JP2018051503A - Water treatment device, water treatment system and water treatment method - Google Patents
Water treatment device, water treatment system and water treatment method Download PDFInfo
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- JP2018051503A JP2018051503A JP2016192614A JP2016192614A JP2018051503A JP 2018051503 A JP2018051503 A JP 2018051503A JP 2016192614 A JP2016192614 A JP 2016192614A JP 2016192614 A JP2016192614 A JP 2016192614A JP 2018051503 A JP2018051503 A JP 2018051503A
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Landscapes
- Water Treatment By Sorption (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
Description
本発明は、有機物質として少なくとも１，４−ジオキサンを含有する地下水から１，４−ジオキサンを除去する水処理装置、水処理システム及び水処理方法に関する。 The present invention relates to a water treatment apparatus, a water treatment system, and a water treatment method for removing 1,4-dioxane from groundwater containing at least 1,4-dioxane as an organic substance.
従来より、水から有機物質を除去する装置として、粒状活性炭のなど吸着材を使用した吸着式水処理装置が知られている（例えば特許文献１参照）。これは、吸着材が充填された充填槽へ処理対象の被処理水を通水することで、被処理水中の有機物質を吸着除去するシンプルな水処理装置である。 Conventionally, an adsorption-type water treatment apparatus using an adsorbent such as granular activated carbon is known as an apparatus for removing organic substances from water (see, for example, Patent Document 1). This is a simple water treatment apparatus that adsorbs and removes organic substances in the water to be treated by passing the water to be treated through the filling tank filled with the adsorbent.
しかし、従来の水処理装置は、被処理水を一定期間通水し、吸着材の吸着能力が飽和に達すると、吸着材を新品へと交換するもしくは一旦装置から吸着材を取り出して再生する必要があり、連続浄化ができないという課題がある。これに対して、吸着材の交換や再生の頻度を少なくするために、多量の吸着材を充填させ、長期間吸着（被処理水の通水）を行うと、吸着材は微生物の繁殖や固形物の付着などによって、目詰まりや寿命が縮まるために、定期的な清掃や逆洗浄が必要になり、その労力やコストが増えるという課題がある。 However, in conventional water treatment equipment, when the water to be treated is passed for a certain period and the adsorption capacity of the adsorbent reaches saturation, it is necessary to replace the adsorbent with a new one or to remove the adsorbent from the apparatus and regenerate it. There is a problem that continuous purification cannot be performed. On the other hand, in order to reduce the frequency of replacement and regeneration of the adsorbent, if the adsorbent is filled with a large amount of adsorbent and adsorbed for a long period of time (water to be treated is passed), Since clogging and lifespan are shortened due to adhesion of objects, periodic cleaning and backwashing are required, which increases the labor and cost.
また、粒状活性炭では、水中の有機物質の中でも１，４−ジオキサンの吸着量が小さいという課題がある。ここで、食品製造に使用する食品製造用水として地下水を用いる場合には、「食品、添加物等の規格基準」に定められている「食品製造用水」の基準に適合することが求められるが、近年、上記規格基準が改正されて今まで以上に厳しい基準となり、特に、１，４−ジオキサンを多く取り除くことが水処理装置に求められている。しかし、従来の水処理装置では、水から１，４−ジオキサンを効果的に取り除くことができないという課題がある。 In addition, granular activated carbon has a problem that the adsorption amount of 1,4-dioxane is small among organic substances in water. Here, when using groundwater as water for food production used in food production, it is required to conform to the standards for “water for food production” defined in “Standards for Food, Additives, etc.” In recent years, the above-mentioned standard has been revised to be a stricter standard than ever, and in particular, water treatment apparatuses are required to remove much 1,4-dioxane. However, the conventional water treatment apparatus has a problem that 1,4-dioxane cannot be effectively removed from water.
そこで、本発明は上記の課題を解決するためになされ、その目的は、地下水から１，４−ジオキサンを効果的に除去できる吸着材を使用し、かつ、基本的に吸着材の目詰まりと交換のない水処理装置、水処理システム及び水処理方法を提供することである。 Therefore, the present invention has been made to solve the above-mentioned problems, and its purpose is to use an adsorbent that can effectively remove 1,4-dioxane from groundwater, and basically to replace the adsorbent with clogging. A water treatment apparatus, a water treatment system, and a water treatment method are provided.
本発明者らは鋭意検討した結果、以下に示す手段により、上記課題を解決できることを見出し、本発明に到達した。すなわち本発明は以下の構成からなる。 As a result of intensive studies, the present inventors have found that the above problems can be solved by the following means, and have reached the present invention. That is, the present invention has the following configuration.
（１）活性炭素繊維を含む吸着素子に地下水を通流させ、前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させて処理水を排出する吸着工程と、前記吸着素子にクリーンスチームを通気させて、前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着工程と、を順に繰り返し実行し、前記吸着工程及び前記脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更することを特徴とする水処理装置。
（２）活性炭素繊維を含む吸着素子を収容した処理槽と、前記処理槽に接続され、前記処理槽内の前記吸着素子に地下水を通流させて前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させ、処理水を排出する水通流部と、前記処理槽に接続され、前記処理槽内の前記吸着素子にクリーンスチームを通気させて前記吸着素子に吸着された１，４−ジオキサンを脱着するクリーンスチーム通気部と、前記吸着素子による１，４−ジオキサンの吸着工程及び前記吸着素子に対する１，４−ジオキサンの脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更する制御手段と、を備えることを特徴とする水処理装置。
（３）前記脱着工程では、前記吸着素子にクリーンスチームを通気させて前記吸着素子に付着した付着水を除去する脱水処理と、前記吸着素子にクリーンスチームを通気させて前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着処理とが行われることを特徴とする前記（１）又は（２）に記載の水処理装置。
（４）前記制御手段は、処理対象の地下水量の減少又は地下水中の１，４−ジオキサン濃度の減少に伴い、吸脱着繰り返し周期を長くすることを特徴とする前記（１）から（３）のいずれか１項に記載の水処置装置。
（５）前記制御手段は、処理対象の地下水量の減少又は地下水中の１，４−ジオキサン濃度の減少に伴い、前記吸着工程にて吸着処理を行う地下水の単位時間当たりの水量を減少させ、かつ前記吸着処理の時間を長くすることを特徴とする前記（４）に記載の水処置装置。
（６）前記制御手段は、処理対象の地下水量の減少又は地下水中の１，４−ジオキサン濃度の減少に伴い、前記吸着工程にて吸着処理を行う地下水の単位時間当たりの水量は変更せず、かつ前記吸着工程において前記吸着処理後に待機時間をとることで吸脱着繰り返し周期を長くすることを特徴とする前記（４）に記載の水処置装置。
（７）前記吸着素子の前記脱着工程が行われた部分を前記吸着工程を行う部分に移行させるとともに、前記吸着素子の前記吸着工程が行われた部分を前記脱着工程を行う部分に移行させる操作が繰り返し実施されることを特徴とする前記（１）から（６）のいずれか１項に記載の水処置装置。
（８）前記吸着素子から１，４−ジオキサンを脱着させたクリーンスチームを、前記吸着素子に通流させる地下水との熱交換により凝縮して濃縮水とする熱交換器をさらに備えることを特徴とする前記（１）から（７）のいずれかに記載の水処置装置。
（９）前記吸着素子から除去した付着水を、再度、前記吸着素子に通流させるための返送ルートをさらに備えることを特徴とする前記（３）に記載の水処理装置。
（１０）前記吸着素子に対して、クリーンスチームを通気させる通気方向と、地下水を通流させる通流方向とが逆であることを特徴とする前記（１）から（９）のいずれかに記載の水処理装置。
（１１）前記吸着素子は、繊維径が１７μｍ〜４０μｍの活性炭素繊維で構成された不織布であることを特徴とする前記（１）から（１０）のいずれかに記載の水処理装置。
（１２）前記有機物質は、１，４−ジオキサン以外にシス−１，２−ジクロロエチレン、トランス−１，２−ジクロロエチレン、ジクロロメタン、四塩化炭素、テトラクロロエチレン、トリクロロエチレン及び総トリハロメタンのいずれか一つ以上を含むことを特徴とする前記（１）から（１１）のいずれかに記載の水処理装置。
（１３）前記（１）から（１２）のいずれかに記載の水処理装置と、前記水処理装置にクリーンスチームを供給するクリーンスチーム発生装置と、を備えることを特徴とする水処理システム。
（１４）活性炭素繊維を含む吸着素子に地下水を通流させ、前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させて処理水を排出する吸着工程と、前記吸着素子にクリーンスチームを通気させて、前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着工程と、を順に繰り返し実行し、前記吸着工程及び前記脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更することを特徴とする水処理方法。
(1) An adsorption process in which ground water is passed through an adsorbing element containing activated carbon fibers, and at least 1,4-dioxane in the ground water is adsorbed to the adsorbing element to discharge treated water, and clean steam is applied to the adsorbing element. A desorption step of aerating and desorbing 1,4-dioxane adsorbed on the adsorbing element in order, and repeating the adsorption step and the desorption step one by one. The water treatment device is characterized in that the water treatment device is changed according to the amount of groundwater to be treated or the concentration of 1,4-dioxane in the groundwater.
(2) A treatment tank containing an adsorption element containing activated carbon fibers, and connected to the treatment tank, and allowing groundwater to flow through the adsorption element in the treatment tank so that at least 1, 4 in the groundwater is contained in the adsorption element. -A water flow part for adsorbing dioxane and discharging treated water; and connected to the treatment tank, and adsorbing the adsorption element in the treatment tank by passing clean steam through the adsorption element. A clean steam ventilation part for desorbing dioxane, and an adsorption / desorption repetition cycle of 1 cycle for performing the adsorption process of 1,4-dioxane by the adsorption element and the desorption process of 1,4-dioxane to the adsorption element once, And a control unit that changes the amount of groundwater to be treated or the concentration of 1,4-dioxane in the groundwater to be passed through the adsorption element.
(3) In the desorption step, the desorption process of passing clean steam through the adsorbing element to remove adhering water adhering to the adsorbing element and the adsorbing element being adsorbed by the adsorbing element through the clean steam. The water treatment apparatus according to (1) or (2), wherein a desorption treatment for desorbing 1,4-dioxane is performed.
(4) The control means lengthens the adsorption / desorption repetition period in accordance with a decrease in the amount of groundwater to be treated or a decrease in 1,4-dioxane concentration in the groundwater. The water treatment apparatus of any one of these.
