JPS59123599A - Treatment of waste water containing nitrogenous sulfer compound and ammonia - Google Patents
Treatment of waste water containing nitrogenous sulfer compound and ammoniaInfo
- Publication number
- JPS59123599A JPS59123599A JP22757782A JP22757782A JPS59123599A JP S59123599 A JPS59123599 A JP S59123599A JP 22757782 A JP22757782 A JP 22757782A JP 22757782 A JP22757782 A JP 22757782A JP S59123599 A JPS59123599 A JP S59123599A
- Authority
- JP
- Japan
- Prior art keywords
- stage
- nitrification
- nitrifying
- liquid
- compd
- 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 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims description 40
- 229910021529 ammonia Inorganic materials 0.000 title claims description 7
- 150000001875 compounds Chemical class 0.000 title description 31
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 title 1
- 238000000034 method Methods 0.000 claims description 41
- 238000000354 decomposition reaction Methods 0.000 claims description 10
- 238000006386 neutralization reaction Methods 0.000 claims description 7
- -1 nitrogen-containing sulfur compounds Chemical class 0.000 claims description 7
- 239000007788 liquid Substances 0.000 abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 20
- 230000001546 nitrifying effect Effects 0.000 abstract description 16
- 239000002253 acid Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 150000001408 amides Chemical class 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 230000003247 decreasing effect Effects 0.000 abstract description 2
- 230000003472 neutralizing effect Effects 0.000 abstract description 2
- 230000007935 neutral effect Effects 0.000 abstract 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 13
- 239000000243 solution Substances 0.000 description 13
- 239000003795 chemical substances by application Substances 0.000 description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000003638 chemical reducing agent Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 3
- 238000005273 aeration Methods 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000010979 pH adjustment Methods 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009435 amidation Effects 0.000 description 1
- 238000007112 amidation reaction Methods 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- ZVUZTTDXWACDHD-UHFFFAOYSA-N gold(3+);trinitrate Chemical compound [Au+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O ZVUZTTDXWACDHD-UHFFFAOYSA-N 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 125000002349 hydroxyamino group Chemical group [H]ON([H])[*] 0.000 description 1
- 150000003949 imides Chemical class 0.000 description 1
- 229940005654 nitrite ion Drugs 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、石炭火力発電所の脱硝脱硫廃水など、アンモ
ニアと、同一分子内に窒素及び硫黄を含む化合物（含窒
素硫黄化合物、以下、ＮＳ化合物と略記する）を含有す
る廃水からこれらの化合物を除去する方法に関するもの
である。Detailed Description of the Invention The present invention is directed to denitrification and desulfurization wastewater from coal-fired power plants that contain ammonia and a compound containing nitrogen and sulfur in the same molecule (nitrogen-containing sulfur compound, hereinafter abbreviated as NS compound). The present invention relates to a method for removing these compounds from wastewater.
石炭火力発電所の廃水中にはＮＨ３（アンモニア）と、
ＣＯＤ成分となるイミドジスルホン酸（ＮＨ（ＳＯ３）
： ）、ハイドロオキシモノスルホン酸（ＮＨ（ＯＨ）
（ＳＯ３） ）などのＮＳ化合物が含有されている。こ
のようなＮＳ化合物は微生物では分解できないため、現
在の実用的な処理方法では、第（１）式
％式％（１）
Ｋ示す如く、例えばイミドジスルホン酸をｐＨ２近傍、
８０℃前後でアミド化したのち、さらに第（２）弐ＮＨ
２ＳＯ３＋ＮＯ２−＋ Ｎ２ ＋ＳＯ４＋Ｈ２０−−−
山（２）に示すように酸性下でＮＯ２−（亜硝酸イオン
）と反応せしめてＮ２ガスにまで分解し除去している。Wastewater from coal-fired power plants contains NH3 (ammonia),
Imidodisulfonic acid (NH(SO3)), which is a COD component
: ), hydroxymonosulfonic acid (NH(OH)
Contains NS compounds such as (SO3) ). Since such NS compounds cannot be decomposed by microorganisms, in the current practical treatment method, for example, imidodisulfonic acid is treated at around pH 2, as shown in formula (1).
