WO2016092620A1 - 水処理装置 - Google Patents
水処理装置 Download PDFInfo
- Publication number
- WO2016092620A1 WO2016092620A1 PCT/JP2014/082459 JP2014082459W WO2016092620A1 WO 2016092620 A1 WO2016092620 A1 WO 2016092620A1 JP 2014082459 W JP2014082459 W JP 2014082459W WO 2016092620 A1 WO2016092620 A1 WO 2016092620A1
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- Prior art keywords
- catalyst
- water
- treated
- flow path
- reverse osmosis
- Prior art date
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 209
- 238000011282 treatment Methods 0.000 title claims abstract description 43
- 239000003054 catalyst Substances 0.000 claims abstract description 159
- 239000012528 membrane Substances 0.000 claims abstract description 91
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 51
- 229910052751 metal Inorganic materials 0.000 claims abstract description 41
- 239000002184 metal Substances 0.000 claims abstract description 39
- 238000002347 injection Methods 0.000 claims abstract description 36
- 239000007924 injection Substances 0.000 claims abstract description 36
- 239000000460 chlorine Substances 0.000 claims abstract description 21
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 18
- 150000002739 metals Chemical class 0.000 claims abstract description 18
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 17
- 150000002736 metal compounds Chemical class 0.000 claims abstract description 17
- 150000004649 carbonic acid derivatives Chemical class 0.000 claims abstract description 6
- 150000003467 sulfuric acid derivatives Chemical class 0.000 claims abstract description 6
- 239000003206 sterilizing agent Substances 0.000 claims description 25
- 238000002156 mixing Methods 0.000 claims description 16
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 14
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 12
- 230000005484 gravity Effects 0.000 claims description 10
- 230000001737 promoting effect Effects 0.000 claims description 10
- 229910017052 cobalt Inorganic materials 0.000 claims description 7
- 239000010941 cobalt Substances 0.000 claims description 7
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical group [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 7
- 229910052742 iron Inorganic materials 0.000 claims description 7
- 229910021472 group 8 element Inorganic materials 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical group [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 5
- 229910052749 magnesium Inorganic materials 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- 229910052712 strontium Inorganic materials 0.000 claims description 5
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 claims description 5
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 3
- 230000001133 acceleration Effects 0.000 claims 1
- 230000000638 stimulation Effects 0.000 claims 1
- 239000003899 bactericide agent Substances 0.000 abstract description 37
- 230000000844 anti-bacterial effect Effects 0.000 abstract description 19
- 230000006866 deterioration Effects 0.000 abstract description 8
- 150000004679 hydroxides Chemical class 0.000 abstract description 3
- -1 oxides Chemical class 0.000 abstract description 2
- 239000011368 organic material Substances 0.000 abstract 1
- 238000009287 sand filtration Methods 0.000 description 60
- 239000010410 layer Substances 0.000 description 59
- 239000013535 sea water Substances 0.000 description 58
- 238000010612 desalination reaction Methods 0.000 description 49
- 238000001914 filtration Methods 0.000 description 38
- 239000005416 organic matter Substances 0.000 description 26
- 239000004576 sand Substances 0.000 description 25
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 18
- 239000003830 anthracite Substances 0.000 description 18
- 239000001301 oxygen Substances 0.000 description 17
- 229910052760 oxygen Inorganic materials 0.000 description 17
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 16
- 239000000126 substance Substances 0.000 description 15
- 238000000354 decomposition reaction Methods 0.000 description 12
- 230000000694 effects Effects 0.000 description 12
- 239000005708 Sodium hypochlorite Substances 0.000 description 11
- 230000002070 germicidal effect Effects 0.000 description 11
- 239000000463 material Substances 0.000 description 11
- 230000009471 action Effects 0.000 description 10
- 239000003002 pH adjusting agent Substances 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000011144 upstream manufacturing Methods 0.000 description 9
- 239000000701 coagulant Substances 0.000 description 8
- 239000011247 coating layer Substances 0.000 description 8
- 230000002093 peripheral effect Effects 0.000 description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 239000013505 freshwater Substances 0.000 description 6
- 230000001954 sterilising effect Effects 0.000 description 6
- 238000011001 backwashing Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000003204 osmotic effect Effects 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 229910052788 barium Inorganic materials 0.000 description 4
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 239000000645 desinfectant Substances 0.000 description 4
- 239000013067 intermediate product Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000004659 sterilization and disinfection Methods 0.000 description 4
- 239000011248 coating agent Substances 0.000 description 3
- 238000000576 coating method Methods 0.000 description 3
- 238000004080 punching Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000011230 binding agent Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
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- 244000005700 microbiome Species 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000003421 catalytic decomposition reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001804 chlorine Chemical class 0.000 description 1
- 229910001902 chlorine oxide Inorganic materials 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007634 remodeling Methods 0.000 description 1
- 235000015170 shellfish Nutrition 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000002459 sustained effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- 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
-
- 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
-
- 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
- B01D61/08—Apparatus therefor
-
- 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
-
- 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
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2311/12—Addition of chemical agents
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- 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
- B01D2311/263—Chemical reaction
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- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
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- 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
- B01D2311/2649—Filtration
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- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
-
- 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
- C02F2103/08—Seawater, e.g. for desalination
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/20—Prevention of biofouling
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Definitions
- the present invention relates to a water treatment apparatus having a reverse osmosis membrane and a chlorine-based sterilant injected into the water to be treated.
