JPH0632831B2 - Organic wastewater treatment method - Google Patents
Organic wastewater treatment methodInfo
- Publication number
- JPH0632831B2 JPH0632831B2 JP62200944A JP20094487A JPH0632831B2 JP H0632831 B2 JPH0632831 B2 JP H0632831B2 JP 62200944 A JP62200944 A JP 62200944A JP 20094487 A JP20094487 A JP 20094487A JP H0632831 B2 JPH0632831 B2 JP H0632831B2
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- sludge
- slurry
- denitrification
- organic wastewater
- 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
- 238000004065 wastewater treatment Methods 0.000 title 1
- 239000012528 membrane Substances 0.000 claims description 35
- 239000010802 sludge Substances 0.000 claims description 31
- 238000000034 method Methods 0.000 claims description 23
- 238000000926 separation method Methods 0.000 claims description 22
- 239000002002 slurry Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052698 phosphorus Inorganic materials 0.000 claims description 8
- 239000011574 phosphorus Substances 0.000 claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 5
- 238000005345 coagulation Methods 0.000 claims description 3
- 230000015271 coagulation Effects 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000011575 calcium Substances 0.000 description 17
- 239000007788 liquid Substances 0.000 description 9
- 239000001506 calcium phosphate Substances 0.000 description 7
- 229910000389 calcium phosphate Inorganic materials 0.000 description 7
- 235000011010 calcium phosphates Nutrition 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 7
- 210000002700 urine Anatomy 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 5
- 239000010800 human waste Substances 0.000 description 4
- 239000012466 permeate Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910017119 AlPO Inorganic materials 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 244000144992 flock Species 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、し尿系汚水その他のリンと窒素成分を含む有
機性汚水を新規なプロセスにより合理的に処理し、常に
安定して高度の処理水を得る方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial field of application] The present invention reasonably treats human wastewater sewage and other organic sewage containing phosphorus and nitrogen components by a novel process, and always provides stable and advanced treatment. It is about how to get water.
し尿系汚水等を処理するのに、最も代表的なプロセス
は、 というプロセスであるが、このプロセスは固液分離が不
安定で、かつ難脱水性の凝集沈殿汚泥が大量に発生する
という大きな欠点があった。The most typical process for treating human waste system wastewater is However, this process has the major drawbacks that solid-liquid separation is unstable and a large amount of coagulation sedimentation sludge, which is difficult to dehydrate, is generated.
一方、ごく最近では、 という新しいプロセスが提案され、数ケ所で実用化され
た。このプロセスは、固液分離が確実であり、しかも凝
集沈殿工程が不要であるという長所がある反面、pH調
整、再中和、吸着材の再生及び再生廃液の処分という繁
雑な工程を必要とするリン吸着除去工程を限外過膜
（ＵＦ膜）分離工程のあとに配備しなければならないと
いう欠点をもっている。On the other hand, most recently, A new process was proposed and put into practical use in several places. This process has the advantage that solid-liquid separation is reliable and that the coagulation-sedimentation step is not necessary, but it requires complicated steps such as pH adjustment, re-neutralization, regeneration of adsorbent and disposal of regeneration waste liquid. It has a drawback that the phosphorus adsorption removal step must be arranged after the ultrafiltration membrane (UF membrane) separation step.
このようなリン吸着除去工程を設けなくてはならない理
由は、ＵＦ膜ではPO4 3-が全く除去されずにそのまま透
過してしまうためであり、これがＵＦ膜を使う活性汚泥
処理法の最大の問題点であった。The reason why such a phosphorus adsorption / removal step must be provided is that PO 4 3− is not removed at all in the UF membrane and permeates as it is, which is the maximum of the activated sludge treatment method using the UF membrane. It was a problem.
本発明は、これらの従来法のもつ問題点を解決すること
を課題としており、具体的には、 凝集沈殿処理を省略してなおかつ充分なリン除去率を
得ること。An object of the present invention is to solve the problems of these conventional methods, and specifically, to omit the coagulation-precipitation treatment and to obtain a sufficient phosphorus removal rate.
ＵＦ膜分離工程のあとに、PO4 3-吸着除去工程を設け
ることを不要にすること。Eliminating the need for a PO 4 3- adsorption removal step after the UF membrane separation step.
汚泥の脱水性を改善すること。To improve the dewaterability of sludge.
プロセス構成を一層簡潔化すること。Further simplify the process structure.
