JP5860989B2 - Water treatment method and water treatment apparatus - Google Patents
Water treatment method and water treatment apparatus Download PDFInfo
- Publication number
- JP5860989B2 JP5860989B2 JP2015117738A JP2015117738A JP5860989B2 JP 5860989 B2 JP5860989 B2 JP 5860989B2 JP 2015117738 A JP2015117738 A JP 2015117738A JP 2015117738 A JP2015117738 A JP 2015117738A JP 5860989 B2 JP5860989 B2 JP 5860989B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- anaerobic
- treated
- treated water
- draw liquid
- 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.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 224
- 238000000034 method Methods 0.000 title claims description 51
- 239000007788 liquid Substances 0.000 claims description 107
- 239000012528 membrane Substances 0.000 claims description 68
- 150000003839 salts Chemical class 0.000 claims description 54
- 239000010802 sludge Substances 0.000 claims description 29
- 239000013535 sea water Substances 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 238000011084 recovery Methods 0.000 claims description 18
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 230000003204 osmotic effect Effects 0.000 claims description 10
- 229910052698 phosphorus Inorganic materials 0.000 claims description 10
- 239000011574 phosphorus Substances 0.000 claims description 10
- 239000005416 organic matter Substances 0.000 claims description 9
- 239000012141 concentrate Substances 0.000 claims description 3
- 230000008595 infiltration Effects 0.000 claims description 3
- 238000001764 infiltration Methods 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims 1
- 235000015097 nutrients Nutrition 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 239000012466 permeate Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- 238000009292 forward osmosis Methods 0.000 description 5
- 238000001223 reverse osmosis Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 238000005273 aeration Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 238000010979 pH adjustment Methods 0.000 description 3
- 238000003825 pressing Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229910052567 struvite Inorganic materials 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- -1 for example Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 230000009545 invasion Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
本発明は、有機物を含有する被処理水を嫌気処理する水処理方法および水処理装置に関する。 The present invention relates to a water treatment method and a water treatment apparatus for anaerobically treating water to be treated containing organic matter.
下水、河川水又は海水等の有機物を含有する被処理水を処理する水処理方法として、種々の方法が提案されている。例えば、好気的な活性汚泥法では、被処理水が活性汚泥と混合されることで、活性汚泥中の好気性微生物の作用によって、被処理水中の有機物は、好気的に分解され、主に二酸化炭素等として除去される。このため、斯かる活性汚泥法では、活性汚泥中の微生物の活性を維持するために、被処理水と活性汚泥とが混合された混合水の曝気が行われている。 Various methods have been proposed as water treatment methods for treating water to be treated containing organic matter such as sewage, river water or seawater. For example, in the aerobic activated sludge method, the water to be treated is mixed with the activated sludge, so that the organic matter in the treated water is aerobically decomposed by the action of aerobic microorganisms in the activated sludge. To be removed as carbon dioxide. For this reason, in such an activated sludge method, in order to maintain the activity of microorganisms in the activated sludge, aeration of mixed water in which treated water and activated sludge are mixed is performed.
このような好気的な活性汚泥法では、曝気を行う際にブロア等の設備が必要となるため、それを稼動させるための動力が必要となり、エネルギーの消費が比較的大きい。このため、エネルギーの消費を抑える等の観点から、有機物を分解する際の曝気を必要としない嫌気的な活性汚泥法が用いられる。斯かる方法としては、嫌気的な活性汚泥法と膜分離法とを組み合わせた嫌気性膜分離活性汚泥法（以下、嫌気性ＭＢＲ法とも記す）が知られている。斯かる嫌気性ＭＢＲ法では、嫌気性微生物を含有する汚泥と被処理水とが混合されて嫌気的な環境下に配置されることで、斯かる汚泥中の嫌気性細菌の作用によって、被処理水中の有機物が嫌気的に分解されるように構成されている（浄化工程）。そして、浄化工程後の混合水が分離膜（精密濾過膜（ＭＦ膜）や限外濾過膜（ＵＦ膜）等）で濾過されることで（膜分離工程）、活性汚泥が分離されてなる処理水が得られる。一方、分離された活性汚泥は、浄化工程へ返送されて再利用されることで、活性汚泥の流出が防止される（特許文献１参照）。 In such an aerobic activated sludge method, since equipment such as a blower is required when aeration is performed, power for operating the equipment is required, and energy consumption is relatively large. For this reason, the anaerobic activated sludge method which does not require aeration at the time of decomposing | disassembling organic substance from a viewpoint of suppressing consumption of energy etc. is used. As such a method, an anaerobic membrane separation activated sludge method (hereinafter, also referred to as an anaerobic MBR method) in which an anaerobic activated sludge method and a membrane separation method are combined is known. In such anaerobic MBR method, the sludge containing anaerobic microorganisms and the water to be treated are mixed and placed in an anaerobic environment, so that the treatment is performed by the action of the anaerobic bacteria in the sludge. It is comprised so that the organic substance in water may be decomposed | disassembled anaerobically (purification process). Then, the mixed water after the purification process is filtered through a separation membrane (microfiltration membrane (MF membrane), ultrafiltration membrane (UF membrane), etc.) (membrane separation step), and activated sludge is separated. Water is obtained. On the other hand, the separated activated sludge is returned to the purification process and reused, thereby preventing the activated sludge from flowing out (see Patent Document 1).
ところで、上記のように、嫌気性ＭＢＲ法で処理された被処理水（以下、嫌気処理水とも記す）は、通常、環境中（河川や海域等）に放流されることになるが、斯かる嫌気処理水には、窒素成分やリン成分等が含有されている。これらの成分は、植物の肥料や活性汚泥の栄養成分等として利用可能な塩類であるため、斯かる塩類を回収することが望まれている。 By the way, as described above, the water to be treated (hereinafter also referred to as anaerobic treated water) treated by the anaerobic MBR method is usually discharged into the environment (river, sea area, etc.). The anaerobic treated water contains a nitrogen component, a phosphorus component, and the like. Since these components are salts that can be used as nutrients for plant fertilizers, activated sludge, and the like, it is desired to recover such salts.
そこで、本発明は、嫌気性ＭＢＲ法によって処理された被処理水から塩類を効率的に回収することができ、斯かる塩類を有効に使用することを可能にする水処理方法および水処理装置を提供することを課題とする。 Therefore, the present invention provides a water treatment method and a water treatment apparatus capable of efficiently recovering salts from water to be treated treated by the anaerobic MBR method, and enabling effective use of such salts. The issue is to provide.
