JP7034897B2 - Wastewater treatment method - Google Patents

Wastewater treatment method Download PDF

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JP7034897B2
JP7034897B2 JP2018230793A JP2018230793A JP7034897B2 JP 7034897 B2 JP7034897 B2 JP 7034897B2 JP 2018230793 A JP2018230793 A JP 2018230793A JP 2018230793 A JP2018230793 A JP 2018230793A JP 7034897 B2 JP7034897 B2 JP 7034897B2
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tubular
membrane
wastewater treatment
water
treatment method
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JP2019107645A (en
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修志 中塚
敏充 浜田
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Daicen Membrane Systems Ltd
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Daicen Membrane Systems Ltd
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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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

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  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Description

本発明は、工場排水などの各種排水から水と固形分を分離して、最終的に乾燥した固形分のみを廃棄することができる排水処理方法に関する。 The present invention relates to a wastewater treatment method capable of separating water and solids from various wastewaters such as factory wastewater and finally discarding only the dried solids.

各種装置を使用して工場排水を処理するとき、工場排水から一部水を回収して再利用する一方で、残部の水は下水に流したり、最終的には水を生物処理するなどして河川に流したりしている。
しかし最近では、世界的にも液体排出量をゼロとするという考え方（ＺＬＤ: Zero Liquid Discharge）が採用されており、そのための処理装置や処理方法の発明が提案されている（特許文献１～７）。 When treating factory wastewater using various devices, some water is recovered from the factory wastewater and reused, while the remaining water is drained into sewage and finally the water is biologically treated. It is drained into a river.
However, recently, the idea of zero liquid discharge (ZLD: Zero Liquid Discharge) has been adopted worldwide, and inventions of treatment devices and treatment methods for that purpose have been proposed (Patent Documents 1 to 7). ).

特表２００９－５３０１００号公報Special Table 2009-530100 Gazette 特表２０１０－５１７７４６号公報Special Table 2010-571746 Gazette 特表２０１３－５００１５７号公報Special Table 2013-500157 Gazette 特表２０１４－５１２９５２号公報Japanese Patent Publication No. 2014-512952 特開２０１６－１１２５５９号公報Japanese Unexamined Patent Publication No. 2016-11259 特表２０１６－５０６８６７号公報Special Table 2016-50686 No. 特表２０１７－５３３８１５号公報Special Table 2017-533815 Gazette

本発明は、上記のＺＬＤを実施することができる排水処理方法を提供することを課題とする。 An object of the present invention is to provide a wastewater treatment method capable of carrying out the above-mentioned ZLD.

本発明は、排水処理において水分を回収し、最終的に乾燥された固形分のみを廃棄又は再利用する排水処理方法であって、管状ＲＯ膜による処理工程を有している排水処理方法を提供する。 The present invention provides a wastewater treatment method in which water is recovered in wastewater treatment and only the finally dried solid content is discarded or reused, and the wastewater treatment method includes a treatment step using a tubular RO membrane. do.

本発明の排水処理方法によれば、排水処理をしたとき、実質的に排水中の全ての水分を回収して、最終的には乾燥した固形分のみを廃棄又は再利用することができる。 According to the wastewater treatment method of the present invention, when the wastewater is treated, substantially all the water in the wastewater can be recovered, and finally only the dried solid content can be discarded or reused.

管状ＲＯ膜エレメントの斜視図。Perspective view of tubular RO membrane element. 管状ＲＯ膜エレメント集合体の平面図。但し、一部を省略して示している。Top view of tubular RO membrane element assembly. However, some parts are omitted. 管状ＲＯ膜モジュールの斜視図。但し、実際には見えない内部が見えるように示している。Perspective view of the tubular RO membrane module. However, it is shown so that the inside that cannot be actually seen can be seen. 実施例で用いた排水処理装置の概略図Schematic diagram of the wastewater treatment equipment used in the examples

本発明の排水処理方法はＺＬＤを実施できるものであり、水分を回収し、最終的に乾燥した固形分のみを廃棄又は再利用する方法である。
本発明の排水処理方法は、管状ＲＯ（逆浸透）膜による処理工程を有しており、必要に応じて、前記管状ＲＯ膜による処理工程の前に前処理工程を、前記管状ＲＯ膜による処理工程の後に蒸発工程または分離工程を付加することができる。 The wastewater treatment method of the present invention can carry out ZLD, and is a method of recovering water and finally discarding or reusing only the dried solid content.
The wastewater treatment method of the present invention includes a treatment step using a tubular RO (reverse osmosis) membrane, and if necessary, a pretreatment step is performed before the treatment step using the tubular RO membrane, and the treatment with the tubular RO membrane is performed. An evaporation step or a separation step can be added after the step.

