JPH0661551B2 - Ammonia-containing organic wastewater treatment method - Google Patents
Ammonia-containing organic wastewater treatment methodInfo
- Publication number
- JPH0661551B2 JPH0661551B2 JP6598489A JP6598489A JPH0661551B2 JP H0661551 B2 JPH0661551 B2 JP H0661551B2 JP 6598489 A JP6598489 A JP 6598489A JP 6598489 A JP6598489 A JP 6598489A JP H0661551 B2 JPH0661551 B2 JP H0661551B2
- Authority
- JP
- Japan
- Prior art keywords
- ammonia
- organic wastewater
- treatment
- bod
- compound
- 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
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims description 20
- 229910021529 ammonia Inorganic materials 0.000 title claims description 10
- 238000004065 wastewater treatment Methods 0.000 title 1
- 239000010802 sludge Substances 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 20
- 239000002351 wastewater Substances 0.000 claims description 19
- 150000001875 compounds Chemical class 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 6
- 230000000813 microbial effect Effects 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 22
- 238000006243 chemical reaction Methods 0.000 description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000003513 alkali Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 239000002689 soil Substances 0.000 description 5
- 241000894006 Bacteria Species 0.000 description 3
- 238000005273 aeration Methods 0.000 description 3
- 239000010800 human waste Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- OIRDTQYFTABQOQ-KQYNXXCUSA-N adenosine Chemical compound C1=NC=2C(N)=NC=NC=2N1[C@@H]1O[C@H](CO)[C@@H](O)[C@H]1O OIRDTQYFTABQOQ-KQYNXXCUSA-N 0.000 description 2
- -1 are used Chemical class 0.000 description 2
- 230000001580 bacterial effect Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 239000002126 C01EB10 - Adenosine Substances 0.000 description 1
- 229960005305 adenosine Drugs 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 244000144992 flock Species 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 150000003018 phosphorus compounds Chemical class 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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
- Activated Sludge Processes (AREA)
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有機性廃水の処理方法に係り、
特に、し尿、浄化槽汚泥などのし尿系汚水を生物学的及
び物理化学的に処理する方法に関する。Description: TECHNICAL FIELD The present invention relates to a method for treating an organic wastewater containing ammonia,
In particular, it relates to a method for biologically and physicochemically treating night soil-based wastewater such as night soil and septic tank sludge.
し尿系汚水は、現在、生物学的硝化脱窒法によつて処理
され、該汚水中のＢＯＤとともに窒素分も除去されてい
るが、難生物分解物質である▲PO3- 4▼，ＣＯＤ成分、
色度成分は生物処理工程の後段に配備された凝集処理工
程において、アルミニウム塩、鉄塩によつて凝集処理さ
れている。Night soil based wastewater is now being by connexion processed biological nitrification denitrification, but nitrogen content is also removed with the BOD of the soil water, is hardly biodegradable material ▲ PO 3- 4 ▼, COD components,
The chromaticity component is coagulated with an aluminum salt and an iron salt in a coagulation treatment step provided in the latter stage of the biological treatment step.
しかしながら、このような従来技術は、例えば、「し尿
処理ガイドブツク」（昭和５６年５月１日増補改訂、環
境技術研究会発行）、第６７９〜６８１頁に記載のよう
に、プロセス構成が複雑になるため、処理操作が煩雑で
あり、建設費、運転費用が高いという欠点があつた。ま
た、生物学的硝化脱窒法においては、硝化菌が低pH域及
び高pH域、水温４０℃以上、毒性物質の存在下では失活
するため、処理条件を所定範囲に維持するための装置及
び厳重な運転管理が必要であつた。However, such a conventional technique has a complicated process configuration, as described in, for example, “Nuclear Treatment Guidebook” (May 1, 1981, supplemental revision, published by Environmental Technology Research Group), pp. 679-681. Therefore, the processing operation is complicated, and the construction cost and operation cost are high. In the biological nitrification denitrification method, nitrifying bacteria are inactivated in the low pH range and high pH range, at a water temperature of 40 ° C. or higher, and in the presence of toxic substances. Strict operation management was necessary.
上記したように、従来技術においては、し尿系汚水の処
理に関しては、現在までに十分に満足のいく方法はなか
つた。As described above, in the prior art, there has been no sufficiently satisfactory method to treat human wastewater until now.
そこで、本発明は、アンモニアを含有する有機性廃水の
処理において、プロセス構成が簡単で、処理操作の容易
な処理方法を提供することを目的とする。Therefore, it is an object of the present invention to provide a treatment method for treating an organic wastewater containing ammonia, which has a simple process configuration and an easy treatment operation.