After amidation at around 80°C, the second (2) NH
2SO3+NO2-+ N2 +SO4+H20--
As shown in the mountain (2), it is reacted with NO2- (nitrite ion) under acidic conditions, decomposed into N2 gas, and removed.
しかして、ＮＨ３の硝化、脱窒およびこのようなＮＳ化
合物除去方法が採用されている従来の火力発電所の廃水
処理方法について第１図を参照して説明すると、廃水１
はＮＳ化合物分解工程２に流入し水温８０℃、酸６の添
加によってｐＨ２に調整されてイミドｍＮｓ化合物がア
ミド型ＮＳ化合物に加水分解されたのち、中和槽４でア
ルカリ剤（例えば消石灰）５によって中和され、熱交換
あるいは冷却水の注入によって水温が低下されたのち、
循環脱窒液１４とともに好気的条件にある硝化工程６に
流入し、廃水１のＮ′Ｈ３は硝化菌の作用によってＮＯ
ｘに硝化される。循環脱窒液１４の循環は、硝化に際し
て生ずるＨ＋を脱窒に際して生ずるアルカリ分で中和す
るだめであるが、不足分は別途中和用アルカリ剤（例え
ばＮａＯＨ） ７が注入される。硝化工程乙には硝化菌
の付着した媒体が充填されており、硝化反応はＮＯ２が
生成することを前提に運転される。The conventional wastewater treatment method for thermal power plants that employs NH3 nitrification, denitrification, and NS compound removal methods will be explained with reference to Figure 1.
flows into the NS compound decomposition step 2, where the water temperature is 80°C and the pH is adjusted to 2 by adding acid 6 to hydrolyze the imide mNs compound into an amide type NS compound. After the water temperature is lowered by heat exchange or injection of cooling water,
It flows into the nitrification process 6 under aerobic conditions together with the circulating denitrification liquid 14, and the N'H3 of the wastewater 1 is converted to NO by the action of nitrifying bacteria.
It is nitrified by x. The purpose of circulating the denitrifying liquid 14 is to neutralize H+ produced during nitrification with alkaline content produced during denitrification, but an alkaline agent (for example, NaOH) 7 for neutralization is separately injected to compensate for the deficiency. Nitrification process B is filled with a medium to which nitrifying bacteria are attached, and the nitrification reaction is operated on the premise that NO2 is produced.
硝化液は次にＮＳ化合物除去工程８に流入し酸９によっ
てｐＨが３以下になるように調整される。The nitrifying solution then flows into an NS compound removal step 8, where the pH is adjusted to 3 or less using an acid 9.
ＮＳ化合物分解工程２で生成したアミド型ＮＳ化合物は
ｐＨ３以下、ＮＯ２の存在下でＮ２ガスに分解されたの
ち、中和槽１０に流入し、アルカリ剤（例えばＮａＯＨ
） １１によって中和されたのち、好気的条件にあり脱
窒菌の付着した媒体が充填されている脱窒工程１２に流
入し、メタノールなどの還元剤１６が注入され、ＮＯ２
はＮ２ガスに分解除去される。The amide type NS compound generated in the NS compound decomposition step 2 is decomposed into N2 gas at a pH of 3 or less in the presence of NO2, and then flows into the neutralization tank 10 where it is treated with an alkaline agent (e.g. NaOH).
) After being neutralized by 11, it flows into the denitrification step 12 which is under aerobic conditions and is filled with a medium to which denitrifying bacteria are attached, where a reducing agent 16 such as methanol is injected and the NO2
is decomposed into N2 gas and removed.
