JP5258714B2 - Water treatment method and water treatment apparatus - Google Patents
Water treatment method and water treatment apparatus Download PDFInfo
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- JP5258714B2 JP5258714B2 JP2009212019A JP2009212019A JP5258714B2 JP 5258714 B2 JP5258714 B2 JP 5258714B2 JP 2009212019 A JP2009212019 A JP 2009212019A JP 2009212019 A JP2009212019 A JP 2009212019A JP 5258714 B2 JP5258714 B2 JP 5258714B2
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 136
- 238000011282 treatment Methods 0.000 title claims description 60
- 238000000034 method Methods 0.000 title claims description 41
- 239000000126 substance Substances 0.000 claims description 92
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 82
- 238000002347 injection Methods 0.000 claims description 58
- 239000007924 injection Substances 0.000 claims description 58
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 37
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 37
- 239000000701 coagulant Substances 0.000 claims description 18
- 239000007787 solid Substances 0.000 claims description 13
- 238000011276 addition treatment Methods 0.000 claims description 12
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 12
- 238000005345 coagulation Methods 0.000 claims description 7
- 230000015271 coagulation Effects 0.000 claims description 7
- 239000004155 Chlorine dioxide Substances 0.000 claims description 6
- 235000019398 chlorine dioxide Nutrition 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 230000001112 coagulating effect Effects 0.000 claims 1
- 239000012528 membrane Substances 0.000 description 27
- 238000005374 membrane filtration Methods 0.000 description 25
- 230000008569 process Effects 0.000 description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 13
- 230000002776 aggregation Effects 0.000 description 13
- 229910052799 carbon Inorganic materials 0.000 description 13
- 238000005054 agglomeration Methods 0.000 description 11
- 230000008859 change Effects 0.000 description 11
- 238000002156 mixing Methods 0.000 description 9
- 239000003002 pH adjusting agent Substances 0.000 description 7
- 230000007812 deficiency Effects 0.000 description 6
- 238000005189 flocculation Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 238000010979 pH adjustment Methods 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Natural products CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000002835 absorbance Methods 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 239000008239 natural water Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 description 2
- 229960002218 sodium chlorite Drugs 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Description
本発明は、処理対象となる原水中に化学物質を添加する化学物質添加処理と、前記化学物質添加処理後の原水中に凝集剤を注入して前記原水中の固形分を凝集させる凝集処理とを含む水処理方法に関する。 The present invention includes a chemical substance addition process for adding a chemical substance to the raw water to be treated, and a coagulation process for injecting a flocculant into the raw water after the chemical substance addition process to aggregate the solid content in the raw water. The present invention relates to a water treatment method including
水処理には、その工程の１つとして、原水（処理対象水）に凝集剤を注入して原水中の固形分を凝集させる凝集処理が含まれる。従来、この凝集処理における凝集剤の注入量は、処理システムに流入する原水の濁度に基づいて制御するのが一般的である（特許文献１及び２参照）。なお、凝集処理には沈殿処理（＋砂ろ過）を伴うのが通常であり、その場合の凝集処理は、凝集によって形成されたフロックを良好に沈殿させることを目標としていた。 One of the processes in the water treatment includes a flocculation treatment in which a flocculant is injected into the raw water (treatment target water) to agglomerate solids in the raw water. Conventionally, the amount of flocculant injected in this flocculation process is generally controlled based on the turbidity of raw water flowing into the treatment system (see Patent Documents 1 and 2). The agglomeration process is usually accompanied by a precipitation process (+ sand filtration). In this case, the agglomeration process is aimed at precipitating the flocs formed by the agglomeration well.
近年、凝集処理の対象は、河川水や工場排水だけでなく、無機成分が少なく、かつ有機物が多く含まれる下水の二次処理水など多様化している。また、凝集処理後、必ずしも沈殿処理を行わず、凝集物（懸濁物）を除去する方式（膜ろ過処理など）が用いられつつある。沈殿処理を行わず、例えば膜ろ過処理により凝集物（懸濁物）の除去を行う場合には、原水中の微細固形物が膜に詰まって膜の透過抵抗が増大するのを抑制するため、凝集処理において、原水中の微細固形物を十分に凝集させておくことが重要である。 In recent years, not only river water and factory effluent but also sewage secondary treatment water that contains few inorganic components and contains a large amount of organic substances has been diversified. In addition, a method of removing aggregates (suspension) (such as membrane filtration process) is being used without necessarily performing a precipitation process after the aggregation process. For example, when removing aggregates (suspension) by membrane filtration without carrying out precipitation treatment, fine solids in raw water are prevented from clogging the membrane and increasing the permeation resistance of the membrane. In the flocculation process, it is important that the fine solids in the raw water are sufficiently flocculated.