上記目的を達成するために、本発明では、アンモニアを
含有する有機性廃水を処理する方法において、該有機性
廃水中のＢＯＤ成分を処理する好気性生物処理工程に、
少なくともCa化合物又はMg化合物の一種を添加すると共
にpHを9.5〜11.0に保持し、物理化学的に液中からアン
モニアを放散するとともに、前記Ca化合物、Mg化合物に
よつて、ＣＯＤ成分の一部を凝集しつつ固液分離工程に
導入し、pH9.5〜11.0で増殖した活性汚泥菌体を分離
し、前記好気性生物処理工程に返送することによるアン
モニア含有有機性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, in a method for treating an organic wastewater containing ammonia, in an aerobic biological treatment step of treating a BOD component in the organic wastewater,
At least one kind of Ca compound or Mg compound is added and the pH is maintained at 9.5 to 11.0, and ammonia is physicochemically diffused from the liquid, while the Ca compound and the Mg compound cause a part of the COD component. Introduced into the solid-liquid separation step while aggregating, separating the activated sludge bacterial cells grown at pH 9.5 to 11.0, and treating the ammonia-containing organic wastewater by returning to the aerobic biological treatment step. is there.
次に、本発明を第１図に基づいて詳しく説明する。第１
図は本発明の一実施態様を示す工程図である。Next, the present invention will be described in detail with reference to FIG. First
The drawings are process diagrams showing an embodiment of the present invention.
し尿１は、返送汚泥２とともに、pHが9.5〜11.0に保持
されている生物反応槽３に導入される。該反応槽３で
は、ブロワー１０により曝気されており、ＢＯＤ成分が
槽中の耐アルカリ性活性汚泥によつてCO2，H2Oに分解さ
れ、同時に、高pHのため液中のNH3がNH3（ガス）に遊離
されて曝気により気相中に放散される。反応槽３に配備
するデイヒユーザはデイスク型のものを用いるとスケー
ルによる目詰まりを防止できる。The human waste 1 is introduced together with the returned sludge 2 into the biological reaction tank 3 whose pH is maintained at 9.5-11.0. In the reaction tank 3, the BOD component is aerated by the blower 10, and the BOD component is decomposed into CO 2 and H 2 O by the alkali-resistant activated sludge in the tank, and at the same time, NH 3 in the liquid is NH 3 due to the high pH. It is released into 3 (gas) and released into the gas phase by aeration. A Dehi user who is placed in the reaction tank 3 can prevent clogging due to scale by using a disk type.
該反応槽３には、アルカリ導入管４からCa化合物又はMg
化合物のうち少なくとも一種類が添加され、同時にpHを
上昇するためにアルカリ剤としてNaOH，KOHなどを注入
してもよいが、Ca又はMg化合物としてCa(OH)2，Mg(OH)2
などのアルカリ性Ca，Mg化合物を用いれば、NaOH，KOH
の添加を省略することができる。In the reaction tank 3, a Ca compound or Mg is fed from the alkali introducing pipe 4.
At least one of the compounds is added, and at the same time, NaOH, KOH or the like may be injected as an alkaline agent in order to raise the pH, but Ca (OH) 2 , Mg (OH) 2 as Ca or Mg compounds may be injected.
If alkaline Ca, Mg compounds such as are used, NaOH, KOH
Can be omitted.
し尿１中のリン化合物、難生物分解性のＣＯＤ、色度成
分も高pH条件下でCaあるいはMgの作用によつて不溶化し
液中から除去される。反応槽３の水温はＢＯＤ成分の酸
化熱によつて３０〜６０℃にまで上昇するが、高水温ほ
どNH3の放散効率がよくなるので、希釈水を注入するな
どして水温を低下させるのは好ましくない。Phosphorus compounds, COD that is hardly biodegradable, and chromatic components in human urine 1 are also insolubilized by the action of Ca or Mg under high pH conditions and removed from the liquid. The water temperature in the reaction tank 3 rises to 30 to 60 ° C. due to the heat of oxidation of the BOD component, but the higher the water temperature, the better the NH 3 emission efficiency. Therefore, it is not possible to lower the water temperature by injecting dilution water. Not preferable.