脱窒反応で液中のアルカリ変分が増加するので、このア
ルカリ変分を硝化工程乙の中和剤に利用するため大部分
が硝化工程乙に循環され、残部は好気的条件にあるばっ
気工程１５に流入し、脱窒液中に残留する還元剤が酸化
分解されたのち濾過工程１６でＳＳが除去され、放流あ
るいはさらに高度の処理を受けて放流される。Since the denitrification reaction increases the alkaline content in the liquid, most of this alkaline content is recycled to the nitrification process (B) to be used as a neutralizing agent in the nitrification process (B), and the remainder is left in the aerobic condition. After the reducing agent remaining in the denitrification liquid is oxidized and decomposed, SS is removed in a filtration step 16, and the denitrification liquid is discharged or subjected to further advanced treatment.
ＮＳ化合物とＮ０丁の反応は通常、Ｎ０２−Ｎ／Ｎｓ化
合物−Ｎ中１．５程度で行われるが、ＮＳ化合物−Ｎは
硝化液中のＮＯ２Ｎに比べけるかに少ないので、生成し
たＮＯ２Ｎのζ１とんどは脱窒工程１２で除去される。The reaction between the NS compound and N0 is usually carried out at about 1.5% in N02-N/Ns compound-N, but since the amount of NS compound-N is much smaller than that of NO2N in the nitrification solution, the amount of NO2N produced is Most of ζ1 is removed in the denitrification step 12.
しかしながら、以上の従来方法は、ｐｎ調整に消費され
る薬品の量が多いため、ランニングコストが高くなると
いう大きな欠点があり、そのうえ第（３）式
％式％
（３）
に示すようにＮＨ３がＮＯａ （硝酸イオン）まで硝化
されてしまうことがあり、安定してＮＯ２を生成できな
いため、ＮＳ化合物の除去率が低下し、処理水中のＣＯ
Ｄを当初の目標値まで除去できない場合が生じている。However, the conventional method described above has the major drawback of increasing running costs due to the large amount of chemicals consumed for pn adjustment. NOa (nitrate ions) may be nitrified, making it impossible to stably generate NO2, reducing the removal rate of NS compounds and reducing CO in the treated water.
There are cases where D cannot be removed to the original target value.
本発明は、ｐＨ調整用の薬品を節減し、さらに安定した
亜硝酸型硝化を行うことにより、上記従来法の欠点を解
消することを目的とするものである。The present invention aims to eliminate the above-mentioned drawbacks of the conventional method by reducing the amount of pH adjusting chemicals and performing more stable nitrite-type nitrification.
すなわち本発明は１．アンモニアおよびＮＳ化合物を含
む廃水の処理方法において、ＮＳ化合物分解除去工程、
中和工程、複数段に分割された生物学的硝化工程及び生
物学的脱窒工程を順次廃水の流下方向に設置し、前記分
割された硝化工程の前部硝化工程の硝化液の一部を前記
ＮＳ化合物分解除去工程へ循環して硝化液中のＮＯ２（
亜硝酸イオン）と廃水中のＮＳ化合物とを反応せしめる
ことによってＮＳ化合物を除去し、循環しない残部の硝
化液を前記脱窒工程から循環した脱窒液と共に前記分割
された硝化工程の後部硝化工程に通液して液中に残留す
るアンモニアを硝化したのち、液中のＮＯｘ （ＮＯ２
及び／又はＮＯ３）を前記脱窒工程で除去することを特
徴とするものである。That is, the present invention has 1. In a method for treating wastewater containing ammonia and NS compounds, an NS compound decomposition and removal step;
A neutralization process, a biological nitrification process divided into multiple stages, and a biological denitrification process are sequentially installed in the downstream direction of wastewater, and a part of the nitrification liquid from the front nitrification process of the divided nitrification process is NO2 (
NS compounds are removed by reacting nitrite ions) with NS compounds in the wastewater, and the remaining nitrification solution that is not circulated is used together with the denitrification solution circulated from the denitrification step in the subsequent nitrification step of the divided nitrification step. After passing the liquid through the liquid to nitrify the ammonia remaining in the liquid, NOx (NO2
and/or NO3) is removed in the denitrification step.
次に、本発明の一実施態様について第２図に基づいて説
明する。Next, one embodiment of the present invention will be described based on FIG. 2.
