JPS6159798B2 - - Google Patents
Info
- Publication number
- JPS6159798B2 JPS6159798B2 JP54158472A JP15847279A JPS6159798B2 JP S6159798 B2 JPS6159798 B2 JP S6159798B2 JP 54158472 A JP54158472 A JP 54158472A JP 15847279 A JP15847279 A JP 15847279A JP S6159798 B2 JPS6159798 B2 JP S6159798B2
- Authority
- JP
- Japan
- Prior art keywords
- treatment
- aeration tank
- biological treatment
- human waste
- biological
- 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
Links
- 238000011282 treatment Methods 0.000 claims description 47
- 238000000034 method Methods 0.000 claims description 45
- 238000005273 aeration Methods 0.000 claims description 27
- 239000007787 solid Substances 0.000 claims description 27
- 238000010790 dilution Methods 0.000 claims description 20
- 239000012895 dilution Substances 0.000 claims description 20
- 239000010800 human waste Substances 0.000 claims description 20
- 239000002351 wastewater Substances 0.000 claims description 15
- 239000000725 suspension Substances 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 8
- 229920006317 cationic polymer Polymers 0.000 claims description 7
- 244000005700 microbiome Species 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 6
- 230000016615 flocculation Effects 0.000 claims description 6
- 239000012295 chemical reaction liquid Substances 0.000 claims description 4
- 239000002689 soil Substances 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 30
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 22
- 239000007788 liquid Substances 0.000 description 10
- 239000004576 sand Substances 0.000 description 8
- 239000010802 sludge Substances 0.000 description 8
- 238000004062 sedimentation Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 239000000377 silicon dioxide Substances 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 238000005187 foaming Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000010815 organic waste Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000003254 anti-foaming effect Effects 0.000 description 1
- 239000002518 antifoaming agent Substances 0.000 description 1
- 230000032770 biofilm formation Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000011328 necessary treatment Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002062 proliferating effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000010457 zeolite Substances 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
- Biological Treatment Of Waste Water (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
本発明は、し尿など濃厚有機性廃液の革新的な
処理方法に関するものである。
一般にし尿系汚水の処理方法としては、種々の
生物学的処理方法、例えば活性汚泥法および散水
床法、回転円板法、チユーブ接触酸化法などの
生物膜処理法が採用されており、これら処理法に
ついて種々の面から検討が重ねられるかなりの技
術的進歩が見られる。
しかしながらこれら生物学的処理方法は、し尿
などの濃厚な有機性廃液に対しては充分満足な処
理を遂行することは困難である。
すなわち従来のし尿処理プロセスにおける重大
な問題点は、
活性汚泥法などの生物処理工程においては、
し尿に対し５〜20倍量の多量の希釈水を要する