- Patent Document 1 Since the reverse osmosis membrane is oxidized and deteriorated by this bactericidal agent if a chlorine-based bactericidal agent remains in the water to be treated, sodium bisulfite (in the water to be treated is Hereinafter, a reducing agent such as SBS is injected by an injection device to reduce (detoxify) the sterilizing agent in the water to be treated (see, for example, Patent Document 1).
- Patent Document 2 does not use a reverse osmosis membrane, but adds a chlorine-based oxidizing agent to treated water containing an organic matter, passes it through a manganese-based filter material, and catalytically decomposes the organic matter by catalytic decomposition. Have been described.
- Patent Document 1 has the following problems. That is, (1) when the injection device fails and SBS is not injected into the treated water, (2) when SBS is not sufficiently stirred in the treated water even when SBS is injected into the treated water, (3) When the injection amount of SBS is insufficient relative to the amount of the bactericide, the bactericide remains in the water to be treated, and the remaining bactericide causes oxidative degradation of the reverse osmosis membrane. For this reason, it will lead to the fall of the water quality of the treated water which penetrated the reverse osmosis membrane.
- Patent Document 2 it is necessary to specially prepare a chlorine-based oxidizing agent for removing organic substances from water to be treated and equipment for adding this chlorine-based oxidizing agent. There is a problem that the initial cost and the running cost for adding the oxidizing agent are required.
- the present invention was conceived in view of the above problems, and provides a water treatment apparatus capable of preventing deterioration of a reverse osmosis membrane and adhesion of an organic substance to the reverse osmosis membrane while suppressing cost increase. With the goal.
- the water treatment apparatus of the present invention comprises a channel through which the water to be treated flows, and a sterilizing agent injecting means for injecting a chlorine-based germicide at the injection position of the channel
- a reverse osmosis membrane module is provided, which is disposed in the flow path downstream of the injection position in the flow direction of the water to be treated and has a reverse osmosis membrane.
- the metals or metal compounds described in (1), (2) and (3) below between the injection position and the reverse osmosis membrane module Kinds of metals or metal compounds are arranged as catalysts.
- Metals belonging to Group 8 elements, Group 9 elements and Group 10 elements (2) Metals belonging to Group 2 elements (3) Hydroxide which is a metal compound of each metal described in the above (1) and (2) , Oxides, carbonates and sulfates
- the flow path be provided with mixing promoting means for promoting mixing of the sterilizing agent and the water to be treated, between the injection position and the catalyst.
- a filter medium be provided between the mixing promotion means and the reverse osmosis membrane module in the flow path, and the catalyst be fixed at least to a part of the filter medium.
- the flow path be provided with a filter medium between the catalyst and the reverse osmosis membrane module.
- the flow path is provided with a filter medium between the mixing promoting means and the reverse osmosis membrane module, and the catalyst is fixed to a portion for supplying the water to be treated to the filter medium in the flow path. Is preferred.
- a filter medium is provided between the mixing promoting unit and the reverse osmosis membrane module, a mesh body is disposed above the filter medium, and the catalyst is fixed to the mesh body. Is preferred.
- the mesh body be disposed on the filter medium so as to be submerged in an aqueous layer formed by the water to be treated.