本発明に係る水処理方法は、有機物を含有する被処理水の嫌気処理と該嫌気処理後の被処理水の膜分離とを行う膜分離活性汚泥法を用いた嫌気処理工程を備える水処理方法であって、前記嫌気処理工程で処理された被処理水から構成される嫌気処理水と該嫌気処理水から半透膜を介して水分の浸透を受けて浸透圧が生じるように構成されたドロー液とを半透膜を介して接触させることで嫌気処理水を濃縮する濃縮工程と、該濃縮工程で濃縮された嫌気処理水から構成される濃縮水から窒素成分又はリン成分の少なくとも一方の塩類を回収すると共に嫌気処理工程後であって濃縮工程前の嫌気処理水へ塩類を回収した後の濃縮水を返送する塩類回収工程とを備え、前記ドロー液は、海水から構成されることを特徴とする。
A water treatment method according to the present invention comprises an anaerobic treatment step using a membrane separation activated sludge method that performs anaerobic treatment of water to be treated containing organic matter and membrane separation of the water to be treated after the anaerobic treatment. An anaerobic treatment water composed of the treated water treated in the anaerobic treatment step and a draw configured to generate an osmotic pressure by receiving moisture permeation from the anaerobic treatment water through a semipermeable membrane. A concentration step of concentrating anaerobic treated water by contacting the liquid with a semipermeable membrane, and at least one salt of a nitrogen component or a phosphorus component from the concentrated water composed of the anaerobic treated water concentrated in the concentration step and a salt recovery step to return your concentrated water after salt was collected even after the anaerobic treatment step to concentration step prior to the anaerobic treatment water is recovered, said draw liquid, the Rukoto consists seawater Features.
斯かる構成によれば、濃縮工程では、浸透圧によって嫌気処理水からドロー液側へ半透膜を介して水分が浸透することになる（正浸透）。これにより、濃縮工程では、逆浸透のように圧力を掛けたり、減圧したりする動力を用いることなく、嫌気処理水の水分量が減少し、嫌気処理水が濃縮されることになる。そして、濃縮された嫌気処理水（以下、濃縮水とも記す）には、塩類が濃縮前よりも高濃度で含有されるため、塩類回収工程において濃縮水から塩類を効率的に回収することができる。 According to such a configuration, in the concentration step, moisture permeates from the anaerobic treated water to the draw liquid side through the semipermeable membrane by the osmotic pressure (forward osmosis). As a result, in the concentration step, the amount of moisture in the anaerobic treated water is reduced and the anaerobic treated water is concentrated without using power for applying pressure or reducing pressure as in reverse osmosis. In the concentrated anaerobic treated water (hereinafter also referred to as concentrated water), since salts are contained at a higher concentration than before concentration, the salts can be efficiently recovered from the concentrated water in the salt recovery step. .
前記ドロー液は、海水から構成される。
The draw solution, that consists of sea water.
斯かる構成によれば、ドロー液が海水から構成されることで、ドロー液の環境中への放出を容易に行うことができる。具体的には、ドロー液が海水である場合には、嫌気処理水からドロー液側へは水分のみが移動し、他の溶質は半透膜によりドロー液側への移動が阻止され濃縮側（即ち、嫌気処理水側）に残存する。このため、嫌気処理水から水分の浸透を受けたドロー液は、海水が希釈されたものとなる。このため、濃縮工程後のドロー液に対して、環境中へ排水するための処理（例えば、ｐＨ調整や不要な成分の除去等）を行う必要が無く、濃縮工程後のドロー液を直接海洋へ放流することが可能となる。
According to such a configuration, since the draw solution is constituted sea water or, et al., It is possible to easily release into the draw solution in the environment. Specifically, when the draw liquid is seawater, only moisture moves from the anaerobic treated water to the draw liquid side, and other solutes are prevented from moving to the draw liquid side by the semipermeable membrane, and the concentration side ( That is, it remains on the anaerobic treated water side). For this reason, the draw liquid that has received moisture permeation from the anaerobic treated water is one in which seawater is diluted. For this reason, there is no need to perform a process for draining into the environment (for example, pH adjustment or removal of unnecessary components) on the draw liquid after the concentration process, and the draw liquid after the concentration process is directly sent to the ocean. It can be discharged and that Do not.
前記塩類は、窒素成分又はリン成分の少なくとも一方である。
The salts, Ru least one Der nitrogen component or phosphorous component.
本発明に係る水処理装置は、有機物を含有する被処理水の嫌気処理と該嫌気処理後の被処理水の膜分離とを行う膜分離活性汚泥法を用いた嫌気処理部を備える水処理装置であって、前記嫌気処理部で処理された被処理水で構成される嫌気処理水を濃縮する濃縮装置と、該濃縮装置で濃縮された嫌気処理水から構成される濃縮水から窒素成分又はリン成分の少なくとも一方の塩類を回収すると共に嫌気処理部で処理されて濃縮装置へ供給される前の嫌気処理水へ塩類を回収した後の濃縮水を返送可能に構成された塩類回収部とを更に備え、前記濃縮装置は、半透膜を介して嫌気処理水から水分の浸透を受けて浸透圧が生じるように構成されたドロー液が供給されるドロー液供給部と、嫌気処理水が供給される嫌気処理水供給部とを備えると共に半透膜を介して嫌気処理水とドロー液とが接触するように構成されており、前記ドロー液は、海水から構成されることを特徴とする。
A water treatment apparatus according to the present invention includes an anaerobic treatment unit using a membrane separation activated sludge method that performs anaerobic treatment of water to be treated containing organic matter and membrane separation of the water to be treated after the anaerobic treatment. A concentrating device for concentrating anaerobic treated water composed of the treated water treated in the anaerobic treatment section, and a nitrogen component or phosphorus from the concentrated water composed of the anaerobic treated water concentrated by the concentrating device. and salts recovery section is returned feed configured to be able to concentrate after the recovery of salts Previous anaerobic process water is treated in anaerobic processing unit is supplied to the concentrator is recovered at least one of the salts of component The concentrating device further includes a draw liquid supply unit configured to receive a water permeation from the anaerobic treated water through the semipermeable membrane to generate an osmotic pressure, and the anaerobic treated water is supplied. With an anaerobic treated water supply unit Through the permeable membrane is configured to contact and anaerobic treated water and draw liquid, the draw solution is composed of sea water, characterized in Rukoto.
斯かる構成によれば、濃縮装置では、浸透圧によって嫌気処理水からドロー液側へ半透膜を介して水分が浸透することになる（正浸透）。これにより、濃縮装置では、逆浸透のように圧力を掛けたり、減圧したりする動力を用いることなく、嫌気処理水の水分量が減少し、嫌気処理水が濃縮されることになる。そして、濃縮された嫌気処理水（以下、濃縮水とも記す）には、塩類が濃縮前よりも高濃度で含有されるため、塩類回収部において濃縮水から塩類を効率的に回収することができる。 According to such a configuration, in the concentrating device, moisture permeates from the anaerobic treated water to the draw liquid side through the semipermeable membrane by the osmotic pressure (forward osmosis). Thereby, in the concentrating device, the amount of water in the anaerobic treated water is reduced and the anaerobic treated water is concentrated without using power for applying pressure or reducing pressure as in reverse osmosis. The concentrated anaerobic treated water (hereinafter also referred to as concentrated water) contains salts at a higher concentration than before the concentration, so that the salts can be efficiently recovered from the concentrated water in the salt recovery unit. .
前記ドロー液は、海水から構成される。
The draw solution, that consists of sea water.
