WO2014087991A1 - 有機性汚水の処理方法および処理装置 - Google Patents
有機性汚水の処理方法および処理装置 Download PDFInfo
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- WO2014087991A1 WO2014087991A1 PCT/JP2013/082453 JP2013082453W WO2014087991A1 WO 2014087991 A1 WO2014087991 A1 WO 2014087991A1 JP 2013082453 W JP2013082453 W JP 2013082453W WO 2014087991 A1 WO2014087991 A1 WO 2014087991A1
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- reverse osmosis
- osmosis membrane
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- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 description 2
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
- B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/06—Specific process operations in the permeate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2623—Ion-Exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2688—Biological processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/025—Permeate series
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
-
- 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
Definitions
- the present invention relates to a method and apparatus for treating organic sewage.
- the present invention relates to a method and a processing apparatus for treating organic sewage discharged from a fiber raw material or a fiber production process by a membrane separation activated sludge treatment method and a reverse osmosis membrane method.
- polyester widely used as a representative fiber material is a polymer having an ester bond.
- PET polyethylene terephthalate
- PTA high-purity terephthalic acid
- ethylene glycol ethylene glycol
- the wastewater is biologically treated to decompose and remove organic matter in the water, and further treated with a reverse osmosis membrane to remove inorganic matter along with the remaining organic matter.
- a membrane separation activated sludge method in which wastewater is biologically treated and solid-liquid separated with a separation membrane may be used.
- the membrane separation activated sludge method solid-liquid separation is performed with a separation membrane immersed in a biological treatment tank, so that the treated water becomes clear and the obtained treated water can be directly used for reverse osmosis membrane treatment.
- Patent Document 1 treats water to be treated with activated sludge in a biological treatment tank, performs membrane separation treatment on the activated sludge treated water in the biological treatment tank, and then performs reverse osmosis treatment on the water subjected to membrane separation treatment.
- the water treatment method which has the process to do is disclosed.
- Patent Document 1 further discloses a method of performing an ultraviolet treatment after the membrane separation treatment and before the reverse osmosis treatment. In the above method, a method of adding a reducing agent immediately after the reverse osmosis membrane treatment after adding a heavy metal ion and a reducing agent is disclosed.
- Patent Document 2 discloses a step of treating activated water in a biological treatment tank, a step of subjecting a mixture of treated water and activated sludge to membrane separation treatment with a microfiltration membrane in the biological treatment tank or outside the biological treatment tank. And a water treatment method comprising a step of reverse osmosis treatment of the water after the membrane separation treatment. Furthermore, Patent Document 2 discloses a treatment process having a step for removing hydrophilic organic substances after the membrane separation treatment and before the reverse osmosis treatment. Then, it is described that fouling can be suppressed by removing hydrophilic organic substances at the front stage of the reverse osmosis membrane.
- JP 2007-0669204 A Japanese Patent Laid-Open No. 2007-244979
- An object of the present invention is to provide a method for treating organic wastewater drained from a fiber raw material or a fiber production process to obtain a higher quality water when obtaining high purity water, and a treatment apparatus therefor. is there.
- the present invention for solving the above-described problems has the following configuration.
- (1) After treating organic sewage by the membrane separation activated sludge method, the treated water is treated with the first-stage reverse osmosis membrane, and further treated with the first-stage reverse osmosis membrane.
- the processing method of organic wastewater which has the process processed with an eye reverse osmosis membrane.
- (2) The method for treating organic sewage, wherein the organic sewage is discharged from the fiber raw material manufacturing process or the fiber manufacturing process.
- a membrane separation activated sludge treatment tank that comprises activated sludge and a membrane unit and treats organic wastewater by a membrane separation activated sludge method;
- a first-stage reverse osmosis membrane module for treating treated water obtained from a membrane separation activated sludge treatment tank with a first-stage reverse osmosis membrane;
- An organic wastewater treatment apparatus comprising: a second-stage reverse osmosis membrane module that treats permeate obtained from the first-stage reverse osmosis membrane module with a second-stage reverse osmosis membrane.
- the said organic wastewater processing apparatus provided with the ion exchange treatment apparatus which ion-exchange-processes the permeate obtained from the 2nd step
- any of the above comprising a carbonic acid removal treatment apparatus for removing carbonic acid from permeated water obtained from the first-stage reverse osmosis membrane module between the first-stage reverse osmosis membrane module and the second-stage reverse osmosis membrane module Organic sewage treatment equipment.
