JPH02145885A - Method for preventing ash from clogging in soda recovering boiler and apparatus therefor - Google Patents
Method for preventing ash from clogging in soda recovering boiler and apparatus thereforInfo
- Publication number
- JPH02145885A JPH02145885A JP29635488A JP29635488A JPH02145885A JP H02145885 A JPH02145885 A JP H02145885A JP 29635488 A JP29635488 A JP 29635488A JP 29635488 A JP29635488 A JP 29635488A JP H02145885 A JPH02145885 A JP H02145885A
- Authority
- JP
- Japan
- Prior art keywords
- ash
- slurry
- stirring tank
- collected
- water
- 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
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 title claims description 12
- 239000002002 slurry Substances 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims description 26
- 238000011084 recovery Methods 0.000 claims description 13
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 238000010979 pH adjustment Methods 0.000 claims description 2
- 239000000428 dust Substances 0.000 abstract description 7
- 239000010446 mirabilite Substances 0.000 abstract description 2
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 239000012047 saturated solution Substances 0.000 abstract 1
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 abstract 1
- 238000002844 melting Methods 0.000 description 9
- 230000008018 melting Effects 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 239000013505 freshwater Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 208000005156 Dehydration Diseases 0.000 description 1
- 239000007832 Na2SO4 Substances 0.000 description 1
- 229920001131 Pulp (paper) Polymers 0.000 description 1
- 108091006587 SLC13A5 Proteins 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005496 eutectics Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 229910021473 hassium Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Incineration Of Waste (AREA)
- Paper (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は硫酸塩法によるケミカルパルプ製造時のソーダ
回収ボイラの灰詰シ防止方法及びその装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a method and apparatus for preventing ash clogging in a soda recovery boiler during the production of chemical pulp using the sulfate method.
従来、ソーダ回収ボイラ内に付着した灰を機械的に除去
する手段としてスーツプロワ−が設置されているが、こ
れまでに灰そのものの付着性を低減する方法及び装置は
なかった。Conventionally, a suit blower has been installed as a means for mechanically removing ash adhering to the inside of a soda recovery boiler, but there has been no method or device for reducing the adhesion of the ash itself.
ソーダ回収ボイラでは集塵機で捕集した灰を黒液に混合
し、再燃焼させて黒液からのソーダ分回収の効率を高め
ているが、ボイラの運転時間の経過と共に燃焼灰の付着
性が過速的に増加し、ボイラエレメントやバンクに厚く
つもり、腐食や灰詰シか発生した。In soda recovery boilers, the ash collected by the dust collector is mixed with the black liquor and re-burned to increase the efficiency of soda recovery from the black liquor. It increased rapidly and thickened the boiler elements and banks, causing corrosion and ash clogging.
灰中のに分と灰の融点の関係を第２図に示す。Figure 2 shows the relationship between the content of ash in the ash and the melting point of the ash.
灰の温度を上げてゆくとき、灰が一成分あるいは多成分
でも共融点（共晶点）Ｍｉ成ならば、融点は１つである
が、一般に多成分混合系の場合、溶融する温度幅が広が
る。第２図中の初期融点とは最初に液相が生じる温度、
溶融終了点とは半球状を示す温度を指す。この温度が低
い程、また幅が広い程付着し易いことを示す。When increasing the temperature of the ash, if the ash has a eutectic point (M) of one component or multiple components, it will have one melting point, but in general, in the case of a multi-component mixture, the melting temperature range is spread. The initial melting point in Figure 2 is the temperature at which a liquid phase first appears.
The melting end point refers to the temperature at which a hemispherical shape is exhibited. The lower the temperature and the wider the width, the easier it is to adhere.
灰を所定温度に上げた後、所定条件で空気によりブロー
するとき、吹飛べば×、吹飛ばなければ０（１０回テス
トの内１回でも）、吹飛びが中途半端なものがΔで示さ
れている。灰の付着性が強い程、×の範囲、すなわちＸ
Ｏの境界線が低温側、低圧側によって来る。この表示は
灰の付着性を評価する一つの方法として一般に採用され
ているものである。When the ash is blown to a specified temperature and then blown with air under specified conditions, if it is blown away, it is indicated by ×, if it is not blown off, it is 0 (even if it is only once out of 10 tests), and if it is not blown away, it is indicated by Δ. has been done. The stronger the adhesion of ash, the greater the range of
The boundary line of O comes from the low temperature side and the low pressure side. This display is generally adopted as a method for evaluating the adhesion of ash.
