JPH0694029B2 - Ammonia-containing wastewater treatment method - Google Patents
Ammonia-containing wastewater treatment methodInfo
- Publication number
- JPH0694029B2 JPH0694029B2 JP1065983A JP6598389A JPH0694029B2 JP H0694029 B2 JPH0694029 B2 JP H0694029B2 JP 1065983 A JP1065983 A JP 1065983A JP 6598389 A JP6598389 A JP 6598389A JP H0694029 B2 JPH0694029 B2 JP H0694029B2
- Authority
- JP
- Japan
- Prior art keywords
- ammonia
- wastewater
- absorption
- stripping
- catalyst
- 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.)
- Expired - Lifetime
Links
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明はアンモニア含有廃水の処理方法に係り、特に廃
水からアンモニアを放散処理した後の排ガスの処理方法
に関する。Description: TECHNICAL FIELD The present invention relates to a method for treating ammonia-containing wastewater, and more particularly to a method for treating exhaust gas after ammonia is diffused from wastewater.
廃水からNH3を放散する方法として、従来廃水に蒸気を
吹き込んで行うスチームストリツピング法、廃水にCa(O
H)2,NaOHなどのアルカリ剤を添加してpHを上昇せしめ空
気を吹き込むエアストリツピング法およびそれらを組み
合わせた方法が利用されている。放散アンモニアは硫酸
等の鉱酸に吸収させるか、あるいは白金系の触媒を用い
て酸化分解を行い、NH3が大気中に排出されないように
処理されている。As a method of dissipating NH 3 from wastewater, steam stripping method, which is conventionally performed by blowing steam into wastewater, Ca (O 2
An air striping method in which an alkaline agent such as (H) 2 or NaOH is added to raise pH to blow air, and a method combining them are used. The released ammonia is absorbed in a mineral acid such as sulfuric acid or oxidatively decomposed using a platinum-based catalyst so that NH 3 is not discharged into the atmosphere.
そのうち、NH3を硫酸で吸収する方法では、肥料として
有効な硫安を製造することができるが、廃水処理施設に
おいてはその製造工程（濃縮、精製等）が煩雑なため、
一般には放散アンモニアの処理としては、触媒による分
解方法が行われている。Among them, the method of absorbing NH 3 with sulfuric acid can produce ammonium sulfate effective as a fertilizer, but the production process (concentration, purification, etc.) of a wastewater treatment facility is complicated,
Generally, as a treatment of the emitted ammonia, a decomposition method using a catalyst is performed.
しかしながら、触媒による分解方法では、アンモニアの
分解が必ずしも完全に行われず、またNH3の一部がNOxに
まで酸化するため、完全な処理を行うためのプロセス構
成が複雑になり、また運転操作も煩雑になるという問題
があつた。さらに触媒は劣化が早く、また高価なため処
理費用が高くなるという欠点がある。However, in the catalytic decomposition method, ammonia is not always completely decomposed, and a part of NH 3 is oxidized to NOx, which complicates the process configuration for complete treatment and also requires operation. There was a problem that it became complicated. Further, the catalyst has a drawback that it is rapidly deteriorated and the treatment cost is high because it is expensive.
そこで、本発明の目的は、上記のような問題点のない、
簡単な設備で安価な触媒を用いた分解方法による排ガス
の処理方法を提供することにある。Therefore, an object of the present invention is to eliminate the above problems.
An object of the present invention is to provide a method for treating exhaust gas by a decomposition method using a simple facility and an inexpensive catalyst.
前記目的を達成するために、本発明では、アンモニアを
含有する廃水からアンモニアを放散し、放散アンモニア
を触媒で分解処理した後、残留するアンモニア及び／又
は副生する窒素酸化物を含有する排ガスを、吸収工程で
吸収液によつて吸収処理し、該吸収液をアンモニア放散
工程あるいは該廃水の貯留槽に注入することによるアン
モニア含有廃水の処理方法としたものである。In order to achieve the above-mentioned object, in the present invention, ammonia is discharged from wastewater containing ammonia, and after exhausted ammonia is decomposed by a catalyst, exhaust gas containing residual ammonia and / or nitrogen oxide by-produced is produced. The method for treating ammonia-containing wastewater is carried out by absorbing with an absorbing solution in the absorbing step and injecting the absorbing solution into the ammonia-dissipating step or the wastewater storage tank.