ところで、凝集剤の注入量を、処理対象である原水の濁度に基づいて制御する従来の方法においては、原水の濁度が低い、若しくは濁度変化が小さいため制御ができない場合がある。また、濁度が同一であっても、濁度として計測される物質の中の無機物と有機物との比が異なっていたり、濁度として計測されない物質（溶解性の有機物など）が含まれていたりすると、必要とされる凝集剤の量が異なる場合があるため、原水の濁度に基づいて凝集剤の注入量を制御する方法では、凝集剤の過不足が生じることが有る。 By the way, in the conventional method of controlling the injection amount of the flocculant based on the turbidity of the raw water to be treated, the turbidity of the raw water is low or the turbidity change is small, so there are cases where it cannot be controlled. In addition, even if the turbidity is the same, the ratio of the inorganic substance to the organic substance in the substance measured as turbidity is different, or substances that are not measured as turbidity (such as soluble organic substances) are included. Then, since the amount of the flocculant required may differ, in the method of controlling the injection amount of the flocculant based on the turbidity of raw water, the flocculant may be excessive or insufficient.
また、凝集剤の注入量を、原水中の有機物量に基づいて制御することも行われており、その際、有機物量の指標としてはＥ２６０（波長２６０ｎｍの紫外線の吸光度）やＴＯＣ（総有機炭素量）などが用いられているが、これらの指標を用いる場合、有機物量の測定作業が繁雑で、迅速かつ連続的な測定を行うことが困難である。また、これらの指標は、凝集すべき有機物の総量を表してはおらず、更に無機成分については考慮されていないため、やはりそれらの値に基づいて凝集剤の注入量を過不足なく適切に制御することは困難である。 In addition, the amount of the flocculant injected is controlled based on the amount of organic matter in the raw water. In this case, E260 (absorbance of ultraviolet light having a wavelength of 260 nm) or TOC (total organic carbon) is used as an indicator of the amount of organic matter. However, when these indicators are used, the work of measuring the amount of organic substances is complicated, and it is difficult to perform quick and continuous measurement. In addition, these indicators do not represent the total amount of organic matter to be aggregated, and further, inorganic components are not taken into account, and accordingly, the injection amount of the flocculant is appropriately controlled based on those values without excess or deficiency. It is difficult.
本発明は、このような従来の事情に鑑みてなされたものであり、その目的とするところは、凝集処理における凝集剤の注入量を、原水中に含まれる凝集すべき成分の量に対して過不足なく適切に制御できるような水処理方法及び水処理装置を提供することにある。 This invention is made | formed in view of such a conventional situation, The place made into the objective is the amount of injection | pouring of the coagulant | flocculant in a coagulation process with respect to the quantity of the component which should be aggregated contained in raw | natural water. It is an object of the present invention to provide a water treatment method and a water treatment apparatus that can be appropriately controlled without excess or deficiency.
上記目的を達成するため、本発明によれば、以下の水処理方法及び水処理装置が提供される。 In order to achieve the above object, according to the present invention, the following water treatment method and water treatment apparatus are provided.
［１］ 処理対象となる原水中にオゾン、次亜塩素酸ナトリウム及び二酸化塩素からなる群より選択される何れか１種の化学物質を添加する化学物質添加処理と、前記化学物質添加処理後の原水中に凝集剤を注入して前記原水中の固形分を凝集させる凝集処理とを含む水処理方法であって、前記処理対象となる原水は、前記化学物質により酸化され、その酸化後に前記凝集剤により凝集される成分を含むものであり、前記凝集剤の注入量を、前記化学物質添加後の残留化学物質濃度を一定制御した場合における前記化学物質の必要添加量に比例するように制御する水処理方法。 [1] A chemical substance addition process for adding any one chemical substance selected from the group consisting of ozone, sodium hypochlorite, and chlorine dioxide to the raw water to be treated, and after the chemical substance addition process A water treatment method comprising injecting a flocculant into raw water to agglomerate solids in the raw water, wherein the raw water to be treated is oxidized by the chemical substance, and after the oxidation, the agglomeration The amount of the flocculant injected is controlled so as to be proportional to the required amount of the chemical substance when the concentration of the residual chemical substance after the chemical substance addition is controlled to be constant. Water treatment method.
［２］ 処理対象となる原水中にオゾン、次亜塩素酸ナトリウム及び二酸化塩素からなる群より選択される何れか１種の化学物質を添加する化学物質添加処理と、前記化学物質添加処理後の原水中に凝集剤を注入して前記原水中の固形分を凝集させる凝集処理とを行う水処理装置であって、前記処理対象となる原水は、前記化学物質により酸化され、その酸化後に前記凝集剤により凝集される成分を含むものであり、前記凝集剤の注入量を、前記化学物質添加後の残留化学物質濃度を一定制御した場合における前記化学物質の必要添加量に比例するように制御する水処理装置。 [ 2 ] A chemical substance addition process for adding any one chemical substance selected from the group consisting of ozone, sodium hypochlorite and chlorine dioxide to the raw water to be treated, and after the chemical substance addition process A water treatment apparatus that performs a flocculation process for injecting a flocculant into raw water to agglomerate solids in the raw water, wherein the raw water to be treated is oxidized by the chemical substance, and after the oxidation, The amount of the flocculant injected is controlled so as to be proportional to the required amount of the chemical substance when the concentration of the residual chemical substance after the chemical substance addition is controlled to be constant. Water treatment equipment.
