JP2004230377A - Method for treating organic waste water - Google Patents
Method for treating organic waste water Download PDFInfo
- Publication number
- JP2004230377A JP2004230377A JP2003428166A JP2003428166A JP2004230377A JP 2004230377 A JP2004230377 A JP 2004230377A JP 2003428166 A JP2003428166 A JP 2003428166A JP 2003428166 A JP2003428166 A JP 2003428166A JP 2004230377 A JP2004230377 A JP 2004230377A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- membrane
- liquid
- organic wastewater
- solubilization
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title abstract description 32
- 239000010815 organic waste Substances 0.000 title abstract 4
- 239000007788 liquid Substances 0.000 claims abstract description 113
- 238000005063 solubilization Methods 0.000 claims abstract description 86
- 230000007928 solubilization Effects 0.000 claims abstract description 86
- 238000011282 treatment Methods 0.000 claims abstract description 78
- 238000006243 chemical reaction Methods 0.000 claims abstract description 68
- 239000010802 sludge Substances 0.000 claims abstract description 68
- 239000002351 wastewater Substances 0.000 claims abstract description 58
- 239000012528 membrane Substances 0.000 claims description 82
- 238000000926 separation method Methods 0.000 claims description 43
- 238000005374 membrane filtration Methods 0.000 claims description 27
- 238000001914 filtration Methods 0.000 claims description 26
- 239000000706 filtrate Substances 0.000 claims description 21
- 244000005700 microbiome Species 0.000 claims description 13
- 238000000108 ultra-filtration Methods 0.000 claims description 12
- 238000001471 micro-filtration Methods 0.000 claims description 11
- 230000000694 effects Effects 0.000 claims description 9
- 108091005804 Peptidases Proteins 0.000 claims description 8
- 239000004365 Protease Substances 0.000 claims description 7
- 102100037486 Reverse transcriptase/ribonuclease H Human genes 0.000 claims description 7
- 230000000813 microbial effect Effects 0.000 claims description 6
- 230000003381 solubilizing effect Effects 0.000 claims description 3
- 239000012466 permeate Substances 0.000 claims description 2
- 239000000126 substance Substances 0.000 description 16
- 239000012141 concentrate Substances 0.000 description 12
- 239000011148 porous material Substances 0.000 description 10
- 239000007787 solid Substances 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 108010041102 azocasein Proteins 0.000 description 8
- 238000012360 testing method Methods 0.000 description 8
- 102000004190 Enzymes Human genes 0.000 description 7
- 108090000790 Enzymes Proteins 0.000 description 7
- 238000011001 backwashing Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 7
- 239000012510 hollow fiber Substances 0.000 description 7
- 239000006228 supernatant Substances 0.000 description 7
- 238000002835 absorbance Methods 0.000 description 6
- 238000005273 aeration Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000010998 test method Methods 0.000 description 6
- 238000011010 flushing procedure Methods 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 239000008363 phosphate buffer Substances 0.000 description 4
- 229920002492 poly(sulfone) Polymers 0.000 description 4
- 238000003672 processing method Methods 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 108010067770 Endopeptidase K Proteins 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000011088 calibration curve Methods 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 208000028659 discharge Diseases 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010408 film Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 230000029058 respiratory gaseous exchange Effects 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 229920002307 Dextran Polymers 0.000 description 1
- 241000193385 Geobacillus stearothermophilus Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 102000035195 Peptidases Human genes 0.000 description 1
- 239000001888 Peptone Substances 0.000 description 1
- 108010080698 Peptones Proteins 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000002202 Polyethylene glycol Substances 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000006911 enzymatic reaction Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 102000034238 globular proteins Human genes 0.000 description 1
- 108091005896 globular proteins Proteins 0.000 description 1
- 239000010800 human waste Substances 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 235000013372 meat Nutrition 0.000 description 1
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
- 235000019796 monopotassium phosphate Nutrition 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 235000019319 peptone Nutrition 0.000 description 1
- 239000008055 phosphate buffer solution Substances 0.000 description 1
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920002239 polyacrylonitrile Polymers 0.000 description 1
- -1 polyethylene Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000007655 standard test method Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- YNJBWRMUSHSURL-UHFFFAOYSA-N trichloroacetic acid Chemical compound OC(=O)C(Cl)(Cl)Cl YNJBWRMUSHSURL-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004804 winding 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
Abstract
Description
本発明は、有機性廃水を生物反応により処理する方法に関する。 The present invention relates to a method for treating organic wastewater by a biological reaction.
有機性廃水を処理する方法としては、活性汚泥法と呼ばれる好気性生物処理法が、最も一般的に実施されている。この方法は、例えば図２に示すように、有機性廃水貯留槽１から生物反応槽３に導入された下水などの有機性廃水が、生物反応槽３において好気性条件にて、微生物による酸化分解反応である生物酸化によって、二酸化炭素もしくは水などの無機物にまで分解される方法である。そして、生物反応槽３にて処理された有機性廃水は、固液分離槽５にて処理水３０１と汚泥３０２に固液分離され、汚泥３０２の一部は微生物源として生物反応槽３に返送されるとともに、残りの汚泥は余剰汚泥３０３として廃棄等の処理をされているのが一般的である。 As a method for treating organic wastewater, an aerobic biological treatment method called an activated sludge method is most commonly performed. In this method, as shown in FIG. 2, for example, organic wastewater such as sewage introduced from an organic wastewater storage tank 1 into a biological reaction tank 3 is oxidatively decomposed by microorganisms under aerobic conditions in the biological reaction tank 3. This is a method of decomposing to inorganic substances such as carbon dioxide or water by biological oxidation as a reaction. The organic wastewater treated in the biological reaction tank 3 is solid-liquid separated into treated water 301 and sludge 302 in the solid-liquid separation tank 5, and a part of the sludge 302 is returned to the biological reaction tank 3 as a microorganism source. At the same time, the remaining sludge is generally disposed of as excess sludge 303 by disposal or the like.
このため、できるだけ余剰汚泥を排出しない処理方法として、近年、余剰汚泥を可溶化処理槽で可溶化して、可溶化した汚泥を生物反応槽にもどし、再び生物処理する方法が提案されている。例えば、汚泥を高温好気状態の可溶化処理槽で好熱菌により可溶化し、その液を生物反応槽に戻すことで、活性汚泥法において、余剰汚泥を減容化する技術が開示されている（例えば特許文献１）。
また、可溶化処理槽部分に投入する汚泥を濃縮機などを利用して、水分率９９％以下にすることで可溶化処理槽の大きさを小さくできる技術が開示されている（例えば特許文献２）。
Therefore, as a treatment method that does not discharge excess sludge as much as possible, in recent years, a method has been proposed in which excess sludge is solubilized in a solubilization treatment tank, the solubilized sludge is returned to the biological reaction tank, and biological treatment is performed again. For example, a technique for reducing the volume of excess sludge in the activated sludge method by solubilizing sludge with a thermophilic bacterium in a solubilization treatment tank in a high-temperature aerobic state and returning the solution to a biological reaction tank has been disclosed. (For example, Patent Document 1).
Further, there is disclosed a technology in which the size of the solubilization tank can be reduced by reducing the water content of the sludge to be supplied to the solubilization tank to 99% or less using a concentrator (for example, Patent Document 2). ).
さらに、可溶化後に固液分離装置を利用して、固体部分を再度可溶化処理することと曝気槽に可溶化処理により、有機物の好気性生物処理に寄与しない、活性のなくなった汚泥（以下この汚泥を不活性汚泥とする）を曝気槽に戻さないことにより処理水質の悪化を防止することができ、かつ効率よく有機性廃水を好気性生物処理する技術が開示されている（例えば特許文献３）。 Further, after the solubilization, the solid portion is again solubilized by using a solid-liquid separation device, and the solubilization process in the aeration tank is performed. By not returning sludge to inert sludge) to the aeration tank, deterioration of treated water quality can be prevented, and a technique for efficiently treating organic wastewater with an aerobic biological treatment is disclosed (for example, Patent Document 3). ).
