JPS5910327A - Method for removing ammonia from fly ash by rinsing method - Google Patents
Method for removing ammonia from fly ash by rinsing methodInfo
- Publication number
- JPS5910327A JPS5910327A JP57118183A JP11818382A JPS5910327A JP S5910327 A JPS5910327 A JP S5910327A JP 57118183 A JP57118183 A JP 57118183A JP 11818382 A JP11818382 A JP 11818382A JP S5910327 A JPS5910327 A JP S5910327A
- Authority
- JP
- Japan
- Prior art keywords
- fly ash
- gas
- ammonia
- water
- slurry
- 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
- 239000010881 fly ash Substances 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims description 74
- 229910021529 ammonia Inorganic materials 0.000 title claims description 31
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 31
- 230000023556 desulfurization Effects 0.000 claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000002002 slurry Substances 0.000 claims abstract description 17
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 8
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims abstract description 5
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 40
- 239000002699 waste material Substances 0.000 abstract description 8
- 239000000428 dust Substances 0.000 abstract description 4
- 239000002912 waste gas Substances 0.000 abstract description 3
- 239000002956 ash Substances 0.000 abstract description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 abstract 1
- 239000003245 coal Substances 0.000 abstract 1
- 238000010304 firing Methods 0.000 abstract 1
- 239000012717 electrostatic precipitator Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- -1 ammonia compound Chemical class 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 101100248191 Salmo salar rft2 gene Proteins 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- UKFWSNCTAHXBQN-UHFFFAOYSA-N ammonium iodide Chemical compound [NH4+].[I-] UKFWSNCTAHXBQN-UHFFFAOYSA-N 0.000 description 1
- 150000001721 carbon Chemical class 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000010169 landfilling Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 235000019645 odor Nutrition 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は水洗法によるフライアッシュの脱アンモニア法
に関し、詳しくは石炭焚Ｉイラ排ガス処理工程において
回収されるフライアッシュの脱アンモニア法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for removing ammonia from fly ash using a water washing method, and more particularly, to a method for removing ammonia from fly ash recovered in a coal-fired I-Ira exhaust gas treatment process.
石炭焚ボイラ排ガスのクリーン化は現在、除塵と脱硫及
び脱硝の３技術が主体となっている。Currently, three technologies are being used to clean coal-fired boiler exhaust gas: dust removal, desulfurization, and denitrification.
コ（７） ３９１ｉを備えた排ガス処理プロセスノ中テ
実用性の高いものは、排ガスをアンモニア注入下で乾式
脱硝処理し、次いで電気集塵装置によりガス中のフライ
アッシュを回収し、更に石灰−石こう法もしくは石灰石
−石こう法による脱硫処理を組合わせたものである。(7) A highly practical exhaust gas treatment process equipped with 391i is to perform dry denitration treatment on the exhaust gas while injecting ammonia, then collect the fly ash in the gas using an electrostatic precipitator, and then remove lime. This is a combination of desulfurization treatment using the gypsum method or the limestone-gypsum method.
このような排ガス処理プルセスでは、脱硝装置から排出
されるガス中に５Ｐ程度のリークアンモニアが存在して
おり、主として（ＮＨ４）ｌ ８０４又はＮ）Ｉ４Ｈ８
Ｏ，としてフライアッシュに吸着される。従って、リー
クアンモニアの大部分はフライアッシュと共に電気集塵
機で回収される。In such exhaust gas treatment process, leak ammonia of about 5P exists in the gas discharged from the denitrification equipment, and it is mainly (NH4)l 804 or N)I4H8.
It is adsorbed by fly ash as O. Therefore, most of the leaked ammonia is collected together with fly ash in an electrostatic precipitator.
フライアッシュは、埋立処理等で処分□されるが、吸着
されたアンモニア化合物が経時的に分解し、アンモニア
を遊離するため、悪臭発生等の生活環境を損う問題があ
った。Fly ash is disposed of by landfilling, etc., but the adsorbed ammonia compounds decompose over time and liberate ammonia, which poses problems such as the generation of bad odors that impair the living environment.
