JP2006167611A - Water cleaning system - Google Patents

Water cleaning system Download PDF

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JP2006167611A
JP2006167611A JP2004364216A JP2004364216A JP2006167611A JP 2006167611 A JP2006167611 A JP 2006167611A JP 2004364216 A JP2004364216 A JP 2004364216A JP 2004364216 A JP2004364216 A JP 2004364216A JP 2006167611 A JP2006167611 A JP 2006167611A
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water
membrane
basin
membrane separation
sand filtration
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JP4539321B2 (en
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Yuji Yamada
雄司 山田
Daisuke Hirano
大助 平野
Manabu Matsumoto
学 松本
Yosuke Sakamoto
陽介 坂元
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Hitachi Plant Technologies Ltd
株式会社日立プラントテクノロジー
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Abstract

<P>PROBLEM TO BE SOLVED: To prevent almost treatment load of a sedimentation basin and a sand filter basin from increasing even when the membrane permeate obtained by subjecting settled sludge and cleaning effluent to membrane separation is refluxed to the system. <P>SOLUTION: The water cleaning system comprises the sedimentation basin 12 in which the suspended solid in raw water 30 is separated as sedimented sludge 34, the sand filtration basin 14 which filters supernatant 36 in the sedimentation basin 12 by sand to form treated water 38, a first membrane separator 24 which subjects the sedimented sludge 34 withdrawn from the sedimentation basin 12 to membrane separation, a second membrane separator 26 which subjects the cleaning effluent 46 of the sand filtration basin 14 to membrane separation, an oxidation means 28 which subjects the membrane permeate 50 of the first membrane separator 24 to an oxidation treatment, a means which makes the oxidation-treated membrane permeate 50 confluent with the cleaning effluent 46, and a means which makes the membrane permeate 58 of the second membrane separator 26 confluent with the treated water 38. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

本発明は浄水システムに係り、特に原水中の懸濁物質を沈殿汚泥として分離する沈殿池と、この沈殿池の上澄水を砂濾過して処理水とする砂濾過池を備えた浄水システムに関する。   The present invention relates to a water purification system, and more particularly to a water purification system including a sedimentation basin that separates suspended substances in raw water as sedimentation sludge, and a sand filtration basin that uses the supernatant water of the sedimentation basin as a filtered water.

この種の浄水システムの沈殿池では原水量に対して1%未満の沈殿汚泥が発生する。また、砂濾過池では定期的(例えば1日に1回程度)に逆洗などの洗浄操作が必要であり、この洗浄操作の際に原水量の5〜10%程度に相当する量の処理水が使われ、洗浄排水として排出される。これらの沈殿汚泥や洗浄排水は濃縮処理を施すことによって濃縮汚泥と分離水に分け、濃縮汚泥は別系の汚泥処理設備で処理する。また、分離水は沈殿池の入口側に返送し、原水と混合して再び沈殿池に流入させるようにしている。   In the sedimentation basin of this type of water purification system, sediment sludge of less than 1% is generated with respect to the amount of raw water. In addition, the sand filtration pond requires regular washing operations such as backwashing (for example, about once a day), and the amount of treated water corresponding to about 5 to 10% of the amount of raw water during this washing operation. Is used and discharged as cleaning wastewater. These settled sludge and washing wastewater are separated into concentrated sludge and separated water by concentrating, and the concentrated sludge is treated in a separate sludge treatment facility. The separated water is returned to the inlet side of the sedimentation basin, mixed with the raw water, and again flows into the sedimentation basin.

濃縮処理としては一般に沈殿処理が採用されている。しかしながら、沈殿処理によって得られた分離水は懸濁物質を多く含んでおり、これを上記のように沈殿池に還流させると量的にも質的にも沈殿池及び砂濾過池の処理負荷を増大させ、浄水効率を低下させる。   In general, a precipitation process is employed as the concentration process. However, the separated water obtained by the precipitation treatment contains a lot of suspended solids, and when this is refluxed to the precipitation basin as described above, the treatment load of the precipitation basin and sand filtration pond is quantitatively and qualitatively increased. Increase the water purification efficiency.

このような問題点を改善するために、沈殿汚泥や洗浄排水を濃縮処理する手段として膜分離手段を用いる方法が提案されている(例えば、特許文献1及び特許文献2参照)。   In order to improve such problems, a method using a membrane separation means as a means for concentrating precipitation sludge and washing wastewater has been proposed (see, for example, Patent Document 1 and Patent Document 2).