- the organic sewage treatment apparatus wherein the carbonation removal treatment apparatus is a decarboxylation tower that performs aeration under acidic conditions.
- the said organic wastewater treatment apparatus whose acid conditions are pH 4-6.
- the organic wastewater treatment method and treatment apparatus of the present invention can further improve the quality of water obtained when treating wastewater from a fiber raw material or fiber production process.
- Membrane separation activated sludge method is often used for wastewater treatment.
- Organic matter is biologically treated with microorganisms in a biological treatment tank containing activated sludge and decomposed.
- the organic substance is removed by filtering the water in which part or all of the water is decomposed, and the turbidity due to activated sludge is efficiently removed.
- FIG. 1 shows a flow of a conventional treatment process in which a membrane separation activated sludge method and a reverse osmosis membrane treatment are combined.
- Organic sewage from the manufacturing process of fiber raw materials or the like generally contains a large amount of organic matter, and when it is discharged into the environment, it causes eutrophication. Therefore, the organic sewage 1 from the manufacturing process of the fiber raw material or the like is introduced into the membrane separation activated sludge treatment tank 3.
- the organic sludge 1 is treated with activated sludge in the membrane separation activated sludge treatment tank 3 to remove organic matter and turbidity.
- the residence time of the organic sewage 1 in the activated sludge treatment tank 3 is usually about 1 to 24 hours, but an optimum time is selected according to the impurity concentration of the organic sewage 1 and the like.
- the concentration of Mixed Liquor Suspended Solids (hereinafter referred to as “MLSS”) is approximately 5,000mg / L to 15,000mg / L in the membrane separation activated sludge treatment tank 3. If the MLSS concentration is increased, the processing efficiency per volume of the membrane separation activated sludge treatment tank 3 is improved. However, if the MLSS concentration is too high, the viscosity of the activated sludge mixture increases and membrane filtration cannot be performed properly. Is preferred.
- the mixed liquid of the organic sludge 1 and the activated sludge is filtered by the membrane unit 2, and the activated sludge and the treated water are separated into solid and liquid.
- the air compressed by the blower 7 is aerated from the aeration unit 8.
- the membrane surface of the membrane unit 2 is cleaned by aeration air, and the membrane surface is kept clean. Filtration is performed by the suction pump 5.
- the treated water 4 is stored in the first-stage reverse osmosis membrane treated raw water tank 6.
- the water stored in the first-stage reverse osmosis membrane treated raw water tank 6 is supplied to the first-stage reverse osmosis membrane module 10 via the first-stage high-pressure pump 9.
- the water treated with the reverse osmosis membrane is used for reuse as the first-stage permeated water 11, and the first-stage concentrated water 12 is concentrated and dried, discharged or the like.
- a single-stage reverse osmosis membrane treatment can provide water with a good water quality of about 95% to 99% as a salt rejection, but depending on the reuse process, water with higher water quality is required. There is a case.
- FIG. 2 shows a flow diagram of an embodiment of the present invention, in which the organic sewage 1 is treated by the membrane separation activated sludge method, and then the treated water is subjected to reverse osmosis membrane treatment in two stages.
- the processing process of FIG. 2 is the same as the processing process of FIG. 1 described above until the processing by the first-stage reverse osmosis membrane module 10.
- the first-stage permeated water 11 is stored in the second-stage reverse osmosis membrane treated raw water tank 13 and then supplied to the second-stage reverse osmosis membrane module 15 by the second-stage high-pressure pump 14.
- the second-stage permeated water 16 subjected to the reverse osmosis membrane treatment is used for applications such as reuse.
- the second-stage concentrated water 17 is concentrated to dryness, discharged or the like, like the first-stage concentrated water 12.
- the concentration of components such as salts that could not be removed by the first-stage reverse osmosis membrane module 10 by performing the second-stage reverse osmosis membrane treatment.
- the salt concentration of the raw water is 100 mg / L.
- the salt concentration of the first stage permeated water is 5 mg / L
- the salt concentration of the second stage permeated water is 0.25 mg / L
- the desalting rate throughout the process is 99.75%.
- Organic wastewater 1 can generally be treated with microorganisms such as activated sludge treatment. What is drained from the fiber raw material or fiber manufacturing process, or the plastic raw material or plastic manufacturing process, particularly the PTA manufacturing process, is effective.
- microorganisms such as activated sludge treatment. What is drained from the fiber raw material or fiber manufacturing process, or the plastic raw material or plastic manufacturing process, particularly the PTA manufacturing process, is effective.
