JP4996068B2 - Waste water concentration method and apparatus - Google Patents

Waste water concentration method and apparatus Download PDF

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JP4996068B2
JP4996068B2 JP2005184596A JP2005184596A JP4996068B2 JP 4996068 B2 JP4996068 B2 JP 4996068B2 JP 2005184596 A JP2005184596 A JP 2005184596A JP 2005184596 A JP2005184596 A JP 2005184596A JP 4996068 B2 JP4996068 B2 JP 4996068B2
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JP2007000789A (en
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徹 神成
和彦 石田
和人 前川
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Sasakura Engineering Co Ltd
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本発明は，例えば，地下水，又は埋立地浸出水，或いは排煙脱硫装置から排出される廃水等のように有害を不純物を含む廃水を，加熱による沸騰蒸発にて濃縮するようにした処理する方法と，その装置とに関するものである。   The present invention is a method for treating wastewater containing harmful impurities, such as groundwater, landfill leachate, or wastewater discharged from flue gas desulfurization equipment, by boiling evaporation by heating. And the device.

従来，カルシウムを含む地下水，又は埋立地浸出水，或いは排煙脱硫装置から排出される廃水の処理に際しては，その減量化を図るために，間接加熱の沸騰蒸発による蒸発濃縮装置において濃縮することが行われている（特許文献１参照）。   Conventionally, in the treatment of groundwater containing calcium, landfill leachate, or wastewater discharged from flue gas desulfurization equipment, in order to reduce the amount, it is necessary to concentrate in an evaporative concentrator by indirect heating boiling evaporation. (See Patent Document 1).

なお，前記特許文献１には，前記蒸発濃縮装置において濃縮した濃縮廃水は，これを乾燥にて固形化することが記載されている。
特開昭５１−１０２３５７号公報 Note that Patent Document 1 describes that the concentrated waste water concentrated in the evaporative concentration apparatus is solidified by drying.
JP-A-51-102357

しかし，この従来による処理方法は，処理すべき廃水，つまり，被処理廃水の全てを，蒸発濃縮装置に供給して沸騰蒸発するものであることにより，前記蒸発濃縮装置における蒸発負荷が大きいから，当該蒸発濃縮装置における大型化を招来するばかりか，運転コストも可成り嵩むという問題があった。   However, this conventional treatment method supplies the waste water to be treated, that is, all the waste water to be treated, to the evaporation concentrator and evaporates to the boiling point. In addition to causing an increase in the size of the evaporative concentrator, there is a problem that the operating cost is considerably increased.

しかも，前記蒸発濃縮装置からは，純度の高い凝縮水が排出されるものの，この凝縮水は，その温度が可成り高いことにより，この凝縮水を，そのままでは河川等に放流することができず，河川等に放流する場合には，自然環境に悪影響を及ぼすことがない温度の状態にまで冷却するようにしなければならないという問題もあった。   Moreover, although the condensed water with high purity is discharged from the evaporative concentrator, the condensed water cannot be discharged into a river or the like as it is because of its high temperature. However, when it is released into rivers, there is a problem that it must be cooled to a temperature that does not adversely affect the natural environment.

本発明は，廃水に含まれている有害な不純物は，膜を透過するという膜処理にて確実に分離することができる一方，前記膜処理の処理効率は，温度に略比例して向上することに着目し，このことを利用して，前記従来における問題を解消した処理方法と，その装置とを提供することを技術的課題とするものである。   According to the present invention, harmful impurities contained in wastewater can be reliably separated by membrane treatment that permeates the membrane, while the treatment efficiency of the membrane treatment is improved substantially in proportion to the temperature. It is a technical problem to provide a processing method and an apparatus for solving the conventional problems by utilizing this fact.

この技術的課題を達成するため本発明の処理方法は，請求項１に記載したように，
「被処理廃水を，逆浸透膜を使用したＲＯ膜モジュールに供給して，その透過水と非透過水とに分離し，非透過水を，間接加熱にて沸騰蒸発する蒸発濃縮装置に供給して濃縮する一方，前記蒸発濃縮装置における凝縮水にて，前記ＲＯ膜モジュールに供給する被処理廃水を間接加熱する。」
ことを特徴としている。 In order to achieve this technical problem, the processing method of the present invention is as described in claim 1,
“The wastewater to be treated is supplied to an RO membrane module using a reverse osmosis membrane and separated into permeate and non-permeate. The non-permeate is supplied to an evaporative concentrator that evaporates to boiling by indirect heating. On the other hand, the waste water to be treated supplied to the RO membrane module is indirectly heated with the condensed water in the evaporative concentrator.
It is characterized by that.

本発明の処理方法は，請求項２に記載したように，
「被処理廃水を，ナノフィルトレーション膜を使用したＮＦ膜モジュールに供給して，透過水と非透過水とに分離し，その透過水を，逆浸透膜を使用したＲＯ膜モジュールに供給して，透過水と非透過水とに分離し，前記ＮＦ膜モジュール及び前記ＲＯ膜モジュールにおける非透過水を，間接加熱にて沸騰蒸発する蒸発濃縮装置に供給して濃縮する一方，前記蒸発濃縮装置における凝縮水にて，前記ＮＦ膜モジュールに供給する被処理廃水を間接加熱する。」
ことを特徴としている。 The processing method of the present invention, as described in claim 2,
“The wastewater to be treated is supplied to an NF membrane module using a nanofiltration membrane, separated into permeated water and non-permeated water, and the permeated water is supplied to an RO membrane module using a reverse osmosis membrane. The non-permeate water is separated into permeate and non-permeate water, and the non-permeate water in the NF membrane module and the RO membrane module is supplied to the evaporative concentrator for boiling and evaporating by indirect heating. The wastewater to be treated to be supplied to the NF membrane module is indirectly heated with the condensed water in the process. "
It is characterized by that.