特許文献1に記載された方法は、沈殿汚泥や洗浄排水を多段処理して最終的に分離した膜透過水を砂濾過池の処理水に合流させる。この方法によれば膜透過水を沈殿池に還流させないので、沈殿池及び砂濾過池の処理負荷が増大せず、浄水効率の優れた浄水システムを実現できる。   In the method described in Patent Document 1, membrane permeated water finally separated by multistage treatment of precipitated sludge and washing wastewater is combined with the treated water of the sand filtration pond. According to this method, since the membrane permeated water is not refluxed to the settling basin, the treatment load of the settling basin and the sand filtration pond is not increased, and a water purification system with excellent water purification efficiency can be realized.

また、特許文献2に記載された方法は、同様に沈殿汚泥や洗浄排水を多段処理して最終的に分離した膜透過水を沈殿池に還流させる。このため、沈殿池及び砂濾過池の処理負荷が量的に増大する欠点は依然として残る。しかしながら、膜透過水は清澄であるため、質的な面では沈殿池及び砂濾過池の処理負荷は殆んど増大しないという、優れた改善効果を達成できる。
特開平10−165990号公報 特開2003−236558号公報
Moreover, the method described in Patent Document 2 similarly returns the membrane permeated water finally separated by multistage treatment of the precipitated sludge and washing wastewater to the settling basin. For this reason, the fault that the processing load of a sedimentation basin and a sand filtration pond increases quantitatively still remains. However, since the permeated water of the membrane is clear, an excellent improvement effect that the treatment load of the sedimentation basin and the sand filtration basin is hardly increased in terms of quality can be achieved.
Japanese Patent Laid-Open No. 10-165990 JP 2003-236558 A

しかしながら、本発明者の実験によれば、上記特許文献1に記載された方法で分離された膜透過水には溶解性のマンガンが比較的多く含まれていることが判明した。したがって、この膜透過水を砂濾過池の処理水に合流させると、処理水のマンガン濃度を引き上げ、処理水の水質を悪化させることがある。上記特許文献2に記載された方法では、沈殿池に還流させた膜透過水中の溶解性のマンガンは、沈殿池と砂濾過池を経由する過程でその大部分が除去される。したがって、砂濾過池の処理水のマンガン濃度が飲用基準を上回るケースは殆んどない。しかしながら、上記したように、特許文献2に記載された方法は、沈殿池及び砂濾過池の処理負荷を量的に増大させるという欠点がある。   However, according to the experiment by the present inventor, it was found that the membrane permeated water separated by the method described in Patent Document 1 contains a relatively large amount of soluble manganese. Therefore, when this membrane permeated water is merged with the treated water of the sand filtration pond, the manganese concentration of the treated water is raised and the quality of the treated water may be deteriorated. In the method described in Patent Document 2, most of the soluble manganese in the membrane permeated water refluxed to the sedimentation basin is removed in the process of passing through the sedimentation basin and sand filtration basin. Therefore, there are almost no cases where the manganese concentration of the treated water in the sand filtration pond exceeds the drinking standard. However, as described above, the method described in Patent Document 2 has a drawback that the processing load of the settling basin and the sand filtration basin is quantitatively increased.

本発明の目的は、上記従来技術の問題点を改善し、沈殿池と砂濾過池を備えた浄水システムにおいて、沈殿汚泥や洗浄排水を膜分離して得た膜透過水を当該浄水システムに還流させた場合でも、沈殿池及び砂濾過池の処理負荷を殆んど増大させず、かつ、処理水中の溶解性のマンガン濃度を低く抑えることが可能な浄水システムを提供することにある。   The object of the present invention is to improve the above-mentioned problems of the prior art, and in a water purification system having a sedimentation basin and a sand filtration pond, the membrane permeate obtained by membrane separation of sedimentation sludge and washing wastewater is returned to the water purification system. It is an object of the present invention to provide a water purification system that can increase the treatment load of a settling basin and a sand filtration basin almost without increasing the soluble manganese concentration in the treated water.