汚泥の肥料的価値を高めること。すなわち、植物にと
って利用容易な形態のリン酸化合物を豊富に含んだ汚泥
脱水ケーキを生産すること。To increase the fertilizer value of sludge. That is, to produce a sludge dewatering cake rich in phosphate compounds in a form that is easy for plants to use.
水酸化アルミ、水酸化鉄などのバルキーで難濃縮脱水
性汚泥の発生を防ぎ、汚泥処理工程を合理化すること。To prevent the generation of difficult-to-concentrate dehydrated sludge with bulky aluminum hydroxide, iron hydroxide, etc., and to streamline the sludge treatment process.
を目的としている。It is an object.
本発明は、リン及び窒素成分を含む有機性汚水を生物学
的硝化脱窒素工程で処理し、得られた活性汚泥スラリー
にCa2+を添加混和してpH7.0〜9.5の条件下に維持しつつ
膜分離し、この膜透過水にFe3+を添加してCa2+の共存下
で凝集分離することを特徴とする有機性汚水の処理方法
である。The present invention treats organic wastewater containing phosphorus and nitrogen components in a biological nitrification and denitrification step, and adds Ca 2+ to the resulting activated sludge slurry to mix and maintain it under conditions of pH 7.0 to 9.5. A method for treating organic sewage is characterized by performing membrane separation while simultaneously performing the membrane separation, and adding Fe 3+ to the membrane permeated water to perform coagulation separation in the presence of Ca 2+ .
以下に本発明の一実施例態様を示す図面を参照しなが
ら、し尿処理を例にあげて本発明の作用を説明する。Hereinafter, the operation of the present invention will be described with reference to the drawings showing one embodiment of the present invention, taking human waste treatment as an example.
まず、スクリーン等によって除渣した除渣し尿１を希釈
することなく生物学的硝化脱窒素工程２に供給し、硝化
脱窒素処理する。次に生物学的硝化脱窒素工程２で得ら
れた活性汚泥スラリーにCa2+3(CaCl2,Ca(OH))2のいずれ
かが好適である）を添加するが、その添加場所は図示例
のように生物学的硝化脱窒素工程２内の最終段の脱窒素
部２′等の工程内で添加したり、この工程から流出する
活性汚泥スラリーに添加するようにしても良い。First, the removed urine 1 removed by a screen or the like is supplied to the biological nitrification and denitrification step 2 without being diluted, and nitrification and denitrification is performed. Next, Ca 2+ 3 (either CaCl 2 or Ca (OH)) 2 is suitable) is added to the activated sludge slurry obtained in the biological nitrification and denitrification step 2. As shown in the example, it may be added in the process such as the final denitrification section 2'in the biological nitrification and denitrification process 2, or may be added to the activated sludge slurry flowing out from this process.
Ca2+3を添加した活性汚泥スラリーはpH7.0〜9.5、好ま
しくは8.0〜9.0の条件下に維持されるが、好適には１０
〜４８時間滞留されると良く、この過程で活性汚泥スラ
リー中のPO4 3-の大部分は、 ５Ca2+＋OH-＋３PO4 3-→Ca5(OH)(PO4)3↓ などのリン酸カルシウム沈殿生成反応によって、不溶性
ＳＳに転換される。The activated sludge slurry containing Ca 2+ 3 is maintained under the conditions of pH 7.0 to 9.5, preferably 8.0 to 9.0, and preferably 10
Well Once residence 48 hours, PO 4 3- majority of the activated sludge in the slurry during this process, 5Ca 2+ + OH - + 3PO 4 3- → Ca 5 (OH) (PO 4) 3 ↓ calcium phosphate such as It is converted to insoluble SS by the precipitation reaction.
しかも極めて興味深いことに、活性汚泥スラリーの液側
に含まれている非生物分解性ＣＯＤ成分（色度成分な
ど）は、リン酸カルシウム沈殿物の界面に吸着されて効
果的に除去されることが知見された。このように、し尿
中の非生物分解性COD成分が、低アルカリ性領域におい
てリン酸カルシウムによって非常に効果的に除去される
ことは、従来知られていなかった知見である。Moreover, it is extremely interesting to find that the non-biodegradable COD components (such as chromaticity components) contained on the liquid side of the activated sludge slurry are adsorbed to the interface of the calcium phosphate precipitate and effectively removed. It was Thus, it is a previously unknown finding that the non-biodegradable COD component in human waste is very effectively removed by calcium phosphate in the low alkaline region.