斯かる構成によれば、ドロー液が海水から構成されることで、ドロー液の環境中への放出を容易に行うことができる。具体的には、ドロー液が海水である場合には、嫌気処理水からドロー液側へは水分のみが移動し、他の溶質は半透膜によりドロー液側への移動が阻止され濃縮側（即ち、嫌気処理水側）に残存する。このため、嫌気処理水から水分が浸透したドロー液は、海水が希釈されたものとなる。このため、濃縮装置から放出されるドロー液に対して、環境中へ排水するための処理（例えば、ｐＨ調整や不要な成分の除去等）を行う必要が無く、濃縮装置から放出されるドロー液を直接海洋へ放流することが可能となる。
According to such a configuration, since the draw solution is constituted sea water or, et al., It is possible to easily release into the draw solution in the environment. Specifically, when the draw liquid is seawater, only moisture moves from the anaerobic treated water to the draw liquid side, and other solutes are prevented from moving to the draw liquid side by the semipermeable membrane, and the concentration side ( That is, it remains on the anaerobic treated water side). For this reason, the draw liquid in which water permeates from the anaerobic treated water is diluted with seawater. For this reason, it is not necessary to perform a process for draining into the environment (for example, pH adjustment or removal of unnecessary components) with respect to the draw liquid discharged from the concentration apparatus, and the draw liquid discharged from the concentration apparatus. that Do is possible to make the discharged directly into the ocean.
前記塩類は、窒素成分又はリン成分の少なくとも一方である。 The salts, Ru least one Der nitrogen component or phosphorous component.
以上のように、本発明によれば、嫌気性ＭＢＲ法によって処理された被処理水から塩類を効率的に回収し、斯かる塩類を有効に使用することができる。 As described above, according to the present invention, salts can be efficiently recovered from water to be treated treated by the anaerobic MBR method, and such salts can be used effectively.
＜第一実施形態＞
以下、本発明の第一実施形態について図１および２を参照しながら説明する。なお、以下の図面において同一又は相当する部分には同一の参照符号を付しその説明は繰り返さない。
<First embodiment>
Hereinafter, a first embodiment of the present invention will be described with reference to FIGS. 1 and 2. In the following drawings, the same or corresponding parts are denoted by the same reference numerals, and the description thereof will not be repeated.
本実施形態に係る水処理装置１は、有機物を含有する被処理水が嫌気処理されるように構成される。具体的には、水処理装置１は、被処理水が供給されて嫌気処理される嫌気処理部２と、嫌気処理部２で処理された被処理水（以下、嫌気処理水とも記す）を濃縮する濃縮装置３と、濃縮された嫌気処理水から塩類を回収する塩類回収部４とを備える。被処理水としては、特に限定されるものではないが、下水や食品工場等からの排水等が挙げられる。 The water treatment apparatus 1 according to the present embodiment is configured such that water to be treated containing an organic substance is subjected to anaerobic treatment. Specifically, the water treatment apparatus 1 concentrates the anaerobic treatment unit 2 that is supplied with the treated water and anaerobically treated, and the treated water treated by the anaerobic treatment unit 2 (hereinafter also referred to as anaerobic treated water). And a salt recovery unit 4 that recovers salts from the concentrated anaerobic treated water. The water to be treated is not particularly limited, and examples thereof include sewage and waste water from food factories.
嫌気処理部２は、被処理水の嫌気処理を行う嫌気処理槽２ａと、嫌気処理後の被処理水を膜分離する膜分離装置２ｂとを備える。嫌気処理槽２ａは、例えば、メタン発酵法によって被処理水中の有機物を分解可能に構成される。具体的には、嫌気処理槽２ａは、有機物を嫌気的に分解する嫌気性細菌を含有する汚泥（以下、嫌気性汚泥とも記す）が内部に供給されており、被処理水と嫌気性汚泥とが混合されて混合液が形成されるように構成される。そして、斯かる混合水が嫌気処理槽２ａ内の嫌気的な環境下に配置されることで、嫌気性汚泥によって有機物が分解されるように構成される。嫌気処理槽２ａに供給される被処理水のＢＯＤとしては、特に限定されるものではなく、１０００ｍｇ／Ｌ以上２０００ｍｇ／Ｌ未満であってもよく、２０００ｍｇ／Ｌ以上であってもよい。 The anaerobic treatment unit 2 includes an anaerobic treatment tank 2a that performs anaerobic treatment of water to be treated and a membrane separation device 2b that membrane-separates the water to be treated after the anaerobic treatment. The anaerobic treatment tank 2a is configured to be able to decompose organic substances in the water to be treated by, for example, a methane fermentation method. Specifically, the anaerobic treatment tank 2a is supplied with sludge containing anaerobic bacteria that decomposes organic matter anaerobically (hereinafter also referred to as anaerobic sludge). Are mixed to form a mixed solution. And it is comprised so that organic substance may be decomposed | disassembled by anaerobic sludge by arrange | positioning such mixed water in the anaerobic environment in the anaerobic treatment tank 2a. The BOD of the water to be treated supplied to the anaerobic treatment tank 2a is not particularly limited, and may be 1000 mg / L or more and less than 2000 mg / L, or 2000 mg / L or more.
膜分離装置２ｂでは、嫌気処理槽２ａで処理された被処理水（具体的には、嫌気処理槽２ａから排出される混合水）から嫌気性汚泥が分離される。具体的には、膜分離装置２ｂは、混合水が供給される内部空間と、該内部空間に配置された分離膜（精密濾過膜（ＭＦ膜）や限外濾過膜（ＵＦ膜）等）とを備える。そして、混合水が分離膜によって濾過されることで、被処理水（即ち、嫌気処理水）と嫌気性汚泥とが分離される。分離された嫌気性汚泥は、嫌気処理槽２ａへ返送されるように構成される。なお、濃縮装置３に供給される前の嫌気処理水に対して、温度やｐＨや流量等の調節が行われてもよい。これによりファウリングを抑制することができる。 In the membrane separation device 2b, anaerobic sludge is separated from the water to be treated (specifically, the mixed water discharged from the anaerobic treatment tank 2a) treated in the anaerobic treatment tank 2a. Specifically, the membrane separation device 2b includes an internal space to which mixed water is supplied, and a separation membrane (such as a microfiltration membrane (MF membrane) or an ultrafiltration membrane (UF membrane)) disposed in the internal space. Is provided. And the to-be-processed water (namely, anaerobic treated water) and anaerobic sludge are isolate | separated by filtering mixed water with a separation membrane. The separated anaerobic sludge is configured to be returned to the anaerobic treatment tank 2a. The temperature, pH, flow rate, and the like may be adjusted for the anaerobic treated water before being supplied to the concentrating device 3. Thereby, fouling can be suppressed.
濃縮装置３は、図２に示すように、半透膜３ａで仕切られた内部空間を備える。これにより、濃縮装置３は、嫌気処理水が供給される内部空間を有する嫌気処理水供給部３ｂと、半透膜３ａを介して被処理水から水分の浸透を受けて浸透圧を生じるように構成されたドロー液が供給される内部空間を有するドロー液供給部３ｃとを備える。そして、濃縮装置３は、供給される被処理水とドロー液とが半透膜３ａを介して接触するように構成される。つまり、本実施形態の濃縮装置３は、嫌気処理水供給部３ｂの内部空間とドロー液供給部３ｃ内の内部空間とが半透膜３ａを介して併設されるように構成される（槽外型）。半透膜３ａとしては、特に限定されるものではなく、一般的な正浸透膜や逆浸透膜を用いることができる。 As shown in FIG. 2, the concentrating device 3 includes an internal space partitioned by a semipermeable membrane 3a. Thereby, the concentrating device 3 receives an infiltration of moisture from the water to be treated through the anaerobic treated water supply unit 3b having an internal space to which the anaerobic treated water is supplied, and the semipermeable membrane 3a so as to generate osmotic pressure. And a draw liquid supply unit 3c having an internal space to which the constituted draw liquid is supplied. And the concentration apparatus 3 is comprised so that the to-be-processed water and draw liquid which are supplied may contact via the semipermeable membrane 3a. That is, the concentrating device 3 of the present embodiment is configured such that the internal space of the anaerobic treated water supply unit 3b and the internal space of the draw liquid supply unit 3c are provided side by side through the semipermeable membrane 3a (outside the tank). Type). The semipermeable membrane 3a is not particularly limited, and a general forward osmosis membrane or reverse osmosis membrane can be used.