反応槽３の活性汚泥は、次に、沈殿分離、遠心分離、膜
分離などの公知の固液分離工程６で分離され、返送汚泥
２として反応槽３に導入され、一部は余剰汚泥７として
系外に排出され、後処理される。分離水８は、pH調整さ
れたのち放流あるいは更に高度な処理が行なわれたのち
放流される。反応槽３から放散されたNH3を含有する排
ガス５は、H2SO4等による吸収、触媒を利用したNH3の分
解、水洗浄などのNH3除去装置９によつて、排ガスからN
H3が除去される。The activated sludge in the reaction tank 3 is then separated in a known solid-liquid separation step 6 such as sedimentation, centrifugation, membrane separation, etc., and is introduced into the reaction tank 3 as return sludge 2, and part of it is converted into excess sludge 7. It is discharged out of the system and post-processed. The separated water 8 is discharged after being adjusted in pH or after being subjected to more advanced treatment. Exhaust gas 5 containing NH 3 emitted from the reaction tank 3 is absorbed by H 2 SO 4, etc., decomposes NH 3 using a catalyst, and is removed from the exhaust gas by an NH 3 removing device 9 such as water washing.
H 3 is removed.
次に、第３図について説明する。第３図は本発明の他の
実施態様を示す工程図である。Next, FIG. 3 will be described. FIG. 3 is a process drawing showing another embodiment of the present invention.
第３図においては、反応槽３の散水床塔には、プラス
チツク、砂などの微生物を付着する担体を充填した充填
槽１１を配備しており、充填槽１１内にはフアン１３か
ら空気が導入されている。そして、散水液供給管１２に
よつて、処理液が充填層上に散水されている。この充填
層１１と供給管を除いては、第１図の構成と同じであ
り、このように微生物を担体に付着させて行うこともで
きる。In FIG. 3, the sprinkling bed tower of the reaction tank 3 is provided with a packing tank 11 filled with a carrier to which microorganisms such as plastic and sand adhere, and air is introduced from the fan 13 into the packing tank 11. Has been done. Then, the treatment liquid is sprinkled on the packed bed by the sprinkling liquid supply pipe 12. The configuration is the same as that of FIG. 1 except for the packed bed 11 and the supply pipe, and the microorganism can be attached to the carrier in this way.
耐アルカリ性活性汚泥は、高pH域の条件下で種汚泥とし
た通常の活性汚泥が淘汰されたもので、好気的条件にお
いてＢＯＤ成分を分解する。菌の種類については同定し
ていないが、沈降性の良好な緻密なフロツクを形成する
ものが多い。The alkali-resistant activated sludge is a normal activated sludge that has been selected as a seed sludge under high pH conditions, and decomposes BOD components under aerobic conditions. Although the type of bacteria has not been identified, many of them form dense flocks with good sedimentation properties.
本発明において、活性汚泥の返送は極めて重要である。
これは耐アルカリ性活性汚泥の増殖速度が極めて小さい
ため、長期間の汚泥令をとらなければ、生物処理工程で
十分量の汚泥を確保できないからである。例えば、４〜
６日滞留の曝気槽を用いても沈殿槽、汚泥返送設備のな
い一過性の好気性処理では耐アルカリ性活性汚泥を曝気
槽に十分保持することは不可能である。In the present invention, returning activated sludge is extremely important.
This is because the growth rate of alkali-resistant activated sludge is extremely low, and a sufficient amount of sludge cannot be secured in the biological treatment process without taking a long-term sludge age. For example, 4 ~
Even if a 6-day retention aeration tank is used, it is impossible to sufficiently retain the alkali-resistant activated sludge in the aeration tank by a transient aerobic treatment without a settling tank or a sludge returning facility.
本発明は、従来アンモニアストリツピング処理を行つた
のちに活性汚泥処理を行つていた、コークス製造排水
（安水）の処理にも好適であり、その他のNH3含有有機
性廃水にはいずれも適用可能である。INDUSTRIAL APPLICABILITY The present invention is suitable for the treatment of coke-producing wastewater (ammonium), which has conventionally been subjected to activated sludge treatment after ammonia stripping treatment, and is suitable for other NH 3 -containing organic wastewater. Is also applicable.
以下、本発明を実施例により具体的に説明するが、本発
明はこれらの実施例に限定されるものではない。Hereinafter, the present invention will be specifically described with reference to examples, but the present invention is not limited to these examples.
実施例１ 第１図に基づいて、次の条件により行つた。Example 1 Based on FIG. 1, it was carried out under the following conditions.