しかし、特許文献１のような汚泥の可溶化方法では、完全に溶けない物質が生物反応槽で難分解性物質として蓄積されてくる。この蓄積物は、可溶化した汚泥を生物反応槽に戻す方法において固液分離後の処理水の化学的酸素要求量いわゆるＣＯＤや透視度などの水質を悪化させる原因の１つとなっている。特許文献２では、可溶化処理反応槽を小さくするために、可溶化処理槽の前に濃縮機を入れている。その際脱水しやすくするために、高分子凝集剤などの凝集剤を入れることがあるが、そのような場合には高分子凝集剤自体が有機物であるために、生物処理をするための負荷が高くなることがあった。また、特許文献３の方法は、可溶化処理槽に移送する汚泥の量は、生物処理によって発生する汚泥の２〜２．５倍と多量の汚泥を可溶化処理に送っており、可溶化処理槽の規模が大きくなってしまっている。 However, in the method for solubilizing sludge as in Patent Document 1, substances that are not completely dissolved accumulate as hardly decomposable substances in a biological reaction tank. The accumulated matter is one of the causes of deteriorating the water quality such as the so-called COD and transparency of the treated water after solid-liquid separation in the method of returning the solubilized sludge to the biological reaction tank. In Patent Literature 2, a concentrator is placed in front of the solubilization tank in order to reduce the size of the solubilization reaction tank. At this time, a flocculant such as a polymer flocculant may be added to facilitate dehydration.In such a case, the load for biological treatment is increased because the polymer flocculant itself is an organic substance. It could be high. Further, in the method of Patent Document 3, the amount of sludge transferred to the solubilization treatment tank is 2 to 2.5 times as large as the sludge generated by biological treatment, and is sent to the solubilization treatment. The size of the tank has increased.
また、一般的に溶質を溶媒に溶かした液は、粘度が高くなるため、汚泥を可溶化した際にも、菌などが液にとけるので、液の粘度が上がり、膜での濾過には高粘度のために適さないと思われてきた。
本発明は、上記のような従来技術の問題点を解消し、有機性廃水の生物処理に伴って発生する余剰汚泥の発生量を顕著に減少させることが可能な新規な有機性廃水の処理方法を提供することを目的とする。 The present invention solves the above-mentioned problems of the prior art, and a novel method for treating organic wastewater that can significantly reduce the amount of excess sludge generated due to biological treatment of organic wastewater. The purpose is to provide.
本発明者は、有機性廃水の生物処理に伴って発生する汚泥を可溶化処理槽で可溶化し、可溶化液を固液分離装置により分離し、分離処理液を生物反応槽で生物処理し、濃縮液は、可溶化処理槽内で濃縮される方法により余剰汚泥発生量を顕著に減少することが可能であることを見出し、本発明を完成させた。 The inventor of the present invention solubilized sludge generated in the biological treatment of organic wastewater in a solubilization treatment tank, separated the solubilized liquid by a solid-liquid separator, and biologically treated the separated treatment liquid in a biological reaction tank. The present inventors have found that the amount of surplus sludge can be remarkably reduced by a method of concentrating a concentrated liquid in a solubilization tank, and completed the present invention.
すなわち本発明は、下記のとおりである。
１）有機性廃水を生物反応槽にて生物処理し、発生する余剰汚泥分の１倍以上２倍未満を可溶化処理槽に移送し、該可溶化処理槽中の液の少なくとも一部を固液分離装置により分離処理液と濃縮液に分離し、分離処理液は前記生物反応槽に戻し、濃縮液は該可溶化処理槽に戻すことを特徴とする有機性廃水の処理方法。
２）生物反応槽に戻す分離処理液のＢＯＤ負荷が、有機性廃水のＢＯＤ負荷に対して１０％以下であることを特徴とする１）記載の有機性廃水の処理方法。
３）可溶化処理槽での可溶化方法が中高温の微生物処理であることを特徴とする１）または２）の有機性廃水の処理方法。
４）濃縮液のプロテアーゼ活性が０．２[mUnit/ml]以上であることを特徴とする１）〜３）のいずれかに記載の有機性廃水の処理方法。
５）固液分離が中高温で行われることを特徴とする請求項１）〜４）のいずれかに記載の有機性廃水の処理方法。
６）固液分離装置が、遠心分離装置又は、膜濾過装置であることを特徴とする請求項１）〜５）のいずれかに記載の有機性廃水の処理方法。
７）膜濾過装置の濾過膜が、限外濾過膜であることを特徴とする６）に記載の有機性廃水の処理方法。
８）膜濾過装置の濾過膜が、精密濾過膜であることを特徴とする６）に記載の有機性廃水の処理方法。
９）膜濾過装置が、精密濾過膜と限外濾過膜を直列に組み合わせてなり、前者の透過液が後者の供給液となることを特徴とする６）に記載の有機性廃水の処理方法。
１０）有機性廃水を生物反応槽にて生物処理し、発生する汚泥を可溶化処理槽で中高温の微生物処理により可溶化させるとともに、該可溶化処理槽の液中に浸漬した濾過膜により、濾過と濃縮を行い、膜濾過液を、前記生物反応槽に戻すことを特徴とする有機性廃水の処理方法。
That is, the present invention is as follows.
1) Biological treatment of the organic wastewater in a biological reaction tank, transferring 1 to 2 times the excess sludge generated to the solubilization tank, and solidifying at least a part of the liquid in the solubilization tank. A method for treating organic wastewater, comprising separating a separation treatment liquid and a concentrated liquid by a liquid separation device, returning the separated treatment liquid to the biological reaction tank, and returning the concentrated liquid to the solubilization treatment tank.
2) The method for treating organic wastewater according to 1), wherein the BOD load of the separation treatment liquid returned to the biological reaction tank is 10% or less of the BOD load of the organic wastewater.
3) The method for treating organic wastewater according to 1) or 2), wherein the solubilization method in the solubilization treatment tank is a medium-high temperature microorganism treatment.
4) The method for treating organic wastewater according to any one of 1) to 3), wherein the protease activity of the concentrate is 0.2 [mUnit / ml] or more.
(5) The method for treating organic wastewater according to any one of (1) to (4), wherein the solid-liquid separation is performed at an intermediate temperature.
(6) The method for treating organic wastewater according to any one of (1) to (5), wherein the solid-liquid separation device is a centrifugal separation device or a membrane filtration device.
7) The method for treating organic wastewater according to 6), wherein the filtration membrane of the membrane filtration device is an ultrafiltration membrane.
8) The method for treating organic wastewater according to 6), wherein the filtration membrane of the membrane filtration device is a microfiltration membrane.
9) The method for treating organic wastewater according to 6), wherein the membrane filtration device comprises a series combination of a microfiltration membrane and an ultrafiltration membrane, and the former permeate serves as the latter feed.
10) Organic wastewater is biologically treated in a biological reaction tank, and the generated sludge is solubilized by medium-high temperature microbial treatment in a solubilization tank, and a filtration membrane immersed in the liquid in the solubilization tank is used. A method for treating organic wastewater, comprising performing filtration and concentration, and returning a membrane filtrate to the biological reaction tank.
有機性廃水の生物処理に伴って発生する汚泥を可溶化処理槽で可溶化し、可溶化液を固液分離装置で分離し、分離処理液を生物反応槽で生物処理し、濃縮液は、可溶化処理槽内で濃縮する方法により余剰汚泥発生量を顕著に減少させることが可能である。
また、生物反応槽後の固液分離後の処理水の水質も放流可能な水質を保つことが可能である。
The sludge generated during the biological treatment of organic wastewater is solubilized in a solubilization tank, the solubilized liquid is separated by a solid-liquid separator, and the separated liquid is subjected to biological treatment in a biological reaction tank. The amount of excess sludge generated can be significantly reduced by a method of concentrating in the solubilization tank.
Further, the quality of the treated water after the solid-liquid separation after the biological reaction tank can be maintained at the quality that can be discharged.
以下、本発明について、特にその好ましい形態を中心に、具体的に説明する。
本発明に用いる、生物反応槽は、好気性生物処理あるいは嫌気性生物処理のいずれの方式も適用できる。一般的には、かかる有機性廃水を処理する方法としては、活性汚泥法と呼ばれる好気性生物処理法が、最も一般的に実施されている。
本発明における生物処理とは、下水などの廃水中の汚濁物質を生物学的作用により分解、安定化させる処理のことであり、好気性処理と嫌気性処理に区別される。一般的に有機物は、生物処理により酸素呼吸・硝酸呼吸・発酵過程などで分解されて、ガス化されるか、微生物の体内に取り込まれ、汚泥として除去される。窒素（硝化脱窒法）やりん（生物学的リン除去法）の除去処理もできる。このような生物処理を行なう槽を生物反応槽という。
Hereinafter, the present invention will be specifically described with a particular emphasis on its preferred embodiments.
The biological reaction tank used in the present invention can employ either aerobic biological treatment or anaerobic biological treatment. In general, as a method for treating such organic wastewater, an aerobic biological treatment method called an activated sludge method is most commonly performed.
