JPH0771617B2 - Control method of flue gas desulfurization equipment - Google Patents
Control method of flue gas desulfurization equipmentInfo
- Publication number
- JPH0771617B2 JPH0771617B2 JP62057653A JP5765387A JPH0771617B2 JP H0771617 B2 JPH0771617 B2 JP H0771617B2 JP 62057653 A JP62057653 A JP 62057653A JP 5765387 A JP5765387 A JP 5765387A JP H0771617 B2 JPH0771617 B2 JP H0771617B2
- Authority
- JP
- Japan
- Prior art keywords
- flue gas
- content
- stored
- gas desulfurization
- controlling
- 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 27
- 230000023556 desulfurization Effects 0.000 title claims description 27
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 17
- 239000003546 flue gas Substances 0.000 title claims description 17
- 238000000034 method Methods 0.000 title claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 17
- 239000002803 fossil fuel Substances 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000003245 coal Substances 0.000 description 22
- 239000002002 slurry Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 5
- 229910052731 fluorine Inorganic materials 0.000 description 4
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000011737 fluorine Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 229910004261 CaF 2 Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002516 radical scavenger Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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、石炭などを燃焼した排煙（排ガス）中の硫黄
酸化物等を吸収除去する湿式排煙脱硫装置の制御方法に
関するものである。Description: TECHNICAL FIELD The present invention relates to a method for controlling a wet flue gas desulfurization apparatus that absorbs and removes sulfur oxides and the like in flue gas (exhaust gas) that burns coal and the like. .
［従来の技術］ 石炭焚ボイラ等においては、燃焼排ガスによる公害防止
のために、硫黄酸化物（SOx）を除去するための脱硫装
置が設けられており、該脱硫装置には、脱硫を行う吸収
塔の上流側に湿式の脱じん塔が備えられて排ガスの脱じ
んが行われている。[Prior Art] In a coal-fired boiler or the like, a desulfurization device for removing sulfur oxides (SO x ) is provided to prevent pollution by combustion exhaust gas, and the desulfurization device performs desulfurization. A wet dedusting tower is provided on the upstream side of the absorption tower for dedusting exhaust gas.
しかし、上記公害の要因となる排ガス中の有害成分の量
は、炭種や産出地等によって大きく変化する。However, the amount of harmful components in the exhaust gas, which causes the pollution, greatly changes depending on the type of coal and the place of production.
このため、従来装置においては、脱硫装置における吸収
塔でのスラリー循環ポンプの運転台数を、硫黄Ｓ分が最
も多い石炭を燃焼した場合の石灰スラリーの供給量のと
きの最大運転台数に設定して循環を行うようにしてお
り、又脱じん塔への給水及びそこからの排水の量を、腐
食などの問題を生じる塩素Cl分の最も多い石炭を燃焼し
たときの排水中の塩素Cl分が所定値以下に希釈されるよ
うに最大量に設定し、更に排水中のフッ素Ｆ分を除去す
るために、フッ素Ｆ分の最も多い石炭を燃焼したときの
排水中のフッ素分を除去できる多目のＦ分除去剤（Ca
（OH）２）をＦ分除去タンクに供給するようにしてい
る。Therefore, in the conventional device, the operating number of slurry circulation pumps in the absorption tower of the desulfurization device is set to the maximum operating number of the lime slurry when the coal having the largest sulfur S content is burned. Circulation is performed, and the amount of water supplied to the dedusting tower and the amount of wastewater discharged from it are specified by the chlorine chloride content in the wastewater when coal with the highest chlorine content, which causes problems such as corrosion, is burned. The maximum amount is set so that it is diluted below the value, and in order to further remove the fluorine F content in the wastewater, it is possible to remove the fluorine content in the wastewater when burning coal with the largest amount of fluorine F content. F component remover (Ca
(OH) 2 ) is supplied to the F removal tank.
［発明が解決しようとする問題点］ しかし、上記従来装置においては、吸収塔及び脱じん塔
の運転制御を、有害な成分を最も多量に含んでいる石炭
の場合に合わせて高めに設定された設定値に基づいて行
うようにしているため、ポンプ等の運転費、水及びCa
（OH）２の消費量等の増加をまねき、運転コストが増大
する問題を有していた。[Problems to be Solved by the Invention] However, in the above-mentioned conventional apparatus, the operation control of the absorption tower and the dedusting tower is set to a high value in accordance with the case of coal containing the largest amount of harmful components. Since it is performed based on the set value, the operating cost of pumps, water and Ca
There has been a problem that the operating cost increases because of an increase in the consumption amount of (OH) 2 .