(1)実施条件 原 水：し尿、処理量：１０ｋ／日、 反応槽：４０m3、沈殿槽：２０m3、 水温：４１〜４８℃、反応槽MLSS：13000〜14100mg／
、 返送汚泥量：１０m3／日 (2)し尿性状 ＢＯＤ：１１０００mg／ CODMn： ４２００ 〃 NH3-N： ２７００ 〃 ▲PO3- 4▼-P：２３０ 〃 上記し尿を用い、Ca(OH)2，Mg(OH)2，CaCl2，MgCl2，Na
OHを添加し、反応槽のpHをそれぞれ9.5，10.0，11.0調
整して処理を行つたところ第１表に示す如き処理結果を
得た。(1) Implementation conditions Raw water: night soil, throughput: 10 k / day, reaction tank: 40 m 3 , precipitation tank: 20 m 3 , water temperature: 41 to 48 ° C., reaction tank MLSS: 13000 to 14100 mg /
, Returned sludge volume: 10 m 3 / day (2) excreta Properties BOD: 11000mg / CODMn: 4200 〃 NH 3 -N: 2700 〃 ▲ PO 3- 4 ▼ -P: 230 〃 using the human waste, Ca (OH) 2 , Mg (OH) 2 , CaCl 2 , MgCl 2 , Na
When OH was added and the pH of the reaction vessel was adjusted to 9.5, 10.0, and 11.0, and the treatment was performed, the treatment results shown in Table 1 were obtained.
第１表に示したように、滞留日数４日の反応槽で、例え
ばCa(OH)2を加えて、pHを１０にした例では、BOD，COD
Mn，NH3-N，▲PO3- 4▼-Pをそれぞれ約９８％，９３％，
９４％，１００％処理することができた。これは生物処
理は温和な条件で行うという従来の固定観念を一掃した
ことによつて初めて生み出されたものである。 As shown in Table 1, in a reaction vessel with a residence time of 4 days, for example, Ca (OH) 2 was added to adjust the pH to 10, and BOD, COD
Mn, NH 3 -N, ▲ PO 3- 4 ▼ -P about 98%, respectively, 93%,
It was possible to treat 94% and 100%. This was born for the first time by eliminating the conventional stereotype that biological treatment is performed under mild conditions.
菌体の発生量は、菌体量をＡＴＰ（アデノシントリフオ
スフエイト）換算で測定したところ、pH9.5〜11.0のも
のは、反応槽pH8.1のものに比べ４３％〜５２％の値と
なつた。The amount of microbial cells was measured by converting the amount of microbial cells in terms of ATP (adenosine triphosphite), and those of pH 9.5 to 11.0 had a value of 43% to 52% compared to those of the reaction tank pH 8.1. Tonatsuta.
余剰汚泥の脱水ケーキ含水等は、Ca(OH)2添加、pH１０
のものでは、フイルタプレスを用い、無薬法で５８％に
することができた。Excess sludge dehydrated cake water content, etc., Ca (OH) 2 addition, pH 10
In the case of No. 1, it was possible to obtain 58% by a drugless method using a filter press.
なお、比較例として第１表のNo.１２，No.１３の実験例
に示したように、２価のアルカリ金属を添加せず、NaOH
のみを用いて高pHに調整した例では、高pHによつて菌
体、廃水ＳＳから溶出した成分によつて処理水のCO
DMn，色度が著しく上昇した（No.１実験例と比較して下
さい）。しかしながら、本発明（No.１〜１１）例ではC
aあるいはMgを添加することによつて処理水CODMn、色度
はむしろNo.１例よりも低下し、良好な水質となつてい
る。As a comparative example, as shown in No. 12 and No. 13 experimental examples in Table 1, divalent alkali metal was not added and NaOH was used.
In the case where the pH was adjusted to a high pH by using only water, CO was treated by the high pH and the treated water by the components eluted from the wastewater SS.
D Mn and chromaticity increased significantly (compare with No. 1 experimental example). However, in the example of the present invention (No. 1 to 11), C
By adding a or Mg, the treated water COD Mn and chromaticity were lowered rather than the No. 1 case, and the water quality is good.