嫌気処理水供給部３ｂは、嫌気処理部２と流体的に連結される。具体的には、嫌気処理水供給部３ｂは、膜分離装置２ｂと流体的に連結されて嫌気処理水供給部３ｂ内へ嫌気処理水を導入する嫌気処理水導入部３１ｂと、塩類回収部４に流体的に連結されて嫌気処理水供給部３ｂ内から被処理水を排出する嫌気処理水排出部３２ｂとを備える。 The anaerobic treated water supply unit 3 b is fluidly connected to the anaerobic treatment unit 2. Specifically, the anaerobic treated water supply unit 3b is fluidly connected to the membrane separation device 2b and introduces the anaerobic treated water into the anaerobic treated water supply unit 3b, and the salt recovery unit 4 And an anaerobic treated water discharge part 32b for discharging treated water from the anaerobic treated water supply part 3b.
ドロー液供給部３ｃは、ドロー液の供給源と流体的に連結されてドロー液供給部３ｃ内へドロー液を導入するドロー液導入部３１ｃと、ドロー液の排出先に流体的に連結されてドロー液供給部３ｃ内からドロー液を排出するドロー液排出部３２ｃとを備える。 The draw liquid supply unit 3c is fluidly connected to a draw liquid supply source and fluidly connected to a draw liquid introduction unit 31c for introducing the draw liquid into the draw liquid supply unit 3c, and a discharge destination of the draw liquid. And a draw liquid discharge part 32c for discharging the draw liquid from the draw liquid supply part 3c.
ドロー液としては、特に限定されるものではなく、本実施形態では、海水が用いられる。つまり、本実施形態では、ドロー液の供給源および排出先としては、海洋Ｓを使用することができる。 The draw liquid is not particularly limited, and seawater is used in the present embodiment. That is, in this embodiment, the ocean S can be used as the supply source and the discharge destination of the draw liquid.
塩類回収部４は、濃縮装置３に流体的に連結されて濃縮された嫌気処理水が供給されるように構成される。斯かる嫌気処理水には、塩類（具体的には、窒素成分やリン成分等の栄養塩類）が含有されているため、塩類回収部４では、濃縮された嫌気処理水から塩類（具体的には、栄養塩類）が回収されるように構成される。 The salt recovery unit 4 is configured to be supplied with concentrated anaerobic water that is fluidly connected to the concentrating device 3. Since such anaerobic treated water contains salts (specifically, nutrient salts such as nitrogen components and phosphorus components), the salt recovery unit 4 uses salts (specifically, from the concentrated anaerobic treated water). Is configured to recover nutrients).
次に、上記のように構成される水処理装置１を用いて被処理水を処理する方法について説明する。 Next, a method for treating the water to be treated using the water treatment apparatus 1 configured as described above will be described.
被処理水（原水）は、嫌気処理部２に供給される。具体的には、被処理水は、嫌気処理槽２ａに供給される。嫌気処理槽２ａでは、被処理水と嫌気性汚泥とが混合されて混合水が形成される。そして、該混合水が嫌気処理（メタン発酵）に適した条件（具体的には、ｐＨや温度等）で維持される。これにより、被処理水中の有機物が嫌気処理されて分解され、メタンガスが生成される（嫌気処理工程）。生成したメタンガスは、嫌気処理槽２ａから排出されて回収され、燃料や原料として使用することができる。一方、嫌気処理槽２ａ内の混合水は、嫌気処理槽２ａから排出されて、膜分離装置２ｂへ供給される。 The treated water (raw water) is supplied to the anaerobic treatment unit 2. Specifically, the water to be treated is supplied to the anaerobic treatment tank 2a. In the anaerobic treatment tank 2a, the water to be treated and anaerobic sludge are mixed to form mixed water. And this mixed water is maintained on the conditions (specifically pH, temperature, etc.) suitable for anaerobic treatment (methane fermentation). Thereby, the organic substance in to-be-processed water is anaerobically treated and decomposed | disassembled, and methane gas is produced | generated (anaerobic treatment process). The produced | generated methane gas is discharged | emitted from the anaerobic processing tank 2a, is collect | recovered, and can be used as a fuel or a raw material. On the other hand, the mixed water in the anaerobic treatment tank 2a is discharged from the anaerobic treatment tank 2a and supplied to the membrane separation device 2b.
膜分離装置２ｂでは、混合水が分離膜によって濾過されることで、有機物が分解された被処理水（即ち、嫌気処理水）と嫌気性汚泥とが分離される。分離された嫌気性汚泥は、少なくとも一部が嫌気処理槽２ａへ返送される。嫌気処理水は、嫌気処理部２（具体的には、膜分離装置２ｂ）から排出されて濃縮装置３（具体的には、嫌気処理水供給部３ｂ）へ供給される。これに伴い、濃縮装置３（具体的には、ドロー液供給部３ｃ）には、ドロー液として海水が供給される。 In the membrane separation device 2b, the water to be treated (that is, anaerobic treated water) from which the organic matter has been decomposed and the anaerobic sludge are separated by filtering the mixed water through the separation membrane. At least a part of the separated anaerobic sludge is returned to the anaerobic treatment tank 2a. The anaerobic treated water is discharged from the anaerobic treatment unit 2 (specifically, the membrane separation device 2b) and supplied to the concentrating device 3 (specifically, the anaerobic treated water supply unit 3b). Along with this, seawater is supplied to the concentrator 3 (specifically, the draw liquid supply unit 3c) as the draw liquid.
このように、嫌気処理水供給部３ｂに嫌気処理水が供給され、ドロー液供給部３ｃにドロー液として海水が供給されることで、濃縮装置３内で被処理水と海水とが半透膜３ａを介して接触した状態になると共に、浸透圧によって嫌気処理水の水分が半透膜３ａを透過して海水側に浸透（正浸透）する。これにより、嫌気処理水供給部３ｂ内で、嫌気処理水が濃縮されて塩類（具体的には、栄養塩類）の濃度が上昇する（濃縮工程）。一方、ドロー液供給部３ｃ内では、嫌気処理水からの水分の浸透を受けて海水が希釈される。 As described above, the anaerobic treated water is supplied to the anaerobic treated water supply unit 3b, and seawater is supplied as the draw liquid to the draw liquid supply unit 3c. While being in contact via 3a, the moisture of the anaerobic treated water permeates through the semipermeable membrane 3a and permeates into the seawater side (forward osmosis). Thereby, in the anaerobic treated water supply part 3b, the anaerobic treated water is concentrated and the concentration of salts (specifically, nutrient salts) increases (concentration step). On the other hand, in the draw liquid supply unit 3c, seawater is diluted by receiving moisture permeation from the anaerobic treated water.