次に，本発明の処理装置は，請求項３に記載したように，
「被処理廃水を逆浸透膜にて透過水と非透過水とに分離するＲＯ膜モジュールと，前記ＲＯ膜モジュールにおける非透過水を間接加熱にて沸騰蒸発する蒸発濃縮装置とを備え，更に，前記蒸発濃縮装置における凝縮水を熱源として前記ＲＯ膜モジュールに供給する被処理廃水を間接加熱する熱交換器を備えている。」
ことを特徴としている。 Next, the processing apparatus of the present invention, as described in claim 3,
“A RO membrane module that separates wastewater to be treated into permeate and non-permeate water using a reverse osmosis membrane, and an evaporative concentration device that evaporates the non-permeate water in the RO membrane module by indirect heating. It includes a heat exchanger that indirectly heats the wastewater to be treated supplied to the RO membrane module using the condensed water in the evaporative concentration apparatus as a heat source. "
It is characterized by that.

本発明の処理装置は，請求項４に記載したように，
「被処理廃水をナノフィルトレーション膜にて透過水と非透過水とに分離するＮＦ膜モジュールと，このＮＦ膜モジュールにおける透過水を逆浸透膜にて透過水と非透過水とに分離するＲＯ膜モジュールと，前記ＮＦ膜モジュール及び前記ＲＯ膜モジュールにおける非透過水を間接加熱にて沸騰蒸発する蒸発濃縮装置とを備え，更に，前記蒸発濃縮装置における凝縮水を熱源として前記ＮＦ膜モジュールに供給する被処理廃水を間接加熱する熱交換器を備えている。」
ことを特徴としている。 The processing apparatus of the present invention is as described in claim 4,
“An NF membrane module that separates wastewater to be treated into permeate and non-permeate water using a nanofiltration membrane, and permeate water in this NF membrane module is separated into permeate and non-permeate water using a reverse osmosis membrane. An RO membrane module; an NF membrane module; and an evaporating and concentrating device for boiling and evaporating non-permeate water in the RO membrane module by indirect heating. It has a heat exchanger that indirectly heats the wastewater to be treated. "
It is characterized by that.

請求項１及び３の記載において，被処理廃水を，逆浸透膜を使用したＲＯ膜モジュールに供給することにより，この被処理廃水を，不純物を含まないか殆ど含まない純水な透過水と，不純物を含む非透過水とに膜分離することができるから，前記非透過水を，蒸発濃縮装置に供給して濃縮処理することにより，この蒸発濃縮装置において濃縮処理する廃水の量を，前記ＲＯ膜モジュールにおける透過水の分だけ少なくできて，蒸発濃縮装置における蒸発負荷を軽減できるから，蒸発濃縮装置を小型化できるとともに，運転コストを低減することができる。   In claim 1 and 3, by supplying the wastewater to be treated to the RO membrane module using the reverse osmosis membrane, the wastewater to be treated is pure permeated water containing little or no impurities, Since the membrane can be separated into impervious water containing impurities, the amount of waste water to be concentrated in the evaporative concentrator is reduced by supplying the impervious water to the evaporative concentrator and concentrating. Since the amount of permeated water in the membrane module can be reduced and the evaporation load in the evaporation concentrator can be reduced, the evaporation concentrator can be reduced in size and the operating cost can be reduced.

そして，前記蒸発濃縮装置における凝縮水によって，前記ＲＯ膜モジュールに供給する被処理廃水を，熱交換器において間接加熱することにより，前記被処理廃水における温度を高くすることができるから，前記ＲＯ膜モジュールにおける処理効率を大幅に向上することができ，ＲＯ膜モジュールを小型化できる一方，前記凝縮水における温度を下げることができ，この凝縮水を，殊更，冷却することなく，そのまま，河川等に放流することが可能になる。   Since the wastewater to be treated supplied to the RO membrane module is indirectly heated in the heat exchanger by the condensed water in the evaporative concentrator, the temperature in the wastewater to be treated can be increased. The processing efficiency in the module can be greatly improved, and the RO membrane module can be reduced in size, while the temperature in the condensed water can be lowered, and the condensed water can be used as it is in the river without further cooling. It becomes possible to discharge.

つまり，請求項１及び３に記載した発明によると，蒸発濃縮装置における蒸発負荷を，その前処理としてのＲＯ膜モジュールにて軽減することができて，その小型化を図ることができるものでありながら，前記蒸発濃縮装置における凝縮水が有する熱を利用して，前記ＲＯ膜モジュールにおける処理効率を向上できて，その小型化を図ることができるとともに，前記凝縮水におけるそのままでの河川等への放流を可能にするという効果を有する。   That is, according to the invention described in claims 1 and 3, the evaporation load in the evaporation concentrator can be reduced by the RO membrane module as the pretreatment, and the miniaturization can be achieved. However, the heat of the condensed water in the evaporative concentrator can be used to improve the processing efficiency in the RO membrane module and to reduce the size of the RO membrane module. It has the effect of allowing discharge.