ので、希釈水源の確保に難点のあるし尿処理場
では、希釈水不足に悩まされている。
このように、多量の希釈水で希釈されている
ので、たとえ、最終放流水のBOD濃度を低く
するための少量の廃水処理は容易となつても処
理するべき廃水の負荷の総量は以前として変わ
らず、全廃水量を処理するのは容易ではないの
で、希釈しないでも従来のように予め、希釈さ
れた廃水を処理する場合と同等の放流水が得ら
れることが望まれている。
活性汚泥法が広く採用されているが、汚泥返
送、汚泥引抜き量のコントロール、SVIの測
定、最終沈殿池におけるスカム発生など、維持
管理上多くの問題点がある。
一方、散水床法、回転円板法、チユーブ接
触酸化法などの生物膜プロセスは、維持管理は
容易なもののし尿など高濃度のBODを含む廃
水に対して無希釈もしくは５倍以下の希釈倍率
では、生物膜の過剰な発生による接触媒体の閉
塞、酸素供給量に限界があることによる処理の
嫌気化、処理水質の不良および必要な処理槽の
〓〓〓〓〓
容積の膨大化など、多くの難点があり、上記条
件の生物膜プロセスは採用不可能と認識されて
おり実施された例も見当らない。
本発明は、このような従来のし尿系汚水の処理
方法の幾多の重大な欠点を解決した新規且つ合理
的、効果的な生物学的処理方法を提供することを
目的とするものである。
本発明者は、前記のような従来のし尿処理方法
の欠点を解決することを目的とする検討の過程に
おいて曝気槽内に砂、活性炭、ゼオライトなどの
任意の粒状固体を懸濁させ、この粒状固体の表面
に微生物を付着させて生物処理する方法が、従来
下水などBOD100〜300mg／程度の希薄有機性
廃水についてのみ検討され、し尿など濃厚有機性
廃水については研究例、実施例が皆無であるとい
う事実を知見した。
本発明者はこの事実にもとづいて、粒状固体懸
濁生物処理法をし尿処理に適用することに着眼
し、そのためにはどのようなプロセスが最も合理
的、効率的であるかを追求した結果、し尿のよう
な高濃度の有機性廃水を粒状固体懸濁法で、無希
釈で処理すると、希釈する場合よりも極めて、効
果的に、粒状固体に微生物が付着繁殖し、かつ、
曝気による発泡も、ほとんど生じないことを見出
し本発明に到達したものである。
すなわち本発明は、し尿などの濃厚有機性廃水
を、無希釈のまま、又は予め５倍以下の希釈倍率
で希釈した後、微生物が付着した粒状固体を懸濁
流動させている曝気槽に導入して粒状固体懸濁生
物処理を行い、前記曝気槽からの流出スラリーに
少なくともカチオン性高分子凝集剤を添加し、得
られる凝集反応液を機械脱水することを特徴とす
るし尿系汚水の処理方法である。
次に本発明の実施態様を図面を参照しつつ説明
する。
まず、原水（生し尿）１は、スクリーン（図示
せず）などで、夾雑物を除去されたのち、希釈水
で希釈することなく、粒径0.2〜0.3mmの硅砂を数
10％（容積比）懸濁流動させた曝気槽２に流入さ
れ、所定滞留時間、生物処理を受ける。曝気槽２
内にはエアリフトチユーブ３が配備され、その下
部に空気４が供給される。硅砂の流動化と硅砂へ
の酸素供給はエアリフトチユーブ３内を上昇する
空気泡によつて行われる。
次に硅砂は媒体分離部５で沈降分離され、原水
中SSおよび増殖微生物によるSSと、生物処理水
との混合液である流出スラリー６が媒体分離部５
から流出してゆく。
曝気槽２からの前記流出スラリー６は、従来法
とは異なり重力沈殿池（最終沈殿池）を経由せず
に一旦貯槽７に貯留された後、ポンプ８により凝
集反応槽９へ送液され、ここでカチオン性高分子
凝集剤１０が添加、混合され凝集反応が行なわれ
る。凝集反応液１２は脱水機１３へ供給され脱水
ケーキ１４と脱水分離液１５に分離される。なお
１１は撹拌機である。
脱水分離液１５はそのまま放流されるか、さら
に高度な処理を必要とする場合は、硫酸バンド、
塩化第２鉄などの無機凝集剤によつて凝集沈殿処
理される。
本発明においては、原水を無希釈もしくは希釈
倍率５倍以下の希釈条件が好ましいが、このよう
な限定の意義は次のとおりである。すなわち、本
発明においては、原水を無希釈で処理するのが最
も合理的なのであるが、５倍以下の希釈倍率まで
なら、本発明の効果は本質的に失われるものでな
い。これは５倍をこえて希釈すると処理効率が低
下し粒状媒体懸濁曝気槽の所要容積が増加した
り、また脱水機への流入水量が増加し、脱水機の
規模、消費動力の著しい増加を招き、イニシヤル
コスト、ランニングコストの面で非常に不利なり
本発明の目的達成が困難となるためである。
また曝気槽２における被処理水の滞留時間（前
記曝気槽内の処理水量を希釈前の原水流入量で除
したもの）は、0.2日以上が好ましい。これは滞
留日数0.2日未満では、処理水質（とくにBOD）
が著しく悪化するためである。
本発明において適用される生物処理としては、
生物学的硝化脱窒素法、生物学的脱リン工程をも
つ活性汚泥法など、公知の任意の生物処理方法が
含まれる。
また曝気槽における粒状固体懸濁生物処理工程
と脱水工程の間に、回転円板法、単純曝気法、接
触酸化法など任意の生物処理工程を介在させて多
段処理を行つてもよいことは勿論である。例え
ば、介在させる生物処理工程として生物学的硝化
脱窒素処理工程を採用すれば、極めて効果的な処
理が可能となる。
〓〓〓〓〓
このように生物処理を多段に行えば、万一硅砂
などの粒状固体が粒状固体懸濁生物処理工程から
流出しても２段目の生物処理工程で沈降し脱水工
程に流入することはなくなり、また浮遊固形物質
（SS分）の凝集性が向上し、カチオン性高分子凝
集剤の添加量が小量ですむ利点がある。
なお、粒状固体懸濁生物処理工程を多段にする
ことも可能である。
以上の如く、従来の無希釈の活性汚泥処理で
は、著しい発泡が生じ、消泡剤もしくは消泡機を
使用しないと処理不能になることが少なくなかつ
たのに対し、本発明によれば発泡は殆ど生ずるこ
となく、極めて効果的に処理を行うことができ、
しかも、希釈しないため処理水量が少なくてすみ
前記媒体分離部の分離面積が著しく小さくてすむ
という副次的効果も得られ、また、高濃度BOD
除去の際、発生する発酵熱によつて、曝気槽内水
温が冬期においても30〜35℃に、外部熱源を要す
ることなく維持できる。
以上のような現象の相乗効果によつて、前記曝
気槽における被処理水の所要滞留時間は0.2日〜
１日で充分となるものであり、0.2日の曝気槽滞
留時間で、BODが90％以上除去できるという事
実は、従来全く予想されなかつた点である。