本発明によれば、凝集処理における凝集剤の注入量を制御するための指標（基準）として、化学物質添加処理における化学物質要求量（化学物質添加後の水質を一定制御した場合における化学物質の必要添加量）を用いたことにより、凝集剤を、原水中に含まれる凝集すべき成分の量に対して過不足なく注入することができ、その結果、凝集処理後段のプロセス（膜ろ過処理など）の効率及び処理水の水質を向上させることができるとともに、凝集剤の過剰な注入を防ぐことでその注入量を減少させ、水処理のランニングコストを低減させることができる。 According to the present invention, as an index (standard) for controlling the injection amount of the flocculant in the agglomeration treatment, the required amount of the chemical substance in the chemical substance addition treatment (the chemical substance in the case where the water quality after the chemical substance addition is controlled constant) By using the necessary addition amount), the flocculant can be injected without excess or deficiency with respect to the amount of the components to be aggregated contained in the raw water, and as a result, the process after the aggregation treatment (membrane filtration treatment, etc.) ) And the quality of the treated water can be improved, and the injection amount of the flocculant can be prevented to reduce the injection amount, thereby reducing the running cost of the water treatment.
以下、本発明を具体的な実施形態に基づき説明するが、本発明は、これに限定されて解釈されるものではなく、本発明の範囲を逸脱しない限りにおいて、当業者の知識に基づいて、種々の変更、修正、改良を加え得るものである。 Hereinafter, the present invention will be described based on specific embodiments, but the present invention should not be construed as being limited thereto, and based on the knowledge of those skilled in the art without departing from the scope of the present invention. Various changes, modifications, and improvements can be added.
本発明の水処理方法は、処理対象となる原水中に化学物質を添加する化学物質添加処理と、前記化学物質添加処理後の原水中に凝集剤を注入して前記原水中の固形分を凝集させる凝集処理とを含む。 The water treatment method of the present invention includes a chemical substance addition treatment for adding a chemical substance to raw water to be treated, and a flocculant is injected into the raw water after the chemical substance addition treatment to agglomerate solids in the raw water. Coagulation treatment.
化学物質添加処理において、処理対象となる原水中に添加する化学物質としては、オゾン、次亜塩素酸ナトリウム、二酸化塩素等が好適なものとして挙げられ、これらの化学物質は、原水中に含まれる成分を酸化する酸化剤として用いられる。 In the chemical substance addition treatment, ozone, sodium hypochlorite, chlorine dioxide and the like are preferable as chemical substances added to the raw water to be treated, and these chemical substances are contained in the raw water. Used as an oxidizing agent to oxidize components.
凝集処理は、化学物質添加処理後の原水中に凝集剤を注入して原水中の固形分を凝集させる処理であり、本発明は、この凝集処理における凝集剤の注入量を、前記化学物質添加後の水質を一定制御した場合における前記化学物質の必要添加量（以下、この必要添加量のことを「化学物質要求量」と称する。）に応じて制御することを、その主要な特徴とする。ここで、「水質」とは、前記化学物質の添加により変化する水の性質であって、例えば、前記化学物質の添加後に消費されず残留する化学物質の濃度（例えば、残留溶存オゾン濃度や残留塩素濃度）、色度、濁度、吸光度などを指す。 The agglomeration treatment is a treatment for injecting a flocculant into the raw water after the chemical substance addition treatment to agglomerate solids in the raw water, and the present invention determines the injection amount of the flocculant in the agglomeration treatment by adding the chemical substance. Its main feature is that it is controlled according to the required amount of chemical substance added (hereinafter referred to as “chemical substance required amount”) when the water quality is controlled at a later stage. . Here, the “water quality” is the property of water that changes due to the addition of the chemical substance. For example, the concentration of the chemical substance that is not consumed after the chemical substance is added (for example, residual dissolved ozone concentration or residual Chlorine concentration), chromaticity, turbidity, absorbance, etc.
凝集処理において、化学物質添加処理後の原水中に注入する凝集剤としては、ＰＡＣ（ポリ塩化アルミニウム）、硫酸バンド、塩化第二鉄、ＰＳＩ（ポリシリカ鉄）等が好適なものとして挙げられる。 In the agglomeration treatment, PAC (polyaluminum chloride), sulfate band, ferric chloride, PSI (polysilica iron) and the like are preferable as the aggregating agent to be injected into the raw water after the chemical substance addition treatment.
本発明において、凝集剤の注入量を制御するための指標（基準）として用いられる、化学物質要求量は、当該化学物質によって酸化される原水中の有機物や無機物の量及び質(種類)によって複合的に変化する。このため、化学物質要求量は、濁度や総有機炭素量などで表される原水中の一部の水質を表した指標と異なり、処理水の水質負荷（被処理物質）の総量を示す代替指標となり得る。したがって、化学物質要求量に基づいて凝集剤の注入量を制御することにより、凝集剤を、原水中に含まれる凝集すべき成分の量に対して過不足なく注入することができる。 In the present invention, the required amount of chemical substance used as an index (standard) for controlling the injection amount of the flocculant is compounded according to the quantity and quality (type) of organic and inorganic substances in raw water oxidized by the chemical substance. Changes. Therefore, the chemical substance requirement is an alternative to the total amount of the treated water quality load (substance to be treated), unlike the indicator of the quality of some of the raw water expressed by turbidity and total organic carbon. Can be an indicator. Therefore, by controlling the injection amount of the flocculant based on the required amount of the chemical substance, the flocculant can be injected without excess or deficiency with respect to the amount of the component to be aggregated contained in the raw water.