上記目的を達成するために、本発明に係る第1の浄水システムは、原水中の懸濁物質を沈殿汚泥として分離する沈殿池と、前記沈殿池の上澄水を砂濾過して処理水とする砂濾過池と、前記沈殿池から抜き出した沈殿汚泥を膜分離する第1膜分離装置と、前記砂濾過池の洗浄排水を膜分離する第2膜分離装置と、前記第1膜分離装置の膜透過水を酸化処理する酸化手段と、前記酸化手段によって酸化処理された前記膜透過水を前記洗浄排水に合流させる手段と、前記第2膜分離装置の膜透過水を前記処理水に合流させる手段とを具備したことを特徴とする。   In order to achieve the above object, a first water purification system according to the present invention includes a sedimentation basin that separates suspended substances in raw water as sedimentary sludge, and sand filtration that uses the supernatant water of the sedimentation basin as a sand filter to obtain treated water. A pond, a first membrane separation device for separating the sludge extracted from the sedimentation basin, a second membrane separation device for membrane separation of the waste water from the sand filtration pond, and a membrane permeate for the first membrane separation device Oxidizing means for oxidizing the membrane, means for joining the membrane permeated water oxidized by the oxidizing means to the washing waste water, and means for joining the membrane permeated water of the second membrane separation device to the treated water It is characterized by having.

また、本発明に係る第2の浄水システムは、原水中の懸濁物質を沈殿汚泥として分離する沈殿池と、前記沈殿池の上澄水を砂濾過して処理水とする砂濾過池と、前記沈殿池から抜き出した沈殿汚泥を膜分離する第1膜分離装置と、前記砂濾過池の洗浄排水を膜分離する第2膜分離装置と、前記第1膜分離装置の膜透過水を前記沈殿池の入口側に返送する手段と、前記第2膜分離装置の膜透過水を前記処理水に合流させる手段とを具備したことを特徴とする。   Moreover, the 2nd water purification system which concerns on this invention is a sedimentation basin which isolate | separates the suspended substance in raw | natural water as a sedimentation sludge, the sand filtration pond which sand-filters the supernatant water of the said sedimentation basin, and the said sedimentation basin A first membrane separation device for separating the precipitated sludge extracted from the membrane, a second membrane separation device for membrane-separating the washing waste water of the sand filtration pond, and an inlet of the sedimentation basin for the membrane permeated water of the first membrane separation device And a means for joining the permeated water of the second membrane separation device to the treated water.

本発明に係る第1の浄水システムによれば、沈殿汚泥や洗浄排水を膜分離して最終的に得られた膜透過水は清澄であり、溶解性のマンガンもほとんど含まず、砂濾過池の処理水と同等レベルの水質を維持している。したがって、膜透過水を沈殿池の入口側に還流させることなく、直接に砂濾過池の処理水に合流させることができる。このため、沈殿池及び砂濾過池の処理負荷を増大させず、かつ、処理水中の溶解性のマンガン濃度を低く抑えることができる。   According to the 1st water purification system which concerns on this invention, the membrane permeate finally obtained by carrying out the membrane separation of the sedimentation sludge and washing | cleaning waste_water | drain is clear, hardly contains soluble manganese, Maintains water quality equivalent to treated water. Therefore, the membrane permeated water can be directly merged with the treated water of the sand filtration pond without returning to the inlet side of the settling basin. For this reason, the processing load of a sedimentation basin and a sand filtration pond is not increased, and the soluble manganese concentration in treated water can be kept low.

本発明に係る第2の浄水システムによれば、第1膜分離装置の膜透過水を沈殿池の入口側に返送するようにした。この膜透過水は清澄であるが溶解性のマンガンを比較的多く含んでいる。ただし、膜透過水の水量は原水量に対して多くとも1%未満であり、このような清澄かつ少量の膜透過水を原水に混合しても、沈殿池及び砂濾過池の処理負荷は殆んど増大しない。また、膜透過水に含まれる溶解性のマンガンは沈殿池での凝集沈殿や砂濾過池での砂濾過を受ける過程でその大部分が除去されるので、処理水中の溶解性のマンガン濃度を低く抑えることができる。また、この第2の浄水システムでは酸化手段を省略することが可能であり、第1の浄水システムに比べてシステムの簡略化を図ることができる。   According to the 2nd water purification system which concerns on this invention, the membrane permeated water of the 1st membrane separator was returned to the entrance side of a sedimentation basin. This membrane permeate is clear but contains a relatively large amount of soluble manganese. However, the amount of membrane permeated water is less than 1% at most with respect to the amount of raw water, and even if such a clear and small amount of membrane permeated water is mixed with raw water, the treatment load on the sedimentation basin and sand filtration pond is almost the same. Does not increase. In addition, most of the soluble manganese contained in the permeated water is removed during the process of coagulating sedimentation in the sedimentation basin and sand filtration in the sand filtration basin, so the concentration of soluble manganese in the treated water is lowered. Can be suppressed. Moreover, in this 2nd water purification system, an oxidation means can be abbreviate | omitted and the system can be simplified compared with a 1st water purification system.