この問題を解決するには、予めアンモニア化合物をフラ
イアッシュから分離する必要があり、従来では熱分解法
が実施されていた。即ち、フライアッシュを約４００Ｃ
以上に加熱してアンモニア化合物を分解する方法である
が、加熱に要するエネルギー消費量が大きく経済的に不
利であった。一方、アンモニアを水により溶出させる方
法も知られており、この方法は前記熱分解法に比ベエネ
ルギー面で有利な方法である。To solve this problem, it is necessary to separate the ammonia compound from the fly ash in advance, and conventionally a thermal decomposition method has been used. That is, about 400C of fly ash
This is a method of decomposing ammonia compounds by heating to a higher degree, but the amount of energy required for heating is large and is economically disadvantageous. On the other hand, a method in which ammonia is eluted with water is also known, and this method is more advantageous than the thermal decomposition method in terms of relative energy.
しかしながら、アンモニアを含む廃液処理の問題が生じ
、廃液中のアンモニアは低濃度であるためアンモニアの
回収は困難である。まして、アンモニアの有効利用は全
くなされていなかった。However, a problem arises in the treatment of waste liquid containing ammonia, and since the concentration of ammonia in the waste liquid is low, it is difficult to recover ammonia. Furthermore, ammonia was not used effectively at all.
本発明の目的は、上記問題を解決し、水洗法によりフラ
イアッシュ中のアンモニア成分を容易に分離し、更に遊
離アンモニアを有効に利用し、そして、その廃スラリー
を脱硫装置における脱硫剤として使用するようにした方
法を提供するところにある。The purpose of the present invention is to solve the above problems, easily separate the ammonia component in fly ash by a water washing method, effectively utilize free ammonia, and use the waste slurry as a desulfurization agent in a desulfurization equipment. The purpose is to provide a method for doing so.
即ち、本発明は石炭焚ぜイラ排ガスをアンモニアガス注
入下で脱硝処理し、次いでガス中のフライアッシュを回
収除去し、更に湿式脱硫処理することを主工程とする排
ガス処理工程において、前記回収されるフライアッシュ
に吸着したアンモニア化合物を水に溶解させ、フライア
ッシュとアンモニア含有水に分離した後、このアンモニ
ア含有水にＣａ又はＭｇの炭酸塩、水酸化物、酸化物の
いずれかを添加してアンモニアガスを発生させ・、更に
このアンモニアガスを前記排ガスの脱硝処理に使用し、
更にＣａ又はＭｇの炭酸塩水酸化物を多量に含んだ廃ス
ラリーを脱硫装置の脱硫剤として使用することを特徴と
するものである。That is, the present invention provides an exhaust gas treatment process in which the main steps are denitration treatment of coal-fired kerosene exhaust gas while injecting ammonia gas, then recovery and removal of fly ash in the gas, and further wet desulfurization treatment. After dissolving the ammonia compound adsorbed on fly ash in water and separating it into fly ash and ammonia-containing water, either Ca or Mg carbonate, hydroxide, or oxide is added to this ammonia-containing water. Generating ammonia gas and further using this ammonia gas for denitration treatment of the exhaust gas,
Furthermore, the present invention is characterized in that a waste slurry containing a large amount of Ca or Mg carbonate hydroxide is used as a desulfurization agent in a desulfurization device.
次に、本発明を図にそって説明を行う。図は本発明に係
る石炭焚ぎイラ排ガスの脱硫脱硝プロセスの構成例を示
すものである。１ぜイラｌよりの排ガスは通常ａＯＯ〜
４５０Ｃの温度で排出され、乾式の脱硝装置２に導かれ
ここでＮＨ。Next, the present invention will be explained with reference to the drawings. The figure shows an example of the configuration of the desulfurization and denitrification process for coal-fired waste gas according to the present invention. Exhaust gas from 1.