- the membrane unit used in the membrane separation activated sludge method here is a submerged membrane unit, and in order to improve the handleability and physical durability of the filtration membrane, for example, the filtered water channel material on both sides of the frame
- Examples include a flat membrane element structure in which a filtration membrane is bonded to a sandwich, and a hollow fiber type structure in which hollow fiber membranes are bundled.
- Examples of the membrane structure of the filtration membrane include, but are not limited to, a porous membrane and a composite membrane in which a functional layer is combined with the porous membrane.
- membranes include polyacrylonitrile porous membrane, polyimide porous membrane, polyethersulfone porous membrane, polyphenylene sulfide sulfone porous membrane, polytetrafluoroethylene porous membrane, polyvinylidene fluoride porous membrane, Examples thereof include a porous film such as a polypropylene porous film and a polyethylene porous film. Among them, a polyvinylidene fluoride porous film and a polytetrafluoroethylene porous film are particularly preferable because of high chemical resistance.
- a composite film in which a rubbery polymer such as cross-linked silicone, polybutadiene, polyacrylonitrile butadiene, ethylene propylene rubber, or neoprene rubber is combined as a functional layer can be used as a functional layer.
- a rubbery polymer such as cross-linked silicone, polybutadiene, polyacrylonitrile butadiene, ethylene propylene rubber, or neoprene rubber is combined as a functional layer
- Those having a pore diameter of about 0.01 ⁇ m to 10 ⁇ m are preferable.
- the pore size is generally coarser than that of an ultrafiltration membrane that is separated by molecular sieve.
- the operation with the membrane is usually operated at a pressure of 200 kPa or less from a reduced pressure state.
- the first-stage reverse osmosis membrane module 10 and the second-stage reverse osmosis membrane module 15 have a performance capable of reducing solutes and suspended substances in filtered water to a concentration that can be used as reclaimed water depending on the combination. It is preferable. Furthermore, chemical fouling (chemical fouling) in which dissolved organic matter adheres to the membrane surface and biofouling (biological fouling) in which microorganisms grow and adhere to the membrane surface using dissolved organic matter as a nutrient source are unlikely to occur. A reverse osmosis membrane is used.
- reverse osmosis membranes examples include TML20 manufactured by Toray Industries, Inc., LF10 manufactured by Nitto Denko Corporation, LFC1, LFC3 manufactured by Hydranautics, and BW30-365FR manufactured by Dow.
- the reverse osmosis membrane modules used for the first-stage reverse osmosis membrane module 10 and the second-stage reverse osmosis membrane module 15 may be of the same type, but different types may be combined. What is necessary is just to select an optimal thing from required water quality, a desalination rate, an operating cost, etc.
- the water quality can be improved by further ion-exchange treatment of the second-stage permeated water.
- the flow is shown in FIG.
- the second-stage permeated water 16 is supplied to the ion exchange treatment device 18 to perform ion exchange treatment, and the ion exchange treatment water 19 is reused.
- the ion exchange treatment materials such as an ion exchange resin and an ion exchange membrane are usually used, and an optimum material can be selected according to the purpose and cost.
- An ion exchange resin often used in water treatment is a kind of ion exchange substance (ion exchanger), which is a water-insoluble synthetic resin such as a cation exchange resin, an anion exchange resin, or an amphoteric ion exchange resin. is there.
- an exchange group having an ion exchange function is stably bonded by a covalent bond to a polymer compound having a three-dimensional structure, and the exchange group is uniformly distributed on the resin surface.
- the polymer compound a copolymer of styrene and divinylbenzene can be used.
- the two-stage reverse osmosis membrane treatment is performed, and the concentration of ion components loaded on the ion exchange resin is at a very low level. It becomes possible to keep.
- the regeneration frequency of the ion exchange resin varies depending on the quality of water supplied to the ion exchange resin, the required water quality, and the amount of the ion exchange resin.
- the treated water after membrane separation activated sludge treatment is subjected to reverse osmosis membrane treatment in two stages, preferably further subjected to ion exchange treatment, but the organic matter in the organic wastewater 1 as raw water is activated sludge. Therefore, the treated water contains a carbonic acid component.
- FIG. 4 shows the relationship between the pH and the composition ratio of each carbonic acid component.
- the composition ratio shown in FIG. 4 is an equivalent ratio based on carbonic acid.
- Each carbonic acid component is in an equilibrium state as shown in the following equation.
- the first-stage permeated water 11 is introduced into the decarboxylation tower 20 to remove the carbonic acid component.
