JPH01176493A - Treatment of waste water from incineration plant - Google Patents
Treatment of waste water from incineration plantInfo
- Publication number
- JPH01176493A JPH01176493A JP33247587A JP33247587A JPH01176493A JP H01176493 A JPH01176493 A JP H01176493A JP 33247587 A JP33247587 A JP 33247587A JP 33247587 A JP33247587 A JP 33247587A JP H01176493 A JPH01176493 A JP H01176493A
- Authority
- JP
- Japan
- Prior art keywords
- waste water
- supernatant liquid
- wastewater
- tank
- ash
- 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
- 239000002351 wastewater Substances 0.000 title claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 50
- 239000006228 supernatant Substances 0.000 claims abstract description 41
- 238000005406 washing Methods 0.000 claims abstract description 31
- 229920000642 polymer Polymers 0.000 claims abstract description 27
- 239000013522 chelant Substances 0.000 claims abstract description 19
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 238000004062 sedimentation Methods 0.000 claims description 30
- 238000005345 coagulation Methods 0.000 claims description 25
- 230000015271 coagulation Effects 0.000 claims description 25
- 239000000779 smoke Substances 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 13
- 238000004056 waste incineration Methods 0.000 claims description 13
- 238000004140 cleaning Methods 0.000 claims description 7
- 239000000701 coagulant Substances 0.000 claims description 3
- 230000001112 coagulating effect Effects 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 32
- 229910052753 mercury Inorganic materials 0.000 abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 20
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 19
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 229920005989 resin Polymers 0.000 abstract description 8
- 239000011347 resin Substances 0.000 abstract description 8
- 238000005189 flocculation Methods 0.000 abstract description 7
- 230000016615 flocculation Effects 0.000 abstract description 7
- 238000002156 mixing Methods 0.000 abstract description 2
- 239000002245 particle Substances 0.000 abstract description 2
- 239000010908 plant waste Substances 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 24
- 238000003756 stirring Methods 0.000 description 14
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 13
- 229910052793 cadmium Inorganic materials 0.000 description 13
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 13
- 229910052725 zinc Inorganic materials 0.000 description 13
- 239000011701 zinc Substances 0.000 description 13
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 12
- 229910052804 chromium Inorganic materials 0.000 description 12
- 239000011651 chromium Substances 0.000 description 12
- 239000010802 sludge Substances 0.000 description 12
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 8
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 8
- 235000011121 sodium hydroxide Nutrition 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 239000008235 industrial water Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 238000006386 neutralization reaction Methods 0.000 description 6
- 238000007796 conventional method Methods 0.000 description 5
- 230000003472 neutralizing effect Effects 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 5
- 239000002699 waste material Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000008394 flocculating agent Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 230000003466 anti-cipated effect Effects 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 229920001429 chelating resin Polymers 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229960002089 ferrous chloride Drugs 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002516 radical scavenger Substances 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Removal Of Specific Substances (AREA)
Abstract
Description
【発明の詳細な説明】 産業上の利用分野 本発明は、ごみ焼却工場排水の処理方法に関する。[Detailed description of the invention] Industrial applications The present invention relates to a method for treating wastewater from a waste incineration plant.
従来の技術及びその問題点
従来、ごみ焼却工場では、ごみを焼却することによって
発生する排煙中に含まれる水銀等の重金属は、次のよう
な方法により処理されてきた。即ち、排煙中に含まれる
重金属は、まずスクラバーで水洗することにより水中に
捕捉され(このようにして発生する排水を「洗煙排水」
という)、清浄になった排ガスは大気中に放出される。Conventional techniques and their problems Conventionally, in garbage incineration plants, heavy metals such as mercury contained in flue gas generated by incinerating garbage have been treated by the following methods. In other words, the heavy metals contained in flue gas are first captured in water by washing with water using a scrubber (the wastewater generated in this way is called "smoke washing wastewater").
), and the purified exhaust gas is released into the atmosphere.
一方、重金属を含んだ洗煙排水には、液体キレート(重
金属捕集剤)及び塩化鉄が添加され、苛性ソーダでpH
7付近に中和された後、更に高分子凝集剤が添加されて
凝集沈澱処理され(ここで水銀以外の重金属は排出基準
以下となる)、次いで砂濾過後、上記凝集沈澱処理では
充分に凝集沈澱しなかった水銀はキレート樹脂により排
出基準を満たす低濃度にまで除去され、その後、無害化
された排水は下水道又は公共水域へ放流されてきた。そ
の一方において、ごみの焼却で生じる焼却灰の冷却には
、別途清浄な工業用水が用いられ(このようにして発生
した排水を「灰汚水」という)、その後この灰汚水は装
置φ床洗浄排水等と混合され、この混合液(プラント排
水)が上記と同様に凝集沈澱処理され、無害化されて、
下水道又は公共水域へ放流されているのが現状である。On the other hand, liquid chelate (heavy metal scavenger) and iron chloride are added to smoke washing wastewater containing heavy metals, and pH is adjusted with caustic soda.
After being neutralized to around 7, a polymer flocculant is further added to perform a coagulation-sedimentation treatment (heavy metals other than mercury are below the emission standards), and then after sand filtration, the above-mentioned coagulation-sedimentation treatment is sufficient to flocculate. The unprecipitated mercury is removed using chelating resins to a low concentration that meets emission standards, and the detoxified wastewater is then discharged into sewers or public waters. On the other hand, separate clean industrial water is used to cool the incinerated ash generated from garbage incineration (the wastewater generated in this way is called ``ash wastewater''), and this ash wastewater is then used as wastewater from the equipment φ floor cleaning drain. etc., and this mixed liquid (plant wastewater) is subjected to coagulation and sedimentation treatment in the same manner as above, and rendered harmless.
Currently, it is discharged into sewers or public water bodies.