また特に、微生物フロツクを分離するための最
終沈殿池を省略して、粒状媒体懸濁生物処理工程
と機械脱水工程とを結合したことは、本発明にお
ける最重要ポイントの一つであり、従来法にその
例をみないものである。
以上のように本発明は、し尿などの濃厚有機性
廃水を、無希釈のまま、又は予め５倍以下の希釈
倍率で希釈した後、微生物が付着した粒状固体を
懸濁流動させている曝気槽に導入して粒状固体懸
濁生物処理を行い、前記曝気槽からの流出スラリ
ーに少なくともカチオン性高分子凝集剤を添加
し、得られる凝集反応液を機械脱水することによ
り、生し尿などBOD10000mg／以上という高濃
度有機性廃水を希釈水の添加を要することなく、
しかも、極めて小容量の装置で効率の良い、安定
した処理を遂行することを可能にし、生物処理工
程において従来不可欠とされていた最終沈殿池を
不要とするのみならず汚泥返送操作も不必要と
し、かつ粒状固体懸濁曝気槽流出液を直接脱水機
で固液分離するため、微生物の沈降性に無関係に
確実に固液分離でき、維持管理も極めて容易にな
るなど実用上大きな利点を有するものである。
次に、本発明によるし尿の無希釈処理の実施例
について説明する。
第１表の水質を有する神奈川県Ｆ市のし尿処理
場から採取した生し尿を0.1〜３Kl／日の流入量
で無希釈処理実験を行つた。
The present invention relates to an innovative method for treating concentrated organic waste liquids such as human waste. In general, various biological treatment methods are used to treat night soil wastewater, such as activated sludge method, trickling bed method, rotating disk method, tube catalytic oxidation method, and other biofilm treatment methods. Considerable technological advances have been made that have led to the examination of various aspects of the law. However, it is difficult for these biological treatment methods to fully and satisfactorily treat concentrated organic waste liquids such as human waste. In other words, the major problem with conventional human waste treatment processes is that biological treatment processes such as the activated sludge method
Since a large amount of dilution water is required, which is 5 to 20 times the amount of human waste, human waste treatment plants, which have difficulty securing a dilution water source, are suffering from a shortage of dilution water. In this way, since it is diluted with a large amount of dilution water, even if it becomes easy to treat a small amount of wastewater to lower the BOD concentration of the final effluent, the total amount of wastewater to be treated will remain unchanged. First, it is not easy to treat the entire amount of wastewater, so it is desirable to be able to obtain effluent water that is equivalent to the conventional treatment of diluted wastewater without dilution. Although the activated sludge method has been widely adopted, there are many problems in maintenance and management, such as sludge return, control of the amount of sludge removed, SVI measurement, and scum generation in the final settling tank. On the other hand, biofilm processes such as the sprinkled bed method, rotating disk method, and tube contact oxidation method are easy to maintain and manage, but they cannot be used without dilution or at a dilution rate of 5 times or less for wastewater containing high concentrations of BOD such as human waste. , clogging of the contact medium due to excessive biofilm formation, anaerobic treatment due to limited oxygen supply, poor quality of treated water and lack of necessary treatment tanks.