なお、凝集処理後の原水は、膜ろ過処理等の後段のプロセスにより凝集物（懸濁物）が分離される。膜ろ過処理を行う場合、分離膜としては、ＭＦ膜やＵＦ膜が好適に使用できる。分離膜の材質は、高分子膜であってもセラミック膜であっても良い。また、分離膜の形状は、一般的なモノリス型の他、チューブラー膜、ハニカム膜、中空糸膜、平膜等、任意の形状のものを使用できる。 The raw water after the coagulation treatment is separated into aggregates (suspensions) by a subsequent process such as membrane filtration. When performing a membrane filtration treatment, an MF membrane or a UF membrane can be suitably used as the separation membrane. The material of the separation membrane may be a polymer membrane or a ceramic membrane. In addition to the general monolith type, the separation membrane may have any shape such as a tubular membrane, a honeycomb membrane, a hollow fiber membrane, and a flat membrane.
本発明の水処理装置は、本発明の水処理方法を実施するために使用されるものである。この水処理装置は、処理対象となる原水中に化学物質を添加する化学物質添加処理と、前記化学物質添加処理後の原水中に凝集剤を注入して前記原水中の固形分を凝集させる凝集処理とを行うものであり、前記凝集剤の注入量を、前記化学物質添加後の水質を一定制御した場合における前記化学物質の必要添加量に応じて制御することを、その主要な特徴とする。 The water treatment apparatus of the present invention is used for carrying out the water treatment method of the present invention. This water treatment device includes a chemical substance addition process for adding a chemical substance to the raw water to be treated, and an agglomeration that injects a flocculant into the raw water after the chemical substance addition process to agglomerate solids in the raw water The main feature is that the injection amount of the flocculant is controlled according to the required addition amount of the chemical substance when the water quality after the chemical substance addition is controlled to be constant. .
図１は、本発明の水処理装置の構成の一例を示すフロー図である。この水処理装置１００は、オゾン接触槽１、ｐＨ調整槽２、凝集混和槽３、膜ろ過装置４、及び処理水槽５を備える。処理対象である原水は、原水供給ポンプ６によりオゾン接触槽１に圧送される。オゾン接触槽１では、オゾン発生装置７より発生したオゾンガスがディフューザー８より散気され、原水中に溶解させられる。所定時間オゾンと接触した原水は、オゾン接触槽１から越流し、ｐＨ調整槽２でｐＨ調整剤を添加された後、凝集剤混和槽３へと送水される。凝集剤混和槽３にはｐＨ計１５が設けられており、ｐＨ調整剤は、このｐＨ計１５にて計測されるｐＨが所定の値になるようにｐＨ調整剤供給ポンプ１６によりｐＨ調整槽２に添加される。凝集剤混和槽３では、凝集剤貯留槽９から、凝集剤注入ポンプ１０を介して凝集剤が添加され、撹拌スクリュー１７により混和された後、膜ろ過供給ポンプ１１を介して膜ろ過装置４へと圧送される。膜ろ過装置４で膜ろ過処理された水は、処理水槽５に貯留された後、処理水として送水される。
FIG. 1 is a flowchart showing an example of the configuration of the water treatment apparatus of the present invention. The
本実施例における、化学物質要求量としては、オゾン発生装置７より発生したオゾンガス濃度が使用される。オゾン発生装置７より発生したオゾンガスは、オゾン接触槽１へ注入される。オゾンガス発生濃度は、溶存オゾン濃度計１２で計測される残留溶存オゾン濃度が一定の範囲（例えば０．３〜１．０ｍｇ／Ｌ）になるよう制御する。溶存オゾン濃度計１２で計測された残留溶存オゾン濃度の情報は制御部１３に送られる。制御部１３は、溶存オゾン濃度計１２で計測された残留溶存オゾン濃度が制御値（例えば０．３〜１．０ｍｇ／Ｌ）より低い場合は、オゾン発生装置７の出力を上げ、残留溶存オゾン濃度が制御値より高い場合は、オゾン発生装置７の出力を下げるよう指令を出すための演算処理装置である。オゾン発生装置７で発生させたオゾンガスは、オゾンガス濃度計１４にて濃度が計測される。オゾンガス濃度計１４にて計測されたオゾンガス濃度の情報は、制御部１３に送られ、制御部１３は、そのオゾンガス濃度に基づいて凝集剤注入ポンプ１０の出力を制御する。
As the chemical substance requirement amount in this embodiment, the ozone gas concentration generated from the ozone generator 7 is used. Ozone gas generated from the ozone generator 7 is injected into the ozone contact tank 1. The ozone gas generation concentration is controlled so that the residual dissolved ozone concentration measured by the dissolved
図３は、前記水処理装置で、オゾン接触槽１の出口の残留溶存オゾン濃度を一定になるよう制御した場合における、オゾン発生装置７からのオゾンガス発生濃度、原水の総有機物炭素濃度及び濁度を示したグラフである。なお、このグラフにおいて、左側縦軸の数値は、総有機物炭素濃度（ｍｇ／Ｌ）と濁度（度）との両方に共有される。このグラフから、残留溶存オゾン濃度を一定になるよう制御した場合に必要となるオゾンの添加量（オゾンガスの発生濃度）は、濁度や総有機炭素濃度の変動のみに依存していないことがわかる。 FIG. 3 shows the ozone concentration generated from the ozone generator 7, the total organic carbon concentration and the turbidity of the raw water when the water treatment apparatus controls the residual dissolved ozone concentration at the outlet of the ozone contact tank 1 to be constant. It is the graph which showed. In this graph, the numerical value on the left vertical axis is shared by both the total organic carbon concentration (mg / L) and the turbidity (degree). From this graph, it can be seen that the amount of ozone added (ozone gas generation concentration) required when the residual dissolved ozone concentration is controlled to be constant does not depend only on fluctuations in turbidity or total organic carbon concentration. .