- the water from which the carbonic acid component has been removed is stored in the decarboxylated water tank 21 and then supplied to the second-stage reverse osmosis membrane module 15 by the second-stage high-pressure pump 14 and used for the second-stage reverse osmosis membrane treatment.
- the in the decarboxylation treatment it is preferable to remove the carbonic acid component by adding an acid to the raw water to reduce the pH to a predetermined value or less to generate CO 2 (gas) and exposing it to air.
- the acidic conditions for performing the aeration treatment as shown in FIG. 4, if low pH is, although desirable from the standpoint to remove the CO 2, is the far too low chemicals added for pH adjustment From the economical viewpoint, the pH is preferably 4 or more and 6 or less.
- the carbonic acid removal treatment may be carried out before the first-stage reverse osmosis membrane treatment, but if the carbonic acid removal treatment is carried out before the first-stage reverse osmosis membrane treatment, the amount of chemicals required for pH adjustment is large. There is a problem.
- the carbonic acid removal treatment may be performed at a stage prior to the first-stage reverse osmosis membrane treatment, but there is a problem that the amount of the chemical solution for pH adjustment increases due to the buffering action of various components in water. For this reason, it is preferable to remove the carbonic acid by performing aeration treatment under acidic conditions after reducing the salt concentration to some extent by removing the possibility of buffering as much as possible by the first-stage reverse osmosis membrane treatment.
- the reason why it is preferable to perform the carbonic acid removal treatment between the first-stage reverse osmosis membrane treatment and the second-stage reverse osmosis membrane treatment rather than performing the carbonic acid removal treatment after the second-stage reverse osmosis membrane treatment is as follows.
- the chemicals added for pH adjustment after the carbonic acid removal treatment are directly loaded onto the ion exchange resin, resulting in regeneration of the ion exchange resin. This is to prevent the frequency from becoming high.
- the present invention is effective if it is sewage containing an organic compound. Furthermore, the effect of the present invention is particularly remarkable as long as it contains 500 mg / L or more of bicarbonate ions. In addition, if it is a fiber manufacturing process represented by PTA or a polyester manufacturing process, it is effective not only for fibers but also for processes for manufacturing plastics. Further, before the treatment of the membrane separation activated sludge method, there may be a pretreatment such as anaerobic treatment such as methane fermentation for decomposing organic substances by anaerobic bacteria.
- the quality of water to be treated and the test conditions are shown in each table.
- the membrane separation activated sludge treatment is shown in Table 1, and the reverse osmosis membrane treatment (the quality of the water to be treated is the first stage) is shown in Table 2.
- the amount of treated water, membrane separation activated sludge process with 100 m 3 / day, the reverse osmosis membrane treatment was 30 m 3 / day at the first stage 33 m 3 / day, 2 stage.
- the TDS (total soluble matter) of the treated water after the membrane separation activated sludge treatment was 1,000 mg / L.
- COD represents the chemical oxygen demand
- TN represents the total nitrogen content
- TP represents the total phosphorus content.
- Both the first-stage reverse osmosis membrane module and the second-stage reverse osmosis membrane module use SU-710 (4-inch type) manufactured by Toray Industries, Inc.
- the first-stage permeate recovery rate is 80%.
- the permeated water recovery rate was 90%.
- Table 3 shows the results of water quality tests for treated water.
- the treated water is the permeated water after the first-stage reverse osmosis membrane treatment in Comparative Example 1, the permeated water after the second-stage reverse osmosis membrane treatment in Example 1, and the ion exchange treatment in Example 2. It refers to the treated water afterwards.
- an ion exchange resin product name: Amberlite (registered trademark) purified ion exchange resin MB-1) sold by Organo Corporation was used.
- the TDS concentration was 1,000 mg / L, but the treated water of Comparative Example 1 was 50 mg / L, and the treated water of Example 1 was 3.0 mg / L. In the treated water of Example 2, it was 0.1 mg / L.
- the TDS concentration of treated water can be significantly reduced by performing reverse osmosis membrane treatment in two stages, and further, the TDS of treated water can be obtained by performing ion exchange treatment in the subsequent stage. The concentration could be further greatly reduced.
- pure water level water can be obtained from organic sewage by performing reverse osmosis membrane treatment in two stages.
