JPH11128972A - For waste-water treatment in coke production equipment - Google Patents
For waste-water treatment in coke production equipmentInfo
- Publication number
- JPH11128972A JPH11128972A JP9296871A JP29687197A JPH11128972A JP H11128972 A JPH11128972 A JP H11128972A JP 9296871 A JP9296871 A JP 9296871A JP 29687197 A JP29687197 A JP 29687197A JP H11128972 A JPH11128972 A JP H11128972A
- Authority
- JP
- Japan
- Prior art keywords
- ammonia
- wastewater
- amount
- treatment system
- steam
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Degasification And Air Bubble Elimination (AREA)
- Activated Sludge Processes (AREA)
- Physical Water Treatments (AREA)
Abstract
Description
【0001】[0001]
【発明の属する技術分野】本発明はコークス製造設備に
おける廃水の処理方法に関するものであり、特に廃水中
のアンモニア分の除去方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating wastewater in a coke making facility, and more particularly to a method for removing ammonia from wastewater.
【0002】[0002]
【従来の技術】コークス製造設備では各種の廃水が発生
する。この第一は余剰ガス液である。コークス製造で
は、コークス炉から流出する高温のコークス炉ガスに水
を噴射してガスを冷却し、含まれているタール分を凝縮
させる。次いでコークス炉ガスは間接冷却により更に冷
却し、ガス精製装置に送られる。これらのガス冷却工程
では水を回収し、含まれているタール分をデカンターな
どで除去したのち、コークス炉ガスへの噴射に循環再利
用している。この水はガス液と称されており、コークス
炉ガス中のアンモニアを吸収して数千ppmのアンモニ
ア分を含んでいる。このアンモニア分の一部は酸と塩を
形成した固定アンモニアとして、他は遊離アンモニアと
して存在している。またコークス炉から流出するコーク
ス炉ガス中には、石炭付着水や乾留過程で石炭から生成
した水が水蒸気として含まれている。従ってガス液の量
は、放置しておくと、この水蒸気から生成する水量だけ
漸増するので、ガス液の循環系からその一部を抜出し
て、循環系の液量が所定の範囲に収まるようにしてい
る。この抜出されたガス液が余剰ガス液であり、前述の
如く数千ppmのアンモニア分を含んでおり、かつ有機
物で高度に汚染されているので、活性汚泥処理を経た後
でなければ、公共水域に排出することはできない。コー
クス製造設備では、余剰ガス液以外にも、コークス炉ガ
スの精製工程やタールの処理工程などからも種々の廃水
が排出される。これらの種々の排出源からの廃水も、相
当量のアンモニア分と有機物を含んでいるものが多く、
それらは余剰ガス液と同様に、活性汚泥処理を経た後で
なければ、公共水域に排出することはできない。2. Description of the Related Art Various kinds of wastewater are generated in coke making equipment. The first is excess gas liquid. In coke production, water is injected into a high-temperature coke oven gas flowing out of the coke oven to cool the gas and condense the contained tar. The coke oven gas is then further cooled by indirect cooling and sent to a gas purification unit. In these gas cooling processes, water is recovered, and the tar content contained in the gas is removed by a decanter or the like, and then recycled for injection into coke oven gas. This water is called a gas liquid, and absorbs ammonia in coke oven gas and contains several thousand ppm of ammonia. A part of this ammonia exists as fixed ammonia which forms a salt with an acid, and the other exists as free ammonia. In addition, the coke oven gas flowing out of the coke oven contains water adhering to coal and water generated from coal during the carbonization process as steam. Therefore, the amount of gas liquid gradually increases by the amount of water generated from the water vapor when left undisturbed. ing. The extracted gas liquid is a surplus gas liquid, contains several thousand ppm of ammonia as described above, and is highly contaminated with organic substances. It cannot be discharged into water bodies. In a coke production facility, various wastewaters are discharged from a coke oven gas purification process and a tar treatment process in addition to the surplus gas liquid. Wastewater from these various sources also often contains significant amounts of ammonia and organics,
They, like surplus gas liquids, can only be discharged into public waters after activated sludge treatment.
