JPS60821A - Wet method for desulfurizing stack gas - Google Patents
Wet method for desulfurizing stack gasInfo
- Publication number
- JPS60821A JPS60821A JP58109251A JP10925183A JPS60821A JP S60821 A JPS60821 A JP S60821A JP 58109251 A JP58109251 A JP 58109251A JP 10925183 A JP10925183 A JP 10925183A JP S60821 A JPS60821 A JP S60821A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- slurry
- tower
- slaked lime
- supplied
- 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
Landscapes
- Treating Waste Gases (AREA)
- Removal Of Specific Substances (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、ボイラ排ガスなどの排ガス中のイオウ酸化物
を吸収Rすで吸収除去し、その吸収液を酸化、刺網した
のち固液分離して石こうを回収する湿式排煙脱硫方法に
関するものである。Detailed Description of the Invention The present invention is a wet method in which sulfur oxides in exhaust gas such as boiler exhaust gas are absorbed and removed by absorption R, and the absorbed liquid is oxidized and gill-netted, and then solid-liquid separation is performed to recover gypsum. The present invention relates to a flue gas desulfurization method.
湿式排煙脱硫方法は、排ガス中のダストヲ脱しん塔で除
去したのち、吸収塔内に導入し、そこで石灰などのスラ
リー吸収液と接触させて排ガス中のイオウ酸比物を除去
し、クリーンな排ガスとし、他方イオウ酸比物を吸収し
たスラリー吸収液は酸化塔内で酸比させ、そのば1ヒ後
のスラリー液をソツ、クナー等で濃縮し、さらにその濃
縮液を脱水機により固液分離して石ξうを回収するもの
である。この場合シックナーからの上澄液の一部はス・
ラリ−吸収液の母液として再循環し使用さ几るが、残9
の上澄液eま排水処理装置で排水処理さ九る。吸収塔内
ではスラリー吸収液のpf(が低いと亜硫酸水素カルシ
ウム〔Ca(H8O3)2〕ができ、こnが逆反応を伴
うことによって二酸化イオウ〔So2〕が発生するため
脱硫率が低下するので、スラリー吸収液は実用上pH5
,0以上を必要とし、またpH値が高6s@は炭酸カル
シウム[Ca CO3〕が残り、未反応となり、過剰の
Ca分が必要となり不利であるためPHは60以下好ま
しくは58以下にすることが望ましい。In the wet flue gas desulfurization method, the dust in the flue gas is removed in a desulfurization tower, and then introduced into an absorption tower, where it is brought into contact with a slurry absorbent such as lime to remove sulfuric acid compounds in the flue gas, producing a clean On the other hand, the slurry absorption liquid that has absorbed sulfuric acid compounds is acidified in an oxidation tower, and the slurry liquid after one oxidation is concentrated using a sotsu, kuna, etc., and then the concentrated liquid is converted into a solid liquid by a dehydrator. The stone is separated and collected. In this case, some of the supernatant liquid from the thickener is
The remaining 9
The supernatant liquid is then treated with wastewater treatment equipment. In the absorption tower, if the pf (pf) of the slurry absorption liquid is low, calcium hydrogen sulfite [Ca(H8O3)2] is formed, which causes a reverse reaction and generates sulfur dioxide [So2], which reduces the desulfurization rate. , the slurry absorption liquid has a practical pH of 5.
, 0 or more, and if the pH value is high at 6s @, calcium carbonate [Ca CO3] will remain unreacted and excessive Ca content will be required, which is disadvantageous, so the pH should be 60 or less, preferably 58 or less. is desirable.