- catalyst supply means for supplying the catalyst to the flow path is provided.
- the flow path is provided with a filter medium between the mixing promotion means and the reverse osmosis membrane module, and the catalyst supply means supplies the treated water to the filter medium of the flow path.
- the catalyst is supplied.
- the catalyst preferably has a specific gravity greater than that of the filter medium.
- the metal belonging to the group 8 element is iron
- the metal belonging to the group 9 element is cobalt
- the metal belonging to the group 10 element is nickel
- the metal belonging to the group 2 element is magnesium
- Preferred are calcium, strontium and barium.
- the flow path of the water to be treated in the present invention includes not only the flow path between the intake channel and the constituent devices of the water treatment apparatus, but also the circulation portion of the water to be treated in each component. Therefore, for example, filter water also circulates the water to be treated, so the space occupied by the filter medium is also included in the flow path, and fixing the catalyst to the filter medium means arranging the catalyst in the flow path.
- the aspect in which the catalyst is disposed in the flow path is not limited to the aspect in which the catalyst is fixed to the flow path by coating or the like, but the catalyst moves in the flow path by inserting the catalyst into the flow path It also includes an aspect such as not to be completely fixed in the flow path.
- the chlorine-based bactericide injected into the water to be treated is decomposed and reacted by the action of the catalyst to generate active oxygen radicals. Therefore, the organic compounds in the water to be treated are oxidized and decomposed by the active oxygen radicals. can do.
- An organic substance can be decomposed with a simple configuration such as arranging a catalyst in a flow path by using a sterilizing agent conventionally injected into treated water for removing living organisms in water, and moreover, it is chlorine-based Since the bactericidal agent is decomposed by the action of the catalyst, the deterioration of the reverse osmosis membrane can be prevented even if the equipment for removing the conventionally used chlorine-based bactericidal agent is omitted. Therefore, the deterioration of the reverse osmosis membrane and the adhesion of the organic matter to the reverse osmosis membrane can be prevented without requiring a significant cost increase.
- FIG. 1 is a schematic diagram which shows the whole structure of the water treatment apparatus which concerns on 1st Embodiment of this invention.
- FIG. 2 is a schematic cross-sectional view showing the configuration of the sand filtration device according to the first embodiment of the present invention and the periphery thereof.
- FIG. 3A is a schematic cross-sectional view showing the configuration of the sand filtration device according to the second embodiment of the present invention and the periphery thereof, and FIG. 3B is an enlarged view of a portion A of FIG. 3A.
- FIG. 4 is a schematic cross-sectional view showing a sand filtration device according to a third embodiment of the present invention and the configuration around the sand filtration device.
- FIG. 5 is a schematic cross-sectional view showing the configuration of a sand filtration device according to a fourth embodiment of the present invention and the periphery thereof.
- FIG. 1 is a schematic diagram which shows the whole structure of the water treatment apparatus which concerns on this embodiment.
- FIG. 2 is a schematic cross-sectional view showing the configuration of the sand filtration device according to the present embodiment and the periphery thereof.
- the seawater desalination plant 1 includes, from the upstream side, a seawater supply pump 3, a mixer 6 which is an example of mixing promoting means, and a sand filter 7, tank 8, water pump 9, MCF (Micron Cartridge Filter) 10, high pressure pump 11, 1 stage reverse osmosis membrane module (hereinafter referred to as 1 stage RO membrane module) 12, 2 stage reverse osmosis membrane module (hereinafter referred to as 2 stages
- the RO membrane module 13) and the fresh water tank 14 are arranged in this order.
- Flow paths 20b to 20j through which the to-be-treated water 100b to 100g flow are respectively provided between the elements 14 to.
- the flow channels 20a to 20j are configured by piping, open-cut and the like.
- the seawater desalination plant 1 further includes a bactericide injection device 2, a pH adjuster injection device 4 and a coagulant injection device 5.
- the germicide injection device 2 injects the chlorine germicide 2a into the seawater 100a taken in from the intake channel 20a.
- the pH adjuster injection device 4 injects the pH adjuster 4 a into the water 100 b flowing through the flow path 20 b between the seawater supply pump 3 and the mixer 6.
- the coagulant injection device 5 injects the coagulant 5a into the water 100b to be treated.
- the sand filtration apparatus 7 is provided with two or more in parallel.
