JP4000642B2 - Method for treating surplus gas liquid in coke production facility - Google Patents
Method for treating surplus gas liquid in coke production facility Download PDFInfo
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- JP4000642B2 JP4000642B2 JP31180297A JP31180297A JP4000642B2 JP 4000642 B2 JP4000642 B2 JP 4000642B2 JP 31180297 A JP31180297 A JP 31180297A JP 31180297 A JP31180297 A JP 31180297A JP 4000642 B2 JP4000642 B2 JP 4000642B2
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- Prior art keywords
- gas liquid
- ammonia
- surplus gas
- circulation system
- surplus
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Description
【０００１】
【発明の属する技術分野】
本発明は、それぞれ独立したガス液の循環系を有する複数の炉団からなるコークス製造設備における、余剰ガス液の処理方法に関するものである。
【０００２】
【従来の技術】
コークスの製造では、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などを除去したのち、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、循環系の流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。
【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。コークス製造設備では、廃水処理系に持込まれるアンモニア分の大部分は、通常は余剰ガス液が持込むものである。従って余剰ガス液の持込むアンモニア分の量を低減させると、廃水処理系においてアンモニア分を除去する負担が軽減される。廃水処理系においてアンモニア分を除去する好ましい態様の一つは、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の濃度を低減させる方法である。この場合において、余剰ガス液の一部はスチームストリッピングに供してから、残部はスチームストリッピングに供することなく、後続する活性汚泥処理を含む廃水処理系に流入させ、かつ余剰ガス液のうちスチームストリッピングに供する比率を、後続する廃水処理系へのアンモニアの持込量を許容限度内とするためにスチームストリッピングで除去すべきアンモニア量に応じて調節するならば、スチームの消費量も大幅に低減できる。
【０００４】
余剰ガス液が持込むアンモニア分の量は、余剰ガス液の量とそのアンモニア分の濃度により定まる。しかし余剰ガス液の量は、コークス炉に装入される石炭の性状及びコークスの生産量により定まるので、削減は極めて困難である。従って余剰ガス液が持込むアンモニア量を削減するには、余剰ガス液中のアンモニア分の濃度を低減させることが必要である。本発明は複数の独立したガス液循環系を有するコークス製造設備において、廃水処理系に排出される余剰ガス液中のアンモニア分の濃度を全体として低下させる方法を提供しようとするものである。
【０００５】
【課題を解決するための手段】
本発明によれば、それぞれ独立したガス液の循環系を有する複数の炉団から成るコークス製造設備において、各循環系から余剰ガス液を余剰ガス液の処理系に排出する代りに、ガス液中のアンモニア分濃度の高い循環系からその余剰ガス液をアンモニア分濃度の低い循環系に排出し、アンモニア分濃度の低い循環系から過剰のガス液を余剰ガス液として余剰ガス液の処理系に排出することにより、処理すべき余剰ガス液中のアンモニア分濃度を全体として低下させることができる。
【０００６】
【発明の実施の形態】
本発明について詳細に説明すると、大規模なコークス製造設備では、コークス炉は通常は炉団毎に時間をおいて順次建設される。この建設時期の相異により、多くの場合には、各炉団はその仕様が若干なりとも異なっている。各炉団にはガス液の循環系が設置されているが、このガス液の循環系は多くの場合には炉団毎に独立して設置される。前述のように各炉団は建設時期が異なるので、通常はガス液の循環系も含めてその仕様も若干なりとも異なっている。このような仕様の相異や、各炉団に装入される石炭の性状、更には各循環系の操作条件の相異により、複数の独立したガス液循環系を有するコークス製造設備では、各循環系のガス液のアンモニア分濃度は一致しないのが通常であり、場合によっては相当に大きな相異を生ずることもある。
【０００７】
本発明はこの点に着目してなされたもので、ガス液中のアンモニア分濃度の高い循環系からその余剰ガス液を、ガス液中のアンモニア分濃度の低い循環系に排出し、ガス液中のアンモニア分濃度の低い循環系からこの循環系で発生する余剰ガス液と他の循環系から受入れた余剰ガス液との和に等しい量のガス液を、余剰ガス液として余剰ガス液の処理系に排出する。このようにすれば、余剰ガス液処理系が受入れる余剰ガス液量は同一で、しかもその全量がアンモニア分濃度の低い循環系のガス液なので、余剰ガス液処理系のアンモニア負荷は大いに軽減される。また、循環系で発生する余剰ガス液は、循環液量のせいぜい数％程度なので、上記のようにアンモニア分濃度の高い余剰ガス液をアンモニア分濃度の低い循環系に流入させても、この循環系の運転には全く支障を生じない。
【０００８】
本発明の実施の態様の１例について説明すれば、アンモニア分の濃度が３４００ｍｇ／ｌ（遊離アンモニア２０００ｍｇ／ｌ、固定アンモニア１４００ｍｇ／ｌ）、二酸化炭素濃度が１０００ｍｇ／ｌ、硫化水素濃度が２００ｍｇ／ｌの１号ガス液循環系と、アンモニア分濃度４４００ｍｇ／ｌ（遊離アンモニア３０００ｍｇ／ｌ、固定アンモニア１４００ｍｇ／ｌ）、二酸化炭素濃度１５００ｍｇ／ｌ、硫化水素濃度３００ｍｇ／ｌの２号ガス液循環系とを有するコークス製造設備において、各循環系からそれぞれ４０ｍ3 ／ｈｒの余剰ガス液を排出すると、そのアンモニア量は３１２ｋｇ／ｈｒとなる。しかし、２号ガス液循環系から４０ｍ3 ／ｈｒのガス液を１号ガス液循環系に流入させ、１号ガス液循環系から８０ｍ3 ／ｈｒのガス液をガス液処理系に排出すると、１号ガス液循環系の遊離アンモニア濃度が若干上昇するので、そのアンモニア量は約２８０ｋｇ／ｈｒであって、約３２ｋｇ／ｈｒだけガス液処理系に持込まれるアンモニア量が減少する。
【０００９】
また、活性汚泥処理を含む廃水処理系に持込まれる余剰ガス液中のアンモニアの許容量を２３０ｋｇ／ｈｒとすると、前者の場合には８２ｋｇ／ｈｒ、後者の場合には５０ｋｇ／ｈｒのアンモニアを予め除去しなくてはならない。アンモニアの除去をスチームストリッピングで行うものとし、かつスチームストリッピングで遊離アンモニアの９０％が除去されるとすると、前者の場合には１号ガス液循環系及び２号ガス液循環系の合計の排出量８０ｔ／ｈｒのうち３６．５ｔ／ｈｒをスチームストリッピングに供する必要がある。これに対し後者の場合には２６．５ｔ／ｈｒをスチームストリッピングに供すればよく、スチームストリッピングに供する余剰ガス液量を１０ｔ／ｈｒ、すなわち２７．４％ほど削減でき、従ってスチーム消費量もそれだけ低減できる。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method for treating surplus gas liquid in a coke production facility composed of a plurality of furnace groups each having an independent gas liquid circulation system.
[0002]
[Prior art]