廃水１は水温８０℃、酸乙によってｐＨ２に調整された
ＮＳ化合物分解除去工程１８に流入し、廃水１中のＮＳ
化合物はアミド型ＮＳ化合物に加水分解され、さらに循
環硝化液１７中のＮＯｚと反応してＮ２ガスあるいはｌ
’Ｊ２０ガスに分解除去される。上記加水分解反応、ガ
ス化反応とも高水温、低ｐＨはど反応が促進される。Ｎ
Ｓ化合物が除去された液は中和槽４で中性付近に中和さ
れ、熱交換あるいは冷水の注入によって４０℃程度にま
で水温降下したのち、第１硝化工程６−１に流入し、廃
水１中のＮＨ３の一部が硝化され、さらに次の第２硝化
工程６−２で残部のＮＨ３の一部が硝化される。The wastewater 1 flows into the NS compound decomposition and removal step 18 where the water temperature is 80°C and the pH is adjusted to 2 with acid.
The compound is hydrolyzed into an amide-type NS compound, and further reacts with NOz in the circulating nitrification solution 17 to produce N2 gas or l
'It is decomposed and removed into J20 gas. Both the hydrolysis reaction and the gasification reaction are accelerated by high water temperature and low pH. N
The liquid from which the S compounds have been removed is neutralized to near neutrality in the neutralization tank 4, and the water temperature is lowered to about 40°C by heat exchange or injection of cold water, and then flows into the first nitrification step 6-1, where it is treated as wastewater. A part of NH3 in 1 is nitrified, and a part of the remaining NH3 is further nitrified in the next second nitrification step 6-2.
硝化工程６で硝化反応をＮＯ２で止めるためには、前述
の第（３）式から判るように硝酸菌を失活するとよく、
そのだめには水温を４０〜４２℃程度の高温に維持およ
び／又はｐＨを７．５近傍以上にして液中のＮＨ３濃度
を高く保持すると効果的である。第１硝化工程６−１、
第２硝化工程６−２でＮＨ３を残留せしめるためには、
これらの硝化工程のＮＨ３負荷を過大にするか、あるい
は酸素供給量を制限するなどの装置設計、運転操作の°
工夫を行えばよい。In order to stop the nitrification reaction with NO2 in the nitrification step 6, it is best to deactivate the nitrate bacteria, as seen from equation (3) above.
To prevent this, it is effective to maintain the water temperature at a high temperature of about 40 to 42°C and/or to maintain the pH in the vicinity of 7.5 or higher to maintain a high NH3 concentration in the liquid. First nitrification step 6-1,
In order to make NH3 remain in the second nitrification step 6-2,
Equipment design and operational changes such as increasing the NH3 load in the nitrification process or limiting the amount of oxygen supplied
All you have to do is come up with some ideas.
しかして、ＮＯ２とＮＨａの混合した硝化液は第１硝化
工程６−１および／又は第２硝化工程６−２からＮＳ化
合物分解除去工程１８に前記循環硝化液１７として循環
される。これらの硝化工程にはｐＨ調整用のアルカリ剤
７が注入されるが、ＮＨ３の残留のだめｐＨが低下しな
ければ勿論注入は不要であり、また第３硝化士程６−６
、第４硝化工程６−４でｐＨ低下が生ずれば、図示して
いないが両硝化工程６−３゜６−４のいずれかあるいは
両方にアルカリ剤７を注入すればよい。Thus, the nitrified solution containing NO2 and NHa is circulated as the circulating nitrified solution 17 from the first nitrification step 6-1 and/or the second nitrification step 6-2 to the NS compound decomposition and removal step 18. In these nitrification processes, an alkaline agent 7 for pH adjustment is injected, but unless the pH is lowered due to residual NH3, injection is of course not necessary.
If the pH decreases in the fourth nitrification step 6-4, an alkaline agent 7 may be injected into either or both of the nitrification steps 6-3 and 6-4, although not shown.
