JP2005169253A - Method for decreasing excess sludge - Google Patents
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- JP2005169253A JP2005169253A JP2003412756A JP2003412756A JP2005169253A JP 2005169253 A JP2005169253 A JP 2005169253A JP 2003412756 A JP2003412756 A JP 2003412756A JP 2003412756 A JP2003412756 A JP 2003412756A JP 2005169253 A JP2005169253 A JP 2005169253A
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000003247 decreasing effect Effects 0.000 title claims 2
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 239000006228 supernatant Substances 0.000 claims abstract description 7
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 230000000813 microbial effect Effects 0.000 claims description 11
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 229910002804 graphite Inorganic materials 0.000 claims description 6
- 239000010439 graphite Substances 0.000 claims description 6
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- 238000001556 precipitation Methods 0.000 claims description 3
- 238000005868 electrolysis reaction Methods 0.000 abstract description 24
- 230000008021 deposition Effects 0.000 abstract description 7
- 239000010865 sewage Substances 0.000 abstract description 4
- 239000000126 substance Substances 0.000 description 19
- 244000005700 microbiome Species 0.000 description 18
- 230000001954 sterilising effect Effects 0.000 description 13
- 238000004659 sterilization and disinfection Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000002244 precipitate Substances 0.000 description 10
- 238000004062 sedimentation Methods 0.000 description 10
- 239000005416 organic matter Substances 0.000 description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- 238000002156 mixing Methods 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 7
- 239000002253 acid Substances 0.000 description 7
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 230000000844 anti-bacterial effect Effects 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 210000004027 cell Anatomy 0.000 description 4
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- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
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- 238000010586 diagram Methods 0.000 description 3
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- 239000012811 non-conductive material Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 238000011088 calibration curve Methods 0.000 description 2
- 210000002421 cell wall Anatomy 0.000 description 2
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- 238000010979 pH adjustment Methods 0.000 description 2
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- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 108091005804 Peptidases Proteins 0.000 description 1
- 239000004365 Protease Substances 0.000 description 1
- 102100037486 Reverse transcriptase/ribonuclease H Human genes 0.000 description 1
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- 229910003481 amorphous carbon Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
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- 238000003756 stirring Methods 0.000 description 1
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Classifications
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- 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
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- Treatment Of Sludge (AREA)
- Activated Sludge Processes (AREA)
Abstract
Description
本発明は、余剰汚泥の削減システムに関し、さらに詳しくは、有機性汚水の微生物処理によって生じる余剰汚泥を電解（「電気分解」を簡略化して「電解」で表す）により削減する方法であって、電解時の電極への不導体化物の析出を防止して、効率よく余剰汚泥を削減することができる、余剰汚泥の削減方法に関する。 The present invention relates to a surplus sludge reduction system, more specifically, a method for reducing surplus sludge generated by microbial treatment of organic wastewater by electrolysis (represented by “electrolysis” by simplifying “electrolysis”), The present invention relates to a method for reducing excess sludge, which can prevent the precipitation of non-conductors on an electrode during electrolysis and efficiently reduce excess sludge.
有機性汚水の微生物処理では、汚水中に存在する可溶性有機物を微生物が消化処理する一方で微生物の増殖を引き起こす。この増殖した微生物を含む汚泥はいわゆる余剰汚泥として排出する必要がある。この余剰汚泥は脱水処理した後にそのまま埋立処分されるか、または焼却処分されているが、余剰汚泥が難脱水性であるため、脱水処理した後でも７０〜８０質量％の水分を有するのが通常である。従って、これをそのまま埋立処分するにしても固形分２０〜３０質量％程度のものを運搬し埋め立てることになり、その質量および体積の大半が大部分を占める水分の搬送費および埋立費として費やされているのが現状である。また、焼却処分するにしても同様で余剰汚泥中に多量に存在する水分のためにその乾燥および蒸発潜熱にエネルギーの大半が費やされているのが現状であって、その費用は高額なものとなっている。 In microbial treatment of organic sewage, the microorganisms digest the soluble organic matter present in the sewage while causing microbial growth. The sludge containing the grown microorganisms needs to be discharged as so-called surplus sludge. This surplus sludge is either landfilled or incinerated after being dehydrated, but the surplus sludge is hardly dehydrated, so it usually has a water content of 70 to 80% by mass even after dehydration. It is. Therefore, even if this is landfilled as it is, it will be transported and landfilled with a solid content of about 20 to 30% by mass, and the mass and volume of the majority will be spent as moisture transportation and landfill costs. This is the current situation. In addition, even if it is incinerated, most of the energy is spent on drying and latent heat of evaporation due to the large amount of moisture in the excess sludge, and the cost is high. It has become.
これら余剰汚泥の量は年々増加の一途をたどっており、前記埋立処分するにしても焼却処分にしてもいずれも処理費用の占める割合が高く、また埋立場所の確保や焼却残さの処理など、経済面および環境面の両面において問題が顕在化している。 The amount of excess sludge has been increasing year by year, and the disposal cost is high for both landfill disposal and incineration. The problem has become obvious in both environmental and environmental aspects.