(5) The control means reduces the amount of water per unit time of the groundwater to be subjected to the adsorption treatment in the adsorption step, along with a decrease in the amount of groundwater to be treated or a decrease in the 1,4-dioxane concentration in the groundwater, And the time of the said adsorption process is lengthened, The water treatment apparatus as described in said (4) characterized by the above-mentioned.
(6) The control means does not change the amount of water per unit time of the groundwater to be subjected to the adsorption treatment in the adsorption step with a decrease in the amount of groundwater to be treated or a decrease in the 1,4-dioxane concentration in the groundwater. The water treatment device according to (4), wherein the adsorption / desorption repetition cycle is lengthened by taking a waiting time after the adsorption treatment in the adsorption step.
(7) The operation of moving the portion of the adsorption element where the desorption process has been performed to the portion where the adsorption process is performed and moving the portion of the adsorption element where the adsorption process is performed to the portion where the desorption process is performed The water treatment device according to any one of (1) to (6), wherein is repeatedly performed.
(8) It further comprises a heat exchanger which condenses clean steam from which 1,4-dioxane has been desorbed from the adsorbing element by heat exchange with groundwater to be passed through the adsorbing element to form concentrated water. The water treatment device according to any one of (1) to (7).
(9) The water treatment apparatus according to (3), further comprising a return route for allowing the adhering water removed from the adsorption element to flow again through the adsorption element.
(10) The method according to any one of (1) to (9), wherein a ventilation direction for allowing clean steam to flow through the adsorbing element and a flow direction for allowing groundwater to flow are opposite to each other. Water treatment equipment.
(11) The water treatment apparatus according to any one of (1) to (10), wherein the adsorption element is a nonwoven fabric composed of activated carbon fibers having a fiber diameter of 17 μm to 40 μm.
(12) The organic substance may contain at least one of cis-1,2-dichloroethylene, trans-1,2-dichloroethylene, dichloromethane, carbon tetrachloride, tetrachloroethylene, trichloroethylene, and total trihalomethane in addition to 1,4-dioxane. The water treatment device according to any one of (1) to (11), wherein the water treatment device is included.
(13) A water treatment system comprising: the water treatment device according to any one of (1) to (12); and a clean steam generator for supplying clean steam to the water treatment device.
(14) An adsorption step of allowing groundwater to flow through an adsorption element containing activated carbon fibers, adsorbing at least 1,4-dioxane in groundwater to the adsorption element and discharging treated water; and clean steam to the adsorption element A desorption step of aerating and desorbing 1,4-dioxane adsorbed on the adsorbing element in order, and repeating the adsorption step and the desorption step one by one. The water treatment method is characterized by changing according to the amount of groundwater to be treated or the concentration of 1,4-dioxane in the groundwater to be passed through the adsorption element.
なお、本発明の水処理装置の制御手段をコンピュータに実行させるプログラム及びそれを記録した記憶媒体、あるいは、本発明の水処理方法をコンピュータに実行させるプログラム及びそれを記録した記憶媒体も、本発明の範疇に含まれる。 A program for causing a computer to execute the control means of the water treatment apparatus of the present invention and a storage medium recording the program, or a program for causing the computer to execute the water treatment method of the present invention and a storage medium recording the program are also included in the present invention. Included in the category.
本発明の水処理装置、水処理システム及び水処理方法によれば、基本的に吸着材の交換の必要がなく、地下水中の１，４−ジオキサンを高い効率で除去することができる。また、吸着素子に吸着された１，４−ジオキサンを脱着するためのガスとしてクリーンスチームを用いているので、処理水を食品製造に使用する食品製造用水や飲料水などの用途に用いることができる。さらに、地下水の揚水量（処理対象の地下水量）に応じて、吸着工程及び脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を変更することで、単位時間当たりの吸着素子の脱着回数を減らすことができる。その結果、吸着素子の脱着処理に要するクリーンスチームの量を減らすことができ、クリーンスチームの製造に要する消費電力及び消費水量を減らすことができるので、装置全体として省エネルギーを実現できる。 According to the water treatment device, water treatment system, and water treatment method of the present invention, it is basically unnecessary to replace the adsorbent, and 1,4-dioxane in groundwater can be removed with high efficiency. Moreover, since clean steam is used as a gas for desorbing 1,4-dioxane adsorbed on the adsorbing element, it can be used for uses such as water for food production and drinking water in which treated water is used for food production. . Furthermore, the number of adsorption / desorption times per unit time can be changed by changing the cycle of adsorption / desorption of one cycle in which the adsorption process and desorption process are executed once according to the amount of groundwater pumped (the amount of groundwater to be treated). Can be reduced. As a result, the amount of clean steam required for the desorption process of the adsorption element can be reduced, and the power consumption and water consumption required for the production of clean steam can be reduced, so that energy saving can be realized for the entire apparatus.
本発明に係る水処理装置は、活性炭素繊維を含む吸着素子に地下水を通流させ、前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させて処理水を排出する吸着工程と、前記吸着素子にクリーンスチームを通気させて、前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着工程と、を順に繰り返し実行し、前記吸着工程及び前記脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更する構成のものである。 The water treatment apparatus according to the present invention includes an adsorption step of allowing groundwater to flow through an adsorption element containing activated carbon fibers, adsorbing at least 1,4-dioxane in groundwater to the adsorption element, and discharging the treated water; A cycle in which clean steam is passed through the adsorbing element, and a desorption process for desorbing 1,4-dioxane adsorbed on the adsorbing element is sequentially performed, and the adsorption process and the desorption process are performed once each. The adsorption / desorption repetition period is changed according to the amount of groundwater to be treated or the concentration of 1,4-dioxane in the groundwater to be passed through the adsorption element.
また、本発明に係る水処理装置は、以下の構成のものと言うこともできる。つまり、水処理装置は、活性炭素繊維を含む吸着素子を収容した処理槽と、前記処理槽に接続され、前記処理槽内の前記吸着素子に地下水を通流させて前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させ、処理水を排出する水通流部と、前記処理槽に接続され、前記処理槽内の前記吸着素子にクリーンスチームを通気させて前記吸着素子に吸着された１，４−ジオキサンを脱着するクリーンスチーム通気部と、前記吸着素子による１，４−ジオキサンの吸着工程及び前記吸着素子に対する１，４−ジオキサンの脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更する制御手段と、を備える構成のものである。 Moreover, it can be said that the water treatment apparatus according to the present invention has the following configuration. In other words, the water treatment device is connected to the treatment tank containing the adsorption element containing activated carbon fiber, and is connected to the treatment tank, and allows the adsorption element in the treatment tank to flow through the groundwater so that the adsorption element is in the groundwater. At least 1,4-dioxane was adsorbed and connected to the water flow portion for discharging treated water and the treatment tank, and clean steam was passed through the adsorption element in the treatment tank and adsorbed to the adsorption element. A clean steam vent for desorbing 1,4-dioxane, and a cycle of adsorption / desorption in which the adsorption process of 1,4-dioxane by the adsorption element and the desorption process of 1,4-dioxane to the adsorption element are performed once. And a control unit that changes the repetition cycle according to the amount of groundwater to be processed or the concentration of 1,4-dioxane in the groundwater to be passed through the adsorption element.
ここで、クリーンスチームとは、食品製造や食品加工に使用可能な程度まで汚染物質が除かれた蒸気を指す。以下で説明する実施形態では、クリーンスチームとして、ボイラーからの蒸気を耐圧容器内で飽和熱水へ液相化することにより、蒸気に含まれる汚染物質を液中に留め易くし、飽和熱水を再度気相化することにより汚染物質を分離した蒸気を用いている。また、処理対象とは、吸着素子に通流する（処理槽に導入する）という意味で用いている。 Here, clean steam refers to steam from which contaminants have been removed to the extent that it can be used in food production and food processing. In the embodiment described below, as the clean steam, the vapor from the boiler is liquidified into saturated hot water in the pressure-resistant container, thereby making it easy to keep contaminants contained in the steam in the liquid, The vapor separated from the pollutants by vaporizing again is used. Further, the processing target is used in the sense of flowing through the adsorption element (introducing into the processing tank).
本発明に係る水処理装置は、上記構成により、吸着素子の交換を必要とすることがなく、処理対象の地下水に含まれる１，４−ジオキサンを効果的に除去する水処理を行うことができる。また、吸着素子に吸着された１，４−ジオキサンを脱着するためのガスとしてクリーンスチームを用いているので、処理水を食品製造に使用する食品製造用水や飲料水などの用途に用いることができる。さらに、地下水の揚水量（処理対象の地下水量）に応じて、吸着工程及び脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を変更することで、単位時間当たりの吸着素子の脱着回数を減らすことができる。その結果、吸着素子の脱着処理に要するクリーンスチームの量を減らすことができ、クリーンスチームの製造に要する消費電力及び消費水量を減らすことができるので、装置全体として省エネルギーを実現できる。以下、本発明に係る水処理装置の実施形態について図面を参照しつつ詳細に説明する。 With the above configuration, the water treatment apparatus according to the present invention can perform water treatment that effectively removes 1,4-dioxane contained in the groundwater to be treated without requiring replacement of the adsorption element. . Moreover, since clean steam is used as a gas for desorbing 1,4-dioxane adsorbed on the adsorbing element, it can be used for uses such as water for food production and drinking water in which treated water is used for food production. . Furthermore, the number of adsorption / desorption times per unit time can be changed by changing the cycle of adsorption / desorption of one cycle in which the adsorption process and desorption process are executed once according to the amount of groundwater pumped (the amount of groundwater to be treated). Can be reduced. As a result, the amount of clean steam required for the desorption process of the adsorption element can be reduced, and the power consumption and water consumption required for the production of clean steam can be reduced, so that energy saving can be realized for the entire apparatus. Hereinafter, embodiments of a water treatment apparatus according to the present invention will be described in detail with reference to the drawings.
［実施形態１］
図１は、本発明に係る水処理装置を備えた水処理システムの一実施形態の概略構成を示している。本実施形態の水処理システムＳは、水処理装置１００と、水処理装置１００にクリーンスチームを供給するクリーンスチーム発生装置４０と、を備えている。さらに、本実施形態の水処理システムＳは、純水を製造する純水製造装置５０を備えている。
[Embodiment 1]
FIG. 1 shows a schematic configuration of an embodiment of a water treatment system provided with a water treatment apparatus according to the present invention. The water treatment system S of the present embodiment includes a water treatment device 100 and a clean steam generator 40 that supplies clean steam to the water treatment device 100. Furthermore, the water treatment system S of the present embodiment includes a pure water production apparatus 50 that produces pure water.