＜管状ＲＯ膜＞
本発明の排水処理方法で使用する管状ＲＯ膜エレメント１０は、図１に示すとおり、多孔支持管１１内に管状ＲＯ膜１２が配置されているものである。
多孔支持管１１は、合成樹脂（好ましくは繊維強化樹脂）または金属（好ましくはステンレス）からなるものであり、厚さ方向に貫通された多数の孔１３が分散配置されている。
管状ＲＯ膜１２は、不織布、紙などからなる支持管の内側にＲＯ膜が形成されたものでもよい。
ＲＯ膜の材質は、特に限定されなく、セルロースアセテート、芳香族ポリアミド、及びスルホン化ポリエーテルスルホンなどが挙げられ、これらは１種又は２種以上を用いることができる。
ＲＯ膜の材質は、ファウリング防止の観点から、セルロースアセテート及びスルホン化ポリエーテルスルホンから選ばれる１種以上が好ましい。
管状ＲＯ膜１２の内径は、被処理水の濃度（固形分濃度）に応じて調整することができるものであり、例えば５～１５ｍｍの範囲にすることができる。
管状ＲＯ膜１２は、排水の流路が大きいため膜が閉塞し難く、排水の流入が膜面閉塞物を剥離する方向に流れているため、排水の高濃度濃縮に適している。 <Tubular RO membrane>
As shown in FIG. 1, the tubular RO membrane element 10 used in the wastewater treatment method of the present invention has the tubular RO membrane 12 arranged in the porous support tube 11.
The porous support tube 11 is made of a synthetic resin (preferably fiber reinforced resin) or a metal (preferably stainless steel), and a large number of holes 13 penetrating in the thickness direction are dispersedly arranged.
The tubular RO film 12 may have an RO film formed inside a support tube made of a non-woven fabric, paper, or the like.
The material of the RO membrane is not particularly limited, and examples thereof include cellulose acetate, aromatic polyamide, and sulfonated polyether sulfone, and one or more of these can be used.
The material of the RO membrane is preferably one or more selected from cellulose acetate and sulfonated polyether sulfone from the viewpoint of preventing fouling.
The inner diameter of the tubular RO membrane 12 can be adjusted according to the concentration (solid content concentration) of the water to be treated, and can be, for example, in the range of 5 to 15 mm.
The tubular RO membrane 12 is suitable for high-concentration concentration of drainage because the drainage flow path is large and the membrane is difficult to block, and the inflow of drainage flows in the direction of peeling the membrane surface blockage.

管状ＲＯ膜は、図２に示すとおり、複数本の管状ＲＯ膜エレメント１０が連結されて１本になった管状ＲＯ膜集合体２０が好ましい。例えば、管状ＲＯ膜は、合成樹脂または金属からなる多孔支持管１１内にチューブ状のＲＯ膜が配置された管状ＲＯ膜エレメント１０が複数組み合わされたものであり、前記ＲＯ膜がセルロースアセテート、芳香族ポリアミド、及びスルホン化ポリエーテルスルホンから選ばれる１種以上のものを用いることができる。
図２に示す管状ＲＯ膜集合体２０では、並列配置された管状ＲＯ膜エレメント１０のうち、隣接する管状ＲＯ膜エレメント１０同士がＵ字管２１で連結されているものである。Ｕ字管２１に代えて他の連結方法を使用することもできる。
管状ＲＯ膜集合体２０の第１端開口部２０ａには原水供給部２３が接続され、反対側の第２端開口部２０ｂには濃縮水排水部２４が接続されている。
管状ＲＯ膜集合体２０は、例えば、１０～２０本の管状ＲＯ膜エレメント１０からなるものにすることができる。 As shown in FIG. 2, the tubular RO membrane is preferably a tubular RO membrane aggregate 20 in which a plurality of tubular RO membrane elements 10 are connected to form a single tubular RO membrane. For example, the tubular RO membrane is a combination of a plurality of tubular RO membrane elements 10 in which a tubular RO membrane is arranged in a porous support tube 11 made of synthetic resin or metal, and the RO membrane is cellulose acetate and fragrance. One or more selected from group polyamide and sulfonated polyether sulfone can be used.
In the tubular RO membrane assembly 20 shown in FIG. 2, among the tubular RO membrane elements 10 arranged in parallel, adjacent tubular RO membrane elements 10 are connected to each other by a U-shaped tube 21. Other connecting methods can be used instead of the U-shaped tube 21.
The raw water supply unit 23 is connected to the first end opening 20a of the tubular RO membrane assembly 20, and the concentrated water drainage unit 24 is connected to the second end opening 20b on the opposite side.
The tubular RO membrane assembly 20 can be made up of, for example, 10 to 20 tubular RO membrane elements 10.

本発明の排水処理で使用する管状ＲＯ膜は、図３に示すように、筒状のケーシング３１内に複数本の前記管状ＲＯ膜エレメント１０が配置された管状ＲＯ膜モジュールであって、前記複数本の管状ＲＯ膜エレメント１０が、それぞれの開口部同士が接続され、全体として１本の管状ＲＯ膜エレメント（管状ＲＯ膜集合体２０）になっている管状ＲＯ膜モジュール３０が好ましい。
管状ＲＯ膜モジュール３０は、両端面（第１端面３２と第２端面３３）が閉塞された筒状のケーシング３１内に管状ＲＯ膜集合体２０が巻き込まれて円柱状になった形態で収容されているものである。
筒状のケーシング３１の第１端面３２には、管状ＲＯ膜集合体２０の原水供給部２３と濃縮水排水部２４が突き出されている。
筒状ハウジング３１の側面３４からは、透過水出口部２５が突き出されており、さらに図示していない通気孔が形成されている。
管状ＲＯ膜モジュール３０は、１または複数を組み合わせて使用することができる。 As shown in FIG. 3, the tubular RO membrane used in the wastewater treatment of the present invention is a tubular RO membrane module in which a plurality of the tubular RO membrane elements 10 are arranged in a tubular casing 31, and the plurality. A tubular RO membrane module 30 in which the tubular RO membrane elements 10 of the book are connected to each other to form one tubular RO membrane element (tubular RO membrane aggregate 20) as a whole is preferable.
The tubular RO membrane module 30 is housed in a cylindrical shape in which the tubular RO membrane aggregate 20 is caught in a tubular casing 31 in which both end faces (first end face 32 and second end face 33) are closed. Is what you are doing.
The raw water supply portion 23 and the concentrated water drainage portion 24 of the tubular RO membrane aggregate 20 are projected from the first end surface 32 of the tubular casing 31.
A permeation water outlet portion 25 protrudes from the side surface 34 of the tubular housing 31, and a ventilation hole (not shown) is further formed.
The tubular RO membrane module 30 can be used alone or in combination of two or more.