また、前記吸収工程においては、水による吸収とアルカ
リ水による吸収の２つの吸収液によつて吸収処理するの
がよい。In addition, in the absorption step, it is preferable to perform absorption treatment with two absorption liquids, one with water and the other with alkaline water.
次に、第１図の本発明の一実施態様に基づいて更に詳し
く説明する。Next, a more detailed description will be given based on the embodiment of the present invention shown in FIG.
廃水１は貯留槽２を経由し熱交換器３で加温されてスト
リツピング工程４に導入される。ストリツピング工程４
では、スチーム５よつてストリツピングされ、放散され
たNH3は予熱された空気６につて希釈されたのち、予熱
炉７で250〜350℃に加熱され、触媒分解工程８に導入さ
れる。触媒分解工程８では、NH3の大部分がN2とH2Oに酸
化分解される。触媒としては白金、パナジウムなどの市
販されているアンモニアの酸化分解触媒が全て利用でき
る。排ガスは熱交換器９で希釈用空気６と熱交換された
のち、残留NH3、副生NOx、その他残留ガスが吸収工程10
で吸収液により吸収処理される。吸収処理された吸収排
液12は貯留槽２あるいはストリツピング工程４に移送さ
れ再度ストリツピング処理が行われる。The wastewater 1 is heated in the heat exchanger 3 via the storage tank 2 and introduced into the stripping step 4. Stripping process 4
Then, NH 3 which has been stripped by the steam 5 and released is diluted with the preheated air 6 and then heated to 250 to 350 ° C. in the preheating furnace 7 and introduced into the catalytic decomposition step 8. In the catalytic decomposition step 8, most of NH 3 is oxidatively decomposed into N 2 and H 2 O. As the catalyst, all commercially available ammonia oxidative decomposition catalysts such as platinum and vanadium can be used. After the exhaust gas is heat-exchanged with the diluting air 6 in the heat exchanger 9, residual NH 3 , by-product NOx, and other residual gas are absorbed in the absorption process 10
Is absorbed by the absorbing solution. The absorbed drainage liquid 12 that has been absorbed is transferred to the storage tank 2 or the stripping process 4 and is subjected to the stripping process again.
ストリツピング工程の蒸気量は廃水量の10〜20％でよ
く、また、エアストリツピングを行う場合は、廃水量の
1000〜1500倍の空気が必要である。ストリツピング工程
のpHは10〜12程度がよく、特にエアストリツピングの場
合にはpHを10〜12程度にしておかないと良好なアンモニ
ア除去率を達成できない。The amount of steam in the stripping process may be 10 to 20% of the amount of wastewater, and in the case of air striping, the amount of wastewater
1000 to 1500 times more air is needed. The pH of the stripping step is preferably about 10 to 12, and particularly in the case of air stripping, a good ammonia removal rate cannot be achieved unless the pH is set to about 10 to 12.
なお、エアストリツピングの場合でも、触媒分解工程に
流入するガスのNH3濃度が高い場合には希釈用空気が必
要があり、ガスのNH3濃度は廃水中のNH3濃度によつて変
化するので、希釈用空気は導入するのが好ましい。Even when the Easuto rate ping, when the NH 3 concentration in the gas flowing into the catalytic decomposition process higher needs dilution air, NH 3 concentration of the gas is due connexion changes NH 3 concentration in the wastewater Therefore, it is preferable to introduce the dilution air.
残留NH3、副生NOxの吸収除去は単一の反応塔を用いて、
水で吸収してもよいが、吸収工程10の反応塔を酸、アル
カリ液用をそれぞれ１塔づつ直列に配備するとNH3,NOx
の除去率を向上することができる。吸収液12は貯留槽２
に移送するのが望ましい。これはストリツピングでは放
散しないNOxが貯留槽２において廃水に同伴された微生
物によつて還元されるからであり、またこれによつて廃
水の腐敗が防止されるからである。The absorption and removal of residual NH 3 and by-product NOx is performed using a single reaction tower.