図1は本発明に係る第1の浄水システムの実施形態を示す系統図である。当該浄水システムは浄水製造系Aと汚泥・洗浄排水処理系Bに区分される。浄水製造系Aは、主に着水井10と沈殿池12と砂濾過池14と処理水貯槽18とによって構成される。汚泥・洗浄排水処理系Bは、主に沈殿汚泥貯槽20と洗浄排水貯槽22と第1膜分離装置24と第2膜分離装置26と酸化手段28とによって構成される。   FIG. 1 is a system diagram showing an embodiment of a first water purification system according to the present invention. The water purification system is divided into a water purification production system A and a sludge / washing waste water treatment system B. The water purification production system A is mainly composed of a landing well 10, a sedimentation basin 12, a sand filtration basin 14, and a treated water storage tank 18. The sludge / washing waste water treatment system B is mainly composed of a precipitated sludge storage tank 20, a washing waste water storage tank 22, a first membrane separation device 24, a second membrane separation device 26, and an oxidizing means 28.

着水井10を経て沈殿池12へ供給された原水30に凝集剤32を添加することによって、原水30中の懸濁物質が凝集してフロックを形成する。これらのフロックは沈殿池12の底部に沈殿し、沈殿汚泥34として抜き出される。沈殿池12の上澄水36は後段の砂濾過池14に送られる。砂濾過池14では上澄水36に含まれる微細な懸濁物質を砂濾過し、処理水38とする。この砂濾過池14では上澄水36に含まれる溶解性の鉄やマンガンの除去作用もある。処理水38は処理水貯槽18に一旦貯えられた後に塩素系の消毒剤を添加されて、水道水42として配水される。   By adding the flocculant 32 to the raw water 30 supplied to the sedimentation basin 12 through the landing well 10, the suspended substances in the raw water 30 are aggregated to form a flock. These flocs settle at the bottom of the sedimentation basin 12 and are extracted as sedimentation sludge 34. The supernatant water 36 of the sedimentation basin 12 is sent to the subsequent sand filtration basin 14. In the sand filtration pond 14, fine suspended substances contained in the supernatant water 36 are sand-filtered to obtain treated water 38. The sand filtration pond 14 also has an action of removing soluble iron and manganese contained in the supernatant water 36. The treated water 38 is temporarily stored in the treated water storage tank 18, then added with a chlorine-based disinfectant and distributed as tap water 42.

砂濾過池14では長時間の運転によって、砂濾材の表面及びその間隙に微細な懸濁物質が付着、蓄積して目詰まりを起こす。このため、定期的に(例えば1日に1回程度の頻度)で砂濾材層の洗浄を行う。洗浄に使用する洗浄水44は処理水貯槽18に貯えた処理水を充当する。この砂濾過池14の洗浄操作によって多量の洗浄排水46が発生する。   In the sand filter pond 14, fine suspended substances adhere to and accumulate on the surface of the sand filter medium and the gaps between them for a long time, causing clogging. For this reason, the sand filter medium layer is periodically cleaned (for example, once a day). The cleaning water 44 used for cleaning is filled with the processing water stored in the processing water storage tank 18. A large amount of washing waste water 46 is generated by the washing operation of the sand filtration pond 14.

汚泥・洗浄排水処理系Bでは、前記沈殿池12の底部から抜き出した沈殿汚泥34と上記砂濾過池14の洗浄操作によって発生した洗浄排水46を処理する。すなわち、沈殿汚泥貯槽20には沈殿池12からの沈殿汚泥34が一時的に貯えられる。この沈殿汚泥貯槽20には後述する第2膜分離装置26からの濃縮液48が合流する。沈殿汚泥貯槽20に貯えられた沈殿汚泥34は第1膜分離装置24に送られ、膜分離を受ける。第1膜分離装置24としては特許文献2に開示されている回転平膜分離装置が好ましく用いられる。回転平膜分離装置は高価であるが過酷な条件でも安定した運転を長時間継続できる長所がある。したがって、沈殿汚泥34のように高濃度な汚泥の濃縮に好適である。また、背景技術の項で述べたように、沈殿汚泥34の発生量は原水量に対して1%未満と少量であるから、回転平膜分離装置を採用した際の費用負担もそれほど重荷にはならない。   In the sludge / washing wastewater treatment system B, the treated sludge 34 extracted from the bottom of the sedimentation basin 12 and the washing operation of the sand filtration basin 14 are treated. That is, the sedimentation sludge 34 from the sedimentation basin 12 is temporarily stored in the sedimentation sludge storage tank 20. A concentrated liquid 48 from the second membrane separation device 26 described later joins the sedimented sludge storage tank 20. The precipitated sludge 34 stored in the precipitated sludge storage tank 20 is sent to the first membrane separation device 24 and subjected to membrane separation. As the first membrane separation device 24, a rotating flat membrane separation device disclosed in Patent Document 2 is preferably used. Although the rotary flat membrane separator is expensive, it has an advantage that stable operation can be continued for a long time even under severe conditions. Therefore, it is suitable for the concentration of sludge having a high concentration like the precipitated sludge 34. In addition, as described in the background section, the amount of precipitated sludge 34 generated is as small as less than 1% of the amount of raw water, so the cost burden when adopting a rotary flat membrane separator is not so heavy. Don't be.

