JPH05116B2 - - Google Patents
Info
- Publication number
- JPH05116B2 JPH05116B2 JP58211911A JP21191183A JPH05116B2 JP H05116 B2 JPH05116 B2 JP H05116B2 JP 58211911 A JP58211911 A JP 58211911A JP 21191183 A JP21191183 A JP 21191183A JP H05116 B2 JPH05116 B2 JP H05116B2
- Authority
- JP
- Japan
- Prior art keywords
- waste liquid
- tank
- water
- liquid
- concentrated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000007788 liquid Substances 0.000 claims description 54
- 239000002699 waste material Substances 0.000 claims description 38
- 238000000034 method Methods 0.000 claims description 20
- 238000001914 filtration Methods 0.000 claims description 12
- 239000000706 filtrate Substances 0.000 claims description 11
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 22
- 238000001816 cooling Methods 0.000 description 9
- 239000012528 membrane Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000004094 surface-active agent Substances 0.000 description 2
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- -1 OH - and Cl - Chemical class 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000006103 coloring component Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 150000005846 sugar alcohols Polymers 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】
本発明は廃液の処理方法、特には、廃液からの
澄水の回収率を増加させて処分すべき廃液量を顕
著に減らすことができる廃液の処理方法に関す
る。従来、廃液を処理して再利用可能な水に還元
するために、限外ロ過器（以下、UFという）や
逆浸透ロ過器（以下、ROという）を使用する方
式が採用されている。UFは、一般に20Å以上の
大きさの廃液成分を分離し、ROは一般に５〜20
Åの大きさの廃液成分を分離できるものである。
廃液中に含まれるイオン化物質、界面活性剤、着
色成分、臭気成分などはROで分離される。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for treating waste liquid, and more particularly to a method for treating waste liquid, which can increase the recovery rate of clear water from waste liquid and significantly reduce the amount of waste liquid to be disposed of. Conventionally, methods using ultrafilters (hereinafter referred to as UF) and reverse osmosis filters (hereinafter referred to as RO) have been adopted to treat waste liquid and reduce it to reusable water. . UF generally separates waste liquid components with a size of 20 Å or larger, and RO generally separates effluent components with a size of 5 to 20 Å.
It is capable of separating waste liquid components with a size of Å.
Ionized substances, surfactants, coloring components, odor components, etc. contained in the waste liquid are separated by RO.
ここで、UFとは、ロ過しようとする廃液に圧
力をかけ、高分子物質やコロイド状物質を半透膜
によつて阻止し、水および水に含まれる低分子物
質を半透膜の膜面に無数に存在する微細な孔を通
して透過させるロ過技術である。 Here, UF refers to applying pressure to the waste liquid to be filtered, blocking high molecular substances and colloidal substances with a semi-permeable membrane, and removing water and low molecular substances contained in water through the semi-permeable membrane. This is a filtration technology that allows water to pass through the countless microscopic pores that exist on the surface.
また、ROはロ過しようとする濃厚溶液（廃
液）と濃厚溶液より希薄な希薄溶液を半透膜で仕
切り、濃厚溶液側に浸透圧より大きい圧力をかけ
ることにより、浸透現像とは逆に溶媒が濃厚溶液
側から希薄溶液側に移動することを利用したロ過
技術である。これによつて、バクテリア、コロイ
ドなどの他、溶解塩類（イオン）、低分子有機物
などもロ過できるものである。 In addition, in RO, the concentrated solution (waste liquid) to be filtered and the dilute solution, which is more dilute than the concentrated solution, are separated by a semi-permeable membrane, and a pressure greater than the osmotic pressure is applied to the concentrated solution side. This is a filtration technology that utilizes the movement of water from the concentrated solution side to the dilute solution side. This makes it possible to filter out bacteria, colloids, and other substances such as dissolved salts (ions) and low-molecular organic matter.