しかしながら、斯かる従来の方法では、水銀の除去に用
いられるキレート樹脂が高価であり、しかもこのキレー
ト樹脂の表面は、水銀捕捉性能低下をもたらす懸濁物質
やコロイド物質等で汚染されたり、黴等の微生物が繁殖
し易く、該樹脂の維持管理が困難になるという欠点があ
る。更にこの方法では、焼却灰の冷却等に多量の工業用
水を必要としている。そこで、ごみ焼却工場の排水処理
の簡素化、処理費の削減、工業用水費の軽減等が要望さ
れているが、未だその有効な解決方法が見い出されてい
ない。However, in such conventional methods, the chelate resin used to remove mercury is expensive, and the surface of this chelate resin is often contaminated with suspended matter, colloidal substances, etc. that reduce mercury capture performance, and mold, etc. The drawback is that microorganisms tend to propagate, making it difficult to maintain and manage the resin. Furthermore, this method requires a large amount of industrial water for purposes such as cooling the incinerated ash. Therefore, there are demands for simplifying the treatment of wastewater from waste incineration plants, reducing treatment costs, and reducing industrial water costs, but no effective solution has yet been found.
問題点を解決するための手段
本発明者は、上記要望に合致するごみ焼却工場の排水処
理方法を開発すべく鋭意研究を重ねてきた。その結果、
洗煙排水を凝集沈澱処理した後の上澄液を灰汚水や装置
・床洗浄排水と混合すれば、上澄液中に残存している水
銀等の重金属は、灰汚水中の焼却灰や装置・床洗浄排水
中の懸濁粒子に吸着され、そしてこれを再度無機凝集剤
を用いて凝集沈澱処理すれば、上記上澄液中に残存して
いた微量の水銀をも上記上澄液から排出基準を満たす低
濃度にまで除去できるという、当業者にとり予期し得な
い驚くべき効果が発現され得ることを見い出した。本発
明は、斯かる知見に基づいて完成されたものである。Means for Solving the Problems The present inventor has conducted extensive research in order to develop a wastewater treatment method for waste incineration plants that meets the above requirements. the result,
If the supernatant liquid after coagulating and settling the smoke washing wastewater is mixed with ash wastewater and equipment/floor washing wastewater, heavy metals such as mercury remaining in the supernatant liquid can be removed from the incinerated ash and equipment in the ash wastewater.・If the suspended particles in the floor cleaning wastewater are adsorbed, and if this is coagulated and precipitated again using an inorganic flocculant, the trace amount of mercury remaining in the supernatant can be removed from the supernatant. It has been found that a surprising effect that could not have been anticipated by those skilled in the art can be achieved in that it can be removed to a low concentration that meets the standards. The present invention was completed based on this knowledge.
即ち、本発明は、液体キレート、無機凝集剤及び高分子
凝集剤によりごみ焼却工場の洗煙排水を凝集沈澱処理し
た後、この上澄液に灰汚水や装置・床洗浄排水を混合し
、該混合物を無機凝集剤及び高分子凝集剤により再度凝
集沈澱処理することを特徴とするごみ焼却工場排水の処
理方法、並びに液体キレート、無機凝集剤及び高分子凝
集剤によりごみ焼却工場の洗煙排水を凝集沈澱処理した
後、この上澄液を焼却灰の冷却用水として使用し、次い
でこの使用済み液を無機凝集剤及び高分子凝集剤により
再度凝集沈澱処理することを特徴とするごみ焼却工場排
水の処理方法に係る。That is, the present invention coagulates and settles smoke washing wastewater from a waste incineration plant using a liquid chelate, an inorganic flocculant, and a polymer flocculant, and then mixes ash wastewater and equipment/floor cleaning wastewater with this supernatant liquid. A method for treating waste incineration factory wastewater, which is characterized by subjecting the mixture to coagulation and sedimentation treatment again using an inorganic flocculant and a polymer flocculant, and a waste incineration factory wastewater treatment method using a liquid chelate, an inorganic flocculant, and a polymer flocculant. After coagulation and sedimentation treatment, this supernatant liquid is used as cooling water for incinerated ash, and then this used liquid is subjected to coagulation and sedimentation treatment again using an inorganic flocculant and a polymer flocculant. It concerns the processing method.
本発明の方法を第1図に基づき以下に説明する。The method of the invention will be explained below with reference to FIG.
第1図は、本発明方法の一実施態様を示すフローチャー
トである。FIG. 1 is a flowchart showing one embodiment of the method of the present invention.
本発明で処理対象となるごみ焼却工場の洗煙排水は、重
金属を含有するものである。重金属としては、例えば水
銀、マンガン、カドミウム、クロム、鉛、亜鉛、銅、ニ
ッケル、鉄等が挙げられる。Smoke washing wastewater from a waste incineration plant, which is the object of treatment in the present invention, contains heavy metals. Examples of heavy metals include mercury, manganese, cadmium, chromium, lead, zinc, copper, nickel, and iron.
まず上記洗煙排水を第1調整槽を経て第1反応槽に導き
、ここで液体キレート、無機凝集剤及び高分子凝集剤を
添加し、次に該排水を第1次凝集沈澱槽に導き、ここで
第1次凝集沈澱処理する。First, the smoke washing wastewater is led to a first reaction tank through a first adjustment tank, where a liquid chelate, an inorganic flocculant, and a polymer flocculant are added, and then the wastewater is led to a first coagulation sedimentation tank, Here, the first coagulation and precipitation treatment is performed.