本実施形態では、嫌気処理水排出部３２ｂおよびドロー液排出部３２ｃが半透膜３ａの近傍に設けられ、被処理水とドロー液とが濃縮装置３へ適度な流量で供給されることで、半透膜３ａの近傍の嫌気処理水（即ち、濃縮された嫌気処理水）および海水（即ち、希釈された海水）が迅速に濃縮装置３の外側に排出される。これにより、嫌気処理水および海水が半透膜３ａの近傍で滞留し、浸透効率が低下するのが防止される。そして、濃縮された嫌気処理水は、塩類回収部４へ供給される。一方、希釈された海水は、河川や海洋Ｓ等の環境中に放出可能な水質であれば、更に水処理されることなく環境中に放出することができるが、更に所望の水質となるように水処理された後、環境中へ放出されてもよい。 In this embodiment, the anaerobic treated water discharge part 32b and the draw liquid discharge part 32c are provided in the vicinity of the semipermeable membrane 3a, and the treated water and the draw liquid are supplied to the concentrating device 3 at an appropriate flow rate. Anaerobic treated water (ie, concentrated anaerobic treated water) and seawater (ie, diluted seawater) in the vicinity of the semipermeable membrane 3a are quickly discharged to the outside of the concentrating device 3. This prevents anaerobic treated water and seawater from staying in the vicinity of the semipermeable membrane 3a and lowering the permeation efficiency. The concentrated anaerobic treated water is supplied to the salt recovery unit 4. On the other hand, diluted seawater can be released into the environment without further water treatment as long as it can be released into the environment such as rivers and ocean S, so that the desired water quality can be obtained. After being treated with water, it may be released into the environment.
塩類回収部４では、濃縮された嫌気処理水から塩類が回収される。塩類を回収する方法としては、特に限定されるものではないが、例えば、栄養塩類である窒素成分を回収する方法としては、濃縮された嫌気処理水に空気やスチームを吹き込むことで、嫌気処理水中のアンモニア性窒素をアンモニアガスとして回収するアンモニアストリッピング法等を採用することができる。また、栄養塩類であるリン成分を回収する方法としては、濃縮された嫌気処理水に対し、アルミニウム塩（硫酸バンドやＰＡＣ等）を添加してリン成分を凝集沈殿させることで回収する方法等を採用することができる。又は、濃縮された嫌気処理水中のリン成分をリン酸マグネシウムアンモニウム（ＭＡＰ）として造粒して回収する方法等を採用することができる。回収された栄養塩類は、系外へ排出され、栄養塩類以外の水分は膜分離装置２ｂ後の被処理水ラインに返送される。また、図示していないが嫌気処理部２（具体的には、嫌気処理槽２ａ）へ供給される被処理水ラインへ返送することも可能である。 In the salt recovery unit 4, salts are recovered from the concentrated anaerobic treated water. The method for recovering the salt is not particularly limited. For example, as a method for recovering the nitrogen component that is a nutrient salt, by blowing air or steam into the concentrated anaerobic treated water, An ammonia stripping method or the like that recovers ammonia nitrogen as ammonia gas can be employed. In addition, as a method of recovering the phosphorus component that is a nutrient salt, a method of recovering the concentrated anaerobic treated water by adding an aluminum salt (sulfuric acid band, PAC, etc.) and coagulating and precipitating the phosphorus component, etc. Can be adopted. Alternatively, a method of granulating and recovering the phosphorus component in the concentrated anaerobic treated water as magnesium ammonium phosphate (MAP) can be employed. The collected nutrient salts are discharged out of the system, and moisture other than the nutrient salts is returned to the treated water line after the membrane separation device 2b. Moreover, although not shown in figure, it is also possible to return to the to-be-processed water line supplied to the anaerobic process part 2 (specifically, the anaerobic process tank 2a).
以上のように、本発明に係る水処理方法および水処理装置によれば、嫌気性ＭＢＲ法によって処理された被処理水から塩類を効率的に回収し、斯かる塩類を有効に使用することができる。 As described above, according to the water treatment method and the water treatment apparatus according to the present invention, it is possible to efficiently recover salts from the water to be treated treated by the anaerobic MBR method, and to effectively use such salts. it can.
即ち、上記水処理装置１は、濃縮装置３では、浸透圧によって嫌気処理水からドロー液側へ半透膜３ａを介して水分が浸透することになる（正浸透）。これにより、濃縮装置３では、逆浸透のように圧力を掛けたり、減圧したりする動力を用いることなく、嫌気処理水の水分量が減少し、嫌気処理水が濃縮されることになる。そして、濃縮された嫌気処理水（以下、濃縮水とも記す）には、塩類が濃縮前よりも高濃度で含有されるため、塩類回収部４において濃縮水から塩類を効率的に回収することができる。回収された塩類が窒素成分やリン成分等の栄養塩類である場合には、植物等の肥料として利用することにより、嫌気処理水に含有される栄養塩類の有効利用を図ることができる。 That is, in the water treatment apparatus 1, in the concentration apparatus 3, moisture permeates from the anaerobic treated water to the draw liquid side through the semipermeable membrane 3 a due to osmotic pressure (forward osmosis). Thereby, in the concentration apparatus 3, the water content of anaerobic treated water is reduced and the anaerobic treated water is concentrated without using power for applying pressure or reducing pressure as in reverse osmosis. In the concentrated anaerobic treated water (hereinafter also referred to as concentrated water), the salts are contained at a higher concentration than before the concentration, so that the salts can be efficiently recovered from the concentrated water in the salt recovery unit 4. it can. When the recovered salts are nutrient salts such as nitrogen component and phosphorus component, effective utilization of the nutrient salts contained in the anaerobic treated water can be achieved by using them as fertilizers such as plants.
また、ドロー液が海水である場合には、嫌気処理水から水分の浸透を受けたドロー液は、海水が希釈されたものとなる。このため、濃縮装置から放出されるドロー液に対して、環境中へ排水するための処理（例えば、ｐＨ調整や不要な成分の除去等）を行う必要が無く、濃縮装置から放出されるドロー液を直接海洋へ放流することが可能となる。 In addition, when the draw liquid is seawater, the draw liquid that has been infiltrated with moisture from the anaerobic treated water is diluted with seawater. For this reason, it is not necessary to perform a process for draining into the environment (for example, pH adjustment or removal of unnecessary components) with respect to the draw liquid discharged from the concentration apparatus, and the draw liquid discharged from the concentration apparatus. Can be released directly into the ocean.
＜第二実施形態＞
次に、本発明の第二実施形態について、図３を用いて説明する。第二実施形態に係る水処理方法および水処理装置は、第一実施形態に係る水処理方法および水処理装置１と比較すると、主に濃縮装置３００の構成が異なるものである。具体的には、濃縮装置３００は、第一実施形態に係る濃縮装置３と比較すると、主に嫌気処理水供給部３００ｂとドロー液供給部３００ｃの構成が異なる。従って、以下では、第一実施形態と異なる点を中心に説明し、同一の構成に対しては同一の符号を付すこととして説明を省略する。
<Second embodiment>
Next, a second embodiment of the present invention will be described with reference to FIG. Compared with the water treatment method and the water treatment apparatus 1 according to the first embodiment, the water treatment method and the water treatment apparatus according to the second embodiment mainly differ in the configuration of the concentration apparatus 300. Specifically, the concentrating device 300 is different from the concentrating device 3 according to the first embodiment mainly in the configurations of the anaerobic treated water supply unit 300b and the draw liquid supply unit 300c. Therefore, below, it demonstrates centering on a different point from 1st embodiment, and abbreviate | omits description by attaching | subjecting the same code | symbol to the same structure.