このように吸収塔内でのスラリー吸収液のPH制御範囲
は5.0〜5.8と狭いが、酸化塔内では亜硫酸カルシ
ウム[Ca5Os〕を酸比し石こう(CaSO4,:l
とするためには、中間的VcCa (H8O3)2の存
在が必要となり、その結果pH値が低いほど酸化が早く
行なわ几るため、吸収塔内ではCa (H8O3)2が
生じやすいpH5,0近傍で運転するのが望ましい。In this way, the pH control range of the slurry absorption liquid in the absorption tower is narrow, 5.0 to 5.8, but in the oxidation tower, calcium sulfite [Ca5Os] is acidified and gypsum (CaSO4, :l
In order to achieve this, the presence of intermediate VcCa (H8O3)2 is required, and as a result, the lower the pH value, the faster the oxidation occurs, so Ca (H8O3)2 is likely to be generated in the absorption tower at around pH 5.0. It is preferable to drive with
しかしながら、排ガス中にはフッ素やフライアッシュ中
のアルミニュームなどの不純物が含まnており、吸収塔
内でpH5,0近傍で運転するとIR化塔を出たスラリ
ー液のp+Iは3.5以下となった場合、不純物は溶解
し、こ7tが7ツクナーの上澄液中にF−。However, the exhaust gas contains impurities such as fluorine and aluminum in fly ash, and if the absorption tower is operated at a pH of around 5.0, the p+I of the slurry liquid exiting the IR tower will be 3.5 or less. When the impurity is dissolved, this 7t is F- in the supernatant of the 7tschner.
At3”イオンとして存在する形となり、この上澄液を
母液として再び吸収塔に循環するとスラリー吸収液の活
性低下をきたし、吸収塔内でのPH制イ卸が困離となり
、かつ不純物イオンにより糸円か腐食さnやすい。At3'' ions exist in the form, and when this supernatant liquid is recycled to the absorption tower as a mother liquid, the activity of the slurry absorption liquid decreases, it becomes difficult to control the pH in the absorption tower, and the impurity ions cause threads. It is easy to corrode.
また上記不純物が溶存した上1ず液を排水処理装置へ或
は脱しん塔を通したのち排水処理装置へ供給すると、排
水処理でのF−処理が増大するといった問題がある。Furthermore, if the above-mentioned liquid containing the impurities dissolved therein is supplied to the wastewater treatment apparatus after passing through the wastewater treatment apparatus or after passing through a dehydrogenation tower, there is a problem that F-treatment in the wastewater treatment increases.
本発明の目的は湿式排煙脱硫装置の系内に捕促さ几てい
る不純物を除去し、系全体のPHの上昇を図ると共に吸
収塔のI)H値が45位迄低下しても脱硫装置の運転に
支障のない湿式排煙脱硫方法を提供しようとするもので
ある。The purpose of the present invention is to remove the impurities trapped in the system of the wet flue gas desulfurization equipment, to increase the pH of the entire system, and to improve the performance of the desulfurization equipment even when the I)H value of the absorption tower has decreased to about 45. The purpose is to provide a wet flue gas desulfurization method that does not interfere with the operation of the system.
本発明は、脱しん後の排ガス全吸収塔に誘引して排ガス
とスラリー吸収液とを接触させ、その接触後のスラリー
吸収液を酸比したのちシックナー等のml縮装置に供給
し、その濃縮装置の上澄it排水処理装置へ、またその
一部を吸収塔に供給する湿式排煙脱硫方法において、上
記濃縮装置の上澄液QPHを測定し、そのpH値に応じ
て濃縮装置の前に設けたラインミキザーで消石灰を消石
灰乳液として供給し、濃縮装置の上澄液中にF−At”
として溶解した不純物を消石灰によりCaF2゜At(
OH)3として沈でんさせ上置液から除去するようにし
たものである。In the present invention, the exhaust gas is brought into a total absorption tower after desulfurization, the exhaust gas is brought into contact with the slurry absorption liquid, and after the contact, the slurry absorption liquid is acid-ratioed and then supplied to a ml condensation device such as a thickener, and then concentrated. In a wet flue gas desulfurization method in which the supernatant liquid of the equipment is supplied to the wastewater treatment equipment and a part of it is supplied to the absorption tower, the supernatant liquid QPH of the concentrator is measured, and depending on the pH value, the supernatant liquid QPH of the concentrator is Slaked lime is supplied as a slaked lime emulsion using the installed line mixer, and F-At” is added to the supernatant liquid of the concentrator.
Impurities dissolved as CaF2゜At(
It is designed to be precipitated as OH)3 and removed from the supernatant liquid.