【0003】[0003]
【発明が解決しようとする課題】公共水域に排出する廃
水のアンモニア分の濃度は厳しく規制されている。従っ
てコークス製造設備の廃水のように高濃度のアンモニア
分を含むものの処理においては、公共水域へ排出する際
のアンモニア分の濃度を如何にして規制値以下にするか
が、廃水処理費用に大きく影響する。すなわち廃水の発
生量及びそのアンモニア分の含有量は常に変動するの
で、仮にこのような変動が生じても規制値を遵守し得る
ように常に余裕をもってアンモニア分の除去を行うと、
当然のことながら処理費用が増大する。逆に平均的な廃
水の発生量及びそのアンモニア分の含有量を基準にして
処理を行う方法は、処理費用が安くて済むが、大容量の
貯槽を設置して発生源での変動を平均化するなど、変動
を吸収し得る手段を用意しておかなければ、規制値を遵
守することはできない。本発明は廃水処理費用を低く維
持しつつ、規制値を遵守することのできる方法を提供せ
んとするものである。SUMMARY OF THE INVENTION The concentration of ammonia in wastewater discharged into public waters is strictly regulated. Therefore, in the treatment of wastewater containing a high concentration of ammonia, such as wastewater from coke production equipment, how to reduce the concentration of ammonia when discharged to public waters to or below the regulation value has a significant effect on wastewater treatment costs. I do. That is, since the amount of wastewater generated and its ammonia content constantly fluctuate, if the ammonia content is always removed with a sufficient margin so that the regulation value can be complied with even if such a fluctuation occurs,
Naturally, processing costs increase. Conversely, a method that treats wastewater based on the average amount of wastewater generated and its ammonia content can reduce the cost of treatment, but it is necessary to install large-capacity storage tanks to average fluctuations at the source Unless measures are taken to absorb fluctuations, such as by doing so, it will not be possible to comply with the regulation values. The present invention seeks to provide a method that allows compliance with regulatory values while keeping wastewater treatment costs low.
【0004】[0004]
【課題を解決するための手段】本発明によれば、ガス液
循環系から排出される余剰ガス液を、他の排出源からの
汚染された廃水と一緒にして、活性汚泥法を含む廃水処
理系で処理するコークス製造設備における廃水の処理方
法において、廃水処理系に流入する全廃水のアンモニア
分が所定の範囲になるように、少くとも余剰ガス液をス
チームストリッピングに供してそのアンモニア分を低減
させてから廃水処理系に流入させること、及びスチーム
ストリッピングにおけるアンモニアの除去量を廃水の持
込むアンモニア分の量に応じて調節することにより、廃
水処理費用を低減させることができる。SUMMARY OF THE INVENTION According to the present invention, excess gas liquid discharged from a gas liquid circulation system is combined with contaminated wastewater from another discharge source to treat wastewater containing activated sludge. In a method of treating wastewater in a coke manufacturing facility for treating in a system, at least an excess gas liquid is subjected to steam stripping so that the ammonia content of all wastewater flowing into the wastewater treatment system falls within a predetermined range. The wastewater treatment cost can be reduced by flowing the wastewater into the wastewater treatment system after the reduction, and adjusting the amount of ammonia removed in the steam stripping in accordance with the amount of ammonia carried into the wastewater.