オゾンは、総有機炭素や濁度として計測される成分の全部若しくは一部に消費される。総有機炭素で計測される成分では、有機物の形態（高分子、低分子など）によってオゾンの消費量が変わり、濁度として計測される濁質は、有機性と無機性のものがあり、存在する濁質の質と量によってオゾンの消費量は異なる。このため、同じ総有機物炭素濃度や濁度であっても、原水中の含有成分によってオゾンの消費量は異なるものとなる。また、オゾンを消費する物質は、総有機炭素や濁度として計測される成分だけではない。残留溶存オゾン濃度一定制御下において、オゾン発生装置７からのオゾンガス発生濃度（オゾン接触槽１へのオゾンガス注入量）は、原水中に含まれる、オゾンを消費する成分（オゾンにより酸化される成分）の総量に対応して変動する。このため、オゾン発生濃度は、処理水の水質負荷（被処理物質）の総量を示す代替指標となり得る。このオゾンガス発生濃度に基づいて凝集剤の注入量を制御することにより、凝集剤を、原水中に含まれる凝集すべき成分の量に対して過不足なく注入することができる。 Ozone is consumed by all or part of the components measured as total organic carbon and turbidity. Among the components measured in total organic carbon, ozone consumption varies depending on the form of organic matter (polymer, low molecule, etc.), and turbidity measured as turbidity can be organic or inorganic. The amount of ozone consumed varies depending on the quality and amount of suspended matter. For this reason, even if it is the same total organic carbon density | concentration and turbidity, the consumption of ozone changes with the components contained in raw | natural water. In addition, substances that consume ozone are not limited to components measured as total organic carbon or turbidity. Under the constant control of the residual dissolved ozone concentration, the ozone gas generation concentration from the ozone generator 7 (the amount of ozone gas injected into the ozone contact tank 1) is the component that consumes ozone contained in the raw water (component that is oxidized by ozone). It fluctuates corresponding to the total amount. Therefore, the ozone generation concentration can be an alternative index indicating the total amount of treated water quality load (substance to be treated). By controlling the injection amount of the flocculant based on the ozone gas generation concentration, the flocculant can be injected without excess or deficiency with respect to the amount of the component to be aggregated contained in the raw water.
図４及び図５は、オゾンガス発生濃度（化学物質要求量）に応じて凝集剤の注入量を制御する方法の例を示すグラフである。本発明においては、図４に示すように、凝集剤の注入量を、化学物質要求量に比例するように制御（比例制御）しても良いし、図５に示すように、凝集剤の注入量を、化学物質要求量に応じて段階的に変化するように制御（多段制御）しても良い。 4 and 5 are graphs showing an example of a method for controlling the injection amount of the flocculant according to the ozone gas generation concentration (chemical substance requirement amount). In the present invention, as shown in FIG. 4, the injection amount of the flocculant may be controlled (proportional control) so as to be proportional to the chemical substance requirement amount, or as shown in FIG. The amount may be controlled (multistage control) so as to change stepwise according to the chemical substance requirement.
図６は、図４のように、凝集剤の注入量をオゾンガス発生濃度(化学物質要求量)に応じて比例制御した場合における、化学物質要求量と凝集剤の注入量との時間変化を示すグラフである。また、図７は、凝集剤の注入量をオゾンガス発生濃度(化学物質要求量)に応じて比例制御した場合における、凝集剤の注入量と、原水の濁度と、凝集処理後段の膜ろ過処理における膜差圧との時間変化を示すグラフであり、図８は、原水の濁度に応じて比例制御した場合における、凝集剤の注入量と、原水の濁度と、凝集処理後段の膜ろ過処理における膜差圧との時間変化を示すグラフである。なお、図７及び図８のグラフにおいて、左側縦軸の数値は、凝集剤注入量（ｍｇ／Ｌ）と膜差圧（ｋＰａ）との両方に共有される。 FIG. 6 shows the change over time in the required amount of chemical substance and the injected amount of flocculant when the amount of flocculant injected is proportionally controlled according to the ozone gas generation concentration (chemical substance required amount) as shown in FIG. It is a graph. FIG. 7 shows the amount of flocculant injected, the turbidity of raw water, and the membrane filtration treatment after the flocculant treatment when the amount of flocculant injected is proportionally controlled according to the ozone gas generation concentration (chemical substance requirement amount). FIG. 8 is a graph showing a change with time in the membrane differential pressure in FIG. 8, and FIG. 8 shows the amount of the flocculant injected, the turbidity of the raw water, and the membrane filtration after the flocculation treatment when proportional control is performed according to the turbidity of the raw water. It is a graph which shows the time change with the film | membrane differential pressure | voltage in a process. 7 and 8, the numerical value on the left vertical axis is shared by both the flocculant injection amount (mg / L) and the membrane differential pressure (kPa).