- Examples 3 to 5 In Examples 3 to 5 below, after removing organic sewage by the membrane separation activated sludge method, carbonic acid removal treatment was performed between the first-stage reverse osmosis membrane treatment and the second-stage reverse osmosis membrane treatment. The effect was verified by comparing the period until the regeneration of the ion exchange resin when the pilot tests of Examples 3 to 5 were carried out (hereinafter referred to as “regeneration exchange period”). The regeneration method of the ion exchange resin was carried out by passing hydrochloric acid and sodium hydroxide.
- Example 3 Membrane separation activated sludge treatment ⁇ first stage reverse osmosis membrane treatment ⁇ second stage reverse osmosis membrane treatment ⁇ ion exchange treatment
- Example 4 Membrane separation activated sludge treatment ⁇ First stage reverse osmosis membrane treatment ⁇ Second stage reverse osmosis membrane treatment ⁇ (pH adjustment) ⁇ Carbon dioxide removal treatment ⁇ (pH adjustment) ⁇ Ion exchange treatment
- Example 5 Membrane Separation activated sludge treatment ⁇ first stage reverse osmosis membrane treatment ⁇ (pH adjustment) ⁇ carbonic acid removal treatment ⁇ (pH adjustment) ⁇ second stage reverse osmosis membrane treatment ⁇ ion exchange treatment [FIG.
- Example 4 and Example 5 Comparing Example 3 with Examples 4 and 5, in Examples 4 and 5, since the carbonic acid removal treatment is incorporated, the regeneration exchange period of the ion exchange resin is longer than that in Example 3. .
- a carbonic acid removal treatment is incorporated between the first-stage reverse osmosis membrane treatment and the second-stage reverse osmosis membrane treatment, so that the latter stage of the second-stage reverse osmosis membrane treatment.
- the regeneration exchange regeneration period of the ion exchange resin can be extended.
- ion exchange is performed after the second-stage reverse osmosis membrane treatment by incorporating a carbonic acid removal treatment between the first-stage reverse osmosis membrane treatment and the second-stage reverse osmosis membrane treatment.
- the regeneration exchange period of the ion exchange resin in the treatment can be extended, and the total reuse cost can be kept low.
- the present invention can be used in all industrial fields where water is used because organic sewage is treated to obtain high-quality water.
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Abstract
Description
(1)有機性汚水を膜分離活性汚泥法により処理した後、その処理水を1段目逆浸透膜で処理し、さらに1段目逆浸透膜で処理して得られた透過水を2段目逆浸透膜で処理する工程を有する有機性汚水の処理方法。