以下本発明に係る湿式排煙脱硫方法を実施するための装
置を示す添付図面に基づき、本発明の好適実施例を説明
する。DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of the present invention will be described below with reference to the accompanying drawings showing an apparatus for carrying out the wet flue gas desulfurization method according to the present invention.
ボイラ等からの排ガスは昇圧通風機1からガス−ガスヒ
ータ夕2を通り、脱じん塔3に導入される。Exhaust gas from a boiler or the like passes through a booster fan 1, a gas-gas heater 2, and is introduced into a dust removal tower 3.
脱しん塔3内では、脱じん塔3内のg、4をスプレーポ
ンプ5で吸引し、スプレー接合管6に取付けらnたスプ
レーノズルから液を噴射して排ガス中のダスト等全除去
する。数4は脱じん塔3からポンプ7により排水処理装
置8へ供給される。脱しん塔3を通った排ガスは、ダク
ト9より吸収塔10に導か九る。ここで吸収1li1o
を通過する排ガスは循環ポンプ12により吸収塔10下
部欣溜部から吸入ざ几て塔10の上部に設けた多数のス
プレー接合管13に取付けたスプレーノズルより噴射さ
nるスラリー吸収液11と接触しガス中の5o2−fス
ラリー吸収液11により吸収、除去さnる。噴射管13
の塔10上部にはミストエリミネータ14が設けらnl
ミストエリミネータ14で分離さ九たミスト分は原水
供給装置15又は母液タンク32からノぐイブ16全通
して供給さnる洗浄液によって洗浄さ几た液と共に塔1
0へ戻さnる。塔10の頂部には排気ダクト1γが設け
らn、ガス−ガスヒータ2を通って昇温さn煙突18よ
り排出さ九る。吸収塔10内のスラリー吸収液11はス
ラリーピット19よりポンプ20に介して塔10円に供
給さnる。スラリーピット19にはスラリー吸収液11
の吸収剤例えば炭酸カルシウムや消石灰などが吸収剤供
給装置21からホッパー22t−介してスラリーピント
19内に供給さ几る。In the dedusting tower 3, the dust in the dust removal tower 3 is sucked by a spray pump 5, and a liquid is injected from a spray nozzle attached to a spray joint pipe 6 to completely remove dust and the like from the exhaust gas. The number 4 is supplied from the dust removal tower 3 to the wastewater treatment device 8 by the pump 7. The exhaust gas that has passed through the desulfurization tower 3 is led to an absorption tower 10 through a duct 9. Absorption 1li1o here
The exhaust gas passing through is sucked from the lower part of the absorption tower 10 by a circulation pump 12 and comes into contact with the slurry absorption liquid 11 which is injected from spray nozzles attached to a number of spray joint pipes 13 provided at the upper part of the tower 10. The 5O2-F slurry in the gas is absorbed and removed by the absorption liquid 11. Injection pipe 13
A mist eliminator 14 is provided at the top of the tower 10.
The mist separated by the mist eliminator 14 is washed with a washing liquid supplied from the raw water supply device 15 or the mother liquor tank 32 through the nozzle 16, and then sent to the column 1.
Return to 0. An exhaust duct 1γ is provided at the top of the tower 10, and the gas is heated through the gas heater 2 and discharged from the chimney 18. The slurry absorption liquid 11 in the absorption tower 10 is supplied from the slurry pit 19 to the tower 10 through a pump 20. Slurry absorbing liquid 11 is placed in the slurry pit 19.
An absorbent such as calcium carbonate or slaked lime is supplied into the slurry pinto 19 from an absorbent supply device 21 via a hopper 22t.