図１に示すように、本実施形態の水処理装置１００は、吸着材として吸着素子１１，１２をそれぞれ収容した複数の処理槽１０，２０と、各処理槽１０，２０内に地下水を導入するための地下水導入ラインＬ１（水通流部）と、各処理槽１０，２０内にクリーンスチームを供給するためのクリーンスチーム供給ラインＬ３（クリーンスチーム通気部）と、を備えている。また、本実施形態の水処理装置１００は、各処理槽１０，２０内の吸着素子１１，１２により清浄化された後の水である処理水を排出するための処理水導出ラインＬ２（水通流部）と、各処理槽１０，２０内に供給されたクリーンスチームを排出するためのクリーンスチーム排出ラインＬ４（クリーンスチーム通気部）と、クリーンスチーム排出ラインＬ４から分岐して地下水導入ラインＬ１に還流する循環ラインＬ５（返送ルート）と、クリーンスチーム排出ラインＬ４から排出される１，４−ジオキサンを含む脱着ガスを冷却して凝縮する凝縮器３０と、をさらに備えている。 As shown in FIG. 1, the water treatment apparatus 100 according to the present embodiment introduces ground water into each of the treatment tanks 10 and 20 that accommodates the adsorption elements 11 and 12 as adsorbents. And a clean steam supply line L3 (clean steam ventilation section) for supplying clean steam into the treatment tanks 10 and 20. Further, the water treatment apparatus 100 of the present embodiment has a treated water derivation line L2 (water flow) for discharging treated water that is water after being cleaned by the adsorption elements 11 and 12 in the treatment tanks 10 and 20, respectively. Flow field), a clean steam discharge line L4 (clean steam ventilation part) for discharging clean steam supplied into the treatment tanks 10 and 20, and a branch line from the clean steam discharge line L4 to the groundwater introduction line L1. A recirculation line L5 (return route) for refluxing and a condenser 30 for cooling and condensing the desorption gas containing 1,4-dioxane discharged from the clean steam discharge line L4 are further provided.
なお、本実施形態の水処理装置１００は、吸着素子１１，１２を収容した処理槽１０，２０を複数備えている。そして、ダンパーやバルブなどを用いて各ラインＬ１〜Ｌ５を制御し、地下水を導入・排出する経路、クリーンスチームを供給・排出する経路を適宜切り替えることで、吸着工程を行う処理槽と、脱着工程を行う処理槽とに分けられている。これにより、吸着工程をどちらかの処理槽の吸着素子により連続して行うことが可能であり、いずれかの処理槽（例えば処理槽１０）にて吸着素子により地下水の清浄化（吸着処理）が行われている間、他の処理槽（例えば処理槽２０）では吸着素子の再生化（脱水処理及び脱着処理）を行うことが可能である。 In addition, the water treatment apparatus 100 according to the present embodiment includes a plurality of treatment tanks 10 and 20 that accommodate the adsorption elements 11 and 12. And the processing tank which performs an adsorption | suction process by controlling each line L1-L5 using a damper, a valve, etc., and switching the path | route which introduces / discharges groundwater, and the path | route which supplies / discharges clean steam, and a desorption process It is divided into the processing tank which performs. Thereby, it is possible to perform an adsorption process continuously by the adsorption element of one of processing tanks, and in one of the processing tanks (for example, processing tank 10), the purification of groundwater (adsorption treatment) is performed by the adsorption elements. During the process, the adsorption element can be regenerated (dehydration process and desorption process) in another process tank (for example, the process tank 20).
図１に示すように、本実施形態の水処理装置１００は、それぞれ吸着素子１１，１２を内部に収容した処理槽１０，２０を２つ備えている。なお、吸着素子１１，１２及び処理槽１０，２０の数は限定されない。後述する各処理槽１０，２０内における吸着工程及び脱着工程は、各バルブＶ１〜Ｖ１０の開閉操作を行い、地下水を導入・排出する経路、クリーンスチームを供給・排出する経路を適宜切り替えることで行われる。 As shown in FIG. 1, the water treatment apparatus 100 of the present embodiment includes two treatment tanks 10 and 20 in which adsorption elements 11 and 12 are housed, respectively. In addition, the number of adsorption | suction elements 11 and 12 and the processing tanks 10 and 20 is not limited. The adsorption process and the desorption process in each processing tank 10 and 20 described later are performed by opening and closing each valve V1 to V10, and appropriately switching the path for introducing and discharging groundwater and the path for supplying and discharging clean steam. Is called.
各処理槽１０，２０には、地下水導入ラインＬ１がそれぞれバルブＶ１，Ｖ２を介して接続されている。また、各処理槽１０，２０には、処理水導出ラインＬ２がそれぞれバルブＶ３，Ｖ４を介して接続されている。 A groundwater introduction line L1 is connected to each treatment tank 10 and 20 via valves V1 and V2, respectively. In addition, a treated water lead-out line L2 is connected to each of the treatment tanks 10 and 20 via valves V3 and V4, respectively.
水処理装置１００は、地下水導入ラインＬ１により各処理槽１０，２０内に地下水を供給して各処理槽１０，２０内の吸着素子１１，１２に地下水を所定時間通流させることで、地下水に含まれる少なくとも１，４−ジオキサンを吸着する吸着処理（吸着工程）が行われる。地下水に１，４−ジオキサン以外にも有機物質が含まれている場合には、吸着工程では、その有機物質も吸着される。これにより、地下水が清浄化される。清浄化された後の処理水は、処理水導出ラインＬ２より各処理槽１０，２０の外部に排出される。 The water treatment apparatus 100 supplies groundwater into the treatment tanks 10 and 20 through the groundwater introduction line L1 and passes the groundwater through the adsorbing elements 11 and 12 in the treatment tanks 10 and 20 for a predetermined time. An adsorption treatment (adsorption step) for adsorbing at least 1,4-dioxane contained therein is performed. When the groundwater contains an organic substance other than 1,4-dioxane, the organic substance is also adsorbed in the adsorption step. Thereby, groundwater is cleaned. The treated water after being cleaned is discharged outside the treatment tanks 10 and 20 from the treated water lead-out line L2.
吸着素子１１，１２は、活性炭素繊維を含んでいる。活性炭素繊維は、表面に微細な細孔を均一に多数有しているので、地下水中の１，４−ジオキサンの極めて高い除去効率を実現できる。活性炭素繊維は、原料である繊維を不織布などのシート状の構造体に加工し、炭化・賦活して得ることができる。 The adsorption elements 11 and 12 include activated carbon fibers. Since the activated carbon fiber has a large number of fine pores uniformly on the surface, the removal efficiency of 1,4-dioxane in the groundwater can be realized. The activated carbon fiber can be obtained by processing a raw material fiber into a sheet-like structure such as a nonwoven fabric, and then carbonizing and activating it.
活性炭素繊維は、繊維径が１７μｍ〜４０μｍであることが好ましい。繊維径が１７μｍ以上とすることで、クリーンスチームを通気させる際の吸着素子１１，１２の圧力損失を低減させることができ、繊維表面の付着水量を減らして、脱着効率を向上させることができるからである。一方、繊維径が４０μｍを越えると、上述の脱着効率の向上効果は期待できるが、繊維径が大きくなることにより、地下水中の吸着物質（１，４−ジオキサン）と吸着素子１１，１２との接触効率が低下するために、吸着性能が低下するからである。 The activated carbon fiber preferably has a fiber diameter of 17 μm to 40 μm. By setting the fiber diameter to 17 μm or more, the pressure loss of the adsorbing elements 11 and 12 when clean steam is ventilated can be reduced, and the amount of water adhering to the fiber surface can be reduced to improve the desorption efficiency. It is. On the other hand, when the fiber diameter exceeds 40 μm, the above-described effect of improving the desorption efficiency can be expected. However, when the fiber diameter is increased, the adsorbing substance (1,4-dioxane) in the groundwater and the adsorbing elements 11 and 12 are increased. This is because the contact efficiency is lowered and the adsorption performance is lowered.
活性炭素繊維の原料となる繊維は、特に限定されるものではないが、例えばフェノール系繊維、セルロース系繊維、アクリロニトリル系繊維、ピッチ系繊維などが好ましい。中でも、フェノール系繊維は、炭化・賦活後の活性炭素繊維の収率が高く、繊維強度が強い点でさらに好ましい。 Although the fiber used as the raw material of activated carbon fiber is not specifically limited, For example, a phenol fiber, a cellulose fiber, an acrylonitrile fiber, a pitch fiber, etc. are preferable. Among these, phenol fibers are more preferable in terms of high yield of activated carbon fibers after carbonization / activation and strong fiber strength.
フェノール系繊維としては、フェノール樹脂に脂肪酸アミド類、リン酸エステル類、セルロース類よりなる群から選択される少なくとも１種の化合物（配合物）を混合した混合物を紡糸して得られるフェノール系繊維を原糸としてもよい。これにより、さらに繊維強度を高めることができる。 As the phenolic fiber, a phenolic fiber obtained by spinning a mixture in which a phenol resin is mixed with at least one compound (compound) selected from the group consisting of fatty acid amides, phosphate esters, and celluloses is used. It may be a raw yarn. Thereby, fiber strength can be raised further.
吸着素子１１，１２に用いられる活性炭素繊維の物性は、特に限定されるものではないが、吸着素子１１，１２の吸着量や強度、コストなどを考慮すると、ＢＥＴ比表面積が９００ｍ２／ｇ〜２５００ｍ２／ｇで、細孔容積が０．４ｃｍ３／ｇ〜０．９ｃｍ３／ｇで、平均細孔経が１４Å〜１８Åであることが好ましい。 The physical properties of the activated carbon fiber used for the adsorbing elements 11 and 12 are not particularly limited. However, in consideration of the adsorbing amount, strength, cost and the like of the adsorbing elements 11 and 12, the BET specific surface area is 900 m 2 / g to in 2500 m 2 / g, a pore volume of at 0.4cm 3 /g~0.9cm 3 / g, and an average pore through is 14A～18A.