こうした背景の下で、この余剰汚泥の処理に微生物処理を有効に活用することが検討されている。余剰汚泥はその中に含まれている微生物を一旦死滅させて可溶性の有機物にすれば有機物の消化処理同様に活性汚泥により消化処理されることはよく知られている。可溶性有機物の消化処理により増殖した余剰汚泥を死滅させて可溶性有機物にした後、活性汚泥槽に返送することで微生物が可溶性有機物の消化処理を行い、余剰汚泥を減量化（または減容化）する。すなわち、余剰汚泥中の可溶性有機物を微生物に消化処理させることによって、余剰汚泥中の微生物は可溶性有機物を経てＣＯ2 とＨ2 Ｏとに分解されて減量化される。 Under such a background, effective utilization of microbial treatment for the treatment of surplus sludge has been studied. It is well known that surplus sludge is digested with activated sludge in the same way as digestion of organic matter once the microorganisms contained therein are killed to form soluble organic matter. Excess sludge grown by digestion of soluble organic matter is killed to become soluble organic matter, and then returned to the activated sludge tank so that microorganisms can digest soluble organic matter and reduce excess sludge (or volume reduction). . That is, by digesting the soluble organic matter in the excess sludge with microorganisms, the microorganisms in the excess sludge are decomposed into CO 2 and H 2 O via the soluble organic matter, and the amount is reduced.
余剰汚泥を減量化させる手段としては、種々の方法が提案されており、例えば、余剰汚泥に塩化物を添加して電解（電気分解）することによって余剰汚泥中の微生物を死滅させ、それを活性汚泥槽に返送することで余剰汚泥を減量化する方法が提案されている（例えば、特許文献１参照）。
この方法によれば、電解処理時に電極で次亜塩素酸（ＨＣｌＯ）を発生させ、その電極で発生した次亜塩素酸による酸化力を利用して余剰汚泥中の微生物を死滅させ、死滅した微生物を活性汚泥槽中に戻すことにより、微生物を可溶性の有機物として消化処理させることができる。 According to this method, hypochlorous acid (HClO) is generated at the electrode during the electrolytic treatment, and microorganisms in the excess sludge are killed using the oxidizing power of hypochlorous acid generated at the electrode. Is returned to the activated sludge tank to digest the microorganisms as soluble organic matter.
しかしながら、上記電解処理で余剰汚泥を直接電解処理した場合、余剰汚泥中に存在するミネラル成分含有物が酸化物や水酸化物などの化合物となってアノード（負極）に析出し、電極を不導体化させて導電率を低下させたり、あるいは電極を絶縁化して電解時の電流を流れにくくさせるという問題があった。 However, when the excess sludge is directly electrolytically treated by the above-described electrolytic treatment, the mineral component-containing material present in the excess sludge is deposited as a compound such as an oxide or hydroxide on the anode (negative electrode), and the electrode is non-conductive. There has been a problem that the conductivity is lowered by reducing the conductivity, or the electrode is insulated to make it difficult for current to flow during electrolysis.
この問題を解決するための方法としては、機械的なメンテナンスによる不導体化析出物の除去や電極の極性反転による不導体化析出物の除去方法が考えられる。後者の電極の極性反転による不導体化析出物の除去方法は一般に浄水器などのアルカリ成分を作るための機器に用いられており、この用途で用いる場合において、極性反転はおよそ６０秒間に１秒の割合で行われるなど周期的に反転するのが一般的であり、これはアルカリ、酸などを各電極で作り出してそれぞれの配管から流すためである。 As a method for solving this problem, there can be considered a method for removing a non-conductive precipitate by mechanical maintenance or a method for removing a non-conductive precipitate by reversing the polarity of an electrode. The latter method for removing non-conductive precipitates by polarity reversal of electrodes is generally used in equipment for producing alkaline components such as water purifiers, and in this application, polarity reversal takes approximately 1 second every 60 seconds. In general, the inversion is periodically performed, for example, in order to produce alkali, acid, or the like at each electrode and flow from each pipe.
しかしながら、上記電極の極性反転による方法を余剰汚泥の電解処理に用いた場合、余剰汚泥は水道水よりはるかに多いミネラル成分を含有しているため、定期的な極性反転では電極への不導体化析出物を充分に除去することができなかった。 However, when the electrode polarity reversal method is used for surplus sludge electrolysis, the surplus sludge contains much more minerals than tap water, so periodic polarity reversal makes the electrode nonconductive. The precipitate could not be removed sufficiently.
本発明は、上記のように従来の余剰汚泥の削減にあたっての電解処理時における問題点を解決し、電解処理時に電極に不導体化物が析出するのを防止して、電解処理により、余剰汚泥中の微生物を効率的に死滅化させ、余剰汚泥を効率よく削減することができる方法を提供することを目的とする。 The present invention solves the problems during the electrolytic treatment in reducing the conventional excess sludge as described above, prevents the decontamination from being deposited on the electrode during the electrolytic treatment, It is an object of the present invention to provide a method capable of efficiently killing microorganisms and efficiently reducing excess sludge.