流出硝化液を循環する硝化工程を２分割しているのは、
廃水１の流入口に向かって段階的にＮＨ３濃度を高くす
ることによりＮｏ夏の生成を促進するためであり、循環
硝化液１７の取水口を各硝化工程＜ ６−１ 、６−２
）に分けているのは、最もＮｏ夏濃度の高い部分より
随童に循環硝化液１７をとるためである。The nitrification process that circulates the effluent nitrification liquid is divided into two parts.
This is to promote the generation of No summer by increasing the NH3 concentration stepwise toward the inlet of the wastewater 1, and the intake of the circulating nitrification liquid 17 is connected to each nitrification process <6-1, 6-2.
) The reason for this is to take the circulating nitrifying liquid 17 from the part with the highest No summer concentration.
第３硝化工程６−６、第４硝化工程６−４では前段の硝
化工程で残留したＩ’ＪＨ３が完全に硝化され、生成し
たＮＯｘは脱窒工程１２で脱窒され、脱窒水の一部は第
３硝化工程６−６および／又は第４硝化工程６−４に循
環され、残部はばつ気工程１５に流入し、脱窒工程１２
で添加された還元剤の残留分が酸化分解されたのち、濾
過工程１６あるいはさらに高度の処理を受けたのち放流
される。In the third nitrification step 6-6 and the fourth nitrification step 6-4, I'JH3 remaining in the previous nitrification step is completely nitrified, and the generated NOx is denitrified in the denitrification step 12, and part of the denitrified water is A portion is recycled to the third nitrification step 6-6 and/or the fourth nitrification step 6-4, and the remainder flows into the aeration step 15 and denitrification step 12.
After the residual amount of the reducing agent added in step 1 is oxidized and decomposed, it is subjected to a filtration step 16 or a more advanced treatment and then discharged.
循環脱窒液１４は後段の硝化工程（６−３，＜５−４）
に循環されるが、これは前段の硝化工程（６−１、６−
２）の残留ＮＨ３を循環脱窒液１４で希釈せずに高濃度
に保つことにより亜硝酸化金促進し、かつ循環硝化液１
７中のＮＯ２’ａ度を高濃度に維持するだめに行われる
。The circulating denitrification liquid 14 is used in the subsequent nitrification process (6-3, <5-4)
This is recycled to the previous nitrification process (6-1, 6-
By keeping the residual NH3 in 2) at a high concentration without diluting it with the circulating denitrifying solution 14, gold nitrite oxide is promoted, and the circulating nitrifying solution 1
This is done in order to maintain a high concentration of NO2'a in the water.
硝化工程乙の分割はＮＨ３を段階的に残留させ、Ｎｏ２
の生成を促進するためのものであるから、その分割数は
特に限定されるわけではなく、最少２分割から数十分割
まで分割可能であるが、実用的な分割数は２〜５程度で
ある。The division of nitrification process B leaves NH3 in stages, and No2
Since the purpose is to promote the generation of .
前記硝化工程６、脱窒工程１２、ばっ気工程１５は微生
物の付着する媒体を充填させたものが望ましく、充填部
は流動床でも固定床でもよい。但し、浮遊汚泥法は各工
程に固液分離工程を設けて返送しなければならないので
、プロセスが複雑になる。The nitrification step 6, denitrification step 12, and aeration step 15 are preferably filled with a medium to which microorganisms adhere, and the filling section may be a fluidized bed or a fixed bed. However, the suspended sludge method requires a solid-liquid separation step for each step before being returned, making the process complicated.
脱窒液の循環は、前述のように脱窒液のアルカリ分で硝
化工程乙の酸を中和する目的のほか、硝化液中のＮＯｘ
を希釈してその濃度を低く抑えることにより、脱窒工程
１２のｐＨ上昇を抑制し、高ｐＨによる脱窒菌の活性低
下と処理水のｐＨが規制値の範囲を越えないようにする
ためである。脱窒液の循環量は廃水１のＮＨ３濃度にも
よるが、ＮＨａ Ｎが２００〜５ｏｏｍｙＡ程度の廃水
では廃水量の１０倍程度の量を循環すればよい。The circulation of the denitrification liquid is used not only to neutralize the acid in the nitrification process B with the alkaline content of the denitrification liquid, but also to reduce NOx in the nitrification liquid.