用いられる液体キレートとしては、従来公知のものを広
(使用でき、例えばスミキレ−)HM6000 [住人
化学社製〕、エポフロックし−1゜L−2,L−3(い
ずれもミヨシ油脂社製〕、ユニチカUML5000 (
ユニチカ社製〕、ALM−648(日本曹達社製〕等を
挙げることができる。無機凝集剤としては、従来公知の
ものを広く使用でき、例えば塩化第1鉄、塩化第2鉄、
硫酸第2鉄、ポリ塩化アルミニウム、硫酸アルミニウム
等を挙げることができる。また高分子凝集剤としても、
従来公知のものを広く使用でき、例えばコーナンフロッ
ク#2000 C興南化学工業社製〕、ハイモロツクL
−113[協和有機社製〕、アロンN−100(東亜有
機合成社製〕、クリタEDPフロック101〔栗田工業
社製〕等が挙げられる。洗煙排水に添加すべき液体キレ
ートの量としては、特に制限がなく広い範囲内から適宜
選択し得るが、通常排水IQに対して2〜50mg程度
、好ましくは10〜20mg程度とするのがよい。As the liquid chelate used, conventionally known ones can be used (for example, Sumikire) HM6000 [manufactured by Sumire Kagaku Co., Ltd.], Epofloc-1°L-2, L-3 (both manufactured by Miyoshi Yushi Co., Ltd.), Unitika UML5000 (
Unitika Co., Ltd.], ALM-648 (Nippon Soda Co., Ltd.), etc. As the inorganic flocculant, a wide variety of conventionally known coagulants can be used, such as ferrous chloride, ferric chloride,
Examples include ferric sulfate, polyaluminum chloride, aluminum sulfate, and the like. Also, as a polymer flocculant,
A wide variety of conventionally known products can be used, such as Konan Flock #2000 C (manufactured by Konan Kagaku Kogyo Co., Ltd.), Himorok L
-113 [manufactured by Kyowa Organic Co., Ltd.], Aron N-100 (manufactured by Toa Organic Gosei Co., Ltd.), Kurita EDP Flock 101 [manufactured by Kurita Water Industries, Ltd.], etc.The amount of liquid chelate to be added to the smoke washing wastewater is as follows: There is no particular restriction and the amount can be appropriately selected within a wide range, but it is usually about 2 to 50 mg, preferably about 10 to 20 mg, based on the wastewater IQ.
洗煙排水に添加すべき無機凝集剤の量としては、特に制
限がなく広い範囲内から適宜選択し得るが、通常排水1
Qに対して50〜2000mg程度、好ましくは100
〜200mg程度とするのがよい。The amount of inorganic flocculant to be added to the smoke washing wastewater is not particularly limited and can be appropriately selected from a wide range;
About 50 to 2000 mg, preferably 100 mg to Q
The amount is preferably about 200 mg.
また洗煙排水に添加すべき高分子凝集剤の量としては、
特に制限がなく広い範囲内から適宜選択し得るが、通常
排水IQに対して1〜10mg程度、好ましくは2〜4
mg程度とするのがよい。液体キレート、無機凝集剤及
び高分子凝集剤の添加量が上記範囲より少ないと、目的
の重金属除去効果が得られないという難点が生ずる傾向
となり、一方逆に上記範囲より多くなっても、排水中の
重金属の除去効果はそれ程向上せず、経済的に好ましく
ない。In addition, the amount of polymer flocculant that should be added to smoke washing wastewater is as follows:
There is no particular limit and it can be selected appropriately from a wide range, but it is usually about 1 to 10 mg, preferably 2 to 4 mg, based on the drainage IQ.
It is preferable to use about mg. If the amount of liquid chelate, inorganic flocculant, and polymer flocculant added is less than the above range, there will be a tendency that the desired heavy metal removal effect cannot be obtained; The removal effect of heavy metals is not significantly improved, and it is economically unfavorable.
洗煙排水の第1次凝集沈澱処理は、常法に従い行なうこ
とができ、この凝集沈澱処理により、上澄液と汚泥とに
分離される。ここで分離される汚泥は、後に行なわれる
第2次凝集沈澱処理で得られる汚泥と共に、埋立てに供
される。一方、上澄液は、プラント排水貯槽に送られる
。The first coagulation and sedimentation treatment of the smoke washing wastewater can be carried out according to a conventional method, and by this coagulation and sedimentation treatment, it is separated into supernatant liquid and sludge. The sludge separated here is sent to landfill together with the sludge obtained in the secondary coagulation and sedimentation treatment that will be performed later. Meanwhile, the supernatant liquid is sent to the plant wastewater storage tank.
尚、本発明では、第1次凝集沈澱処理により、上澄液中
の水銀含有量を一定量以下、例えば0.05mg/Q以
下に減じておくのが好ましい。In the present invention, it is preferable to reduce the mercury content in the supernatant liquid to a certain amount or less, for example, 0.05 mg/Q or less, by the first coagulation and precipitation treatment.
上澄液中に含まれている水銀量が多すぎると、後に行な
われる第2次凝集沈澱処理によっても、水銀含有量を排
出基準以下のレベルにまで減少させることが困難になる
傾向となる。If the amount of mercury contained in the supernatant liquid is too large, it tends to be difficult to reduce the mercury content to a level below the emission standard even in the subsequent secondary coagulation and precipitation treatment.
プラント排水貯槽に送られた上澄液は、ここで灰汚水及
び/又は装置・床洗浄排水と混合される。The supernatant liquid sent to the plant wastewater storage tank is here mixed with ash wastewater and/or equipment/floor washing wastewater.
灰汚水や装置・床洗浄排水としては、従来公知のものを
そのまま使用できる。上澄液と灰汚水及び/又は装置・
床洗浄排水との混合割合としては、特に限定されるもの
ではないが、通常前者に対して後者を0.5〜4倍程度
、好ましくは1〜2倍程度の割合で混合するのがよい。As ash wastewater and equipment/floor cleaning wastewater, conventionally known ones can be used as they are. Supernatant liquid and ash wastewater and/or equipment/
The mixing ratio with the floor washing waste water is not particularly limited, but it is usually good to mix the latter at a ratio of about 0.5 to 4 times, preferably about 1 to 2 times, to the former.