【0005】[0005]
【発明の実施の形態】本発明では、廃水から予じめスチ
ームストリッピングによりアンモニア分を除去しておく
ことにより、廃水処理系に流入する廃水のアンモニア分
が所定の範囲に収まるようにする。前述のようにコーク
ス製造設備では排出源を異にする種々の廃水が廃水処理
系に流入するが、廃水の全アンモニア分の相当部分、通
常は50%以上、は余剰ガス液のアンモニア分である。
余剰ガス液は、大量に循環しているガス液の一部を抜出
したものであり、その量及びアンモニア分の変動は比較
的緩慢である。本発明ではこの余剰ガス液をスチームス
トリッピングに供する。通常は余剰ガス液だけをスチー
ムストリッピングに供するが、所望ならば余剰ガス液に
加えて他の排出源からの廃水もスチームストリッピング
に供してもよい。スチームストリッピングにおいて廃水
から除去するアンモニア分の量は、廃水処理系に流入す
る廃水のアンモニア分が所定の範囲内になるように決定
する。スチームストリッピングでは、供給する廃水及び
スチーム量を調節することにより、アンモニア分の除去
量を殆ど時間遅れなく且つ任意に制御することができ
る。従って廃水が持込むアンモニア分の変動に直ちに対
応することができる。DESCRIPTION OF THE PREFERRED EMBODIMENTS In the present invention, the ammonia content of wastewater flowing into a wastewater treatment system falls within a predetermined range by removing ammonia content from wastewater in advance by steam stripping. As described above, in the coke making facility, various wastewaters having different discharge sources flow into the wastewater treatment system. A considerable portion of the total ammonia of the wastewater, usually 50% or more, is the ammonia content of the surplus gas liquid. .
The surplus gas liquid is obtained by extracting a part of the gas liquid circulating in a large amount, and the amount and the fluctuation of the ammonia content are relatively slow. In the present invention, this surplus gas liquid is subjected to steam stripping. Normally, only the excess gas liquid is subjected to steam stripping, but if desired, wastewater from other discharge sources may be subjected to steam stripping in addition to the excess gas liquid. The amount of ammonia removed from wastewater in steam stripping is determined so that the amount of ammonia in wastewater flowing into the wastewater treatment system falls within a predetermined range. In steam stripping, the amount of ammonia removed can be arbitrarily controlled with little time delay by adjusting the amount of wastewater and the amount of steam supplied. Therefore, it is possible to immediately cope with a change in the amount of ammonia brought into the wastewater.
【0006】スチームストリッピングによるアンモニア
除去量の制御は、いくつかの方法で行うことができる。
例えば余剰ガス液の全量を常にスチームストリッピング
に供給しておき、スチーム量を制御することによりアン
モニア分の除去量を制御することができる。しかし通常
は、スチームストリッピングに供給する余剰ガス液量を
制御することにより、アンモニア分の除去量を制御する
のが好ましい。図1は、このような方式を実施する場合
の液の流れの1例を示すもので、余剰ガス液は導管1を
経て供給され、その一部はストリッピング塔2を経て、
残部は直接に、廃水貯槽3に流入する。ストリッピング
塔2には導管4を経てスチームが供給され、余剰ガス液
中のアンモニア分はスチームと一緒に塔頂から導管5を
経て流出する。このアンモニアはコークス炉ガスの脱ア
ンモニア系に導入するなど、適宜の方法で処理される。
廃水貯槽3には、導管6を経て他の排出源からの廃水も
流入している。廃水貯槽3からは導管7を経て廃水が一
定速度で流出し、活性汚泥法を含む廃水処理系に流入す
る。図1において、導管7を流れる廃水のアンモニア分
の濃度を窒素計で測定し、余剰ガス液のアンモニア分
を、窒素計と流量計で測定する。この測定値に基いてス
トリッピング塔2で除去すべきアンモニア分の量を算出
し、ストリッピング塔でのアンモニア分の除去率に基い
て、ストリッピング塔に供給する余剰ガス液量を算出す
る。またストリッピング塔から流出する余剰ガス液中の
アンモニア分を測定し、除去率が所定の値となるように
供給するスチーム量を調節する。[0006] Control of the amount of ammonia removed by steam stripping can be accomplished in several ways.
For example, the entire amount of excess gas liquid is always supplied to steam stripping, and the amount of ammonia removed can be controlled by controlling the amount of steam. However, usually, it is preferable to control the amount of the ammonia gas removed by controlling the amount of excess gas liquid supplied to the steam stripping. FIG. 1 shows an example of a liquid flow when such a method is carried out. The surplus gas liquid is supplied through a conduit 1, and a part of the liquid gas is supplied through a stripping column 2.