- the flow path of the water to be treated in the present invention refers not only to the flow paths 20b to 20j between the intake channel 20a and the component devices 3, 6 to 14, but also in the respective component devices 3, 6 to 14. It also includes the distribution section for treated water. Therefore, for example, since the to-be-processed water distribute
- the channels 20a to 20j will be referred to as the channels 20 if they are not particularly distinguished, and the treated water 100 if they are not particularly distinguished.
- the seawater desalination plant 1 will be described in detail.
- the sterilizing agent injection device 2a injects a chlorine-based sterilizing agent 2a into the seawater 100a taken in from the intake channel 20a at the injection position 2A.
- the chlorine-based germicide 2a is sodium hypochlorite (NaClO), which is hereinafter also referred to as sodium hypochlorite 2a.
- the sterilizing agent injection device 2a has a function of generating sodium hypochlorite by itself, and is provided with a seawater electrolytic cell (not shown) for generating sodium hypochlorite from seawater.
- a seawater electrolytic cell chlorine (Cl 2 ) is generated at the anode by passing a direct current to seawater containing salinity (NaCl), and caustic soda (NaOH) is generated when hydrogen (H 2 ) is generated at the cathode. Be done. Then, these chlorine and sodium hydroxide react to form sodium hypochlorite (2NaOH + Cl 2 ⁇ NaCl + NaClO + H 2 O).
- the water containing salt to be supplied to the seawater electrolytic cell may be taken from the channels 20a to 20i (preferably channels 20a to 20h having a high salinity of treated water), or a line different from the channel 20 may be used.
- Sea water may be directly taken in from the sea, or concentrated concentrated water with high salinity separated by the RO membrane modules 12 and 13 may be taken in.
- the seawater supply pump 3 takes seawater 100a from the intake water passage 20a into the seawater desalination plant 1, and treats the raw water (seawater) 100 injected with the bactericidal agent 2a in the intake water passage 20a through the flow passage 20b. Supply to equipment.
- the pH adjuster injection device 4 injects the pH adjuster (here, sulfuric acid) 4a into the treated water 100b flowing through the flow path 20b, and the coagulant injection device 5 injects the pH adjuster 4a into the treated water 100b.
- Flocculant (here, iron chloride) 5a is injected downstream of the position.
- the flocculant 5a By injecting the flocculant 5a, the suspended matter contained in the water 100b is aggregated, and the suspended matter can be efficiently trapped by the sand filtration device 7 on the downstream side. Since the aggregation effect of the aggregating agent 5a is affected by the pH of the water to be treated 100b, the pH adjuster 4a is injected to optimize the pH of the water to be treated 100b.
- the mixer 6 stirs the treated water 100b into which the bactericide 2a, the pH adjuster 4a and the coagulant 5a are injected, and mixes the water 100b, the bactericide 2a, the pH adjuster 4a and the coagulant 5a without bias. Do. Thus, the sterilizing treatment, pH adjustment and aggregation treatment of seawater can be effectively performed.
- a line mixer provided in a pipe is used.
- the sand filtration device 7 traps suspended solids aggregated by the action of the coagulant 5 a from the water 100 c having passed through the mixer 6.
- a flow path (hereinafter, also referred to as supply piping) 20 c configured by piping is inserted in the upper space 7 ⁇ / b> A inside the sand filtration device 7.
- the supply pipe 20 c is closed at its downstream end, and a plurality of injection holes penetrating the pipe wall are provided at the lower part of the circumferential surface of the insertion portion into the sand filtration device 7. Thereby, the to-be-processed water 100c which has flowed through the supply piping 20c is sprayed downward from each injection hole inside the sand filtering device 7.
- a second filtration layer 7C formed of 7c and a third filtration layer 7D formed of gravel (hereinafter also referred to as a filter medium) 7d are provided in this order in the laminated state.
- a net 7E provided transversely is provided inside the sand filtration device 7, and the third filtration layer 7D is supported from below by this net 7E.
- the second filtration layer 7C mainly filters the water to be treated 100c, and the first filtration layer 7B traps a relatively large one to reduce the load on the second filtration layer 7C.
- the third filtration layer 7D is an auxiliary filtration layer, and plays a role of supporting the filtration layers 7B and 7C from the lower side and equalizing the circulation of the water to be treated 100c and the circulation of the backwash water.