ところで、本発明者は、廃液処理によつて、で
きるだけ多く再利用可能な水を還元するために
ROの前処理としてUF処理を行うことを試みた。
しかし、廃液をUFで処理し、次いでROで処理
するだけのものであつたために、廃液から回収さ
れる再利用可能な水量は少なく、従つて濃縮水が
多くなり、廃液処理コストが高いものになつてい
た。また、水資源の効率的利用も図られないもの
であつた。 By the way, the present inventor has developed a method to reduce as much reusable water as possible through waste liquid treatment.
We attempted to perform UF treatment as a pretreatment for RO.
However, since the waste liquid was simply treated with UF and then treated with RO, the amount of reusable water recovered from the waste liquid was small, resulting in a large amount of concentrated water, resulting in high waste liquid treatment costs. I was getting used to it. Furthermore, efficient use of water resources was not possible.
而して本発明は、廃液から回収される再利用可
能な水量を大幅に増すことができる廃液処理方法
を提供することを主たる目的とする。 Therefore, the main object of the present invention is to provide a waste liquid treatment method that can significantly increase the amount of reusable water recovered from waste liquid.
本発明による廃液処理方法は廃液をUFにより
ロ過する第１工程、第１工程のロ過液をROによ
りロ過する第２工程、および第２工程の濃縮液を
冷却処理後再度UFとROでロ過する第３工程を
有することを特徴とするものである。 The waste liquid treatment method according to the present invention includes a first step in which the waste liquid is filtered through UF, a second step in which the filtrate from the first step is filtered through RO, and a concentrated liquid in the second step is cooled and then re-filtered with UF and RO. This method is characterized by having a third step of filtering through the filter.
本発明による廃液処理方法においては、ROで
濃縮された濃縮液をそのまま廃棄しないで再度
UFとROでロ過処理するものであるが、再度UF
とROでロ過処理する前にUFの濃縮液を冷却処
理する。この冷却処理によつて、濃縮液中に含有
する溶解成分が析出し、この析出物は再度のUF
により分離されることができる。このため、再度
のUFのロ過液には一度ROで濃縮された濃縮液
であるにも拘らず溶解成分は濃縮液よりずつと少
なくなつており、再度のROによるロ過において
再利用可能な水分を効率よく再度ロ過することが
できるようになるものである。即ち、ROは処理
しようとする液中の溶解成分の濃度が一定以上に
なるとロ過液中に溶解成分が混入してロ過機能を
失う。これは、処理しようとする液を高圧（例え
ば40Kg／cm2〜60Kg／cm2）にしてROによるロ過を
行うため、処理しようとする液中にあまり多くの
溶解成分を含むと、その溶解成分まで半透膜から
押し出されてしまうからである。また、ROの半
透膜は非常に小さい多数の穴があるが、処理しよ
うとする液中にあまり多くの溶解成分を含むとロ
過中に穴が溶解成分の析出で塞がれてROのロ過
機能を短期間に失つてしまうが、本発明では冷却
処理によつて処理しようとする液中の溶解成分は
低く押えられているので、ROの使用可能期間を
著しく長くすることができるものである。 In the waste liquid treatment method according to the present invention, the concentrated liquid concentrated by RO is not discarded as it is, but is recycled again.
UF and RO process RO, but UF again
The UF concentrate is then cooled before being filtered through RO. By this cooling process, the dissolved components contained in the concentrate precipitate, and this precipitate is re-treated with UF.
can be separated by Therefore, even though the UF filtrate has been concentrated by RO once, the amount of dissolved components in the UF filtrate is gradually decreasing compared to the concentrated solution, and it can be reused in the second RO filtration. This allows moisture to be filtered out again efficiently. That is, when the concentration of dissolved components in the liquid to be treated exceeds a certain level, the dissolved components are mixed into the filtrate and the RO loses its filtration function. This is because the liquid to be treated is subjected to high pressure (e.g. 40Kg/cm 2 - 60Kg/cm 2 ) and filtration is performed using RO, so if the liquid to be treated contains too many dissolved components, they will dissolve. This is because even the components are pushed out through the semipermeable membrane. In addition, the semipermeable membrane of RO has many very small holes, but if the liquid to be treated contains too many dissolved components, the holes will become clogged with precipitation of dissolved components during filtration, and the RO However, in the present invention, the dissolved components in the liquid to be treated are suppressed to a low level through the cooling process, so the usable period of the RO can be significantly extended. It is.