濃縮装置３００は、ドロー液供給部３００ｃにおけるドロー液を供給する内部空間に、嫌気処理水供給部３００ｂが配置されて構成される。該嫌気処理水供給部３００ｂは、嫌気処理水を供給する内部空間を備え、該内部空間が半透膜３ａによってドロー液供給部３００ｃの内部空間から仕切られている。つまり、嫌気処理水供給部３００ｂは、少なくとも一部が半透膜３ａから構成され、少なくとも半透膜３ａで構成された部分が嫌気処理水供給部３００ｂの内部空間に位置する。なお、ドロー液供給部３００ｃは、槽外型のようにドロー液排出部３２ｃを備えていない。 The concentrator 300 is configured by disposing an anaerobic treated water supply unit 300b in an internal space for supplying the draw liquid in the draw liquid supply unit 300c. The anaerobic treated water supply unit 300b includes an internal space for supplying anaerobic treated water, and the internal space is partitioned from the internal space of the draw liquid supply unit 300c by a semipermeable membrane 3a. That is, at least a part of the anaerobic treated water supply unit 300b is configured by the semipermeable membrane 3a, and at least a part configured by the semipermeable membrane 3a is located in the internal space of the anaerobic treated water supply unit 300b. In addition, the draw liquid supply part 300c is not provided with the draw liquid discharge part 32c unlike the outside tank type.
斯かる構成の濃縮装置３００では、ドロー液供給部３００ｃに（具体的には、ドロー液を供給する設備Ｘから）ドロー液が供給されることで、嫌気処理水供給部３００ｂ（具体的には、半透膜３ａで構成された部分）がドロー液に浸漬された状態となる（浸漬型）。そして、嫌気処理水供給部３００ｂに嫌気処理水が供給されることで、半透膜３ａを介して嫌気処理水とドロー液とが接触した状態となり、嫌気処理水からドロー液への水分の浸透が生じる。斯かる構成によれば、嫌気処理水供給部３００ｂがドロー液内に浸漬された状態となるため、ドロー液側へ浸透した水分がドロー液供給部３００ｃ内に拡散され易い。このため、半透膜３ａの近傍において嫌気処理水側の濃度とドロー液側の濃度との差が少なくなって浸透圧が生じ難くなるのが防止される。これにより、被処理水からドロー液への水分の浸透が効率的に行われるため、嫌気処理水の濃縮を効率的に行うことができる。なお、ドロー液供給部３００ｃ内のドロー液は、オーバーフローすることで、ドロー液供給部３００ｃ内から排出される。また、ドロー液と嫌気処理水との半透膜３ａを介した接触（言い換えれば、半透膜３ａとの接触）を効率的に行うべく、攪拌装置等（図示せず）を用いてドロー液供給部３００ｃ内を攪拌して流量（ドロー液供給部３００ｃからのドロー液の排出量）を調節してもよい。 In the concentrator 300 having such a configuration, the anaerobic treated water supply unit 300b (specifically, the draw liquid is supplied to the draw liquid supply unit 300c (specifically, from the equipment X that supplies the draw liquid). , The portion constituted by the semipermeable membrane 3a) is immersed in the draw liquid (immersion type). Then, the anaerobic treated water is supplied to the anaerobic treated water supply unit 300b, whereby the anaerobic treated water and the draw liquid are brought into contact with each other through the semipermeable membrane 3a, and moisture permeates from the anaerobic treated water into the draw liquid. Occurs. According to such a configuration, since the anaerobic treated water supply unit 300b is immersed in the draw liquid, moisture that has permeated into the draw liquid side is easily diffused into the draw liquid supply unit 300c. For this reason, in the vicinity of the semipermeable membrane 3a, the difference between the concentration on the anaerobic treated water side and the concentration on the draw liquid side is reduced, thereby preventing the occurrence of osmotic pressure. Thereby, since the penetration | infiltration of the water | moisture content from a to-be-processed water to a draw liquid is performed efficiently, anaerobic treated water can be concentrated efficiently. The draw liquid in the draw liquid supply unit 300c overflows and is discharged from the draw liquid supply unit 300c. Further, in order to efficiently make contact between the draw liquid and the anaerobic treated water through the semipermeable membrane 3a (in other words, contact with the semipermeable membrane 3a), the draw liquid is used by using a stirring device or the like (not shown). The inside of the supply unit 300c may be agitated to adjust the flow rate (the amount of discharge of the draw liquid from the draw liquid supply unit 300c).
なお、本発明に係る水処理方法および水処理装置は、上記実施形態に限定されるものではなく、本発明の要旨を逸脱しない範囲で種々の変更が可能である。また、上記した複数の実施形態の構成や方法等を任意に採用して組み合わせてもよく（１つの実施形態に係る構成や方法等を他の実施形態に係る構成や方法等に適用してもよく）、さらに、下記する各種の変更例に係る構成や方法等を任意に選択して、上記した実施形態に係る構成や方法等に採用してもよいことは勿論である。 The water treatment method and the water treatment apparatus according to the present invention are not limited to the above-described embodiment, and various modifications can be made without departing from the gist of the present invention. Further, the configurations and methods of the plurality of embodiments described above may be arbitrarily adopted and combined (even if the configurations and methods according to one embodiment are applied to the configurations and methods according to other embodiments). Of course, it is of course possible to arbitrarily select configurations, methods, and the like according to various modifications described below and employ them in the configurations, methods, and the like according to the above-described embodiments.
例えば、第一実施形態の濃縮装置３では、嫌気処理水とドロー液との流れる方向が並流となるように構成されているが、これに限定されるものではなく、例えば、逆流となるように構成されてもよい。具体的には、嫌気処理水が嫌気処理水導入部３１ｂ（又は嫌気処理水排出部３２ｂ）から嫌気処理水供給部３ｂに導入されて嫌気処理水排出部３２ｂ（又は嫌気処理水導入部３１ｂ）から排出されると共に、ドロー液がドロー液排出部３２ｃ（又はドロー液導入部３１ｃ）からドロー液供給部３ｃに導入されてドロー液導入部３１ｃ（又はドロー液排出部３２ｃ）から排出されることで、逆流となるように構成しても良い。 For example, in the concentration apparatus 3 of the first embodiment, the flow direction of the anaerobic treated water and the draw liquid is configured to be a parallel flow, but is not limited to this, for example, a reverse flow is performed. May be configured. Specifically, the anaerobic treated water is introduced from the anaerobic treated water introduction unit 31b (or the anaerobic treated water discharge unit 32b) to the anaerobic treated water supply unit 3b, and the anaerobic treated water discharge unit 32b (or the anaerobic treated water introduction unit 31b). And the draw liquid is introduced into the draw liquid supply part 3c from the draw liquid discharge part 32c (or the draw liquid introduction part 31c) and discharged from the draw liquid introduction part 31c (or the draw liquid discharge part 32c). Therefore, it may be configured to have a reverse flow.