The biological treatment in the present invention is a treatment for decomposing and stabilizing pollutants in wastewater such as sewage by a biological action, and is classified into an aerobic treatment and an anaerobic treatment. In general, organic substances are decomposed in the process of oxygen respiration, nitrate respiration, fermentation, and the like by biological treatment, and are gasified or taken into microorganisms and removed as sludge. It can also remove nitrogen (nitrification and denitrification) and phosphorus (biological phosphorus removal). A tank for performing such biological treatment is called a biological reaction tank.
可溶化とは、水不溶物であった有機物が微生物による生分解や熱処理による熱分解、或いは、オゾン等による酸化を受け、低分子化等の変化の結果、水にとける様になることである。可溶化処理槽で中高温の微生物処理とは、中高温の温度がかかっている状態で上記の可溶化が微生物による酵素反応で起こっていることを指す。温度として、好ましくは、４０〜７０℃である。
膜濾過装置とは、濾過膜と配管とポンプ等を組み合わせて濾過できるしくみにした装置を指す。ここでいうポンプとは、液を送るポンプや空気を送るエアーポンプも含まれる。
プロテアーゼ活性とは、下記のように測定した。
Solubilization means that water-insoluble organic matter undergoes biodegradation by microorganisms, thermal decomposition by heat treatment, or oxidation by ozone, etc., and becomes soluble in water as a result of changes such as low molecular weight. . The medium-high temperature microbial treatment in the solubilization tank means that the above-described solubilization is caused by an enzymatic reaction by the microorganism in a state where the medium-high temperature is applied. The temperature is preferably 40 to 70 ° C.
The membrane filtration device refers to a device configured to perform filtration by combining a filtration membrane, piping, a pump, and the like. The pump here includes a pump for sending a liquid and an air pump for sending air.
The protease activity was measured as described below.
１）試料の調整
０．１（ｍｏｌ／ｌ）リン酸バッファーの調整は、リン酸水素２ナトリウム（和光純薬）１４．１９６ｇを水に溶かす。これをＡ液とする。リン酸２水素カリウム（和光純薬）１３．０６９ｇを水１Ｌ溶かす。これをＢ液とする。Ａ：Ｂ＝７：３の割合で混合し、ｐＨを確認し、ｐＨ＝７．２からずれていたら、１Ｎ塩酸あるいは、１Ｎ水酸化ナトリウムを使って、調整する。これをリン酸バッファー液とする。
指標となるプロテアーゼは、メーカー：シグマ。商品番号Ｐ５５６８のプロテーゼＫを使用した。このプロテアーゼの活性は、３４４[ＵＮＩＴ／ｍｌ]であった。たんぱく質の基質として、アゾカゼイン（シグマ社：商品名Ａ２７６５）を使用した。アゾカゼインは、１重量％液を使用した。反応停止剤として、トリクロロ酢酸（和光純薬）の１０％溶液を使用した。
1) Preparation of Sample To adjust the 0.1 (mol / l) phosphate buffer, dissolve 14.196 g of disodium hydrogen phosphate (Wako Pure Chemical Industries) in water. This is designated as solution A. 13.069 g of potassium dihydrogen phosphate (Wako Pure Chemical) is dissolved in 1 L of water. This is called liquid B. A: B: Mix at a ratio of 7: 3, check the pH, and if the pH deviates from 7.2, adjust with 1N hydrochloric acid or 1N sodium hydroxide. This is used as a phosphate buffer solution.
Protease used as an indicator is a manufacturer: Sigma. Prosthesis K with product number P5568 was used. The activity of this protease was 344 [UNIT / ml]. Azocasein (Sigma: A2765) was used as a protein substrate. Azocasein used was a 1% by weight solution. As a reaction terminator, a 10% solution of trichloroacetic acid (Wako Pure Chemical Industries, Ltd.) was used.
２）検量線の作成
上記のプロテアーゼＫを１万倍、１０万倍、１００万倍希釈したものを試験管に１ｍｌづつ入れた。希釈には、リン酸バッファーを使用した。各々の試験管に１重量％溶液のアゾカゼインを２ｍｌ入れた。対照として、試験管にリン酸バッファーを１ｍｌと１重量％溶液のアゾカゼインを２ｍｌ入れ、各々撹拌した。これらを６０℃の恒温水槽で１時間加温した。１時間の加温後、恒温水槽から取り出し、反応停止剤を２ｍｌ添加し、反応停止とした。反応停止した液を撹拌した後、４９ｋｍ／ｓ２で１０分間の遠心分離により、上澄み液を採取して、λ（波長）＝３７６ｎｍで吸光度を測定し、アゾカゼインを基質としたプロテアーゼＫの活性の検量線とした。吸光度の測定には、島津製作所のＵＶ−１２００（商品名）を使用した。吸光度のゼロ点調整は、対照の上澄み液で行った。
2) Preparation of calibration curve The above-mentioned protease K was diluted 10,000 times, 100,000 times, and 1,000,000 times, and each 1 ml was put into a test tube. For dilution, a phosphate buffer was used. Each test tube contained 2 ml of a 1% by weight solution of azocasein. As a control, 1 ml of a phosphate buffer and 2 ml of a 1% by weight solution of azocasein were placed in a test tube, and each was stirred. These were heated in a constant temperature water bath at 60 ° C. for 1 hour. After heating for 1 hour, the reaction mixture was taken out of the thermostatic water bath, and 2 ml of a reaction terminator was added to stop the reaction. After the reaction-stopped solution was stirred, the supernatant was collected by centrifugation at 49 km / s 2 for 10 minutes, the absorbance was measured at λ (wavelength) = 376 nm, and the activity of protease K using azocasein as a substrate was measured. The calibration curve was used. For the measurement of absorbance, UV-1200 (trade name) manufactured by Shimadzu Corporation was used. Zero adjustment of the absorbance was performed with the control supernatant.
３）サンプルの測定
対象となる液を固液分離するため、９８ｋｍ／ｓ２の１０分間の遠心分離にて、上澄みをとった。この上澄み液を試験管に１ｍｌ採取し、各々の試験管に１重量％溶液のアゾカゼインを２ｍｌ入れた。対照として、試験管にリン酸バッファーを１ｍｌとアゾカゼインを２ｍｌ入れた。これらを６０℃の恒温水槽で１時間加温した。１時間の加温後、恒温水槽から取り出し、反応停止剤を２ｍｌ添加し、反応停止とした。反応停止した液を撹拌した後、４９ｋｍ／ｓ２で１０分間の遠心分離により、上澄み液を採取して、λ＝３７６ｎｍで吸光度を測定し、得られた吸光度から上記検量線に照らし合わせ、アゾカゼインを基質としたプロテアーゼＫの活性とした。吸光度のゼロ点調整は、対照の上澄み液で行った。
以上は、Bioresource Technology (2002)157-164 Enhancement of proteolytic enzyme activity excreted from Bacillus stearothermophilus for a thermophilic aerobic digestion processsを参考にした。
3) Measurement of sample In order to separate the liquid to be subjected to solid-liquid separation, the supernatant was collected by centrifugation at 98 km / s 2 for 10 minutes. 1 ml of the supernatant was collected in a test tube, and each test tube was charged with 2 ml of a 1% by weight solution of azocasein. As a control, 1 ml of a phosphate buffer and 2 ml of azocasein were placed in a test tube. These were heated in a constant temperature water bath at 60 ° C. for 1 hour. After heating for 1 hour, the reaction mixture was taken out of the thermostatic water bath, and 2 ml of a reaction terminator was added to stop the reaction. After stirring the liquid after stopping the reaction, the supernatant was collected by centrifugation at 49 km / s 2 for 10 minutes, the absorbance was measured at λ = 376 nm, and the obtained absorbance was compared with the above calibration curve to obtain azocasein. Was used as the activity of protease K. Zero adjustment of the absorbance was performed with the control supernatant.
The above refers to Bioresource Technology (2002) 157-164 Enhancement of proteolytic enzyme activity excreted from Bacillus stearothermophilus for a thermophilic aerobic digestion process.