管状ＲＯ膜モジュールとしては、次のものを使用することができる。
管状ＲＯ膜エレメント１０：図１に示すような、内径１１．５ｍｍの管状ポリエステル不織布支持体の管内表面に０．２ｍｍの酢酸セルロース逆浸透膜を積層させた長さ２,５００ｍｍのもの。
管状膜エレメント集合体２０：図２に示すとおり、Ｕ字管２１を使用して、管状膜エレメント１０の１８本を直列に接続して１本にしたもの。
管状膜モジュール３０：図３に示すもの。 The following can be used as the tubular RO membrane module.
Tubular RO membrane element 10: As shown in FIG. 1, a tubular polyester non-woven fabric support having an inner diameter of 11.5 mm and a length of 2,500 mm in which a 0.2 mm cellulose acetate reverse osmosis membrane is laminated on the inner surface of the tube.
Tubular membrane element assembly 20: As shown in FIG. 2, 18 tubular membrane elements 10 are connected in series to form one by using a U-shaped tube 21.
Tubular membrane module 30: as shown in FIG.

＜排水処理方法＞
次に、管状ＲＯ膜を使用した排水処理方法を説明する。
本発明の排水処理方法は、例えば、図３に示す管状ＲＯ膜モジュール３０などの管状ＲＯ膜のみを使用して排水処理を実施することができる。このとき、管状ＲＯ膜モジュール３０を複数使用することもできる。
管状ＲＯ膜モジュール３０を複数使用するときは、幹管と、前記幹管から分岐された複数の枝管の組み合わせを使用することができる。
例えば、前記原水タンクと第１幹管を接続し、複数の第１枝管と複数の管状ＲＯ膜モジュール３０の原水供給部２３を接続して原水を供給し、管状ＲＯ膜モジュール３０の複数の濃縮水排出部２４と複数の第２枝管を接続し、前記第２枝管で集めた濃縮水は、第２幹管を経て原水タンクに戻し、これを繰り返すことができる。
透過水は、複数の透過水出口２５と複数の第３枝管を接続し、前記第３枝管で集めた透過水は第３幹管を経て、透過水タンクに貯水して回収される。また透過水は再利用することができる。 <Wastewater treatment method>
Next, a wastewater treatment method using a tubular RO membrane will be described.
In the wastewater treatment method of the present invention, for example, wastewater treatment can be carried out using only a tubular RO membrane such as the tubular RO membrane module 30 shown in FIG. At this time, a plurality of tubular RO membrane modules 30 can also be used.
When a plurality of tubular RO membrane modules 30 are used, a combination of a trunk tube and a plurality of branch tubes branched from the trunk tube can be used.
For example, the raw water tank and the first trunk pipe are connected, the plurality of first branch pipes and the raw water supply units 23 of the plurality of tubular RO membrane modules 30 are connected to supply raw water, and a plurality of tubular RO membrane modules 30 are supplied. The concentrated water discharge unit 24 is connected to a plurality of second branch pipes, and the concentrated water collected by the second branch pipe is returned to the raw water tank via the second main pipe, and this can be repeated.
The permeated water connects a plurality of permeated water outlets 25 and a plurality of third branch pipes, and the permeated water collected by the third branch pipe is stored in a permeated water tank through the third trunk pipe and collected. In addition, the permeated water can be reused.

本発明の排水処理は、前処理工程と管状ＲＯ膜による処理工程を組み合わせて実施することもできる。
前処理工程は特に制限されるものではなく、公知の水処理工程で汎用されている処理方法を実施することができる。公知の前処理工程としては、活性炭処理工程、軟水化処理工程、ＭＦ膜処理工程、ＮＦ膜処理工程、ＵＦ膜処理工程、凝集沈殿処理工程などを挙げることができる。 The wastewater treatment of the present invention can also be carried out by combining a pretreatment step and a treatment step using a tubular RO membrane.
The pretreatment step is not particularly limited, and a treatment method widely used in known water treatment steps can be implemented. Examples of known pretreatment steps include an activated carbon treatment step, a water softening treatment step, an MF membrane treatment step, an NF membrane treatment step, a UF membrane treatment step, and a coagulation sedimentation treatment step.

本発明の排水処理方法では、前処理工程としてスパイラルＲＯ膜による処理工程を含むことが好ましく、前処理工程がスパイラルＲＯ膜による処理工程のみからなるものでもよい。
スパイラルＲＯ膜による処理工程は、公知のスパイラルＲＯ膜モジュールを使用した処理工程であり、前記スパイラルＲＯ膜モジュールは１または複数を組み合わせて使用することもできる。 In the wastewater treatment method of the present invention, it is preferable that the pretreatment step includes a treatment step using a spiral RO membrane, and the pretreatment step may consist only of a treatment step using a spiral RO membrane.
The treatment step using the spiral RO membrane is a treatment step using a known spiral RO membrane module, and the spiral RO membrane module may be used alone or in combination of two or more.