プラント排水貯槽の混合液は、次いで第2調整槽を経て
第2反応槽に送られ、ここで無機凝集剤及び高分子凝集
剤が添加された後、第2次凝集沈澱槽に導かれ、第2次
凝集沈澱処理される。無機凝集剤及び高分子凝集剤とし
ては、上記第1次凝集沈澱処理に用いられる無機凝集剤
及び高分子凝集剤をいずれも使用することができる。無
機凝集剤の使用量は、特に制限がなく広い範囲内から適
宜選択し得るが、通常処理すべき混合液IQに対して1
00〜4000mg程度、好ましくは100〜300m
g程度とするのがよく、また高分子凝集剤の使用量も、
特に制限がなく広い範囲内から適宜選択し得るが、通常
処理すべき混合液IQに対して1〜10mg程度、好ま
しくは2〜4mg程度とするのがよい。無機凝集剤及び
高分子凝集剤の添加量が上記範囲より少ないと、水銀除
去の効果が得られないという難点が生ずる傾向となり、
一方逆に上記範囲より多くなっても、混合液中の水銀の
除去効果はそれ程向上せず、経済的に好ましくない。The mixed liquid in the plant wastewater storage tank is then sent to the second reaction tank via the second adjustment tank, where an inorganic flocculant and a polymer flocculant are added, and then led to the second coagulation and sedimentation tank. Secondary coagulation and sedimentation treatment is performed. As the inorganic flocculant and the polymer flocculant, any of the inorganic flocculants and polymer flocculants used in the above-mentioned first coagulation and precipitation treatment can be used. The amount of the inorganic flocculant to be used is not particularly limited and can be appropriately selected from a wide range, but it is usually 1
00~4000mg, preferably 100~300m
The amount of polymer flocculant used should be approximately
There is no particular restriction and the amount can be appropriately selected within a wide range, but it is usually about 1 to 10 mg, preferably about 2 to 4 mg, for the mixed liquid IQ to be treated. If the amount of the inorganic flocculant and polymer flocculant added is less than the above range, there will be a tendency that the mercury removal effect will not be obtained.
On the other hand, if the amount exceeds the above range, the effect of removing mercury from the mixed liquid will not improve much, and this is not economically preferable.
斯かる第2次凝集沈澱処理も、常法に従い行なうことが
でき、この凝集沈澱処理により、上澄水と汚泥とに分離
される。ここで分離される汚泥は、上記したように埋立
てに供され、一方、上澄水は、中和槽で中和処理され、
無害化されて下水道に放流される。上澄水の中和処理も
、従来公知の方法に従い行ない得る。Such secondary flocculation and sedimentation treatment can also be carried out according to a conventional method, and by this flocculation and sedimentation treatment, supernatant water and sludge are separated. The sludge separated here is sent to landfill as described above, while the supernatant water is neutralized in a neutralization tank.
It is rendered harmless and discharged into the sewer system. Neutralization of the supernatant water can also be carried out according to conventionally known methods.
本発明の好ましい他の実施態様によれば、上述した第1
次凝集沈澱処理で得られる上澄液を焼却灰の冷却用水と
して使用した後、これをプラント排水貯槽に送り、更に
第2調整槽に送り、ここで上記と同様にして第2次凝集
沈澱処理を行なう(第2図参照)。この実施態様によれ
ば、洗煙排水中に含まれている重金属を排出基準以下の
レベルにまで減少させることができると共に、焼却灰の
冷却に用いる工業用水量を大きく削減でき、従ってごみ
焼却に要する費用をより一層軽減できる。According to another preferred embodiment of the present invention, the first
After using the supernatant liquid obtained in the secondary coagulation-sedimentation treatment as cooling water for the incinerated ash, it is sent to the plant wastewater storage tank, and further sent to the second adjustment tank, where it is subjected to the second coagulation-sedimentation treatment in the same manner as above. (See Figure 2). According to this embodiment, it is possible to reduce the heavy metals contained in the smoke washing wastewater to a level below the emission standard, and it is also possible to greatly reduce the amount of industrial water used for cooling the incineration ash, thereby reducing waste incineration. The required costs can be further reduced.
発明の効果
本発明の方法によれば、従来法のごとく高価なキレート
樹脂を使用しなくても有害な水銀等の重金属を排出基準
値以下のレベルにまで減少させることができる。また本
発明の方法では、第1次凝集沈澱処理で得られる上澄液
を焼却灰の冷却用水として使用することもできるので、
工業用水量の軽減を図ることができる。従って、本発明
の方法では、排水処理の簡素化、処理費の削減、工業用
水量の軽減等が可能となり、ごみ焼却工場排水の処理を
工業的規模で行なうことができる。Effects of the Invention According to the method of the present invention, harmful heavy metals such as mercury can be reduced to a level below the emission standard value without using an expensive chelate resin as in the conventional method. Furthermore, in the method of the present invention, the supernatant liquid obtained in the first coagulation-sedimentation treatment can be used as water for cooling the incinerated ash.
The amount of industrial water can be reduced. Therefore, with the method of the present invention, it is possible to simplify wastewater treatment, reduce treatment costs, reduce the amount of industrial water, etc., and it is possible to treat wastewater from waste incineration plants on an industrial scale.
実 施 例 以下に実施例を掲げて本発明をより一層明らかにする。Example Examples are given below to further clarify the present invention.
実施例1
ごみ焼却工場の洗煙排水1g(水銀を3.4mg/Qの
濃度で含有)をビーカーに取り、ここにスミキレート6
000H(液体キレート、住人化学社製)10mg及び
塩化第2鉄300mgを添加し、20%苛性ソーダ溶液
でpH7まで中和した後、高分子凝集剤(コーナンフロ
ック#2000)を2mg/Q添加し、急速攪拌5分、
緩速攪拌10分を経た後、静置沈澱させ、沈澱汚泥と上
澄液とに分離した。この上澄液中の各種重金属の濃度及
び除去率は以下の通りである。Example 1 Take 1 g of smoke washing wastewater from a garbage incineration factory (containing mercury at a concentration of 3.4 mg/Q) in a beaker, and add Sumikylate 6 to it.