なお、第１表No.６〜８の実施例と同様にCaCl25000mg／
を添加し、pHを9.5〜11.0の範囲外に設定したとこ
ろ、NH3-N除去率あるいはＢＯＤ除去率の一方が悪化し
良好な処理水を得ることができなかつた。その結果を第
２図に示す。第２図はpHとＢＯＤ、NH3-N除去率の関係
を示すグラフであり、ＢＯＤ除去率は白丸で示し、NH3-
N除去率は黒丸で示している。pHが低くなるとNH3-N除去
率が低くなり、pHが高くなるとＢＯＤ除去率が低くな
る。これより本発明においては、pHを9.5〜11.0で生物
処理を行なうことが肝要となる。In addition, as in the examples of Table 1, Nos. 6 to 8, CaCl 2 5000 mg /
Was added and the pH was set outside the range of 9.5 to 11.0, one of the NH 3 -N removal rate and the BOD removal rate deteriorated, and good treated water could not be obtained. The results are shown in FIG. FIG. 2 is a graph showing the relationship between pH, BOD, and NH 3 -N removal rate. The BOD removal rate is indicated by a white circle, NH 3-
The N removal rate is indicated by a black circle. The lower the pH, the lower the NH 3 -N removal rate, and the higher the pH, the lower the BOD removal rate. From this, in the present invention, it is important to perform biological treatment at a pH of 9.5 to 11.0.
実施例２ 原水は、BOD 50000mg／、NH3-N 23000mg／、▲PO3-
4▼-P 1200mg／の人口廃水を用いた。Example 2 Raw water is BOD 50000 mg /, NH 3 -N 23000 mg /, ▲ PO 3 −
4 ▼ -P 1200 mg / g of artificial wastewater was used.
実施条件は次の通りである。The implementation conditions are as follows.
反応槽１６（＝８＋８）、沈殿槽１６、処理槽
２／日、水温５２〜５５℃、反応槽MLSS9000〜9600mg
／、返送汚泥量４／日、Ca(OH)2，CaCl2，NaOHを用
い、反応槽のpHが１０になるように設定して原水の処理
を行つた。結果を第２表に示す。Reaction tank 16 (= 8 + 8), precipitation tank 16, treatment tank 2 / day, water temperature 52 to 55 ° C, reaction tank MLSS 9000 to 9600 mg
The amount of sludge to be returned was 4 / day, Ca (OH) 2 , CaCl 2 , and NaOH were used, and the raw water was treated by setting the pH of the reaction tank to 10. The results are shown in Table 2.
また同一の原水を用いて、第３図に基づいて反応槽にプ
ラスチツク板を充填して液を槽上部から散水した結果第
２表と同様の処理成績をえた。なお、このときの反応槽
は３０、プラスチツク充填部は２０で、他の条件は
実施例２と同様であつた。 Also, the same raw water was used to fill the reaction tank with a plastic plate based on FIG. 3 and the solution was sprayed from the upper part of the tank. As a result, the same treatment results as in Table 2 were obtained. At this time, the reaction tank was 30, the plastic filling part was 20, and other conditions were the same as in Example 2.
本発明によれば次のような効果を奏する。 The present invention has the following effects.
1.同一の槽でNH3の放散とＢＯＤの生物学的処理及びリ
ンとCODMn、色度成分の凝集処理が一挙に達成すること
ができる。NH3，BOD，リン，CODMn，色度成分は汚水中
の主要汚濁成分であり、これらの同時除去は極めて大き
な効果である。1. NH 3 emission and BOD biological treatment and phosphorus, COD Mn and chromaticity component agglomeration treatment can be achieved all at once in the same tank. NH 3 , BOD, phosphorus, COD Mn , and chromaticity components are major pollutants in wastewater, and their simultaneous removal is extremely effective.
2.汚水中の汚濁物を生物学的に浄化しつつNH3を放散す
るので、生物学的に無処理、あるいはほとんど処理して
いない汚水のNH3を放散した従来技術よりもはるかに衛
生的な処理を行うことができる。2. Since dissipating NH 3 while purifying contaminants in wastewater biologically, much more hygienic than prior art dissipating biologically intact or sewage NH 3 of which hardly processed, It is possible to perform various processing.
3.汚水中のＢＯＤ成分を生化学的に酸化分解することに
よつて発生する熱で、反応槽中の液温が４０〜６０℃程
度にまで上昇するので、従来技術の如く蒸気を利用せず
とも、NH3の放散効率を上昇することができる。3. The heat generated by the biochemical oxidative decomposition of the BOD component in the wastewater raises the liquid temperature in the reaction tank to about 40 to 60 ° C, so use steam as in the prior art. Even without this, the emission efficiency of NH 3 can be increased.
4.好気性生物処理法と物理化学処理方法を巧みに利用す
ることによつて、生物処理工程の大きさを従来の1/6〜1
/2にすることが可能になり、装置の建設費を著しく低減
することができる。4. By making good use of the aerobic biological treatment method and the physicochemical treatment method, the size of the biological treatment process can be reduced to 1/6 to 1 of the conventional one.