また、第二実施形態では、ドロー液がオーバーフローすることでドロー液供給部３００ｃから排出されるように構成されているが、これに限定されるものではなく、ドロー液供給部３００ｃにおいてドロー液排出部３２ｃを備え、該ドロー液排出部３２ｃからドロー液を排出するように構成されてもよい。 In the second embodiment, the draw liquid overflows and is discharged from the draw liquid supply unit 300c. However, the present invention is not limited to this, and the draw liquid supply unit 300c discharges the draw liquid. A part 32c may be provided, and the draw liquid may be discharged from the draw liquid discharge part 32c.
また、上記実施形態の濃縮装置３，３００に代えて、図４に示す構成の濃縮装置３０１を採用してもよい。濃縮装置３０１は、上記実施形態に係る濃縮装置３，３００と比較すると、主に嫌気処理水供給部３０１ｂとドロー液供給部３０１ｃの構成が異なる。従って、以下では、上記実施形態と異なる点を中心に説明し、同一の構成に対しては同一の符号を付すこととして説明を省略する。 Moreover, it may replace with the concentration apparatuses 3 and 300 of the said embodiment, and may employ | adopt the concentration apparatus 301 of the structure shown in FIG. Compared with the concentration apparatuses 3 and 300 which concern on the said embodiment, the concentration apparatus 301 mainly differs in the structure of the anaerobic treated water supply part 301b and the draw liquid supply part 301c. Accordingly, the following description will be focused on differences from the above-described embodiment, and the same components will be denoted by the same reference numerals and description thereof will be omitted.
図４に示すように、濃縮装置３０１は、複数のドロー液供給部３０１ｃが嫌気処理水供給部３０１ｂを貫通するように配置されて構成される。ドロー液供給部３０１ｃは、一方向に伸びる管状の形状を有する。そして、ドロー液供給部３０１ｃは、嫌気処理水供給部３０１ｂの内部空間に位置する領域が半透膜３ａを用いて形成され、内部空間の外側の領域によってドロー液導入部３１ｃおよびドロー液排出部３２ｃが形成される。 As shown in FIG. 4, the concentrator 301 is configured by arranging a plurality of draw liquid supply units 301c so as to penetrate the anaerobic treated water supply unit 301b. The draw liquid supply unit 301c has a tubular shape extending in one direction. The draw liquid supply unit 301c has a region located in the internal space of the anaerobic treated water supply unit 301b formed using the semipermeable membrane 3a, and the draw liquid introduction unit 31c and the draw liquid discharge unit are formed by a region outside the internal space. 32c is formed.
斯かる構成の濃縮装置３０１では、ドロー液供給部３０１ｃの内部空間がドロー液によって満たされると共に、ドロー液供給部３０１ｃにおける半透膜３ａで形成された領域全体が嫌気処理水に浸漬されるように嫌気処理水供給部３０１ｂに嫌気処理水が供給される。これにより、嫌気処理水とドロー液とが半透膜３ａを介して接触した状態となる。 In the concentrator 301 having such a configuration, the interior space of the draw liquid supply unit 301c is filled with the draw liquid, and the entire region formed by the semipermeable membrane 3a in the draw liquid supply unit 301c is immersed in the anaerobic treated water. The anaerobic treated water is supplied to the anaerobic treated water supply unit 301b. As a result, the anaerobic treated water and the draw liquid are brought into contact with each other through the semipermeable membrane 3a.
また、上記実施形態では、ドロー液として、海水を用いているが、被処理水からの水分の浸透によって浸透圧が生じるように構成されたものであれば、特に限定されるものではない。例えば、ドロー液としては、溶質として、無機塩、糖、水可溶低沸点気体、磁性体微粒子、有機溶媒等の何れかを含有するものを用いることができる。更に、ドロー液として、例えば、海水と磁性体微粒子のように、海水と他の溶質を組合せてもよい。これらのドロー液を用いる場合、海水のように使用後に直接環境中へ放出することができないため、使用後のドロー液から溶質を除去することが必要となる。このため、ドロー液の溶質としては、容易に水分から分離可能なものを選択することが好ましい。斯かる場合、ドロー液から分離された溶質は、回収されて再度ドロー液の成分として使用することができる。 Moreover, in the said embodiment, although seawater is used as a draw liquid, if it was comprised so that an osmotic pressure might arise by the penetration | invasion of the water | moisture content from to-be-processed water, it will not specifically limit. For example, as the draw liquid, a liquid containing any one of an inorganic salt, a sugar, a water-soluble low-boiling gas, a magnetic fine particle, an organic solvent and the like as a solute can be used. Furthermore, seawater and other solutes may be combined as the draw liquid, for example, seawater and magnetic fine particles. When these draw liquids are used, it is necessary to remove the solute from the used draw liquid since it cannot be directly released into the environment after use, like seawater. For this reason, it is preferable to select a solute of the draw liquid that can be easily separated from moisture. In such a case, the solute separated from the draw liquid can be recovered and used again as a component of the draw liquid.
また、上記実施形態では、濃縮装置３で濃縮された嫌気処理水は、塩類回収部４へ供給されているが、これに限定されるものではなく、斯かる嫌気処理水の一部又は全部が、再度、濃縮装置３へ供給されるようにしてもよい。又は、濃縮装置３を複数使用したり、濃縮装置３とは異なる濃縮装置を濃縮装置３の前後の少なくとも一方に使用したりすることで、段階的に嫌気処理水を濃縮してもよい。 Moreover, in the said embodiment, although the anaerobic treated water concentrated with the concentration apparatus 3 is supplied to the salt collection | recovery part 4, it is not limited to this, A part or all of such anaerobic treated water is Alternatively, it may be supplied to the concentrating device 3 again. Alternatively, the anaerobic treated water may be concentrated stepwise by using a plurality of concentrating devices 3 or by using a concentrating device different from the concentrating device 3 at least before and after the concentrating device 3.
１…水処理装置、２…嫌気処理部、２ａ…嫌気処理槽、２ｂ…膜分離装置、３，３００，３０１…濃縮装置、３ａ…半透膜、３ｂ，３００ｂ，３０１ｂ…嫌気処理水供給部、３ｃ，３００ｃ，３０１ｃ…ドロー液供給部、４…塩類回収部、３１ｂ…嫌気処理水導入部、３１ｃ…ドロー液導入部、３２ｂ…嫌気処理水排出部、３２ｃ…ドロー液排出部、Ｓ…海洋 DESCRIPTION OF SYMBOLS 1 ... Water treatment apparatus, 2 ... Anaerobic treatment part, 2a ... Anaerobic treatment tank, 2b ... Membrane separation apparatus, 3,300,301 ... Concentration apparatus, 3a ... Semipermeable membrane, 3b, 300b, 301b ... Anaerobic treatment water supply part 3c, 300c, 301c ... Draw liquid supply part, 4 ... Salt recovery part, 31b ... Anaerobic treated water introduction part, 31c ... Draw liquid introduction part, 32b ... Anaerobic treated water discharge part, 32c ... Draw liquid discharge part, S ... Ocean
Claims (2)
前記嫌気処理工程で処理された被処理水から構成される嫌気処理水と該嫌気処理水から半透膜を介して水分の浸透を受けて浸透圧が生じるように構成されたドロー液とを半透膜を介して接触させることで嫌気処理水を濃縮する濃縮工程と、該濃縮工程で濃縮された嫌気処理水から構成される濃縮水から窒素成分又はリン成分の少なくとも一方の塩類を回収すると共に嫌気処理工程後であって濃縮工程前の嫌気処理水へ塩類を回収した後の濃縮水を返送する塩類回収工程とを備え、前記ドロー液は、海水から構成されることを特徴とする水処理方法。 A water treatment method comprising an anaerobic treatment step using a membrane separation activated sludge method for anaerobic treatment of water to be treated containing organic matter and membrane separation of the water to be treated after the anaerobic treatment,
Half of an anaerobic treated water composed of the treated water treated in the anaerobic treatment step and a draw liquid configured to generate osmotic pressure by receiving moisture from the anaerobic treated water through a semipermeable membrane. Recovering at least one salt of the nitrogen component or the phosphorus component from the concentration step comprising concentrating the anaerobic treated water by contacting through a permeable membrane and the anaerobic treated water concentrated in the concentration step and a salt recovery step to return your concentrated water after even after the anaerobic treatment step to recover the concentration step salts Previous anaerobic treated water, the draw solution is characterized Rukoto consists sea water Processing method.