After adding 10 mg of 000H (liquid chelate, manufactured by Sumima Kagaku Co., Ltd.) and 300 mg of ferric chloride and neutralizing it to pH 7 with a 20% caustic soda solution, 2 mg/Q of a polymer flocculant (Konan Floc #2000) was added. Rapid stirring 5 minutes,
After 10 minutes of slow stirring, the mixture was left to settle and separated into precipitated sludge and supernatant liquid. The concentrations and removal rates of various heavy metals in this supernatant are as follows.
重金属 洗煙排水 上澄液 除去率(mg#!
) (mg#! ) (%)水銀 3.4 0
.042 99
亜鉛 11.7 0.4 97
鉛 5.2 0.01 10
0カドミウム 0.2 0.01 95この各
種重金属の中で水銀濃度は、排出基準以上であるので、
焼却工場より採取したプラント排水500mQを上記上
澄液500n+Qに添加し、塩化第2鉄300mg/
Q 、高分子凝集剤(コーナンフロック#2000)2
mg/Qを加え、10%苛性ソーダ溶液でpH7に中和
し、急速攪拌5分、緩速10分を経た後、静置沈澱させ
た。その結果、上澄水中の水銀濃度は、排出基準0.0
05mg/2以下の0. 0005mg/ Qとなった
。Heavy metals Smoke washing wastewater Supernatant liquid Removal rate (mg #!
) (mg#!) (%) Mercury 3.4 0
.. 042 99 Zinc 11.7 0.4 97 Lead 5.2 0.01 10
0 Cadmium 0.2 0.01 95 Among these various heavy metals, the concentration of mercury is higher than the emission standard, so
500 mQ of plant wastewater collected from the incineration plant was added to the above supernatant liquid 500n+Q, and 300 mg of ferric chloride/
Q, polymer flocculant (Konan Floc #2000) 2
mg/Q was added, neutralized to pH 7 with 10% caustic soda solution, stirred rapidly for 5 minutes and slowly for 10 minutes, and then allowed to settle. As a result, the mercury concentration in the supernatant water was 0.0, which was the emission standard.
0.05mg/2 or less. 0005mg/Q.
実施例2
一般廃棄物を1日550トン焼却している焼却工場では
、洗煙排水を1日当り14’5m3排出し、その重金属
濃度は、水銀が3.0〜3.4mg/Q。Example 2 An incineration factory that incinerates 550 tons of general waste per day discharges 14'5 m3 of smoke washing wastewater per day, and the heavy metal concentration is 3.0 to 3.4 mg/Q of mercury.
、 鉛が0.03〜0.41mg/&、カドミ
ウムが0.005〜0.02mg/R1亜鉛が0.01
〜3.0mg/Q、クロムが0.05〜0.82mg/
Qである。, Lead 0.03~0.41mg/&, Cadmium 0.005~0.02mg/R1 Zinc 0.01
~3.0mg/Q, chromium 0.05~0.82mg/
It is Q.
この洗煙排水を第1調整槽を経て第1反応槽へ導き、ス
ミキレート6000Hを10mg/2及び塩化第2鉄を
300mg/Q添加し、苛性ソーダ溶液でpH7まで中
和した後、高分子凝集剤(コーナンフロック#2000
)を2mg/Q添加し、急速攪拌10分、緩速攪拌25
分を経た後、第1次凝集沈澱処理槽へ導き、上澄液と汚
泥とに沈澱分離した。この凝集沈澱処理により、鉛が0
.0′2未満〜0. 07mg/ Q 、カドミウムが
0.002未満〜0.02mg/Q、亜鉛が0.001
〜0.09n+g/Q、クロムが0. 01〜0. 0
7mg/Qと排出基準を満たす程度まで減少する。水銀
は0.0041〜0.047mg/!2程度にまで減少
するが、尚排出基準には達していない。This smoke washing waste water is led to the first reaction tank via the first adjustment tank, 10 mg/2 of Sumikylate 6000H and 300 mg/Q of ferric chloride are added, and after neutralized to pH 7 with a caustic soda solution, a polymer flocculant is added. (Konan Flock #2000
) was added at 2 mg/Q, followed by rapid stirring for 10 minutes and slow stirring for 25 minutes.
After a few minutes, the mixture was introduced into a primary coagulation and sedimentation treatment tank, where it was separated into a supernatant liquid and sludge. Through this coagulation and sedimentation treatment, lead is reduced to 0.
.. Less than 0'2 ~ 0. 07mg/Q, cadmium less than 0.002~0.02mg/Q, zinc 0.001
~0.09n+g/Q, chromium is 0. 01~0. 0
The amount decreases to 7mg/Q, which meets the emission standards. Mercury is 0.0041-0.047mg/! However, it still does not meet the emission standards.
一方、焼却灰冷却排水(灰汚水)は、11yH7,85
〜11.69であり、水銀が
0、 OO15〜O,’ 0049mg/ Q 、鉛が
12.2〜40.9mg/Q、カドミウムが0、 05
〜0.20mg/ Q 、亜鉛が1.5〜20mg/
Q sクロムが0. 04〜0. 56mg/L7.浮
遊物質が84〜33’5mg/Qの割合で含有されてい
る。この灰汚水と装置・床洗浄排水とを合したプラント
排水(278m3/日)及び上記で得られた上澄液を合
せて第2調整槽へ送り、更に第2反応槽で塩化第2鉄3
00mg/Qを添加し、苛性ソーダ溶液でpH10まで
中和した後、高分子凝集剤(コーナンフロック#200
0)を2mg/R添加し、急速攪拌10分、緩速攪拌2
0分を経た後、第2次凝集沈澱処理槽へ導き、上澄水と
汚泥とに沈澱分離し、最終中和槽でpH6,5〜7.5
に中和した。この処理により、水銀が0.0005未満
〜0.0029mg/2 (平均値0.0011mg/
Q) 、鉛が0.05〜0.14mg/Q、カドミウム
が0.002mg/Q未満、亜鉛が0.001未満〜0
.09mg/Q、クロムが0.01未満〜0.04mg
/Qとなって、充分排出基準を満たす程度まで減少でき
た。尚、排出基準は、水銀が0.005mg/ Q 、
鉛が1 mg/ Q 。On the other hand, incineration ash cooling wastewater (ash sewage) is 11yH7,85
~11.69, mercury is 0, OO15~O,'0049mg/Q, lead is 12.2~40.9mg/Q, cadmium is 0,05
~0.20mg/Q, zinc 1.5~20mg/
Qs chromium is 0. 04-0. 56mg/L7. Suspended solids are contained at a rate of 84 to 33'5 mg/Q. The plant wastewater (278 m3/day), which is a combination of this ash wastewater and the equipment/floor cleaning wastewater, and the supernatant liquid obtained above are sent to the second adjustment tank, and further in the second reaction tank.