本発明は、上記従来の問題点に着目してなしたもので、
脱じん塔の排水量、Ｆ分除去タンクへのCa（OH）２の供
給量、及び吸収塔のスラリー循環ポンプの運転台数を、
化石燃料の成分に応じて許容最小限に押えることにより
運転費の低減を図ることを目的としている。The present invention was made by focusing on the above-mentioned conventional problems,
The amount of wastewater from the dedusting tower, the amount of Ca (OH) 2 supplied to the F removal tank, and the number of operating slurry circulation pumps in the absorption tower are
The objective is to reduce operating costs by controlling the amount of fossil fuels to an acceptable minimum.
［問題点を解決するための手段］ 本発明は、上記技術的課題を解決しようとしてなしたも
ので、化石燃料の燃焼排ガスを処理する湿式排煙脱硫装
置の制御方法において、化石燃料の成分分析を入荷時に
行い、その成分分析結果を記憶しておき、前記化石燃料
の使用時に、前記記憶しておいた成分分析結果のＳ分に
応じて吸収塔循環ポンプの運転台数を変更すると共に、
前記記憶しておいた成分分析結果のC1分に応じて排煙脱
硫装置からの排水量を制御することを特徴とする排煙脱
硫装置の制御方法、及び、化石燃料の燃焼排ガスを処理
する湿式排煙脱硫装置の制御方法において、化石燃料の
成分分析を入荷時に行い、その成分分析結果を記憶して
おき、前記化石燃料の使用時に、前記記憶しておいた成
分分析結果のＳ分に応じて吸収塔循環ポンプの運転台数
を変更すると共に、前記記憶しておいた成分分析結果の
Ｆ分に応じて排煙脱硫装置から排出される排水中のＦ分
を除去するためのＦ分除去剤の供給量を制御することを
特徴とする排煙脱硫装置の制御方法、に係るものであ
る。[Means for Solving Problems] The present invention has been made in order to solve the above technical problem, and in a method for controlling a wet flue gas desulfurization apparatus for treating combustion exhaust gas of fossil fuel, analysis of fossil fuel components. When the fossil fuel is used, the number of operating absorption tower circulation pumps is changed according to S of the stored component analysis result.
A method for controlling a flue gas desulfurization device, characterized by controlling the amount of waste water from the flue gas desulfurization device according to C1 minutes of the stored component analysis results, and a wet exhaust for treating combustion exhaust gas of fossil fuels. In the method of controlling a smoke desulfurization apparatus, a component analysis of fossil fuel is performed at the time of arrival, the result of the component analysis is stored, and when the fossil fuel is used, the result of the stored component analysis is determined according to the S component. In addition to changing the number of operating absorption tower circulation pumps, an F content removing agent for removing the F content in the wastewater discharged from the flue gas desulfurization apparatus according to the stored F content of the component analysis results The present invention relates to a method for controlling a flue gas desulfurization device, which is characterized by controlling a supply amount.
［作用］ 従って、本発明では、予め化石燃料をサンプリングして
得た検出成分データを制御装置に記憶させておき、その
成分データに基づいて、脱硫装置の排水量、Ｆ分除去タ
ンクへのＦ分除去剤の供給量、吸収塔のスラリー循環ポ
ンプの運転台数等を設定する。[Operation] Therefore, in the present invention, the detected component data obtained by sampling the fossil fuel in advance is stored in the control device, and the amount of waste water of the desulfurization device and the F component to the F component removal tank are stored based on the component data. Set the supply amount of scavenger and the number of operating slurry circulation pumps in the absorption tower.
［実 施 例］ 以下、本発明の実施例を図面を参照しつつ説明する。[Examples] Examples of the present invention will be described below with reference to the drawings.
第１図は本発明の方法を実施する装置の一例を示すもの
で、船１から荷揚げされた石炭2a,2b,2cを燃料としてボ
イラ３に供給して燃焼させ、そのときの排ガス４を、ガ
スエアーヒータ（熱交換器）５及び電気集じん器６を介
して脱硫装置７に導くようにしている。FIG. 1 shows an example of an apparatus for carrying out the method of the present invention, in which coal 2a, 2b, 2c unloaded from a ship 1 is supplied to a boiler 3 as fuel and burned, and an exhaust gas 4 at that time is discharged. A gas air heater (heat exchanger) 5 and an electric dust collector 6 are used to guide the gas to a desulfurizer 7.