膜差圧は、膜ろ過処理に用いられる分離膜の目詰まりの程度によりその値が変動し、膜差圧の値が上昇するほど膜の目詰まりが進行して運転が困難になる。図７に示すように、凝集剤の注入量を化学物質要求量に応じて比例制御した場合、膜差圧はほとんど上昇することなく安定運転が可能である。これは、原水中に含まれる凝集すべき成分の量に対して適切な量の凝集剤の注入されたため、目詰まりの原因となる微細固形物が膜ろ過処理の前に十分に凝集されて、分離膜の目詰まりが抑制されためである。 The value of the membrane differential pressure varies depending on the degree of clogging of the separation membrane used in the membrane filtration treatment, and as the value of the membrane differential pressure increases, clogging of the membrane proceeds and operation becomes difficult. As shown in FIG. 7, when the amount of flocculant injected is proportionally controlled according to the chemical substance requirement, stable operation is possible with almost no increase in the membrane differential pressure. This is because an appropriate amount of the flocculant was injected relative to the amount of the component to be aggregated contained in the raw water, so that the fine solid matter causing clogging was sufficiently aggregated before the membrane filtration treatment, This is because clogging of the separation membrane is suppressed.
一方、図８に示すように、凝集剤の注入量を原水の濁度に応じて比例制御した場合、図中に星印で示した濁度が低い時には、それに対応して凝集剤の注入量を低下させる。最初の濁度低下時（左側の星印）には、それに対応して凝集剤の注入量を低下させても膜差圧の上昇が見られないため、凝集剤の注入量は十分であると考えられる。一方、２度目の濁度低下時（右側の星印）には、濁度低下に対応して凝集剤の注入量を低下させると、膜差圧が大きく上昇している。この膜差圧の上昇は、凝集剤の注入量が不足して、微細固形物が十分に凝集されず、分離膜の目詰まりを引き起こしたことを意味する。すなわち、最初の濁度低下時と２度目の濁度低下時とでは、濁度の値はほぼ同一であるが、前者においては凝集剤の注入量が十分であるのに対し、後者では凝集剤の注入量が不足しており、このことから、同じ濁度においても、必要な凝集剤の注入量が異なる場合があり、凝集剤の注入量を原水の濁度に基づいて制御する方法では、適切な量の凝集剤の注入ができないことがわかる。 On the other hand, as shown in FIG. 8, when the injection amount of the flocculant is proportionally controlled in accordance with the turbidity of the raw water, when the turbidity indicated by an asterisk in the figure is low, the injection amount of the flocculant correspondingly Reduce. When the turbidity drops for the first time (the star on the left), there is no increase in membrane differential pressure even if the injection amount of the flocculant is correspondingly reduced. Therefore, the injection amount of the flocculant is sufficient. Conceivable. On the other hand, when the turbidity is lowered for the second time (the star on the right side), if the injection amount of the flocculant is reduced corresponding to the turbidity reduction, the membrane differential pressure is greatly increased. This increase in the membrane differential pressure means that the injection amount of the flocculant was insufficient, and the fine solids were not sufficiently aggregated, causing clogging of the separation membrane. That is, the turbidity value is almost the same when the first turbidity is lowered and when the turbidity is lowered for the second time. In the former, the injection amount of the flocculant is sufficient, whereas in the latter, the flocculant is injected. From this, there is a case where the required amount of flocculant injected is different even at the same turbidity, and in the method of controlling the amount of flocculant injected based on the turbidity of raw water, It can be seen that an appropriate amount of flocculant cannot be injected.
また、凝集剤の注入量を平均値で比較すると、図７に示すように、凝集剤の注入量を化学物質要求量に応じて比例制御した場合では１５．５ｍｇ／Ｌであったのに対し、図８に示すように、凝集剤の注入量を原水の濁度に応じて比例制御した場合では１８．９ｍｇ／Ｌであった。このことから、凝集剤の注入量を、化学物質要求量に応じて制御した場合には、原水の濁度に応じて制御した場合に比べて、凝集剤の過剰な注入が生じにくく、その結果、凝集剤の注入量を低減できることがわかる。 Moreover, when the injection amount of the flocculant was compared with the average value, as shown in FIG. 7, it was 15.5 mg / L when the injection amount of the flocculant was proportionally controlled according to the chemical substance requirement amount. As shown in FIG. 8, it was 18.9 mg / L when the amount of the flocculant injected was proportionally controlled according to the turbidity of the raw water. From this, when the injection amount of the flocculant is controlled according to the required amount of the chemical substance, compared with the case where it is controlled according to the turbidity of the raw water, the excessive injection of the flocculant is less likely to occur. It can be seen that the amount of the flocculant injected can be reduced.