本発明は、有機性汚水の微生物処理により生じる余剰汚泥を削減するにあたり、活性汚泥槽からの活性汚泥含有液を濃縮汚泥と上澄液とに分離し、濃縮汚泥の一部を活性汚泥槽に返送する第一工程と、前記余剰汚泥を電解槽内で電極を用いて電解処理を施す第二工程と、処理した余剰汚泥を再び活性汚泥槽に返送する第三工程とを有し、前記第二行程において行う電解処理時に電極の極性を一定の周期で反転させることにより、電極への不導体化物の析出を防止しつつ、余剰汚泥を削減することによって、前記課題を解決したものである。 In the present invention, in reducing surplus sludge generated by microbial treatment of organic sludge, the activated sludge-containing liquid from the activated sludge tank is separated into concentrated sludge and supernatant liquid, and a part of the concentrated sludge is converted into the activated sludge tank. A first step of returning, a second step of subjecting the excess sludge to electrolytic treatment using an electrode in an electrolytic cell, and a third step of returning the treated excess sludge to the activated sludge tank again, By reversing the polarity of the electrode at a constant period during the electrolytic treatment performed in the two steps, the above-mentioned problems are solved by reducing the excess sludge while preventing the deposition of the non-conductive material on the electrode.
すなわち、本発明においては、前記第二行程の電解処理時に、例えば、電源にスイッチ素子を設け、交互に切り替えて電極への印加電圧を逆転させるなどの方法を用いて電極を反転させることにより、余剰汚泥中に含まれるカルシウム、マグネシウムなどのミネラル成分が不導体化物として電極に析出するのを防止し、それによって、電極への不導体化析出物による電極の導電率の低下やそれに基づく電解効率の低下を防止することができる。従って、本発明によれば、電解時に生じる電極への不導体化析出物によって妨げられることなく、余剰汚泥を効率よく削減することができる。 That is, in the present invention, at the time of the electrolytic treatment in the second step, for example, by providing a switch element in the power source and switching the electrodes alternately by reversing the applied voltage to the electrodes, Prevents mineral components such as calcium and magnesium contained in excess sludge from precipitating on the electrode as deconductors, thereby reducing the conductivity of the electrode due to the deconductors deposit on the electrode and the electrolysis efficiency based on it Can be prevented. Therefore, according to the present invention, it is possible to efficiently reduce excess sludge without being hindered by the non-conducting precipitate on the electrode generated during electrolysis.
本発明によれば、有機性汚水の微生物処理により生じる余剰汚泥を効率よく削減することができる。 According to the present invention, it is possible to efficiently reduce excess sludge generated by microbial treatment of organic wastewater.
すなわち、本発明においては、前記のように、活性汚泥槽からの活性汚泥含有液を濃縮汚泥と上澄液とに分離し、濃縮汚泥の一部を活性汚泥槽に返送する第一工程と、前記余剰汚泥を電解槽内で電極を用いて電気分解処理を施す第二工程と、処理した余剰汚泥を再び活性汚泥槽に返送する第三工程を有する電解処理による余剰汚泥の削減システムにおいて、前記第二行程において行う電解処理時に電極の極性を反転させることにより、電極への不導体化物の析出を防止して、電極への不導体化析出物によって余剰汚泥の電解処理が妨げられることなく、効率的な電解処理が行えるようにして、余剰汚泥を効率よく削減することができるようにしたのである。 That is, in the present invention, as described above, the activated sludge-containing liquid from the activated sludge tank is separated into concentrated sludge and supernatant liquid, and a part of the concentrated sludge is returned to the activated sludge tank; In the system for reducing excess sludge by electrolytic treatment, which has a second step of subjecting the excess sludge to electrolysis treatment using an electrode in an electrolytic tank, and a third step of returning the treated excess sludge to the activated sludge tank again, By reversing the polarity of the electrode during the electrolytic treatment performed in the second step, the deposition of the non-conductive material on the electrode is prevented, and the electrolytic treatment of excess sludge is not hindered by the non-conductive material on the electrode, By making it possible to perform efficient electrolytic treatment, excess sludge can be efficiently reduced.
本発明において、前記第二行程の電解処理に用いる電極の材料は、陰極、陽極ともにグラファイトであることが好ましい。グラファイト以外の材料として白金を使用することができる。その他の材料を用いた場合、反転を周期的に行うことによって電極が溶解するか、あるいは、不導体化するなどの問題が生じるようになる。また、前記グラファイトのカーボン純度は９５％以上であることが好ましい。カーボン純度が低い場合、電位が安定しないことや、消耗が激しいなどの問題が生じるようになる。 In the present invention, the electrode material used for the electrolytic treatment in the second step is preferably graphite for both the cathode and the anode. Platinum can be used as a material other than graphite. When other materials are used, problems such as electrode dissolution or non-conductivity occur due to periodic inversion. The carbon purity of the graphite is preferably 95% or more. When the carbon purity is low, problems such as unstable electric potential and severe exhaustion occur.