しかし，このように，被処理廃水を，そのままＲＯ膜モジュールに供給して透過水と非透過水とに膜分離することは，前記逆浸透膜（ＲＯ膜）に目詰まりが発生し，この逆浸透膜における目詰まりを解消するための洗浄を頻繁に行うようにしなければならない煩わしさがあるばかりか，逆浸透膜（ＲＯ膜）の耐久性を低下することになる。   However, if the wastewater to be treated is supplied to the RO membrane module as it is and separated into permeated water and non-permeated water as described above, clogging occurs in the reverse osmosis membrane (RO membrane). In addition to being bothered by frequent cleaning to eliminate clogging in the osmosis membrane, the durability of the reverse osmosis membrane (RO membrane) is reduced.

これに対しては，前記請求項１及び３に記載した発明を前提として，請求項２及び４に記載したように構成することを提案する。   For this, on the premise of the inventions described in claims 1 and 3, it is proposed to configure as described in claims 2 and 4.

すなわち，請求項２及び４に記載したように，被処理廃水を，ナノフィルトレーション膜（ＮＦ膜）を使用したＮＦ膜モジュールに供給して，このＮＦ膜モジュールにおける透過水を前記ＲＯ膜モジュールに供給する一方，前記ＮＦ膜モジュールにおける非透過水を，蒸発濃縮装置に供給し，この蒸発濃縮装置における凝縮水にて，前記ＮＦ膜モジュールへの被処理廃水を熱交換器において間接加熱する。   That is, as described in claims 2 and 4, wastewater to be treated is supplied to an NF membrane module using a nanofiltration membrane (NF membrane), and the permeated water in the NF membrane module is supplied to the RO membrane module. On the other hand, the non-permeated water in the NF membrane module is supplied to the evaporating and concentrating device, and the waste water to be treated to the NF membrane module is indirectly heated in the heat exchanger with the condensed water in the evaporating and concentrating device.

これにより，前記被処理廃水に含まれている多価イオンや中乃至高分子量物質を，前記ＲＯ膜モジュールに供給する前に，前記ＮＦ膜モジュールにおいて膜分離することができ，この分だけ，前記ＲＯ膜モジュールにおける逆浸透膜に目詰まりが発生することを低減できるから，前記請求項１及び３に記載した発明が有する効果を奏することに加えて，前記逆浸透膜（ＲＯ膜）の耐久性を低下することを回避できるばかりか，その洗浄の頻度を大幅に低減することができる。   Thereby, the polyvalent ions and the medium to high molecular weight substances contained in the wastewater to be treated can be separated in the NF membrane module before being supplied to the RO membrane module, and the amount of the above-mentioned Since the occurrence of clogging in the reverse osmosis membrane in the RO membrane module can be reduced, in addition to the effects of the inventions described in claims 1 and 3, the durability of the reverse osmosis membrane (RO membrane) Can be avoided, and the frequency of cleaning can be greatly reduced.

しかも，前記ＮＦ膜モジュールに供給する被処理廃水を前記蒸発濃縮装置における凝縮水にて間接加熱することにより，前記ＮＦ膜モジュールにおける処理効率を大幅に向上することができるから，ＮＦ膜モジュールを小型化できる。   Moreover, since the wastewater to be treated to be supplied to the NF membrane module is indirectly heated with the condensed water in the evaporative concentrator, the treatment efficiency in the NF membrane module can be greatly improved. Can be

以下，本発明の実施の形態を，図１の図面について説明する。   An embodiment of the present invention will be described below with reference to the drawing of FIG.

この図において，符号１は，被処理廃水タンクを示し，この被処理廃水タンク１内には，処理する目的であるところのカルシウム及び硫酸等の有害な不純物を含む被処理廃水が，廃水供給管路２より供給されている。   In this figure, reference numeral 1 denotes a treated wastewater tank. In this treated wastewater tank 1, treated wastewater containing harmful impurities such as calcium and sulfuric acid, which is the purpose of treatment, is disposed in a wastewater supply pipe. It is supplied from the path 2.

また，符号３は，ナノフィルトレーション膜（ＮＦ膜）を使用した第１段ＮＦ膜モジュールを，符号４は，同じくナノフィルトレーション膜（ＮＦ膜）を使用した第２段ＮＦ膜モジュールを，符号５は，同じくナノフィルトレーション膜（ＮＦ膜）を使用した第３段ＮＦ膜モジュールを，そして，符号６は，逆浸透膜（ＲＯ膜）を使用したＲＯ膜モジュールを各々示す。   Reference numeral 3 denotes a first-stage NF membrane module using a nanofiltration membrane (NF membrane), and reference numeral 4 denotes a second-stage NF membrane module using a nanofiltration membrane (NF membrane). Reference numeral 5 denotes a third-stage NF membrane module that also uses a nanofiltration membrane (NF membrane), and reference numeral 6 denotes an RO membrane module that uses a reverse osmosis membrane (RO membrane).