The remainder directly flows into the wastewater storage tank 3. Steam is supplied to the stripping column 2 via a conduit 4, and the ammonia in the surplus gas liquid flows out of the column via the conduit 5 together with the steam. This ammonia is treated by an appropriate method such as introduction into a deammonification system of coke oven gas.
Wastewater from another discharge source also flows into the wastewater storage tank 3 via the conduit 6. From the wastewater storage tank 3, wastewater flows out at a constant speed via a conduit 7, and flows into a wastewater treatment system including the activated sludge method. In FIG. 1, the concentration of ammonia in the wastewater flowing through the conduit 7 is measured with a nitrogen meter, and the ammonia in the surplus gas liquid is measured with a nitrogen meter and a flow meter. The amount of ammonia to be removed in the stripping tower 2 is calculated based on the measured values, and the amount of excess gas liquid to be supplied to the stripping tower is calculated based on the removal rate of ammonia in the stripping tower. Further, the ammonia content in the surplus gas liquid flowing out of the stripping tower is measured, and the amount of steam supplied is adjusted so that the removal rate becomes a predetermined value.
【0007】廃水貯槽3から流出する廃水を受入れる廃
水処理系は、活性汚泥法を主体とし、これに更に所望に
より他の処理を組合せたものである。最も簡単には、活
性汚泥法によりBODを低減させたのち、浮遊物(S
S)を濾過ないしは沈降により除去して公共水域に排出
する。所望ならば活性汚泥法と硝化菌、脱窒菌による硝
化・脱窒とを組合せ、廃水中のアンモニア分を更に低減
させることもできる。The wastewater treatment system for receiving the wastewater flowing out of the wastewater storage tank 3 is mainly composed of an activated sludge method, and may be further combined with another treatment as required. Most simply, after the BOD is reduced by the activated sludge method, the suspended solids (S
S) is removed by filtration or sedimentation and discharged to public waters. If desired, the activated sludge method can be combined with nitrification and denitrification by nitrifying bacteria and denitrifying bacteria to further reduce the ammonia content in the wastewater.
【0008】本発明によれば、廃水処理系に流入する廃
水のアンモニア分を平均化させるための大きな廃水貯槽
を設置する必要がない。また余剰ガス液には微生物の生
育に有害なシアンが含まれているが、このシアンにより
後続する廃水処理系が悪影響を受けるのを回避できる。
例えば、硝化菌や脱窒菌はシアンの影響を受け易く、シ
アン濃度が脱窒槽で約30ppm以上になると生育が著
しく阻害されるとされている。また活性汚泥もシアンの
影響を受け、シアン濃度が曝気槽で約50ppm以上に
なると生育が阻害されるようになる。しかし本発明によ
れば、スチームストリッピングによりアンモニアを除去
すると、余剰ガス液中のシアンも容易に留去されるの
で、後続する廃水処理系が余剰ガス液中のシアンにより
阻害されるのを回避することができる。更に本発明で
は、廃水処理系に流入するアンモニア分が所定の値とな
るように、廃水から除去すべきアンモニア分の量に応じ
て、必要最小限のスチームストリッピングを行えばよい
ので、スチーム量を大幅に節減できる。例えば平均し
て、余剰ガス液が遊離アンモニアを195kg/hr、
固定アンモニアを105kg/hrで廃水処理系に持込
んでおり、他の排出源からの廃水が100kg/hrの
アンモニア分を廃水処理系に持込んでいるが、公共水域
へ排出する廃水中のアンモニア分の規制により、後続す
る廃水処理系には300kg/hrのアンモニア分しか
流入させられない場合を想定する。廃水の量とそのアン
モニア濃度が常に一定ならば、スチームストリッピング
により余剰ガス液の遊離アンモニアのうち100kg/
hrを除去すればよい。スチームストリッピングによる
遊離アンモニアの除去率を90%とすると、余剰ガス液
の約57%をスチームストリッピングに供すればよい。
しかし若し他の排出源からの排水の持込むアンモニア分
が最大で150kg/hrに達するとすると、この場合
においても後続する廃水処理系に300kg/hrのア
ンモニア分しか流入させない為には、余剰ガス液の遊離
アンモニアのうちの150kg/hrを除去しなければ
ならない。そのためには余剰ガス液の約86%をスチー
ムストリッピングに供しなければならず、スチームスト
リッピングに供する余剰ガス液は約50%増加する。ス
チームストリッピングに供する液量とスチーム消費量と
はほぼ比例するので、スチームの消費量も約50%増加
することになる。この想定事例からも明らかなように、
廃水の持込むアンモニア分が変動しても大丈夫なように
常に余裕をもってスチームストリッピングを行うと、廃
水の持込むアンモニア量に応じてスチームストリッピン
グでのアンモニア除去量を調節する場合に比し、スチー
ム消費量が著しく増加する。かつ、後続する廃水処理系
の活性汚泥も、アンモニア分の濃度が変動するので管理