電極の極性反転の時間比率（すなわち、一方の電極を陰極としているときと陽極としているときとの時間比率）は、電極への不導体化物の析出除去と電極の消耗を考え合わせると、４０％〜６０％（一方の電極と他方の電極との時間比率で示すと、４０：６０〜６０：４０）が好ましく、特に５０％が好ましい。これを詳しく説明すると、陽極は電解時に酸化されるため、電極材料としてグラファイトなどの炭素を用いていると、炭素が二酸化炭素になる反応が生じ陽極が消耗する。そのため、対となって存在する陽極と陰極を均一に消耗させるには電極の極性反転の時間比率は、４０％〜６０％が好ましく、特に５０％が好ましい。極性反転の時間比率を５０％に近付けることで、電極への不導体化物の析出を防止することができるとともに、電極の消耗の均一化も図れるのである。また、この電極の極性反転の切替時には０．０１秒から１分間の電解の休止時間を設けることが好ましい。すなわち、極性反転時に過渡的に電極にストレスが加わり消耗が加速するが、休止を設けることにより、極性反転の際に生じるストレスを緩和することができ消耗を抑えることができるからである。 The time ratio of the polarity inversion of the electrode (that is, the time ratio between when one electrode is used as a cathode and when it is used as an anode) is 40%, considering the removal of deconducted substances from the electrode and the consumption of the electrode. -60% (in terms of time ratio between one electrode and the other electrode, 40: 60-60: 40) is preferable, and 50% is particularly preferable. More specifically, since the anode is oxidized during electrolysis, if carbon such as graphite is used as an electrode material, the reaction of carbon into carbon dioxide occurs and the anode is consumed. Therefore, the time ratio of the polarity reversal of the electrodes is preferably 40% to 60%, and particularly preferably 50%, in order to evenly consume the anode and cathode present in pairs. By bringing the time ratio of polarity reversal closer to 50%, it is possible to prevent the deposition of non-conductors on the electrode and to make the electrode wear even. Further, it is preferable to provide an electrolysis rest period of 0.01 second to 1 minute when switching the polarity inversion of the electrode. That is, stress is applied to the electrode transiently during polarity reversal and wear is accelerated, but by providing a pause, the stress generated during polarity reversal can be mitigated and wear can be suppressed.
また、極性反転時の電流は０％から１００％まで増加または１００％から０％まで減少するのに要する時間は０．１秒から１分間とすることが好ましい。そうすることによって、極性反転時に過渡的に電極に与えられるストレスを緩和できる。 Further, it is preferable that the time required for the current during polarity reversal to increase from 0% to 100% or to decrease from 100% to 0% is from 0.1 second to 1 minute. By doing so, the stress transiently given to an electrode at the time of polarity reversal can be relieved.
次に、本発明の有機性汚水の微生物処理により生じる余剰汚泥の削減方法の実施の形態を図１および図２を用いて説明する。 Next, an embodiment of a method for reducing excess sludge generated by microbial treatment of organic wastewater according to the present invention will be described with reference to FIGS.
図１は本発明の有機性汚水の微生物処理により生じる余剰汚泥の削減方法を実施するための処理プロセスの概要を示す図であり、図２はその要部と電解処理に用いる電解装置を示す図である。 FIG. 1 is a diagram showing an outline of a treatment process for carrying out the method for reducing excess sludge generated by microbial treatment of organic wastewater of the present invention, and FIG. 2 is a diagram showing an essential part thereof and an electrolyzer used for electrolytic treatment. It is.
上記処理プロセスにおいて、まず、有機性汚水１は活性汚泥槽（曝気槽）２に導入され、その活性汚泥槽２中で微生物によって消化処理される。そして、その活性汚泥槽２から排出された活性汚泥含有液３は沈殿槽４に導入され、その沈殿槽４中で重力沈降法により活性汚泥を沈殿させ、濃縮汚泥と上澄液とに分離される。沈殿槽４中の上澄液は処理済水５として沈殿槽４から排出され、この処理済水５は殺菌して処理プロセス系外に放出される。 In the above treatment process, the organic sewage 1 is first introduced into an activated sludge tank (aeration tank) 2 and digested by microorganisms in the activated sludge tank 2. And the activated sludge containing liquid 3 discharged | emitted from the activated sludge tank 2 is introduce | transduced into the sedimentation tank 4, and activated sludge is settled by the gravity sedimentation method in the sedimentation tank 4, and it isolate | separates into a concentrated sludge and a supernatant liquid. The The supernatant liquid in the settling tank 4 is discharged from the settling tank 4 as treated water 5, and the treated water 5 is sterilized and discharged out of the treatment process system.
そして、沈殿槽４の底部に沈殿して濃度が高くなった活性汚泥は濃縮汚泥６として沈殿槽４から取り出され、そのうちの一部が返送汚泥７として前記活性汚泥槽２に戻される。ここまでのプロセスは従来の有機性汚水の微生物処理の場合と同様であるが、本発明では、この従来プロセスにおける濃縮汚泥の一部を余剰汚泥として引き抜き、後記のように、その余剰汚泥に特定の態様で電解を施し、余剰汚泥中の微生物を死滅させ、溶解性有機物に変えて微生物による消化処理を容易にさせる。 Then, the activated sludge precipitated at the bottom of the sedimentation tank 4 and having a high concentration is taken out from the sedimentation tank 4 as concentrated sludge 6, and a part of the sludge is returned to the activated sludge tank 2 as return sludge 7. The process so far is the same as in the case of conventional microbial treatment of organic wastewater, but in the present invention, a part of the concentrated sludge in this conventional process is extracted as excess sludge and specified as the excess sludge as described below. In this embodiment, electrolysis is performed to kill the microorganisms in the excess sludge and change to soluble organic substances to facilitate digestion with microorganisms.