本発明を、図１で説明する。有機性廃水貯留槽１から生物反応槽３に導入された下水などの有機性廃水が、生物反応槽３において好気性条件にて、微生物による酸化分解反応である生物酸化によって、二酸化炭素もしくは水などの無機物に分解される方法である。そして、生物反応槽３にて処理された廃水は、固液分離槽５にて処理水３０１と汚泥３０２に固液分離され、汚泥３０２の一部は微生物源として生物反応槽３に返送される。
生物反応槽に返送される汚泥の一部を可溶化処理槽８に送る。この可溶化反応、としては、任意の方法を採用することが できる。例えば、中高温での微生物による可溶化処理、オゾン処理による可溶化処理、酸処理による可溶化処理、アルカリ処理による可溶化処理、加熱処理による可溶化処理、高圧パルス放電処理、ボールミル、コロイドミル等のミルによる磨砕処理、これらを組み合わせた可溶化処理等を採用することができる。これらの処理は公知の処理装置を可溶化処理槽として用いることができる。
The present invention is illustrated in FIG. Organic wastewater such as sewage introduced from the organic wastewater storage tank 1 to the biological reaction tank 3 is subjected to biooxidation, which is an oxidative decomposition reaction of microorganisms, under aerobic conditions in the biological reaction tank 3, such as carbon dioxide or water. It is a method that is decomposed into inorganic substances. The wastewater treated in the biological reaction tank 3 is separated into treated water 301 and sludge 302 in the solid-liquid separation tank 5, and a part of the sludge 302 is returned to the biological reaction tank 3 as a microorganism source. .
A part of the sludge returned to the biological reaction tank is sent to the solubilization tank 8. Any method can be adopted as the solubilization reaction. For example, solubilization treatment by microorganisms at medium and high temperatures, solubilization treatment by ozone treatment, solubilization treatment by acid treatment, solubilization treatment by alkali treatment, solubilization treatment by heat treatment, high-pressure pulse discharge treatment, ball mill, colloid mill, etc. , A solubilization treatment or the like obtained by combining them. For these treatments, a known treatment device can be used as a solubilization treatment tank.
本発明で使用する固液分離装置は特に制限されず、膜濾過装置、遠心分離装置、デカンター、濾過装置などの任意の 固液分離装置を用いることができる。
本発明では、可溶化処理と固液分離装置の組み合わせることによって、可溶化処理槽に送る液は、発生する余剰汚泥分の１倍以上２倍未満が好ましい。さらに好ましくは、１倍以上１．７倍以下である。この倍率は、可溶化処理方法や固液分離方法により、倍率を変更する。本発明では、固液分離することにより、生物処理槽に返送される液のＢＯＤ負荷が低くなることと可溶化した際に発生する不活性汚泥が生物処理槽に移送されなくなるので、可溶化処理槽に送る液が少なくて済む。この中で好ましい形態は、生物処理槽には、好気性生物処理を用い、固液分離し、固液分離した汚泥の可溶化反応には、中高温での微生物処理を用い、固液分離法には、膜濾過法を用いることが、有機性排液の処理に際し、低コストで汚泥を減容化して系外へ排出する汚泥量を減少させ、しかも処理水質の悪化を防止し、かつ効率よく有機性廃水を処理することができる点で好ましい。本発明の中高温での微生物処理は、４０〜７０℃が好ましい。この方法は、中高温の嫌気性処理、好気性処理のいずれでも適用できる。好気性にするためには、該可溶化処理槽の中に空気を入れ、可溶化処理槽の液を曝気できれば、何でも良い。例えば、ブロアーで可溶化処理槽中に空気を管で導入しても良い。また、エアレータを可溶化処理槽内に入れて、曝気しても良い。膜濾過法の場合、濾過膜は、中空糸膜状、平膜状、など何でも良いが、中空糸膜状のものが目詰まり物質の洗浄を逆洗により行ないやすく好ましい。膜の材質は、ポリエチレン系、ポリアクリロニトリル系、ポリスルホン系、ポリフッ化ビニリデン系、酢酸セルロース系など様々なものが適用できるが、温度や液により膜の材質を使い分けることが効果的である。耐熱性、薬品洗浄の耐性からポリスルホン系およびポリフッ化ビニリデン系が特に好ましい。
The solid-liquid separator used in the present invention is not particularly limited, and any solid-liquid separator such as a membrane filter, a centrifuge, a decanter, and a filter can be used.
In the present invention, by combining the solubilization treatment and the solid-liquid separation device, it is preferable that the amount of the liquid to be sent to the solubilization treatment tank is not less than one time and less than twice the amount of excess sludge generated. More preferably, it is 1 time or more and 1.7 times or less. The magnification is changed by a solubilization method or a solid-liquid separation method. In the present invention, the solid-liquid separation reduces the BOD load of the liquid returned to the biological treatment tank, and the inert sludge generated when solubilized is not transferred to the biological treatment tank. Less liquid needs to be sent to the tank. Among these, a preferred form is that the biological treatment tank uses an aerobic biological treatment, is subjected to solid-liquid separation, and the solubilization reaction of the solid-liquid separated sludge uses a microbial treatment at a medium to high temperature. In order to reduce the volume of sludge discharged at low cost and reduce the amount of sludge discharged out of the system at the time of treating organic wastewater, it is also possible to use a membrane filtration method to This is preferable because organic wastewater can be treated well. The microorganism treatment at a medium to high temperature of the present invention is preferably at 40 to 70 ° C. This method can be applied to both anaerobic and aerobic treatments at medium and high temperatures. In order to achieve aerobicity, anything may be used as long as air can be introduced into the solubilization tank and the liquid in the solubilization tank can be aerated. For example, air may be introduced into the solubilization tank with a blower through a tube. Further, an aerator may be placed in the solubilization tank and aerated. In the case of the membrane filtration method, the filtration membrane may be a hollow fiber membrane, a flat membrane, or the like, but a hollow fiber membrane is preferred because the clogging substance can be washed by backwashing. As the material of the film, various materials such as polyethylene, polyacrylonitrile, polysulfone, polyvinylidene fluoride, and cellulose acetate can be used. It is effective to use different materials for the film depending on the temperature and liquid. Polysulfone and polyvinylidene fluoride are particularly preferred from the viewpoint of heat resistance and resistance to chemical cleaning.
濾過膜は、膜同士を束ねたり、のり巻き状に巻いたり、端部を接着材によりシールして膜モジュールという濾過膜の一次側と２次側とを隔離した形にして使用する。膜モジュールの形は、スパイラル型、中空糸膜型、管状型及びプレート型のいずれでも良い。先に述べた理由で中空糸膜型がより好ましい。本発明で使用する膜濾過装置とは、濾過膜の１次側入り口配管と出口配管と２次側の出口配管を備え、1次側と２次側に差圧を与える手段を持つ装置をいう。
例えば、本実施例での膜濾過装置は、ポリスルホン系の膜材質を使用した中空糸膜型モジュールを使用し、中空糸膜モジュールの1次側入り口配管と出口配管と２次側出口配管を備え、１次側の入り口配管には、膜モジュールに液を送るためのポンプと1次側出口配管には、バルブを備え、1次側と２次側に差圧を与える手段を持つ装置とした。
The filtration membrane is used in a form in which the primary side and the secondary side of a filtration membrane, which is a membrane module, are separated by bundling the membranes, winding the membranes in a roll, or sealing the ends with an adhesive. The shape of the membrane module may be any of a spiral type, a hollow fiber type, a tubular type and a plate type. The hollow fiber membrane type is more preferable for the reasons described above. The membrane filtration device used in the present invention refers to a device provided with a primary side inlet pipe, an outlet pipe, and a secondary side outlet pipe of a filtration membrane, and having a means for giving a differential pressure between the primary side and the secondary side. .
For example, the membrane filtration device in the present embodiment uses a hollow fiber membrane type module using a polysulfone-based membrane material, and is provided with a primary inlet pipe, an outlet pipe, and a secondary outlet pipe of the hollow fiber membrane module. 1. A pump for sending liquid to the membrane module at the inlet pipe on the primary side, and a valve at the outlet pipe on the primary side, and a device having means for applying a differential pressure between the primary side and the secondary side. .