が面倒である。According to the present invention, there is no need to provide a large wastewater storage tank for averaging the ammonia content of the wastewater flowing into the wastewater treatment system. Although the surplus gas liquid contains cyan, which is harmful to the growth of microorganisms, it is possible to prevent the subsequent wastewater treatment system from being adversely affected by the cyan.
For example, nitrifying bacteria and denitrifying bacteria are susceptible to cyanide, and it is said that the growth is significantly inhibited when the cyanide concentration is about 30 ppm or more in a denitrification tank. Activated sludge is also affected by cyanide, and its growth is inhibited if the cyanide concentration is about 50 ppm or more in an aeration tank. However, according to the present invention, when ammonia is removed by steam stripping, cyan in the surplus gas liquid is also easily distilled off, so that the subsequent wastewater treatment system is prevented from being hindered by cyan in the surplus gas liquid. can do. Furthermore, in the present invention, the necessary minimum steam stripping may be performed in accordance with the amount of ammonia to be removed from the wastewater so that the ammonia flowing into the wastewater treatment system has a predetermined value. Can be greatly reduced. For example, on average, the surplus gas liquid converts free ammonia to 195 kg / hr,
Fixed ammonia is brought into the wastewater treatment system at 105 kg / hr, and wastewater from other sources brings 100 kg / hr of ammonia into the wastewater treatment system, but ammonia in the wastewater discharged to public waters. It is assumed that only 300 kg / hr of ammonia can be flowed into the subsequent wastewater treatment system due to the regulation of minute. If the amount of wastewater and its ammonia concentration are always constant, 100 kg / free ammonia of excess gas liquid is removed by steam stripping.
hr may be removed. Assuming that the removal rate of free ammonia by steam stripping is 90%, about 57% of the surplus gas liquid may be subjected to steam stripping.
However, if the amount of ammonia brought in by the wastewater from another discharge source reaches a maximum of 150 kg / hr, even in this case, excess 300 mm / hr of ammonia is required to flow into the subsequent wastewater treatment system. 150 kg / hr of the free ammonia in the gas liquid must be removed. For that purpose, about 86% of the surplus gas liquid must be subjected to steam stripping, and the surplus gas liquid to be subjected to steam stripping increases by about 50%. Since the amount of liquid to be subjected to steam stripping is substantially proportional to the amount of steam consumed, the amount of steam consumed also increases by about 50%. As is clear from this assumption,
If steam stripping is always performed with a margin so that it is OK even if the amount of ammonia brought into the wastewater fluctuates, compared to adjusting the amount of ammonia removed by steam stripping according to the amount of ammonia brought into the wastewater, Steam consumption increases significantly. In addition, the activated sludge of the succeeding wastewater treatment system is also troublesome to manage because the concentration of ammonia fluctuates.
【図1】本発明方法により余剰ガス液のスチームストリ
ッピングを行う場合の液の流れの1例を示すものであ
る。FIG. 1 shows an example of the flow of a liquid in the case of performing steam stripping of a surplus gas liquid by the method of the present invention.