そして、前記残りの濃縮汚泥６は余剰汚泥８として薬剤混合槽９に送られ、通常、その薬剤混合槽９中で上記余剰汚泥８に塩化物が添加され、かつ酸が添加されてｐＨが２〜６に調整されるとともに固形分濃度が０．２〜３質量％に調整される。 The remaining concentrated sludge 6 is sent to the chemical mixing tank 9 as surplus sludge 8, and usually chloride is added to the surplus sludge 8 in the chemical mixing tank 9 and an acid is added to adjust the pH to 2. The solid content concentration is adjusted to 0.2 to 3% by mass.
上記塩化物としては、例えば、塩化ナトリウム、塩化カリウム、塩化マグネシウム、塩化カルシウムなどが好ましい。これは、それらの塩化物が後の電解処理工程において殺菌作用の高い次亜塩素酸を発生させやすいからである。そして、この余剰汚泥８への塩化物の添加量は０．１〜３．５質量％が好ましい。 As said chloride, sodium chloride, potassium chloride, magnesium chloride, calcium chloride etc. are preferable, for example. This is because those chlorides tend to generate hypochlorous acid having a high bactericidal action in the subsequent electrolytic treatment process. And the addition amount of the chloride to this excess sludge 8 is preferably 0.1 to 3.5% by mass.
薬剤混合槽９において、余剰汚泥８に添加する酸は、殺菌作用（微生物の死滅化作用）を高めるために添加するものであるが、この酸としては、例えば、塩酸や硫酸などの強酸が好ましく、特に塩酸は次亜塩素酸の供給源にもなることから好ましい。 In the chemical mixing tank 9, the acid added to the excess sludge 8 is added to enhance the bactericidal action (microbe killing action). As this acid, for example, a strong acid such as hydrochloric acid or sulfuric acid is preferable. In particular, hydrochloric acid is preferable because it also serves as a source of hypochlorous acid.
本発明においては、上記のように余剰汚泥に酸を添加してｐＨ２〜６に調整することによって、電解時に上記塩化物から効率よく次亜塩素酸を発生させ、殺菌作用を向上させることができるが、このｐＨとしては特にｐＨ４〜６が好ましい。ｐＨが２より低い場合は有害な塩素ガスが発生し、ｐＨが６より高い場合は殺菌作用が低下するおそれがある。また、アルカリ性にすると、殺菌作用が低下するだけでなく、微生物の細胞壁が傷つけられやすく、プロテアーゼにより微生物内部から細胞壁を溶解させることができなくなり、不溶解性有機物を溶解性有機物に効率よく変えることができなくなるおそれがある。ただし、前記のような塩化物の添加や酸化によるｐＨ調整、余剰汚泥の固形分濃度などは必ずしも上記例示の場合のみに限られることはない。 In the present invention, by adding acid to excess sludge as described above and adjusting to pH 2-6, hypochlorous acid can be efficiently generated from the chloride during electrolysis, and the bactericidal action can be improved. However, this pH is particularly preferably pH 4-6. When the pH is lower than 2, harmful chlorine gas is generated, and when the pH is higher than 6, the bactericidal action may be lowered. In addition, when alkaline, not only the bactericidal action is lowered, but also the cell wall of the microorganism is easily damaged, and it becomes impossible to dissolve the cell wall from inside the microorganism by protease, and the insoluble organic substance can be efficiently converted into the soluble organic substance. There is a risk that it will not be possible. However, pH adjustment by addition of chloride and oxidation as described above, solid content concentration of excess sludge, and the like are not necessarily limited to the above examples.
本発明の第二工程においては、薬剤混合槽９で薬剤（すなわち、塩化物と酸）が混合された余剰汚泥は薬剤混合汚泥１０として電解槽１１に導入され、その電解槽１１において電解されることで、電極表面で生じる次亜塩素酸による殺菌（微生物の死滅化）が行われる。上記電解時の電流密度は大きいほど、電解時間が短くて済むが、電極間の電圧が上昇して水の分解も起こり殺菌効率を低下させるため、電流密度は１〜１００ｍＡ／ｃｍ2 が好ましく、特に２〜５０ｍＡ／ｃｍ2 が好ましい。 In the second step of the present invention, surplus sludge mixed with the chemical (that is, chloride and acid) in the chemical mixing tank 9 is introduced into the electrolytic tank 11 as the chemical mixed sludge 10 and electrolyzed in the electrolytic tank 11. Thus, sterilization (determination of microorganisms) by hypochlorous acid generated on the electrode surface is performed. The larger the current density during the electrolysis, the shorter the electrolysis time, but the voltage between the electrodes rises and water is decomposed to reduce the sterilization efficiency. Therefore, the current density is preferably 1 to 100 mA / cm 2 , 2-50 mA / cm < 2 > is particularly preferable.