There are many drawbacks such as the large volume, and it is recognized that the biofilm process under the above conditions cannot be adopted, and there are no examples of it being implemented. The object of the present invention is to provide a novel, rational, and effective biological treatment method that overcomes the many serious drawbacks of the conventional human waste wastewater treatment methods. In the course of research aimed at solving the drawbacks of the conventional human waste treatment methods as described above, the present inventor suspended arbitrary granular solids such as sand, activated carbon, and zeolite in an aeration tank, and Conventionally, methods for biological treatment by attaching microorganisms to the surface of solids have been studied only for dilute organic wastewater such as sewage with a BOD of 100 to 300 mg/kg, and there are no research examples or examples for concentrated organic wastewater such as human waste. I discovered this fact. Based on this fact, the present inventor focused on applying the granular solid suspension biological treatment method to human waste treatment, and as a result of pursuing what kind of process would be the most rational and efficient for that purpose, When highly concentrated organic wastewater such as human waste is treated without dilution using the granular solid suspension method, microorganisms adhere to and propagate on the granular solids much more effectively than when diluting.
The present invention was achieved by discovering that foaming due to aeration hardly occurs. That is, in the present invention, concentrated organic wastewater such as human waste is introduced into an aeration tank in which granular solids with attached microorganisms are suspended and fluidized after being undiluted or diluted in advance at a dilution ratio of 5 times or less. A method for treating night soil wastewater, characterized in that the slurry discharged from the aeration tank is subjected to a granular solid suspension biological treatment, at least a cationic polymer flocculant is added to the slurry flowing out from the aeration tank, and the resulting flocculation reaction liquid is mechanically dehydrated. be. Next, embodiments of the present invention will be described with reference to the drawings. First, raw water (raw human waste) 1 is filtered with impurities using a screen (not shown), etc., and then several silica sand particles with a particle size of 0.2 to 0.3 mm are added to it without diluting it with dilution water.
It flows into the aeration tank 2 with 10% (volume ratio) suspension and fluidization, and undergoes biological treatment for a predetermined residence time. Aeration tank 2
An air lift tube 3 is provided inside, and air 4 is supplied to the lower part of the tube. Fluidization of the silica sand and supply of oxygen to the silica sand are performed by air bubbles rising inside the air lift tube 3. Next, the silica sand is separated by sedimentation in the media separation section 5, and an effluent slurry 6, which is a mixed liquid of raw water SS, SS caused by proliferating microorganisms, and biologically treated water, is produced in the media separation section 5.
It flows out from. The slurry 6 discharged from the aeration tank 2 is temporarily stored in a storage tank 7 without passing through a gravity settling tank (final settling tank), unlike the conventional method, and then sent to a flocculation reaction tank 9 by a pump 8. Here, the cationic polymer flocculant 10 is added and mixed, and a flocculation reaction is carried out. The agglomerated reaction liquid 12 is supplied to a dehydrator 13 and separated into a dehydrated cake 14 and a dehydrated separated liquid 15. Note that 11 is a stirrer. The dehydrated separated liquid 15 can be discharged as is, or if more advanced treatment is required, it can be treated with sulfuric acid band,
It is coagulated and precipitated using an inorganic flocculant such as ferric chloride. In the present invention, it is preferable that the raw water is not diluted or diluted at a dilution rate of 5 times or less, but the significance of such limitations is as follows. That is, in the present invention, it is most rational to treat the raw water without dilution, but the effects of the present invention are not essentially lost as long as the dilution ratio is 5 times or less. If this is diluted more than 5 times, the treatment efficiency will decrease, the required volume of the granular media suspension aeration tank will increase, and the amount of water flowing into the dehydrator will increase, resulting in a significant increase in the size and power consumption of the dehydrator. This is because it is very disadvantageous in terms of initial costs and running costs, making it difficult to achieve the object of the present invention. Further, the residence time of the water to be treated in the aeration tank 2 (the amount of treated water in the aeration tank divided by the amount of inflow of raw water before dilution) is preferably 0.2 days or more. This is due to the quality of treated water (especially BOD) when the retention period is less than 0.2 days.