本発明の排水処理方法の一実施形態を図１～図３により説明する。
ポンプを使用して、原水タンクから管状ＲＯ膜モジュール３０の原水供給部２３に原水を供給する。
原水供給部２３から供給した原水は、管状ＲＯ膜集合体２０を通過する過程でろ過され、透過液は管状ＲＯ膜エレメント１０の多孔支持管１１に形成されている孔１３からケーシング３１内に排出される。
ケーシング３１内に排出した透過水は、透過水出口部２５から排出した後、回収して再利用する。
管状ＲＯ膜集合体２０内でろ過した後の濃縮水は、濃縮水排出部２４から排出した後、原水タンクに戻す。
このろ過運転を繰り返すことで濃縮水中の固形分濃度を高めることができる。
本発明の排水処理方法では、原水をスパイラルＲＯ膜でろ過処理することで固形分濃度が高められた一次処理水を管状ＲＯ膜モジュール３０で処理すると、より固形分濃度が高められるので好ましい。
本発明の管状ＲＯ膜を使用する排水処理方法では、原水の種類により異なるが、例えば、原水の固形分濃度を１．０質量％以上、好ましくは１０質量％以上、さらに好ましくは２０質量％以上、さらに好ましくは３０質量％以上、最も好ましくは５０質量％以上にまで高めることができる。 An embodiment of the wastewater treatment method of the present invention will be described with reference to FIGS. 1 to 3.
A pump is used to supply raw water from the raw water tank to the raw water supply unit 23 of the tubular RO membrane module 30.
The raw water supplied from the raw water supply unit 23 is filtered in the process of passing through the tubular RO membrane aggregate 20, and the permeate is discharged into the casing 31 from the hole 13 formed in the porous support pipe 11 of the tubular RO membrane element 10. Will be done.
The permeated water discharged into the casing 31 is discharged from the permeated water outlet portion 25, and then collected and reused.
The concentrated water after filtering in the tubular RO membrane aggregate 20 is discharged from the concentrated water discharge unit 24 and then returned to the raw water tank.
By repeating this filtration operation, the solid content concentration in the concentrated water can be increased.
In the wastewater treatment method of the present invention, it is preferable to treat the primary treated water whose solid content concentration has been increased by filtering the raw water with a spiral RO membrane with the tubular RO membrane module 30 because the solid content concentration is further increased.
The wastewater treatment method using the tubular RO membrane of the present invention varies depending on the type of raw water, but for example, the solid content concentration of the raw water is 1.0% by mass or more, preferably 10% by mass or more, and more preferably 20% by mass or more. , More preferably, it can be increased to 30% by mass or more, and most preferably to 50% by mass or more.

本発明の排水処理方法は、管状ＲＯ膜による処理工程の後、被処理水中の水分を蒸発させて回収し、固形分と分離する蒸発工程または処理液を冷却し結晶化物を遠心分離器やフィルタープレス装置によって回収する分離工程を実施する。蒸発工程は既存の蒸発装置、乾燥装置が使用できる。結晶化装置及び篩分・分離装置も既存の装置を使用できる。また、管状ＲＯ膜による処理工程の前後で、攪拌・振動等の運動エネルギー、熱エネルギー、電気・磁気・光エネルギーなどによる析出・造粒工程を実施することもできる。 In the wastewater treatment method of the present invention, after the treatment step using the tubular RO membrane, the moisture in the water to be treated is evaporated and recovered, and the evaporation step for separating from the solid content or the treatment liquid is cooled to centrifuge the crystallized product into a centrifuge or filter. A separation process of collecting by a press device is carried out. The existing evaporation device and drying device can be used for the evaporation step. Existing equipment can also be used for the crystallization device and the sieving / separating device. Further, before and after the treatment step using the tubular RO film, it is also possible to carry out the precipitation / granulation step by kinetic energy such as stirring / vibration, thermal energy, electric / magnetic / optical energy and the like.

蒸発工程は、各種の汚泥乾燥機が使用できるが、特に乾燥効率が高い間接加熱型汚泥乾燥機の使用が好ましい。
間接加熱型汚泥乾燥機は、直接加熱型汚泥乾燥機と比べ省エネルギーだけでなく、据付設置面積が少ない、排気ガス量が少ない、水分調整が容易などの長所がある。
間接加熱型汚泥乾燥機としては、ドラム型乾燥機、製紙用シリンダー乾燥機などと呼ばれる乾燥機が挙げられ、具体的には西村鐵工所製ＣＤドライヤー、月島製作所製インクラインドディスクドライヤー、大和三光製作所製タコロータリー乾燥機、ウェッジスタイルドライヤー、攪拌ロータリー乾燥機、西村鐵工所製ＣＤドライヤーへ大川原製作所製のヒートポンプシステムを組み込んだ直接加圧型ヒートポンプ式濃縮乾燥機H-VCDドライヤーなどが挙げられる。
西村鐵工所製ＣＤドライヤーは、伝熱面として円筒ドラムの外周面でなく、内部に空洞を有する独自の中空円盤（ＣＤ：コンパクトディスク）の両面を使うことで熱通過係数を高めたものである。 Various sludge dryers can be used in the evaporation step, but it is particularly preferable to use an indirect heating type sludge dryer having high drying efficiency.
The indirect heating type sludge dryer has advantages such as energy saving as compared with the direct heating type sludge dryer, a small installation area, a small amount of exhaust gas, and easy moisture adjustment.
Examples of the indirect heating type sludge dryer include a drum type dryer, a dryer called a paper cylinder dryer, and specifically, a CD dryer manufactured by Nishimura Iron Works, an inclined disc dryer manufactured by Tsukishima Seisakusho, and Sanko Yamato. Examples include a direct pressure type heat pump type concentration dryer H-VCD dryer that incorporates a heat pump system manufactured by Okawara Seisakusho into a taco rotary dryer manufactured by Seisakusho, a wedge style dryer, a stirring rotary dryer, and a CD dryer manufactured by Nishimura Iron Works.
Nishimura Works Co., Ltd.'s CD dryer has an increased heat transfer coefficient by using both sides of a unique hollow disk (CD: compact disc) that has a cavity inside, not the outer peripheral surface of the cylindrical drum as the heat transfer surface. be.