It is discharged at a temperature of 450C and led to a dry denitrification device 2 where NH is produced.
ガスがライン１１より注入され、更に後述するライン１
２より回収されたＮＨ，（場合によってＣＯ鵞金含有ガ
スが注入される。脱硝後、排ガスは空気予熱器３にてゼ
イラ燃焼空気と熱交換され１１０〜１８０ｃのガス温度
で電気集塵ＩＩＩＡ４（他の集塵機でも可）に入いり、
ガス中のフライアッシュが捕集される。次いで、熱交換
機５で脱硫後の排ガスと熱交換された後、脱硫剤として
Ｃ１又はＭｇの炭ｍ塩、水酸化物、酸化物を使用する湿
式脱硫システム６に入いり脱硫され、熱交換機５を介し
て大気に排出される。Ｃｍ系によるスケーリングの問題
を避けたい場合はＭｇ系が好ましい。Gas is injected from line 11, and further from line 1, which will be described later.
NH, (sometimes CO) containing gas is injected. After denitrification, the exhaust gas is heat exchanged with the Zeila combustion air in the air preheater 3, and is electrostatically precipitated at a gas temperature of 110 to 180C ( (You can also use other dust collectors)
Fly ash in the gas is collected. Next, after being heat exchanged with the desulfurized exhaust gas in a heat exchanger 5, it enters a wet desulfurization system 6 that uses carbon salt, hydroxide, or oxide of C1 or Mg as a desulfurization agent, and is desulfurized. is emitted to the atmosphere via If it is desired to avoid the scaling problem caused by Cm-based materials, Mg-based materials are preferred.
ガスのフｐ−は以上述べた通りであるが、前記の如く脱
硝後の排ガス中にはリークアンモニアが存在しているた
めにアンモニアを吸着したフライアッシュが電気集塵機
で回収される。以下、図にそってフライアッシュの脱ア
ンモニアのプロセスを詳述する。The gas flow rate is as described above, but since leaked ammonia is present in the exhaust gas after denitrification as described above, fly ash adsorbing ammonia is recovered by an electrostatic precipitator. Below, the process of removing ammonia from fly ash will be explained in detail according to the diagram.
電気集塵機４からのフライアッシュにはライ ５ −
ン１３により水を添加してライン１４より水流によって
スラリータンク７に供給される。勿論、７ライアツシユ
をドライな状態でスラリータンク７へ供給しここで水を
添加してスラリー状にしても良い。Water is added to the fly ash from the electrostatic precipitator 4 through line 5-13, and the fly ash is supplied to the slurry tank 7 through line 14 by a water flow. Of course, the 7 lithium ash may be supplied in a dry state to the slurry tank 7 and water may be added here to form a slurry.
次いで一ライン１５により脱水機８に送られフライアッ
シュとアンモニア含有水に分離される。脱水機としては
、シックナー、遠心分離器、各種濾過機又はそれらの組
合わせが考えられる。Next, it is sent to a dehydrator 8 through a line 15 and separated into fly ash and ammonia-containing water. As the dehydrator, a thickener, a centrifugal separator, various filters, or a combination thereof can be considered.
アンーＩ！−ニア含有水には主として（ＮＨ４）１８０
４％ ＮＨ４・Ｈ，ｓｏ、、を溶解している。この際ｐ
Ｈ（７となるように脱硫装置の排水又は循環水等の酸性
の水で処理すれば、この段階でＮＨ，が遊離することは
ない。Ann-I! -Nia-containing water mainly contains (NH4)180
4% NH4.H, so, is dissolved. At this time p
If treated with acidic water such as wastewater from the desulfurization equipment or circulating water so that H(7), NH, will not be liberated at this stage.