現状の対応策としては煤吹装置（スーツプロワ）を増強
（台数を増す又は、噴射蒸気圧力を増すなどの手段によ
り）しているがいずれも不経済でめった。Current countermeasures include increasing the number of soot blowers (by increasing the number of soot blowers or increasing the injection steam pressure), but both are uneconomical and have failed.
上記技術水準に鑑み、本発明はソーダ回収ボイラの灰詰
シを防止できる方法及びその装置を提供しようとするも
のでるる。In view of the above state of the art, the present invention seeks to provide a method and apparatus for preventing ash clogging in a soda recovery boiler.
本発明者らは鋭意研究、実験の結果、灰の付着性増加の
原因が、灰中に含ま゛れるに分が灰の再燃焼の循環過程
で増加し、これが灰の融点を下げて、灰の付着性を高め
ていることを確認し、その結果、灰のに分を除くことで
灰の付着性を下げる仁とができるとの知見を得た。As a result of intensive research and experiments, the present inventors found that the reason for the increased adhesion of ash is that the content of ash increases during the cycling process of ash re-burning, which lowers the melting point of ash and It was confirmed that the adhesion of the ash was increased, and as a result, they found that by removing the particulate matter from the ash, it was possible to create particles that lowered the adhesion of the ash.
本発明は上記知見に基づいて完成されたものでろって、
（１） ソーダ回収ボイラで燃焼排ガスから集塵した
灰を黒液に混合して循環再燃焼させて燃焼排ガス中に含
まれるンーダ分を回収する方法において、集塵した灰に
水又は温水を加えて混合し、濃度５〜２０チの灰スラリ
ーｔ−調製し、該灰スラリーを６０〜１００℃の温度に
調整した後、脱水して灰からに分を除去し、該に分を除
去した灰を黒液に混合することを特徴とするソーダ回収
ボイラの灰詰り防止方法及び
（２） 集塵した灰と水又は温水とを混合して灰スラ
リーを調製する第１攪拌タンク、該第１攪拌タンクと連
通し、かつ蒸気供給手段、ｐＨ調整手段を有する第２攪
拌タンク、該第２攪拌タンクから排出される灰スラリー
を脱水して灰分とＫＣｌ含有水とに分離する脱水機を具
備することを特徴とするソーダ回収ボイラの燃焼排ガス
から集塵した灰よｐＫ分を除去する装置
でるる。The present invention has been completed based on the above findings. (1) Ash collected from combustion exhaust gas in a soda recovery boiler is mixed with black liquor and recycled and re-burned to remove the powder contained in the combustion exhaust gas. In the method of collecting dust, water or warm water is added to the collected ash and mixed to prepare an ash slurry with a concentration of 5 to 20 degrees Celsius, and the ash slurry is adjusted to a temperature of 60 to 100 degrees Celsius, and then dehydrated. A method for preventing ash clogging in a soda recovery boiler, characterized by removing dust from the ash and mixing the ash from which the dust has been removed with black liquor, and (2) mixing the collected ash with water or hot water. a first stirring tank for preparing an ash slurry; a second stirring tank communicating with the first stirring tank and having a steam supply means and a pH adjusting means; a second stirring tank for dewatering the ash slurry discharged from the second stirring tank; This apparatus is equipped with a dehydrator that separates ash and KCl-containing water from ash and KCl-containing water.
灰の付着性を高めるに分の除去により、ソーダ回収ボイ
ラへの灰の付着が防止され、ボイラエレメントやバンク
の腐食、灰詰シが防止される。Removal of the amount that increases ash adhesion prevents ash from adhering to the soda recovery boiler, preventing corrosion of boiler elements and banks, and ash clogging.
以下、本発明の一態様を第１図によって説明する。Hereinafter, one embodiment of the present invention will be explained with reference to FIG.
図示省略の集塵装置で捕集された灰は、芒硝コンベヤ１
によって第１攪拌タンク２に供給される。第１攪拌タン
ク２には灰スラリーを調製するための清水３と適度な温
度に保つため加温用としての蒸気４が供給される。更に
充分均一な灰スラリーを調製するためアジテータ５が設
置されている。The ash collected by the dust collector (not shown) is transferred to the mirabilite conveyor 1.
is supplied to the first stirring tank 2 by. The first stirring tank 2 is supplied with fresh water 3 for preparing ash slurry and steam 4 for heating to maintain the temperature at an appropriate level. Furthermore, an agitator 5 is installed to prepare a sufficiently uniform ash slurry.