前記各段のＮＦ膜モジュール３，４，５の各々における非透過側には，循環ポンプ３ａ，４ａ，５ａ及び逆止弁３ｂ，４ｂ，５ｂを備えた循環管路３ｃ，４ｃ，５ｃが設けられ，また，前記ＲＯ膜モジュール６における非透過側には，循環ポンプ６ａを備えた循環管路６ｂが設けられている。   Circulation pipes 3c, 4c, 5c provided with circulation pumps 3a, 4a, 5a and check valves 3b, 4b, 5b are provided on the non-permeation side of each of the NF membrane modules 3, 4, 5 of each stage. In addition, on the non-permeate side of the RO membrane module 6, a circulation line 6b provided with a circulation pump 6a is provided.

前記被処理廃水タンク１内における被処理廃水を，ポンプ７を備えた廃水移送管路８にて，前記第１段ＮＦ膜モジュール３における循環管路３ｃに供給バルブ９を介して供給し，この第１段ＮＦ膜モジュール３における非透過水を，排出バルブ１０より排出して，前記第２段ＮＦ膜モジュール４における循環管路４ｃに供給バルブ１１を介して供給し，第２段ＮＦ膜モジュール４における非透過水を，排出バルブ１２より排出して，前記第３段ＮＦ膜モジュール５における循環管路５ｃに供給バルブ１３を介して供給し，この第３段ＮＦ膜モジュール５における非透過水を，排出バルブ１４より管路１５を介して攪拌機１６を備えた反応槽１７に排出するようにしている。   The wastewater to be treated in the wastewater tank 1 to be treated is supplied via a supply valve 9 to a circulation line 3c in the first stage NF membrane module 3 through a wastewater transfer line 8 provided with a pump 7. The non-permeate water in the first stage NF membrane module 3 is discharged from the discharge valve 10 and supplied to the circulation line 4c in the second stage NF membrane module 4 via the supply valve 11, and the second stage NF membrane module. 4 is discharged from the discharge valve 12 and supplied to the circulation line 5c in the third stage NF membrane module 5 through the supply valve 13, and the non-permeate water in the third stage NF membrane module 5 is supplied. Is discharged from a discharge valve 14 through a pipe line 15 to a reaction tank 17 equipped with a stirrer 16.

この場合，前記第１段ＮＦ膜モジュール３における供給バルブ９と排出バルブ１０との間，前記第２段ＮＦ膜モジュール４における供給バルブ１１と排出バルブ１２との間，及び前記第３段ＮＦ膜モジュール５における供給バルブ１３と排出バルブ１４との間の各々には，切換バルブ２６，２７，２８を備え，これらを各切換バルブ２６，２７，２８を閉じているときには，管路８からの処理すべき廃水は，先ず，第１段ＮＦ膜モジュール３に供給され，この第１段ＮＦ膜モジュール３における非透過水が，第２段ＮＦ膜モジュール４に供給され，この第２段ＮＦ膜モジュール４における非透過水が，第３段ＮＦ膜モジュール５に供給され，この第３段ＮＦ膜モジュール５における非透過水が，前記反応槽１７に排出するような状態になっているが，以下に述べるように，前記三段のＮＦ膜モジュール３，４，５のうち少なくとも任意の二つのＮＦ膜モジュールを使用して二段の膜処理を行う一方，残り一つのＮＦ膜モジュールにおける膜処理を停止する状態に切り換え可能に構成している。   In this case, between the supply valve 9 and the discharge valve 10 in the first stage NF membrane module 3, between the supply valve 11 and the discharge valve 12 in the second stage NF membrane module 4, and the third stage NF membrane. Each of the module 5 between the supply valve 13 and the discharge valve 14 is provided with switching valves 26, 27, and 28. When these switching valves 26, 27, and 28 are closed, processing from the pipe line 8 is performed. Waste water to be supplied is first supplied to the first stage NF membrane module 3, and the non-permeate water in the first stage NF membrane module 3 is supplied to the second stage NF membrane module 4, and this second stage NF membrane module. 4 is supplied to the third stage NF membrane module 5, and the non-permeate water in the third stage NF membrane module 5 is discharged to the reaction tank 17. However, as described below, two-stage membrane treatment is performed using at least two arbitrary NF membrane modules among the three-stage NF membrane modules 3, 4 and 5, while the remaining one NF membrane module is used. The film processing can be switched to a state where the film processing is stopped.

すなわち，前記第１段ＮＦ膜モジュール３における供給バルブ９及び排出バルブ１０を閉じて第１段ＮＦ膜モジュール３における膜処理を停止する一方，切換バルブ２６を開くことにより，被処理廃水は，先ず，第２段ＮＦ膜モジュール４に供給され，この第２段ＮＦ膜モジュール４における非透過水が第３段ＮＦ膜モジュール５に供給され，この第３段ＮＦ膜モジュール５における非透過水が前記反応槽１７に排出されるというように，前記第２段ＮＦ膜モジュール４と前記第３段ＮＦ膜モジュール５とで二段の膜処理を行う。   That is, the supply valve 9 and the discharge valve 10 in the first stage NF membrane module 3 are closed to stop the membrane treatment in the first stage NF membrane module 3, while the switching valve 26 is opened, , Supplied to the second stage NF membrane module 4, the non-permeated water in the second stage NF membrane module 4 is supplied to the third stage NF membrane module 5, and the non-permeated water in the third stage NF membrane module 5 The second stage NF membrane module 4 and the third stage NF membrane module 5 perform a two-stage membrane treatment so that it is discharged into the reaction tank 17.