蒸発工程は、固形化する物質の性質や有用性から常圧または加圧・減圧下で実施できる。
常圧での蒸発工程の処理は、管状ＲＯ膜による処理水を１００℃で蒸発処理したとき、水分の発生が１０～１０，０００mL／min以下、好ましくは１０～１，０００mL／min以下となったときを終了として、そのときの蒸発残渣が「乾燥された固形分」となる。「乾燥された固形分」とは、固形物としての取り扱いが可能であれば良く、少量の水分を含んでいてもよい。
水分の発生が１０～１０，０００mL／min以下（好ましくは１０～１，０００mL／min以下）となった場合には、水分が滴り落ちることなく、実質的に固形物として取扱いが可能になり、さらにその後に回収される水分もごく少量であることと、回収される水分量と蒸発に使用するエネルギー量を考慮すると、さらに蒸発工程を継続することは運転コストの削減とＣＯ２量の削減の観点からも好ましくない。 The evaporation step can be carried out under normal pressure or pressurized / reduced pressure due to the nature and usefulness of the solidified substance.
In the treatment of the evaporation step under normal pressure, when the treated water by the tubular RO membrane is evaporated at 100 ° C., the generation of water is 10 to 10,000 mL / min or less, preferably 10 to 1,000 mL / min or less. The evaporation residue at that time becomes the "dried solid content". The "dried solid content" may be any material as long as it can be handled as a solid substance, and may contain a small amount of water.
When the generation of water is 10 to 10,000 mL / min or less (preferably 10 to 1,000 mL / min or less), the water does not drip and can be treated as a substantially solid substance. Furthermore, considering that the amount of water recovered after that is very small, and the amount of water recovered and the amount of energy used for evaporation, continuing the evaporation process further reduces operating costs and CO 2 content. It is also not preferable from the viewpoint.

乾燥された固形分（汚泥）は廃棄又は再利用することができる。前記固形分中に、例えば貴金属などの有価物が含まれている場合には回収して再利用することができる。また乾燥された固形分（汚泥）は、大和三光製作所製ボルテックス乾燥焼却装置などを使用して、バイオ燃料として使用することもできる。
本発明の排水処理方法では、管状ＲＯ膜を使用するろ過工程の処理により被処理水中の固形分濃度が高められているため、蒸発工程における使用エネルギー量および処理時間を削減できるようになる。 The dried solids (sludge) can be discarded or reused. When the solid content contains valuable resources such as precious metals, it can be recovered and reused. The dried solid content (sludge) can also be used as a biofuel by using a vortex drying incinerator manufactured by Yamato Sanko Seisakusho.
In the wastewater treatment method of the present invention, the solid content concentration in the water to be treated is increased by the treatment in the filtration step using the tubular RO membrane, so that the amount of energy used in the evaporation step and the treatment time can be reduced.

前処理工程、管状ＲＯ膜による処理工程、及び乾燥工程において、本発明の排水処理を円滑に行う観点から、被処理水中へ消泡剤などの添加剤を、一括添加、又は逐次添加してもよい。 From the viewpoint of smoothly performing the wastewater treatment of the present invention in the pretreatment step, the treatment step using the tubular RO membrane, and the drying step, even if an additive such as a defoaming agent is added collectively or sequentially to the water to be treated. good.

本発明の排水処理方法は、各種技術分野における排水処理においてＺＬＤ（Zero LiquidDischarge）を適用する場合に好適である。
排水源は特に制限されるものではないが、発電所、海水淡水化施設などのエネルギー施設や造船・自動車・家電製品等の製造工場、切削部品加工工場、塗装工場、染色工場、食品工場、製紙工場などの工場などを挙げることができる。 The wastewater treatment method of the present invention is suitable for applying ZLD (Zero Liquid Discharge) in wastewater treatment in various technical fields.
The drainage source is not particularly limited, but energy facilities such as power plants and seawater desalination facilities, manufacturing factories for shipbuilding, automobiles, home appliances, etc., cutting parts processing factories, painting factories, dyeing factories, food factories, papermaking Factories such as factories can be mentioned.

［管状ＲＯ膜を用いた排水処理装置の作製］
図１に示す管状ＲＯ膜エレメント１０を、図２に示すように、Ｕ字管２１を使用して、直列に１８本連結させた管状ＲＯ膜集合体２０を作製した。管状ＲＯ膜エレメント１０は、内径１１．５ｍｍの管状ポリエステル不織布支持体の管内表面に０．３ｍｍの酢酸セルロース逆浸透膜（NaCl除去率９０％）を積層させた長さ２６５４ｍｍのものである。この管状ＲＯ膜集合体２０を図３に示す筒状のケーシング３０に収容し、図３に示す管状ＲＯ膜モジュール３０を作製した。この管状ＲＯ膜モジュール３０を合計４本（３０ａ～３０ｄ）と、原水タンク１と、ポンプ２と、透過水タンク３とを、各ライン４１～４９で連結させて、図４に示す排水処理装置を作製した。原水タンク１内に入れた排水は、ポンプ２を使用して、ライン４１を通過させて、管状ＲＯ膜モジュール３０ａの原水供給部２３ａから各管状ＲＯ膜モジュール３０ａ～３０ｄに順に供給され、各管状ＲＯ膜モジュールの管状ＲＯ膜集合体２０を通過する過程でろ過される。各管状ＲＯ膜モジュールでろ過した後の透過水は、各管状ＲＯ膜モジュールの各透過水出口２５ａ～２５ｄから排出され、各ライン４６～４９を通過させて、透過水タンク３に回収される。各管状ＲＯ膜モジュールでろ過した後の濃縮水は、最終的に管状ＲＯ膜モジュール３０ｄの濃縮水排出部２４ｄから排出され、ライン４５を通過させて、原水タンク１に戻され、再度ろ過されることにより原水タンク１内の排水は濃縮される。 [Manufacturing of wastewater treatment equipment using tubular RO membrane]
As shown in FIG. 2, a tubular RO membrane assembly 20 in which 18 tubular RO membrane elements 10 shown in FIG. 1 are connected in series using a U-shaped tube 21 was produced. The tubular RO membrane element 10 has a length of 2654 mm in which a 0.3 mm cellulose acetate reverse osmosis membrane (NaCl removal rate 90%) is laminated on the inner surface of a tubular polyester nonwoven fabric support having an inner diameter of 11.5 mm. The tubular RO membrane assembly 20 was housed in the tubular casing 30 shown in FIG. 3, and the tubular RO membrane module 30 shown in FIG. 3 was produced. A total of four tubular RO membrane modules 30 (30a to 30d), a raw water tank 1, a pump 2, and a permeated water tank 3 are connected by lines 41 to 49, and the wastewater treatment apparatus shown in FIG. 4 is connected. Was produced. The drainage put into the raw water tank 1 is passed through the line 41 using the pump 2 and is sequentially supplied from the raw water supply unit 23a of the tubular RO membrane module 30a to the tubular RO membrane modules 30a to 30d, and each tubular It is filtered in the process of passing through the tubular RO membrane assembly 20 of the RO membrane module. The permeated water after filtering by each tubular RO membrane module is discharged from each permeated water outlets 25a to 25d of each tubular RO membrane module, passes through each line 46 to 49, and is collected in the permeated water tank 3. The concentrated water after filtering by each tubular RO membrane module is finally discharged from the concentrated water discharge section 24d of the tubular RO membrane module 30d, passed through the line 45, returned to the raw water tank 1, and filtered again. As a result, the wastewater in the raw water tank 1 is concentrated.