本発明の処理方法では、濾過速度を高く保つために、逆洗を適用したほうが良い。逆洗とは、濾過速度の低下を極力抑制するための膜の洗浄方法であり、この方法は、膜の濾過液側に濾過時とは逆の濾過圧をかけて、膜濾過液側から膜濃縮液側に液を流して、膜濃縮液側の膜表面に付着した目詰まり物質を除く方法である。さらに、逆洗の時に膜に対する目詰まり物を洗浄する薬剤を投入しても良い。膜濾過装置には、逆洗可能な設備、例えば膜モジュールの濾過液側から圧力がかけられるように逆洗ポンプと逆洗時薬剤を添加できる装置を付加した方が好ましい。また、濾過をせずに、１次側に可溶化処理槽内の液を流すことやろ過しながらも通常よりも早い線速で液を循環することをフラッシングという。 In the treatment method of the present invention, it is better to apply backwashing in order to keep the filtration rate high. Backwashing is a method of cleaning a membrane in order to minimize a decrease in filtration rate. This method applies a reverse filtration pressure to the filtrate side of the membrane during filtration, so that the membrane is filtered from the membrane filtrate side. In this method, a clogging substance attached to the membrane surface on the membrane concentrate side is removed by flowing the solution to the concentrate side. Further, at the time of back washing, an agent for washing clogs on the membrane may be added. It is preferable to add a device capable of backwashing, for example, a backwash pump and a device capable of adding a backwashing agent so that pressure is applied from the filtrate side of the membrane module to the membrane filtration device. Also, flushing refers to flowing the liquid in the solubilization tank to the primary side without filtering or circulating the liquid at a linear velocity faster than usual while filtering.
また、フラッシングの循環方向は、ろ過している時と逆でも良い。逆方向にフラッシングする方法を逆フラッシングとする。このフラッシングや逆フラッシングを濾過や逆洗の間に行なうとさらに良く、濾過速度を保つことができる。膜濾過装置での膜濾過液は、生物反応槽に戻し、膜濃縮液は、可溶化処理槽に戻す。膜濃縮液には、膜を透過できない好熱菌や酵素が存在し、可溶化処理槽で再利用される。 Further, the circulation direction of the flushing may be opposite to that during the filtration. The method of flushing in the reverse direction is referred to as reverse flushing. This flushing or backflushing is more preferably performed during filtration or backwashing, and the filtration speed can be maintained. The membrane filtrate in the membrane filtration device is returned to the biological reaction tank, and the membrane concentrate is returned to the solubilization tank. The membrane concentrate contains thermophilic bacteria and enzymes that cannot pass through the membrane, and is reused in the solubilization tank.
本発明では、図３のように、生物反応槽に返送される液の一部を中高温の微生物処理による可溶化反応可能な装置に送るところまでは、図１と同様であるが、図３のように濾過液側から吸引ポンプ１５などで濾過液を吸引することが好ましい。膜濾過液を得て、得た膜濾過液は、生物反応槽に戻す。濾過膜を透過しない濃縮液は、可溶化処理槽内に返送される。濾過膜の孔径は、限外濾過膜の場合は、分画分子量５００〜１００万程度の孔径ものを指し、精密濾過膜の場合０．０１マイクロメートルから１０マイクロメートル程度の平均膜孔径のものを指す。分画分子量とは、膜が特定の阻止率で阻止できる最小の分子量を意味する。
本発明では特定の阻止率として９０％を用いた。分画分子量を測定する際の標準物質としては、ポリエチレングリコールやデキストラン、球状タンパクなどが用いられる。
In the present invention, as shown in FIG. 3, up to a point where a part of the liquid returned to the biological reaction tank is sent to a device capable of solubilization reaction by microbial treatment at medium and high temperatures, the same as FIG. It is preferable to suck the filtrate from the filtrate side with the suction pump 15 or the like. A membrane filtrate is obtained, and the obtained membrane filtrate is returned to the biological reactor. The concentrate that does not pass through the filtration membrane is returned to the solubilization tank. The pore size of the filtration membrane refers to a pore size having a molecular weight cut off of about 500 to 1,000,000 in the case of an ultrafiltration membrane, and an average membrane pore size of about 0.01 to 10 micrometers in the case of a microfiltration membrane. Point. By fractional molecular weight is meant the minimum molecular weight that the membrane can block at a particular rejection.
In the present invention, 90% is used as a specific rejection. As a standard substance for measuring the molecular weight cut off, polyethylene glycol, dextran, globular protein and the like are used.
本発明において、限外濾過膜は、可溶化処理槽内の酵素の濃縮に有効に使用される。一般的に酵素は、数千から数十万の分子量である。従って、限外濾過膜は酵素を阻止できる分画分子量１，０００〜１００，０００程度である事が好ましい。さらに好ましくは、分画分子量５，０００〜５０，０００程度である。さらに好ましくは、６，０００〜１０，０００である。あまり小さいと、濾過速度が小さくなる傾向があり、大きすぎても、酵素が抜けやすくなる。酵素が濃縮できると可溶化処理槽において酵素による可溶化反応が進む効果がある。 In the present invention, the ultrafiltration membrane is effectively used for concentrating the enzyme in the solubilization tank. Generally, enzymes have molecular weights of thousands to hundreds of thousands. Therefore, it is preferable that the ultrafiltration membrane has a molecular weight cut-off of about 1,000 to 100,000 that can inhibit the enzyme. More preferably, the molecular weight cut off is about 5,000 to 50,000. More preferably, it is 6,000 to 10,000. If it is too small, the filtration rate tends to be low, and if it is too large, the enzyme tends to escape. When the enzyme can be concentrated, the solubilization reaction by the enzyme proceeds in the solubilization tank.
精密濾過膜は、菌体を濃縮できる。一般に菌体の大きさは、０．２マイクロメートルから数マイクロメートルであるので、精密濾過膜の平均膜孔径は、０．１マイクロメートルから１マイクロメートルが好ましい。あまり小さいと、濾過速度が小さくなる傾向があり、大きすぎても、菌体が抜けやすい。菌体を可溶化処理槽において濃縮できると菌体による可溶化が進む効果がある。精密濾過膜の平均膜孔径とは、ＡＳＴＭ Ｆ３１６−８６の「泡立ち点試験及び平均流量細孔試験による薄膜フィルタ細孔径の特定標準試験方法による測定」で平均流量の細孔の圧力から求めた細孔径のことを指す。 The microfiltration membrane can concentrate cells. In general, the size of the microbial cells is from 0.2 micrometer to several micrometers, so the average membrane pore size of the microfiltration membrane is preferably from 0.1 micrometer to 1 micrometer. If it is too small, the filtration rate tends to be low, and if it is too large, the cells are easily removed. When the cells can be concentrated in the solubilization treatment tank, the solubilization by the cells is effective. The average membrane pore diameter of the microfiltration membrane is a fine pore diameter obtained from the pore pressure at the average flow rate in ASTM F316-86 “Measurement by a specific standard test method for the thin film filter pore diameter by the bubble point test and the average flow pore test”. It refers to the pore size.
また、中高温の微生物処理の場合、固液分離は、中高温のまま行なうことが最も好ましい。中高温のまま固液分離すると、固液分離した濃縮液の無機化合物や汚泥を不活性汚泥が温度を高くすることにより、溶解し、濾過液となって、生物処理槽に移行する。また、固液分離の濃縮液は、可溶化処理槽に戻るので、再び、温度がかかるので、可溶化処理槽の温度に近ければ、再び可溶化させる熱量を節約できる。 Further, in the case of a microorganism treatment at an intermediate temperature, it is most preferable to perform the solid-liquid separation at an intermediate temperature. When the solid-liquid separation is performed at a high temperature, the inert sludge dissolves the inorganic compounds and sludge of the concentrated liquid that has been solid-liquid separated by increasing the temperature, and turns into a filtrate to be transferred to the biological treatment tank. In addition, since the concentrated liquid for solid-liquid separation returns to the solubilization tank and is heated again, if the temperature is close to the temperature of the solubilization tank, the amount of heat to be solubilized again can be saved.
本発明では、図５に示すように、膜濾過装置として１段目に精密濾過膜１３を設置し、２段目に限外濾過膜１４を設置することが好ましい。それぞれから発生する膜濃縮液はまとめて膜濾過装置の膜濃縮液として、可溶化処理槽に戻すようにした。２段目の限外濾過の膜濾過液は、膜濾過装置の膜濾過液として生物反応槽にもどす。 In the present invention, as shown in FIG. 5, it is preferable to install a microfiltration membrane 13 at the first stage and an ultrafiltration membrane 14 at the second stage as a membrane filtration device. The membrane concentrates generated from each of them were collectively returned to the solubilization tank as a membrane concentrate of the membrane filtration device. The membrane filtrate of the second stage ultrafiltration is returned to the biological reaction tank as a membrane filtrate of the membrane filtration device.