また，前記第２段ＮＦ膜モジュール４における供給バルブ１１及び排出バルブ１２を閉じて第２段ＮＦ膜モジュール４における膜処理を停止する一方，切換バルブ２７を開くことにより，被処理廃水は，先ず，第１段ＮＦ膜モジュール３に供給され，この第１段ＮＦ膜モジュール３における非透過水が第３段ＮＦ膜モジュール５に供給され，この第３段ＮＦ膜モジュール５における非透過水が前記反応槽１７に排出されるというように，前記第１段ＮＦ膜モジュール３と前記第３段ＮＦ膜モジュール５とで二段の膜処理を行う。   Further, the supply valve 11 and the discharge valve 12 in the second stage NF membrane module 4 are closed to stop the membrane treatment in the second stage NF membrane module 4, while the switching valve 27 is opened, , Supplied to the first stage NF membrane module 3, the non-permeate water in the first stage NF membrane module 3 is supplied to the third stage NF membrane module 5, and the non-permeate water in the third stage NF membrane module 5 The first stage NF membrane module 3 and the third stage NF membrane module 5 perform a two-stage membrane treatment so that it is discharged into the reaction tank 17.

更にまた，前記第３段ＮＦ膜モジュール５における供給バルブ１３及び排出バルブ１４を閉じて第３段ＮＦ膜モジュール５における膜処理を停止する一方，切換バルブ２８を開くことにより，被処理廃水は，先ず，第１段ＮＦ膜モジュール３に供給され，この第１段ＮＦ膜モジュール３における非透過水が第２段ＮＦ膜モジュール４に供給され，この第２段ＮＦ膜モジュール４における非透過水が前記反応槽１７に排出されるというように，前記第１段ＮＦ膜モジュール３と前記第２段ＮＦ膜モジュール４とで二段の膜処理を行う。   Furthermore, the supply valve 13 and the discharge valve 14 in the third stage NF membrane module 5 are closed to stop the membrane treatment in the third stage NF membrane module 5, while the switching valve 28 is opened, First, the first stage NF membrane module 3 is supplied, the non-permeate water in the first stage NF membrane module 3 is supplied to the second stage NF membrane module 4, and the non-permeate water in the second stage NF membrane module 4 is supplied. The first stage NF membrane module 3 and the second stage NF membrane module 4 perform a two-stage membrane treatment so that it is discharged into the reaction tank 17.

一方，前記各段のＮＦ膜モジュール３，４，５の各々における透過水を，バルブ１８，１９，２０より取り出し，管路２１を介して前記ＲＯ膜モジュール６における循環管路６ｂに供給し，前記ＲＯ膜モジュール６における非透過水を，管路２２にて，前記反応槽１７に排出する一方，前記ＲＯ膜モジュール６における透過水を，管路２３を介して溜め槽２４に溜めたのち，管路２５より河川等に放流するように構成している。   On the other hand, the permeated water in each of the NF membrane modules 3, 4, 5 at each stage is taken out from the valves 18, 19, 20 and supplied to the circulation pipeline 6 b in the RO membrane module 6 through the pipeline 21. The non-permeated water in the RO membrane module 6 is discharged to the reaction tank 17 through the conduit 22, while the permeated water in the RO membrane module 6 is collected in the reservoir tank 24 through the conduit 23, The pipe 25 is configured to be discharged into a river or the like.

前記反応槽１７には，前記各段のＮＦ膜モジュール３，４，５における非透過水，及び前記ＲＯ膜モジュール６における非透過水が被処理廃水として集められ，この反応槽１７内における被処理廃水は，管路２９からの苛性ソーダ等のアルカリの供給によってＰＨが９〜１０になるように調節される。   In the reaction tank 17, the non-permeated water in the NF membrane modules 3, 4, 5 of each stage and the non-permeated water in the RO membrane module 6 are collected as treated waste water. The wastewater is adjusted so that the pH becomes 9 to 10 by supplying alkali such as caustic soda from the pipe line 29.

更に，前記反応槽１７内における被処理廃水には，炭酸ソーダ（Ｎａ2 ＣＯ3)の適宜量が，管路３０を介して添加される。 Furthermore, an appropriate amount of sodium carbonate (Na 2 CO 3 ) is added to the wastewater to be treated in the reaction tank 17 through a pipe 30.

この炭酸ソーダの添加は，当該炭酸ソーダを水に溶解した水溶液の状態にて行うか，或いは，炭酸ソーダを粉末の状態で行うようにしても良い。   The addition of the sodium carbonate may be performed in the form of an aqueous solution obtained by dissolving the sodium carbonate in water, or the sodium carbonate may be performed in a powder state.

前記炭酸ソーダの添加により，前記被処理廃水に含まれるカルシウムを，炭酸カルシウムの結晶として析出する。   By adding the sodium carbonate, calcium contained in the wastewater to be treated is precipitated as calcium carbonate crystals.