吸収塔10円のスジ゛り1吸収液11はポンプ23によ
り酸化塔24に供給される。酸化塔24内には酸化塔出
口液のPH制御によ゛り硫酸供給装置25から硫酸が供
給さn、酸化塔24の下部からは空気供給装置26から
空気が供給さnる。酸化塔24に供給さnた空気は、吸
収塔10から供給されたスラリー吸収液と酸比反応し、
残ったガス分はノソイプ27全介してダクト9に流扛込
む。酸化塔24円で酸比された液はポンプ28により循
環され、パイプ29及びラインミキザー54を経てシッ
クナー等の濃縮装置30へ供給される。濃縮装置30で
オーバーフローした上澄液はiPイブ31よp母液タン
ク32に供給される。母液タンク32内の上置液はポン
プ33よりパイプ34′f:介して排水装置8へ、また
一部は母液としてパイプ35を介してスラリービット1
9及び吸収塔10に供給さnる。The absorption tower 10 stripes 1 and the absorption liquid 11 are supplied to the oxidation tower 24 by a pump 23. Sulfuric acid is supplied into the oxidation tower 24 from a sulfuric acid supply device 25 by controlling the pH of the oxidation tower outlet liquid, and air is supplied from the lower part of the oxidation tower 24 from an air supply device 26. The air supplied to the oxidation tower 24 undergoes an acid ratio reaction with the slurry absorption liquid supplied from the absorption tower 10,
The remaining gas flows into the duct 9 through the nosoip 27. The liquid acidified in the oxidation tower 24 is circulated by a pump 28, and is supplied to a concentrator 30 such as a thickener via a pipe 29 and a line mixer 54. The supernatant liquid overflowing from the concentrator 30 is supplied to the IP mother liquor tank 32 through the IP Eve 31 . The upper liquid in the mother liquid tank 32 is sent from the pump 33 to the draining device 8 via the pipe 34′f, and a part of it is transferred as the mother liquid to the slurry bit 1 via the pipe 35.
9 and absorption tower 10.
濃縮装置30の濃ki液はポンプ36より脱水機供給夕
/り31に供給さ几、供給タンク31からポンプ38に
より石こう脱水@39に供給さnlそこで遠心脱水さn
た固型分は、ベルトコンベア40より石こう貯蔵槽41
に導か几る。The concentrated liquid in the concentrator 30 is supplied from the pump 36 to the dehydrator supply tank 31, and then from the supply tank 31 to the gypsum dehydrator 39 by the pump 38, where it is centrifugally dehydrated.
The solid content is transferred from the belt conveyor 40 to the gypsum storage tank 41.
Guided to.
石こう脱水機39で脱水さ几た液分は排水ピット42v
こ供給さn1ポンプ43より濃縮装置30に戻さnる。The liquid dehydrated by the gypsum dehydrator 39 is drained into a drainage pit 42v.
This is supplied and returned to the concentrator 30 by the pump 43.
酸比塔出ロバイブ29に設けらnたラインミキサ54に
は強アルカリ性である消石灰を供給する消石灰供給装置
44が接続さ几る。この供給装置44は、濃縮装置30
からオーバフロー管31中の母液のpH′fr:測定す
るptl測定装置46のPH信号41に応じて消石灰乳
液をラインミキサ54に供給し酸化塔出口液と混合させ
た後濃縮装置30に入り母液タンク32の母g45のP
l値が7.0〜8.0の範囲になるよう制御している。A slaked lime supply device 44 that supplies slaked lime, which is strongly alkaline, is connected to the line mixer 54 provided in the acid ratio tower outlet vibe 29. This supply device 44 is the concentrator 30
pH'fr of the mother liquor in the overflow pipe 31: The slaked lime emulsion is supplied to the line mixer 54 according to the pH signal 41 of the PTL measuring device 46 to measure it, and after being mixed with the oxidation tower outlet liquid, it enters the concentrator 30 and is transferred to the mother liquor tank. Mother of 32 g45 P
The l value is controlled to be in the range of 7.0 to 8.0.
なお、脱しん塔3同には原水供給装置15より・ぐイブ
48を介して原水が、また母液タンク32からポンプ3
3、パイプ49′f:介して母液が夫々供給式れる。ま
た吸収塔10内のスラリー吸収液11は攪拌機53によ
り攪拌さnている。In addition, raw water is supplied to the desulfurization tower 3 from the raw water supply device 15 via the guide 48, and from the mother liquor tank 32 to the pump 3.
3. Pipe 49'f: mother liquor is supplied through each pipe. Further, the slurry absorption liquid 11 in the absorption tower 10 is stirred by a stirrer 53.