It may be absorbed by water, but if one reaction tower for the absorption step 10 is installed in series for acid and one for alkali solution, NH 3 , NOx
The removal rate can be improved. Absorption liquid 12 is storage tank 2
It is desirable to transfer to. This is because NOx, which is not released by stripping, is reduced by the microorganisms entrained in the wastewater in the storage tank 2, and this also prevents the decay of the wastewater.
処理水13にBOD,CODが残留する場合にはさらに生物学的
あるいは物理化学的方法によつてそれらの汚濁成分を除
去することができる。When BOD and COD remain in the treated water 13, those polluted components can be further removed by a biological or physicochemical method.
以下、本発明を実施例により具体的に説明するが、本発
明はこの実施例に限定されるものではない。Hereinafter, the present invention will be specifically described by way of examples, but the present invention is not limited to these examples.
実施例１ 次の実施条件で第１図によつて行つた。Example 1 The procedure was as shown in FIG. 1 under the following conditions.
実施条件 廃 水 人口廃水 NH3−Ｎ 5000mg/l BOD 4800 〃 貯留槽 15 NH3ストリツピング塔 11（φ100mm,h1500mm） 排ガス吸収槽 ５×２（φ100mm,h800mm） 第１塔：水，第２塔：アルカリ水（pH10） 廃水処理量 ３／日 ストリツピング用空気量 ３／分 ストリツピング塔 pH12 水温 60℃ 触媒分解工程入口 ガス温度 230〜280℃ 触 媒 白金含有量 0.0018％のもの 排ガス吸収槽 第１塔 1.0／日 流出液量 （吸収液流量） 第２塔 0.5 〃 その結果を第１表、第２表に示す。Implementation conditions Wastewater Populated wastewater NH 3 -N 5000mg / l BOD 4800〃 Storage tank 15 NH 3 Stripping tower 11 (φ100mm, h1500mm) Exhaust gas absorption tank 5 × 2 (φ100mm, h800mm) 1st tower: Water, 2nd tower: Alkaline water (pH10) Wastewater treatment amount 3 / day Stripping air amount 3 / min Stripping tower pH12 Water temperature 60 ℃ Catalyst decomposition process inlet gas temperature 230-280 ℃ Catalyst platinum content 0.0018% Exhaust gas absorption tank 1st tower 1.0 / Day Effluent volume (absorption fluid flow rate) Second tower 0.5 〃 The results are shown in Tables 1 and 2.
第１表に示したように触媒分解工程の後段にさらに後処
理として触媒処理することなく、排ガス中の窒素分を除
去することができ、また第２表に示したようにストリツ
ピング流出液の窒素濃度を特に増加することもない。特
に吸収液を貯留槽に注入したものはストリツピング流出
液のNOx−Ｎ濃度も大幅に低くなつている。 As shown in Table 1, the nitrogen content in the exhaust gas can be removed without further catalytic treatment as a post-treatment after the catalytic decomposition step. Further, as shown in Table 2, the nitrogen in the stripping effluent can be removed. There is no particular increase in concentration. In particular, when the absorption liquid was injected into the storage tank, the NOx-N concentration in the stripping effluent was also significantly reduced.
以上のように本発明によれば、消耗が激しく、高価な触
媒を利用する従来の後段の触媒分解工程を、設備費が安
価で堅牢な吸収工程とすることが出来、また吸収液のNH
3を同一工程で再ストリツピングするのでプロセス構成
も簡単で処理水NH3−Ｎ濃度も安定して低減できるとい
う効果がある。As described above, according to the present invention, the conventional catalyst decomposing step of the latter stage, which consumes a lot of electricity and uses an expensive catalyst, can be made into a robust absorption step at low equipment cost, and the NH
Since 3 is restriped in the same step, the process configuration is simple and the concentration of treated water NH 3 —N can be reduced stably.