図９は、オゾンガス発生濃度(化学物質要求量)に応じて凝集剤の注入量を制御した場合と、原水の濁度に応じて凝集剤の注入量を制御した場合とにおける、膜ろ過処理後の処理水中に含まれる総有機炭素濃度の時間変化を示すグラフである。このグラフより、濁度に応じて凝集剤の注入量を制御した場合には、処理水の水質が安定せず、急激な水質の悪化（総有機炭素濃度の増大）が生じることがあるが、化学物質要求量に応じて凝集剤の注入量を制御した場合には、そのような急激な水質の悪化は発生せず、安定した水質を維持しながら装置の運転ができることがわかる。 FIG. 9 shows the results after the membrane filtration treatment in the case where the injection amount of the flocculant is controlled according to the ozone gas generation concentration (chemical substance requirement amount) and in the case where the injection amount of the flocculant is controlled according to the turbidity of the raw water. It is a graph which shows the time change of the total organic carbon concentration contained in the treated water. From this graph, when the amount of the flocculant injected is controlled according to the turbidity, the quality of the treated water is not stable, and a sudden deterioration of the water quality (increased total organic carbon concentration) may occur. It can be seen that when the injection amount of the flocculant is controlled in accordance with the chemical substance requirement, such a rapid deterioration of water quality does not occur, and the apparatus can be operated while maintaining a stable water quality.
なお、以上説明してきた実施形態においては、化学物質添加処理の際の化学物質としてオゾンを用い、凝集処理における凝集剤の注入量を制御するための指標（基準）として、オゾンガス発生濃度（オゾンガス注入率）を用いているが、化学物質添加処理に用いる化学物質は、オゾンに限定されるものではなく、他の化学物質、例えば次亜塩素酸ナトリウムや二酸化塩素であっても良い。 In the embodiment described above, ozone is used as the chemical substance in the chemical substance addition process, and the ozone gas generation concentration (ozone gas injection) is used as an index (reference) for controlling the injection amount of the coagulant in the coagulation process. However, the chemical substance used for the chemical substance addition treatment is not limited to ozone, and may be another chemical substance such as sodium hypochlorite or chlorine dioxide.
図２は、化学物質添加処理の際の化学物質として次亜塩素酸ナトリウムを用い、次亜塩素酸ナトリウム添加後の残留次亜塩素酸ナトリウム濃度を一定制御した場合における前記次亜塩素酸ナトリウムの添加量に応じて、凝集剤の注入量を制御する場合に使用可能な水処理装置の一例である。 FIG. 2 shows the sodium hypochlorite concentration when sodium hypochlorite is used as the chemical substance in the chemical substance addition treatment, and the residual sodium hypochlorite concentration after the sodium hypochlorite addition is controlled to be constant. It is an example of the water treatment apparatus which can be used when controlling the injection amount of the flocculant according to the addition amount.
この水処理装置２００は、次亜塩素酸ナトリウム添加槽２１、ｐＨ調整槽２、凝集混和槽３、膜ろ過装置４、及び処理水槽５を備える。処理対象である原水は、原水供給ポンプ６により次亜塩素酸ナトリウム添加槽２１に圧送される。次亜塩素酸ナトリウム添加槽２１では、次亜塩素酸ナトリウム注入装置２７より送られた次亜塩素酸ナトリウムが、原水に添加される。次亜塩素酸ナトリウムが添加された原水は、亜塩素酸ナトリウム添加槽２１から越流し、ｐＨ調整槽２でｐＨ調整剤を添加された後、凝集剤混和槽３へと送水される。凝集剤混和槽３にはｐＨ計１５が設けられており、ｐＨ調整剤は、このｐＨ計１５にて計測されるｐＨが所定の値になるようにｐＨ調整剤供給ポンプ１６によりｐＨ調整槽２に添加される。凝集剤混和槽３では、凝集剤貯留槽９から、凝集剤注入ポンプ１０を介して凝集剤が添加され、撹拌スクリュー１７により混和された後、膜ろ過供給ポンプ１１を介して膜ろ過装置４へと圧送される。膜ろ過装置４で膜ろ過処理された水は、処理水槽５に貯留された後、処理水として送水される。
The
次亜塩素酸ナトリウム添加槽２１への次亜塩素酸ナトリウムの添加量は、残留塩素濃度計２２で計測される残留次亜塩素酸ナトリウム濃度が一定の範囲になるよう制御する。残留塩素濃度計２２で計測された残留次亜塩素酸ナトリウム濃度の情報は制御部２３に送られ、制御部２３は、残留次亜塩素酸ナトリウム濃度が制御値より低い場合は、次亜塩素酸ナトリウム注入装置２７からの注入量を増加させ、残留次亜塩素酸ナトリウム濃度が制御値より高い場合は、次亜塩素酸ナトリウム注入装置２７からの注入量を減少させるよう指令を出す。次亜塩素酸ナトリウム注入装置２７から次亜塩素酸ナトリウム添加槽２１に注入される次亜塩素酸ナトリウムの添加量は、流量計２４にて計測される。流量計２４にて計測された次亜塩素酸ナトリウムの添加量の情報は、制御部２３に送られ、制御部２３は、その添加量に基づいて凝集剤注入ポンプ１０の出力を制御する。
The amount of sodium hypochlorite added to the sodium
本実施例においても、凝集剤の注入量は、次亜塩素酸ナトリウム濃度（化学物質要求量）に比例するように制御（比例制御）しても良いし、次亜塩素酸ナトリウム濃度（化学物質要求量）に応じて段階的に変化するように制御（多段制御）しても良い。これら制御における、適正な制御切り替え点の数値（化学物質要求量と凝集剤注入量）は、各水処理装置とその処理原水の性質により定まるものであり、水処理装置を運手しながら、切り替え点の数値を選択してゆけばよい。 Also in this embodiment, the injection amount of the flocculant may be controlled (proportional control) so as to be proportional to the sodium hypochlorite concentration (chemical substance requirement), or the sodium hypochlorite concentration (chemical substance). Control (multi-stage control) may be performed so as to change in a stepwise manner according to (request amount). In these controls, the numerical values of the appropriate control switching points (chemical substance request amount and coagulant injection amount) are determined by the properties of each water treatment device and its raw water, and can be switched while handling the water treatment device. Just select the point value.