次に本発明の詳細な説明する。Next, the present invention will be explained in detail.
脱しん塔3金通って脱しんされた排ガスは吸収塔10内
に導かnそこで接合管13に数句けたスプレーノズルか
ら噴射さnるスラリー吸収液11と接触する。接触によ
って排ガス中のイオウ岐比物はスラリ吸−収液11に吸
収され、吸収塔10の上部からは脱硫さnた排ガスがダ
クト1γを介しガス−ガスヒータ2によって昇温さ汎て
煙突18より排気される。The exhaust gas that has been desulfurized through the desulfurization tower 3 is introduced into the absorption tower 10, where it comes into contact with the slurry absorption liquid 11 that is injected from several spray nozzles arranged in the joint pipe 13. Due to the contact, the sulfur compounds in the exhaust gas are absorbed by the slurry absorbing liquid 11, and the desulfurized exhaust gas from the upper part of the absorption tower 10 is heated by the gas-gas heater 2 through the duct 1γ, and then sent out from the chimney 18. Exhausted.
スラリー吸収液11に吸収された排ガス中のイオウ藪f
ヒ物はスラリー中のCa分と反応し亜硫酸カルシウムと
なって改比塔24に供給される。17比塔24内では酸
化塔24の下部から供給さnる空気によって次の反応が
行われる。Sulfur thicket f in exhaust gas absorbed by slurry absorption liquid 11
The arsenic reacts with the Ca content in the slurry to become calcium sulfite, which is supplied to the ratio reforming tower 24. In the 17 ratio column 24, the following reaction is carried out by air supplied from the lower part of the oxidation column 24.
またイオウ醒化物と反応しなかった未反応吸収剤分は硫
酸により石こう比さnる。In addition, the unreacted absorbent that did not react with the sulfurized product was mixed with gypsum using sulfuric acid.
上記反応によりば比塔24から排出さnるガスには少量
のSO2が含ま几るためパイプ2γにより再びダクト9
に供給する。According to the above reaction, the gas discharged from the ratio column 24 contains a small amount of SO2, so it is returned to the duct 9 via the pipe 2γ.
supply to.
酸化後のスラリーはパイプ29に取付けたラインミキサ
54を通り濃縮装置30に供給さ几、そこでd縮された
濃縮液は供給タンク37より石こう脱水機39により固
液分離さ九固型分は石こうとして貯蔵槽41に貯蔵さ汎
る。The slurry after oxidation is supplied to the concentrator 30 through the line mixer 54 attached to the pipe 29, where the condensed concentrate is separated into solid and liquid from the supply tank 37 by the gypsum dehydrator 39. It is stored in the storage tank 41 as a general purpose.
濃縮装置30の上澄液は母液タンク32に供給され、一
部は咳収塔1υのスラリー吸収液11の母液として、ま
た一部は脱しん塔3に供給され、その他の残りは排水処
理装置8へ供給さnる。この脱硫装置では原水供給装置
15から吸収塔1υに原水の一部が供給さ九るが、スラ
リー吸収液11の液分の大部分は母液タンク32内の母
液45を循環して使用するため、母液45中には排力゛
ス中の不純物でるるフッ素、アルミニューム等が混入し
、分離さ几ない丑ま蓄iされやすい。The supernatant liquid of the concentrator 30 is supplied to the mother liquor tank 32, a part of which is used as a mother liquor of the slurry absorption liquid 11 of the cough collection tower 1υ, a part of which is supplied to the desulfurization tower 3, and the remaining part is supplied to the wastewater treatment equipment. 8. In this desulfurization equipment, a part of the raw water is supplied from the raw water supply device 15 to the absorption tower 1υ, but most of the liquid content of the slurry absorption liquid 11 is used by circulating the mother liquor 45 in the mother liquor tank 32. Fluorine, aluminum, etc., which are impurities in the exhaust gas, are mixed into the mother liquor 45 and tend to accumulate without being separated.