- the anthracite 7b is not limited to this, for example, one having an effective diameter of 1.2 mm and a uniformity coefficient of 1.4 or less can be used.
- the sand 7c is not limited to this, for example, those having an effective diameter of 0.6 mm and a uniformity coefficient of 1.4 or less can be used.
- the sand filtration apparatus is provided with the discharge port which is not shown in figure which discharges
- the filter media 7b, 7c and 7d forming the filtration layers 7B, 7C and 7D are selected from metals or metal compounds described in the following (1), (2) and (3) At least one metal or metal compound is supported as a catalyst.
- (1) Metals belonging to Group 8 elements, Group 9 elements or Group 10 elements (2) Metals belonging to Group 2 elements (3) Hydroxide which is a metal compound of each metal described in the above (1) and (2) , Oxides, carbonates and sulfates
- metal belonging to the group 8 element (1) iron is preferable as the metal belonging to the group 8 element (1)
- cobalt is preferable as the metal belonging to the group 9 element
- nickel is preferable as the metal belonging to the group 10 element because of easy availability and low cost.
- Metals belonging to Group 2 elements are preferably magnesium, calcium, strontium or barium
- metal compounds are hydroxides of iron, cobalt, nickel, magnesium, calcium, strontium or barium, oxidation , Carbonates or sulfates are preferred.
- the catalysts supported on the anthracite 7b, the sand 7c and the gravel 7d do not have to be the same catalyst. Therefore, for example, iron may be supported on anthracite 7b, cobalt may be supported on sand 7c, and nickel may be supported on gravel 7d.
- the first filtration layer 7B may be formed by mixing anthracite 7b supporting iron and anthracite 7b supporting cobalt.
- the method for supporting the catalyst on the filter media 7b, 7c, 7d is not limited to this, but after a binder is applied to the surface of the filter media 7b, 7c, 7d, the powdery catalyst is filtered through the binder via the filter media.
- a method of supporting on the surface of 7b, 7c, 7d is exemplified.
- the water to be treated 100c supplied from the supply piping 20c into the sand filtration device 7 temporarily forms the water layer 100C on the first filtration layer 7B, and then passes sequentially through the filtration layers 7B, 7C, and 7D.
- sodium hypochlorite 2a (NaClO) remaining in the water to be treated 100c contacts the catalyst supported by the filter media 7b, 7c, 7d, and the decomposition shown in the following reaction formula [1]
- the reaction takes place and is decomposed into salt and active oxygen radicals.
- the active oxygen radical reacts with the organic matter contained in the water to be treated 100c to oxidize and decompose the organic matter.
- the water to be treated 100c passes through the filtration layers 7B, 7C, 7D, but also sodium hypochlorite 2a and organic matter are decomposed. That is, the water to be treated 100c is treated water 100d from which the suspended matter, the sodium hypochlorite 2a and the organic matter are removed.
- the to-be-treated water 100d is sent to the downstream tank 8 as shown in FIG. 1 through the lower space 7F and the flow path 20d inside the sand filtration device 7, and is temporarily stored in the tank 8.
- the water 100d stored in the tank 8 is sucked by the water pump 9 via the flow passage 20e and supplied to the MCF 10 via the flow passage 20f.
- a cartridge filter (filter material) 10a is set inside, and removes fine suspended solids and the like that can not be trapped by the sand filtration device 7 from the water 100d to be treated.
- the high pressure pump 11 is for applying a pressure higher than the osmotic pressure to the one-stage RO membrane module 12 and the two-stage RO membrane module 13.
- the treated water 100e from which fine suspended matter has been removed by the MCF 10 is sucked by the high pressure pump 11 through the flow passage 20g, and is pressurized by the high pressure pump 11 to the first RO membrane module 12 through the flow passage 20h. It is pumped.
- a high pressure pump may be further provided between the one-stage RO membrane module 12 and the two-stage RO membrane module 13, and the high-pressure pump may apply a pressure higher than the osmotic pressure to the two-stage RO membrane module 13.
- the high pressure pump 11 is more than when applying a pressure higher than the osmotic pressure to both RO membrane modules 12 and 13 with only one high pressure pump 11. It is possible to lower the discharge pressure of the
- the one-stage RO membrane module 12 desalts the water to be treated 100e to create water, and the one-stage reverse osmosis membrane (hereinafter referred to as one-stage RO membrane) built in the pressure-resistant casing 12a and the pressure-resistant casing 12a. ) 12 b is configured.