前記図１において，符号３１は，自己蒸気圧縮式の蒸発濃縮装置を示す。   In FIG. 1, reference numeral 31 denotes a self-vapor compression evaporation concentrator.

この蒸発濃縮装置３１は，内部を図示しない真空発生装置にて大気圧以下の減圧に保持した密閉型の蒸発缶３１ａと，この蒸発缶３１ａ内の上部に，水平の多段状に設けた多数本の伝熱管３１ｂと，この各伝熱管３１ｂの一端に対する入口ヘッダー３１ｃと，他端に対するヘッダー３１ｄとを備え，前記蒸発缶３１ａ内の底部における濃縮廃水は，循環ポンプ３１ｅにて汲み出して，前記蒸発缶３１ａ内の上部におけるノズル３１ｆから前記各伝熱管３１ｂの外表面に散布したのち前記蒸発缶３１ａ内の底部に戻るという循環を行うように構成されている。   The evaporative concentrator 31 includes a hermetic evaporator 31a whose interior is maintained at a reduced pressure below atmospheric pressure by a vacuum generator (not shown), and a large number of horizontal evaporators provided in the upper portion of the evaporator 31a. Each of the heat transfer tubes 31b, an inlet header 31c for one end of each heat transfer tube 31b, and a header 31d for the other end, and the concentrated waste water at the bottom in the evaporator 31a is pumped out by a circulation pump 31e and is evaporated. The nozzle 31f in the upper part of the can 31a is circulated from the nozzle 31f to the outer surface of each heat transfer tube 31b and then returned to the bottom of the evaporator 31a.

また，前記蒸発缶３１ａ内に発生した蒸気は，ブロワー圧縮機３１ｇにて，圧力及び温度を高くするように圧縮したのち，前記入口ヘッダー３１ｃを介して前記各伝熱管３１ｂ内に供給されて，この各伝熱管３１ｂの外表面における濃縮廃水を，間接加熱することによって沸騰蒸発する一方，前記各伝熱管３１ｂ内おける凝縮水は，管路３１ｈより取り出するように構成している。   The steam generated in the evaporator 31a is compressed by the blower compressor 31g so as to increase the pressure and temperature, and then supplied to the heat transfer tubes 31b via the inlet header 31c. The concentrated waste water on the outer surface of each heat transfer tube 31b is boiled and evaporated by indirect heating, while the condensed water in each heat transfer tube 31b is taken out from the pipe line 31h.

そして，前記反応槽１７内における被処理廃水を，これに前記炭酸カルシウムの結晶を含むスラリーの状態のままで，廃水移送ポンプ３２にて汲み出し，廃水供給管路３３を介して，前記蒸発缶３１ａに導入することにより，前記したように，間接加熱による沸騰蒸発にて濃縮するように構成している。   Then, the wastewater to be treated in the reaction tank 17 is pumped out by the wastewater transfer pump 32 in the state of the slurry containing the calcium carbonate crystals, and is passed through the wastewater supply pipe 33 to the evaporator 31a. As described above, it is configured to be concentrated by boiling evaporation by indirect heating.

また，前記蒸発濃縮装置３１における濃縮廃水を，濃縮廃水管路３６を介して乾燥固形化装置３７に供給して，この乾燥固形化装置３７において，乾燥して固形化するように構成している。   Further, the concentrated waste water in the evaporative concentration device 31 is supplied to a dry solidifying device 37 via a concentrated waste water conduit 36, and is dried and solidified in the dry solidifying device 37. .

一方，前記被処理廃水タンク１から前記各段のＮＦ膜モジュール３，４，５への廃水移送管路８には，前記処理廃水タンク１への戻り管路３４を接続して，この戻り管路３４の途中に，前記蒸発濃縮装置３１において管路３１ｈより取り出される凝縮水を熱源として，前記被処理廃水を間接加熱するようにした熱交換器３５を設けている。   On the other hand, a return pipe 34 to the treated wastewater tank 1 is connected to the wastewater transfer pipe 8 from the treated wastewater tank 1 to the NF membrane modules 3, 4, 5 of each stage, and this return pipe A heat exchanger 35 that indirectly heats the wastewater to be treated is provided in the middle of the path 34 using the condensed water taken out from the pipe line 31h in the evaporative concentrator 31 as a heat source.

この構成において，被処理廃水タンク１内に廃水供給管路２より供給された被処理廃水は，この被処理廃水タンク１内と熱交換器３５との間を循環する間に，前記蒸発濃縮装置３１における凝縮水によって加熱されて温度が高くなる。   In this configuration, the waste water to be treated supplied from the waste water supply line 2 into the waste water tank 1 to be treated is circulated between the waste water tank 1 and the heat exchanger 35 while the evaporative concentrating device. Heated by the condensed water at 31 increases the temperature.

このようにして温度が高くなった被処理廃水は，前記ＮＦ膜モジュール３，４，５に供給されて，不純物を含む不透過水と，不純物の少ない透過水とに膜分離され，非透過水は，反応槽１７内に流入する一方，透過水は，前記ＲＯ膜モジュール６に供給され，不純物を含む不透過水と，カルシウム及び硫酸等の有害な不純物を殆ど含まない状態の透過水とに膜分離され，非透過水は，反応槽１７内に流入する一方，透過水は，溜め槽２４を経て管路２５より河川等に放流される。   The wastewater to be treated whose temperature has been increased in this way is supplied to the NF membrane modules 3, 4 and 5 and separated into impervious water containing impurities and permeated water with less impurities. Flows into the reaction tank 17 while the permeate is supplied to the RO membrane module 6 and is converted into non-permeate containing impurities and permeate containing almost no harmful impurities such as calcium and sulfuric acid. The membrane is separated and the non-permeated water flows into the reaction tank 17, while the permeated water is discharged to the river or the like from the conduit 25 through the reservoir tank 24.