ここで、この電解処理の詳細およびその電解処理における電極の極性反転を図２を参照しつつ説明する。まず、図２中の参照符号とその対象物について説明すると、２１は電解槽であって、図１の電解槽１１に対応するものである。２２は塩化ナトリウムと塩酸が添加された余剰汚泥で、図１の薬液混合汚泥１０に相当するものであり、電解処理では、いわば電解液に相当するものである。そして、２３と２４はそれぞれ電極Ａと電極Ｂであって、これらの電極Ａ、Ｂはその表面がいずれもカーボン純度９５％以上のグラファイトで構成され、図２では１枚ずつしか示していないものの、実際には、それぞれ複数枚が並列に接続されている。２５は電解用の電源であって、この電源２５はタイミング発回路２６からの指令で出力のオン・オフ、１秒から１分の漸増、漸減の立ち上がり、立下りができる特性を有している。２７はスイッチの駆動回路であり、４個のスイッチ（スイッチング素子）２８〜３１は図２中においてＳＷ１、ＳＷ２、ＳＷ３、ＳＷ４で表示されている。電解処理のための動作は、タイミング発回路２６の作り出すタイミングで進行する。例えば、休止時間から説明を始めると、電源２５の出力は最初はオフで、２８〜３１のスイッチ（ＳＷ１〜ＳＷ４）のいずれも開放である。この期間が１秒から１分持続した後、次の期間は、２８のスイッチ（ＳＷ１）と３１のスイッチ（ＳＷ４）が閉じ、電源２５の出力は１秒から１分で０％から１００％に立ち上がり、次の期間は１００％の出力が電極Ａ、Ｂに印加され続け、電解処理が行われる。この期間が１秒から１０時間続いた後、電源２５は１秒から１分で１００％から０％に立ち下がる。
Here, details of the electrolytic treatment and polarity inversion of the electrodes in the electrolytic treatment will be described with reference to FIG. First, reference numerals and objects in FIG. 2 will be described. Reference numeral 21 denotes an electrolytic cell, which corresponds to the electrolytic cell 11 in FIG. Reference numeral 22 denotes an excess sludge to which sodium chloride and hydrochloric acid are added, which corresponds to the chemical liquid mixed sludge 10 in FIG. 1, and corresponds to an electrolyte in an electrolytic process. Reference numerals 23 and 24 denote an electrode A and an electrode B, respectively, and the surfaces of these electrodes A and B are both composed of graphite having a carbon purity of 95% or more, although only one sheet is shown in FIG. Actually, a plurality of each is connected in parallel. Reference numeral 25 denotes a power source for electrolysis. The power source 25 has a characteristic capable of turning on / off the output, gradually increasing from 1 second to 1 minute, gradually rising and falling by a command from the timing generation circuit. . Reference numeral 27 denotes a switch drive circuit, and the four switches (switching elements) 28 to 31 are represented by SW1, SW2, SW3, and SW4 in FIG. The operation for the electrolytic process proceeds at a timing generated by the timing generation circuit 26. For example, when the description starts from the downtime, the output of the power supply 25 is initially off, and all the
電源２５がオフの後、２８〜３１のスイッチ（ＳＷ１〜ＳＷ４）はすべて開放で、この状態が０．０１秒から１分続き、その後、２９のスイッチ（ＳＷ２）との３０のスイッチ（ＳＷ３）が閉じ、これで電極Ａ、Ｂのアノードとカソードが入れ替わる。ついで電源２５の出力は１秒から１分で０％から１００％に立ち上がる、次の期間は１００％の出力が電極に印加され続け、逆方向の電解が行われる。
After the power supply 25 is turned off, the
次に、実施例を挙げて本発明をより具体的に説明するが、本発明はそれらの実施例に限定されるものではない。 EXAMPLES Next, the present invention will be described more specifically with reference to examples, but the present invention is not limited to these examples.
実施例１
図１に示す処理プロセスに基づき、次の（ｉ）、（ｉｉ）、（ｉｉｉ）の条件で余剰汚泥の電解処理による削減を行った。なお、以下において、濃度を示す％は、特に基準を付記しないかぎり、質量％である。
（ｉ） 余剰汚泥８として固形分濃度が０. ９５％の余剰汚泥２００ｍｌを準備し、薬剤混合槽９としての２００ｍｌビーカーに投入した。なお、この余剰汚泥は、図２に示すように、有機性汚水１を活性汚泥槽２に導入し、その活性汚泥槽２で微生物により消化処理させ、その活性汚泥槽２から活性汚泥含有液３として排出し、その活性汚泥含有液３を沈殿槽４に導入し、その沈殿槽４で活性汚泥を沈殿させ、上澄液を処理済水５として沈殿槽４から放出し（この処理済水５は殺菌処理して処理系外に放出される）、沈殿して濃度が高くなった汚泥を濃縮汚泥６として沈殿槽４から取り出し、その濃縮汚泥６の一部を返送汚泥７として活性汚泥槽２に戻し、その際に残ったものを余剰汚泥８としたものである。
Example 1
Based on the treatment process shown in FIG. 1, the excess sludge was reduced by electrolytic treatment under the following conditions (i), (ii), and (iii). In the following, “%” indicating concentration is “% by mass” unless otherwise specified.