This is because the condition deteriorates significantly. The biological treatment applied in the present invention includes:
Any known biological treatment method is included, such as a biological nitrification denitrification method and an activated sludge method with a biological dephosphorization process. It goes without saying that any biological treatment process such as a rotating disk method, simple aeration method, or catalytic oxidation method may be interposed between the particulate solid suspended biological treatment process in the aeration tank and the dehydration process to perform multi-stage treatment. It is. For example, if a biological nitrification and denitrification treatment process is employed as the intervening biological treatment process, extremely effective treatment becomes possible. 〓〓〓〓〓
If biological treatment is performed in multiple stages in this way, even if granular solids such as silica sand flow out from the granular solid suspension biological treatment process, they will settle in the second biological treatment process and will not flow into the dewatering process. It also has the advantage of improving the flocculation of suspended solids (SS) and requiring only a small amount of cationic polymer flocculant. Note that it is also possible to perform the granular solid suspension biological treatment process in multiple stages. As described above, in the conventional activated sludge treatment without dilution, significant foaming occurs and treatment is often impossible without the use of an antifoaming agent or an antifoaming machine.However, according to the present invention, foaming is prevented. The treatment can be carried out extremely effectively with almost no generation.
Moreover, since there is no dilution, the amount of water to be treated is small, and the separation area of the medium separation section is extremely small.
During removal, the fermentation heat generated allows the water temperature in the aeration tank to be maintained at 30 to 35°C even in winter without requiring an external heat source. Due to the synergistic effect of the above-mentioned phenomena, the required residence time of the water to be treated in the aeration tank is 0.2 days or more.
One day is sufficient, and the fact that more than 90% of BOD can be removed with a residence time in the aeration tank of 0.2 days is something that was completely unexpected. In particular, one of the most important points of the present invention is that the final sedimentation tank for separating microbial flocs is omitted and the granular media suspended biological treatment process and mechanical dehydration process are combined, and the conventional method There is no other example of this. As described above, the present invention provides an aeration tank in which concentrated organic wastewater such as human waste is diluted undiluted or diluted at a dilution ratio of 5 times or less in advance, and granular solids with attached microorganisms are suspended and fluidized. By introducing at least a cationic polymer flocculant into the slurry flowing out from the aeration tank and mechanically dehydrating the resulting flocculation reaction liquid, BOD of 10,000 mg/or more of BOD such as human waste can be obtained. The highly concentrated organic wastewater can be processed without adding dilution water.
Furthermore, it is possible to carry out highly efficient and stable treatment with extremely small capacity equipment, eliminating not only the need for a final sedimentation tank, which was previously considered indispensable in the biological treatment process, but also eliminating the need for sludge return operations. , and the granular solid suspension aeration tank effluent is directly separated into solid and liquid using a dehydrator, so solid-liquid separation can be achieved reliably regardless of the sedimentation properties of microorganisms, and maintenance and management are also extremely easy. It is. Next, an example of the non-dilution treatment of human waste according to the present invention will be described. A undiluted treatment experiment was conducted on raw human waste collected from a human waste treatment plant in F City, Kanagawa Prefecture, which has the water quality shown in Table 1, at an inflow rate of 0.1 to 3 Kl/day.
【表】
ことを表わす。
実験装置のフローシートは図面に示したとおり
であつて、実験条件は次のとおりである。曝気槽
容積は0.5m3で粒状固体としては粒径0.2〜0.3mmの
硅砂を使用し、硅砂の投入量は曝気槽容積に対し
30％（容積比）とした。酸素供給は空気を図面に
示したエアリフトチユーブに吹込む方法によつ
た。カチオン性高分子凝集剤としてはフローナツ
ク（商品名）を採用し、注入率SSに対し2.0％に
設定した。脱水機としてはＴ社製スクリユーデカ
ンタを使用した。
曝気槽における処理水の滞留時間0.1〜10日の
範囲に設定し、滞留時間に対する処理水としての
脱水分離液のBODおよびCOD―Mnの変化を調べ
た。その結果は第２表のとおりである。なお脱水
ケーキの含水率は80〜83％であつた。
〓〓〓〓〓
[Table] represents something.