そして，反応槽１７内に流入した被処理廃水には，これに炭酸ソーダを添加することにより，当該廃水中に含まれているカルシウムを，炭酸カルシウムの結晶として析出され，この炭酸カルシウムの結晶を含む状態のままで，前記蒸発濃縮装置３１に供給して，沸騰蒸発により濃縮し，その濃縮廃水を，前記炭酸カルシウムの結晶を含む状態のままで，前記乾燥固形化装置３７に供給されることにより，乾燥して固形化される。   And by adding sodium carbonate to the wastewater to be treated which has flowed into the reaction tank 17, calcium contained in the wastewater is precipitated as calcium carbonate crystals. In the state of containing, it is supplied to the evaporative concentrating device 31 and concentrated by boiling evaporation, and the concentrated waste water is supplied to the dry solidifying device 37 while containing the calcium carbonate crystals. To dry and solidify.

一方，前記蒸発濃縮装置３１における凝縮水は，前記熱交換器３５に供給されて，前記被処理廃水を加熱することにより，温度が下がることになるから，殊更，冷却することなく，そのままで河川等に放流することが可能になる。   On the other hand, the condensate in the evaporative concentrator 31 is supplied to the heat exchanger 35 and the temperature of the waste water to be treated is lowered by heating. It becomes possible to discharge to etc.

このように，本発明によると，被処理廃水を蒸発濃縮装置３１において沸騰蒸発にて濃縮処理する場合に，この蒸発濃縮装置３１において濃縮処理する廃水の量を，前記ＲＯ膜モジュール６における透過水の分だけ少なくする一方，前記蒸発濃縮装置３１における凝縮水にて，前記被処理廃水を加熱して，前記ＲＯ膜モジュール６における処理効率を向上し，前記凝縮水の温度を下げて，そのままでの河川等への放流を可能にすることができるのである。   Thus, according to the present invention, when the waste water to be treated is concentrated by boiling evaporation in the evaporation concentrator 31, the amount of waste water to be concentrated in the evaporation concentrator 31 is determined by the permeated water in the RO membrane module 6. On the other hand, the waste water to be treated is heated with the condensate in the evaporative concentrator 31 to improve the treatment efficiency in the RO membrane module 6, and the temperature of the condensate is lowered as it is. Can be released into rivers.

また，前記ＲＯ膜モジュール６の前段における各段のＮＦ膜モジュール３，４，５によって，前記ＲＯ膜モジュール６における逆浸透膜に目詰まりが発生することを低減できるから，その逆浸透膜の耐久性を低下することを回避できるとともに，その洗浄の頻度を大幅に低減することができる。   Further, since the clogging of the reverse osmosis membrane in the RO membrane module 6 can be reduced by the NF membrane modules 3, 4, 5 at the previous stage of the RO membrane module 6, the durability of the reverse osmosis membrane can be reduced. Can be avoided, and the frequency of cleaning can be greatly reduced.

なお，前記各段のＮＦ膜モジュール３，４，５におけるＮＦ膜は，以下に述べるような方法にて洗浄処理される。   The NF membranes in the NF membrane modules 3, 4, and 5 at each stage are cleaned by the method described below.

すなわち，前記溜め槽２４内における透過水を，ポンプ３８にて汲み出し，管路３９を介して，前記各段のＮＦ膜モジュール３，４，５のうち膜処理を停止している状態の一つのＮＦ膜モジュールにおける透過側に供給して，ＮＦ膜を逆方向に透過するといういわゆる逆洗浄を行うように構成している。この逆洗浄において，ＮＦ膜を逆方向に透過した洗浄水は，管路４０より排出される。   That is, the permeated water in the reservoir tank 24 is pumped out by the pump 38, and one of the NF membrane modules 3, 4 and 5 in each stage is stopped through the pipeline 39. It is configured to perform so-called reverse cleaning in which the NF membrane module is supplied to the permeate side and permeates through the NF membrane in the reverse direction. In this reverse cleaning, the cleaning water that has permeated through the NF membrane in the reverse direction is discharged from the conduit 40.

また，前記各段のＮＦ膜モジュール３，４，５における非透過側の洗浄は，洗浄水槽４１に溜めた洗浄水を，ポンプ４２にて汲み出し，フィルタ４３にて濾過し，次いで，管路４４を介して，前記各段のＮＦ膜モジュール３，４，５のうち膜処理を停止している状態の一つのＮＦ膜モジュールにおける非透過側に供給し，非透過水を管路４５にて前記洗浄水槽４１に戻し，透過水を管路４６にて前記洗浄水槽４１に戻すというように循環することによって行うように構成している。   The non-permeate side of the NF membrane modules 3, 4, 5 in each stage is washed with the washing water stored in the washing water tank 41 by the pump 42, filtered by the filter 43, and then the pipe line 44. The non-permeate water is supplied to the non-permeate side of one NF membrane module in a state where the membrane treatment is stopped among the NF membrane modules 3, 4, 5 of each stage, It returns to the washing water tank 41, and it is comprised by circulating so that permeated water may be returned to the said washing water tank 41 by the pipe line 46. FIG.