本実施形態では、処理対象の地下水に含まれる処理対象物質は、１，４−ジオキサンを例に説明しているが、以下の有機物質についても、本実施形態の水処理装置１００は同様の除去効果がある。例えば、ホルムアルデヒド、アセトアルデヒド、プロピオンアルデヒド、アクロレインなどのアルデヒド類、メチルエチルケトン、ジアセチル、メチルイソブチルケトン、アセトンなどのケトン類、２−メチル−１，３−ジオキソラン、１，３−ジオキソラン、テトラヒドロフラン、酢酸メチル、酢酸エチル、酢酸プロピル、酢酸ブチルなどのエステル類、エタノール、ｎ−プロピルアルコール、イソプロピルアルコール、ブタノールなどのアルコール類、エチレングリコール、プロピレングリコール、ジエチレングリコール、トリエチレングリコールなどのグリコール類、酢酸、プロピオン酸などの有機酸、フェノール類、トルエン、キシレン、シクロヘキサンなどの芳香族有機物質、ジエチルエーテル、アリルグリシジルエーテルなどのエーテル類、アクリロニトリルなどの二トリル類、ジクロロメタン、１，２−ジクロロエタン、トリクロロエチレン、エピクロロヒドリンなどの塩素有機物質、Ｎ−メチル−２−ピロリドン、ジメチルアセトアミド、Ｎ，Ｎ−ジメチルホルムアミドの有機物質、ポリ塩化ジベンゾパラジオキシン (PCDD)、ポリ塩化ジベンゾフラン (PCDF)、ダイオキシン様ポリ塩化ビフェニル (DL-PCB)などのダイオキシン類、テトラサイクリン、オセルタミビル、リン酸オセルタミビル、ベザフィブラート、トリクロサンなどの抗生物質、ベザフィブラート、フェノフィブラートなどの抗脂血症剤成分、ジクロフェナク、サリチル酸、アセトアミノフェンなどの解熱鎮痛剤成分、カルバマゼピンなどの抗てんかん剤成分、フミン酸、フルボ酸などのフミン物質、ヘキサメチレンテトラミン、ジオスミン、２−メチルイソボルネオールなどを一例として挙げることができる。本実施形態の水処理装置１００が処理する地下水に含まれる処理対象物質は、これらのうちの１種類あるいは複数種類であってもよい。 In the present embodiment, the processing target substance contained in the groundwater to be processed is described by taking 1,4-dioxane as an example, but the water treatment apparatus 100 of the present embodiment also removes the following organic substances in the same manner. effective. For example, aldehydes such as formaldehyde, acetaldehyde, propionaldehyde, acrolein, ketones such as methyl ethyl ketone, diacetyl, methyl isobutyl ketone, acetone, 2-methyl-1,3-dioxolane, 1,3-dioxolane, tetrahydrofuran, methyl acetate, Esters such as ethyl acetate, propyl acetate, butyl acetate, alcohols such as ethanol, n-propyl alcohol, isopropyl alcohol, butanol, glycols such as ethylene glycol, propylene glycol, diethylene glycol, triethylene glycol, acetic acid, propionic acid, etc. Organic acids, phenols, aromatic organic substances such as toluene, xylene, cyclohexane, diethyl ether, allyl glycidyl ether, etc. Ethers, nitriles such as acrylonitrile, chlorinated organic substances such as dichloromethane, 1,2-dichloroethane, trichloroethylene, epichlorohydrin, organic substances such as N-methyl-2-pyrrolidone, dimethylacetamide, N, N-dimethylformamide Dioxins such as polychlorinated dibenzopararadioxin (PCDD), polychlorinated dibenzofuran (PCDF), dioxin-like polychlorinated biphenyl (DL-PCB), tetracycline, oseltamivir, oseltamivir phosphate, bezafibrate, triclosan and other antibiotics, bezafibrate, Antilipidemic components such as fenofibrate, antipyretic analgesic components such as diclofenac, salicylic acid and acetaminophen, antiepileptic components such as carbamazepine, humic substances such as humic acid and fulvic acid, hexa Examples include methylenetetramine, diosmine, 2-methylisoborneol and the like. The substance to be treated contained in the ground water to be treated by the water treatment apparatus 100 of the present embodiment may be one type or a plurality of types.
図１において、各処理槽１０，２０には、クリーンスチーム供給ラインＬ３がそれぞれバルブＶ５，Ｖ６を介して接続されている。クリーンスチーム供給ラインＬ３は、クリーンスチーム発生装置４０にも接続されている。さらに、各処理槽１０，２０には、クリーンスチーム排出ラインＬ４がバルブＶ７，Ｖ８を介して接続されている。クリーンスチーム排出ラインＬ４は、バルブＶ９を介して凝縮器３０にも接続されている。 In FIG. 1, a clean steam supply line L3 is connected to each of the processing tanks 10 and 20 via valves V5 and V6, respectively. The clean steam supply line L3 is also connected to the clean steam generator 40. Further, a clean steam discharge line L4 is connected to each of the treatment tanks 10 and 20 via valves V7 and V8. The clean steam discharge line L4 is also connected to the condenser 30 via the valve V9.
吸着工程後、水処理装置１００は脱着工程を行うが、この脱着工程では、まず、クリーンスチーム供給ラインＬ３により各処理槽１０，２０内にクリーンスチームを供給して各処理槽１０，２０内の吸着素子１１，１２にクリーンスチームを所定時間通気させることで、各吸着素子１１，１２に付着した付着水を除去する脱水処理が行われる。各吸着素子１１，１２は、付着した付着水がクリーンスチームの通流により除去されて乾いた状態となることにより、その後のクリーンスチームによる１，４−ジオキサンの脱着処理を容易にすることができる。 After the adsorption process, the water treatment apparatus 100 performs a desorption process. In this desorption process, first, clean steam is supplied into the treatment tanks 10 and 20 through the clean steam supply line L3, and the water in the treatment tanks 10 and 20 is supplied. A dehydration process for removing the adhering water adhering to each of the adsorbing elements 11 and 12 is performed by passing clean steam through the adsorbing elements 11 and 12 for a predetermined time. Each adsorbing element 11, 12 can facilitate the desorption process of 1,4-dioxane by subsequent clean steam by removing the adhering adhering water by the flow of clean steam and becoming dry. .
脱水処理において各処理槽１０，２０内に供給されるクリーンスチームは、不純物を含まないあるいはほとんど含まない純粋な蒸気（「ピュアスチーム」と呼ばれるものも含む。）であり、例えば純水や超純水などの精製水を沸騰させたものである。脱水処理において各処理槽１０，２０内に供給されるクリーンスチームの温度は、例えば１００℃〜１４０℃である。脱水処理にて脱水された付着水はクリーンスチームとともにクリーンスチーム排出ラインＬ４より各処理槽１０，２０の外部に排出される。このとき、付着水は、バルブＶ９の閉操作かつバルブＶ１０の開操作により循環ラインＬ５より地下水導入ラインＬ１に還流され、再び吸着素子１１，１２に通流させるために各処理槽１０，２０内に導入される。これにより、工程数を省略することができるので、効率的である。 The clean steam supplied into the treatment tanks 10 and 20 in the dehydration process is pure vapor (including what is called “pure steam”) that does not contain impurities or almost does not contain impurities, for example, pure water or ultrapure. Purified water such as water is boiled. The temperature of the clean steam supplied into each processing tank 10 and 20 in a dehydration process is 100 to 140 degreeC, for example. The adhering water dehydrated in the dehydration process is discharged to the outside of the treatment tanks 10 and 20 through the clean steam discharge line L4 together with the clean steam. At this time, the adhering water is recirculated from the circulation line L5 to the groundwater introduction line L1 by the closing operation of the valve V9 and the opening operation of the valve V10, and is recirculated to the adsorption elements 11 and 12 in each processing tank 10 and 20. To be introduced. Thereby, the number of steps can be omitted, which is efficient.
脱着工程では、脱水処理後、次に、クリーンスチーム供給ラインＬ３によりにより各処理槽１０，２０内にクリーンスチームを供給して各処理槽１０，２０内の吸着素子１１，１２にクリーンスチームを所定時間通気させることで、各吸着素子１１，１２に吸着した少なくとも１，４−ジオキサンを除去する脱着処理が行われる。吸着素子１１，１２に１，４−ジオキサン以外の有機物質も吸着された場合には、その有機物質も脱着される。脱着処理において各処理槽１０，２０内に供給されるクリーンスチームの温度は、例えば１００℃〜１４０℃である。脱着処理にて脱着された１，４−ジオキサンはクリーンスチームとともに脱着ガスとしてクリーンスチーム排出ラインＬ４より各処理槽１０，２０の外部に排出され、凝縮器３０にて凝縮される。１，４−ジオキサン以外の有機物質も脱着された場合には、脱着ガスにはその有機物質も含まれる。 In the desorption process, after the dehydration process, clean steam is then supplied into the processing tanks 10 and 20 through the clean steam supply line L3, and clean steam is supplied to the adsorption elements 11 and 12 in the processing tanks 10 and 20, respectively. The desorption process which removes at least 1, 4- dioxane adsorb | sucked to each adsorption | suction element 11 and 12 by performing aeration for time is performed. When an organic substance other than 1,4-dioxane is adsorbed on the adsorption elements 11 and 12, the organic substance is also desorbed. The temperature of the clean steam supplied into each processing tank 10 and 20 in the desorption process is, for example, 100 ° C to 140 ° C. The 1,4-dioxane desorbed in the desorption process is discharged out of the treatment tanks 10 and 20 from the clean steam discharge line L4 as a desorption gas together with the clean steam, and is condensed in the condenser 30. When an organic substance other than 1,4-dioxane is also desorbed, the desorbed gas includes the organic substance.
凝縮器３０は、脱着ガスを冷却する装置であれば、脱着ガスの冷却方法は特に限定されない。例えば、冷却水、工業用水、冷水、ブラインなどの冷媒と脱着ガスとを間接的に接触させて、熱交換により脱着ガスを液化凝縮させる装置（熱交換器）を用いることができる。本実施形態では、冷媒として処理対象の地下水を用いており、地下水は凝縮器３０にて脱着ガスとの熱交換後、処理槽１０，２０にて吸着処理される。冷媒として地下水を用いることで、脱着ガスを冷却するための冷媒を別途用いる必要がなく、効率的である。 As long as the condenser 30 is a device that cools the desorption gas, the cooling method of the desorption gas is not particularly limited. For example, it is possible to use a device (heat exchanger) that makes the desorbed gas liquefy and condense by heat exchange by bringing the desorbed gas into indirect contact with a coolant such as cooling water, industrial water, cold water, or brine. In the present embodiment, groundwater to be treated is used as the refrigerant, and the groundwater is subjected to adsorption treatment in the treatment tanks 10 and 20 after heat exchange with the desorption gas in the condenser 30. By using groundwater as the refrigerant, there is no need to separately use a refrigerant for cooling the desorption gas, which is efficient.
クリーンスチーム発生装置４０は、例えばステンレス製の配管６０を介して純水製造装置５０に接続されている。クリーンスチーム発生装置４０としては、特に限定されるものではなく、食品分野や医療分野などで用いられている従来から公知の装置、例えば、ボイラーで発生させた一般蒸気を熱源として、ステンレス製の熱交換器でクリーンスチームを発生させるリボイラーの様式のものなど、を用いることができる。 The clean steam generator 40 is connected to the pure water manufacturing apparatus 50 via, for example, a stainless steel pipe 60. The clean steam generating device 40 is not particularly limited, and a conventionally known device used in the food field, the medical field, or the like, for example, a general steam generated by a boiler as a heat source, is made of stainless steel heat. A reboiler type that generates clean steam in the exchanger can be used.