After adding 00mg/Q and neutralizing to pH 10 with caustic soda solution, polymer flocculant (Konan Floc #200
0) was added at 2 mg/R, followed by rapid stirring for 10 minutes and slow stirring for 2 minutes.
After 0 minutes, it is led to the second coagulation and sedimentation treatment tank, where it is separated into supernatant water and sludge, and the final neutralization tank has a pH of 6.5 to 7.5.
was neutralized. Through this treatment, mercury is less than 0.0005 to 0.0029 mg/2 (average value 0.0011 mg/2).
Q), lead is 0.05 to 0.14 mg/Q, cadmium is less than 0.002 mg/Q, zinc is less than 0.001 to 0
.. 09mg/Q, chromium less than 0.01~0.04mg
/Q, and the amount was reduced to a level that satisfies the emission standards. In addition, the emission standards are 0.005mg/Q of mercury,
Lead is 1 mg/Q.
カドミウムがO,1mg/Q、亜鉛が5mg/(2,ク
ロムが2mg/(2である。Cadmium is O, 1 mg/Q, zinc is 5 mg/(2, and chromium is 2 mg/(2).
実施例3
一般廃棄物を1日540トン焼却している焼却工場では
、洗煙排水を1日当り151m3排出し、その重金属濃
度は、水銀が2.8〜5.2mg/Q。Example 3 An incineration factory that incinerates 540 tons of general waste per day discharges 151 m3 of smoke washing wastewater per day, and the heavy metal concentration is 2.8 to 5.2 mg/Q of mercury.
鉛が0.25〜O,!53D/f2.カドミウムが0.
008〜0.025mg/12.亜鉛が0.020〜3
.5mg/Q、クロムが0.20〜0.83mg/Qで
ある。Lead is 0.25~O,! 53D/f2. Cadmium is 0.
008-0.025mg/12. Zinc is 0.020-3
.. 5 mg/Q, and chromium is 0.20 to 0.83 mg/Q.
この洗煙排水を第1調整槽を経て第1反応槽へ導き、エ
ポフロックL−2〔液体キレート、ミヨシ油脂社製〕を
1 ’Omg/ Q及び塩化第2鉄を300 mg/Ω
添加し、苛性ソーダ溶液でpH7まで中和した後、高分
子凝集剤(コーナンフロック#2000)を2mg/Q
添加し、急速攪拌5分、緩速攪拌10分を経た後、第1
次凝集沈澱処理槽へ導き、上澄液と汚泥とに沈澱分離し
た。This smoke washing waste water was led to the first reaction tank through the first adjustment tank, and Epofloc L-2 [liquid chelate, manufactured by Miyoshi Oil Co., Ltd.] was added at 1'Omg/Q and ferric chloride was added at 300mg/Ω.
After adding and neutralizing to pH 7 with caustic soda solution, add 2 mg/Q of polymer flocculant (Konan Floc #2000).
After 5 minutes of rapid stirring and 10 minutes of slow stirring,
Next, it was led to a coagulation sedimentation treatment tank, where it was separated into supernatant liquid and sludge by sedimentation.
上記で得られた上澄液を焼却灰の冷却に使用した後、こ
れを第2調整槽へ送り、更に第2反応槽で塩化第2鉄3
00mg/Qを添加し、苛性ソーで溶液でpH10まで
中和した後、高分子凝集剤(コーナンフロック#200
0)を2mg/Q添加し、急速攪拌10分、緩速攪拌2
0分を経た後、第2次凝集沈澱処理槽へ導き、上澄水と
汚泥とに沈澱分離し、最終中和槽でpH6,5〜7.5
に中和した。この処理により、水銀が0.0005未満
〜0.0018mg/Q、鉛が0.02未満〜0.13
mg/Q、カドミウムが0.002未満、亜鉛が0.0
01未満〜0.05mg/Q、クロムが0.01mg/
Q未満〜0.04mg/12となって、充分排出基準を
満たす程度まで減少できた。After the supernatant liquid obtained above is used to cool the incinerated ash, it is sent to the second adjustment tank, and further in the second reaction tank, ferric chloride 3
After adding 00mg/Q and neutralizing the solution to pH 10 with a caustic saw, a polymer flocculant (Konan Floc #200
0) was added at 2 mg/Q, followed by rapid stirring for 10 minutes and slow stirring for 2 minutes.
After 0 minutes, it is led to the second coagulation and sedimentation treatment tank, where it is separated into supernatant water and sludge, and the final neutralization tank has a pH of 6.5 to 7.5.
was neutralized. Through this treatment, mercury is less than 0.0005 to 0.0018 mg/Q, and lead is less than 0.02 to 0.13.
mg/Q, cadmium less than 0.002, zinc 0.0
Less than 01 to 0.05mg/Q, chromium 0.01mg/
It was less than Q to 0.04 mg/12, which was sufficient to meet the emission standards.