上述したように吸収塔10内のスラリー吸収液11のp
l(値を5.0近傍で運転すると酸化塔24を通って酸
化さルた石こうスラ1)−WOPH値は35近傍迄下が
る傾向にあり上記7ノ累、アルミニューム等の溶解濃度
が増し、母液45中にAt”、F−として浴屏してしま
う。この母液45’ffニスラリ−ピット19及び吸収
q1o同に循環するとスラリー吸収液1′1の活性低下
をきたし、吸収塔10内でOPH値が下がってそのPl
−1値の制御が困離となる。As mentioned above, the p of the slurry absorption liquid 11 in the absorption tower 10
l (When the value is operated at around 5.0, the oxidized gypsum slurry 1 passed through the oxidation tower 24)-WOPH value tends to decrease to around 35, and the dissolved concentration of aluminum etc. in the above 7 cases increases, At'' and F- are absorbed into the mother liquor 45.If this mother liquor 45'ff is circulated through the slurry pit 19 and the absorber q1o, the activity of the slurry absorbent 1'1 will decrease, and OPH will be removed in the absorption tower 10. The value decreases and its Pl
It becomes difficult to control -1 values.
また排水処理装置8へ供給すると特に溶解したフッ素成
分の除去が困離となる。Furthermore, if the wastewater is supplied to the wastewater treatment device 8, it becomes particularly difficult to remove dissolved fluorine components.
従って濃縮装置3υJ:9オーバー乙ローする母液45
のPl値をPH測定装置46により測定し、そのPl値
に応じて消石灰乳液を消石灰供給装置44よシラインミ
キサ54を通じて濃縮装置30内に投入する。消石灰乳
液の投入により溶解したF−1At3+は次の反応によ
り固形物となり沈でんする。Therefore, the concentrator 3υJ: 9 over-low mother liquor 45
The Pl value of is measured by the PH measuring device 46, and the slaked lime emulsion is charged into the concentrating device 30 through the slaked lime supply device 44 and the sill line mixer 54 according to the Pl value. F-1At3+, which was dissolved by adding the slaked lime emulsion, becomes a solid and precipitates through the following reaction.
2F−十Ca2−* CaF、、↓
At + 30H−> A7(OH)34投入する消石
灰の量は濃縮装#30でオーバーフロー中の母液45の
pH値が7.0〜8.0となるよう適宜pH測定装置4
671>らpi信号41を消石灰供給装置44に伝え、
その信号により消石灰の供給量を制御する。2F-10Ca2-*CaF,, ↓ At + 30H-> A7(OH)34 The amount of slaked lime to be added is such that the pH value of the mother liquor 45 overflowing in concentrator #30 is 7.0 to 8.0. Appropriate pH measuring device 4
671> transmit the pi signal 41 to the slaked lime supply device 44,
The amount of slaked lime supplied is controlled by the signal.
濃縮装置30円に沈でんする不純物の量はごくわずかで
あ95石こう中に混入しても製品として全く支障がない
。The amount of impurities that settle in the 30 yen concentrator is extremely small, and even if they are mixed into 95 gypsum, there will be no problem with the product.
以上詳述したことから明らかなように本発明によ几は次
の如き優nた効果を発揮する。As is clear from the detailed description above, the present invention exhibits the following excellent effects.
(1) ラインミキサーによって消石灰を混合したf夜
を濃縮装置内に供給するので液中に溶解したアルミ、フ
ッ素等の不純物を除去できる。(1) Since the liquid mixed with slaked lime is fed into the concentrator using a line mixer, impurities such as aluminum and fluorine dissolved in the liquid can be removed.
(2)濃縮装置の上澄液のpHe測走し、そnに応じて
消石灰を投入するのでその上澄液のPHの制御ができ、
そnf:吸収塔に循環しても吸収塔内でのPH制御が容
易である。(2) The pH of the supernatant liquid of the concentrator is measured and slaked lime is added accordingly, so the pH of the supernatant liquid can be controlled.
Sonf: Even if it is circulated to the absorption tower, it is easy to control the pH within the absorption tower.