冷却処理によるROの濃縮液からの溶解成分の
析出は、温度差による溶解度の違いを利用したも
のであり、具体的には、UFおよびROは処理し
ようとする液の加圧下で用いられるため処理液の
温度が上昇し、それに伴いROからの濃縮水には
より多くの溶解成分が含まれることになる。これ
を冷却することによつて、溶解成分の一部を析出
させることができるものである。この冷却温度
は、溶解成分の析出を生じさせることができる範
囲に適宜設定されるが、一般には25℃以下、特に
は20℃以下が好適である。 Precipitation of dissolved components from the concentrated liquid of RO by cooling treatment takes advantage of the difference in solubility due to temperature difference. Specifically, since UF and RO are used under pressure of the liquid to be treated, As the temperature of the liquid increases, the concentrated water from RO will contain more dissolved components. By cooling this, a part of the dissolved components can be precipitated. This cooling temperature is appropriately set within a range that allows precipitation of dissolved components, but is generally preferably 25°C or lower, particularly 20°C or lower.
このようにして、本発明による廃液処理方法に
よれば、単にUFとORとを組合せた方法に較べ
数倍以上の再利用可能な水分を廃液から回収で
き、さらに廃液処理装置、特にROの寿命を大幅
に長くすることができるものである。また、本発
明による廃液処理方法は自動化処理に適するよう
に循環方式として実施することができる。即ち、
ROの濃縮水を冷却後、はじめに用いたUFおよ
びROに導びくことによつて廃液を循環させなが
らROから継続的にロ過液として再使用可能な水
分を回収することができる。このときROからの
濃縮水の一部は除去されてもよい。また、本発明
による廃液処理方法は、一般に工場から廃出され
る液の処理として広く利用できるものである。即
ち、一般の工場廃液には、Pb，As，Zn，Ba，
Na，Fe，ＢおよびLaなどの金属イオン、SO4 2-，
OH-，Cl-などの非金属イオン、ベンゼン、塩化
エチレン、多価アルコールなどの溶剤および各種
オイル、界面活性剤などを溶解成分として又は微
粒子として含有しており、本発明では、UFと
ROを併用することによつてこれらの工場廃液を
処理できるものである。 In this way, according to the waste liquid treatment method of the present invention, several times more reusable water can be recovered from the waste liquid compared to a method that simply combines UF and OR, and the waste liquid treatment equipment, especially RO, can have a long lifespan. can be significantly lengthened. Further, the waste liquid treatment method according to the present invention can be implemented as a circulation method so as to be suitable for automated treatment. That is,
After the concentrated water from the RO is cooled, it is guided to the UF and RO that were used initially, thereby allowing the waste liquid to be circulated and water that can be reused as a filtrate to be continuously recovered from the RO. At this time, part of the concentrated water from the RO may be removed. Furthermore, the waste liquid treatment method according to the present invention can be widely used for treating liquid generally discharged from factories. In other words, general factory waste liquid contains Pb, As, Zn, Ba,
Metal ions such as Na, Fe, B and La, SO 4 2- ,
It contains nonmetallic ions such as OH - and Cl -, solvents such as benzene, ethylene chloride, and polyhydric alcohols, various oils, and surfactants as dissolved components or as fine particles.
These factory waste liquids can be treated by using RO together.