It is possible to reduce the cost to 1/2, and the construction cost of the device can be significantly reduced.
5.生物処理工程で発生する余剰菌体重量が従来の約５０
％になつた。5. The surplus cell weight generated in the biological treatment process is about 50
% Has been reached.
6.菌体を含有する余剰汚泥（CaCO3を含む）の脱水性は
著しく向上し、薬品を添加せずに良好なる脱水を行うこ
とができる。6. The dehydration property of surplus sludge (including CaCO 3 ) containing bacterial cells is remarkably improved, and good dehydration can be performed without adding chemicals.
7.放散NH3を硫酸に吸収せしめて、肥料として有価の硫
安を製造することができる。7. It is possible to produce valuable ammonium sulfate as a fertilizer by absorbing the diffused NH 3 in sulfuric acid.
8.廃水に硝化菌を失活するようなシアン化合物が流入し
てきてもNH3の処理を行うことができる。8. NH 3 treatment can be performed even if a cyanide compound that inactivates nitrifying bacteria flows into the wastewater.
第１図と第３図は、本発明の処理方法を示す工程図であ
り、第２図はpHとBOD、NH3-N除去率の関係を示すグラフ
である。 １…し尿、２…返送汚泥、３…生物反応槽、４…アルカ
リ導入管、５…排ガス、６…固液分離工程、７…余剰汚
泥、８…分離水、９…NH3除去装置、１０…ブロワー、
１１…微生物付着担体充填層、１２…散水液供給管、１
３…フアン、１４…水面1 and 3 are process diagrams showing the treatment method of the present invention, and FIG. 2 is a graph showing the relationship between pH, BOD, and NH 3 —N removal rate. 1 ... Human waste, 2 ... Return sludge, 3 ... Biological reaction tank, 4 ... Alkali introduction tube, 5 ... Exhaust gas, 6 ... Solid-liquid separation process, 7 ... Excess sludge, 8 ... Separation water, 9 ... NH 3 removal device, 10 ... blower,
11 ... Microorganism-attached carrier packed bed, 12 ... Sprinkling liquid supply pipe, 1
3 ... Juan, 14 ... Water surface
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59−139987（ＪＰ，Ａ)Front Page Continuation (72) Inventor Shinji Yoshida 4-2-1 Motofujisawa, Fujisawa City, Kanagawa Inside EBARA Research Institute Co., Ltd. (56) Reference JP-A-59-139987 (JP, A)
Claims (1)
る方法において、該有機性廃水中のＢＯＤ成分を処理す
る好気性生物処理工程に、少なくともCa化合物又はMg化
合物の一種を添加すると共にpHを9.5〜11.0に保持し、
物理化学的に液中からアンモニアを放散するとともに、
前記Ca化合物、Mg化合物によってＣＯＤ成分の一部を凝
集しつつ、固液分離工程に導入し、pH9.5〜11.0で増殖
した活性汚泥菌体を分離し、前記好気性生物処理工程に
返送することを特徴とするアンモニア含有有機性廃水の
処理方法。1. A method for treating an organic wastewater containing ammonia, wherein at least one Ca compound or Mg compound is added to the aerobic biological treatment step for treating the BOD component in the organic wastewater, and the pH is adjusted. Hold at 9.5 to 11.0,
Ammonia is physicochemically released from the liquid,
While introducing a part of the COD component by the Ca compound and the Mg compound, the COD component is introduced into the solid-liquid separation step, the activated sludge microbial cells grown at pH 9.5 to 11.0 are separated, and returned to the aerobic biological treatment step. A method for treating an ammonia-containing organic wastewater, comprising:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6598489A JPH0661551B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing organic wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6598489A JPH0661551B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing organic wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02245293A JPH02245293A (en) | 1990-10-01 |
| JPH0661551B2 true JPH0661551B2 (en) | 1994-08-17 |
Family
ID=13302781
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6598489A Expired - Lifetime JPH0661551B2 (en) | 1989-03-20 | 1989-03-20 | Ammonia-containing organic wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0661551B2 (en) |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59139987A (en) * | 1983-01-29 | 1984-08-11 | Yoshiaki Motozato | Removal of nitrogen component from waste water in final sewage disposal plant |
-
1989
- 1989-03-20 JP JP6598489A patent/JPH0661551B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02245293A (en) | 1990-10-01 |
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