(2)有機性汚水が繊維原料製造工程または繊維製造工程から排出されたものである前記有機性汚水の処理方法。
(3)2段目逆浸透膜で処理して得られた透過水をさらにイオン交換処理する前記いずれかの有機性汚水の処理方法。
(4)1段目逆浸透膜で処理して得られた透過水を炭酸除去処理してから2段目逆浸透膜で処理する前記いずれかの有機性汚水の処理方法。
(5)炭酸除去処理するための手段が、酸性条件下で曝気を行うものである前記有機性汚水の処理方法。
(6)炭酸除去処理での酸性条件がpH4以上6以下である前記有機性汚水の処理方法。
(7)活性汚泥および膜ユニットを備え膜分離活性汚泥法により有機性汚水を処理する膜分離活性汚泥処理槽と、
膜分離活性汚泥処理槽から得られた処理水を1段目逆浸透膜で処理する1段目逆浸透膜モジュールと、
1段目逆浸透膜モジュールから得られた透過水を2段目逆浸透膜で処理する2段目逆浸透膜モジュールと
を備える有機性汚水の処理装置。
(8)2段目逆浸透膜モジュールから得られた透過水をイオン交換処理するイオン交換処理装置を備える前記有機性汚水の処理装置。
(9)1段目逆浸透膜モジュールから得られた透過水を炭酸除去処理する炭酸除去処理装置を、1段目逆浸透膜モジュールと2段目逆浸透膜モジュールとの間に備える前記いずれかの有機性汚水の処理装置。
(10)炭酸除去処理装置が、酸性条件下で曝気を行う脱炭酸塔である前記有機性汚水の処理装置。
(11)酸性条件がpH4以上6以下である前記有機性汚水の処理装置。
繊維原料であるTPAの製造工程から排出される有機性汚水の処理を下記3種類の条件で実施した。
(比較例1)膜分離活性汚泥処理→1段目逆浸透膜処理[フローは図1に示すとおり。]
(実施例1)膜分離活性汚泥処理→1段目逆浸透膜処理→2段目逆浸透膜処理[フローは図2に示すとおり。]
(実施例2)膜分離活性汚泥処理→1段目逆浸透膜処理→2段目逆浸透膜処理→イオン交換処理[フローは図3に示すとおり]
被処理水の水質および試験条件を各表に示す。膜分離活性汚泥処理については表1に、逆浸透膜処理(被処理水の水質は1段目)については表2に示す。処理水量については、膜分離活性汚泥処理で100m3/day、逆浸透膜処理は1段目33 m3/day、2段目で30m3/dayとした。膜分離活性汚泥処理後の処理水のTDS(全溶解性物)は、1,000mg/Lであった。なお、表に示すCODは化学的酸素要求量、T-Nは全窒素量、T-Pは全リン量を示す。
以下の実施例3~5は、膜分離活性汚泥法で有機性汚水を処理後、1段目の逆浸透膜処理と2段目の逆浸透膜処理の間に、炭酸除去処理を行った。効果の検証は、実施例3~5のパイロット試験を実施した際のイオン交換樹脂の再生までの期間(以下「再生交換期間」)を比較することにより行った。イオン交換樹脂の再生方法としては、塩酸と水酸化ナトリウムを通水することにより行った。
(実施例4)膜分離活性汚泥処理→1段目逆浸透膜処理→2段目逆浸透膜処理→(pH調整)→炭酸除去処理→(pH調整)→イオン交換処理
(実施例5)膜分離活性汚泥処理→1段目逆浸透膜処理→(pH調整)→炭酸除去処理→(pH調整)→2段目逆浸透膜処理→イオン交換処理[図5]
実施例3~5について、比較例1および実施例1,2と同条件でパイロット試験を実施した結果、実施例3のイオン交換樹脂の再生交換期間は14日、実施例4のイオン交換樹脂の再生交換期間は28日、実施例5のイオン交換樹脂の再生交換期間は37日であった。
2:膜ユニット
3:膜分離活性汚泥処理槽
4:処理水
5:吸引ポンプ
6:1段目逆浸透膜処理原水タンク
7:送風機
8:散気ユニット
9:1段目高圧ポンプ
10:1段目逆浸透膜モジュール
11:1段目透過水
12:1段目濃縮水
13:2段目逆浸透膜処理原水タンク
14:2段目高圧ポンプ
15:2段目逆浸透膜モジュール
16:2段目透過水
17:2段目濃縮水
18:イオン交換処理装置
19:イオン交換処理水
20:脱炭酸塔
21:脱炭酸処理水タンク
Claims (11)
- 有機性汚水を膜分離活性汚泥法により処理した後、その処理水を1段目逆浸透膜で処理し、さらに1段目逆浸透膜で処理して得られた透過水を2段目逆浸透膜で処理する工程を有する有機性汚水の処理方法。
- 有機性汚水が繊維原料製造工程または繊維製造工程から排出されたものである請求項1記載の有機性汚水の処理方法。
- 2段目逆浸透膜で処理して得られた透過水をさらにイオン交換処理する請求項1または2に記載の有機性汚水の処理方法。
- 1段目逆浸透膜で処理して得られた透過水を炭酸除去処理してから2段目逆浸透膜で処理する請求項1~3いずれかに記載の有機性汚水の処理方法。
- 炭酸除去処理するための手段が、酸性条件下で曝気を行うものである請求項4に記載の有機性汚水の処理方法。
- 炭酸除去処理での酸性条件がpH4以上6以下である請求項5に記載の有機性汚水の処理方法。
- 活性汚泥および膜ユニットを備え膜分離活性汚泥法により有機性汚水を処理する膜分離活性汚泥処理槽と、
膜分離活性汚泥処理槽から得られた処理水を1段目逆浸透膜で処理する1段目逆浸透膜モジュールと、
1段目逆浸透膜モジュールから得られた透過水を2段目逆浸透膜で処理する2段目逆浸透膜モジュールと
を備える有機性汚水の処理装置。 - 2段目逆浸透膜モジュールから得られた透過水をイオン交換処理するイオン交換処理装置を備える請求項7に記載の有機性汚水の処理装置。
- 1段目逆浸透膜モジュールから得られた透過水を炭酸除去処理する炭酸除去処理装置を、1段目逆浸透膜モジュールと2段目逆浸透膜モジュールとの間に備える請求項7または8に記載の有機性汚水の処理装置。
- 炭酸除去処理装置が、酸性条件下で曝気を行う脱炭酸塔である請求項9に記載の有機性汚水の処理装置。
- 酸性条件がpH4以上6以下である請求項10に記載の有機性汚水の処理装置。
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