以下に、本発明の実施例を記載する。
〔実施例１〕
実施例１で使用した装置概略図を図１に示す。図１において、３が生物反応槽、５が固液分離槽、６が返送汚泥ラインである。６の返送汚泥ラインから分岐して送液ライン７を経て、可溶化処理槽８に液を送る。８１がばっ気装置からのエアー配管である。１０が膜濾過装置である。本実施例において、生物反応槽３に流入する有機性廃水は、ＢＯＤ濃度２００ｍｇ／Ｌであった。該有機性廃水は、肉エキス：ペプトン＝１：１（重量比）とし、ＢＯＤ濃度：窒素濃度：リン濃度＝１００：５：１になるように更に無機塩類を添加したモデル液を使用した。ＢＯＤ濃度とは、１リットル（Ｌ）の水中の有機物が微生物の働きによって分解されるときに消費される酸素の量で、河川の有機汚濁を測る代表的な指標であり、日本工業規格、工場排水試験方法Ｋ０１０２．２１によって測定した。有機性廃水は流入量４０Ｌ／ｄａｙで生物反応槽３に供給した。生物反応槽の容量は１０Ｌであった。生物反応槽３から流出した液は、固液分離槽５に送られる。固液分離槽としてはここでは沈降分離法による固液分離槽を用い、上澄み液と汚泥に分けた。固液分離槽５で沈降分離した汚泥は、一部返送汚泥として生物反応槽３に返送される。
Hereinafter, examples of the present invention will be described.
[Example 1]
FIG. 1 shows a schematic diagram of the apparatus used in Example 1. In FIG. 1, 3 is a biological reaction tank, 5 is a solid-liquid separation tank, and 6 is a return sludge line. The liquid is sent from the return sludge line 6 to the solubilization tank 8 via the liquid sending line 7. 81 is an air pipe from the aeration device. 10 is a membrane filtration device. In this example, the organic wastewater flowing into the biological reaction tank 3 had a BOD concentration of 200 mg / L. The organic wastewater used was a model liquid in which meat extract: peptone = 1: 1 (weight ratio) and inorganic salts were further added so that BOD concentration: nitrogen concentration: phosphorus concentration = 100: 5: 1. The BOD concentration is the amount of oxygen consumed when one liter (L) of organic matter in water is decomposed by the action of microorganisms, and is a representative index for measuring organic pollution in rivers. It measured by the drainage test method K0102.21. The organic wastewater was supplied to the biological reaction tank 3 at an inflow rate of 40 L / day. The volume of the biological reactor was 10 L. The liquid flowing out of the biological reaction tank 3 is sent to the solid-liquid separation tank 5. Here, a solid-liquid separation tank by a sedimentation method was used as a solid-liquid separation tank, and the liquid was separated into a supernatant and sludge. The sludge settled and separated in the solid-liquid separation tank 5 is partially returned to the biological reaction tank 3 as returned sludge.
また、一部の汚泥は、７の送液ラインを通り、浮遊物質（ＳＳ）１重量％で０．５Ｌ／ｄａｙの流量で可溶化処理槽８に送られる。可溶化反応槽は、１．０Ｌであった。可溶化処理槽８には、ばっ気装置からのエアー配管８１で０．０５Ｌ／分のエアーを送り、６０℃の温度が保てるように、保温措置のために可溶化処理槽８のジャケットに温水をいれておいた。可溶化処理槽８を通った液は、送液ライン９の経路上にポンプ（図示せず）を設置し、膜濾過装置１０に送った。固液分離槽５で分離された汚泥はポンプで適宜可溶化処理槽８に送られた。膜濾過装置１０での膜濃縮液は、膜濾過装置濃縮液ライン１１を通り、可溶化処理槽８に送る。膜濾過液は、膜濾過液ライン１２をとおり、生物反応槽３に送液した。膜濾過装置の連続運転条件は、膜濾過液量は、０．５Ｌ／ｄａｙであった。膜濃縮液量３Ｌ／ｈｒで可溶化処理槽８に送った。膜濾過装置に使用した濾過膜モジュールは、ポリスルホン製の中空糸型限外濾過膜である旭化成（株）製、ＳＬＰ−００５３（商品名、膜面積０．０２ｍ２）を使用した。分画分子量は１０，０００である。この状態で、１５日間の連続運転を行った。このとき、固液分離後の膜濾過液のＢＯＤは、５０[ｍｇ／ｌ]であり、ＢＯＤ負荷の増分は、流入水のＢＯＤ負荷が８ｇ／ｄａｙに対して、０．０２５ｇ／ｄａｙであったので、ＢＯＤ負荷の増分は、０．３％であった。また、膜濾過液のＳＳは、０ｍｇ／Ｌであった。そのために、可溶化処理槽に移送する液量は、余剰汚泥量の１倍であった。結果は、表１のとおりである。 Further, a part of the sludge is sent to the solubilization tank 8 at a flow rate of 0.5 L / day with 1% by weight of suspended solids (SS) through the liquid sending line 7. The solubilization reactor was 1.0 L. Air is supplied to the solubilization tank 8 through the air pipe 81 from the aeration apparatus at a rate of 0.05 L / min, and hot water is applied to the jacket of the solubilization tank 8 for heat retention so that the temperature of 60 ° C. can be maintained. I put in. The liquid that passed through the solubilization tank 8 was sent to the membrane filtration device 10 by installing a pump (not shown) on the path of the liquid sending line 9. The sludge separated in the solid-liquid separation tank 5 was appropriately sent to a solubilization tank 8 by a pump. The membrane concentrate in the membrane filtration device 10 is sent to the solubilization tank 8 through the membrane filtration device concentrate line 11. The membrane filtrate was sent to the biological reaction tank 3 through the membrane filtrate line 12. Regarding the continuous operation conditions of the membrane filtration device, the amount of the membrane filtrate was 0.5 L / day. The solution was sent to the solubilization tank 8 at a membrane concentration of 3 L / hr. As a filtration membrane module used for the membrane filtration device, SLP-0053 (trade name, membrane area 0.02 m 2 ) manufactured by Asahi Kasei Corporation, which is a hollow fiber type ultrafiltration membrane made of polysulfone, was used. The molecular weight cut off is 10,000. In this state, continuous operation was performed for 15 days. At this time, the BOD of the membrane filtrate after the solid-liquid separation was 50 [mg / l], and the increase of the BOD load was 0.025 g / day with respect to the BOD load of influent water of 8 g / day. Therefore, the increase in BOD load was 0.3%. The SS of the membrane filtrate was 0 mg / L. Therefore, the amount of liquid transferred to the solubilization tank was one time the amount of excess sludge. The results are as shown in Table 1.
表１は、実験開始日を１日目として、１０日目以降を定常状態として、１０〜１５日目の平均した各値を記載した。
定常状態での可溶化処理槽８に入る液のＳＳは、１０，０００ｍｇ／Ｌであったが膜濾過液のＳＳは、０ｍｇ／Ｌであった。固液分離後の処理水の透視度は、３０度。
固液分離後の処理水の化学的酸素要求量ＣＯＤは、８ｍｇ／Ｌであった。可溶化反応槽のプロテアーゼ活性を確認したところ、０．３ｍＵＮＩＴ／ｍｌであった。また、可溶化処理槽内の強熱残留物を測定したら、５日目は、１．８［ｇ／Ｌ］１０日目は、１．７[ｇ／Ｌ]１５日目は、１．８[ｇ／Ｌ]であった。
Table 1 describes the average values on the 10th to 15th days, with the experiment start date as the first day, the 10th day and after as the steady state.
The SS of the liquid entering the solubilization tank 8 in the steady state was 10,000 mg / L, but the SS of the membrane filtrate was 0 mg / L. The transparency of the treated water after solid-liquid separation is 30 degrees.
The chemical oxygen demand COD of the treated water after the solid-liquid separation was 8 mg / L. When the protease activity of the solubilization reaction tank was confirmed, it was 0.3 mUNIT / ml. Further, when the ignition residue in the solubilization tank was measured, 1.8 [g / L] on the 5th day, 1.7 [g / L] on the 10th day, 1.8 [g / L] on the 15th day [g / L].
浮遊物質（ＳＳ）は、日本工業規格、工場排水試験方法Ｋ１０２．１４．１により測定した。
ＣＯＤは、日本工業規格、工場排水試験方法Ｋ０１０２．１４．１により測定した。
ＢＯＤは日本工業規格、工場排水試験方法Ｋ０１０２．１７により測定した。
透視度は、日本工業規格、工場排水試験方法Ｋ０１０２．９により測定した。
強熱残留物は、日本工業規格、工場排水試験方法Ｋ１０２．１４．４により測定した。
The suspended solids (SS) were measured according to Japanese Industrial Standards, Factory Wastewater Test Method K102.14.1.