This is to suppress the pH increase in the denitrification step 12 by diluting and keeping the concentration low, and to prevent the activity of denitrifying bacteria from decreasing due to high pH and the pH of the treated water from exceeding the regulatory value range. . The amount of denitrification fluid to be circulated depends on the NH3 concentration of the wastewater 1, but in the case of wastewater with NHaN of about 200 to 5 oomyA, it is sufficient to circulate an amount about 10 times the amount of wastewater.
一方、廃水のＮＨ３Ｎ濃度が低くて脱窒工程１２に流入
するＮＯｘが低い場合、あるいは脱窒工程流入液に希釈
水を注入してＮＯ工濃度を低下した場合には、脱窒工程
１２におけるｐＨの上昇幅が小さくなるので、脱窒液の
循環を省略することも可能であるが、脱窒液を循環する
方が好ましい。まだ、廃水のｐＨ緩衝能が強くて、硝化
、脱窒に際してそれぞれｐＨの低下、上昇幅が小さい場
合にも脱窒液の循環の省略が可能となるが、循環する方
が好ましい。On the other hand, if the NH3N concentration in the wastewater is low and the NOx flowing into the denitrification process 12 is low, or if the NOx concentration is lowered by injecting dilution water into the denitrification process influent, the pH in the denitrification process 12 Although it is possible to omit the circulation of the denitrifying liquid since the increase in the amount of the denitrifying liquid becomes smaller, it is preferable to circulate the denitrifying liquid. Although it is possible to omit the circulation of the denitrifying solution even if the pH buffering capacity of the wastewater is strong and the decrease and increase in pH during nitrification and denitrification are small, respectively, it is preferable to circulate it.
前記ＮＳ化合物分解除去工程１８には単一槽を使用して
もよいが、前述の第（１）式、第（２）式の反応が順次
種別に進行するように、２槽に分割してもよい。この場
合、前段の槽に酸を添加し、後段の槽に硝化液を循環す
るとよい。循環量は硝化液中のＮＯ２Ｎが廃水のＮＳ化
合物の１．５倍以上になるようにするとよい。Although a single tank may be used in the NS compound decomposition and removal step 18, it may be divided into two tanks so that the reactions of the above-mentioned formulas (1) and (2) proceed in sequence. Good too. In this case, it is preferable to add acid to the tank at the front stage and circulate the nitrification liquid to the tank at the rear stage. The amount of circulation is preferably such that NO2N in the nitrification solution is 1.5 times or more the NS compound in the wastewater.
定常的な亜硝酸型硝化は、硝化工程＜６−１ 、６−２
）の水温を安定して４１℃程度に保持することによっ
て行うことができるが、不連続的に４４〜４５℃の高温
にしても亜硝酸型硝化を維持することができる。Steady nitrite type nitrification is the nitrification process <6-1, 6-2
) can be carried out by stably maintaining the water temperature at about 41°C, but nitrous acid type nitrification can also be maintained even if the water temperature is raised discontinuously to 44 to 45°C.
硝化工程（６−１、６−２）の中和剤として、Ｃａ（Ｏ
Ｈ）ｚを使用すると工程内でＣａＳＯ４，ＣａＣＯ３な
どのスケールを生成するのでＮａ０）Ｌが推奨される。Ca(O
If H)z is used, scales such as CaSO4 and CaCO3 will be generated in the process, so Na0)L is recommended.