1 余剰ガス液の供給導管 2 ストリッピング塔 3 廃水貯槽 4 スチーム供給導管 5 アンモニアガス流出管 6 他の排出源からの廃水の供給導管 7 廃水の流出管 DESCRIPTION OF SYMBOLS 1 Supply pipe of surplus gas liquid 2 Stripping tower 3 Wastewater storage tank 4 Steam supply pipe 5 Ammonia gas outlet pipe 6 Supply pipe of wastewater from other sources 7 Wastewater outlet pipe
Claims (2)
を、他の排出源からの汚染された廃水と一緒にして、活
性汚泥法を含む廃水処理系で処理するコークス製造設備
における廃水の処理方法において、廃水処理系に持込ま
れるアンモニア分が所定の範囲となるように、少くとも
余剰ガス液をスチームストリッピングに供してそのアン
モニア分を低減させてから廃水処理系に流入させるこ
と、及びスチームストリッピングにおけるアンモニアの
除去量を廃水の持込むアンモニア分の量に応じて調節す
ることを特徴とする方法。1. A wastewater treatment system for a coke making facility, comprising: processing excess gas liquid discharged from a gas liquid circulation system together with contaminated wastewater from another discharge source in a wastewater treatment system including an activated sludge method. In the treatment method, at least an excess gas liquid is subjected to steam stripping to reduce the ammonia content before flowing into the wastewater treatment system so that the ammonia content brought into the wastewater treatment system is within a predetermined range, and A method for adjusting the amount of ammonia removed in steam stripping according to the amount of ammonia carried into wastewater.
ングに供したのち廃水処理系に流入させ、残部はスチー
ムストリッピングに供することなく廃水処理系に流入さ
せ、かつ両者の比率を調節することにより廃水処理系に
持込まれるアンモニア分を調節することを特徴とする請
求項1記載の方法。2. A part of the surplus gas liquid is supplied to a wastewater treatment system after being subjected to steam stripping, and the remainder is supplied to a wastewater treatment system without being subjected to steam stripping, and the ratio between the two is adjusted. 2. The method according to claim 1, wherein the amount of ammonia introduced into the wastewater treatment system is adjusted by the method.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2003112194A (en) * | 2001-10-09 | 2003-04-15 | Fuji Electric Co Ltd | Method for controlling nitrogen removing process |
JP2004514550A (en) * | 2000-12-01 | 2004-05-20 | トタル、フイナ、エルフ、フランス | Method and apparatus for continuously treating spent water of industrial origin by steam stripping. |
JP2007045852A (en) * | 2005-08-05 | 2007-02-22 | Nippon Steel Corp | Method and apparatus for purifying gasified gas and method for using gasified gas |
CN105948306A (en) * | 2016-05-12 | 2016-09-21 | 华陆工程科技有限责任公司 | Pretreatment and comprehensive utilization method of wastewater and waste gas produced during coal gasification |
-
1997
- 1997-10-29 JP JP29687197A patent/JP3755259B2/en not_active Expired - Fee Related
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2004514550A (en) * | 2000-12-01 | 2004-05-20 | トタル、フイナ、エルフ、フランス | Method and apparatus for continuously treating spent water of industrial origin by steam stripping. |
JP2003112194A (en) * | 2001-10-09 | 2003-04-15 | Fuji Electric Co Ltd | Method for controlling nitrogen removing process |
JP2007045852A (en) * | 2005-08-05 | 2007-02-22 | Nippon Steel Corp | Method and apparatus for purifying gasified gas and method for using gasified gas |
CN105948306A (en) * | 2016-05-12 | 2016-09-21 | 华陆工程科技有限责任公司 | Pretreatment and comprehensive utilization method of wastewater and waste gas produced during coal gasification |
CN105948306B (en) * | 2016-05-12 | 2018-09-21 | 华陆工程科技有限责任公司 | A kind of pretreatment of coal gasification waste water exhaust gas and method of comprehensive utilization |
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