実施例
第１図に本実施例で用いた廃水処理装置を示
す。レンズ洗浄研摩廃液の上澄液である廃液１を
タンク２に収容する。この廃液はタンクからポン
プ３によつてパイプ４を通つてUF（商品名：
AEC6050，旭化成製）５，６，７，８および９
に1.5Kg／cm2の圧力でかけられる。UFにより分離
された濃縮液はパイプ１０および１１を通つてタ
ンク１２に収容される。この濃縮液は廃棄物とし
て処理される。UFからのロ過液はパイプ１３を
通つてタンク１４およびさらにパイプ１６を通つ
てタンク１５に収容される。タンク１５は予備タ
ンクであると同時に、UFの半透膜が目詰まりを
生じてロ過作用が低下したときにポンプ１７によ
りタンク１５に収容されているロ過液をパイプ３
１を通してタンク１４に還流させ、さらにパイプ
１３を逆流させてUFを洗浄するものである。タ
ンク１４に収容されたロ過液はパイプ１８を通つ
て50Kg／cm2の圧力でRO（商品名：SP110，東レ
製）１９および２０にかけられる。RO１９およ
び２０からのロ過液はパイプ２６，２７および２
５を通つて再利用可能な水分としてタンク２８に
収容される。RO１９および２０からの濃縮液は
再度RO２３にかけられ、そのロ過液はパイプ２
４および２５を通つてタンク２８に収容される。
RO２３からの濃縮液はパイプ２９を通つて冷却
器３０により冷却されてからタンク２に戻され、
再度UFおよびROに循環してかけられる。Example FIG. 1 shows the wastewater treatment equipment used in this example. A waste liquid 1, which is a supernatant liquid of lens cleaning and polishing waste liquid, is stored in a tank 2. This waste liquid is passed from the tank through a pipe 4 by a pump 3 to UF (product name:
AEC6050, manufactured by Asahi Kasei) 5, 6, 7, 8 and 9
is applied at a pressure of 1.5Kg/cm 2 . The concentrated liquid separated by the UF is stored in a tank 12 through pipes 10 and 11. This concentrated liquid is treated as waste. The filtrate from the UF is received through pipe 13 into tank 14 and further through pipe 16 into tank 15. The tank 15 is a reserve tank, and at the same time, when the semi-permeable membrane of the UF becomes clogged and the filtration effect decreases, the pump 17 pumps the filtrate stored in the tank 15 to the pipe 3.
1 to the tank 14, and further flows back through the pipe 13 to wash the UF. The filtrate contained in the tank 14 passes through a pipe 18 and is applied to RO (trade name: SP110, manufactured by Toray) 19 and 20 at a pressure of 50 kg/cm 2 . The filtrate from RO19 and 20 is passed through pipes 26, 27 and 2.
5 and is stored in a tank 28 as reusable water. The concentrated liquid from RO19 and 20 is passed through RO23 again, and the filtrate is passed through pipe 2.
4 and 25, and is stored in tank 28.
The concentrate from the RO 23 passes through the pipe 29 and is cooled by the cooler 30 before being returned to the tank 2.
It is cycled through UF and RO again.
このようにして、８トンの廃水を処理した結果
タンク２８に回収された再利用可能な水量は5.12
トンであつた。また、ROからの濃縮液の20％は
再度UFにかけないで廃棄した。なお、UFでのロ
過温度は27℃、ROでのロ過温度は42℃、および
冷却温度は18℃であつた。またROの耐久使用期
間は１年以上であつた。また、比較として廃液を
UFとROで順次１回処理した場合には、回収さ
れた再使用可能な水量は1.5トンに過ぎなかつた。
また、冷却処理をしないで廃液処理を連続的に２
週間行つた場合には、タンク２８に回収された水
量は２トンになつてしまい、回収水の電導度の初
期10μから150μと増大しており、再利用可能
な水分とならなかつた。冷却処理をした場合に
は、10μと不変であつた。また、冷却処理をし
なかつた場合にはROの耐久使用時間は２週間に
過ぎなかつた。 As a result of treating 8 tons of wastewater in this way, the amount of reusable water recovered in tank 28 is 5.12
It was a ton. Additionally, 20% of the concentrate from RO was discarded without being subjected to UF again. The filtration temperature in UF was 27°C, the filtration temperature in RO was 42°C, and the cooling temperature was 18°C. Moreover, the durable use period of RO was more than one year. Also, for comparison, waste liquid
In one sequential treatment with UF and RO, only 1.5 tons of reusable water was recovered.
In addition, waste liquid treatment can be carried out continuously without cooling treatment.