In the production of coke, water is injected into the high-temperature coke oven gas flowing out from the coke oven to cool the gas and condense the tar content. 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 collected and the tar content and the like are removed and then recycled for injection into coke oven gas. This water is called a gas liquid and absorbs ammonia in the coke oven gas and contains several thousand ppm of ammonia. A part of this ammonia is present as fixed ammonia which forms a salt with an acid, and the other as free ammonia. The coke oven gas flowing out of the coke oven contains coal adhering water and water produced from coal during the dry distillation process as water vapor. Therefore, the gas liquid gradually increases by the amount of water generated from the water vapor, so that a part of the gas liquid is extracted from the circulation system of the gas liquid so that the flow rate of the circulation system falls within a predetermined range. This extracted gas liquid is a surplus gas liquid that contains several thousand ppm of ammonia as described above, and is highly contaminated with organic matter. It cannot be discharged into the water area. In the coke production facility, various waste water is discharged from the coke oven gas refining process and tar processing process in addition to the surplus gas liquid. Many wastewater from these various sources also contain substantial amounts of ammonia and organic matter, and, like surplus gas liquids, they are discharged into public waters unless they have been subjected to activated sludge treatment. It is not possible.
[0003]
[Problems to be solved by the invention]
The concentration of ammonia in wastewater discharged into public water areas is strictly regulated. In coke production facilities, most of the ammonia that is brought into the wastewater treatment system is usually brought in by surplus gas liquid. Therefore, if the amount of ammonia contained in the surplus gas liquid is reduced, the burden of removing ammonia in the wastewater treatment system is reduced. One of the preferred embodiments for removing the ammonia component in the wastewater treatment system is a method for reducing the concentration of the ammonia component by subjecting the surplus gas liquid to steam stripping. In this case, after a part of the surplus gas liquid is subjected to steam stripping, the remaining part is not subjected to steam stripping and is allowed to flow into a wastewater treatment system including the subsequent activated sludge treatment, and steam of the surplus gas liquid. If the ratio used for stripping is adjusted according to the amount of ammonia to be removed by steam stripping in order to keep the amount of ammonia brought into the subsequent wastewater treatment system within the allowable limit, the consumption of steam will also be greatly increased. Can be reduced.
[0004]
The amount of ammonia contained in the surplus gas liquid is determined by the amount of surplus gas liquid and the concentration of the ammonia content. However, since the amount of surplus gas liquid is determined by the properties of the coal charged into the coke oven and the amount of coke produced, it is extremely difficult to reduce. Therefore, in order to reduce the amount of ammonia brought in by the surplus gas liquid, it is necessary to reduce the concentration of ammonia in the surplus gas liquid. The present invention intends to provide a method for reducing the concentration of ammonia in the surplus gas liquid discharged to the wastewater treatment system as a whole in a coke production facility having a plurality of independent gas liquid circulation systems.