この水は、ライン１６によりＮＨ，ガス発生タンク（ス
ラリータンク）９に送給され、ここで水中のアンモニア
を除去する目的でＣａ又はＭｇの炭酸塩、水酸化物、酸
化物をライン１７により添加してＮＨ，ガスを発生させ
る（必要に応じてライン１８により水を添加する）。This water is sent to the NH gas generation tank (slurry tank) 9 via line 16, where carbonate, hydroxide, or oxide of Ca or Mg is added via line 17 for the purpose of removing ammonia from the water. to generate NH, gas (water is added via line 18 if necessary).
石灰石（ＣａＣＯ，）を使用した場合には（１） （２
）式による。When limestone (CaCO, ) is used, (1) (2
) according to the formula.
（ＮＩ（４）！ Ｓ ０４ ＋Ｃａ ＣＯｓ ＋ＨＩＯ
→２ＮＨ，↑＋ Ｃａ５Ｏ，”ＺＨｔＯ＋ＣＯＩ↑ （
１）ＮＨ４・ＨφＳＯ４＋ＣａＣ０Ｂ＋ＨＩＯ−＋ＮＨ
８↑十Ｃａ Ｓ ０４・２ ＨＩＯ＋ ＣＯｓ↑ （２
）（ＭｇＣ０，の場合は、式中のＣａがＭｇとなる。）
ＣａＯを使用した場合には（３） （４）式による。(NI(4)! S 04 +Ca COs +HIO
→2NH,↑+ Ca5O,”ZHtO+COI↑ (
1) NH4・HφSO4+CaC0B+HIO-+NH
8↑10Ca S 04・2 HIO+ COs↑ (2
) (In the case of MgC0, Ca in the formula becomes Mg.)
When CaO is used, formulas (3) and (4) are used.
（ＮＨ４）Ｉ Ｓ ０４ ＋Ｃａ Ｏ＋ Ｈ，Ｏ→２Ｎ
Ｈ，↑十Ｃａ５Ｏ４ｅ２Ｈ１０（３）
ＮＨ４” １■” ＳＯ４＋ ＣａＯ＋ＨＩＯ４ＮＨＩ
↑＋ＣａＳＯ４９２Ｈ，０（４）
（ＭｇＯの場合は、式中のＣ＆がＭｇとなる。）このよ
うにしてＮＨ，ガス発生タンク９にて発生したＮＨ，ガ
スはライン１２より脱硝袋ｒｆｔ２へ送られ排ガスの脱
硝に供される。なお、ｐｌＩ調整を行わぬ場合はスラリ
ータンク７においてフライアッシュ中のＣａＯと反応し
前記（３）（４）式の如くＮＨ，ガスが、少量ではある
が発生する可能性があるので、この場合ここで発生する
ＮＨ，ガスを脱硝装置へ供給して良い。(NH4)I S 04 +Ca O+ H,O→2N
H, ↑10Ca5O4e2H10 (3) NH4” 1■” SO4+ CaO+HIO4NHI
↑+CaSO492H,0(4) (In the case of MgO, C & in the formula becomes Mg.) In this way, the NH and gas generated in the NH and gas generation tank 9 are sent to the denitrification bag rft2 from the line 12. Used for denitration of exhaust gas. In addition, if the plI adjustment is not performed, there is a possibility that NH and gas will be generated, albeit in small quantities, by reacting with CaO in the fly ash in the slurry tank 7 as shown in equations (3) and (4) above. The NH and gas generated here may be supplied to the denitrification device.
タンク９と脱硫システム６に石灰石等を個別に供給し、
又石ロウ等の副生品をタンク９と脱硫システム６にて個
別に回収するよりも一括して処理することが望ましい。Limestone etc. are individually supplied to the tank 9 and the desulfurization system 6,
Furthermore, it is preferable to process by-products such as stone wax all at once rather than collecting them separately in the tank 9 and the desulfurization system 6.