第１図は、本発明の一実施例を示す工程図である。 １……廃水、２……貯留槽、３……熱交換器、４……ス
トリツピング工程、５……スチーム、６……希釈空気、
７……予熱炉、８……触媒分解工程、９……熱交換器、
10……吸収工程、11……処理ガス、12……吸収排液FIG. 1 is a process drawing showing an embodiment of the present invention. 1 ... Wastewater, 2 ... Storage tank, 3 ... Heat exchanger, 4 ... Stripping process, 5 ... Steam, 6 ... Diluting air,
7 ... Preheating furnace, 8 ... Catalyst decomposition process, 9 ... Heat exchanger,
10 …… Absorption process, 11 …… Process gas, 12 …… Absorption drainage
───────────────────────────────────────────────────── フロントページの続き (72)発明者 吉田 伸二 神奈川県藤沢市本藤沢４丁目２番１号 株 式会社荏原総合研究所内 (56)参考文献 特開 昭47−20979（ＪＰ，Ａ) 特開 昭50−10635（ＪＰ，Ａ) 特開 昭53−88700（ＪＰ，Ａ) 特開 昭60−166021（ＪＰ，Ａ) 実開 昭50−8141（ＪＰ，Ｕ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Shinji Yoshida 4-2-1 Motofujisawa, Fujisawa-shi, Kanagawa Inside the EBARA Research Institute (56) Reference Japanese Patent Laid-Open No. 47-20979 (JP, A) Kai 50-10635 (JP, A) JP 53-88700 (JP, A) JP 60-166021 (JP, A) Actually open Sho 50-8141 (JP, U)
Claims (1)
を放散し、放散アンモニアを触媒で分解処理した後、残
留するアンモニア及び／又は副生する窒素酸化物を含有
する排ガスを、吸収工程で吸収液によつて吸収処理し、
該吸収液をアンモニア放散工程あるいは該廃水の貯留槽
に注入することを特徴とするアンモニア含有廃水の処理
方法。1. Ammonia is diffused from wastewater containing ammonia, and after decomposing the diffused ammonia with a catalyst, exhaust gas containing residual ammonia and / or by-produced nitrogen oxides is used as an absorption liquid in an absorption step. Absorption treatment,
A method for treating ammonia-containing wastewater, comprising injecting the absorption liquid into an ammonia diffusion step or a wastewater storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1065983A JPH0694029B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1065983A JPH0694029B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02245285A JPH02245285A (en) | 1990-10-01 |
| JPH0694029B2 true JPH0694029B2 (en) | 1994-11-24 |
Family
ID=13302752
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1065983A Expired - Lifetime JPH0694029B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0694029B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102908894A (en) * | 2012-11-09 | 2013-02-06 | 湖南高安新材料有限公司 | Ammonia tail gas treatment device and method for preparing nitride for electronic industry |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE60120999T2 (en) * | 2000-08-10 | 2007-01-25 | Babcock-Hitachi K.K. | METHOD AND DEVICE FOR TREATING AMMONIA-CONTAINING WASTEWATER |
| CN102241432A (en) * | 2010-05-11 | 2011-11-16 | 安徽南风环境工程技术有限公司 | Special equipment and method for treating ammonia nitrogen wastewater |
| CN112551776B (en) * | 2020-11-17 | 2024-02-02 | 西安净源水处理科技有限公司 | High-concentration ammonia nitrogen wastewater treatment equipment and process |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2319934A1 (en) * | 1973-04-19 | 1974-11-07 | Kalle Ag | METHOD AND DEVICE FOR REMOVING AMMONIA FROM THE AIR EXHAUST OF COPY MACHINES |
| JPS508141U (en) * | 1973-05-23 | 1975-01-28 | ||
| JPS516352A (en) * | 1974-07-09 | 1976-01-19 | Mitsubishi Heavy Ind Ltd | ANMONIAGANJUHAIEKINO SHORIHOHO |
| JPS5388700A (en) * | 1977-01-14 | 1978-08-04 | Tsukishima Kikai Co | Method of recovering ammonia from waste water |
| JPS5951358A (en) * | 1982-09-18 | 1984-03-24 | Nippon Tectron Co Ltd | Automatic analyzer |
| JPS60166021A (en) * | 1984-02-07 | 1985-08-29 | Kawasaki Heavy Ind Ltd | Deodorization of waste gas from sludge incinerating furnace |
-
1989
- 1989-03-20 JP JP1065983A patent/JPH0694029B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102908894A (en) * | 2012-11-09 | 2013-02-06 | 湖南高安新材料有限公司 | Ammonia tail gas treatment device and method for preparing nitride for electronic industry |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02245285A (en) | 1990-10-01 |
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