The flow sheet of the experimental apparatus is as shown in the drawing, and the experimental conditions are as follows. The volume of the aeration tank is 0.5 m3 , and silica sand with a particle size of 0.2 to 0.3 mm is used as the granular solid, and the amount of silica sand input is proportional to the volume of the aeration tank.
30% (volume ratio). Oxygen was supplied by blowing air into the air lift tube shown in the drawing. Flownac (trade name) was used as the cationic polymer flocculant, and the injection rate was set to 2.0% with respect to SS. A screw decanter manufactured by T Company was used as a dehydrator. The residence time of the treated water in the aeration tank was set in the range of 0.1 to 10 days, and the changes in BOD and COD-Mn of the dehydrated separated liquid as treated water with respect to the residence time were investigated. The results are shown in Table 2. The moisture content of the dehydrated cake was 80 to 83%. 〓〓〓〓〓
【表】
この実験において粒状固体懸濁曝気槽内の
MLVSSは、25000〜30000mg／であり、粒状粉
体を分離した媒体分離部からの流出液中のSSは
10000〜12000mg／であつた。
第２表に示したように、本発明によれば90％以
上のBOD除去率を得るには、滞留日数は0.2日以
上で充分であり、COD―Mnは、滞留日数２日以
上では、逆に増加した。これはNO2―Ｎの生成に
起因するものである。このようなNO2―Ｎの生成
を防ぐには、公知の生物学的硝化脱窒素処理を採
用すればよいことは言うまでもない。
次に、第２表に記載の滞留日数１日における脱
水分離液を硫酸バンドを1000〜2000mg／の注入
率（対SS）で注入して凝集沈殿処理した場合の
処理水質は第３表のようになつた。[Table] In this experiment, the granular solid suspension in the aeration tank was
The MLVSS is 25,000 to 30,000 mg/, and the SS in the effluent from the media separation section that separated the granular powder is
It was 10000-12000mg/. As shown in Table 2, according to the present invention, in order to obtain a BOD removal rate of 90% or more, a retention period of 0.2 days or more is sufficient, and COD-Mn is increased to This is due to the generation of NO 2 -N. It goes without saying that in order to prevent the production of NO 2 -N, a known biological nitrification and denitrification treatment may be employed. Next, when the dehydrated separated liquid with a retention period of 1 day listed in Table 2 is subjected to coagulation and sedimentation treatment by injecting sulfuric acid band at an injection rate of 1000 to 2000 mg/SS (vs. SS), the treated water quality is as shown in Table 3. It became.
【表】
第１表と第３表のデータを比較することによ
り、BODについては、凝集沈殿処理水を２倍希
釈すれば現在のし尿処理放流水質基準に充分合致
できること、原水（生し尿）と滞留日数１日にお
ける脱水分離液の凝集沈殿処理水のBODがそれ
ぞれ10500及び40〜55であることから、従来法に
おいて20倍希釈原水のBODを約90％除去したの
と同等の処理効果が得られたことがわかる。[Table] By comparing the data in Tables 1 and 3, it was found that BOD can sufficiently meet the current quality standards for wastewater treatment effluent if coagulation and sedimentation treated water is diluted 2 times, and that raw water (raw human waste) and Since the BOD of the coagulation-sedimentation treated water of the dehydrated separated liquid after one day of retention is 10,500 and 40-55, respectively, the treatment effect is equivalent to that of removing approximately 90% of the BOD of the 20-fold diluted raw water using the conventional method. I can see that it was done.