実施例１
成型機洗浄による含油排水（ＣＯＤ：２４，６００ｍｇ／Ｌ）６５０ｋｇ（固形分濃度２．６質量％）を、図４の排水処理装置を用いて、排水を濃縮し、排水量を２２分の１（排水量３０ｋｇ：固形分濃度５７質量％）までに減容化する作業を行った（管状ＲＯ膜による処理工程）。
前記排水の固形分をＸ線マイクロアナライザーによって元素分析を行ったところ、主な元素としてはＣ：４６質量％、Ｏ：２４質量％、Ｐ：１２質量％、Ｎａ：１１質量％であった。
排水処理運転は、ポンプ２により一定圧になるように操作され、運転時の入口圧力（原水供給部２３ａ部の圧力）は４ＭＰａ、出口圧力（濃縮水排出部２４ｄ部の圧力）は２ＭＰａ、各管状ＲＯ膜モジュールの膜間圧力は２ＭＰａであった。
各管状ＲＯ膜の透過流速は、運転初期では１００Ｌ／ｈであったが、排水の濃縮とともに透過流速が徐々に低下し、８時間後には排水量が２２分の１となったため、排水処理運転を終了した。この際、透過水のＣＯＤは２８０ｍｇ／Ｌであった。
排水処理運転後に得られた固形分濃度５７重量％の排水を、蒸発装置として、西村鐵工所製ＣＤドライヤーを用いて蒸発工程を実施した。
ＣＤドライヤーにスクレパー（固形分掻き取り刃）をセットし、ディスク回転数を５ｒｐｍで運転し、ディスク中へ蒸気を入れディスク温度を昇温させながら、スクレパーの締め付けトルクを調整し、暖気運転を実施した。ディスク温度が１２０℃になった後、ディスク回転数を１５ｒｐｍに上げ、フィードノズルへ前記排水のポンプ送液を開始した。フィードノズルから吐出される排水は、ディスクの最適位置に当たるように調整した。ディスクに付着しない液分は、排水タンク中へ回収され、再びポンプ送液を行った。ディスクへ付着した液分は、スクレパーへ達するまでにディスク上で蒸発し、生じた固形分はスクレパーで掻き取り、ディスクの直下に設置した固形分回収箱へ落下させ回収した。蒸発水蒸気は、ブロワーにより回収した。蒸発工程中は、蒸気圧を０．２～０．３ＭＰａの範囲内で調整し、ディスク温度が１２０℃で一定になるよう調整した。なおＣＤドライヤーによる蒸発工程の排水処理に要したエネルギー量は、装置規模に対して排水量が少なかったため定量化できなかったが、蒸発工程を問題なく実施することができた。 Example 1
Oil-containing wastewater (COD: 24,600 mg / L) 650 kg (solid content concentration 2.6% by mass) by washing the molding machine is concentrated using the wastewater treatment device shown in FIG. Work was performed to reduce the volume to a displacement of 30 kg (solid content concentration 57% by mass) (treatment step using a tubular RO membrane).
Elemental analysis of the solid content of the wastewater by an X-ray microanalyzer revealed that the main elements were C: 46% by mass, O: 24% by mass, P: 12% by mass, and Na: 11% by mass.
The wastewater treatment operation is operated by the pump 2 so as to have a constant pressure, and the inlet pressure (pressure of the raw water supply section 23a) during operation is 4 MPa and the outlet pressure (pressure of the concentrated water discharge section 24d) is 2 MPa, respectively. The intermembrane pressure of the tubular RO membrane module was 2 MPa.
The permeation flow rate of each tubular RO membrane was 100 L / h at the initial stage of operation, but the permeation flow rate gradually decreased as the wastewater was concentrated, and after 8 hours, the amount of wastewater was reduced to 1/22. finished. At this time, the COD of the permeated water was 280 mg / L.
The wastewater having a solid content concentration of 57% by weight obtained after the wastewater treatment operation was subjected to an evaporation step using a CD dryer manufactured by Nishimura Works Co., Ltd. as an evaporation device.
Set the scraper (solid content scraping blade) in the CD dryer, operate the disk at 5 rpm, and adjust the tightening torque of the scraper while raising the temperature of the disk by putting steam into the disk to perform warm-up operation. did. After the disk temperature reached 120 ° C., the disk rotation speed was increased to 15 rpm, and pumping of the drainage to the feed nozzle was started. The drainage discharged from the feed nozzle was adjusted to hit the optimum position of the disc. The liquid that did not adhere to the disc was collected in the drainage tank and pumped again. The liquid adhering to the disc evaporates on the disc by the time it reaches the scraper, and the generated solid content is scraped off by the scraper and dropped into a solid content collection box installed directly under the disc for recovery. The vaporized steam was recovered by a blower. During the evaporation step, the vapor pressure was adjusted in the range of 0.2 to 0.3 MPa so that the disk temperature became constant at 120 ° C. The amount of energy required for the wastewater treatment in the evaporation process using the CD dryer could not be quantified because the amount of wastewater was small compared to the scale of the apparatus, but the evaporation process could be carried out without any problem.