純水製造装置５０は、水から不純物を取り除いて純水を製造する装置である。純水を製造する原料となる水は、例えば水道水などを用いることができる。純水製造装置５０としては、特に限定されるものではなく、例えば、フィルター、活性炭、イオン交換樹脂、ＲＯ膜（逆浸透膜）、蒸留器、ＥＤＩなどの従来から公知の手段あるいはこれらの手段の２種以上の組み合わせにより、純水を製造することができる。純水は、製法により水質は異なるが、純度が１００％に近い水が好ましく、例えば、電気抵抗率が０．１ＭΩ・ｃｍ以上１５ＭΩ・ｃｍ以下の水が好ましい。 The pure water production apparatus 50 is an apparatus that produces pure water by removing impurities from water. For example, tap water can be used as water as a raw material for producing pure water. The pure water production apparatus 50 is not particularly limited. For example, conventionally known means such as a filter, activated carbon, ion exchange resin, RO membrane (reverse osmosis membrane), distiller, EDI or the like. Pure water can be produced by a combination of two or more. Although pure water has a water quality that varies depending on the production method, water having a purity close to 100% is preferable. For example, water having an electrical resistivity of 0.1 MΩ · cm to 15 MΩ · cm is preferable.
本実施形態の水処理装置１００においては、処理対象の地下水量に応じて、吸着素子１１，１２による１，４−ジオキサンの吸着工程及び吸着素子１１，１２に対する１，４−ジオキサンの脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を変更できるように、運転制御されている。つまり、例えば処理水を食品製造用水として使用する場合、処理水の使用量は例えば時間ごとあるいは日ごとに変動するので、その都度、地下水の揚水量（処理対象の地下水量）に変動が生じる。そこで、地下水の揚水量（処理対象の地下水量）に応じて、前記吸脱着繰り返し周期を変更することで、後述するように、単位時間当たりの吸着素子１１，１２の脱着回数を減少させることができる。その結果、吸着素子１１，１２の脱着処理（さらには脱水処理）に要するクリーンスチームの使用量を減らすことができ、クリーンスチーム発生装置４０での消費電力及び消費水量を減らすことができるので、省エネルギーを実現している。 In the water treatment apparatus 100 of the present embodiment, the adsorption process of 1,4-dioxane by the adsorption elements 11 and 12 and the desorption process of 1,4-dioxane to the adsorption elements 11 and 12 are performed according to the amount of groundwater to be treated. The operation is controlled so that the cycle of one cycle of adsorption / desorption that is executed once can be changed. That is, for example, when the treated water is used as food production water, the amount of treated water varies, for example, every hour or every day, so that the amount of groundwater pumped (the amount of groundwater to be treated) varies each time. Therefore, by changing the adsorption / desorption repetition cycle according to the amount of groundwater pumped (the amount of groundwater to be treated), the number of desorption times of the adsorption elements 11 and 12 per unit time can be reduced as will be described later. it can. As a result, it is possible to reduce the amount of clean steam used for the desorption process (and further the dehydration process) of the adsorbing elements 11 and 12, and to reduce the power consumption and water consumption in the clean steam generator 40, thereby saving energy. Is realized.
具体的に説明すると、地下水導入ラインＬ１に例えば電磁式流量計などの流量計Ｓ１を設置して、単位時間当たりの処理対象の地下水量を測定する。処理対象の地下水量に変動が生じると、ポンプＰを制御して、処理槽１０，２０の吸着素子１１，１２に通流させる単位時間当たりの地下水の通水量を調整し、地下水の通水量は流量計Ｓ２を用いて測定し、地下水の通水量に応じて所望の１，４−ジオキサンの吸着性能を得られる吸着時間となるように吸脱着繰り返し周期を決定し、決定された吸脱着繰り返し周期に応じて、バルブＶ１〜Ｖ１０の開閉操作を行うことができるコンピュータなどの制御手段７０を設置して、水処理装置１００を制御する。 More specifically, a flow meter S1 such as an electromagnetic flow meter is installed in the ground water introduction line L1, and the amount of ground water to be treated per unit time is measured. When the amount of groundwater to be treated varies, the pump P is controlled to adjust the amount of groundwater flow per unit time to be passed through the adsorption elements 11 and 12 of the treatment tanks 10 and 20. Measured using the flow meter S2, and determined the adsorption / desorption repetition period so as to obtain an adsorption time for obtaining the desired 1,4-dioxane adsorption performance according to the amount of groundwater flow, and the determined adsorption / desorption repetition period Accordingly, the water treatment apparatus 100 is controlled by installing a control means 70 such as a computer that can open and close the valves V1 to V10.
例えば、処理対象の地下水量が減少した場合、吸着素子１１，１２への地下水の通水量を下げ、その分、吸着素子１１，１２による吸着時間を長くして吸脱着繰り返し周期を長くすることで、吸着素子１１，１２による１，４−ジオキサンの吸着性能を維持したまま、単位時間当たりの吸着素子１１，１２の脱着回数が減少する。また、処理対象の地下水量が減少した場合、吸着素子１１，１２への地下水の通水量を変更せず、かつ、吸着工程において吸着素子１１，１２による吸着時間も変更しないまま吸着処理後に待機時間をとって吸脱着繰り返し周期を長くすることで、吸着素子１１，１２による１，４−ジオキサンの吸着性能を維持したまま、単位時間当たりの吸着素子１１，１２の脱着回数が減少する。ここで、脱着処理では、吸着素子１１，１２に対して、毎回同じ量のクリーンスチームを供給することになる。例えば、吸着素子１１，１２の重量が１０ｋｇであり、その２倍の重量のクリーンスチームを脱着処理に使用する場合、脱着処理では常に１回当たり２０ｋｇのクリーンスチームを使用することになる。吸着時間を長くする、あるいは、吸着処理後に待機時間をとり、単位時間当たりの脱着回数を減らすことで、クリーンスチームの使用量を削減することができるうえ、クリーンスチーム発生装置４０にてクリーンスチームを製造するために必要な消費電力及び消費水量を減らすことができるので、水処理装置１００全体で、省エネルギー（低コスト）を実現することができる。吸着素子１１，１２への地下水の通水量や吸脱着繰り返し周期は、処理すべき地下水の量や所望の１，４−ジオキサンの吸着性能を達成できる条件に基づき、制御手段７０により変更制御される。 For example, when the amount of groundwater to be treated is reduced, the amount of groundwater flow to the adsorption elements 11 and 12 is lowered, and the adsorption time by the adsorption elements 11 and 12 is lengthened accordingly, and the adsorption / desorption repetition cycle is lengthened. While the adsorption performance of 1,4-dioxane by the adsorption elements 11 and 12 is maintained, the number of desorption times of the adsorption elements 11 and 12 per unit time is reduced. In addition, when the amount of groundwater to be treated decreases, the waiting time after the adsorption treatment without changing the amount of groundwater flow to the adsorption elements 11 and 12 and without changing the adsorption time by the adsorption elements 11 and 12 in the adsorption process. By taking the adsorption / desorption repetition period longer, the number of desorption times of the adsorbing elements 11 and 12 per unit time decreases while maintaining the adsorption performance of 1,4-dioxane by the adsorbing elements 11 and 12. Here, in the desorption process, the same amount of clean steam is supplied to the adsorption elements 11 and 12 each time. For example, when the weights of the adsorbing elements 11 and 12 are 10 kg and clean steam having twice the weight is used for the desorption process, the desorption process always uses 20 kg of clean steam. It is possible to reduce the amount of clean steam used by increasing the adsorption time or by waiting after the adsorption process and reducing the number of desorptions per unit time. Since power consumption and water consumption required for manufacturing can be reduced, energy saving (low cost) can be realized in the water treatment apparatus 100 as a whole. The amount of groundwater flow to the adsorption elements 11 and 12 and the adsorption / desorption repetition cycle are changed and controlled by the control means 70 based on the amount of groundwater to be treated and the conditions for achieving the desired 1,4-dioxane adsorption performance. .
以上、図１を用いて説明した本実施形態の水処理システムＳ及び水処理装置１００では、説明の簡略のため、ポンプやファンなどの流体搬送手段やストレージタンクなどの流体貯留手段などの構成要素を示していないが、これら構成要素は必要に応じて適宜の位置に配置すればよい。 As described above, in the water treatment system S and the water treatment apparatus 100 of the present embodiment described with reference to FIG. 1, components such as a fluid transporting unit such as a pump and a fan and a fluid storage unit such as a storage tank are provided for the sake of simplicity. However, these components may be arranged at appropriate positions as necessary.
［実施形態２］
図２は、本発明に係る水処理装置を備えた水処理システムの他の実施形態の概略構成を示している。なお、本実施形態の水処理システムＳ’は、水処理装置１００と、水処理装置１００にクリーンスチームを供給するクリーンスチーム発生装置４０と、純水を製造する純水製造装置５０とを備えていて、基本的な構成は、上述した実施形態１で説明した水処理システムＳの構成と同様であり、ここでは対応する構成に同一の符号を付することで説明を省略する。
[Embodiment 2]
FIG. 2 shows a schematic configuration of another embodiment of the water treatment system including the water treatment apparatus according to the present invention. The water treatment system S ′ of the present embodiment includes a water treatment apparatus 100, a clean steam generation apparatus 40 that supplies clean steam to the water treatment apparatus 100, and a pure water production apparatus 50 that produces pure water. The basic configuration is the same as the configuration of the water treatment system S described in the first embodiment, and the description thereof is omitted here by assigning the same reference numerals to the corresponding configurations.