しかして、ＣＯＤ成分を吸着したリン酸カルシウム沈殿
を含んだスラリー４を、限外過膜（UF膜）、精密過
膜（ＭＦ膜）などの膜分離工程５に供給して膜分離し、
極めて清澄（ＳＳゼロ）な膜透過水６と膜分離スラリー
７とに分離する。Then, the slurry 4 containing the calcium phosphate precipitate which has adsorbed the COD component is supplied to a membrane separation step 5 such as an ultrapermeation membrane (UF membrane) or a precision permeation membrane (MF membrane) to perform membrane separation,
It is separated into extremely clear (SS zero) membrane permeated water 6 and membrane separation slurry 7.
分離された膜分離スラリー７の大部分は、返送汚泥８と
して生物学的硝化脱窒素工程２にリサイクルされ、残部
は余剰汚泥９として汚泥脱水工程等へ導かれる。Most of the separated membrane separation slurry 7 is recycled to the biological nitrification and denitrification step 2 as return sludge 8, and the rest is guided to the sludge dewatering step etc. as excess sludge 9.
一方、膜透過水６はＳＳゼロの弱アルカリ性の清澄液で
あるが、PO4 3-，ＣＯＤ，色度が微量残存しており、さ
らに前段で添加したCa2+の一部が残留して含まれている
という水質的特徴を示す。Meanwhile, although the film permeate 6 is a weak alkaline clear solution of SS zero, PO 4 3-, COD, chromaticity and trace amount remains, still a part of the added Ca 2+ above with residual It shows the water quality characteristic of being contained.
本発明の第２のポイントは、このCa2+を含んだ膜透過水
６という特定の液に対し、少量のFe3+１０（FeCl3，ポ
リ硫酸鉄の使用が好適である）を添加して凝集分離する
点にあり、Ca2+が不足している時にはこれを適宜補給す
る。The second point of the present invention is to add a small amount of Fe 3+ 10 (FeCl 3 is preferable to use polyiron sulfate) to the specific liquid called the membrane permeated water 6 containing Ca 2+. When Ca 2+ is insufficient, it is replenished appropriately.
すなわち、本発明の技術思想の骨子は、生物学的硝化脱
窒素工程２で得られた活性汚泥スラリーに対してCa2+を
添加して膜分離し、この膜透過水６に対してCa2+の共存
下でさらにFe3+１０を添加するという独自のプロセス構
成によって、し尿中の非生物分離性の種々の成分を効果
的に除去する方法を確立した点にある。That is, the essence of the technical idea of the present invention is that Ca 2+ is added to the activated sludge slurry obtained in the biological nitrification and denitrification step 2 to perform membrane separation, and Ca 2 + is added to the membrane permeated water 6. The point is the establishment of a method for effectively removing various non-bioseparable components in human urine by the unique process configuration of adding Fe 3+ 10 in the presence of + .
このように、Ca2+の共存下で膜透過水６に対して微量の
Fe3+１０を添加して混和すると（pHは４〜５が最適であ
る）、膜透過水６に残留するCOD，色度，PO4 3-が効果的
に凝集フロックとなり、固液分離工程１１で凝集フロッ
クが除去されて処理水１２となる。固液分離工程１１と
しては各種公知のものを適用することができるが、粒状
材による過法が最適である。また、固液分離工程１
１で分離された凝集フロック１３は、膜分離工程５から
の返送汚泥８と共に生物学的硝化脱窒素工程２にリサイ
クルされる。Thus, in the presence of Ca 2+ , a small amount of
When Fe 3+ 10 is added and mixed (pH is optimally 4 to 5), COD, chromaticity, and PO 4 3− remaining in the membrane permeate 6 effectively become floc and solid-liquid separation step. At 11, the flocs are removed to form treated water 12. As the solid-liquid separation step 11, various known ones can be applied, but the pasting method using a granular material is most suitable. In addition, solid-liquid separation step 1
The flocculated flocs 13 separated in 1 are recycled to the biological nitrification and denitrification step 2 together with the returned sludge 8 from the membrane separation step 5.