本発明における実施の形態を示すフローシートである。It is a flow sheet which shows an embodiment in the present invention.

符号の説明Explanation of symbols

１ 被処理廃水タンク
３，４，５ ＮＦ膜モジュール
６ ＲＯ膜モジュール
８ 廃水移送管路
１７ 反応槽
３１ 蒸発濃縮装置
３１ａ 蒸発缶
３１ｂ 伝熱管
３１ｈ 凝縮水管路
３５ 熱交換器 1 Wastewater tank to be treated 3,4,5 NF membrane module 6 RO membrane module 8 Wastewater transfer line 17 Reaction tank 31 Evaporation concentrator 31a Evaporator 31b Heat transfer tube 31h Condensate water line 35 Heat exchanger

Claims (4)

被処理廃水を，逆浸透膜を使用したＲＯ膜モジュールに供給して，その透過水と非透過水とに分離し，非透過水を，間接加熱にて沸騰蒸発する蒸発濃縮装置に供給して濃縮する一方，前記蒸発濃縮装置における凝縮水にて，前記ＲＯ膜モジュールに供給する被処理廃水を間接加熱することを特徴とする廃水の濃縮処理方法。   The wastewater to be treated is supplied to an RO membrane module using a reverse osmosis membrane and separated into permeate and non-permeate water, and the non-permeate water is supplied to an evaporation concentrator that evaporates to boiling by indirect heating. While concentrating, the wastewater to be treated supplied to the RO membrane module is indirectly heated with the condensed water in the evaporative concentrator. 被処理廃水を，ナノフィルトレーション膜を使用したＮＦ膜モジュールに供給して，透過水と非透過水とに分離し，その透過水を，逆浸透膜を使用したＲＯ膜モジュールに供給して，透過水と非透過水とに分離し，前記ＮＦ膜モジュール及び前記ＲＯ膜モジュールにおける非透過水を，間接加熱にて沸騰蒸発する蒸発濃縮装置に供給して濃縮する一方，前記蒸発濃縮装置における凝縮水にて，前記ＮＦ膜モジュールに供給する被処理廃水を間接加熱することを特徴とする廃水の濃縮処理方法。   The wastewater to be treated is supplied to the NF membrane module using the nanofiltration membrane, separated into permeated water and non-permeated water, and the permeated water is supplied to the RO membrane module using the reverse osmosis membrane. The permeated water and the non-permeated water are separated, and the non-permeated water in the NF membrane module and the RO membrane module is supplied and concentrated to an evaporating and concentrating device that evaporates by indirect heating. A wastewater concentration treatment method, wherein the wastewater to be treated supplied to the NF membrane module is indirectly heated with condensed water. 被処理廃水を逆浸透膜にて透過水と非透過水とに分離するＲＯ膜モジュールと，前記ＲＯ膜モジュールにおける非透過水を間接加熱にて沸騰蒸発する蒸発濃縮装置とを備え，更に，前記蒸発濃縮装置における凝縮水を熱源として前記ＲＯ膜モジュールに供給する被処理廃水を間接加熱する熱交換器を備えていることを特徴とする廃水の濃縮処理装置。   A RO membrane module that separates wastewater to be treated into permeated water and non-permeated water using a reverse osmosis membrane; and an evaporating and concentrating device that evaporates the non-permeated water in the RO membrane module by indirect heating. A wastewater concentration treatment apparatus comprising a heat exchanger that indirectly heats the wastewater to be treated supplied to the RO membrane module using the condensed water in the evaporative concentration apparatus as a heat source. 被処理廃水をナノフィルトレーション膜にて透過水と非透過水とに分離するＮＦ膜モジュールと，このＮＦ膜モジュールにおける透過水を逆浸透膜にて透過水と非透過水とに分離するＲＯ膜モジュールと，前記ＮＦ膜モジュール及び前記ＲＯ膜モジュールにおける非透過水を間接加熱にて沸騰蒸発する蒸発濃縮装置とを備え，更に，前記蒸発濃縮装置における凝縮水を熱源として前記ＮＦ膜モジュールに供給する被処理廃水を間接加熱する熱交換器を備えていることを特徴とする廃水の濃縮処理装置。   An NF membrane module that separates the wastewater to be treated into permeated water and non-permeated water using a nanofiltration membrane, and RO that separates the permeated water in this NF membrane module into permeated water and non-permeated water using a reverse osmosis membrane. A membrane module; and an evaporating and concentrating device for boiling and evaporating non-permeate water in the NF membrane module and the RO membrane module by indirect heating. Further, the condensed water in the evaporating and concentrating device is supplied to the NF membrane module as a heat source. A waste water concentration treatment apparatus comprising a heat exchanger for indirectly heating waste water to be treated.
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CN106430794A (en) * 2016-12-20 2017-02-22 大唐国际化工技术研究院有限公司 Resourceful treatment method and treatment system for desulfuration wastewater

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