実施例4
ある焼却工場は、一般廃棄物を1日570トン焼却し、
584m3の工業用水を使用している。Example 4 A certain incineration factory incinerated 570 tons of general waste per day.
584m3 of industrial water is used.
1日168m3発生する洗煙排水中には、水銀が0.1
1〜6.1111g/2、鉛が0.09〜1.49B/
Q、カドミウムが0.046〜0、 13mg/ Q
、亜鉛が0.36〜3.9mg/R、クロムが0.12
〜4.63mg/Qである。Mercury is 0.1 in the smoke washing wastewater generated in 168 m3 per day.
1~6.1111g/2, lead 0.09~1.49B/2
Q. Cadmium is 0.046~0, 13mg/Q
, zinc 0.36-3.9mg/R, chromium 0.12
~4.63 mg/Q.
この洗煙排水を第1調整槽を経て第1反応槽へ導き、A
LM−648を10mg/Q及び塩化第2鉄を300m
gIQ添加し、苛性ソーダ溶液でpH7まで中和した後
、高分子凝集剤(コーナンフロツク# 2000)を2
mg/Q添加し、急速攪拌5分、緩速攪拌10分を経た
後、第1次凝集沈澱処理槽へ導き、上澄液と汚泥とに沈
澱分離した。この凝集沈澱処理により、鉛が0.02m
g/2未満、カドミウムが0.002〜0.057mg
/R,亜鉛が0.18〜2.54mg/Q、クロムが0
.15〜3.86mg/(2と排出基準を満たす程度ま
で減少する。水銀は0.0048〜0.053mg/Q
程度にまで減少するが、尚排出基準には達していない。This smoke washing waste water is led to the first reaction tank via the first adjustment tank,
LM-648 10mg/Q and ferric chloride 300m
After adding gIQ and neutralizing to pH 7 with caustic soda solution, 2 mL of polymer flocculant (Konan Floc #2000) was added.
mg/Q was added, and after rapid stirring for 5 minutes and slow stirring for 10 minutes, the mixture was introduced into a first coagulation and sedimentation treatment tank, and separated into supernatant liquid and sludge by sedimentation. Through this coagulation and sedimentation treatment, lead was reduced to 0.02 m
less than g/2, cadmium 0.002-0.057 mg
/R, zinc 0.18-2.54mg/Q, chromium 0
.. 15 to 3.86 mg/(2), which is reduced to the extent that it meets the emission standards.Mercury is 0.0048 to 0.053 mg/Q
However, it still does not meet the emission standards.
この上澄液を焼却灰冷却用水として使用した結果、焼却
灰冷却排水(灰汚水)は、pH10.75〜11.75
であり、水銀が0.0050〜0.064mg/Q、鉛
が15.5〜22.OB/f2.カドミウムが0.08
6〜0.41mg/Q、亜鉛が8.68〜17.6mg
/Q、クロムが0.43〜1.21mg/Ω、浮遊物質
が116〜282mg/Qの割合で含有されたものとな
っている。この灰汚水と装置・床洗浄排水とを合したプ
ラント排水(340m3/日)を第2調整槽へ送り、更
に第2反応槽で塩化第2鉄300mg/Qを添加し、苛
性ソーダ溶液でpH10まで中和した後、高分子凝集剤
(コーナンフロック#2000)を2 mg/ Q添加
し、急速攪拌10分、超速攪拌20分を経た後、第2次
凝集沈澱処理槽へ導き、上澄水と汚泥とに沈澱分離し、
最終中和槽でpH6,5〜7.5に中和した。この処理
により、水銀が0.0005未満〜0.0034mg/
Q、鉛が0. 03〜0. 18mg/Q、カドミウム
が0.002未満〜0.02801g/ Q 、亜鉛が
0.024〜0.134D/Q。As a result of using this supernatant liquid as water for cooling incinerated ash, the incinerated ash cooling wastewater (ash wastewater) has a pH of 10.75 to 11.75.
mercury is 0.0050 to 0.064 mg/Q, and lead is 15.5 to 22. OB/f2. Cadmium is 0.08
6-0.41mg/Q, zinc 8.68-17.6mg
/Q, chromium is contained at a ratio of 0.43 to 1.21 mg/Ω, and suspended solids are contained at a ratio of 116 to 282 mg/Q. Plant wastewater (340m3/day), which is a combination of this ash wastewater and equipment/floor cleaning wastewater, is sent to the second adjustment tank, where 300mg/Q of ferric chloride is added in the second reaction tank, and the pH is brought to 10 with caustic soda solution. After neutralization, 2 mg/Q of polymer flocculant (Konan Floc #2000) was added, and after rapid stirring for 10 minutes and ultra-fast stirring for 20 minutes, it was led to the second coagulation and sedimentation treatment tank, where supernatant water and sludge were mixed. Separated by precipitation,
It was neutralized to pH 6.5 to 7.5 in the final neutralization tank. Through this treatment, mercury is less than 0.0005 to 0.0034mg/
Q. Lead is 0. 03~0. 18mg/Q, cadmium less than 0.002~0.02801g/Q, zinc 0.024~0.134D/Q.
クロムが0.06〜0.40mg/Qとなって、充分排
出基準を満たす程度まで減少できた。そしてこの処理水
を下水道に放流できた。Chromium was reduced to 0.06 to 0.40 mg/Q, which was sufficient to meet the emission standards. This treated water could then be discharged into the sewer system.
このようにしてキレート樹脂を使用することなく、経済
的に洗煙排水を処理した上、1日168m3の洗煙排水
の凝集沈澱処理した上澄液を焼却灰冷却用水に再利用す
ることによって、1年間にキレート樹脂費400万円、
用水費400万円の大幅節減を計ることができ、しかも
キレート樹脂塔の維持管理の困難性から逃れることがで
きた。In this way, the smoke washing wastewater is treated economically without using chelate resin, and the supernatant liquid obtained by coagulation and sedimentation of 168 m3 of smoke washing wastewater per day is reused as water for cooling the incinerated ash. Chelate resin cost 4 million yen per year,
We were able to significantly reduce water costs by 4 million yen, and also avoided the difficulty of maintaining and managing the chelate resin tower.