(I) As surplus sludge 8, 200 ml of surplus sludge having a solid content concentration of 0.95% was prepared and charged into a 200 ml beaker serving as the chemical mixing tank 9. In addition, as shown in FIG. 2, this excess sludge introduce | transduces the organic sludge 1 into the activated sludge tank 2, makes it digest with microorganisms in the activated sludge tank 2, and the activated sludge containing liquid 3 from the activated sludge tank 2 The activated sludge-containing liquid 3 is introduced into the sedimentation tank 4, the activated sludge is precipitated in the sedimentation tank 4, and the supernatant is discharged from the sedimentation tank 4 as treated water 5 (this treated water 5 Is discharged to the outside of the treatment system after being sterilized), and the sludge having a high concentration after sedimentation is taken out from the sedimentation tank 4 as the concentrated sludge 6, and a part of the concentrated sludge 6 is returned to the activated sludge tank 2 as the return sludge 7. In this case, surplus sludge 8 is obtained from the remaining portion.
（ｉｉ） 薬剤としては１．０ｇの塩化ナトリウムと、ｐＨ調整のための塩酸を用い、余剰汚泥８中に添加してｐＨ約５に調整して薬剤混合汚泥１０とした。この薬剤混合汚泥１０中の塩化ナトリウムの濃度は０．５％であった。 (Ii) 1.0 g of sodium chloride and hydrochloric acid for pH adjustment were used as the chemicals, which were added to the excess sludge 8 to adjust the pH to about 5 to obtain a chemical mixed sludge 10. The concentration of sodium chloride in the drug mixed sludge 10 was 0.5%.
（ｉｉｉ） この薬剤混合汚泥１０が入ったビーカーを電解槽１１とし、電解用の正極および負極としてそれぞれ有効電極面積が２５ｃｍ2 のアモルファスカーボン電極（乾燥時の質量：８．０ｇ）を電極間距離１５ｍｍで薬剤混合汚泥中に差し込み、攪拌を行いながら図２に示す電解装置を用いて直流電流１００ｍＡで、周期１０分ごとに極性の反転を行い、その際の停止（休止）時間は１秒とし、０ｍＡから１００ｍＡおよび１００ｍＡから０ｍＡまでの電流変化時間をそれぞれ０. ５秒として１時間通電した。このときの電圧は４．２Ｖで、汚泥の温度は２５℃であった。 (Iii) The beaker containing the drug-mixed sludge 10 is used as an electrolytic cell 11, and an amorphous carbon electrode (mass when dried: 8.0 g) having an effective electrode area of 25 cm 2 is used as a positive electrode and a negative electrode for electrolysis. At 15 mm, it is inserted into the chemical mixed sludge, and while stirring, the polarity is reversed every 10 minutes with a direct current of 100 mA using the electrolysis apparatus shown in FIG. 2, and the stop (rest) time is 1 second. The current change time from 0 mA to 100 mA and 100 mA to 0 mA was 0.5 seconds, respectively, and the current was applied for 1 hour. The voltage at this time was 4.2 V, and the temperature of the sludge was 25 ° C.
上記処理の結果、薬剤混合時には多量の微生物が生存していたが、それに続く電解処理により殺菌され（殺菌率を溶存酸素の減少率から求めたところ９５％であった。）、電解後の電極表面には析出物が見られなかった。 As a result of the above treatment, a large amount of microorganisms were alive at the time of mixing the chemicals, but were sterilized by the subsequent electrolytic treatment (the sterilization rate was 95% as determined from the decrease rate of dissolved oxygen), and the electrode after electrolysis. No precipitate was observed on the surface.
上記殺菌率（微生物の死滅率）は、次のようにして求めた。すなわち、電解処理後の余剰汚泥に空気を１０分間バブリングを行った後、溶存酸素の減少率を測定した。その溶存酸素の減少率の測定に先立ち、原液（固形分濃度が０. ９５％の余剰汚泥）の溶存酸素の減少率から求めた殺菌率を０％とし、蒸留水の溶存酸素の減少率から求めた殺菌率を１００％とし、上記原液に対して、その２０％を蒸留水で希釈した余剰汚泥（活性汚泥）の殺菌率を２０％とし、５０％を蒸留水で希釈した余剰汚泥（活性汚泥）の殺菌率を５０％とし、７０％を蒸留水で希釈した余剰汚泥（活性汚泥）の殺菌率を７０％として検量線を引き、この検量線を用いて溶存酸素の減少率の測定結果を殺菌率（微生物の死滅率）として求めた。その結果、前記のように、殺菌率（微生物の死滅率）は９５％であった。また、前記（ｉ）〜（ｉｉｉ）の行程を１０回繰り返した後の電解処理時の電位は４．２Ｖであり、電極の不導体化が生じていないことを示していた。また、電極の乾燥質量を測定したところ、電極の乾燥質量は７．７ｇと７．６ｇであって、もとより、不導体化析出物による電極の質量増加はなく、電極の質量減少はほぼ均等であり、かつ電極の消耗が少ないことを示していた。 The sterilization rate (microbe kill rate) was determined as follows. That is, the excess sludge after electrolytic treatment was bubbled with air for 10 minutes, and then the reduction rate of dissolved oxygen was measured. Prior to the measurement of the rate of decrease in dissolved oxygen, the sterilization rate obtained from the rate of decrease in dissolved oxygen in the stock solution (excess sludge with a solid content of 0.95%) was assumed to be 0%, and the rate of decrease in dissolved oxygen from distilled water was The obtained sterilization rate is set to 100%, and the sterilization rate of 20% of excess sludge (activated sludge) diluted with distilled water is set to 20% and 50% of excess sludge diluted with distilled water (active) The sterilization rate of sludge) is 50%, 70% is diluted with distilled water, the sterilization rate of surplus sludge (activated sludge) is 70%, a calibration curve is drawn, and the measurement result of the decrease rate of dissolved oxygen using this calibration curve Was determined as the sterilization rate (microbe kill rate). As a result, as described above, the sterilization rate (microbe kill rate) was 95%. Moreover, the electric potential at the time of the electrolytic treatment after repeating the steps (i) to (iii) 10 times was 4.2 V, indicating that no electrode was made nonconductive. Moreover, when the dry mass of the electrode was measured, the dry mass of the electrode was 7.7 g and 7.6 g. Of course, there was no increase in the mass of the electrode due to the non-conductive precipitate, and the mass decrease in the electrode was almost uniform. And there was little consumption of the electrode.