COD was measured according to Japanese Industrial Standards, Factory Drainage Test Method K0102.14.1.1.
BOD was measured according to Japanese Industrial Standards, Factory Wastewater Test Method K0102.17.
The degree of transparency was measured according to Japanese Industrial Standards, Factory Drainage Test Method K0102.9.
Ignition residue was measured according to Japanese Industrial Standards, Factory Wastewater Test Method K102.14.4.
〔比較例１〕
比較例１で使用した装置概略図を図２に示す。図２において、３が生物反応槽、５が固液分離槽、６が返送汚泥ラインであり、一般的な生物処理装置である。
生物反応槽３に流入する有機性廃水は、ＢＯＤ濃度２００ｍｇ／Ｌ。有機性廃水は、実施例１と同じ組成のものを使用した。有機性廃水は、４０Ｌ／ｄａｙで生物反応槽に供給した。生物反応槽３の容量は１０Ｌであった。生物反応槽３から流出した液は、固液分離槽５に送られる。固液分離槽５で沈降分離した汚泥は、一部返送汚泥として、生物反応槽３に返送される。
その連続運転のデータとして表１の結果を得た。固液分離後の処理水の水質は、表１のように透視度は、３０度、ＣＯＤは、６ｍｇ／Ｌと良好なものの、余剰汚泥は、乾燥重量で、１０〜１５日目の平均で４．８ｇ／ｄａｙ発生した。
〔比較例２〕
使用した装置概略図を図４に示す。図４において、３が生物反応槽、５が固液分離槽、６が返送汚泥ラインであり、一般的な生物処理装置である。６の返送汚泥ラインから分岐して、可溶化処理槽８に液を送る。８１がばっ気装置からのエアー配管である。本比較例において、生物反応槽３に流入する有機性廃水は、ＢＯＤ濃度２００ｍｇ／Ｌ。有機性廃水は、実施例１と同じ組成のものを使用し生物反応槽３へは４０Ｌ／ｄａｙの流入量であった。生物反応槽３の容量は２０Ｌ。生物反応槽３から流出した液は、固液分離槽５に送られる。固液分離槽５で沈降分離した汚泥は、一部返送汚泥として、生物反応槽３に返送される。また、一部の汚泥は、７の送液ラインを通り、ＳＳ濃度１重量％で１．５Ｌ／ｄａｙの流量で可溶化処理槽８に送られる。可溶化処理槽の大きさは、３．０Ｌであった。可溶化処理槽８には、ばっ気装置からのエアー配管８１で０．０５リットル／分のエアーを送り、６０℃の温度が保てるように、保温措置のためにジャケットに温水をいれておいた。可溶化処理槽８を通った液は、可溶化液返送ライン２０で生物反応槽３に戻した。
[Comparative Example 1]
FIG. 2 shows a schematic diagram of the apparatus used in Comparative Example 1. In FIG. 2, 3 is a biological reaction tank, 5 is a solid-liquid separation tank, and 6 is a return sludge line, which is a general biological treatment apparatus.
The organic wastewater flowing into the biological reaction tank 3 has a BOD concentration of 200 mg / L. Organic wastewater having the same composition as in Example 1 was used. Organic wastewater was supplied to the biological reactor at 40 L / day. The volume of the biological reaction tank 3 was 10 L. The liquid flowing out of the biological reaction tank 3 is sent to the solid-liquid separation tank 5. The sludge settled and separated in the solid-liquid separation tank 5 is returned to the biological reaction tank 3 as partially returned sludge.
Table 1 shows the results of the continuous operation. As shown in Table 1, the quality of the treated water after solid-liquid separation is as good as 30 ° in transparency and 6 mg / L in COD, but the excess sludge is dry weight and averaged from 10 to 15 days. 4.8 g / day was generated.
[Comparative Example 2]
FIG. 4 shows a schematic diagram of the apparatus used. In FIG. 4, 3 is a biological reaction tank, 5 is a solid-liquid separation tank, and 6 is a return sludge line, which is a general biological treatment apparatus. The liquid is branched from the return sludge line 6 and sent to the solubilization tank 8. 81 is an air pipe from the aeration device. In this comparative example, the organic wastewater flowing into the biological reaction tank 3 has a BOD concentration of 200 mg / L. Organic wastewater having the same composition as that of Example 1 was used, and the flow rate into the biological reaction tank 3 was 40 L / day. The capacity of the biological reaction tank 3 is 20 L. The liquid flowing out of the biological reaction tank 3 is sent to the solid-liquid separation tank 5. The sludge settled and separated in the solid-liquid separation tank 5 is returned to the biological reaction tank 3 as partially returned sludge. Further, a part of the sludge is sent to the solubilization tank 8 at a SS concentration of 1% by weight and a flow rate of 1.5 L / day through the liquid sending line 7. The size of the solubilization tank was 3.0 L. Air was supplied to the solubilization tank 8 through the air pipe 81 from the aeration apparatus at a rate of 0.05 liter / min, and warm water was placed in the jacket to keep the temperature at 60 ° C. . The liquid that passed through the solubilization treatment tank 8 was returned to the biological reaction tank 3 via the solubilization liquid return line 20.
その連続運転のデータとして表１の結果を得た。固液分離後の処理水の水質は、表１のように透視度は１５度、化学的酸素要求量であるＣＯＤは、２１ｍｇ／Ｌ。余剰汚泥は、乾燥重量で、０ｇ／ｄａｙであった。このとき、生物処理槽に戻した液のＢＯＤは、１１００[ｍｇ／ｌ]であり、ＢＯＤ負荷の増分は、流入水のＢＯＤ負荷が８ｇ／ｄａｙに対して、１．６５ｇ／ｄａｙであったので、ＢＯＤ負荷の増分は、２０．６％であった。また、生物反応槽に戻すＳＳは、４．３ｇ／Ｌ、１．５Ｌ／ｄａｙで移送される。そのために、可溶化処理槽に移送する液量は、余剰汚泥量の約３倍必要になった。また、可溶化反応槽のプロテアーゼ活性を確認したところ、０．１［ｍＵＮＩＴ／ｍｌ］であった。
比較例１では、余剰汚泥が発生し、比較例２では、固液分離後の処理水のＣＯＤが多く残留し、可溶化処理槽の大きさが大きいが、実施例１では、余剰汚泥は、０ｇ／Ｌ、ＣＯＤは、８ｍｇ／Ｌと可溶化反応処理装置と膜濾過装置を入れて、余剰汚泥の削減、固液分離後の処理水水質の維持になっている。
Table 1 shows the results of the continuous operation. As shown in Table 1, the water quality of the treated water after the solid-liquid separation is 15 degrees, and the COD, which is the chemical oxygen demand, is 21 mg / L. Excess sludge was 0 g / day in dry weight. At this time, the BOD of the liquid returned to the biological treatment tank was 1100 [mg / l], and the increase of the BOD load was 1.65 g / day, while the BOD load of the inflow water was 8 g / day. Therefore, the increase in BOD load was 20.6%. The SS returned to the biological reaction tank is transferred at 4.3 g / L and 1.5 L / day. Therefore, the amount of liquid to be transferred to the solubilization tank was required to be about three times the amount of excess sludge. When the protease activity of the solubilization reaction tank was confirmed, it was 0.1 [mUNIT / ml].
In Comparative Example 1, excess sludge is generated, and in Comparative Example 2, a large amount of COD of the treated water after solid-liquid separation remains and the size of the solubilization treatment tank is large. 0 g / L, COD is 8 mg / L, and a solubilization reaction treatment device and a membrane filtration device are installed to reduce excess sludge and maintain the quality of treated water after solid-liquid separation.
本発明は、下水処理場、屎尿処理場などの下水処理プロセス、食品工場、化学工場などの製造プロセスから排出される有機性汚泥を含有する有機性廃水の処理に好適である。 INDUSTRIAL APPLICABILITY The present invention is suitable for treating organic wastewater containing organic sludge discharged from a sewage treatment process such as a sewage treatment plant, a human waste treatment plant, or a manufacturing process such as a food factory or a chemical factory.