即ち、ＮＨ＠ガス発生と排ガス脱硫に必要とされる石灰
石等を一括してタンク９に供給してアンモニア含有水の
処理を行った後、アンモニアとの反応分及び未反応分を
含むスラリーをライン１９により脱硫システム６へ供給
して排ガスの脱硫に供し、ここでシックナー等の固液分
離操作によって副生品（石ロウ等）回収を行う。又、脱
硫システム６からの排水はライン２０もしくはライン２
１により循環使用され、他にライン２２．２３によりス
ラリータンク７へ供給しても良い。That is, limestone and other materials required for NH@ gas generation and exhaust gas desulfurization are supplied to the tank 9 in bulk to treat ammonia-containing water, and then the slurry containing the reacted and unreacted components with ammonia is sent to the tank 9. 19 to the desulfurization system 6 for desulfurization of the exhaust gas, where by-products (stone wax, etc.) are recovered by a solid-liquid separation operation using a thickener or the like. Also, the waste water from the desulfurization system 6 is connected to line 20 or line 2.
1, and may also be supplied to the slurry tank 7 via lines 22 and 23.
なお、タンク９において、ＮＨ，ガスの再溶解を防ぐ目
的で脱硫システム６からの循環水（ｐＨ３〜６）を少な
くし又は使用せずタンク９内のｐｔ＋を高＜（ＰＩＩＩ
Ｏ以上）することが望ましい。In addition, in the tank 9, in order to prevent re-dissolution of NH and gas, the circulating water (pH 3 to 6) from the desulfurization system 6 is reduced or not used, and the pt+ in the tank 9 is set to high < (PIII
O or above) is desirable.
又、排水の温度を高くした方がＮＨ，ガスの水に対する
溶解度は小さくなる。仮に、脱硫システム６に入いる水
中に溶解アンモニアが存在していたとしても１脱硫シス
テム内で水のｐＨを３〜６に保持さえしておけばＮＨ，
ガスの発生の問題はない。そして、必要に応じて脱硫シ
ステムからの排水の一部を排水処理設備１０にて処理し
ても良い。Furthermore, the higher the temperature of the waste water, the lower the solubility of NH and gas in water. Even if there is dissolved ammonia in the water entering the desulfurization system 6, as long as the pH of the water is maintained at 3 to 6 within the desulfurization system, NH,
There is no problem with gas generation. A part of the waste water from the desulfurization system may be treated in the waste water treatment facility 10 if necessary.
以上の説明から明らかなように、本発明はＮＨ，注入下
での脱硝とスラリー吸収による脱硫を組合わせた排ガス
の脱硫脱硝プロセスにおいて回収されるフライアッシュ
の脱アンモニアが容易に行える上、遊離したＮＨ，ガス
を有効に利用し得、又ＮＨ，脱気後の廃スラリーｅ脱硫
装置に投入し、脱硫剤として利用するようにしたため、
過剰のＣａＯ等を投入でき、脱ＮＨ，率を高め得るし、
特に排水処理のための特別な装置を要しないものである
。更に、本発明によれば脱硫剤として公知のＣａＯ等を
そのまま使用してＮＨ。As is clear from the above description, the present invention allows easy removal of ammonia from fly ash recovered in an exhaust gas desulfurization/denitration process that combines denitration under NH injection and desulfurization by slurry absorption, and NH gas can be used effectively, and the waste slurry after NH deaeration can be fed into the e-desulfurization equipment and used as a desulfurization agent.
Excess CaO etc. can be added, increasing the NH removal rate,
It does not require any special equipment for wastewater treatment. Furthermore, according to the present invention, NH is produced by directly using known CaO or the like as a desulfurizing agent.
ガスを発生させることができるため、脱硫システムに容
易に組入れることができりｐ−ズド化 ９−
をはかつて廃液の問題も解決される。Since the gas can be generated, it can be easily incorporated into a desulfurization system, and the problem of waste liquid is also solved.