[0005]
[Means for Solving the Problems]
According to the present invention, in the coke production facility comprising a plurality of furnace groups each having an independent gas liquid circulation system, instead of discharging the excess gas liquid from each circulation system to the surplus gas liquid treatment system, The excess gas liquid is discharged from the circulation system having a high ammonia concentration to the circulation system having a low ammonia concentration, and the excess gas liquid is discharged from the circulation system having a low ammonia concentration to the treatment system of the excess gas liquid as a surplus gas liquid. By doing this, the ammonia concentration in the surplus gas liquid to be processed can be lowered as a whole.
[0006]
DETAILED DESCRIPTION OF THE INVENTION
The present invention will be described in detail. In a large-scale coke production facility, coke ovens are usually constructed sequentially with a time interval for each furnace group. Due to the difference in construction time, in many cases, the specifications of each furnace group are slightly different. Each furnace group is provided with a gas liquid circulation system. In many cases, this gas liquid circulation system is installed independently for each furnace group. As mentioned above, the construction period of each furnace group is different, so the specifications are usually slightly different, including the gas liquid circulation system. Due to the differences in specifications, the properties of the coal charged into each furnace group, and the operating conditions of each circulation system, coke production facilities with multiple independent gas-liquid circulation systems Normally, the ammonia concentration of the gas liquid in the circulation system does not match, and in some cases, a considerably large difference may occur.
[0007]
The present invention has been made paying attention to this point, and discharges the surplus gas liquid from the circulation system having a high ammonia content concentration in the gas liquid to the circulation system having a low ammonia content concentration in the gas liquid. A surplus gas liquid treatment system that uses as a surplus gas liquid an amount of gas liquid equal to the sum of the surplus gas liquid generated in this circulation system from the circulation system having a low ammonia content concentration and the surplus gas liquid received from another circulation system To discharge. In this way, the surplus gas liquid treatment system accepts the same amount of surplus gas liquid, and the total amount is a circulating gas liquid with a low ammonia concentration, so the ammonia load of the surplus gas liquid treatment system is greatly reduced. . In addition, since the surplus gas liquid generated in the circulation system is at most several percent of the circulation liquid volume, even if the surplus gas liquid with a high ammonia concentration is introduced into the circulation system with a low ammonia concentration as described above, this circulation There is no problem in the operation of the system.
[0008]
An example of the embodiment of the present invention will be described. The concentration of ammonia is 3400 mg / l (free ammonia 2000 mg / l, fixed ammonia 1400 mg / l), the carbon dioxide concentration is 1000 mg / l, and the hydrogen sulfide concentration is 200 mg / l. No. 1 gas liquid circulation system, No. 2 gas liquid circulation system with ammonia concentration of 4400 mg / l (free ammonia 3000 mg / l, fixed ammonia 1400 mg / l), carbon dioxide concentration of 1500 mg / l, hydrogen sulfide concentration of 300 mg / l In the coke production facility having the above, when 40 m 3 / hr of excess gas liquid is discharged from each circulation system, the ammonia amount becomes 312 kg / hr. However, if 40m 3 / hr gas liquid flows from No. 2 gas liquid circulation system into No. 1 gas liquid circulation system and 80m 3 / hr gas liquid is discharged from No. 1 gas liquid circulation system to gas liquid treatment system, Since the free ammonia concentration in the No. 1 gas-liquid circulation system slightly increases, the amount of ammonia is about 280 kg / hr, and the amount of ammonia brought into the gas-liquid treatment system decreases by about 32 kg / hr.
[0009]
Further, assuming that the allowable amount of ammonia in the surplus gas liquid brought into the wastewater treatment system including activated sludge treatment is 230 kg / hr, 82 kg / hr in the former case and 50 kg / hr in the latter case are preliminarily added. Must be removed. Assuming that ammonia is removed by steam stripping and 90% of free ammonia is removed by steam stripping, in the former case, the total of No. 1 gas-liquid circulation system and No. 2 gas-liquid circulation system It is necessary to use 36.5 t / hr for steam stripping out of the discharged amount 80 t / hr. On the other hand, in the latter case, 26.5 t / hr may be used for steam stripping, and the amount of excess gas liquid used for steam stripping can be reduced by 10 t / hr, that is, 27.4%. Can be reduced accordingly.
Claims (2)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31180297A JP4000642B2 (en) | 1997-11-13 | 1997-11-13 | Method for treating surplus gas liquid in coke production facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31180297A JP4000642B2 (en) | 1997-11-13 | 1997-11-13 | Method for treating surplus gas liquid in coke production facility |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH11140452A JPH11140452A (en) | 1999-05-25 |
| JP4000642B2 true JP4000642B2 (en) | 2007-10-31 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP31180297A Expired - Fee Related JP4000642B2 (en) | 1997-11-13 | 1997-11-13 | Method for treating surplus gas liquid in coke production facility |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4000642B2 (en) |
-
1997
- 1997-11-13 JP JP31180297A patent/JP4000642B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH11140452A (en) | 1999-05-25 |
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