第１攪拌タンク２で調製された灰スラリーは、その上部
よジオ−バフローさせ、第２攪拌タンク６に導入される
。第２攪拌タンク６内の灰スラリーも濃度、温度調整の
ための清水５、蒸気４が投入される。この第２攪拌タン
ク６ではに＋。The ash slurry prepared in the first stirring tank 2 is geobuffered from the upper part thereof and introduced into the second stirring tank 6. Fresh water 5 and steam 4 are also added to the ash slurry in the second stirring tank 6 to adjust its concentration and temperature. In this second stirring tank 6, +.
Ｃｔ−を溶解を容易に行うためｐＩ（調整を行うもので
、例えばｐＨｍ整はＨ２ＳＯ，７の添加で行われる。蒸
気４はタンク６内温度を制御する九め、温度計１０と蒸
気量制御弁１１によシ調整される。なお、８はＨ２ＢＯ
３の移送ポンプ、９はＨ，３０４貯蔵タンクを示す。In order to easily dissolve Ct-, pI (adjustment is performed. For example, pH adjustment is performed by adding H2SO, 7. Steam 4 is used to control the temperature inside tank 6, thermometer 10 and steam amount control. It is adjusted by valve 11. Note that 8 is H2BO.
3 indicates a transfer pump, 9 indicates an H, 304 storage tank.
第２攪拌タンク６も第１攪拌タンク２同様に７ジテータ
１２′ｆｔ−設置し灰スラリーの均一化を促進し、かつ
沈降を防止すると共に、温度、濃度の均一性を維持する
ようになっている。第２攪拌タンク６の底部よシ灰スラ
リーとＫ”、 Ｃ１−は払出しポンプ１３によシ脱水機
１５に供給される。その際、一部の飽和液はサイクロン
１４にて捕集され攪拌タンク２へ戻される。脱水機１５
で灰スラリーから灰分とＫ”、 Ｃ１−を含む水が分離
され、灰分はケーキコンベア１６により図示省略のアッ
シュ混合タンクへ回収され、−方、脱水機１５からの水
は図示省略の廃液処理タンクへ回収される。Like the first stirring tank 2, the second stirring tank 6 is also equipped with seven 12'ft digitators to promote homogenization of the ash slurry, prevent sedimentation, and maintain uniformity in temperature and concentration. There is. The ash slurry and K", C1- from the bottom of the second stirring tank 6 are supplied to the dewatering machine 15 by the dispensing pump 13. At this time, a part of the saturated liquid is collected by the cyclone 14 and sent to the stirring tank. Returned to 2. Dehydrator 15
The ash content and water containing K" and C1- are separated from the ash slurry, and the ash content is collected by a cake conveyor 16 to an ash mixing tank (not shown). On the other hand, the water from the dehydrator 15 is sent to a waste liquid treatment tank (not shown). will be collected.
灰中からに分を最も効率的に分離するため、灰スラリー
の温度は６０〜１００℃程度、スラリー濃度は５〜’ｌ
Ｏｗｔチ、好ましくは１０〜１５ｗｔ％に調整し、か
つｐＨを適当に調整すべきである。灰スラリー温度を６
０℃〜１００℃に維持するのは、４０℃以下ではＮａ１
ＳＯ４・１０Ｈ，Ｏが析出し、水分を吸収するため、４
０℃を越える温度が必要でメク、又Ｋ”Ｃ１−も温度が
高い程溶解するので６０℃を下限とじ九。そして、灰ス
ラリーの温度が高いと腐蝕性が高まるので、装置の腐蝕
を避けるため１００℃を上限とした。In order to most efficiently separate the ash from the ash, the temperature of the ash slurry should be about 60 to 100℃, and the slurry concentration should be about 5 to 100℃.
It should be adjusted to 10 to 15 wt%, preferably 10 to 15 wt%, and the pH should be adjusted appropriately. Ash slurry temperature 6
Maintaining the temperature between 0°C and 100°C means that below 40°C, Na1
Because SO4・10H,O precipitates and absorbs moisture, 4
A temperature above 0°C is required, and the higher the temperature, the more K'C1- dissolves, so the lower limit is set at 60°C.The higher the temperature of the ash slurry, the more corrosive it becomes, so avoid corrosion of the equipment. Therefore, the upper limit was set at 100°C.
又、灰スラリ二の濃度はスラリーの操作性という点では
低濃度の方がよいが、脱水処理を行なう場合には一定度
灰分が含まれている方が効率的なため、５〜２０％の範
囲に設定するのが合目的である。In addition, a low concentration of ash slurry is better from the viewpoint of slurry operability, but when performing dehydration treatment, it is more efficient if it contains a certain amount of ash, so a concentration of 5 to 20% is better. It is useful to set it within a range.