以上の実施態様の説明から判るＪうに、本発明では大量
の脱窒液を循環する経路にＮＳ化合物除去工程（８）が
ないので、この工程で消費されるｐＨ調整用の酸、アル
カリ剤をまったく使用しなくてすみ、ランニングコスト
の低減化、プロセスの単純化が可能になると共に、硝化
工程で部分的にＮＨ３を高濃度に維持することによって
容易に亜硝酸型硝化を行うことができるので、安定して
ＮＳ化合物を除去することが可能になるなどの効果が得
られる。As can be seen from the above description of the embodiments, in the present invention, there is no NS compound removal step (8) in the route that circulates a large amount of denitrification solution, so that the acid and alkaline agents for pH adjustment that are consumed in this step are removed. It does not need to be used at all, which reduces running costs and simplifies the process. In addition, by maintaining a high concentration of NH3 in parts of the nitrification process, nitrite type nitrification can be easily carried out. Effects such as being able to stably remove NS compounds can be obtained.
次に、本発明の実施例を示す。Next, examples of the present invention will be shown.
実施例
第２表に示す水質の戻水を第２図の処理フローに基づい
て処理した。実施条件を第１表、処理水質を第２表に示
す。Example Returned water having the quality shown in Table 2 was treated based on the treatment flow shown in FIG. The implementation conditions are shown in Table 1, and the treated water quality is shown in Table 2.
第１表 実施条（’４：（１４日間平均値）豪硝化桶は
、各種とも実施当初の７日間３５℃の一定水温に制御し
、その後７日間は３０〜４４℃の範囲で変動させた。Table 1 Implementation conditions ('4: (14-day average value) For each type of nitrification tank, the water temperature was controlled at a constant 35℃ for the first 7 days of implementation, and then varied in the range of 30 to 44℃ for the next 7 days. .
第２表 処理水質（１４日間の平均値）東Ｎ０２−Ｎ
が低いのけ、ＮＨ３Ｎの一部がＮｏ ３にまで硝化され
たことと、循環脱窒液（（よ−って希釈されただめであ
る。Table 2 Treated water quality (average value over 14 days) East N02-N
Although the amount of NH3N is low, some of the NH3N has been nitrified to No.3, and the circulating denitrifying solution ((therefore, it has been diluted).
第１図は従来法のフローシート、第２図は本発明の一実
施態様を示すフローシートである。
１・・廃水、２・・・ＮＳ化合物分解工程、６・・酸、
４・・・中和槽、５・・・アルカリ剤、６・・・硝化工
程、６−１ ・・第１硝化工程、６−２・・・第２硝化
工程、６−６・・第３硝化工程、６−４・・・第４硝化
工程、７・・・アルカリ剤、８・・・ＮＳ化合物除去工
程、９・・酸、１０・・中和槽、１１・・・アルカリ剤
、１２・・・脱屋工程、１６・・・還元剤、１４・・循
環脱窒液、１５・・げっ気工程、１６・・・ｐ過工程、
１７・・・循環硝化液、１８・・・ＮＳ化合物分解除去
工程。
特許出願人 荏原インフィルコ株式会社代理人弁理士
千 １） 稔FIG. 1 is a flow sheet of a conventional method, and FIG. 2 is a flow sheet showing an embodiment of the present invention. 1. Wastewater, 2. NS compound decomposition process, 6. Acid,
4... Neutralization tank, 5... Alkali agent, 6... Nitrification process, 6-1... First nitrification process, 6-2... Second nitrification process, 6-6... Third Nitrification step, 6-4... Fourth nitrification step, 7... Alkaline agent, 8... NS compound removal step, 9... Acid, 10... Neutralization tank, 11... Alkaline agent, 12 ... Breaking process, 16... Reducing agent, 14... Circulating denitrification liquid, 15... Aeration process, 16... P passing process,
17... Circulating nitrification liquid, 18... NS compound decomposition and removal process. Patent applicant Minoru Sen 1) Patent attorney representing Ebara Infilco Co., Ltd.