図は本発明に係る石炭焚ぜイラ排ガスの脱硫脱硝プロセ
スの構成例を示すものである。
１・・・ゼイラ ２・・・脱硝装置４・・・電気
集塵機 ６・・・湿式脱硫システム７・・・スラリー
タンク ８・・・脱水機９・・・ＮＨ，ガス発生タンクThe figure shows an example of the configuration of the desulfurization and denitrification process for coal-fired boiler exhaust gas according to the present invention. 1... Zeira 2... Denitrification device 4... Electrostatic precipitator 6... Wet desulfurization system 7... Slurry tank 8... Dehydrator 9... NH, gas generation tank
Claims (1)
処理し、次いでガス中のフライアッシュを回収除去し、
更に湿式脱硫処理することを主工程とする排ガス処理工
程において、前記回収されるフライアッシュに吸着した
アンモニア化合物を水に溶解させ、フライアッシュとア
ンモニア含有水に分離した後、このアンモニア含有水に
Ｃａ又はＭ、の炭酸塩、水酸化物、酸化物のいずれかを
添加してアンモニアガスを発生させ、更にこのアンモニ
アガスを前記排ガスの脱硝処理に使用すると共に、アン
モニアを脱気したスラリーは脱硫装置の脱硫剤として使
用することを特徴とする水洗法によるフライアッシュの
脱アンモニア法。1. Denitrate the coal-fired zeira exhaust gas while injecting ammonia gas, then collect and remove the fly ash in the gas,
Furthermore, in the exhaust gas treatment process whose main step is wet desulfurization treatment, the ammonia compounds adsorbed on the recovered fly ash are dissolved in water and separated into fly ash and ammonia-containing water, and then Ca is added to the ammonia-containing water. or M, carbonate, hydroxide, or oxide is added to generate ammonia gas, and this ammonia gas is further used for the denitration treatment of the exhaust gas, and the slurry from which the ammonia has been degassed is sent to a desulfurization device. A method for removing ammonia from fly ash by washing with water, which is characterized by its use as a desulfurizing agent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57118183A JPS5910327A (en) | 1982-07-07 | 1982-07-07 | Method for removing ammonia from fly ash by rinsing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57118183A JPS5910327A (en) | 1982-07-07 | 1982-07-07 | Method for removing ammonia from fly ash by rinsing method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS5910327A true JPS5910327A (en) | 1984-01-19 |
Family
ID=14730192
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57118183A Pending JPS5910327A (en) | 1982-07-07 | 1982-07-07 | Method for removing ammonia from fly ash by rinsing method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5910327A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6290066B1 (en) * | 1998-03-26 | 2001-09-18 | Board Of Control For Michigan Technological University | Method for removal of ammonia from fly ash |
| US6790264B2 (en) | 2000-03-08 | 2004-09-14 | Isg Resources, Inc. | Control of ammonia emission from ammonia laden fly ash in concrete |
| CN114956424A (en) * | 2022-05-31 | 2022-08-30 | 中冶赛迪技术研究中心有限公司 | Sintering machine head ash deamination method using desulfurization waste liquid treatment system |
-
1982
- 1982-07-07 JP JP57118183A patent/JPS5910327A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6290066B1 (en) * | 1998-03-26 | 2001-09-18 | Board Of Control For Michigan Technological University | Method for removal of ammonia from fly ash |
| US6790264B2 (en) | 2000-03-08 | 2004-09-14 | Isg Resources, Inc. | Control of ammonia emission from ammonia laden fly ash in concrete |
| CN114956424A (en) * | 2022-05-31 | 2022-08-30 | 中冶赛迪技术研究中心有限公司 | Sintering machine head ash deamination method using desulfurization waste liquid treatment system |
| CN114956424B (en) * | 2022-05-31 | 2023-09-26 | 中冶赛迪技术研究中心有限公司 | Sintering machine head ash deamination method utilizing desulfurization waste liquid disposal system |
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