When the process was carried out for a week, the amount of water collected in the tank 28 was 2 tons, and the electrical conductivity of the collected water had increased from the initial 10μ to 150μ, and the water could not be reused. When subjected to cooling treatment, it remained unchanged at 10μ. Moreover, when no cooling treatment was performed, the durable use time of RO was only two weeks.
第１図は本発明による廃液処理方法を実施する
に用いた処理装置のフローチヤート図である。
１……廃液、２……タンク、５〜９……UF、
１４……タンク、１５……タンク、１９，２０お
よび２３……RO。
FIG. 1 is a flowchart of a treatment apparatus used to carry out the waste liquid treatment method according to the present invention. 1...Waste liquid, 2...Tank, 5-9...UF,
14...tank, 15...tank, 19, 20 and 23...RO.
Claims (1)
第１工程のロ過液を逆浸透ロ過器によりロ過する
第２工程、および第２工程の濃縮液を冷却処理後
再度限外ロ過器と逆浸透ロ過器でロ過する第３工
程を有することを特徴とする廃液処理方法。 ２ 第２工程の濃縮液のロ過を第１工程の限外ロ
過器を用いて循環させて第３工程を行う特許請求
の範囲第１項記載の廃液処理方法。[Claims] 1. A first step of filtering the waste liquid using an ultrafilter;
A second step in which the filtrate from the first step is filtered through a reverse osmosis filter, and a third step in which the concentrated liquid from the second step is filtered again through an ultrafilter and a reverse osmosis filter after being cooled. A waste liquid treatment method characterized by comprising a step. 2. The waste liquid treatment method according to claim 1, wherein the third step is carried out by circulating the filtration of the concentrated liquid in the second step using an ultrafilter in the first step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21191183A JPS60102905A (en) | 1983-11-11 | 1983-11-11 | Treatment of waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21191183A JPS60102905A (en) | 1983-11-11 | 1983-11-11 | Treatment of waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60102905A JPS60102905A (en) | 1985-06-07 |
| JPH05116B2 true JPH05116B2 (en) | 1993-01-05 |
Family
ID=16613692
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21191183A Granted JPS60102905A (en) | 1983-11-11 | 1983-11-11 | Treatment of waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60102905A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19517473A1 (en) * | 1995-05-12 | 1996-11-14 | Henkel Ecolab Gmbh & Co Ohg | Process for wastewater treatment with recovery of drinking water in high product yields |
| JP3379512B2 (en) | 1999-06-30 | 2003-02-24 | セイコーエプソン株式会社 | Cleaning apparatus, cleaning method, and method of manufacturing liquid crystal device |
| KR20020097102A (en) * | 2002-11-16 | 2002-12-31 | 서영석 | Ultrafiltration Reverse Osmosis Compound Purifier |
| KR100705612B1 (en) * | 2004-09-24 | 2007-04-11 | (주)비룡 | Rinsing water recovery apparatus of an electro deposit process and recovery method thereof |
| WO2021078681A1 (en) * | 2019-10-24 | 2021-04-29 | Baxter Healthcare Sa | A water purification apparatus, and a method for cooling a ro-membrane in a water purification apparatus |
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|---|---|---|---|---|
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| JPS58205501A (en) * | 1982-05-26 | 1983-11-30 | Japan Organo Co Ltd | Depositing method of electrolyte salts |
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1983
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50152984A (en) * | 1974-05-31 | 1975-12-09 | ||
| JPS52125476A (en) * | 1975-02-28 | 1977-10-21 | Ebara Infilco Co Ltd | Treatment of suspension |
| JPS5325265A (en) * | 1976-08-23 | 1978-03-08 | Nippon Abukoo Kk | Method of treating solution containing metal ions by using combined superr filter membrane and reverse osmosis membrane |
| JPS57167786A (en) * | 1981-04-08 | 1982-10-15 | Hajime Nakato | Treating device for industrial waste water containing colloidal materials |
| JPS58205501A (en) * | 1982-05-26 | 1983-11-30 | Japan Organo Co Ltd | Depositing method of electrolyte salts |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60102905A (en) | 1985-06-07 |
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