図面は本発明の実施態様を示す系統説明図であ
る。
１…原水、２…曝気槽、３…エアリフトチユー
ブ、４…空気、３…媒体分離部、６…流出スラリ
ー、７…貯槽、８…ポンプ、９…凝集反応槽、１
０…カチオン性高分子凝集剤、１１…脱水機。
〓〓〓〓〓
The drawings are system explanatory diagrams showing embodiments of the present invention. 1... Raw water, 2... Aeration tank, 3... Air lift tube, 4... Air, 3... Media separation section, 6... Outflow slurry, 7... Storage tank, 8... Pump, 9... Coagulation reaction tank, 1
0...Cationic polymer flocculant, 11...Dehydrator. 〓〓〓〓〓
Claims (1)
ま、又は予め５倍以下の希釈倍率で希釈した後、
微生物が付着した粒状固体を懸濁流動させている
曝気槽に導入して粒状固体懸濁生物処理を行い、
前記曝気槽からの流出スラリーに少なくともカチ
オン性高分子凝集剤を添加し、得られる凝集反応
液を機械脱水することを特徴とするし尿系汚水の
処理方法。 ２ 前記凝集剤添加工程が、前記曝気槽からの流
出スラリーをさらに前記粒状固体懸濁生物処理と
は別の生物学的処理によつて処理した後に行われ
るのである特許請求の範囲第１項記載の処理方
法。 ３ 前記生物学的処理工程が、生物学的硝化脱窒
素処理工程である特許請求の範囲第２項記載の処
理方法。[Claims] 1. Concentrated organic wastewater such as human waste, either undiluted or after being diluted in advance at a dilution ratio of 5 times or less,
Particulate solids with attached microorganisms are introduced into an aeration tank where they are suspended and fluidized to perform particulate solid suspension biological treatment.
A method for treating night soil wastewater, which comprises adding at least a cationic polymer flocculant to the slurry flowing out from the aeration tank, and mechanically dewatering the resulting flocculation reaction liquid. 2. According to claim 1, the flocculant addition step is performed after the slurry flowing out from the aeration tank is further treated by a biological treatment different from the granular solid suspension biological treatment. processing method. 3. The treatment method according to claim 2, wherein the biological treatment step is a biological nitrification and denitrification treatment step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15847279A JPS5681190A (en) | 1979-12-06 | 1979-12-06 | Decomposition of sewage such as night soil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15847279A JPS5681190A (en) | 1979-12-06 | 1979-12-06 | Decomposition of sewage such as night soil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5681190A JPS5681190A (en) | 1981-07-02 |
| JPS6159798B2 true JPS6159798B2 (en) | 1986-12-18 |
Family
ID=15672485
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15847279A Granted JPS5681190A (en) | 1979-12-06 | 1979-12-06 | Decomposition of sewage such as night soil |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5681190A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58139798A (en) * | 1982-02-12 | 1983-08-19 | Ebara Infilco Co Ltd | Treatment of organic waste liquid |
| KR100352243B1 (en) * | 1999-12-10 | 2002-09-16 | 에스아이비(주) | A Treatment Method for Livestock Wastewater |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5376547A (en) * | 1976-12-20 | 1978-07-07 | Ataka Kensetsu Kougiyou Kk | Device for treating waste water |
| JPS543365A (en) * | 1977-06-09 | 1979-01-11 | Hitachi Zosen Corp | Disposal of raw sewage |
| JPS544469A (en) * | 1977-06-11 | 1979-01-13 | Kubota Ltd | Mathod of treating raw system organic waste water at high efficiency |
| JPS5412150A (en) * | 1977-06-29 | 1979-01-29 | Kurita Water Ind Ltd | Flow bed type filthy water treating device |
| JPS5413665A (en) * | 1977-07-04 | 1979-02-01 | Ebara Infilco Co Ltd | Process for treating organic waste water |
| JPS54136746A (en) * | 1978-04-14 | 1979-10-24 | Nippon Kentetsu Co Ltd | Waste water disposal process |
-
1979
- 1979-12-06 JP JP15847279A patent/JPS5681190A/en active Granted
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5376547A (en) * | 1976-12-20 | 1978-07-07 | Ataka Kensetsu Kougiyou Kk | Device for treating waste water |
| JPS543365A (en) * | 1977-06-09 | 1979-01-11 | Hitachi Zosen Corp | Disposal of raw sewage |
| JPS544469A (en) * | 1977-06-11 | 1979-01-13 | Kubota Ltd | Mathod of treating raw system organic waste water at high efficiency |
| JPS5412150A (en) * | 1977-06-29 | 1979-01-29 | Kurita Water Ind Ltd | Flow bed type filthy water treating device |
| JPS5413665A (en) * | 1977-07-04 | 1979-02-01 | Ebara Infilco Co Ltd | Process for treating organic waste water |
| JPS54136746A (en) * | 1978-04-14 | 1979-10-24 | Nippon Kentetsu Co Ltd | Waste water disposal process |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5681190A (en) | 1981-07-02 |
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