残留次亜塩素酸ナトリウム濃度一定制御下において、次亜塩素酸ナトリウム注入装置２７から次亜塩素酸ナトリウム添加槽２１に注入される次亜塩素酸ナトリウムの添加量は、原水中に含まれる、次亜塩素酸ナトリウムを消費する成分の総量に対応して変動する。このため、次亜塩素酸ナトリム添加量は、処理水の水質負荷（被処理物質）の総量を示す代替指標となり得る。この次亜塩素酸ナトリウムの添加量に基づいて凝集剤の注入量を制御することにより、凝集剤を、原水中に含まれる凝集すべき成分の量に対して過不足なく注入することができる。
The amount of sodium hypochlorite added to the sodium
本発明は、河川水、工場排水、下水の二次処理水等の水処理方法として好適に利用することができる。 INDUSTRIAL APPLICABILITY The present invention can be suitably used as a water treatment method for river water, factory wastewater, sewage secondary treatment water, and the like.
１：オゾン接触槽、２：ｐＨ調整槽、３：凝集混和槽、４：膜ろ過装置、５：処理水槽、６：原水供給ポンプ、７：オゾン発生装置、８：ディフューザー、９：凝集剤貯留槽、１０：凝集剤注入ポンプ、１１：膜ろ過供給ポンプ、１２：溶存オゾン濃度計、１３：制御部、１４：オゾンガス濃度計、１５：ｐＨ計、１６：ｐＨ調整剤供給ポンプ、１７：撹拌スクリュー、２１：次亜塩素酸ナトリウム添加槽、２２：残留塩素濃度計、２３：制御部、２４：流量計、２７：次亜塩素酸ナトリウム注入装置、１００：水処理装置、２００：水処理装置。 1: ozone contact tank, 2: pH adjustment tank, 3: coagulation mixing tank, 4: membrane filtration device, 5: treated water tank, 6: raw water supply pump, 7: ozone generator, 8: diffuser, 9: coagulant storage Tank: 10: flocculant injection pump, 11: membrane filtration supply pump, 12: dissolved ozone concentration meter, 13: control unit, 14: ozone gas concentration meter, 15: pH meter, 16: pH adjusting agent supply pump, 17: stirring Screw: 21: Sodium hypochlorite addition tank, 22: Residual chlorine concentration meter, 23: Control unit, 24: Flow meter, 27: Sodium hypochlorite injection device, 100: Water treatment device, 200: Water treatment device .
Claims (2)
前記処理対象となる原水は、前記化学物質により酸化され、その酸化後に前記凝集剤により凝集される成分を含むものであり、
前記凝集剤の注入量を、前記化学物質添加後の残留化学物質濃度を一定制御した場合における前記化学物質の必要添加量に比例するように制御する水処理方法。 A chemical substance addition treatment for adding any one chemical substance selected from the group consisting of ozone, sodium hypochlorite and chlorine dioxide to the raw water to be treated, and the raw water after the chemical substance addition treatment A water treatment method including a flocculant that injects a flocculant to agglomerate solids in the raw water,
The raw water to be treated includes a component that is oxidized by the chemical substance and is aggregated by the flocculant after the oxidation.
A water treatment method for controlling an injection amount of the flocculant so as to be proportional to a necessary addition amount of the chemical substance when a residual chemical substance concentration after the chemical substance addition is controlled to be constant.
前記処理対象となる原水は、前記化学物質により酸化され、その酸化後に前記凝集剤により凝集される成分を含むものであり、
前記凝集剤の注入量を、前記化学物質添加後の残留化学物質濃度を一定制御した場合における前記化学物質の必要添加量に比例するように制御する水処理装置。 A chemical substance addition treatment for adding any one chemical substance selected from the group consisting of ozone, sodium hypochlorite and chlorine dioxide to the raw water to be treated, and the raw water after the chemical substance addition treatment A water treatment device for performing a coagulation treatment for injecting a coagulant and coagulating solids in the raw water,
The raw water to be treated includes a component that is oxidized by the chemical substance and is aggregated by the flocculant after the oxidation.
A water treatment apparatus that controls the injection amount of the flocculant so as to be proportional to the required addition amount of the chemical substance when the concentration of the residual chemical substance after the chemical substance addition is controlled to be constant.
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