この第1膜分離装置24によって沈殿汚泥34は膜透過水50と濃縮汚泥52とに分離される。濃縮汚泥52は系外の処理設備に送られ、例えば脱水処理を受けた後に適当な手段によって処理処分される。一方、膜透過水50は酸化手段28に送られる。酸化手段28では膜透過水50に対して酸化処理が施される。酸化処理として例えば酸化剤54を添加する場合にはオゾンガスや次亜塩素酸ソーダ水溶液などを好ましく用いるが、これらの酸化剤に替えて空気を曝気することも可能である。   By the first membrane separation device 24, the precipitated sludge 34 is separated into the membrane permeated water 50 and the concentrated sludge 52. The concentrated sludge 52 is sent to a processing facility outside the system, for example, after being subjected to dehydration treatment, it is treated and disposed of by appropriate means. On the other hand, the membrane permeated water 50 is sent to the oxidizing means 28. In the oxidation means 28, the membrane permeated water 50 is oxidized. For example, ozone gas or sodium hypochlorite aqueous solution is preferably used in the case of adding the oxidizing agent 54 as the oxidizing treatment, but air can be aerated instead of these oxidizing agents.

膜透過水50を酸化処理する目的は、膜透過水50に溶存しているマンガンを酸化して、不溶性の酸化マンガンにすることにある。すなわち、本発明者の実験によれば膜透過水50には溶解性のマンガンが比較的多く、例えば1mg/L前後、含まれていることが判明した。この溶解性のマンガンは元々、河川や地下から取水した原水30に依拠するものである。前記沈殿池12での凝集剤32の添加によって溶解性のマンガンの一部は不溶化して除去されるが、大部分は溶解性のマンガンのままで残存する。また、上記不溶化したマンガンも不安定であり、沈殿汚泥貯槽20や第1膜分離装置24で長時間、嫌気条件下で滞留する過程で再溶出することも考えられる。したがって、酸化手段28では溶存マンガンの除去を目的として、膜透過水50を酸化処理し、溶存マンガンを酸化して、不溶性の酸化マンガンにする。酸化手段28としては上記した酸化剤54を添加する手段以外に、マンガン砂塔のような接触酸化式の手段を用いることができる。   The purpose of oxidizing the membrane permeated water 50 is to oxidize manganese dissolved in the membrane permeated water 50 into insoluble manganese oxide. That is, according to the experiment by the present inventor, it was found that the membrane permeate 50 contained a relatively large amount of soluble manganese, for example, around 1 mg / L. This soluble manganese originally relies on raw water 30 taken from rivers and underground. Although part of the soluble manganese is insolubilized and removed by the addition of the flocculant 32 in the settling basin 12, most of it remains as soluble manganese. The insolubilized manganese is also unstable and may be re-eluted in the process of staying in anaerobic conditions for a long time in the precipitated sludge storage tank 20 or the first membrane separation device 24. Therefore, the oxidation means 28 oxidizes the membrane permeated water 50 for the purpose of removing dissolved manganese, and oxidizes the dissolved manganese to form insoluble manganese oxide. As the oxidizing means 28, in addition to the means for adding the oxidizing agent 54, a catalytic oxidation type means such as a manganese sand tower can be used.