一方で、本実施形態の水処理システムＳ’は、実施形態１の水処理システムＳに対して、以下の通り、水処理装置１００の制御方法が異なる。つまり、実施形態１の水処理システムＳでは、水処理装置１００は、処理対象の地下水量に応じて１サイクルの吸脱着繰り返し周期を変更できるように運転制御されるのに対して、本実施形態では、水処理装置１００は、処理対象の地下水の１，４−ジオキサン濃度に応じて、吸着素子１１，１２による１，４−ジオキサンの吸着工程及び吸着素子１１，１２に対する１，４−ジオキサンの脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を変更できるように運転制御される。つまり、例えば処理水を食品製造用水として使用する場合、処理水の１，４−ジオキサン濃度は季節などで変動する。そこで、地下水の１，４−ジオキサン濃度に応じて、前記吸脱着繰り返し周期を変更することで、後述するように、単位時間当たりの吸着素子１１，１２の脱着回数を減少させることができる。その結果、吸着素子１１，１２の脱着処理（さらには脱水処理）に要するクリーンスチームの使用量を減らすことができ、クリーンスチーム発生装置４０での消費電力及び消費水量を減らすことができるので、省エネルギーを実現している。 On the other hand, the water treatment system S ′ of the present embodiment differs from the water treatment system S of the first embodiment in the control method of the water treatment apparatus 100 as follows. That is, in the water treatment system S of the first embodiment, the water treatment apparatus 100 is controlled to be able to change the cycle of adsorption / desorption of one cycle according to the amount of groundwater to be treated, whereas the present embodiment. Then, according to the 1,4-dioxane concentration of the ground water to be treated, the water treatment apparatus 100 is configured to adsorb 1,4-dioxane by the adsorption elements 11 and 12 and 1,4-dioxane to the adsorption elements 11 and 12. Operation control is performed so that the adsorption / desorption repetition cycle of one cycle in which the desorption process is executed once can be changed. That is, for example, when the treated water is used as food production water, the 1,4-dioxane concentration of the treated water varies depending on the season. Therefore, by changing the adsorption / desorption repetition cycle according to the 1,4-dioxane concentration of groundwater, the number of desorptions of the adsorption elements 11 and 12 per unit time can be reduced as described later. As a result, it is possible to reduce the amount of clean steam used for the desorption process (and further the dehydration process) of the adsorbing elements 11 and 12, and to reduce the power consumption and water consumption in the clean steam generator 40, thereby saving energy. Is realized.
具体的に説明すると、地下水導入ラインＬ１に例えば全有機体炭素計（ＴＯＣ計）やヘッドスペース−ガスクロマトグラフ質量分析装置などの濃度計Ｃを設置して、単位時間当たりの処理対象の１，４−ジオキサン濃度を測定する。処理対象の１，４−ジオキサン濃度に変動が生じると、ポンプＰを制御して、処理槽１０，２０の吸着素子１１，１２に通流させる単位時間当たりの地下水の通水量を調整し、地下水の通水量は流量計Ｓを用いて測定し、地下水の通水量に応じて所望の１，４−ジオキサンの吸着性能を得られる吸着時間となるように吸脱着繰り返し周期を決定し、決定された吸脱着繰り返し周期に応じて、バルブＶ１〜Ｖ１０の開閉操作を行うことができるコンピュータなどの制御手段７０を設置して、水処理装置１００を制御する。 More specifically, for example, a concentration meter C such as a total organic carbon meter (TOC meter) or a headspace gas chromatograph mass spectrometer is installed in the groundwater introduction line L1, and 1, 4 of processing objects per unit time are obtained. -Measure the dioxane concentration. When fluctuations occur in the 1,4-dioxane concentration to be treated, the pump P is controlled to adjust the amount of groundwater flow per unit time that flows through the adsorption elements 11 and 12 of the treatment tanks 10 and 20, The flow rate of water was measured using a flow meter S, and the adsorption / desorption repetition cycle was determined according to the flow rate of groundwater to determine the adsorption time for obtaining the desired 1,4-dioxane adsorption performance. A control means 70 such as a computer capable of opening and closing the valves V1 to V10 is installed according to the adsorption / desorption repetition cycle to control the water treatment apparatus 100.
例えば、処理対象の１，４ージオキサン濃度が減少した場合、吸着素子１１，１２による吸着時間を長くして吸脱着繰り返し周期を長くすることで、吸着素子１１，１２による１，４−ジオキサンの吸着性能を維持したまま、単位時間当たりの吸着素子１１，１２の脱着回数が減少する。例えば、吸着素子１１，１２の重量が１０ｋｇであり、その２倍の重量のクリーンスチームを脱着処理に使用する場合、脱着処理では常に１回当たり２０ｋｇのクリーンスチームを使用することになる。吸着時間を長くして、単位時間当たりの脱着回数を減らすことで、クリーンスチームの使用量を削減することができるうえ、クリーンスチーム発生装置４０にてクリーンスチームを製造するために必要な消費電力及び消費水量を減らすことができるので、水処理装置１００全体で、省エネルギー（低コスト）を実現することができる。吸着素子１１，１２への地下水の通水量や吸脱着繰り返し周期は、処理すべき地下水の量や所望の１，４−ジオキサンの吸着性能を達成できる条件に基づき、制御手段７０により変更制御される。 For example, when the concentration of 1,4-dioxane to be treated is decreased, the adsorption time of the adsorption elements 11 and 12 is lengthened and the adsorption / desorption repetition cycle is lengthened, whereby the adsorption of 1,4-dioxane by the adsorption elements 11 and 12 is performed. The number of desorption times of the adsorption elements 11 and 12 per unit time decreases while maintaining the performance. For example, when the weights of the adsorbing elements 11 and 12 are 10 kg and clean steam having twice the weight is used for the desorption process, the desorption process always uses 20 kg of clean steam. By increasing the adsorption time and reducing the number of desorptions per unit time, it is possible to reduce the amount of clean steam used, as well as the power consumption necessary for producing clean steam with the clean steam generator 40 and Since the amount of water consumption can be reduced, energy saving (low cost) can be realized in the entire water treatment apparatus 100. The amount of groundwater flow to the adsorption elements 11 and 12 and the adsorption / desorption repetition cycle are changed and controlled by the control means 70 based on the amount of groundwater to be treated and the conditions for achieving the desired 1,4-dioxane adsorption performance. .
なお、１サイクルの吸脱着繰り返し周期を、処理対象の地下水量及び地下水中の１，４−ジオキサン濃度の両方に応じて制御してもよい。 In addition, you may control 1 cycle of adsorption / desorption repetition periods according to both the amount of groundwater of a process target, and the 1, 4- dioxane density | concentration in groundwater.
以上、本発明の実施形態についてそれぞれ説明したが、上述した各実施形態は、全ての点で例示であって制限的なものではないため、本発明は上述した各実施形態に限定されるものではない。本発明の技術的範囲は、特許請求の範囲によって画定され、また特許請求の範囲の記載と均等の意味および範囲内での全ての変更を含むものであり、よって、本発明は、本発明の趣旨を逸脱しない限りにおいて種々の変更が可能である。 As mentioned above, although each embodiment of this invention was described, since each embodiment mentioned above is an illustration and restrictive at no points, this invention is not limited to each embodiment mentioned above. Absent. The technical scope of the present invention is defined by the scope of claims, and includes all modifications within the meaning and scope equivalent to the description of the scope of claims. Various changes can be made without departing from the spirit of the invention.
例えば、上述した各実施形態では、水処理装置１００は、吸着素子が複数（図１では２つ）の処理槽にそれぞれ収容され、吸着工程を行う部位（処理槽）と脱着工程を行う部位（処理槽）とを交互に切り替える、前記吸着素子の前記脱着工程が行われた部分を前記吸着工程を行う部分に移行させるとともに、前記吸着素子の前記吸着工程が行われた部分を前記脱着工程を行う部分に移行させる操作が繰り返し実施されることで、吸着素子による吸着工程が連続して行われる構成となっている。しかし、吸着素子を回転可能とし、吸着素子の回転により、吸着工程で１，４−ジオキサンを吸着した吸着素子の部位を脱着工程へ移行させるようにし、脱着工程で１，４−ジオキサンが脱着された吸着素子の部位を吸着工程へ移行させる操作を繰り返し実施するように水処理装置１００を構成することによっても、水処理装置１００として吸着素子による吸着工程を連続して行うことが可能である。 For example, in each of the above-described embodiments, the water treatment apparatus 100 includes a plurality of (two in FIG. 1) adsorption tanks as the adsorption elements, and a site for performing the adsorption process (treatment tank) and a site for performing the desorption process ( The portion where the desorption step of the adsorption element is switched to the treatment tank is shifted to the portion where the adsorption step is performed, and the portion of the adsorption element where the adsorption step is performed is changed to the desorption step. The operation of shifting to the portion to be performed is repeatedly performed, so that the adsorption process by the adsorption element is continuously performed. However, the adsorbing element can be rotated, and by rotating the adsorbing element, the portion of the adsorbing element that has adsorbed 1,4-dioxane in the adsorption process is transferred to the desorption process, and 1,4-dioxane is desorbed in the desorption process. By configuring the water treatment apparatus 100 so as to repeatedly perform the operation of shifting the site of the adsorption element to the adsorption process, the adsorption process using the adsorption element can be continuously performed as the water treatment apparatus 100.
また、必ずしも吸着素子による吸着工程が連続して行われるように水処理装置１００を構成する必要はなく、処理槽を１つとし、脱着工程中は処理槽への地下水の供給を一時的にストップしてタンクなどに貯水し、脱着工程後の吸着工程で一時的に貯水された地下水も併せて吸着処理する構成としてもよい。 In addition, it is not always necessary to configure the water treatment apparatus 100 so that the adsorption process by the adsorption element is continuously performed, and one treatment tank is provided, and the supply of groundwater to the treatment tank is temporarily stopped during the desorption process. Then, the water may be stored in a tank or the like, and the groundwater temporarily stored in the adsorption process after the desorption process may also be adsorbed.
以下に本発明の実施例を示し、本発明をより具体的に説明するが、本発明は、以下の実施例に限定されるものではない。以下の実施例では、実施形態１で説明した水処理システムＳを用いた。なお、評価は下記の方法により行った。 Examples of the present invention will be shown below to describe the present invention more specifically. However, the present invention is not limited to the following examples. In the following examples, the water treatment system S described in the first embodiment was used. The evaluation was performed by the following method.
（ＢＥＴ比表面積）
ＢＥＴ比表面積は、液体窒素の沸点（−１９５．８℃）雰囲気下、相対圧力０．０〜０．１５の範囲で上昇させたときの試料への窒素吸着量を数点測定し、ＢＥＴプロットにより試料単位質量あたりの表面積（ｍ２／ｇ）を求めた。
(BET specific surface area)
The BET specific surface area was measured by measuring the amount of nitrogen adsorbed on the sample when the relative pressure was raised in the range of 0.0 to 0.15 in the atmosphere of the boiling point of liquid nitrogen (-195.8 ° C), and a BET plot. Was used to determine the surface area (m 2 / g) per unit mass of the sample.
（細孔容積）
細孔容積は、相対圧０．９５における窒素ガスの気体吸着法により測定した。
(Pore volume)
The pore volume was measured by a nitrogen gas adsorption method at a relative pressure of 0.95.