なお、膜分離工程５から排出される余剰汚泥９には、脱
水性の良いリン酸カルシウム沈殿が多量に含まれ、難脱
水性のFe(OH)3はわずかしか含有されていないので、ベ
ルトプレス，フィルタプレス，スクリュープレスなどの
脱水機で水分７０〜７２％という低水分の脱水ケーキに
することができる。しかも脱水ケーキには、リンが植物
によって容易に利用できるリン酸カルシウムの形態で含
まれているので、肥料として利用するのに適している
（従来プロセスにおいて、PO4 3-を硫酸アルミニウムな
どで凝集沈殿する際に発生するAlPO4は植物にとって利
用できない）。Since the excess sludge 9 discharged from the membrane separation step 5 contains a large amount of calcium phosphate precipitate having good dehydration property and contains only a small amount of Fe (OH) 3 which is difficult to dehydrate, the belt press and the filter. A dehydrator such as a press or a screw press can be used to form a dehydrated cake having a low water content of 70 to 72%. Moreover, phosphorus is contained in the dehydrated cake in the form of calcium phosphate, which can be easily used by plants, so it is suitable for use as a fertilizer (in the conventional process, PO 4 3− is aggregated and precipitated with aluminum sulfate, etc.). AlPO 4 generated at this time is not available to plants).
滋賀県Ｉ衛生プラントに搬入されたし尿を目開き0.5mm
目のウェッジワイヤスクリーンで除渣し、表−１の水質
を示す除渣し尿を得た。Open 0.5 mm of human waste that has been brought into the Shiga Prefecture I Sanitation Plant
Urine was removed with a wedge wire screen to obtain the urine having the water quality shown in Table 1.
この除渣し尿を、公知の硝化液循環タイプの生物学的硝
化脱窒素工程（第１脱窒素槽→硝化槽→第２脱窒素槽の
順に直列配置したプロセス）に供給し、生物処理を行な
った。運転条件は表−２のように設定した。 This decontamination urine is supplied to a known nitrification solution circulation type biological nitrification and denitrification process (process in which the first denitrification tank → the nitrification tank → the second denitrification tank are arranged in series in this order) to perform biological treatment. It was The operating conditions were set as shown in Table-2.
次に、第２脱窒素槽（滞留日数２日）内の活性汚泥スラ
リーに対し、CaCl2を600〜800mg／as Ca2+添加し、さ
らにNaOHを添加して第２脱窒素槽内スラリーのpHを8.0
〜9.0に制御した。しかるのち、この活性汚泥スラリー
をチューブラタイプのＵＦ膜（分画分子量約１０万）に
圧力３〜４Kgf／cm2でポンプ圧入し、クロスフローで膜
分離した。この結果、UF膜透過水量は1.5m3／日・m2膜
面積が得られ、膜透過の水質は表−３に示す値であっ
た。 Next, 600 to 800 mg / as Ca 2+ of CaCl 2 was added to the activated sludge slurry in the second denitrification tank (retention days 2 days), and further NaOH was added to the slurry in the second denitrification tank. pH 8.0
Controlled to ~ 9.0. Then, this activated sludge slurry was pumped into a tubular type UF membrane (molecular weight cutoff of about 100,000) at a pressure of 3 to 4 Kgf / cm 2 , and the membrane was separated by cross flow. As a result, the amount of UF membrane permeation water was 1.5 m 3 / day · m 2 membrane area, and the water quality of membrane permeation was the value shown in Table 3.
また、第２脱窒素槽内スラリーのpHを9.5より高い値に
制御した場合は、脱窒素菌の活性が劣化し、表−３の水
質のうちT-Nが３８〜４６mg／と大きく悪化した。 Further, when the pH of the slurry in the second denitrification tank was controlled to a value higher than 9.5, the activity of the denitrifying bacteria was deteriorated, and TN in the water quality of Table-3 was greatly deteriorated to 38 to 46 mg /.
これらの結果から、Ca2+が添加された活性汚泥スラリー
のpHを7.0〜9.5の範囲に制御することが重要であること
が認められた。From these results, it was confirmed that it is important to control the pH of the activated sludge slurry containing Ca 2+ in the range of 7.0 to 9.5.
次に、表−３のＵＦ膜透過水に対し、FeCl3を２５０〜
３００mg／添加し、pH5.0の条件で攪拌したところ、
良好なフロック形成が起き、合成樹脂（ポリウレタン）
を材とした過槽にＬＶ＝１０ｍ／hrで供給して過
した結果、表−４に示す処理水を得た。Next, FeCl 3 is added to the UF membrane permeated water in Table 3 at 250
300mg / added and stirred at pH 5.0,
Good flock formation occurs, synthetic resin (polyurethane)
As a result of supplying LV = 10 m / hr to the over tank made from the above, the treated water shown in Table 4 was obtained.
表−４から明らかなように、ＣＯＤ，PO4 3-，色度が表
−３のＵＦ膜透過水より著しく低下していた。As apparent from Table -4, COD, PO 4 3-, chromaticity was decreased significantly from UF membrane permeate in Table -3.