また、砂濾過池14の洗浄操作によって発生した洗浄排水46は洗浄排水貯槽22に貯えられる。洗浄排水は前記したように1日に1回程度の頻度で定期的に発生するが、その水量は原水量の5〜10%程度に相当する多大な量である。このため、洗浄排水貯槽22は1回の洗浄操作で発生する多量の洗浄排水46を一時的に貯留可能な容量を備える。そして、貯留した洗浄排水46を小出しに後段の第2膜分離装置26に供給し、次の洗浄操作までに洗浄排水貯槽22内の洗浄排水46がほぼなくなるような運転がなされる。この洗浄排水貯槽22に前記酸化手段28を経由した膜透過水50Aが投入され、膜透過水50Aは洗浄排水46に合流する。   Further, the cleaning wastewater 46 generated by the cleaning operation of the sand filtration pond 14 is stored in the cleaning wastewater storage tank 22. As described above, the washing wastewater is regularly generated at a frequency of about once a day, but the amount of water is a large amount corresponding to about 5 to 10% of the amount of raw water. For this reason, the cleaning waste water storage tank 22 has a capacity capable of temporarily storing a large amount of the cleaning waste water 46 generated by one cleaning operation. Then, the stored cleaning waste water 46 is supplied to the second membrane separation device 26 in the subsequent stage so that the cleaning waste water 46 in the cleaning waste water storage tank 22 is almost eliminated by the next cleaning operation. Membrane permeated water 50 </ b> A passing through the oxidizing means 28 is introduced into the washing drainage tank 22, and the membrane permeated water 50 </ b> A merges with the washing drainage 46.

洗浄排水46と膜透過水50Aが合流した合流水56は第2膜分離装置26に供給され、膜分離を受ける。この合流水56は比較的清澄であり、かつ水量が多い。このような合流水56を処理する第2膜分離装置26の膜モジュールとしては精密濾過膜からなる中空糸膜モジュール又は静置型浸漬平膜モジュールが好適である。第2膜分離装置26での膜分離によって、洗浄排水46中の微細懸濁物質及び膜透過水50A中の不溶性の酸化マンガンが分離された膜透過水58は清澄であり、溶解性のマンガンもほとんど含まず、砂濾過池14の処理水38と同等レベルの水質を維持している。したがって、膜透過水58は沈殿池12の入口側に還流させることなく、直接に砂濾過池14の処理水38に合流させる。微細懸濁物質及び不溶性の酸化マンガンを含む第2膜分離装置26での濃縮液48は前記したように沈殿汚泥貯槽20に導き、沈殿汚泥34と合流させて第1膜分離装置24での膜分離を受ける。したがって、第1膜分離装置24から排出される濃縮汚泥52には沈殿池12で凝集沈殿させた沈殿物、砂濾過池14の洗浄操作で分離された微細懸濁物、酸化手段28での酸化処理によって生成した不溶性の酸化マンガンなど本浄化システムで発生したすべての固形物が集合されて含まれる。   The combined water 56 in which the washing waste water 46 and the membrane permeated water 50A merge is supplied to the second membrane separation device 26 and subjected to membrane separation. This combined water 56 is relatively clear and has a large amount of water. As the membrane module of the second membrane separation device 26 for treating such combined water 56, a hollow fiber membrane module made of a microfiltration membrane or a stationary immersion flat membrane module is suitable. The membrane permeated water 58 from which the fine suspended solids in the washing waste water 46 and the insoluble manganese oxide in the membrane permeated water 50A are separated by the membrane separation in the second membrane separation device 26 is clear, and soluble manganese is also dissolved. The water quality is almost the same as that of the treated water 38 of the sand filter pond 14. Therefore, the membrane permeated water 58 is directly joined to the treated water 38 of the sand filtration basin 14 without being refluxed to the inlet side of the sedimentation basin 12. As described above, the concentrate 48 in the second membrane separation device 26 containing fine suspended solids and insoluble manganese oxide is guided to the sedimentation sludge storage tank 20 and merged with the sedimentation sludge 34 to form a membrane in the first membrane separation device 24. Get separated. Therefore, the concentrated sludge 52 discharged from the first membrane separation device 24 includes the precipitate coagulated and settled in the sedimentation basin 12, the fine suspension separated by the washing operation of the sand filtration basin 14, and the oxidation in the oxidation means 28. All solids generated by this purification system, such as insoluble manganese oxide produced by the treatment, are collected and included.

上述のとおり、本発明に係る第1の浄水システムの実施形態によれば、沈殿汚泥34や洗浄排水46を膜分離して最終的に得られた膜透過水58は清澄であり、溶解性のマンガンもほとんど含まず、砂濾過池14の処理水38と同等レベルの水質を維持している。したがって、膜透過水58を沈殿池12の入口側に還流させることなく、直接に砂濾過池14の処理水38に合流させることができる。このため、沈殿池及び砂濾過池の処理負荷を増大させず、かつ、処理水中の溶解性のマンガン濃度を低く抑えることができる。   As described above, according to the embodiment of the first water purification system of the present invention, the membrane permeated water 58 finally obtained by membrane separation of the precipitated sludge 34 and the washing waste water 46 is clear and soluble. Manganese is hardly contained, and the water quality is maintained at the same level as the treated water 38 of the sand filtration pond 14. Therefore, the membrane permeated water 58 can be directly merged with the treated water 38 of the sand filtration basin 14 without returning to the inlet side of the sedimentation basin 12. For this reason, the processing load of a sedimentation basin and a sand filtration pond is not increased, and the soluble manganese concentration in treated water can be kept low.