第１攪拌槽の液面に電気集塵装置の捕集灰ＩＴ／ｈ ’
ｉｚコンベアから連続的に落下、供給する。The ash collected by the electrostatic precipitator on the liquid level of the first stirring tank IT/h'
Continuously falls and supplies from the iz conveyor.
同時に液面近傍を強力に攪拌し、液と捕集灰を混合、ス
ラリー化させる。攪拌部には、補給清水α５ Ｔ／ｈ及
び、後述するデカンタによりスラリーから分離した母液
の一部１１１５ Ｔ／ｈを供給して、スラリー化を充分
に行なわせる。この際、＠１攪拌槽は蒸気加熱によりス
ラリー温度を５０〜７０℃に保つようＫする。この状態
で、５〜４時間滞留させ、オーバー７０−するものを第
２攪拌槽に移し、と＼で４〜８時間、攪拌状態の中で滞
留させる。この際、スラリーのｐＨを検出し、アルカリ
性の場合には希硫酸溶液を薬注ポンプで供給し、ｐＨｔ
−中性付近に保つ。At the same time, the area near the liquid surface is strongly stirred to mix the liquid and collected ash and form a slurry. The stirring section is supplied with supplementary fresh water α5 T/h and 1115 T/h of a portion of the mother liquor separated from the slurry by a decanter, which will be described later, to ensure sufficient slurry formation. At this time, the @1 stirring tank is heated by steam to maintain the slurry temperature at 50 to 70°C. In this state, the mixture is allowed to stay for 5 to 4 hours, and the over 70% is transferred to the second stirring tank, where it is left in the stirring state for 4 to 8 hours. At this time, the pH of the slurry is detected, and if it is alkaline, a dilute sulfuric acid solution is supplied with a chemical dosing pump, and the pH
-Keep near neutrality.
第２攪拌槽の底部からスラリー液の一部約２Ｔ／ｈをポ
ンプで取出し、デカンタ−に送り、こ＼でスラリー中の
固形分を分離して、（Ｌ ９ Ｔ／ｈのスラッジと１、
Ｉ Ｔ／ｈの分離液を得た。分離液の１部α５ Ｔ／ｈ
は、前述の第１攪拌槽に循環し、ＣＬ ６ Ｔ／ｈ ｌ
ｄ、用水で稀釈後、工場内の排水処理装置に送られる。Approximately 2 T/h of the slurry liquid is taken out from the bottom of the second stirring tank by a pump and sent to a decanter, where the solid content in the slurry is separated and (L 9 T/h of sludge and 1,
A separated liquid of IT/h was obtained. 1 part of separated liquid α5 T/h
is circulated to the above-mentioned first stirring tank, and CL 6 T/h l
d. After diluting with water, it is sent to the wastewater treatment equipment in the factory.
（Ｌ ９ Ｔ／ｈ〕、’、 ７ ツジは０．８ Ｔ／ｈ
Ｏ固形分ト［１Ｌ１Ｔ／ｈの付着ａｔ含んでおり、付
着液中にカリ及び塩素が残存する。このスラッジ金コン
ベアにより、Ｎａ２８０４ミキシングタンクに戻される
。(L 9 T/h], ', 7 Tsuji is 0.8 T/h
It contains a solid content of 1L1T/h, and potassium and chlorine remain in the deposited liquid. This sludge gold conveyor returns it to the Na2804 mixing tank.
この例におけるＮａ２ＳＯ４回収率は、約８０％、カリ
ウム除去率は、約５０％、ＮａＣ２除去率は、約８０％
であった。In this example, the Na2SO4 recovery rate is approximately 80%, the potassium removal rate is approximately 50%, and the NaC2 removal rate is approximately 80%.
Met.
本発明方法及び装置により、ソーダ回収ボイラの灰中の
に分は徐々に長期運転中に低減し、ボイラの熱交換器（
バンク）部に付着し素灰の融点か上昇しボイラエレメン
トの腐食を防止しかつ、灰詰シを軽減する。灰融点が上
昇することによりボイラバンク上流側に灰付着領域が移
動するが、設計的にはその領域は火炉室上部となってお
シ融溶灰は自動的に炉底に落下する。By means of the method and apparatus of the present invention, the carbon content in the ash of a soda recovery boiler is gradually reduced during long-term operation, and the heat exchanger of the boiler (
The melting point of the base ash increases, preventing boiler element corrosion and reducing ash clogging. As the ash melting point rises, the ash adhesion area moves upstream of the boiler bank, but in terms of design, this area is the upper part of the furnace chamber, and the molten ash automatically falls to the bottom of the furnace.