前記嫌気処理部で処理された被処理水で構成される嫌気処理水を濃縮する濃縮装置と、該濃縮装置で濃縮された嫌気処理水から構成される濃縮水から窒素成分又はリン成分の少なくとも一方の塩類を回収すると共に嫌気処理部で処理されて濃縮装置へ供給される前の嫌気処理水へ塩類を回収した後の濃縮水を返送可能に構成された塩類回収部とを更に備え、前記濃縮装置は、半透膜を介して嫌気処理水から水分の浸透を受けて浸透圧が生じるように構成されたドロー液が供給されるドロー液供給部と、嫌気処理水が供給される嫌気処理水供給部とを備えると共に半透膜を介して嫌気処理水とドロー液とが接触するように構成されており、前記ドロー液は、海水から構成されることを特徴とする水処理装置。
A water treatment apparatus including an anaerobic treatment unit using a membrane separation activated sludge method for performing anaerobic treatment of water to be treated containing organic matter and membrane separation of the water to be treated after the anaerobic treatment,
A concentrating device for concentrating anaerobic treated water composed of water to be treated treated in the anaerobic treatment unit, and at least one of a nitrogen component or a phosphorus component from the concentrated water composed of anaerobic treated water concentrated in the concentrating device anda salt recovery section is returned feed configured to be able to concentrate after the recovery of salts Previous anaerobic treatment water are treated in anaerobic processing unit is supplied to the concentrator with the recovery of salts, the The concentrator includes a draw liquid supply unit configured to receive an infiltration pressure from the anaerobic treated water through a semipermeable membrane to generate an osmotic pressure, and an anaerobic process to which anaerobic treated water is supplied. through the semi-permeable membrane provided with a water supply portion is configured to contact and anaerobic treated water and draw liquid, the draw solution, water treatment apparatus according to claim Rukoto constructed from seawater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015117738A JP5860989B2 (en) | 2015-06-10 | 2015-06-10 | Water treatment method and water treatment apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2015117738A JP5860989B2 (en) | 2015-06-10 | 2015-06-10 | Water treatment method and water treatment apparatus |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2014003733A Division JP5764224B2 (en) | 2014-01-10 | 2014-01-10 | Water treatment method and water treatment apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2015157291A JP2015157291A (en) | 2015-09-03 |
| JP5860989B2 true JP5860989B2 (en) | 2016-02-16 |
Family
ID=54181765
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2015117738A Active JP5860989B2 (en) | 2015-06-10 | 2015-06-10 | Water treatment method and water treatment apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP5860989B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109867414A (en) * | 2019-03-20 | 2019-06-11 | 北京科技大学 | Using the integrated apparatus in Dynamic Membrane anaerobism MBR- positive infiltration technology processing mankind Heisui River |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5845796A (en) * | 1981-09-16 | 1983-03-17 | Nishihara Environ Sanit Res Corp | Anaerobic digestion of highly-concentrated organic waste water |
| JP2008086864A (en) * | 2006-09-29 | 2008-04-17 | Ngk Insulators Ltd | Method for recovering phosphorus by using membrane separation activated sludge process |
| JP2010017614A (en) * | 2008-07-08 | 2010-01-28 | Kurita Water Ind Ltd | Method and apparatus for treating organic wastewater |
| CN103635433B (en) * | 2011-06-24 | 2016-08-24 | 太平洋水泥株式会社 | The recovery of phosphorus and Fertilizer Transformed method |
| WO2013110032A1 (en) * | 2012-01-20 | 2013-07-25 | Hydration Systems, Llc | Low energy forward osmosis membrane water processing system |
-
2015
- 2015-06-10 JP JP2015117738A patent/JP5860989B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| JP2015157291A (en) | 2015-09-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5764224B2 (en) | Water treatment method and water treatment apparatus | |
| Zarebska et al. | Ammonium fertilizers production from manure: a critical review | |
| WO2015005186A1 (en) | Water treatment method and water treatment device | |
| AU2009259824B2 (en) | Forward osmosis separation processes | |
| US9822021B2 (en) | Forward osmosis separation processes | |
| WO2012102677A1 (en) | Method and apparatus for recovering water from a source water | |
| CA2945973A1 (en) | Electrodialysis stacks, systems, and methods for recovering ammonia and monovalent salts from anaerobic digestate | |
| EP2586748A1 (en) | Freshwater-generating device, and freshwater-generating method | |
| JP2015013238A (en) | Water treatment system and water treatment method | |
| JP2012192367A (en) | Treatment device for organic waste water containing nitrogen | |
| KR102100991B1 (en) | Liquefied fertilizer purification apparatus using porous ceramic membrane | |
| JP5860989B2 (en) | Water treatment method and water treatment apparatus | |
| JP5526093B2 (en) | Seawater desalination method and seawater desalination apparatus | |
| JP5572740B1 (en) | Power generation facility and power generation method | |
| KR20160121666A (en) | Water treatment apparatus using forward osmosis membrane bioreactor and reverse osmosis process | |
| JP5998254B1 (en) | Digestion processing apparatus and digestion processing method | |
| JPH07155759A (en) | Waste water treating device | |
| JP5269331B2 (en) | Waste water treatment equipment | |
| WO2016136957A1 (en) | Method for treating water containing organic material, and device for treating water containing organic material | |
| KR102156161B1 (en) | Forward osmosis composting method for collecting phosphors and nitrogen in recycle water of waste water treatment equipment | |
| JP5551628B2 (en) | Method and apparatus for treating wastewater containing organic chemicals | |
| JP2017006844A (en) | Digestion treatment device and digestion treatment method | |
| WO2011155282A1 (en) | Fresh water-generating device and fresh water-generating method | |
| JP7421496B2 (en) | Wastewater treatment equipment and wastewater treatment method | |
| JP2017042765A (en) | Water treatment system and water treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20150610 |
|
| A871 | Explanation of circumstances concerning accelerated examination |
Free format text: JAPANESE INTERMEDIATE CODE: A871 Effective date: 20150610 |
|
| A975 | Report on accelerated examination |
Free format text: JAPANESE INTERMEDIATE CODE: A971005 Effective date: 20150625 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20150828 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20151026 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20151204 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20151221 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 5860989 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |