JP6630689B2 - Water treatment equipment and water treatment method - Google Patents
Water treatment equipment and water treatment method Download PDFInfo
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- JP6630689B2 JP6630689B2 JP2017030308A JP2017030308A JP6630689B2 JP 6630689 B2 JP6630689 B2 JP 6630689B2 JP 2017030308 A JP2017030308 A JP 2017030308A JP 2017030308 A JP2017030308 A JP 2017030308A JP 6630689 B2 JP6630689 B2 JP 6630689B2
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- 238000000034 method Methods 0.000 title claims description 19
- 239000012528 membrane Substances 0.000 claims description 182
- 238000000926 separation method Methods 0.000 claims description 124
- 229920001222 biopolymer Polymers 0.000 claims description 81
- 239000000126 substance Substances 0.000 claims description 41
- 239000003112 inhibitor Substances 0.000 claims description 34
- 238000001471 micro-filtration Methods 0.000 claims description 24
- 238000001914 filtration Methods 0.000 claims description 19
- 239000005416 organic matter Substances 0.000 claims description 18
- 238000005259 measurement Methods 0.000 claims description 17
- 244000005700 microbiome Species 0.000 claims description 12
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- 239000000701 coagulant Substances 0.000 description 12
- 238000005374 membrane filtration Methods 0.000 description 10
- 239000011148 porous material Substances 0.000 description 9
- 238000005070 sampling Methods 0.000 description 9
- 239000000243 solution Substances 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 238000012360 testing method Methods 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000007800 oxidant agent Substances 0.000 description 5
- 239000002033 PVDF binder Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 4
- 238000001223 reverse osmosis Methods 0.000 description 4
- 238000000967 suction filtration Methods 0.000 description 4
- 235000013162 Cocos nucifera Nutrition 0.000 description 3
- 244000060011 Cocos nucifera Species 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 239000003480 eluent Substances 0.000 description 3
- 238000004128 high performance liquid chromatography Methods 0.000 description 3
- 239000012510 hollow fiber Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- USHAGKDGDHPEEY-UHFFFAOYSA-L potassium persulfate Chemical compound [K+].[K+].[O-]S(=O)(=O)OOS([O-])(=O)=O USHAGKDGDHPEEY-UHFFFAOYSA-L 0.000 description 3
- 229910021642 ultra pure water Inorganic materials 0.000 description 3
- 239000012498 ultrapure water Substances 0.000 description 3
- 238000012935 Averaging Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
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- 239000002023 wood Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 230000003373 anti-fouling effect Effects 0.000 description 1
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- 125000002091 cationic group Chemical group 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
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- 150000004676 glycans Chemical class 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 238000000691 measurement method Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 229920005615 natural polymer Polymers 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 230000000644 propagated effect Effects 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Landscapes
- Biological Treatment Of Waste Water (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Description
本発明は、有機物を含む被処理水を膜分離する水処理設備および水処理方法に関する。 The present invention relates to a water treatment facility and a water treatment method for membrane-separating water to be treated containing organic matter.
従来、有機物を含む被処理水を膜分離する水処理設備として、前記被処理水を膜分離する膜分離部と、前記膜分離部の上流側に配され、膜分離前の前記被処理水中の有機物を前処理する前処理部と、を備えるものが知られている。該水処理装置の前処理部においては、膜分離部の分離膜における有機物由来の膜閉塞（以下、ファウリングともいう）を抑制するための前処理が行われている。有機物由来のファウリングは、膜分離部の分離膜の孔の内部に、被処理水中の有機物が入り込むことによって孔が目詰まりし、閉塞することにより生じると考えられている。
このような水処理設備としては、例えば、特許文献１および２に記載のものが挙げられる。
Conventionally, as a water treatment facility for membrane-separating water to be treated containing organic matter, a membrane separation unit for membrane-separating the water to be treated, and disposed upstream of the membrane separation unit, in the water to be treated before membrane separation. There is known a device including a pretreatment unit for pretreating an organic substance. In the pretreatment section of the water treatment apparatus, pretreatment for suppressing membrane blocking (hereinafter, also referred to as fouling) due to organic substances in the separation membrane of the membrane separation section is performed. It is considered that the fouling derived from organic matter is caused by the clogging and blocking of the pores by the entry of the organic matter in the water to be treated into the pores of the separation membrane in the membrane separation unit.
Examples of such water treatment facilities include those described in Patent Documents 1 and 2.
特許文献１に記載の水処理設備は、前処理部として、有機物を含む被処理水中のＴＯＣを測定するＴＯＣ測定手段と、該ＴＯＣ測定手段によって測定された被処理水中のＴＯＣに応じて被処理水中の有機物を酸化分解する酸化剤を添加する酸化剤添加手段と、酸化剤添加後の被処理水を通水させたときに、該被処理水中の有機物を酸化分解する酸化処理層とを備え、膜分離部として、有機物が酸化分解された被処理水を膜分離する分離膜を備えている。
特許文献１に記載の水処理設備の前処理部においては、有機物を低分子化し、該有機物を分離膜の孔を透過させることにより、分離膜における有機物由来のファウリングを抑制している。
The water treatment equipment described in Patent Literature 1 has, as a pretreatment section, a TOC measuring means for measuring TOC in the water to be treated containing organic matter, and a treatment target in accordance with the TOC in the water to be treated measured by the TOC measuring means. An oxidizing agent adding means for adding an oxidizing agent for oxidatively decomposing organic substances in water, and an oxidizing layer for oxidatively decomposing organic substances in the water to be treated when the water to be treated is passed after the addition of the oxidizing agent. And a separation membrane for separating the water to be treated, in which organic substances have been oxidatively decomposed, as a membrane separation unit.
In the pretreatment section of the water treatment facility described in Patent Literature 1, the organic matter is reduced in molecular weight and the organic matter is allowed to pass through the pores of the separation membrane, thereby suppressing fouling derived from the organic matter in the separation membrane.
特許文献２に記載の水処理設備は、膜分離部として、逆浸透膜と、該逆浸透膜の濃縮水のＴＯＣを測定するＴＯＣ測定手段とを備え、前処理部として、膜分離部のＴＯＣ測定手段によって測定された濃縮水のＴＯＣが所定値以上になったときに、有機物を含む被処理水に、有機物を栄養源として繁殖した微生物（バクテリア、カビなど）に由来するスライムの形成を抑制するスライム抑制剤（次亜塩素酸など）を供給するスライム抑制剤供給手段とを備えている。
特許文献２に記載の水処理設備の前処理部においては、被処理水にスライム抑制剤を供給し、被処理水中でのスライムの形成を抑制することによって、逆浸透膜における有機物由来のファウリングを抑制している。
The water treatment facility described in Patent Literature 2 includes a reverse osmosis membrane as a membrane separation unit and TOC measuring means for measuring the TOC of the concentrated water of the reverse osmosis membrane, and a TOC of the membrane separation unit as a pretreatment unit. When the TOC of the concentrated water measured by the measuring means becomes equal to or more than a predetermined value, the formation of slime derived from microorganisms (bacteria, mold, etc.) propagated in the water containing organic matter as a nutrient source is suppressed. A slime inhibitor supplying means for supplying a slime inhibitor (such as hypochlorous acid).
In the pretreatment section of the water treatment facility described in Patent Document 2, by supplying a slime inhibitor to the water to be treated and suppressing the formation of slime in the water to be treated, fouling derived from organic matter in the reverse osmosis membrane is suppressed. Has been suppressed.
上記各特許文献に記載の水処理設備のように、有機物を含む被処理水において、該被処理水中のＴＯＣ値を基準として、膜分離部におけるファウリングを抑制すべく、膜分離前の被処理水に酸化剤やスライム抑制剤を添加した場合、ＴＯＣ値が同じであっても、ファウリングが発生することもあれば、ファウリングが発生ないこともあり、ファウリングの発生にはバラツキがあった。
そのため、ＴＯＣ値を基準として、膜分離部におけるファウリングの発生を適切に抑制することは難しかった。
As in the water treatment facilities described in the above-mentioned patent documents, in the water to be treated containing organic substances, the treatment before the membrane separation is performed in order to suppress the fouling in the membrane separation unit based on the TOC value in the water to be treated. When an oxidizing agent or a slime inhibitor is added to water, even if the TOC value is the same, fouling may occur, or fouling may not occur, and the occurrence of fouling varies. Was.
Therefore, it has been difficult to appropriately suppress the occurrence of fouling in the membrane separation unit based on the TOC value.
本発明は上記実情に鑑みてなされたものであり、膜分離部におけるファウリングの発生を適切に抑制しつつ、被処理水を膜分離することができる水処理設備および水処理方法を提供することを課題とする。 The present invention has been made in view of the above circumstances, and provides a water treatment facility and a water treatment method capable of performing membrane separation of water to be treated while appropriately suppressing generation of fouling in a membrane separation unit. As an issue.
一般に、有機物を含む被処理水においては、該有機物の一部としてバイオポリマーが含まれている。
そして、有機物を含む被処理水を膜分離するときにファウリングが生じる原因について、本発明者が鋭意検討したところ、ファウリングを生じさせる主原因物質はバイオポリマーであることが判明した。
Generally, in the water to be treated containing an organic substance, a biopolymer is contained as a part of the organic substance.
The inventor of the present invention has conducted intensive studies on the cause of fouling when the water to be treated containing organic substances is subjected to membrane separation, and it has been found that the main cause of fouling is a biopolymer.
すなわち、本発明に係る水処理設備は、有機物を含む被処理水を膜分離する膜分離部と、前記膜分離部の上流側に配され、前記被処理水中のバイオポリマー濃度を調整する前処理部と、を備え、前記前処理部は、膜分離前の前記被処理水中のバイオポリマー濃度を測定するバイオポリマー濃度測定部と、前記バイオポリマー濃度測定部によって測定された前記バイオポリマー濃度が所定濃度以上になったときに、ファウリングを抑制するようにファウリング抑制物質を膜分離前の前記被処理水に添加するファウリング抑制物質添加部と、を備える。 That is, the water treatment equipment according to the present invention is a membrane separation unit for membrane-separating the water to be treated containing organic matter, and a pretreatment that is disposed upstream of the membrane separation unit and adjusts the concentration of the biopolymer in the water to be treated. And a pretreatment unit, wherein the pretreatment unit is a biopolymer concentration measurement unit that measures a biopolymer concentration in the water to be treated before membrane separation, and the biopolymer concentration measured by the biopolymer concentration measurement unit is a predetermined value. A fouling suppressing substance adding section for adding a fouling suppressing substance to the water to be treated before membrane separation so as to suppress fouling when the concentration becomes equal to or higher than the concentration.
斯かる構成によれば、前処理部のバイオポリマー濃度測定部によって膜分離前の被処理水中のバイオポリマー濃度を測定し、測定されたバイオポリマー濃度が所定濃度以上になったときに、ファウリング抑制物質を膜分離前の前記被処理水に添加することができる。
これにより、膜分離部におけるファウリングの発生を適切に抑制しつつ、被処理水を膜分離することができる。
According to such a configuration, the biopolymer concentration in the water to be treated before membrane separation is measured by the biopolymer concentration measurement unit in the pretreatment unit, and when the measured biopolymer concentration is equal to or higher than the predetermined concentration, fouling is performed. An inhibitor can be added to the water to be treated before membrane separation.
Thus, the water to be treated can be subjected to membrane separation while appropriately suppressing the occurrence of fouling in the membrane separation section.
また、上記水処理設備においては、前記前処理部は、前記バイオポリマー濃度測定部および前記ファウリング抑制物質添加部よりも上流側に、水質浄化作用を有する微生物を生育させた濾材を有し、かつ該濾材を用いて膜分離前の前記被処理水を濾過する生物接触濾過部を備えてもよい。 Further, in the water treatment facility, the pretreatment section, on the upstream side of the biopolymer concentration measurement section and the fouling suppressing substance addition section, a filter medium having grown microorganisms having a water purification action, Further, a biological contact filtration unit for filtering the water to be treated before membrane separation using the filter medium may be provided.
斯かる構成によれば、被処理水中に含まれ、かつ微生物により浄化される成分を、濾材に生育させた水質浄化作用を有する微生物によって浄化しつつ、被処理水における懸濁物質を濾材によって濾過することができる。
これにより、後段の膜分離部における膜分離の負荷を低減することができる。
According to such a configuration, while the components contained in the water to be treated and purified by the microorganisms are purified by the microorganisms having a water purification effect grown on the filter medium, suspended substances in the water to be treated are filtered by the filter medium. can do.
Thereby, the load of membrane separation in the subsequent membrane separation unit can be reduced.
また、上記水処理設備においては、前記膜分離部は、精密濾過膜または限外濾過膜を備え、該精密濾過膜または該限外濾過膜を用いて膜分離してもよい。 In the above-mentioned water treatment equipment, the membrane separation unit may include a microfiltration membrane or an ultrafiltration membrane, and may perform membrane separation using the microfiltration membrane or the ultrafiltration membrane.
斯かる構成によれば、膜分離部におけるファウリングの進行を抑制しつつ、安定した操作圧力で膜濾過を継続して行うことができる。 According to such a configuration, it is possible to continuously perform membrane filtration at a stable operation pressure while suppressing the progress of fouling in the membrane separation unit.
本発明に係る水処理方法は、有機物を含む被処理水を膜分離する膜分離工程と、前記膜分離工程前に、前記被処理水中のバイオポリマー濃度を調整する前処理工程と、を備え、前記前処理工程は、前記被処理水中のバイオポリマー濃度を測定し、測定されたバイオポリマー濃度が所定濃度以上の場合に、前記被処理水にファウリング抑制物質を添加して、前記膜分離工程で膜分離する被処理水とし、測定されたバイオポリマー濃度が所定濃度未満の場合に、前記被処理水にファウリング抑制物質を添加せずに、前記膜分離工程で膜分離する被処理水とする。 The water treatment method according to the present invention includes a membrane separation step of membrane-separating water to be treated containing an organic substance, and before the membrane separation step, a pretreatment step of adjusting a biopolymer concentration in the water to be treated, The pretreatment step is to measure the biopolymer concentration in the water to be treated, and when the measured biopolymer concentration is equal to or higher than a predetermined concentration, adding a fouling inhibitor to the water to be treated, the membrane separation step In the water to be subjected to membrane separation, when the measured biopolymer concentration is less than a predetermined concentration, without adding a fouling inhibitor to the water to be treated, the water to be subjected to membrane separation in the membrane separation step and I do.
斯かる構成によれば、前処理工程において、測定された被処理水中のバイオポリマー濃度が所定濃度以上の場合に、前記被処理水にファウリング抑制物質を添加して、膜分離工程で膜分離する被処理水を得、測定されたバイオポリマー濃度が所定濃度未満の場合に、前記被処理水にファウリング抑制物質を添加せずに、膜分離工程で膜分離する被処理水を得ることができる。
これにより、膜分離部におけるファウリングの発生を適切に抑制しつつ、被処理水を膜分離することができる。
According to such a configuration, in the pretreatment step, when the measured biopolymer concentration in the water to be treated is equal to or higher than a predetermined concentration, a fouling inhibitor is added to the water to be treated, and the membrane is separated in the membrane separation step. When the measured biopolymer concentration is less than a predetermined concentration, without adding a fouling inhibitor to the water to be treated, it is possible to obtain the water to be subjected to membrane separation in the membrane separation step. it can.
Thus, the water to be treated can be subjected to membrane separation while appropriately suppressing the occurrence of fouling in the membrane separation section.
以上のように、本発明によれば、膜分離部におけるファウリングの発生を適切に抑制しつつ、被処理水を膜分離することができる水処理設備および水処理方法を提供することができる。 As described above, according to the present invention, it is possible to provide a water treatment facility and a water treatment method capable of appropriately separating the generation of fouling in the membrane separation section and separating the water to be treated.
以下、本発明の一実施形態に係る水処理設備について、図面を参照しながら説明する。 Hereinafter, a water treatment facility according to an embodiment of the present invention will be described with reference to the drawings.
水処理設備１は、有機物を含む被処理水Ａを膜分離する膜分離部１０と、膜分離部１０の上流側に配され、被処理水Ａ中のバイオポリマー濃度を調整する前処理部２０と、を備える。
被処理水Ａとしては、例えば、湖水（ダム湖水など）、沼水、河川水などが挙げられる。
The water treatment facility 1 includes a membrane separation unit 10 that performs membrane separation of the water A containing organic matter, and a pretreatment unit 20 that is disposed upstream of the membrane separation unit 10 and that adjusts the concentration of the biopolymer in the water A to be treated. And.
The water to be treated A includes, for example, lake water (dam lake water and the like), swamp water, river water and the like.
ここで、バイオポリマーとは、各種被処理水中に存在する有機物の一種であり、一般的には、みかけ分子量が１０万Ｄａ以上の多糖類およびタンパク質とされている。
バイオポリマーの濃度は、有機炭素検出型排除クロマトグラフ法（ＬＣ−ＯＣＤ）で測定することができる。ここで、ＬＣ−ＯＣＤ法とは、試料中のＴＯＣ成分を分子量ごとに分画し、クロマトグラムとして示す分析法であり、クロマトグラム上では、分子量および親水性の大きい有機物ほど保持時間が短くなる傾向がある。
ＬＣ−ＯＣＤ法の測定条件としては、カラムとして２５０ｍｍ×２０ｍｍ ＴＳＫ ＨＷ５０Ｓを用い、流速を１．１ｍＬ／ｍｉｎにし、サンプル注入量を１ｍＬにし、ＵＶ波長を２５４ｎｍにし、ＯＣＤ計への酸注入量を０．２ｍＬ／ｍｉｎにし、溶離液としてｐＨ６．８５ リン酸バッファを用い、酸性化溶液として１Ｌ超純水に対し、４ｍＬ Ｏ−リン酸（８５％）およびペルオキソ二硫酸カリウム０．５ｇを添加した溶液を用いるというものを採用することができる。
ＬＣ−ＯＣＤ法に用いる測定装置としては、例えば、高速液体クロマトグラフィー（ＨＰＬＣ）に湿式全有機炭素計測器（ＯＣＤ計）を接続したＬＣ−ＯＣＤ装置（ＤＯＣ−Ｌａｂａｒ製）を用いることができる。
Here, the biopolymer is a kind of organic substance existing in various kinds of water to be treated, and is generally regarded as a polysaccharide or protein having an apparent molecular weight of 100,000 Da or more.
The concentration of the biopolymer can be measured by exclusion chromatography with organic carbon detection (LC-OCD). Here, the LC-OCD method is an analytical method in which a TOC component in a sample is fractionated for each molecular weight and is shown as a chromatogram. On the chromatogram, the retention time of an organic substance having a higher molecular weight and hydrophilicity is shorter. Tend.
As measurement conditions of the LC-OCD method, 250 mm × 20 mm TSK HW50S was used as a column, the flow rate was set to 1.1 mL / min, the sample injection amount was set to 1 mL, the UV wavelength was set to 254 nm, and the acid injection amount to the OCD meter was measured. 0.2 mL / min, pH 6.85 phosphate buffer was used as an eluent, and 4 mL O-phosphoric acid (85%) and 0.5 g of potassium peroxodisulfate were added to 1 L ultrapure water as an acidifying solution. A solution using a solution can be employed.
As a measuring device used for the LC-OCD method, for example, an LC-OCD device (manufactured by DOC-Labar) in which a wet total organic carbon measuring device (OCD meter) is connected to high performance liquid chromatography (HPLC) can be used.
膜分離部１０は、精密濾過膜（ＭＦ膜）を含む膜分離ユニットを有し、前処理部２０で前処理された有機物等を含む被処理水Ａの有機物を膜分離ユニットで膜分離するように構成されている。
また、膜分離部１０は、膜分離ユニットでの膜分離によって、精密濾過膜を透過して有機物が低減された透過水Ｚと、精密濾過膜を透過せずに有機物等が濃縮された濃縮水Ｘとを得るように構成されている。
The membrane separation unit 10 has a membrane separation unit including a microfiltration membrane (MF membrane), and performs membrane separation of the organic matter of the water A to be treated including the organic matter pretreated in the pretreatment unit 20 by the membrane separation unit. Is configured.
Further, the membrane separation unit 10 includes a permeated water Z in which organic substances are reduced by permeating through the microfiltration membrane and a concentrated water in which organic substances and the like are condensed without permeating through the microfiltration membrane by the membrane separation in the membrane separation unit. X is obtained.
詳しくは、膜分離部１０は、図２に示すように、複数の膜分離ユニット１１を有する。膜分離部１０においては、複数の膜分離ユニット１１が並列的に被処理水Ａを膜分離するように、膜分離ユニット１１がそれぞれ配されている。すなわち、膜分離部１０は、被処理水Ａを並列的に膜分離する複数の膜分離ユニット１１を有する。
膜分離部１０は、図２に示すように、被処理水Ａの膜分離によって、膜分離ユニット１１のそれぞれで精密濾過膜を透過して有機物が低減された透過水Ｚと、膜分離ユニット１１のそれぞれで精密濾過膜を透過せず有機物等が濃縮された濃縮水Ｘとを得るように構成されている。
すなわち、膜分離部１０は、膜分離によって生じた透過水Ｚと濃縮水Ｘとがそれぞれ取り出されるように構成されている。
Specifically, the membrane separation unit 10 has a plurality of membrane separation units 11, as shown in FIG. In the membrane separation unit 10, the membrane separation units 11 are arranged such that the plurality of membrane separation units 11 perform membrane separation of the water to be treated A in parallel. That is, the membrane separation unit 10 includes a plurality of membrane separation units 11 that perform the membrane separation of the water to be treated A in parallel.
As shown in FIG. 2, as shown in FIG. 2, the membrane separation unit 10 separates the permeated water Z in which the organic substances are reduced through the microfiltration membrane in each of the membrane separation units 11 by membrane separation of the water A to be treated, and the membrane separation unit 11. And a concentrated water X in which organic substances and the like are concentrated without passing through the microfiltration membrane.
That is, the membrane separation unit 10 is configured to take out the permeated water Z and the concentrated water X generated by the membrane separation, respectively.
精密濾過膜の材質としては、例えば、ポリフッ化ビニリデン（ＰＶＤＦ）、酢酸セルロース、芳香族アミドなどのポリアミド、ポリビニルアルコール、ポリスルホンなどを挙げることができる。 Examples of the material of the microfiltration membrane include polyvinylidene fluoride (PVDF), cellulose acetate, polyamide such as aromatic amide, polyvinyl alcohol, and polysulfone.
精密濾過膜の形状としては、従来公知のものが挙げられ、例えば、直径数ｍｍの中空糸状に形成されたいわゆる中空糸膜状、スパイラル状、または板状の平膜状などが挙げられる。 Examples of the shape of the microfiltration membrane include conventionally known ones, for example, a so-called hollow fiber membrane formed into a hollow fiber having a diameter of several mm, a spiral shape, or a plate-shaped flat membrane.
膜分離ユニット１１は、精密濾過膜を含み、該精密濾過膜によって有機物を含む被処理水Ａを膜分離し、精密濾過膜を透過して有機物が低減された透過水Ｚと、精密濾過膜を透過せず有機物等が濃縮された濃縮水Ｘとを得るように構成されている。
膜分離ユニット１１としては、例えば、市販されている一般的なものを用いることができる。
膜分離部１０の上流側には、被処理水Ａを加圧するための加圧ポンプが配されていてもよい。
また、膜分離ユニット１１として浸漬型のものを使用する場合、吸引することにより濾過を行うので、膜分離部１０の下流側（すなわち、分離膜の透過側）に吸引ポンプが配されていてもよい。
The membrane separation unit 11 includes a microfiltration membrane. The microfiltration membrane separates the water to be treated A containing an organic substance, and the permeated water Z in which the organic substance is reduced by passing through the microfiltration membrane, and the microfiltration membrane. It is configured to obtain concentrated water X in which organic substances and the like are not permeated and concentrated.
As the membrane separation unit 11, for example, a commercially available general unit can be used.
A pressurizing pump for pressurizing the water to be treated A may be arranged on the upstream side of the membrane separation unit 10.
In addition, when a immersion type is used as the membrane separation unit 11, since filtration is performed by suction, even if a suction pump is provided on the downstream side of the membrane separation unit 10 (that is, on the permeation side of the separation membrane). Good.
本実施形態においては、膜分離ユニット１１に分離膜として精密濾過膜が含まれる例について説明したが、膜分離ユニット１１に含まれる分離膜はこれに限られない。膜分離ユニット１１に含まれる分離膜は、例えば、逆浸透膜（ＲＯ膜）、限外濾過膜などであってもよい。 In the present embodiment, an example has been described in which the membrane separation unit 11 includes a microfiltration membrane as a separation membrane, but the separation membrane included in the membrane separation unit 11 is not limited thereto. The separation membrane included in the membrane separation unit 11 may be, for example, a reverse osmosis membrane (RO membrane), an ultrafiltration membrane, or the like.
本実施形態の前処理部２０は、膜分離前の被処理水Ａ中のバイオポリマー濃度を測定するバイオポリマー濃度測定部２１と、バイオポリマー濃度測定部２１によって測定されたバイオポリマー濃度が所定濃度以上になったときに、ファウリングの発生を抑制するようにファウリング抑制物質を膜分離前の被処理水Ａに添加するファウリング抑制物質添加部２２とを備える。 The pretreatment unit 20 of the present embodiment includes a biopolymer concentration measurement unit 21 for measuring the biopolymer concentration in the water A to be treated before membrane separation, and a biopolymer concentration measured by the biopolymer concentration measurement unit 21 having a predetermined concentration. A fouling suppressing substance adding section 22 for adding a fouling suppressing substance to the water to be treated A before membrane separation so as to suppress the occurrence of fouling when the above is provided.
また、前処理部２０は、バイオポリマー濃度測定部２１およびファウリング抑制物質添加部２２の上流側に、水質浄化作用を有する微生物を生育させた濾材を有し、かつ該濾材を用いて膜分離前の被処理水Ａを濾過する生物接触濾過部２３を備える。 Further, the pretreatment unit 20 has a filter medium on which microorganisms having a water purification function are grown on the upstream side of the biopolymer concentration measurement unit 21 and the fouling suppressing substance addition unit 22, and performs membrane separation using the filter medium. A biological contact filtration unit 23 for filtering the water to be treated A is provided.
さらに、前処理部２０は、バイオポリマー濃度測定部２１およびファウリング抑制物質添加部２２の下流側に、ファウリング抑制物質と被処理水Ａとを混合するための混合部２４を備える。 Further, the pretreatment unit 20 includes a mixing unit 24 for mixing the fouling inhibitor and the water to be treated A downstream of the biopolymer concentration measuring unit 21 and the fouling inhibitor adding unit 22.
バイオポリマー濃度測定部２１は、膜分離前の被処理水Ａ中のバイオポリマー濃度を測定するように構成され、生物接触濾過後の被処理水Ａをサンプリングするためのサンプリング槽２１ａと、サンプリング槽２１ａ内の被処理水Ａをサンプリングするサンプラー２１ｂと、サンプラー２１ｂによってサンプリングされた被処理水Ａ中のバイオポリマー濃度を測定するための濃度測定装置２１ｃとを備える。 The biopolymer concentration measuring unit 21 is configured to measure the concentration of the biopolymer in the water A to be treated before membrane separation, and a sampling tank 21a for sampling the water A after the biological contact filtration; The apparatus includes a sampler 21b for sampling the water A to be treated in the water 21a, and a concentration measuring device 21c for measuring the concentration of the biopolymer in the water A to be treated sampled by the sampler 21b.
サンプリング槽２１ａは、生物接触濾過部２３において濾過された被処理水Ａを内部空間に収容するように構成されている。また、サンプリング槽２１ａは、内部空間に収容された被処理水Ａを撹拌するように構成されている。 The sampling tank 21a is configured to store the water to be treated A filtered in the biological contact filtration unit 23 in an internal space. The sampling tank 21a is configured to stir the water A to be treated accommodated in the internal space.
サンプラー２１ｂは、サンプリング槽２１ａ内の被処理水Ａをサンプリングできるように構成されている。サンプラー２１ｂとしては、ポータブル自動採水器、ベイラーサンプラーなどを用いることができる。 The sampler 21b is configured to sample the water A to be treated in the sampling tank 21a. As the sampler 21b, a portable automatic water dispenser, a Baylor sampler, or the like can be used.
濃度測定装置２１ｃは、被処理水Ａ中のバイオポリマー濃度を測定できるように構成され、例えば、ＬＣ−ＯＣＤ法や三次元蛍光測定法などの公知のバイオポリマー濃度およびバイオポリマーに類するものの濃度の測定方法で、被処理水Ａ中のバイオポリマー濃度を測定できるように構成されている。 The concentration measuring device 21c is configured to measure the concentration of the biopolymer in the water A to be treated. For example, the concentration of a known biopolymer such as the LC-OCD method or the three-dimensional fluorescence measurement method and the concentration of a similar biopolymer can be measured. It is configured to be able to measure the concentration of the biopolymer in the water A to be treated by the measuring method.
ファウリング抑制物質添加部２２は、バイオポリマー濃度測定部２１で測定された被処理水Ａ中のバイオポリマー濃度が所定濃度以上になったときに、ファウリング抑制物質を添加するように構成されている。前記所定濃度は、任意の値に設定することができる。好ましくは１２μｇ／Ｌ以上の値に設定することができ、より好ましくは９μｇ／Ｌ以上の値に設定することができる。
なお、上記バイオポリマー濃度の値は、ＬＣ−ＯＣＤ法により測定される値である。ＬＣ−ＯＣＤ法の測定条件としては、カラムとして２５０ｍｍ×２０ｍｍ ＴＳＫ ＨＷ５０Ｓを用い、流速を１．１ｍＬ／ｍｉｎにし、サンプル注入量を１ｍＬにし、ＵＶ波長を２５４ｎｍにし、ＯＣＤ計への酸注入量を０．２ｍＬ／ｍｉｎにし、溶離液としてｐＨ６．８５ リン酸バッファを用い、酸性化溶液として１Ｌ超純水に対し、４ｍＬ Ｏ−リン酸（８５％）およびペルオキソ二硫酸カリウム０．５ｇを添加した溶液を用いるというものを採用することができる。
ＬＣ−ＯＣＤ法に用いる測定装置としては、例えば、高速液体クロマトグラフィー（ＨＰＬＣ）に湿式全有機炭素計測器（ＯＣＤ計）を接続したＬＣ−ＯＣＤ装置（ＤＯＣ−Ｌａｂａｒ製）を用いることができる。
The fouling suppressing substance adding unit 22 is configured to add the fouling suppressing substance when the biopolymer concentration in the water A to be treated measured by the biopolymer concentration measuring unit 21 becomes equal to or higher than a predetermined concentration. I have. The predetermined density can be set to an arbitrary value. Preferably, it can be set to a value of 12 μg / L or more, and more preferably, it can be set to a value of 9 μg / L or more.
The value of the biopolymer concentration is a value measured by the LC-OCD method. As measurement conditions of the LC-OCD method, 250 mm × 20 mm TSK HW50S was used as a column, the flow rate was set to 1.1 mL / min, the sample injection amount was set to 1 mL, the UV wavelength was set to 254 nm, and the acid injection amount to the OCD meter was measured. 0.2 mL / min, pH 6.85 phosphate buffer was used as an eluent, and 4 mL O-phosphoric acid (85%) and 0.5 g of potassium peroxodisulfate were added to 1 L ultrapure water as an acidification solution. A solution using a solution can be employed.
As a measuring device used for the LC-OCD method, for example, an LC-OCD device (manufactured by DOC-Labar) in which a wet total organic carbon measuring device (OCD meter) is connected to high performance liquid chromatography (HPLC) can be used.
ファウリング抑制物質としては、凝集剤、粉末活性炭、酸化剤などの各種公知のものを用いることができる。好ましくは、凝集剤、粉末活性炭を用いることができる。より好ましくは、バイオポリマーを捕捉する凝集剤を用いることができる。
凝集剤としては、無機系凝集剤および有機系凝集剤のいずれも用いることができる。
無機系凝集剤としては、鉄系、アルミ系のものを用いることができる。鉄系の凝集剤としては、ポリ鉄、塩化第二鉄などが挙げられる。アルミ系の凝集剤としては、硫酸バンド（硫酸アルミニウム）、ＰＡＣ（ポリ塩化アルミニウム）などが挙げられる。
有機系凝集剤としては、高分子凝集剤などを用いることができる。高分子凝集剤としては、天然高分子系および合成高分子系のいずれも用いることができる。また、高分子凝集剤として、カチオン性、アニオン性、ノニオン性、両性のいずれのものも用いることができる。
上記のような凝集剤の中でも、アルミ系の無機凝集剤を用いることが好ましい。
また、粉末活性炭としては、ヤシ殻、木材（木質）等の植物系のものを原料とするもの、石炭、石油（ピッチ）等の鉱物系のものを原料とするものなどを用いることができる。これらの中でも、ヤシ殻を原料とするヤシ殻炭を用いることが好ましい。
As the fouling inhibitor, various known substances such as a flocculant, powdered activated carbon, and an oxidizing agent can be used. Preferably, a flocculant and powdered activated carbon can be used. More preferably, a flocculant that captures the biopolymer can be used.
As the coagulant, any of an inorganic coagulant and an organic coagulant can be used.
As the inorganic coagulant, iron-based or aluminum-based ones can be used. Examples of iron-based coagulants include polyiron, ferric chloride and the like. Examples of the aluminum-based coagulant include a sulfuric acid band (aluminum sulfate) and PAC (polyaluminum chloride).
As the organic coagulant, a polymer coagulant or the like can be used. As the polymer flocculant, either a natural polymer or a synthetic polymer can be used. Further, any of cationic, anionic, nonionic and amphoteric polymers can be used as the polymer flocculant.
Among the above coagulants, it is preferable to use an aluminum-based inorganic coagulant.
As the powdered activated carbon, those made from plant-based materials such as coconut shell and wood (wood), and those made from mineral-based materials such as coal and petroleum (pitch) can be used. Among them, it is preferable to use coconut shell charcoal made from coconut shell.
ファウリング抑制物質として凝集剤を用いた場合、該凝集剤によってバイオポリマーを膜分離ユニット１１に含まれる精密濾過膜の孔よりも大きなフロックにすることにより、バイオポリマーが精密濾過膜の孔の内部に入り込んで孔を目詰まりさせることを抑制し、精密濾過膜におけるファウリングの発生を抑制することができる。
また、ファウリング抑制物質として粉末活性炭を用いた場合、該粉末活性炭が有する細孔内にバイオポリマーを吸着させて、被処理水Ａ中のバイオポリマー濃度を低下させることにより、精密濾過膜におけるファウリングの発生を抑制することができる。
When a flocculant is used as the fouling inhibitor, the flocculant causes the biopolymer to form flocs larger than the pores of the microfiltration membrane included in the membrane separation unit 11, so that the biopolymer is filled inside the pores of the microfiltration membrane. It is possible to suppress clogging of the holes by entering into the holes, thereby suppressing the occurrence of fouling in the microfiltration membrane.
In addition, when powdered activated carbon is used as a fouling inhibitor, the biopolymer is adsorbed in the pores of the powdered activated carbon to reduce the biopolymer concentration in the water A to be treated, whereby the fouling in the microfiltration membrane is reduced. The generation of a ring can be suppressed.
また、ファウリング抑制物質添加部２２は、図示しない制御部を備えている。該制御部は、被処理水Ａへのファウリング抑制物質の添加の要否を判定するとともに、ファウリング抑制物質の添加が必要な場合には、被処理水Ａ中のバイオポリマー濃度に応じて被処理水Ａへのファウリング抑制物質の添加量を制御している。そのため、必要量以上のファウリング抑制物質を添加することなく、ファウリングの発生を抑制することができる。これにより、膜分離部１０におけるファウリングの発生を適切に抑制することができる。
ファウリング抑制物質の添加量は、ファウリング抑制物質添加後の被処理水Ａ中のバイオポリマー濃度を９μｇ／Ｌ未満とする量であってもよい。
ファウリング抑制物質の添加量は、被処理水Ａに添加するファウリング抑制物質の種類によって異なるが、例えば、ファウリング抑制物質として粉末活性炭を用いた場合、被処理水Ａ中のバイオポリマー濃度が９μｇ／Ｌより大きく１００μｇ／Ｌ以下の場合には、被処理水Ａに対する粉末活性炭の添加量が５ｍｇ／Ｌ以上３０ｍｇ／Ｌ以下となるように添加することが好ましい。
また、ファウリング抑制物質として凝集剤（ＰＡＣ）を用いた場合、被処理水Ａ中のバイオポリマー濃度が９μｇ／Ｌより大きく１００μｇ／Ｌ以下の場合には、被処理水Ａに対する凝集剤（ＰＡＣ）の添加量が３ｍｇ／Ｌ以上となるように添加することが好ましく、５ｍｇ／Ｌ以上となるように添加することがより好ましい。
Further, the fouling suppressing substance adding section 22 includes a control section (not shown). The control unit determines whether or not it is necessary to add the fouling inhibitor to the water to be treated A, and if the addition of the fouling inhibitor is necessary, according to the biopolymer concentration in the water to be treated A. The amount of the fouling inhibitor added to the water to be treated A is controlled. Therefore, generation of fouling can be suppressed without adding a necessary amount of a fouling inhibitor. Thereby, occurrence of fouling in the membrane separation unit 10 can be appropriately suppressed.
The amount of the fouling inhibitor added may be an amount that makes the biopolymer concentration in the water A to be treated after the addition of the fouling inhibitor less than 9 μg / L.
The amount of the fouling inhibitor added depends on the type of the fouling inhibitor added to the water A to be treated. For example, when powdered activated carbon is used as the fouling inhibitor, the biopolymer concentration in the water A to be treated is reduced. When the amount is more than 9 μg / L and 100 μg / L or less, it is preferable that the amount of the activated carbon powder added to the water to be treated A be 5 mg / L or more and 30 mg / L or less.
When a coagulant (PAC) is used as a fouling inhibitor, and when the biopolymer concentration in the water A to be treated is more than 9 μg / L and 100 μg / L or less, the coagulant (PAC) for the water A to be treated is used. ) Is preferably added so as to be 3 mg / L or more, and more preferably 5 mg / L or more.
生物接触濾過部２３は、水質浄化作用を有する微生物を生育させた濾材を有し、かつ該濾材を用いて膜分離前の被処理水Ａを濾過するように構成されている。前記濾材は、水質浄化作用を有する微生物を粉末活性炭などの表面に生育させたものであってもよい。
生物接触濾過部２３は、濾材表面の微生物による浄化作用により、被処理水Ａに含まれる、バイオポリマーを含む有機物のみならず、鉄、マンガン、アンモニア態窒素などを浄化するとともに、被処理水Ａに含まれる懸濁物質を濾材によって除去する。
生物接触濾過部２３は、上向流式および下向流式のいずれのものでも用いることができる。
The biological contact filtration unit 23 has a filter medium on which microorganisms having a water purification function are grown, and is configured to filter the water to be treated A before membrane separation using the filter medium. The filter medium may be obtained by growing microorganisms having a water purification action on the surface of powdered activated carbon or the like.
The biological contact filtration unit 23 purifies not only the organic matter including the biopolymer, but also iron, manganese, ammonia nitrogen, etc., contained in the water A to be treated by the purifying action of the microorganisms on the surface of the filter medium. Is removed by a filter medium.
The biological contact filtration unit 23 may be of either an upward flow type or a downward flow type.
ところで、生物接触濾過部２３においては、濾材表面に生育された微生物は、冬季などの水温が比較的低い時期には活性が低下して、被処理水Ａ中に含まれる有機物を分解する有機物分解能が低下するようになる。
その結果、冬季などの水温が比較的低い時期においては、生物接触濾過部２３によって被処理水Ａ中のバイオポリマーが浄化され難くなるため、水温が比較的高い時期に比べて、生物接触濾過後の被処理水Ａ中のバイオポリマー濃度が大きく上昇する傾向が認められる。
これにより、膜処理前の被処理水Ａ中のバイオポリマー濃度を測定し、測定されたバイオポリマー濃度が所定濃度以上となった場合に、被処理水Ａにファウリング抑制物質を添加しなければ、膜分離部１０の分離膜の孔が目詰まりし易くなる。
本実施形態に係る水処理設備１は、上述のように、前処理部２０で被処理水Ａ中のバイオポリマー濃度を測定し、測定されたバイオポリマー濃度が所定濃度以上となったときに、被処理水Ａにファウリング抑制物質を添加するため、被処理水Ａ中のバイオポリマー濃度が大きく上昇する冬季などの水温が比較的低い時期において、膜分離部１０の分離膜の孔の目詰まりを抑制するのに、特に有用である。
By the way, in the biological contact filtration part 23, the activity of the microorganisms grown on the surface of the filter medium decreases when the water temperature is relatively low such as in winter, and the microorganisms decompose the organic matter contained in the water A to be treated. Will decrease.
As a result, at a time when the water temperature is relatively low such as in winter, the biopolymer in the water to be treated A becomes difficult to be purified by the biological contact filtration unit 23. The tendency that the biopolymer density | concentration in the to-be-processed water A of this greatly increases is recognized.
Thereby, the biopolymer concentration in the water A to be treated before the membrane treatment is measured, and when the measured biopolymer concentration becomes a predetermined concentration or more, the fouling inhibitor must be added to the water A to be treated. In addition, the pores of the separation membrane of the membrane separation unit 10 are easily clogged.
As described above, the water treatment facility 1 according to the present embodiment measures the biopolymer concentration in the water A to be treated in the pretreatment unit 20 and, when the measured biopolymer concentration becomes equal to or higher than a predetermined concentration, Since the fouling inhibitor is added to the water A to be treated, the pores of the separation membrane of the membrane separation unit 10 are clogged at a relatively low water temperature, such as winter, when the concentration of the biopolymer in the water A to be treated increases significantly. It is particularly useful for suppressing
混合部２４は、ファウリング抑制物質と被処理水Ａとを混合できるように構成されている。混合部２４としては、撹拌機付き凝集混和タンク、ラインミキサなどを用いることができる。 The mixing section 24 is configured to mix the fouling suppressing substance and the water to be treated A. As the mixing unit 24, a coagulation mixing tank with a stirrer, a line mixer, or the like can be used.
次に、本発明の一実施形態に係る水処理方法について説明する。 Next, a water treatment method according to an embodiment of the present invention will be described.
本実施形態に係る水処理方法は、図３に示すように、有機物を含む被処理水を膜分離する膜分離工程（Ｓ２）と、前記膜分離工程（Ｓ２）前に、前記被処理水中のバイオポリマー濃度を調整する前処理工程（Ｓ１）と、を備える。 As shown in FIG. 3, the water treatment method according to the present embodiment includes a membrane separation step (S2) for membrane-separating water to be treated containing an organic substance, and before the membrane separation step (S2), A pretreatment step (S1) of adjusting the biopolymer concentration.
本実施形態の水処理方法においては、例えば、上述の水処理設備１を用いて、前処理部２０にて、前記前処理工程（Ｓ１）を行い、膜分離部１０にて、前記膜分離工程（Ｓ２）を行うことができる。 In the water treatment method of the present embodiment, for example, the pretreatment step (S1) is performed in the pretreatment section 20 using the above-described water treatment equipment 1, and the membrane separation step is performed in the membrane separation section 10. (S2) can be performed.
（前処理工程：Ｓ１）
本工程では、まず、バイオポリマー濃度測定部２１にて、膜分離前の被処理水Ａ中のバイオポリマー濃度を測定する。次に、ファウリング抑制物質添加部２２の制御部にて、測定された被処理水Ａ中のバイオポリマー濃度が所定濃度以上であるか否かを判定する。測定されたバイオポリマー濃度が所定濃度以上の場合、被処理水Ａにファウリング抑制物質添加部２２からファウリング抑制物質を添加して、膜分離工程（Ｓ２）にて膜分離する被処理水Ａとする。測定されたバイオポリマー濃度が所定濃度未満の場合、被処理水Ａにファウリング抑制物質を添加せずに、膜分離工程（Ｓ２）にて膜分離する被処理水Ａとする。
先述のように、ファウリング抑制物質の添加量は、ファウリング抑制物質添加部２２の制御部によって制御されているため、本工程においては、被処理水Ａ中のバイオポリマー濃度に応じて必要量のファウリング抑制物質を添加することができる。
(Pretreatment step: S1)
In this step, first, the biopolymer concentration in the water A to be treated before membrane separation is measured by the biopolymer concentration measuring unit 21. Next, the control unit of the fouling suppression substance adding unit 22 determines whether or not the measured biopolymer concentration in the water A to be treated is equal to or higher than a predetermined concentration. If the measured biopolymer concentration is equal to or higher than the predetermined concentration, the water A to be treated is added to the water A to be treated from the fouling suppression substance addition section 22 and subjected to membrane separation in the membrane separation step (S2). And When the measured biopolymer concentration is less than the predetermined concentration, the water to be treated A is subjected to membrane separation in the membrane separation step (S2) without adding a fouling inhibitor to the water to be treated A.
As described above, since the amount of the fouling inhibitor added is controlled by the control unit of the fouling inhibitor adding unit 22, in this step, the required amount depends on the biopolymer concentration in the water A to be treated. Can be added.
（膜分離工程：Ｓ２）
本工程では、前処理工程にて得られた被処理水Ａに含まれる有機物を膜分離部１０にて膜分離する。この膜分離により、精密濾過膜を透過して有機物が低減された透過水と、精密濾過膜を透過せずに有機物等が濃縮された濃縮水とが得られる。
(Membrane separation step: S2)
In this step, organic substances contained in the water to be treated A obtained in the pretreatment step are subjected to membrane separation in the membrane separation section 10. By this membrane separation, permeated water in which organic substances are reduced by passing through the microfiltration membrane, and concentrated water in which organic substances and the like are concentrated without passing through the microfiltration membrane are obtained.
本発明は、本発明の広義の精神と範囲を逸脱することなく、様々な実施形態および変形が可能とされたものである。また、上述の実施形態は、本発明を説明するためのものであり、本発明の範囲を限定するものではない。つまり、本発明の範囲は、実施形態および実施例ではなく、特許請求の範囲によって示される。そして、特許請求の範囲内およびそれと同等の発明の意義の範囲内で施される様々な変形が、本発明の範囲内とみなされる。 The present invention is capable of various embodiments and modifications without departing from the broad spirit and scope of the invention. Further, the above-described embodiments are for explaining the present invention, and do not limit the scope of the present invention. That is, the scope of the present invention is defined by the appended claims rather than the embodiments and examples. Various modifications made within the scope of the claims and the scope of the invention equivalent thereto are considered to be within the scope of the present invention.
以下では、バイオポリマー濃度の異なる被処理水を用いて、精密濾過膜の膜濾過抵抗の上昇速度を測定した試験例について説明する。 Hereinafter, a test example in which the increasing speed of the membrane filtration resistance of the microfiltration membrane is measured using the water to be treated having different biopolymer concentrations will be described.
＜試験例１＞
（被処理水）
某浄水場の水を、サンプリング場所またはサンプリング時期を変えて取水した。取水は計６回行った。
<Test Example 1>
(Water to be treated)
Water from a water purification plant was taken at a different sampling location or sampling time. Water was taken six times in total.
（バイオポリマー濃度の測定）
バイオポリマー濃度は、高速液体クロマトグラフィー（ＨＰＬＣ）に湿式全有機炭素計測器（ＯＣＤ計）を接続したＬＣ−ＯＣＤ（ＤＯＣ−Ｌａｂｏｒ製）により測定した。
この測定は、Ｓｔｅｆａｎ Ａ．Ｈｕｂｅｒ ｅｔ ａｌ．“Ｃｈａｒａｃｔｅｒｉｓａｔｉｏｎ ｏｆ ａｑｕａｔｉｃ ｈｕｍｉｃ ａｎｄ ｎｏｎ−ｈｕｍｉｃ ｍａｔｔｅｒ ｗｉｔｈ ｓｉｚｅ−ｅｘｃｌｕｓｉｏｎ ｃｈｒｏｍａｔｏｇｒａｐｈｙ−ｏｒｇａｎｉｃ ｃａｒｂｏｎ ｄｅｔｅｃｔｉｏｎ−ｏｒｇａｎｉｃ ｎｉｔｒｏｇｅｎ ｄｅｔｅｃｔｉｏｎ（ＬＣ−ＯＣＤ−ＯＮＤ）”Ｗａｔｅｒ Ｒｅｓｅａｒｃｈ ４５（２０１１）ｐｐ８７９−８８５に記載された方法に準じ、以下の条件下で行った。
・流速：１．１ｍＬ／ｍｉｎ
・サンプル注入量：１ｍＬ
・カラム：２５０ｍｍ×２０ｍｍ ＴＳＫ ＨＷ５０Ｓ
・ＵＶ波長：２５４ｎｍ
・ＯＣＤ計：酸注入量 ０．２ｍＬ／ｍｉｎ
・溶離液：ｐＨ６．８５ リン酸バッファ
・酸性化溶液：１Ｌ超純水に対し、４ｍＬ Ｏ−リン酸（８５％）およびペルオキソ二硫酸カリウム０．５ｇを添加
(Measurement of biopolymer concentration)
The biopolymer concentration was measured by LC-OCD (manufactured by DOC-Labor) in which a high-performance liquid chromatography (HPLC) was connected to a wet total organic carbon meter (OCD meter).
This measurement was performed according to Stefan A. Huber et al. The method is described in "Characterization of aquatic humic and non-humic material with size-exclusion chromatography-organic carbon detection-reaction-organic nitrogen-detection-on-reaction-description-on-description-on-description-on-department-on-description-79 It was performed under the conditions.
・ Flow rate: 1.1 mL / min
・ Sample injection volume: 1mL
・ Column: 250mm × 20mm TSK HW50S
・ UV wavelength: 254 nm
・ OCD meter: Acid injection rate 0.2mL / min
-Eluent: pH 6.85 phosphate buffer-Acidification solution: Add 4 mL O-phosphoric acid (85%) and 0.5 g potassium peroxodisulfate to 1 L ultrapure water
（膜濾過抵抗の上昇速度の測定）
膜濾過抵抗Ｒ（ｍ−１）は、以下の式（１）により算出した。
Ｒ＝ΔＰ／（μ×Ｊ）・・（１）
ここで、ΔＰは膜間差圧（Ｐａ）であり、μは透過水の粘度（Ｐａ・ｓ）であり、Ｊは単位濾過面積当たりの流量（ｍ３／（ｍ２×ｓ））である。
単位濾過面積当たりの流量Ｊおよび膜間差圧ΔＰは、浸漬型の膜モジュールを用いて吸引濾過試験により求めた。前記膜モジュールは、ポリフッ化ビニリデン（ｐｏｌｙｖｉｎｙｌｉｄｅｎｅ ｆｌｕｏｒｉｄｅ（ＰＶＤＦ））製の中空糸ＭＦ膜（旭化成ケミカルズ製）８本を有効膜面積が０．００５ｍ２となるようにモジュール化することにより構成した。なお、使用した膜の膜孔径は０．０８μｍであった。
前記吸引濾過試験において、被処理水の濾過速度は、ペリスタリックポンプ（Ｌ／Ｓシリーズ、ヤマト科学株式会社製）を用いて、初期透過フラックスが１．５ｍ／ｄ（６２．５Ｌ／ｍ２／ｈ（ＬＭＨ））となるように調整した。また、前記吸引濾過試験においては、前記膜モジュールの透過水を用いて、３０分ごとに１分間、前記膜モジュールを逆流洗浄（逆洗）した。該逆洗は、ペリスタリックポンプ（ＭＰ型、ＥＹＥＬＡ製）を用いて、フラックスが２．２５ｍ／ｄ（約９４ＬＭＨ）となる条件で行った。
単位濾過面積当たりの流量Ｊは、前記膜モジュールの単位時間当たりの膜透過水量（ｍ３／ｓ）を前記膜モジュールの有効膜面積で除することにより求めた。前記膜モジュールの単位時間当たりの透過水量（ｍ３／ｓ）は、前記膜モジュールの膜透過水を、電子天秤（ＦＧシリーズ デジタルはかり、株式会社Ａ＆Ｄ製）上に設置したタンク内に流入させ、タンク内の膜透過水の質量変化を、データロガー（計量データロガー ＡＤ−１６８８、株式会社Ａ＆Ｄ製）によって１時間ごとに測定し、測定された１時間ごとの質量変化を算術平均し、さらに１秒ごとの質量変化に換算した値（ｋｇ）を透過水の密度（ｋｇ／ｍ３）で除して求めた。
膜間差圧は、被処理水が透過する膜面側の圧力と、被処理水が透過した膜面側の圧力との差を圧力計（プレッシャセンサ、ＳＭＣ製）でモニターし、データロガー（株式会社Ｔ＆Ｄ製）によって１時間ごとに測定し、測定された各圧力差を算術平均することにより求めた。
また、透過水の粘度μは、透過水の膜透水時の温度に応じて、以下の二次近似式（２）を用いて求めた。透過水の膜透水時の温度は、前記の吸引濾過試験においてタンク内の水の温度を、データロガー（株式会社Ｔ＆Ｄ製）によって１時間ごとに測定し、測定された各温度を算術平均することにより求めた。透過水の膜透水時の温度は、４．３５〜１９℃の間のいずれかの温度であった。
μ＝０．００６ｔ２−０．０４９３ｔ＋１．７４７１（Ｒ２＝０．９９９６）・・（２）
ここで、ｔは、透過水の膜透水時の温度である。
(Measurement of rising speed of membrane filtration resistance)
The membrane filtration resistance R (m -1 ) was calculated by the following equation (1).
R = ΔP / (μ × J) (1)
Here, ΔP is the transmembrane pressure difference (Pa), μ is the viscosity of the permeated water (Pa · s), and J is the flow rate per unit filtration area (m 3 / (m 2 × s)). .
The flow rate J per unit filtration area and the transmembrane pressure ΔP were determined by a suction filtration test using a dipping type membrane module. The membrane module was configured by modularizing eight hollow fiber MF membranes (manufactured by Asahi Kasei Chemicals) made of polyvinylidene fluoride (PVDF) such that the effective membrane area was 0.005 m 2 . The pore size of the membrane used was 0.08 μm.
In the suction filtration test, the filtration rate of the water to be treated was determined using a peristaltic pump (L / S series, manufactured by Yamato Scientific Co., Ltd.) with an initial permeation flux of 1.5 m / d (62.5 L / m 2 / h (LMH)). In the suction filtration test, the membrane module was subjected to backwashing (backwashing) using permeated water of the membrane module every 30 minutes for 1 minute. The backwash was performed using a peristaltic pump (MP type, manufactured by EYELA) under the condition that the flux was 2.25 m / d (about 94 LMH).
The flow rate J per unit filtration area was determined by dividing the amount of permeated water (m 3 / s) per unit time of the membrane module by the effective membrane area of the membrane module. The amount of permeated water per unit time (m 3 / s) of the membrane module is determined by flowing the permeated water of the membrane module into a tank installed on an electronic balance (FG series digital balance, manufactured by A & D), The mass change of the membrane permeated water in the tank was measured every hour by a data logger (measurement data logger AD-1688, manufactured by A & D), and the measured mass change every hour was arithmetically averaged. It was determined by dividing the value (kg) converted to the mass change per second by the density of the permeated water (kg / m 3 ).
The differential pressure between the membranes is monitored by a pressure gauge (pressure sensor, manufactured by SMC) using a pressure gauge (pressure sensor, manufactured by SMC) to monitor the difference between the pressure on the membrane surface where the water to be treated permeates and the pressure on the membrane surface where the water to be treated permeates. (Manufactured by T & D Co., Ltd.) every hour, and the measured pressure differences were obtained by arithmetic averaging.
The viscosity μ of the permeated water was determined using the following quadratic approximation (2) according to the temperature at the time of permeation of the permeated water through the membrane. The temperature of the permeated water permeated through the membrane is determined by measuring the temperature of the water in the tank every hour using a data logger (manufactured by T & D Corporation) in the above suction filtration test, and arithmetically averaging the measured temperatures. Determined by The temperature during the permeation of the permeated water through the membrane was any temperature between 4.35 and 19 ° C.
μ = 0.006t 2 −0.0493t + 1.7471 (R 2 = 0.9996) (2)
Here, t is the temperature at the time of membrane permeation of permeated water.
上記のようなバイオポリマー濃度の異なる被処理水を用いて、精密濾過膜の膜濾過抵抗の上昇速度を測定した結果を図４に示した。 FIG. 4 shows the results of measuring the rate of increase in the membrane filtration resistance of the microfiltration membrane using the water to be treated having different biopolymer concentrations as described above.
図４から、被処理水中のバイオポリマー濃度が１２μｇ／Ｌのときの膜濾過抵抗の上昇速度の値は比較的小さい値となることが分かった。
また、被処理水中のバイオポリマー濃度が９μｇ／Ｌのときの膜濾過抵抗の上昇速度の値は、被処理水中のバイオポリマー濃度が１２μｇ／Ｌのときよりも小さい値となることが分かった。
この結果から、被処理水中のバイオポリマー濃度が１２μｇ／Ｌを越えたときに、ファウリング抑制物質を被処理水に添加することにより、膜濾過抵抗の上昇速度の値が大きくなることを抑制でき、被処理水中のバイオポリマー濃度が９μｇ／Ｌを越えたときに、ファウリング抑制物質を被処理水に添加することにより、膜濾過抵抗の上昇速度の値が大きくなることをより好適に抑制することができることが示唆される。
From FIG. 4, it was found that when the concentration of the biopolymer in the water to be treated was 12 μg / L, the value of the rate of increase in the membrane filtration resistance was relatively small.
Further, it was found that the value of the rate of increase in the membrane filtration resistance when the concentration of the biopolymer in the water to be treated was 9 μg / L was smaller than that when the concentration of the biopolymer in the water to be treated was 12 μg / L.
From this result, when the biopolymer concentration in the water to be treated exceeds 12 μg / L, it is possible to suppress the increase in the value of the rate of increase in the membrane filtration resistance by adding the anti-fouling substance to the water to be treated. When the concentration of the biopolymer in the water to be treated exceeds 9 μg / L, by adding a fouling inhibitor to the water to be treated, it is possible to more suitably suppress the increase in the rate of increase in the membrane filtration resistance. It is suggested that you can.
１：水処理設備、１０：膜分離部、２０：前処理部、
１１：膜分離ユニット、２１：バイオポリマー濃度測定部、２２：ファウリング抑制物質添加部、２３：生物接触濾過部、２４：混合部、
２１ａ：サンプリング槽、２１ｂ：サンプラー、２１ｃ：濃度測定装置、
Ｓ１：前処理工程、Ｓ２：膜分離工程
1: water treatment equipment, 10: membrane separation unit, 20: pretreatment unit,
11: membrane separation unit, 21: biopolymer concentration measurement unit, 22: fouling inhibitor addition unit, 23: biological contact filtration unit, 24: mixing unit
21a: sampling tank, 21b: sampler, 21c: concentration measuring device,
S1: Pretreatment step, S2: Membrane separation step
Claims (3)
前記膜分離部の上流側に配され、前記被処理水中のバイオポリマー濃度を所定閾値以下となるように調整する前処理部と、を備え、
前記前処理部は、膜分離前の前記被処理水中のバイオポリマー濃度を測定するバイオポリマー濃度測定部と、
前記バイオポリマー濃度測定部によって測定された前記バイオポリマー濃度が所定閾値以上になったときに、ファウリングを抑制するようにファウリング抑制物質を膜分離前の前記被処理水に添加するファウリング抑制物質添加部と、
前記バイオポリマー濃度測定部および前記ファウリング抑制物質添加部よりも上流側に、水質浄化作用を有する微生物を生育させた濾材を有し、かつ該濾材を用いて膜分離前の前記被処理水を濾過する生物接触濾過部と、を備え、
前記所定閾値は、９μｇ／Ｌ以上１２μｇ／Ｌ以下の範囲のいずれかの値に設定されている、
水処理設備。 A membrane separation unit for membrane-separating water to be treated containing organic matter,
A pretreatment unit arranged on the upstream side of the membrane separation unit and adjusting the biopolymer concentration in the water to be treated to be equal to or less than a predetermined threshold value ,
The pretreatment unit, a biopolymer concentration measurement unit that measures the biopolymer concentration in the water to be treated before membrane separation,
When the biopolymer concentration measured by the biopolymer concentration measurement unit is equal to or greater than a predetermined threshold, fouling suppression by adding a fouling suppressing substance to the water to be treated before membrane separation so as to suppress fouling. A substance addition section;
On the upstream side of the biopolymer concentration measurement section and the fouling inhibitor addition section, a filter medium in which microorganisms having a water purification action are grown, and the water to be treated before membrane separation is performed using the filter medium. A biological contact filtration unit for filtering,
The predetermined threshold is set to any value in a range from 9 μg / L to 12 μg / L,
Water treatment equipment.
請求項１に記載の水処理設備。 The membrane separation unit includes a microfiltration or ultrafiltration membrane, membrane separation of the water to be treated using the microfiltration or the ultrafiltration membrane,
The water treatment facility according to claim 1.
前記膜分離工程前に、前記被処理水中のバイオポリマー濃度を所定閾値以下となるように調整する前処理工程と、を備え、
前記前処理工程は、水質浄化作用を有する微生物を生育させた濾材を用いて前記被処理水を濾過し、濾過された前記被処理水中のバイオポリマー濃度を測定し、測定されたバイオポリマー濃度が所定閾値以上の場合に、前記被処理水にファウリング抑制物質を添加し
て、前記膜分離工程で膜分離する被処理水とし、測定されたバイオポリマー濃度が所定閾値未満の場合に、前記被処理水にファウリング抑制物質を添加せずに、前記膜分離工程で膜分離する被処理水とし、
前記所定閾値は、９μｇ／Ｌ以上１２μｇ／Ｌ以下の範囲のいずれかの値に設定されている、
水処理方法。 A membrane separation step of membrane-separating water to be treated containing organic matter,
Before the membrane separation step, comprising a pretreatment step of adjusting the biopolymer concentration in the water to be treated to be equal to or less than a predetermined threshold ,
The pretreatment step is to filter the water to be treated using a filter medium in which microorganisms having a water purification effect are grown, and to measure the concentration of the biopolymer in the filtered water to be treated, and the measured biopolymer concentration is When the concentration is equal to or more than a predetermined threshold, a fouling inhibitor is added to the water to be treated to obtain water to be subjected to membrane separation in the membrane separation step, and when the measured biopolymer concentration is less than a predetermined threshold, the water is treated. Without adding a fouling inhibitor to the treated water, the treated water to be subjected to membrane separation in the membrane separation step,
The predetermined threshold is set to any value in a range from 9 μg / L to 12 μg / L,
Water treatment method.
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