（平均細孔径）
平均細孔径は、以下の式で求めた。
ｄｐ＝４００００Ｖｐ／Ｓ（ただし、ｄｐ：平均細孔径（Å）、Ｖｐ：細孔容積（ｃｃ／ｇ）、Ｓ：ＢＥＴ比表面積（ｍ２／ｇ）である。）
(Average pore diameter)
The average pore diameter was determined by the following formula.
dp = 40000 Vp / S (where dp: average pore diameter (Å), Vp: pore volume (cc / g), S: BET specific surface area (m 2 / g))
（処理条件及び設計条件）
本発明の実施例の説明にあたり、地下水の１，４−ジオキサン濃度は０．２ｍｇ／Ｌ、水温は１７℃、吸着素子への通水量を２２０Ｌ／ｈとした場合の処理条件において、地下水中の１，４−ジオキサンの処理性能として、地下水中の１，４−ジオキサン除去率を９０％以上確保できる水処理装置の設計条件を以下に示す。水処理装置は、図１に示す実施形態１の通りに吸着素子をそれぞれ有する処理槽を２つ備えた構成とし、吸着素子は、平均細孔径が１７．２（Å）、ＢＥＴ比表面積が２０５０ｍ２／ｇ、全細孔容積が０．８７ｍ３／ｇの活性炭素繊維の不織布を２０ｋｇ積層したものを用いた。また、脱水処理及び脱着処理で使用するクリーンスチームは０．１ＭＰａ、１２０℃の条件で一定速度で供給した。吸脱着繰り返し周期は、図３に示す通り、吸着工程が２０ｍｉｎ、脱着工程が２０ｍｉｎ（自重抜き時間：５ｍｉｎ、脱水時間：３ｍｉｎ、脱着時間：９ｍｉｎ、待機時間：３ｍｉｎ）とした。脱着工程後に排出される脱着ガスは、図１に示す通り、地下水にて間接的に液化凝縮され、濃縮水として排出される。この設計条件における使用冷却水（脱着ガスの冷却水）は０ｍ３／ｈ、クリーンスチームの使用量は１．５ｋｇ／ｈ、濃縮水量は１．７Ｌ／ｈであった。濃縮水は、産廃で二次処理されるものとした。冷却水単価は１０円／ｍ３、クリーンスチーム単価は４円／ｋｇ、産廃単価は２０円／Ｌとすると、単位処理水量当りの冷却水コストは０円／ｍ３、クリーンスチームコストは２７円／ｍ３、濃縮水の二次処理コストは１５５円／ｍ３となった。
(Processing conditions and design conditions)
In the description of the examples of the present invention, the groundwater 1,4-dioxane concentration is 0.2 mg / L, the water temperature is 17 ° C., and the treatment conditions when the water flow rate to the adsorption element is 220 L / h, As the treatment performance of 1,4-dioxane, the design conditions of a water treatment apparatus capable of ensuring 90% or more of the 1,4-dioxane removal rate in groundwater are shown below. As shown in FIG. 1, the water treatment apparatus has two treatment tanks each having an adsorption element, and the adsorption element has an average pore diameter of 17.2 (１７) and a BET specific surface area of 2050 m. A laminate of 20 kg of a nonwoven fabric of activated carbon fibers having a total pore volume of 0.87 m 3 / g was used. The clean steam used in the dehydration process and desorption process was supplied at a constant rate under the conditions of 0.1 MPa and 120 ° C. As shown in FIG. 3, the adsorption / desorption repetition cycle was 20 min for the adsorption process and 20 min for the desorption process (self-drainage time: 5 min, dehydration time: 3 min, desorption time: 9 min, standby time: 3 min). As shown in FIG. 1, the desorption gas discharged after the desorption step is indirectly liquefied and condensed in ground water and discharged as concentrated water. The cooling water used (cooling water for the desorption gas) was 0 m 3 / h, the amount of clean steam used was 1.5 kg / h, and the amount of concentrated water was 1.7 L / h. Concentrated water was assumed to be secondarily treated by industrial waste. If the cooling water unit price is 10 yen / m 3 , the clean steam unit price is 4 yen / kg, the industrial waste unit price is 20 yen / L, the cooling water cost per unit treated water volume is 0 yen / m 3 , and the clean steam cost is 27 yen. / M 3 , the secondary treatment cost of the concentrated water was 155 yen / m 3 .
（１，４−ジオキサンの除去効果）
各処理槽の入口及び出口の１，４−ジオキサン濃度をヘッドスペース−ガスクロマトグラフ質量分析法により定量した。水処理における１，４−ジオキサンの除去率（％）は、１００−（処理水中の１，４−ジオキサン濃度／処理対象の地下水中の１，４−ジオキサン濃度）×１００とした。
(Removal effect of 1,4-dioxane)
The concentration of 1,4-dioxane at the inlet and outlet of each treatment tank was quantified by headspace gas chromatography mass spectrometry. The removal rate (%) of 1,4-dioxane in water treatment was 100- (1,4-dioxane concentration in treated water / 1,4-dioxane concentration in ground water to be treated) × 100.
［実施例１］
上述の設計条件において、処理対象の地下水量の減少に伴い、吸着素子への通水量を１１０Ｌ／ｈに低下した場合に、脱着工程の待機時間を２３ｍｉｎに変更して脱着工程を吸着工程とともに４０ｍｉｎとする吸脱着繰り返し周期の操作条件に変更する制御を導入した。上述の制御においても、設計条件と同等（除去率が９０％以上）の地下水中の１，４−ジオキサンの処理性能を実現できるうえで、上記の制御により、吸脱着繰り返し周期が長くなり、吸着素子に対する単位時間当たりの脱着回数が減るため、クリーンスチームの使用量が０．７５ｋｇ／ｈとなり、設計条件に対して５０％以上削減でき、濃縮水量も０．８５Ｌ／ｈ以下と設計条件に対して２倍以上の濃縮が可能であった。一方で、単位処理水量当たりの冷却水コストは０円／ｍ３、クリーンスチームコストは２７円／ｍ３、濃縮水の二次処理コストは１５５円／ｍ３となり、設計条件とほぼ同じコストでの処理を維持できた。
[Example 1]
Under the above design conditions, when the amount of water flow to the adsorption element is reduced to 110 L / h with the decrease in the amount of groundwater to be treated, the desorption process wait time is changed to 23 min and the desorption process is made 40 min with the adsorption process. Introduced a control to change the operating conditions of the adsorption / desorption cycle. Even in the above control, the treatment performance of 1,4-dioxane in the groundwater equivalent to the design conditions (removal rate of 90% or more) can be realized, and the above control increases the adsorption / desorption repetition cycle, and the adsorption. Since the number of desorptions per unit time to the device is reduced, the amount of clean steam used is 0.75 kg / h, which can be reduced by 50% or more with respect to design conditions, and the amount of concentrated water is 0.85 L / h or less with respect to design conditions. More than twice as much concentration was possible. On the other hand, the cooling water cost per unit treated water amount is 0 yen / m 3 , the clean steam cost is 27 yen / m 3 , and the secondary treatment cost of concentrated water is 155 yen / m 3 , which is almost the same as the design conditions. We were able to maintain the processing.
［実施例２］
上述の設計条件において、処理対象の地下水量の減少に伴い、吸着素子への通水量を５５Ｌ／ｈに低下した場合に、脱着工程の待機時間を６３ｍｉｎに変更して脱着工程を吸着工程とともに８０ｍｉｎとする吸脱着繰り返し周期の操作条件に変更する制御を導入した。上述の制御においても、設計条件と同等（除去率が９０％以上）の地下水中の１，４−ジオキサンの処理性能を実現できるうえで、上記の制御により、吸着素子に対する単位時間当たりの脱着回数が実勢例１よりもさらに減るため、クリーンスチームの使用量が０．４ｋｇ／ｈとなり、設計条件に対して７０％以上削減でき、濃縮水量も０．４５Ｌ／ｈ以下と設計条件に対して３．７倍以上の濃縮が可能であった。一方で、単位処理水量当たりの冷却水コストは０円／ｍ３、クリーンスチームコストは２９円／ｍ３、濃縮水の二次処理コストは１６３円／ｍ３となり、設計条件とほぼ同じコストでの処理を維持できた。
[Example 2]
Under the above-mentioned design conditions, when the amount of water flow to the adsorption element is reduced to 55 L / h as the amount of groundwater to be treated decreases, the desorption process standby time is changed to 63 min and the desorption process is made 80 min together with the adsorption process. Introduced a control to change the operating conditions of the adsorption / desorption cycle. Even in the above control, the processing performance of 1,4-dioxane in groundwater equivalent to the design conditions (removal rate of 90% or more) can be realized, and the number of desorptions per unit time with respect to the adsorbing element by the above control. However, since the amount of clean steam used is 0.4 kg / h, it can be reduced by 70% or more with respect to the design conditions, and the amount of concentrated water is 0.45 L / h or less, which is 3 for the design conditions. It was possible to concentrate more than 7 times. On the other hand, the cooling water cost per unit treated water amount is 0 yen / m 3 , the clean steam cost is 29 yen / m 3 , and the secondary treatment cost of concentrated water is 163 yen / m 3 , which is almost the same as the design conditions. We were able to maintain the processing.
［比較例１］
上述の設計条件において、本発明における制御を導入しなかった場合に、設計条件記載の処理条件から、処理対象の地下水量の減少に伴い、吸着素子への通水量を１１０Ｌ／ｈに低下した場合には、クリーンスチームの使用量は１．５ｋｇ／ｈ、濃縮水量は１．７Ｌ／ｈ以下であり、実施例１と比較して、２倍のクリーンスチームの使用量が必要であり、２倍の量の濃縮水が排出された。また、単位処理水量当たりの冷却水コストは０円／ｍ３であるが、クリーンスチームコストは５４円／ｍ３、濃縮水の二次処理コストは３０９円／Ｌとなり、設計条件の約２倍のコストを要した。
[Comparative Example 1]
When the control in the present invention is not introduced in the above design conditions, the water flow rate to the adsorbing element is reduced to 110 L / h from the processing conditions described in the design conditions as the amount of groundwater to be processed decreases. The amount of clean steam used is 1.5 kg / h, and the amount of concentrated water is 1.7 L / h or less. Compared with Example 1, twice the amount of clean steam used is required. Amount of concentrated water was discharged. The cooling water cost per unit treated water amount is 0 yen / m 3 , but the clean steam cost is 54 yen / m 3 , and the secondary treatment cost of concentrated water is 309 yen / L, approximately twice the design conditions. Cost.