実施例１の含油排水６５０ｋｇ（固形分濃度２．６質量％）を、２２分の１（排水量３０ｋｇ：固形分濃度５７質量％）までに減容化する排水処理に要したエネルギーを、以下に示す（１）と（２）のケースで比較した。
（１）実施例１の排水処理運転（管状ＲＯ膜による処理工程）を実施して、含油排水を減容化した場合
管状ＲＯ膜による処理工程に要するエネルギー：２２．４ｋＷ・ｈ
計算式：管状ＲＯ膜装置の所要動力（２．８ｋＷ）×運転時間（８ｈ）＝２２．４ＫＷ・ｈ
（２）実施例１の排水処理運転を実施せずに、直接加熱型乾燥機を用いて含油排水を減容化した場合
直接加熱型乾燥機の蒸発工程に要するエネルギー：１０２７ＫＷ・ｈ
計算式：水の蒸発潜熱（２．２６ＭＪ／ｋｇ）×蒸発水分量（６２０（６５０－３０）ｋｇ）／蒸発装置の乾燥効率（０．４）＋水の比熱容量（４．２×１０-３ＭＪ／ｋｇ℃）×蒸発水分量（６２０（６５０－３０）ｋｇ）×昇温温度（７５（１００－２５）℃）＝３６９８ＭＪ＝１０２７ＫＷ・ｈ
※蒸発工程に要するエネルギーの計算は、固形分成分の比熱も水と同じとし、排水（６５０ｋｇ）の初期温度は２５℃とし、蒸発装置の乾燥効率を４０％として算出した。 The energy required for wastewater treatment to reduce the volume of the oil-containing wastewater of Example 1 from 650 kg (solid content concentration 2.6% by mass) to 1/22 (displacement 30 kg: solid content concentration 57% by mass) is as follows. The cases (1) and (2) shown were compared.
(1) When the wastewater treatment operation of Example 1 (treatment step using a tubular RO membrane) is carried out to reduce the volume of oil-containing wastewater: Energy required for the treatment step using a tubular RO membrane: 22.4 kW · h
Calculation formula: Required power of tubular RO membrane device (2.8 kW) x operating time (8 h) = 22.4 kW ・ h
(2) When the volume of oil-containing wastewater is reduced by using a direct heating type dryer without carrying out the wastewater treatment operation of Example 1. Energy required for the evaporation process of the direct heating type dryer: 1027 kW · h
Calculation formula: Latent heat for evaporation of water (2.26 MJ / kg) x Moisture evaporation (620 (650-30) kg) / Drying efficiency of evaporation device (0.4) + Specific heat capacity of water ( 4.2 x 10- 3 MJ / kg ° C) x Evaporated water content (620 (650-30) kg) x Temperature rise temperature (75 (100-25) ° C) = 3698MJ = 1027KW · h
* The energy required for the evaporation process was calculated assuming that the specific heat of the solid content component is the same as that of water, the initial temperature of the wastewater (650 kg) is 25 ° C, and the drying efficiency of the evaporator is 40%.

実施例１の排水処理運転を実施して、含油排水６５０ｋｇ（固形分濃度２．６質量％）を、２２分の１（排水量３０ｋｇ：固形分濃度５７質量％）までに減容化するのに要したエネルギー（１）は、実施例１の排水処理運転を実施せずに、直接加熱型乾燥機を用いて含油排水を減容化した場合に要するエネルギー（２）と比較して、約４８分の１であり、著しいエネルギー削減が可能なことが分かる。 To reduce the volume of oil-containing wastewater from 650 kg (solid content concentration 2.6% by mass) to 1/222 (wastewater amount 30 kg: solid content concentration 57% by mass) by carrying out the wastewater treatment operation of Example 1. The required energy (1) is about 48 as compared with the energy (2) required when the oil-containing wastewater is reduced in volume by using a direct heating type dryer without carrying out the wastewater treatment operation of Example 1. It is one-third, and it can be seen that significant energy reduction is possible.

本発明の排水処理方法は、ＺＬＤを実現するため、各種分野の工場排水処理法として利用することができる。 The wastewater treatment method of the present invention can be used as a factory wastewater treatment method in various fields in order to realize ZLD.