図2は本発明に係る第2の浄水システムの実施形態を示す系統図である。図2において、図1と同一の符号を付した要素は上記第1の浄水システムで説明した要素と実質的に同一であるので、その説明を省略する。この実施形態は上記第1の浄水システムに係る酸化手段28を省略した構成であり、第1膜分離装置24の膜透過水50を沈殿池12の入口側である着水井10に返送するようにしている。この膜透過水50は清澄であるが前記したように溶解性のマンガンが比較的多く、例えば1mg/L前後、含まれている。ただし、膜透過水50の水量は前記したように原水量に対して多くとも1%未満である。したがって、このような清澄かつ少量の膜透過水50を着水井10に返送し、原水30に混合しても、沈殿池12及び砂濾過池14の処理負荷は殆んど増大しない。また、膜透過水50に含まれる溶解性のマンガンは沈殿池12での凝集沈殿や砂濾過池14での砂濾過を受ける過程でその大部分が除去される。すなわち、膜透過水50を原水30に混合したことによる悪影響は無視できるレベルである。この第2の浄水システムによれば、前記第1の浄水システムと同様に、沈殿池12及び砂濾過池14の処理負荷を量的に殆んど増大させず、かつ、処理水38中の溶解性のマンガン濃度を低く抑えることができる。この第2の浄水システムの実施形態によれば、前記第1の浄水システムに比べシステムの簡略化を図ることができる。なお、第2の浄水システムでは膜透過水50の酸化処理を完全に排除することを意図するものではなく、膜透過水50を酸化処理した後に沈殿池12の入口側に返送する形態をも含む。   FIG. 2 is a system diagram showing an embodiment of a second water purification system according to the present invention. In FIG. 2, since the element which attached | subjected the code | symbol same as FIG. 1 is substantially the same as the element demonstrated by the said 1st water purification system, the description is abbreviate | omitted. In this embodiment, the oxidation means 28 according to the first water purification system is omitted, and the membrane permeated water 50 of the first membrane separation device 24 is returned to the landing well 10 which is the inlet side of the settling basin 12. ing. The membrane permeated water 50 is clear but contains a relatively large amount of soluble manganese as described above, and is contained, for example, at around 1 mg / L. However, the amount of the membrane permeate 50 is less than 1% at most with respect to the amount of raw water as described above. Therefore, even if such a clear and small amount of membrane permeated water 50 is returned to the landing well 10 and mixed with the raw water 30, the processing load of the sedimentation basin 12 and the sand filtration basin 14 is hardly increased. Further, most of the soluble manganese contained in the membrane permeated water 50 is removed in the process of undergoing coagulation sedimentation in the sedimentation basin 12 and sand filtration in the sand filtration basin 14. That is, the adverse effect caused by mixing the membrane permeated water 50 with the raw water 30 is at a negligible level. According to the second water purification system, as in the first water purification system, the treatment load of the settling basin 12 and the sand filtration basin 14 is hardly increased in quantity, and the dissolution in the treated water 38 is performed. The manganese concentration can be kept low. According to the embodiment of the second water purification system, the system can be simplified as compared with the first water purification system. Note that the second water purification system does not intend to completely eliminate the oxidation treatment of the membrane permeated water 50, and includes a mode in which the membrane permeated water 50 is returned to the inlet side of the settling basin 12 after being oxidized. .

前記各実施形態では、第2膜分離装置26で膜分離された濃縮液48を沈殿汚泥34に合流し、第1膜分離装置24によって再度、膜分離する構成であった。しかしながら、本発明はこのような構成に限定されるものではなく、濃縮液48を沈殿汚泥34に合流させずに独立して抜き出し、第1膜分離装置24の濃縮汚泥52と併行して系外の処理設備に送るようにしてもよい。   In each of the above-described embodiments, the concentrated solution 48 separated by the second membrane separation device 26 is joined to the precipitated sludge 34 and subjected to membrane separation again by the first membrane separation device 24. However, the present invention is not limited to such a configuration, and the concentrated liquid 48 is independently extracted without being combined with the precipitated sludge 34, and is combined with the concentrated sludge 52 of the first membrane separation device 24. You may make it send to the processing facility.

本発明に係る第1の浄水システムの実施形態を示す系統図である。It is a distribution diagram showing an embodiment of the 1st water purification system concerning the present invention. 本発明に係る第2の浄水システムの実施形態を示す系統図である。It is a distribution diagram showing an embodiment of the 2nd water purification system concerning the present invention.

符号の説明Explanation of symbols

10………着水井、12………沈殿池、14………砂濾過池、16………活性炭吸着池、18………処理水貯槽、20………沈殿汚泥貯槽、22………洗浄排水貯槽、24………第1膜分離装置、26………第2膜分離装置、28………酸化手段、30………原水、32………凝集剤、34………沈殿汚泥、36………上澄水、38………処理水、40………処理水、42………水道水、44………洗浄水、46………洗浄排水、48………濃縮液、50………(第1膜分離装置の)膜透過水、52………濃縮汚泥、54………酸化剤、56………合流水、58………(第2膜分離装置の)膜透過水。   10 ... …… Acquisition well, 12 ......... Sedimentation basin, 14 ......... Sand filtration pond, 16 ......... Activated carbon adsorption pond, 18 ......... Treatment water storage tank, 20 ......... Sedimentation sludge storage tank, 22 ......... Washing drainage tank, 24 ......... first membrane separator, 26 ......... second membrane separator, 28 ......... oxidation means, 30 ......... raw water, 32 ......... flocculant, 34 ......... settling sludge 36 ......... Supernatant water, 38 ......... Treatment water, 40 ......... Treatment water, 42 ......... Tap water, 44 ......... Wash water, 46 ......... Wash water, 48 ......... Concentrate, 50 ......... Membrane permeated water (of the first membrane separator), 52 ......... Concentrated sludge, 54 ......... Oxidant, 56 ......... Mixed water, 58 ......... Membrane (of the second membrane separator) Permeated water.

Claims (3)

原水中の懸濁物質を沈殿汚泥として分離する沈殿池と、前記沈殿池の上澄水を砂濾過して処理水とする砂濾過池と、前記沈殿池から抜き出した沈殿汚泥を膜分離する第1膜分離装置と、前記砂濾過池の洗浄排水を膜分離する第2膜分離装置と、前記第1膜分離装置の膜透過水を酸化処理する酸化手段と、前記酸化手段によって酸化処理された前記膜透過水を前記洗浄排水に合流させる手段と、前記第2膜分離装置の膜透過水を前記処理水に合流させる手段とを具備したことを特徴とする浄水システム。   A sedimentation basin that separates suspended matter in raw water as sedimentation sludge, a sand filtration pond that uses sand filtration of the supernatant water of the sedimentation basin, and a first membrane separation that membrane-separates the sedimentation sludge extracted from the sedimentation basin An apparatus, a second membrane separation device for membrane-separating washing wastewater from the sand filtration pond, an oxidation means for oxidizing the membrane permeated water of the first membrane separation device, and the membrane permeation oxidized by the oxidation means A water purification system comprising means for joining water to the washing waste water and means for joining membrane permeated water of the second membrane separation device to the treated water. 原水中の懸濁物質を沈殿汚泥として分離する沈殿池と、前記沈殿池の上澄水を砂濾過して処理水とする砂濾過池と、前記沈殿池から抜き出した沈殿汚泥を膜分離する第1膜分離装置と、前記砂濾過池の洗浄排水を膜分離する第2膜分離装置と、前記第1膜分離装置の膜透過水を前記沈殿池の入口側に返送する手段と、前記第2膜分離装置の膜透過水を前記処理水に合流させる手段とを具備したことを特徴とする浄水システム。   A sedimentation basin that separates suspended matter in raw water as sedimentation sludge, a sand filtration pond that uses sand filtration of the supernatant water of the sedimentation basin as treated water, and a first membrane separation that membrane-separates the sedimentation sludge extracted from the sedimentation basin An apparatus, a second membrane separation device for membrane separation of the waste water from the sand filtration pond, a means for returning the membrane permeated water of the first membrane separation device to the inlet side of the settling basin, and the second membrane separation device And a means for merging the membrane permeated water with the treated water. 前記第2膜分離装置で膜分離された濃縮液を前記沈殿汚泥に合流させる手段を具備したことを特徴とする請求項1又は請求項2に記載の浄水システム。   3. The water purification system according to claim 1, further comprising means for merging the concentrated solution separated by the second membrane separation device with the precipitated sludge. 4.
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JP2006224010A (en) * 2005-02-18 2006-08-31 Hitachi Ltd Operation control method of water purification process
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