第1図及び第2図は、本発明方法の好ましい実施態様を
示すフローチャート図である。
(以 上)1 and 2 are flowchart diagrams illustrating a preferred embodiment of the method of the present invention. (that's all)
Claims (2)
りごみ焼却工場の洗煙排水を凝集沈澱処理した後、この
上澄液に灰汚水や装置・床洗浄排水を混合し、該混合物
を無機凝集剤及び高分子凝集剤により再度凝集沈澱処理
することを特徴とするごみ焼却工場排水の処理方法。(1) After coagulating and settling the smoke washing wastewater from a waste incineration plant using a liquid chelate, an inorganic coagulant, and a polymer coagulant, this supernatant liquid is mixed with ash wastewater and equipment/floor cleaning wastewater, and the mixture is inorganic. A method for treating wastewater from a waste incineration plant, characterized by subjecting it to coagulation and sedimentation treatment again using a flocculant and a polymer flocculant.
りごみ焼却工場の洗煙排水を凝集沈澱処理した後、この
上澄液を焼却灰の冷却用水として使用し、次いでこの使
用済み液を無機凝集剤及び高分子凝集剤により再度凝集
沈澱処理することを特徴とするごみ焼却工場排水の処理
方法。(2) After coagulating and settling wastewater from a waste incineration plant using a liquid chelate, an inorganic flocculant, and a polymer flocculant, this supernatant liquid is used as cooling water for the incinerated ash, and then this used liquid is inorganic. A method for treating wastewater from a waste incineration plant, characterized by subjecting it to coagulation and sedimentation treatment again using a flocculant and a polymer flocculant.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP33247587A JPH01176493A (en) | 1987-12-28 | 1987-12-28 | Treatment of waste water from incineration plant |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP33247587A JPH01176493A (en) | 1987-12-28 | 1987-12-28 | Treatment of waste water from incineration plant |
Publications (2)
Publication Number | Publication Date |
---|---|
JPH01176493A true JPH01176493A (en) | 1989-07-12 |
JPH0445237B2 JPH0445237B2 (en) | 1992-07-24 |
Family
ID=18255376
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP33247587A Granted JPH01176493A (en) | 1987-12-28 | 1987-12-28 | Treatment of waste water from incineration plant |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPH01176493A (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002066573A (en) * | 2000-08-25 | 2002-03-05 | Mitsubishi Heavy Ind Ltd | Method for removing manganese ion in wastewater |
JP2016165689A (en) * | 2015-03-10 | 2016-09-15 | 株式会社神鋼環境ソリューション | Water treatment method and water treatment equipment |
JP2016165688A (en) * | 2015-03-10 | 2016-09-15 | 株式会社神鋼環境ソリューション | Water treatment method and water treatment equipment |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6068094A (en) * | 1983-09-21 | 1985-04-18 | Kawasaki Heavy Ind Ltd | Treatment of waste water from wet gas washing apparatus |
-
1987
- 1987-12-28 JP JP33247587A patent/JPH01176493A/en active Granted
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6068094A (en) * | 1983-09-21 | 1985-04-18 | Kawasaki Heavy Ind Ltd | Treatment of waste water from wet gas washing apparatus |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002066573A (en) * | 2000-08-25 | 2002-03-05 | Mitsubishi Heavy Ind Ltd | Method for removing manganese ion in wastewater |
JP2016165689A (en) * | 2015-03-10 | 2016-09-15 | 株式会社神鋼環境ソリューション | Water treatment method and water treatment equipment |
JP2016165688A (en) * | 2015-03-10 | 2016-09-15 | 株式会社神鋼環境ソリューション | Water treatment method and water treatment equipment |
Also Published As
Publication number | Publication date |
---|---|
JPH0445237B2 (en) | 1992-07-24 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
KR101278230B1 (en) | The method and Appuratus of removing total nitrogen and phosphate in sewage and wastewater using precipitation-agent of rapidity for coagulation an flocculation | |
Amer | Treating metal finishing wastewater | |
JPH01176493A (en) | Treatment of waste water from incineration plant | |
ABDUL et al. | H2O2 Oxidation of pre-coagulated semi aerobic leachate | |
KR100707975B1 (en) | Treatment method for livestock waste water including highly concentrated organic materials | |
JPH10165825A (en) | Cleaning agent for contaminated waste water | |
CN109761446A (en) | A kind of processing system and method for dangerous waste disposition center comprehensive wastewater | |
JP2758607B2 (en) | Treatment method for desulfurization wastewater from wet exhaust gas desulfurization equipment | |
JPS61161191A (en) | Treatment of heavy metal ion-containing solution | |
JPH0141110B2 (en) | ||
JPH07100155B2 (en) | Organic wastewater treatment method | |
JP4203576B2 (en) | Treatment method for boron-containing wastewater | |
KR960011889B1 (en) | Method for treatment of waste water from reclaimed land | |
JP3400630B2 (en) | Water purification method using powdered photocatalyst | |
JPH0314519B2 (en) | ||
JPS601073B2 (en) | Method for removing heavy metals from wastewater | |
JP2002186963A (en) | Method and equipment for removing dioxins contained in wastewater of waste incineration plant | |
JPS63258694A (en) | Treatment of organic sewage | |
JP2003010860A (en) | Treater for cleaning wastewater used for demolishing of incinerator | |
JPS6211633B2 (en) | ||
JPH10180298A (en) | Treatment of waste water and waste water treating device | |
JPH0585240B2 (en) | ||
JPH06269799A (en) | Treatment of sludge | |
KR100475465B1 (en) | Acidic waste water treatment method by means of sludge feedback | |
SU789410A1 (en) | Method of waste water purification |