［比較例２］
上述の設計条件において、本発明における制御を導入しなかった場合に、設計条件記載の処理条件から、処理対象の地下水量の減少に伴い、吸着素子への通水量を５５Ｌ／ｈに低下した場合には、クリーンスチームの使用量は１．５ｋｇ／ｈ、濃縮水量は１．７Ｌ／ｈ以下であり、実施例１と比較して、２倍のクリーンスチームの使用量が必要であり、２倍の量の濃縮水が排出された。また、単位処理水量当たりの冷却水コストは０円／ｍ３であるが、クリーンスチームコストは１０９円／ｍ３、濃縮水の二次処理コストは６１８円／Ｌとなり、設計条件の約４倍のコストを要した。
[Comparative Example 2]
When the control in the present invention is not introduced in the design conditions described above, the water flow rate to the adsorbing element is reduced to 55 L / h from the processing conditions described in the design conditions as the amount of groundwater to be processed decreases. The amount of clean steam used is 1.5 kg / h, and the amount of concentrated water is 1.7 L / h or less. Compared with Example 1, twice the amount of clean steam used is required. Amount of concentrated water was discharged. The cooling water cost per unit treated water amount is 0 yen / m 3 , but the clean steam cost is 109 yen / m 3 , and the secondary treatment cost of concentrated water is 618 yen / L, which is about 4 times the design conditions. Cost.
［比較例３］
上述の設計条件において、処理対象の地下水量の減少に伴い、吸着素子への通水量を１１０Ｌ／ｈに低下した場合に、待機時間を２３ｍｉｎに変更して脱着工程を吸着工程とともに４０ｍｉｎとする吸脱着繰り返し周期の操作条件に変更する制御を導入した。しかし、脱着ガスを冷却するための冷却水として、冷却塔から供給される冷却水(水温３２℃)を使用し、処理対象の地下水は、脱着ガスとの熱交換を行うことなく、直接吸着素子へ通流させた。上記の制御により、吸着素子に対する単位時間当たりの脱着回数が減るため、クリーンスチームの使用量が０．７５ｋｇ／ｈとなり、設計条件に対して５０％以上削減でき、濃縮水量も０．８５Ｌ／ｈ以下と設計条件に対して２倍以上の濃縮が可能であった。しかし、冷却水の使用量は０．４ｍ３／ｈであった。そのため、クリーンスチームコストは２７円／ｍ３、濃縮水の二次処理コストは１５５円／ｍ３と設計条件とほぼ同じコストである一方で、単位処理水量当たりの冷却水コストは３６円／ｍ３となり、設計条件以上のコストを要した。
[Comparative Example 3]
Under the above design conditions, when the water flow rate to the adsorption element is reduced to 110 L / h as the amount of groundwater to be treated decreases, the standby time is changed to 23 min and the desorption process is set to 40 min together with the adsorption process. Introduced control to change the operating conditions of the desorption cycle. However, the cooling water (water temperature 32 ° C.) supplied from the cooling tower is used as the cooling water for cooling the desorption gas, and the groundwater to be treated is directly adsorbed without exchanging heat with the desorption gas. It was made to flow to. With the above control, the number of desorptions per unit time with respect to the adsorbing element is reduced, so the amount of clean steam used is 0.75 kg / h, which can be reduced by 50% or more with respect to the design conditions, and the amount of concentrated water is 0.85 L / h. It was possible to concentrate more than twice the following and design conditions. However, the amount of cooling water used was 0.4 m 3 / h. Therefore, the clean steam cost is 27 yen / m 3 and the secondary treatment cost for concentrated water is 155 yen / m 3 , which is almost the same as the design conditions, while the cooling water cost per unit treated water volume is 36 yen / m. 3 next, took a cost of more than design conditions.
以上の結果から、実施例１，２は、比較例１，２と比べて、クリーンスチームの使用量が少なく、濃縮水量も少ないことが分かる。よって、本発明における制御を導入した実施例１，２では、本発明における制御を導入しなかった比較例１，２に比べて、脱着処理に必要なエネルギーが低減できるうえ、濃縮水の処理エネルギーを低減できることが確認される。よって、水処理装置全体で、省エネルギー（低コスト）にて水処理が可能であることが確認される。また、実施例１，２は、本発明における制御を導入することで、処理対象の地下水量が変動しても、設計条件とほぼ同じコストでの処理を実現できることが確認された。 From the above results, it can be seen that Examples 1 and 2 use less clean steam and less concentrated water than Comparative Examples 1 and 2. Therefore, in Examples 1 and 2 in which the control according to the present invention is introduced, the energy required for the desorption treatment can be reduced as compared with Comparative Examples 1 and 2 in which the control according to the present invention is not introduced. It is confirmed that can be reduced. Therefore, it is confirmed that the entire water treatment apparatus can perform water treatment with energy saving (low cost). Moreover, it was confirmed that Example 1 and 2 can implement | achieve the process at the cost substantially the same as design conditions, even if the amount of groundwater to be processed fluctuates by introducing the control in the present invention.
さらに、実施例１，２は、比較例３と比べて、脱着ガスを冷却するための冷却水として、処理対象の地下水を用いることで、冷却水の使用量を削減できることが分かる。よって、低コストにて水処理が可能であることが確認される。 Furthermore, compared with the comparative example 3, Example 1, 2 shows that the usage-amount of cooling water can be reduced by using the groundwater of a process target as cooling water for cooling desorption gas. Therefore, it is confirmed that water treatment is possible at low cost.
本発明による水処理装置、水処理システム及び水処理方法は、例えば食品製造に使用する食品製造用水を製造する目的で、地下水中から１，４−ジオキサンを除去する装置、システム及び方法に好適に利用することができ、産業界に大いに寄与できる。 The water treatment apparatus, water treatment system, and water treatment method according to the present invention are suitable for an apparatus, system, and method for removing 1,4-dioxane from groundwater, for example, for the purpose of producing water for food production used in food production. It can be used and can greatly contribute to the industry.
１０ 処理槽
１１ 吸着素子
１２ 吸着素子
２０ 処理槽
３０ 凝縮器
４０ クリーンスチーム発生装置
５０ 純水製造装置
７０ 制御手段
１００ 水処理装置
Ｌ１ 地下水導入ライン（水流通部）
Ｌ２ 処理水排出ライン（水流通部）
Ｌ３ クリーンスチーム供給ライン（クリーンスチーム通気部）
Ｌ４ クリーンスチーム排出ライン
Ｌ５ 還流ライン（返送ルート）
Ｖ１〜Ｖ１０ バルブ
Ｓ，Ｓ’ 水処理システム
DESCRIPTION OF SYMBOLS 10 Treatment tank 11 Adsorption element 12 Adsorption element 20 Treatment tank 30 Condenser 40 Clean steam generator 50 Pure water production apparatus 70 Control means 100 Water treatment apparatus L1 Groundwater introduction line (water distribution part)
L2 treated water discharge line (water distribution department)
L3 Clean steam supply line (clean steam ventilation section)
L4 Clean steam discharge line L5 Reflux line (return route)
V1-V10 Valve S, S 'Water treatment system
Claims (14)
前記吸着素子にクリーンスチームを通気させて、前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着工程と、を順に繰り返し実行し、
前記吸着工程及び前記脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更することを特徴とする水処理装置。 An adsorbing step of allowing groundwater to flow through an adsorbing element containing activated carbon fibers, adsorbing at least 1,4-dioxane in the groundwater to the adsorbing element, and discharging treated water;
The desorption step of desorbing 1,4-dioxane adsorbed on the adsorbing element by allowing clean adsorbing clean steam to the adsorbing element, in order,
Changing the cycle of adsorption / desorption repetition of one cycle in which the adsorption step and the desorption step are executed one by one according to the amount of groundwater to be treated or the 1,4-dioxane concentration in the groundwater to be passed through the adsorption element. Water treatment device characterized by.
前記処理槽に接続され、前記処理槽内の前記吸着素子に地下水を通流させて前記吸着素子に地下水中の少なくとも１，４−ジオキサンを吸着させ、処理水を排出する水通流部と、
前記処理槽に接続され、前記処理槽内の前記吸着素子にクリーンスチームを通気させて前記吸着素子に吸着された１，４−ジオキサンを脱着するクリーンスチーム通気部と、
前記吸着素子による１，４−ジオキサンの吸着工程及び前記吸着素子に対する１，４−ジオキサンの脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更する制御手段と、を備えることを特徴とする水処理装置。 A treatment tank containing an adsorbing element containing activated carbon fibers;
A water flow section connected to the treatment tank, allowing ground water to flow through the adsorption element in the treatment tank to adsorb at least 1,4-dioxane in the ground water to the adsorption element, and discharging treated water;
A clean steam ventilation unit connected to the treatment tank, and allowing desorption of 1,4-dioxane adsorbed on the adsorption element by passing clean steam through the adsorption element in the treatment tank;
An adsorption / desorption repetition cycle of one cycle in which the adsorption process of 1,4-dioxane by the adsorption element and the desorption process of 1,4-dioxane to the adsorption element are performed once each for the treatment target to be passed through the adsorption element. And a control means that changes according to the amount of groundwater or the concentration of 1,4-dioxane in the groundwater.
前記水処理装置にクリーンスチームを供給するクリーンスチーム発生装置と、を備えることを特徴とする水処理システム。 The water treatment device according to any one of claims 1 to 12,
A water treatment system comprising: a clean steam generator for supplying clean water to the water treatment device.
前記吸着素子にクリーンスチームを通気させて、前記吸着素子に吸着された１，４−ジオキサンを脱着する脱着工程と、を順に繰り返し実行し、
前記吸着工程及び前記脱着工程を１回ずつ実行する１サイクルの吸脱着繰り返し周期を、前記吸着素子に通流させる処理対象の地下水量又は地下水中の１，４−ジオキサン濃度に応じて変更することを特徴とする水処理方法。 An adsorbing step of allowing groundwater to flow through an adsorbing element containing activated carbon fibers, adsorbing at least 1,4-dioxane in the groundwater to the adsorbing element, and discharging treated water;
The desorption step of desorbing 1,4-dioxane adsorbed on the adsorbing element by allowing clean adsorbing clean steam to the adsorbing element, in order,
Changing the cycle of adsorption / desorption repetition of one cycle in which the adsorption step and the desorption step are executed one by one according to the amount of groundwater to be treated or the 1,4-dioxane concentration in the groundwater to be passed through the adsorption element. A water treatment method characterized by the above.
Priority Applications (1)
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| CN112645404A (en) * | 2020-12-29 | 2021-04-13 | 绍兴东湖高科股份有限公司 | Continuous pretreatment equipment and method for dichloroethane-containing wastewater of ethephon acidolysis process |
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