１ 有機性廃水貯留槽
２ 廃水送液ライン
３ 生物反応槽
４ 送液ライン
５ 固液分離槽
６ 返送汚泥ライン
７ 送液ライン
８ 可溶化処理槽
９ 送液ライン
１０ 膜濾過装置
１１ 膜濾過装置濃縮液ライン
１２ 膜濾過液ライン
１３ 精密濾過膜
１４ 限外濾過膜
１５ 吸引ポンプ
２０ 可溶化液返送ライン
３１ エアー配管
８１ エアー配管
１１１ 限外濾過膜濃縮液ライン
１２１ 精密濾過膜濾過液ライン
３０１ 処理液
３０２ 汚泥
３０３ 余剰汚泥
REFERENCE SIGNS LIST 1 Organic wastewater storage tank 2 Wastewater liquid feed line 3 Biological reaction tank 4 Liquid feed line 5 Solid-liquid separation tank 6 Return sludge line 7 Liquid feed line 8 Solubilization treatment tank 9 Liquid feed line 10 Membrane filtration device 11 Membrane filtration device concentration Liquid line 12 Membrane filtrate line 13 Microfiltration membrane 14 Ultrafiltration membrane 15 Suction pump 20 Solubilized liquid return line 31 Air pipe 81 Air pipe 111 Ultrafiltration membrane concentrate liquid line 121 Microfiltration membrane filtrate line 301 Treatment liquid 302 Sludge 303 Excess sludge
Claims (10)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2003428166A JP2004230377A (en) | 2003-01-09 | 2003-12-24 | Method for treating organic waste water |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2003003256 | 2003-01-09 | ||
| JP2003428166A JP2004230377A (en) | 2003-01-09 | 2003-12-24 | Method for treating organic waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2004230377A true JP2004230377A (en) | 2004-08-19 |
Family
ID=32964650
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2003428166A Pending JP2004230377A (en) | 2003-01-09 | 2003-12-24 | Method for treating organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2004230377A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007268468A (en) * | 2006-03-31 | 2007-10-18 | Toyo Eng Corp | High temperature treatment method for hydrocarbon or manufacture plant waste water of oxygenated compound |
| JP2008119655A (en) * | 2006-11-15 | 2008-05-29 | Nittetsu Kankyo Engineering Kk | Organic waste water treatment method and chemical used for this method |
| JP2008207094A (en) * | 2007-02-26 | 2008-09-11 | Kurita Water Ind Ltd | Biological treatment apparatus and method for organic matter-containing water |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11277095A (en) * | 1998-03-27 | 1999-10-12 | Kurita Water Ind Ltd | Biological treatment of organic waste solution |
| JP2000024690A (en) * | 1998-07-09 | 2000-01-25 | Shinko Pantec Co Ltd | Organic waste water treating device and its operation |
| JP2001025789A (en) * | 1999-07-14 | 2001-01-30 | Kurita Water Ind Ltd | Treatment of organic waste liquid and device therefor |
| JP2001179285A (en) * | 1999-12-24 | 2001-07-03 | Mitsubishi Heavy Ind Ltd | Wastewater treatment system |
| JP2001225090A (en) * | 2000-02-17 | 2001-08-21 | Kurita Water Ind Ltd | Method and apparatus for treating organic waste liquid |
| JP2002166289A (en) * | 2000-09-22 | 2002-06-11 | Shinko Pantec Co Ltd | Method to treat organic waste water and apparatus therefor |
| JP2002177979A (en) * | 2000-12-11 | 2002-06-25 | Mitsubishi Kakoki Kaisha Ltd | Waste water treatment equipment |
| JP2002177981A (en) * | 2000-12-13 | 2002-06-25 | Sumitomo Heavy Ind Ltd | Waste water treatment method and equipment |
| JP2003024972A (en) * | 2001-07-16 | 2003-01-28 | Ebara Corp | Biological treatment method for organic sewage and apparatus therefor |
-
2003
- 2003-12-24 JP JP2003428166A patent/JP2004230377A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11277095A (en) * | 1998-03-27 | 1999-10-12 | Kurita Water Ind Ltd | Biological treatment of organic waste solution |
| JP2000024690A (en) * | 1998-07-09 | 2000-01-25 | Shinko Pantec Co Ltd | Organic waste water treating device and its operation |
| JP2001025789A (en) * | 1999-07-14 | 2001-01-30 | Kurita Water Ind Ltd | Treatment of organic waste liquid and device therefor |
| JP2001179285A (en) * | 1999-12-24 | 2001-07-03 | Mitsubishi Heavy Ind Ltd | Wastewater treatment system |
| JP2001225090A (en) * | 2000-02-17 | 2001-08-21 | Kurita Water Ind Ltd | Method and apparatus for treating organic waste liquid |
| JP2002166289A (en) * | 2000-09-22 | 2002-06-11 | Shinko Pantec Co Ltd | Method to treat organic waste water and apparatus therefor |
| JP2002177979A (en) * | 2000-12-11 | 2002-06-25 | Mitsubishi Kakoki Kaisha Ltd | Waste water treatment equipment |
| JP2002177981A (en) * | 2000-12-13 | 2002-06-25 | Sumitomo Heavy Ind Ltd | Waste water treatment method and equipment |
| JP2003024972A (en) * | 2001-07-16 | 2003-01-28 | Ebara Corp | Biological treatment method for organic sewage and apparatus therefor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007268468A (en) * | 2006-03-31 | 2007-10-18 | Toyo Eng Corp | High temperature treatment method for hydrocarbon or manufacture plant waste water of oxygenated compound |
| JP4679413B2 (en) * | 2006-03-31 | 2011-04-27 | 東洋エンジニアリング株式会社 | High temperature treatment method for hydrocarbon or oxygenated compound production plant wastewater |
| JP2008119655A (en) * | 2006-11-15 | 2008-05-29 | Nittetsu Kankyo Engineering Kk | Organic waste water treatment method and chemical used for this method |
| JP2008207094A (en) * | 2007-02-26 | 2008-09-11 | Kurita Water Ind Ltd | Biological treatment apparatus and method for organic matter-containing water |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Mutamim et al. | Application of membrane bioreactor technology in treating high strength industrial wastewater: a performance review | |
| Mutamim et al. | Membrane bioreactor: applications and limitations in treating high strength industrial wastewater | |
| Stephenson et al. | Membrane bioreactors for wastewater treatment | |
| Li et al. | Treatment of synthetic wastewater by a novel MBR with granular sludge developed for controlling membrane fouling | |
| Dialynas et al. | Integration of a membrane bioreactor coupled with reverse osmosis for advanced treatment of municipal wastewater | |
| Trussell et al. | The effect of organic loading on process performance and membrane fouling in a submerged membrane bioreactor treating municipal wastewater | |
| Baek et al. | Lab-scale study of an anaerobic membrane bioreactor (AnMBR) for dilute municipal wastewater treatment | |
| Ghyoot et al. | Nitrogen removal from sludge reject water with a membrane-assisted bioreactor | |
| Tian et al. | Membrane adsorption bioreactor (MABR) for treating slightly polluted surface water supplies: as compared to membrane bioreactor (MBR) | |
| Baek et al. | Aerobic and anaerobic membrane bioreactors for municipal wastewater treatment | |
| KR20080078550A (en) | Method for biological processing of water containing organic material | |
| Tian et al. | Submerged membrane bioreactor (sMBR) for the treatment of contaminated raw water | |
| Hosseinzadeh et al. | Evaluation of membrane bioreactor for advanced treatment of industrial wastewater and reverse osmosis pretreatment | |
| WO2008066497A1 (en) | Water reclamation without biosludge production | |
| JP5034778B2 (en) | Membrane separation wastewater treatment method and apparatus | |
| Kocadagistan et al. | Treatment investigation of the Erzurum City municipal wastewaters with anaerobic membrane bioreactors | |
| Hasani Zonoozi et al. | Operation of integrated sequencing batch membrane bioreactor treating dye-containing wastewater at different SRTs: study of overall performance and fouling behavior | |
| JP4293529B2 (en) | Organic wastewater treatment method | |
| JP2016117064A (en) | Sewage treatment device and sewage treatment method using it | |
| JP2014000495A (en) | Sewage treatment apparatus, and sewage treatment method using the same | |
| JP2004230377A (en) | Method for treating organic waste water | |
| JP2009189943A (en) | Water treatment method and apparatus | |
| Itonaga et al. | Performance of membrane bioreactor combined with pre-coagulation/sedimentation | |
| JP2014213265A (en) | Method and device for biologically treating organic matter-containing water | |
| Гракова | Optimization of the structure decisions in designing a membrane bioreactor to increase the efficiency of treatment waste water of the dairy industry |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20061122 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20090416 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20090421 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20090618 |
|
| RD03 | Notification of appointment of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7423 Effective date: 20090618 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20100803 |
|
| A02 | Decision of refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A02 Effective date: 20110111 |