo F-term (reference) 4D002 AA02 AA29 AC01 BA02 BA05 BA14 BA16 CA01 DA05 DA16 DA37 DA38 DA41 DA52 DA61 EA02 GA01 GA03 GB01 GB06 GB08 GB09 GB12
Claims (6)
吸収塔によって脱硫処理した後、ミストエリミネータに
よって脱硫排ガスからミストを除去回収する排煙処理シ
ステムにおいて、上記ミストエリミネータ上流で脱硫排
ガス中に酸化剤を供給することを特徴とする排煙処理シ
ステム内の水銀除去方法。1. A flue gas treatment system for desulfurizing an exhaust gas containing mercury and sulfur dioxide gas by a desulfurization absorption tower and then removing and collecting mist from the desulfurized exhaust gas by a mist eliminator, wherein an oxidizing agent is contained in the desulfurized exhaust gas upstream of the mist eliminator. A method for removing mercury in a flue gas treatment system.
トエリミネータであることを特徴とする請求項１記載の
排煙処理システム内の水銀除去方法。2. The method for removing mercury in a flue gas treatment system according to claim 1, wherein the mist eliminator is a vertical mist eliminator.
酸化剤をさらに過剰添加し、酸化剤として循環使用する
ことを特徴とする請求項１または２記載の排煙処理シス
テム内の水銀除去方法。3. The method for removing mercury in a flue gas treatment system according to claim 1, wherein the oxidizing agent is further excessively added to the solution from which the mist has been removed and recovered, and the oxidizing agent is recycled. .
酸化剤をさらに過剰添加し、その溶液の一部を抜き出し
て、脱硫排水処理に用いることを特徴とする請求項１〜
３のいずれかに記載の排煙処理システム内の水銀除去方
法。4. The method according to claim 1, wherein the oxidizing agent is further excessively added to the solution from which the mist has been removed and collected, and a part of the solution is extracted and used for desulfurization wastewater treatment.
3. The method for removing mercury in a flue gas treatment system according to any one of the above items 3.
対して並流または向流に供給することを特徴とする請求
項１〜４のいずれかに記載の排煙処理システム内の水銀
除去方法。5. The mercury removal in a flue gas treatment system according to claim 1, wherein the oxidizing agent is supplied in a cocurrent or countercurrent to the flow of the desulfurization exhaust gas. Method.
噴霧することによって、酸化剤を脱硫排ガス中に供給す
ることを特徴とする請求項１〜５のいずれかに記載の排
煙処理システム内の水銀除去方法。6. The flue gas treatment system according to claim 1, wherein the oxidizing agent is supplied into the desulfurizing exhaust gas by spraying the oxidizing agent into a solution into the desulfurizing exhaust gas. How to remove mercury from inside.
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|---|---|---|---|
| JP21839699A JP4146042B2 (en) | 1999-08-02 | 1999-08-02 | Flue gas treatment method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21839699A JP4146042B2 (en) | 1999-08-02 | 1999-08-02 | Flue gas treatment method |
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| Publication Number | Publication Date |
|---|---|
| JP2001038147A true JP2001038147A (en) | 2001-02-13 |
| JP4146042B2 JP4146042B2 (en) | 2008-09-03 |
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ID=16719263
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|---|---|---|---|
| JP21839699A Expired - Lifetime JP4146042B2 (en) | 1999-08-02 | 1999-08-02 | Flue gas treatment method |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007296469A (en) * | 2006-04-28 | 2007-11-15 | Central Res Inst Of Electric Power Ind | Mercury removing apparatus and method |
| JP2010269277A (en) * | 2009-05-25 | 2010-12-02 | Babcock Hitachi Kk | Method and apparatus of suppressing mercury re-release in desulfurization apparatus |
| JP2011140025A (en) * | 2011-04-04 | 2011-07-21 | Central Res Inst Of Electric Power Ind | Mercury removing apparatus and method |
| JP2011194286A (en) * | 2010-03-17 | 2011-10-06 | Babcock Hitachi Kk | Boiler plant |
| JP2012011317A (en) * | 2010-06-30 | 2012-01-19 | Mitsubishi Heavy Ind Ltd | System for treating mercury in exhaust gas |
| KR101254969B1 (en) | 2010-12-07 | 2013-04-17 | 재단법인 포항산업과학연구원 | Method for removing sulfur dioxide and elemental mercury from the flue gas |
| CN108939875A (en) * | 2018-09-29 | 2018-12-07 | 国电环境保护研究院 | A kind of device of coal-burning power plant's cooperation-removal heavy metal |
| CN112225239A (en) * | 2020-09-10 | 2021-01-15 | 河南华慧有色工程设计有限公司 | Method for producing and co-processing flue gas desulfurization waste liquid by sodium-alkali method through aluminum oxide |
-
1999
- 1999-08-02 JP JP21839699A patent/JP4146042B2/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007296469A (en) * | 2006-04-28 | 2007-11-15 | Central Res Inst Of Electric Power Ind | Mercury removing apparatus and method |
| JP2010269277A (en) * | 2009-05-25 | 2010-12-02 | Babcock Hitachi Kk | Method and apparatus of suppressing mercury re-release in desulfurization apparatus |
| JP2011194286A (en) * | 2010-03-17 | 2011-10-06 | Babcock Hitachi Kk | Boiler plant |
| JP2012011317A (en) * | 2010-06-30 | 2012-01-19 | Mitsubishi Heavy Ind Ltd | System for treating mercury in exhaust gas |
| KR101254969B1 (en) | 2010-12-07 | 2013-04-17 | 재단법인 포항산업과학연구원 | Method for removing sulfur dioxide and elemental mercury from the flue gas |
| JP2011140025A (en) * | 2011-04-04 | 2011-07-21 | Central Res Inst Of Electric Power Ind | Mercury removing apparatus and method |
| CN108939875A (en) * | 2018-09-29 | 2018-12-07 | 国电环境保护研究院 | A kind of device of coal-burning power plant's cooperation-removal heavy metal |
| CN112225239A (en) * | 2020-09-10 | 2021-01-15 | 河南华慧有色工程设计有限公司 | Method for producing and co-processing flue gas desulfurization waste liquid by sodium-alkali method through aluminum oxide |
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| Publication number | Publication date |
|---|---|
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