１０ 管状ＲＯ膜エレメント
２０ 管状ＲＯ膜エレメント集合体
３０ 管状ＲＯ膜モジュール 10 Tubular RO Membrane Element 20 Tubular RO Membrane Element Assembly 30 Tubular RO Membrane Module

Claims (6)

排水処理において水分を回収し、最終的に乾燥された固形分のみを廃棄又は再利用する排水処理方法であって、
前記排水処理における排水源が、船・自動車・家電製品の製造工場、切削部品加工工場、塗装工場、染色工場、製紙工場から選択されるものであり、
前記排水処理方法が、管状ＲＯ膜による処理工程と蒸発工程を有しており、
前記管状ＲＯ膜による処理工程が、
筒状のケーシング内に、管状ポリエステル不織布支持体からなる多孔支持管内に内径５～１５ｍｍのチューブ状のセルロースアセテートからなるＲＯ膜が配置された管状ＲＯ膜エレメントを、１０～２０本配置された管状ＲＯ膜モジュールであって、前記複数本の管状ＲＯ膜エレメントが、それぞれの開口部同士が接続され、全体として１本の管状ＲＯ膜エレメントになっている管状ＲＯ膜モジュールを用いて被処理水のろ過運転を実施して、前記管状ＲＯ膜モジュールを用いてろ過した後の濃縮水を再び前記管状ＲＯ膜モジュールでろ過する運転を繰り返して、濃縮水の固形分濃度を２０質量％以上に高め、
前記管状ＲＯ膜による処理工程の後、濃縮水中の水分を蒸発させて回収し、固形分と分離する蒸発工程を実施する、排水処理方法。 It is a wastewater treatment method that recovers water in wastewater treatment and finally discards or reuses only dried solids.
The wastewater source in the wastewater treatment is selected from a ship / automobile / home appliance manufacturing factory, a cutting parts processing factory, a painting factory, a dyeing factory, and a paper mill.
The wastewater treatment method includes a treatment step using a tubular RO membrane and an evaporation step.
The processing step using the tubular RO membrane
In a tubular casing, 10 to 20 tubular RO membrane elements in which an RO membrane made of tubular cellulose acetate having an inner diameter of 5 to 15 mm is arranged in a porous support tube made of a tubular polyester non-woven support are arranged. The RO membrane module is a tubular RO membrane module in which the plurality of tubular RO membrane elements are connected to each other to form one tubular RO membrane element as a whole, and the water to be treated is used. A filtration operation is performed, and the operation of filtering the concentrated water after filtering using the tubular RO membrane module with the tubular RO membrane module is repeated to increase the solid content concentration of the concentrated water to 20% by mass or more.
A wastewater treatment method for carrying out an evaporation step of evaporating and recovering water in concentrated water and separating it from solids after the treatment step with the tubular RO membrane. 排水処理において水分を回収し、最終的に乾燥された固形分のみを廃棄又は再利用する排水処理方法であって、
前記排水処理方法が、前処理工程と管状ＲＯ膜による処理工程と蒸発工程を有しており、
前記管状ＲＯ膜による処理工程が、
筒状のケーシング内に、管状ポリエステル不織布支持体からなる多孔支持管内に内径５～１５ｍｍのチューブ状のセルロースアセテートからなるＲＯ膜が配置された管状ＲＯ膜エレメントを、１０～２０本配置された管状ＲＯ膜モジュールであって、前記複数本の管状ＲＯ膜エレメントが、それぞれの開口部同士が接続され、全体として１本の管状ＲＯ膜エレメントになっている管状ＲＯ膜モジュールを用いて被処理水のろ過運転を実施して、前記管状ＲＯ膜モジュールを用いてろ過した後の濃縮水を再び前記管状ＲＯ膜モジュールでろ過する運転を繰り返して、濃縮水の固形分濃度を２０質量％以上に高め、
前記管状ＲＯ膜による処理工程の後、濃縮水中の水分を蒸発させて回収し、固形分と分離する蒸発工程を実施する、排水処理方法。 It is a wastewater treatment method that recovers water in wastewater treatment and finally discards or reuses only dried solids.
The wastewater treatment method includes a pretreatment step, a treatment step using a tubular RO membrane, and an evaporation step.
The treatment step using the tubular RO membrane
In a tubular casing, 10 to 20 tubular RO membrane elements are arranged in which an RO membrane made of tubular cellulose acetate having an inner diameter of 5 to 15 mm is arranged in a porous support tube made of a tubular polyester non-woven support. The RO membrane module is a tubular RO membrane module in which the plurality of tubular RO membrane elements are connected to each other to form one tubular RO membrane element as a whole, and the water to be treated is used. A filtration operation is performed, and the operation of filtering the concentrated water after filtering using the tubular RO membrane module with the tubular RO membrane module is repeated to increase the solid content concentration of the concentrated water to 20% by mass or more.
A wastewater treatment method for carrying out an evaporation step of evaporating and recovering water in concentrated water and separating it from solids after the treatment step with the tubular RO membrane . 前記排水処理が、スパイラルＲＯ膜による処理工程を含む前処理工程と、前記管状ＲＯ膜による処理工程と前記蒸発工程を有している、請求項２記載の排水処理方法。 The wastewater treatment method according to claim 2 , wherein the wastewater treatment includes a pretreatment step including a treatment step using a spiral RO membrane, a treatment step using the tubular RO membrane, and the evaporation step. 前記前処理工程、前記管状ＲＯ膜による処理工程、前記蒸発工程において、被処理水中へ消泡剤を一括添加又は逐次添加する、請求項２又は３記載の排水処理方法。 The wastewater treatment method according to claim 2 or 3 , wherein the defoaming agent is collectively or sequentially added to the water to be treated in the pretreatment step, the treatment step using the tubular RO membrane, and the evaporation step. 前記蒸発工程が、間接加熱型汚泥乾燥機を用いて実施する、請求項１～４の何れか１項記載の排水処理方法。 The wastewater treatment method according to any one of claims 1 to 4 , wherein the evaporation step is carried out using an indirect heating type sludge dryer. 前記間接加熱型汚泥乾燥機が、伝熱面として円筒ドラムの外周面でなく、内部に空洞を有する中空円盤（ＣＤ：コンパクトディスク）の両面を使うＣＤドライヤーである、請求項５に記載の排水処理方法。
The drainage according to claim 5 , wherein the indirect heating type sludge dryer is a CD dryer that uses both sides of a hollow disk (CD: compact disk) having a cavity inside instead of the outer peripheral surface of a cylindrical drum as a heat transfer surface. Processing method.
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