(3)不純物が除去さnた上澄液を排水処理装置に供給
するのでフッ素等の排水処理での負担が減少する。(3) Since the supernatant liquid from which impurities have been removed is supplied to the wastewater treatment equipment, the burden of wastewater treatment such as fluorine is reduced.
(4) 吸収塔内でpH値を50以下で運転してもライ
ンミキサーを経て濃縮装置に入った消石灰により、不純
物を除去した後の上澄液全母液として吸収塔に循環する
ので吸収塔内でのPI4制御の弾力的運転が行なえる、
(5)不純物全除去した母液全吸収塔に循環するのでス
ラリー吸収液の活性低下が生じない。(4) Even if the absorption tower is operated at a pH value of 50 or less, the slaked lime that enters the concentrator via the line mixer removes impurities and then circulates to the absorption tower as the entire supernatant mother liquor. (5) Since the mother liquor from which all impurities have been removed is circulated to the total absorption tower, no reduction in the activity of the slurry absorption liquid occurs.
(6) 吸収塔内でPl−15,0近傍あるいはこれ以
下で運転することができるため、は比処理が早く行なえ
る。(6) Since the absorption tower can be operated near or below Pl-15.0, the ratio treatment can be carried out quickly.
(7) 消石灰の投入により母液のpH値を上げること
ができるため装置の耐腐食性がよくなる。(7) By adding slaked lime, the pH value of the mother liquor can be increased, improving the corrosion resistance of the device.
添付図面は本発明を実施する装置の一例を示す図である
。
なお、図中3は脱しん塔、10は吸収塔、11はスラリ
ー吸収液、24は酸化塔、30は濃縮装置、32は母液
タンク、44は消石灰供給装置、46はpH測定装置、
54はラインミキサーである。
特許出願人 石川島播磨重工業株式会社代理人 弁理士
絹 谷 信 雄The accompanying drawings are diagrams showing an example of an apparatus for carrying out the present invention. In addition, in the figure, 3 is a desulfurization tower, 10 is an absorption tower, 11 is a slurry absorption liquid, 24 is an oxidation tower, 30 is a concentration device, 32 is a mother liquor tank, 44 is a slaked lime supply device, 46 is a pH measuring device,
54 is a line mixer. Patent applicant: Ishikawajima-Harima Heavy Industries Co., Ltd. Agent: Nobuo Kinuya, patent attorney
Claims (1)
接触させ、その接触後のスラリー吸収液ヲ酸化したのち
、ンツクナー等の濃縮装置に供給し、該濃縮装置の上澄
液の一部を上記吸収塔に循環する湿式排煙脱硫方法にお
いて、上記濃縮装置の上層液OPHを測定し、そのPI
J値に応じて消石灰を投入することを特徴とする湿式%
式%After desulfurization, all the exhaust gas is introduced into an absorption tower and brought into contact with the slurry absorption liquid, and after the contact, the slurry absorption liquid is oxidized, and then supplied to a concentration device such as a Ntukuner, and a part of the supernatant liquid of the concentration device is In a wet flue gas desulfurization method in which gas is circulated to the absorption tower, the upper layer liquid OPH of the concentration device is measured, and its PI
Wet type % characterized by adding slaked lime according to J value
formula%
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP58109251A JPS60821A (en) | 1983-06-20 | 1983-06-20 | Wet method for desulfurizing stack gas |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP58109251A JPS60821A (en) | 1983-06-20 | 1983-06-20 | Wet method for desulfurizing stack gas |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS60821A true JPS60821A (en) | 1985-01-05 |
Family
ID=14505438
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP58109251A Pending JPS60821A (en) | 1983-06-20 | 1983-06-20 | Wet method for desulfurizing stack gas |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS60821A (en) |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5314693A (en) * | 1976-07-28 | 1978-02-09 | Nippon Kokan Kk <Nkk> | Treating method for slurry in flue gas desulfurization process producing by-product gypsum |
-
1983
- 1983-06-20 JP JP58109251A patent/JPS60821A/en active Pending
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5314693A (en) * | 1976-07-28 | 1978-02-09 | Nippon Kokan Kk <Nkk> | Treating method for slurry in flue gas desulfurization process producing by-product gypsum |
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