比較例１
通常の直流電源を用いて直流電流１００ｍＡで、極性反転および停止（休止）を行わずに１時間通電した以外は、実施例１と同様に処理し、それらの場合における電解後の電極への析出物の付着状態および殺菌率を調べた。その結果、殺菌率は６４％で、電解後のカソードの表面全体が白色析出物で覆われた状態になっていた。この白色析出物を分析した結果、表１に示すように余剰汚泥中に含まれている、カルシウムなどのミネラルを主成分とする析出物であった。また、（ｉ）〜（ｉｉｉ）の行程（ただし、極性反転を行わない）を１０回繰り返した後の電解処理時の電位は５．２Ｖとなり、電極の不導体化が生じていることを示していた。また、電極の乾燥重量を測定したところ、陽極が７．１ｇであるのに対して陰極が８．１ｇになっていて、陽極は質量減少を起こし、陰極は不導体化物の析出により質量増加を起こしていた。
Comparative Example 1
The treatment was the same as in Example 1 except that the current was supplied for 1 hour without polarity reversal and stop (pause) at a DC current of 100 mA using a normal DC power supply, and deposition on the electrode after electrolysis in those cases The adhesion state and sterilization rate of the object were investigated. As a result, the sterilization rate was 64%, and the entire surface of the cathode after electrolysis was covered with white precipitates. As a result of analysis of the white precipitate, as shown in Table 1, it was a precipitate containing, as a main component, a mineral such as calcium contained in excess sludge. In addition, the potential at the time of electrolytic treatment after repeating steps (i) to (iii) (however, polarity inversion is not performed) 10 times becomes 5.2 V, indicating that the electrode is made non-conductive. It was. Further, when the dry weight of the electrode was measured, the anode was 7.1 g while the cathode was 8.1 g, the anode caused a decrease in mass, and the cathode increased in mass due to the deposition of a non-conductor. I was waking up.
上記実施例１と比較例１との対比から明らかなように、電解処理時に電極の表面への不導体化物の析出を防止して、効率的な電解処理を行い、かつ電極の消耗を防止するためには、電解処理時に電極の極性反転を行うことが必要であることがわかる。 As is clear from the comparison between Example 1 and Comparative Example 1, the deposition of non-conductors on the surface of the electrode during electrolytic treatment is prevented, efficient electrolytic treatment is performed, and consumption of the electrode is prevented. For this purpose, it is understood that it is necessary to reverse the polarity of the electrode during the electrolytic treatment.
１ 有機性汚水
２ 活性汚泥槽
３ 活性汚泥含有液
４ 沈殿槽
５ 処理済水
６ 濃縮汚泥
７ 返送汚泥
８ 余剰汚泥
９ 薬剤混合槽
１０ 薬剤混合汚泥
１１ 電解槽
２１ 電解槽
２２ 余剰汚泥（薬剤混合汚泥）
２３ 電極Ａ
２４ 電極Ｂ
２５ 電源
２６ タイミング発回路
２７ スイッチの駆動回路
２８ スイッチ（ＳＷ１）
２９ スイッチ（ＳＷ２）
３０ スイッチ（ＳＷ３）
３１ スイッチ（ＳＷ４）
DESCRIPTION OF SYMBOLS 1 Organic sludge 2 Activated sludge tank 3 Activated sludge containing liquid 4 Precipitation tank 5 Treated water 6 Concentrated sludge 7 Return sludge 8 Surplus sludge 9 Chemical mixing tank 10 Chemical mixing sludge 11 Electrolytic tank 21 Electrolytic tank 22 Surplus sludge (chemical mixed sludge )
23 Electrode A
24 Electrode B
25 Power supply 26 Timing generator circuit 27
29 switch (SW2)
30 switch (SW3)
31 switch (SW4)
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