第１図は本発明の一実施態様を説明するための概略図、
第２図は灰中のに分と灰の融点の関係を示す図表である
。FIG. 1 is a schematic diagram for explaining one embodiment of the present invention,
Figure 2 is a chart showing the relationship between the nitrogen content in the ash and the melting point of the ash.
Claims (2)
黒液に混合して循環再燃焼させて燃焼排ガス中に含まれ
るソーダ分を回収する方法において、集塵した灰に水又
は温水を加えて混合し、濃度５〜２０％の灰スラリーを
調製し、該灰スラリーを６０〜１００℃の温度に調整し
た、後、脱水して灰からに分を除去し、該に分を除去し
た灰を黒液に混合することを特徴とするソーダ回収ボイ
ラの灰詰り防止方法(1) In a method in which ash collected from combustion exhaust gas in a soda recovery boiler is mixed with black liquor and recycled and re-burned to recover the soda contained in the combustion exhaust gas, water or hot water is added to the collected ash. The ash slurry was mixed to prepare an ash slurry with a concentration of 5 to 20%, and the temperature of the ash slurry was adjusted to 60 to 100°C. After that, the ash was dehydrated to remove the ash, and the ash from which the ash was removed was A method for preventing ash clogging in a soda recovery boiler, characterized by mixing it with black liquor.
を調製する第１撹拌タンク、該第１攪拌タンクと連通し
、かつ蒸気供給手段、ｐＨ調整手段を有する第２撹拌タ
ンク、該第２撹拌タンクから排出される灰スラリーを脱
水して灰分とＫＣｌ含有水とに分離する脱水機を具備す
ることを特徴とするソーダ回収ボイラの燃焼排ガスから
集塵した灰よりＫ分を除去する装置(2) a first stirring tank for preparing ash slurry by mixing collected ash and water or warm water; a second stirring tank communicating with the first stirring tank and having a steam supply means and a pH adjustment means; Removing K from ash collected from combustion exhaust gas of a soda recovery boiler, characterized in that it is equipped with a dehydrator that dehydrates the ash slurry discharged from the second stirring tank and separates it into ash and KCl-containing water. equipment to
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29635488A JPH02145885A (en) | 1988-11-25 | 1988-11-25 | Method for preventing ash from clogging in soda recovering boiler and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29635488A JPH02145885A (en) | 1988-11-25 | 1988-11-25 | Method for preventing ash from clogging in soda recovering boiler and apparatus therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02145885A true JPH02145885A (en) | 1990-06-05 |
Family
ID=17832464
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP29635488A Pending JPH02145885A (en) | 1988-11-25 | 1988-11-25 | Method for preventing ash from clogging in soda recovering boiler and apparatus therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02145885A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0754799A2 (en) * | 1995-07-12 | 1997-01-22 | Eka Chemicals AB | Leaching process |
| AU691428B2 (en) * | 1995-07-07 | 1998-05-14 | Eka Chemicals Ab | A process for production of paper and a polymer mixture for use in the process |
| JP2015094042A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method of recovery boiler collected ash and processing device |
| JP2015093240A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method and processing unit for recovery boiler collection ash |
| JP2015093239A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method and processing unit for recovery boiler collection ash |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54115674A (en) * | 1978-03-01 | 1979-09-08 | Babcock Hitachi Kk | Desalting method for ash |
| JPS62177293A (en) * | 1986-01-24 | 1987-08-04 | タイオ−エンジニアリング株式会社 | Desalting method in kraft pulp chemicals recovery equipment |
-
1988
- 1988-11-25 JP JP29635488A patent/JPH02145885A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54115674A (en) * | 1978-03-01 | 1979-09-08 | Babcock Hitachi Kk | Desalting method for ash |
| JPS62177293A (en) * | 1986-01-24 | 1987-08-04 | タイオ−エンジニアリング株式会社 | Desalting method in kraft pulp chemicals recovery equipment |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU691428B2 (en) * | 1995-07-07 | 1998-05-14 | Eka Chemicals Ab | A process for production of paper and a polymer mixture for use in the process |
| EP0754799A2 (en) * | 1995-07-12 | 1997-01-22 | Eka Chemicals AB | Leaching process |
| EP0754799A3 (en) * | 1995-07-12 | 1997-03-26 | Eka Chemicals Ab | Leaching process |
| JP2015094042A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method of recovery boiler collected ash and processing device |
| JP2015093240A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method and processing unit for recovery boiler collection ash |
| JP2015093239A (en) * | 2013-11-12 | 2015-05-18 | 王子ホールディングス株式会社 | Processing method and processing unit for recovery boiler collection ash |
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