上記において、石炭は同一の炭種でも産出地によって、
又同一の産出地においても産出場所によってその成分が
大きく変化するため、石炭を船１から荷揚げする度に微
量の石炭を成分検出計８によりサンプリングし、Ｓ分、
Cl分、Ｆ分、H2O分等を求める。In the above, coal is the same coal type, depending on the origin,
Further, even in the same production site, the composition greatly changes depending on the production site, so a small amount of coal is sampled by the composition detector 8 every time coal is unloaded from the ship 1, and the S component,
Calculate Cl, F, H 2 O, etc.
このとき、船１で運搬されて来る石炭は、バケット及び
コンベヤ等による搬送時に何回となく撹拌を繰返されて
いるために略均一成分となっている。しかし、正確な成
分を求めるには、数回のサンプリングを行ってその平均
値を求めることが好ましい。又、このサンプリング作業
は、石炭が陸揚げされてから燃料となるまでに数日の時
間があるので、その間に容易に実施できる。At this time, the coal carried by the ship 1 has a substantially uniform component because it is repeatedly stirred a number of times during transportation by a bucket, a conveyor, or the like. However, in order to obtain an accurate component, it is preferable to perform sampling several times and obtain the average value thereof. Further, this sampling work can be easily carried out during the period from the time when the coal is unloaded to the time when it becomes a fuel.
上記成分延在計８の検出成分データを制御装置９に入力
して記憶させ、更に複数の種類の石炭2a,2b,2cが混合さ
れて燃焼される場合には、その石炭の種類と混合割合を
制御装置９に入力し、該制御装置９による上記石炭の成
分値に基づいた制御信号10により前記脱硫装置７を制御
するよう構成する。When the detected component data of the component totalizer 8 is input to and stored in the control device 9, and when a plurality of types of coal 2a, 2b, 2c are mixed and burned, the type and mixing ratio of the coal Is inputted to the control device 9, and the desulfurization device 7 is controlled by the control signal 10 based on the component value of the coal by the control device 9.
前記脱硫装置７は、第２図に示す如く、排ガス４を順次
導くようにした脱じん塔11と吸収塔12を備えている。As shown in FIG. 2, the desulfurization device 7 includes a desulfurization tower 11 and an absorption tower 12 that sequentially guide the exhaust gas 4.
前記脱じん塔11は、給水弁13により水14が供給されてお
り、且つ水循環ポンプ15及びスプレーノズル15′により
上記水が循環されて排ガス４と接触することにより脱じ
んを行うようになっており、且つ上記脱じん塔11内の水
は、排水流量計16及び該排水量計16によって制御される
排水弁17を介してＦ分除去タンク18に供給され、該Ｆ分
除去タンク18に流量調節弁19を介して供給されるCa（O
H）220によってＦ分をCaF221として分離された後、排水
22されるようになっている。The dedusting tower 11 is supplied with water 14 by a water supply valve 13 and circulates the water by a water circulation pump 15 and a spray nozzle 15 ′ so as to come into contact with the exhaust gas 4 for dedusting. In addition, the water in the dedusting tower 11 is supplied to the F content removal tank 18 via the drainage flow meter 16 and the drain valve 17 controlled by the drainage meter 16, and the flow rate is adjusted to the F content removal tank 18. Ca (O supplied via valve 19
H) 2 20 separates F as CaF 2 21 and then drains
22.
又、前記吸収塔12には石炭スラリー（吸収剤）23が流量
調節弁24を介して供給され、且つ複数のスラリー循環ポ
ンプ25a,25b,25c及びスプレーノズル26a,26b,26cにより
上記スラリーが循環されて排ガス４と接触することによ
り脱硫を行うようになっており、更に前記吸収塔12内の
スラリーの一部が図示しない石膏工程に送られるように
なっている。Further, coal slurry (absorbent) 23 is supplied to the absorption tower 12 through a flow control valve 24, and the slurry is circulated by a plurality of slurry circulation pumps 25a, 25b, 25c and spray nozzles 26a, 26b, 26c. The desulfurization is performed by contacting the exhaust gas 4 and further, a part of the slurry in the absorption tower 12 is sent to a gypsum process (not shown).