Claims (1)
の処理において、 該廃水を含窒素硫黄化合物分解除去工程、中和工程、複
数段に分割された生物学的硝化工程、生物学的脱窒工程
を順次流下させると共に、前記複数段硝化工程における
前部硝化工程の硝化液の一部を前記含窒素硫黄化合物分
解除去工程へ、前記生物学的脱窒工程の脱窒液の一部を
前記複数段硝化工程における後部硝化工程へそれぞれ循
環して処理することを特徴とする含窒素硫黄化合物およ
びアンモニア含有廃水の処理方法。 ２ 前記前部硝化工程が、前記複数段硝化工程における
最終段を除く少なくとも一つの硝化工程である特許請求
の範囲第１項記載の方法。 ３、 前記後部硝化工程が、前記複数段硝化工程におけ
る最前段を除く少なくとも一つの硝化工程である特許請
求の範囲第１項記載の方法。[Claims] 1. In the treatment of wastewater containing nitrogen-containing sulfur compounds and ammonia, the wastewater is subjected to a nitrogen-containing sulfur compound decomposition and removal step, a neutralization step, a biological nitrification step divided into multiple stages, a biological At the same time, a part of the nitrification solution from the front nitrification step in the multi-stage nitrification step is sent to the nitrogen-containing sulfur compound decomposition and removal step, and the denitrification solution from the biological denitrification step is passed through the biological denitrification step. A method for treating nitrogen-containing sulfur compounds and ammonia-containing wastewater, characterized in that a portion of the wastewater is recycled to a post-nitrification step in the multi-stage nitrification step. 2. The method according to claim 1, wherein the front nitrification step is at least one nitrification step other than the final stage in the multi-stage nitrification step. 3. The method according to claim 1, wherein the rear nitrification step is at least one nitrification step other than the first stage in the multi-stage nitrification step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22757782A JPS59123599A (en) | 1982-12-28 | 1982-12-28 | Treatment of waste water containing nitrogenous sulfer compound and ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22757782A JPS59123599A (en) | 1982-12-28 | 1982-12-28 | Treatment of waste water containing nitrogenous sulfer compound and ammonia |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59123599A true JPS59123599A (en) | 1984-07-17 |
| JPH0116560B2 JPH0116560B2 (en) | 1989-03-24 |
Family
ID=16863091
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22757782A Granted JPS59123599A (en) | 1982-12-28 | 1982-12-28 | Treatment of waste water containing nitrogenous sulfer compound and ammonia |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59123599A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104045152A (en) * | 2014-06-29 | 2014-09-17 | 桂林理工大学 | Method for optimizing oxidation operation process of anaerobic ammonia |
| CN104045153A (en) * | 2014-06-29 | 2014-09-17 | 桂林理工大学 | Device capable of reducing generation amount of nitrous oxide in anaerobic ammonia oxidation reactor |
| CN112028242A (en) * | 2020-07-29 | 2020-12-04 | 江苏大学 | Inhibition of N2Apparatus and method for O-bleed |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5561994A (en) * | 1978-11-02 | 1980-05-10 | Hitachi Zosen Corp | Method of reducing sulfureous nitrogen compounds in waste water |
| JPS5712893A (en) * | 1980-06-26 | 1982-01-22 | Mitsubishi Heavy Ind Ltd | Disposal of waste water |
-
1982
- 1982-12-28 JP JP22757782A patent/JPS59123599A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5561994A (en) * | 1978-11-02 | 1980-05-10 | Hitachi Zosen Corp | Method of reducing sulfureous nitrogen compounds in waste water |
| JPS5712893A (en) * | 1980-06-26 | 1982-01-22 | Mitsubishi Heavy Ind Ltd | Disposal of waste water |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104045152A (en) * | 2014-06-29 | 2014-09-17 | 桂林理工大学 | Method for optimizing oxidation operation process of anaerobic ammonia |
| CN104045153A (en) * | 2014-06-29 | 2014-09-17 | 桂林理工大学 | Device capable of reducing generation amount of nitrous oxide in anaerobic ammonia oxidation reactor |
| CN112028242A (en) * | 2020-07-29 | 2020-12-04 | 江苏大学 | Inhibition of N2Apparatus and method for O-bleed |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0116560B2 (en) | 1989-03-24 |
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