〔発明の効果〕 本発明によれば、次のような数多くの効果を得ることが
でき、従来プロセスの諸欠点を解決することができる。 [Effects of the Invention] According to the present invention, the following numerous effects can be obtained, and various drawbacks of conventional processes can be solved.
Ca2+とFe3+の両者を独自な方法、条件で添加するよう
にした結果、ＣＯＤ，PO4 3-，色度を極めて効果的に除
去することが可能になり、薬剤の使用量も節減できる。Ca 2+ and Fe 3+ both its own way, as a result of such addition under the conditions, COD, PO 4 3-, it is possible to very effectively eliminate the chromaticity, the amount of the drug is also You can save money.
難脱水性のAl系スラッジが全く発生しない Fe系スラッジの発生量が従来の約1/10に低減する一
方、脱水性の良いリン酸カルシウムスラッジを多量に含
んだ汚泥が発生するので、汚泥脱水が容易である。No hard-dehydrating Al-based sludge is generated at all Fe-based sludge is reduced to about 1/10 of the conventional amount, while sludge containing a large amount of calcium phosphate sludge with good dewatering properties is generated, so sludge dewatering is easy Is.
汚泥脱水ケーキ、又は脱水ケーキの乾燥物、焼却灰に
は植物にとって利用容易なリンとカルシウムを含んでい
るので、肥料として有効利用できる。The sludge dewatering cake, the dried cake of the dewatering cake, and the incinerated ash contain phosphorus and calcium, which are easy for plants to use, and thus can be effectively used as fertilizers.
維持管理が煩雑でランニングコストも高いリン酸吸着
工程が不要になる。The phosphoric acid adsorption step, which requires complicated maintenance and high running cost, becomes unnecessary.
処理水のＣＯＤ，色度は従来プロセスよりも低濃度に
なるので、その後活性炭吸着処理する場合にその処理コ
ストが著しく節減される。Since the COD and chromaticity of the treated water are lower than those of the conventional process, the treatment cost for the activated carbon adsorption treatment is significantly reduced.
【図面の簡単な説明】 第１図は本発明の一実施態様を示すフローシートであ
る。 １……除渣し尿、２……生物学的硝化脱窒素工程、２′
……最終段の脱窒素部、３……Ca2+、４……スラリー、
５……膜分離工程、６……膜透過水、７……膜分離スラ
リー、８……返送汚泥、９……余剰汚泥、１０……F
e3+、１１……固液分離工程、１２……処理水、１３…
…凝集フロック。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a flow sheet showing an embodiment of the present invention. 1 ... Waste urine, 2 ... Biological nitrification and denitrification process, 2 '
...... Final denitrification part, 3 ... Ca 2+ , 4 ... slurry,
5 ... Membrane separation process, 6 ... Membrane permeated water, 7 ... Membrane separation slurry, 8 ... Return sludge, 9 ... Excess sludge, 10 ... F
e 3+ , 11 ... Solid-liquid separation process, 12 ... Treated water, 13 ...
… Cohesive flocs.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.5 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０２Ｆ 3/34 １０１ Ａ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 5 Identification code Office reference number FI technical display location C02F 3/34 101 A
Claims (1)
学的硝化脱窒素工程で処理し、得られた活性汚泥スラリ
ーにCa2+を添加混和してpH7.0〜9.5の条件下に維持しつ
つ膜分離し、この膜透過水にFe3+を添加してCa2+の共存
下で凝集分離することを特徴とする有機性汚水の処理方
法。1. An organic wastewater containing phosphorus and nitrogen components is treated in a biological nitrification and denitrification step, and Ca 2+ is added to the obtained activated sludge slurry and mixed under the conditions of pH 7.0 to 9.5. A method for treating organic wastewater, which comprises performing membrane separation while maintaining, and adding Fe 3+ to the membrane permeated water to perform coagulation separation in the presence of Ca 2+ .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62200944A JPH0632831B2 (en) | 1987-08-13 | 1987-08-13 | Organic wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62200944A JPH0632831B2 (en) | 1987-08-13 | 1987-08-13 | Organic wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6447499A JPS6447499A (en) | 1989-02-21 |
| JPH0632831B2 true JPH0632831B2 (en) | 1994-05-02 |
Family
ID=16432895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62200944A Expired - Lifetime JPH0632831B2 (en) | 1987-08-13 | 1987-08-13 | Organic wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0632831B2 (en) |
-
1987
- 1987-08-13 JP JP62200944A patent/JPH0632831B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6447499A (en) | 1989-02-21 |
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