上記において、吸収塔12のスラリー循環ポンプ25a,25b,
25cの駆動台数が制御装置９における燃料石炭のＳ分に
応じた制御信号10aにより制御され、又脱じん塔11の給
水弁13及び排水弁17が燃料石炭のCl分に応じた制御信号
10bによって制御され、更に、Ｆ分除去タンク18にCa（O
H）２を供給する流量調節弁19が燃料石炭のＦ分に応じ
た制御信号10cによって制御される。In the above, the slurry circulation pump 25a, 25b of the absorption tower 12,
The number of driven units 25c is controlled by a control signal 10a corresponding to the S content of the fuel coal in the control device 9, and the water supply valve 13 and the drainage valve 17 of the dedusting tower 11 are control signals corresponding to the Cl content of the fuel coal.
It is controlled by 10b, and Ca (O
The flow control valve 19 for supplying H) 2 is controlled by the control signal 10c corresponding to the F content of the fuel coal.
これにより、石炭の種類、性状に応じて、スラリー循環
ポンプ25a,25b,25cの運転台数を最小の運転台数とし、
且つ脱じん塔11で使用する水の量を最少必要量とし、更
にＦ分除去タンク18に供給するCa（OH）２の量を最少必
要量にすることができる。Thereby, the operating number of the slurry circulation pumps 25a, 25b, 25c is set to the minimum operating number according to the type and property of coal,
Moreover, the amount of water used in the dedusting tower 11 can be set to the minimum required amount, and further, the amount of Ca (OH) 2 supplied to the F content removal tank 18 can be set to the minimum required amount.
尚、本発明は上記実施例にのみ限定されるものではな
く、本発明の要旨を逸脱しない範囲内において種々変更
を加え得る。例えば、Ｆ除去用消石灰（Ca（OH）２）
は、これ以外の苛性ソーダ（NaOH）や水酸化マグネシウ
ム（Mg（OH）２）などのＦ分除去剤でもよい。またＳ分
に応じ循環ポンプ運転台数を変更することの他に吸収剤
供給量を変更してもよい。また石炭以外の石油、オイ
ル、コークス等の燃料の排ガスに適用できる。更に、吸
収塔が脱じん塔を兼ねた脱硫装置にも適用できる。It should be noted that the present invention is not limited to the above embodiments, and various changes can be made without departing from the scope of the present invention. For example, slaked lime for removing F (Ca (OH) 2 )
Other than this, an F content removing agent such as caustic soda (NaOH) or magnesium hydroxide (Mg (OH) 2 ) may be used. Further, the absorbent supply amount may be changed in addition to changing the number of operating circulation pumps in accordance with the S amount. Further, it can be applied to exhaust gas of fuels other than coal, such as petroleum, oil and coke. Further, it can be applied to a desulfurization device in which the absorption tower also serves as a dedusting tower.
［発明の効果］ 上記したように、本発明の排煙脱硫装置の制御方法によ
れば、入荷時に分析を行って記憶しておいた化石燃料の
分析結果のＳ分により吸収塔循環ポンプの運転台数を最
小限に制御すると同時に、前記記憶しておいた分析結果
のCl分により排煙脱硫装置からの排水量を許容最小限に
押えることによって、運転費の大幅低減を図ることがで
きる優れた効果を奏し得る。[Effects of the Invention] As described above, according to the control method of the flue gas desulfurization apparatus of the present invention, the absorption tower circulation pump is operated by the S content of the analysis result of fossil fuel which is analyzed and stored at the time of receipt. An excellent effect that the operating cost can be greatly reduced by controlling the number of units to the minimum and suppressing the amount of wastewater discharged from the flue gas desulfurization unit to the permissible minimum by the Cl content of the stored analysis result. Can play.
また、入荷時に分析を行って記憶しておいた化石燃料の
分析の結果のＳ分により吸収塔循環ポンプの運転台数を
最小限に制御すると同時に、前記記憶しておいた分析結
果のＦ分によりＦ分除去タンクへのＦ分除去剤の供給量
を許容最小限に押えることによって、運転費の大幅低減
を図ることができる優れた効果を奏し得る。Further, the number of operating absorption tower circulation pumps is controlled to the minimum by the S content of the fossil fuel analysis result stored and analyzed at the time of arrival, and at the same time, the F content of the stored analysis result is used. By suppressing the supply amount of the F-content removing agent to the F-content removing tank to an allowable minimum, it is possible to achieve an excellent effect that the operating cost can be significantly reduced.
第１図は本発明の基本原理を示す全体説明図、第２図は
第１図の排煙脱硫装置の詳細を示す説明図である。 １は船、2a,2b,2cは石炭、３はボイラ、４は排ガス、７
は脱硫装置、８は成分検出計、９は制御装置、10a,10b,
10cは制御信号、11は脱じん塔、12は吸収塔、13は給水
弁、14は水、16は排水流量計、17は排水弁、18はＦ分除
去タンク、19は流量調節弁、20はCa（OH）２、23は石灰
スラリー、24は流量調節弁、25はスラリー循環ポンプ、
26はスプレーノズルを示す。FIG. 1 is an overall explanatory view showing the basic principle of the present invention, and FIG. 2 is an explanatory view showing details of the flue gas desulfurization apparatus of FIG. 1 is a ship, 2a, 2b, 2c is coal, 3 is a boiler, 4 is exhaust gas, 7
Is a desulfurizer, 8 is a component detector, 9 is a controller, 10a, 10b,
10c is a control signal, 11 is a dedusting tower, 12 is an absorption tower, 13 is a water supply valve, 14 is water, 16 is a drainage flow meter, 17 is a drainage valve, 18 is a F removal tank, 19 is a flow control valve, 20 Is Ca (OH) 2 , 23 is lime slurry, 24 is a flow control valve, 25 is a slurry circulation pump,
26 indicates a spray nozzle.
───────────────────────────────────────────────────── 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 53/34 ＺＡＢ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Office reference number FI technical display location B01D 53/34 ZAB
Claims (2)
脱硫装置の制御方法において、化石燃料の成分分析を入
荷時に行い、その成分分析結果を記憶しておき、前記化
石燃料の使用時に、前記記憶しておいた成分分析結果の
Ｓ分に応じて吸収塔循環ポンプの運転台数を変更すると
共に、前記記憶しておいた成分分析結果のC1分に応じて
排煙脱硫装置からの排水量を制御することを特徴とする
排煙脱硫装置の制御方法。1. A method of controlling a wet flue gas desulfurization apparatus for treating combustion exhaust gas of fossil fuel, wherein the composition analysis of fossil fuel is carried out at the time of arrival, the result of the composition analysis is stored, and when the fossil fuel is used, The number of operating absorption tower circulation pumps is changed according to the stored S component analysis result, and the amount of waste water discharged from the flue gas desulfurization device is changed according to the stored C component analysis result. A method for controlling a flue gas desulfurization device, characterized by controlling.
脱硫装置の制御方法において、化石燃料の成分分析を入
荷時に行い、その成分分析結果を記憶しておき、前記化
石燃料の使用時に、前記記憶しておいた成分分析結果の
Ｓ分に応じて吸収塔循環ポンプの運転台数を変更すると
共に、前記記憶しておいた成分分析結果のＦ分に応じて
排煙脱硫装置から排出される排水中のＦ分を除去するた
めのＦ分除去剤の供給量を制御することを特徴とする排
煙脱硫装置の制御方法。2. A method of controlling a wet flue gas desulfurization apparatus for treating combustion exhaust gas of fossil fuel, wherein the composition analysis of fossil fuel is carried out at the time of arrival, the result of the composition analysis is stored, and when the fossil fuel is used, The number of operating absorption tower circulation pumps is changed according to the stored S content of the component analysis result, and the exhaust gas is discharged from the flue gas desulfurization apparatus according to the stored F content of the component analysis result. A method for controlling a flue gas desulfurization apparatus, which comprises controlling the supply amount of an F-content removing agent for removing F-content in waste water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62057653A JPH0771617B2 (en) | 1987-03-12 | 1987-03-12 | Control method of flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62057653A JPH0771617B2 (en) | 1987-03-12 | 1987-03-12 | Control method of flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63224719A JPS63224719A (en) | 1988-09-19 |
| JPH0771617B2 true JPH0771617B2 (en) | 1995-08-02 |
Family
ID=13061864
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62057653A Expired - Lifetime JPH0771617B2 (en) | 1987-03-12 | 1987-03-12 | Control method of flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0771617B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2740970B2 (en) * | 1989-10-05 | 1998-04-15 | 株式会社日立製作所 | Operating method of coal boiler |
| JP4701825B2 (en) * | 2005-05-12 | 2011-06-15 | 株式会社日立製作所 | Exhaust gas treatment agent supply system and supply method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60110321A (en) * | 1983-11-18 | 1985-06-15 | Mitsubishi Heavy Ind Ltd | Control of exhaust gas desulfurizing plant |
-
1987
- 1987-03-12 JP JP62057653A patent/JPH0771617B2/en not_active Expired - Lifetime
Non-Patent Citations (1)
| Title |
|---|
| 緒方雅彦他著「重油・排煙脱硫技術」日刊工業新聞社Ｐ．１２３−１２４（昭４６．４．１５） |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS63224719A (en) | 1988-09-19 |
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