- the treated water 100e supplied to the one-stage RO membrane 12b at a pressure higher than the osmotic pressure passes through the one-stage RO membrane 12b and is desalted into a small amount of salted treated water (hereinafter also referred to as intermediate product water) 100f.
- intermediate product water the concentrated water 101a rich in salt remaining on the upstream side of the one-stage RO membrane 12b.
- the intermediate product water 100f is supplied to the two-stage RO membrane module 13 through the flow path 20i, and the concentrated water 101a is supplied to the seawater electric field layer of the sterilizing agent injection device 2 and used for generating sodium hypochlorite 2a. Or used for backwashing of sand filter 7 or MCF 10.
- the two-stage RO membrane module 13 further desalts the intermediate product water 100f, and the pressure-resistant casing 13a and a two-stage reverse osmosis membrane (hereinafter referred to as a two-stage RO membrane) 13b built in the pressure-resistant casing 13a. It is configured to be equipped.
- the intermediate product water 100f supplied to the two-stage RO membrane 13b at a pressure higher than the osmotic pressure passes through the two-stage RO membrane 13b and is 100 g of treated water (hereinafter referred to as fresh water) which is a final product water containing no salt. It is separated into concentrated water 101b containing salt remaining on the upstream side of the two-stage RO membrane 12b.
- 100 g of fresh water is supplied and stored in the fresh water tank 14 via the flow path 20 j, and the concentrated water 101 b is supplied to the seawater electric field layer of the bactericide injection device 2 and used for the production of sodium hypochlorite 2a Or, it is used for backwashing of sand filtration device 7 or MCF 10.
- the concentrated water 101 b is supplied to the seawater electric field layer of the bactericide injection device 2 and used for the production of sodium hypochlorite 2a Or, it is used for backwashing of sand filtration device 7 or MCF 10.
- only one RO membrane module may be used.
- the bactericidal agent 2a remaining in the treated water 100 causes a decomposition reaction by the action of the filter media 7b, 7c and 7d carrying a catalyst, and the organic substances are decomposed by active oxygen radicals generated by this decomposition reaction.
- Ru That is, in the process of passing through the sand filter 7, the water to be treated 100 simultaneously removes suspended solids, organic matter, and the sterilizing agent 2 a.
- the treated water 100 from which the suspended matter, the organic matter and the bactericidal agent 2a have been removed is supplied from the tank 8 to the MCF 10 by the water supply pump 9, and the suspended matter is removed by the MCF 10.
- the water 100 to be treated is further pressurized by the high-pressure pump 11 and supplied to the RO membrane modules 12 and 13, desalted and desalinated by the RO membrane modules 12 and 13, and stored in the fresh water tank 14.
- the sterilizing agent 2a injected into the treated water 100 causes a decomposition reaction by the action of the catalyst supported on the filter media 7b, 7c, 7d of the sand filtration device 7.
- active oxygen radicals are generated, and the organic substances in the water 100 to be treated can be oxidized and decomposed by the active oxygen radicals. That is, the removal of the bactericide 2a and the removal of the organic matter can be performed together.
- the RO films 12b and 13b can be prevented from deterioration due to the bactericide 2a, and organic substances can be removed by using the bactericide 2a conventionally injected into the water 100 to be treated to remove marine organisms.
- the organic matter can be removed only by a simple configuration in which the catalyst is supported on the filter medium. Therefore, the deterioration of the reverse osmosis membrane and the adhesion of the organic matter to the reverse osmosis membrane can be prevented while suppressing the cost increase.
- active oxygen radicals have a sterilizing effect and can suppress the reproduction of marine organisms. Furthermore, since deterioration of the RO films 12b and 13b due to the chlorine-based bactericide 2a and a reduction in the throughput of the RO films 12b and 13b due to the adhesion of organic substances can be prevented, the interval until the RO films 12b and 13b are replaced with new one The running cost can be reduced.
- the mixer 6 is disposed between the injection position 2A of the sterilizing agent 2a and the sand filtration device 7. Thereby, after the water to be treated 100b is mixed with the sterilizing agent 2a by the mixer 6 to effectively sterilize the water to be treated 100b, sand filtration is performed using the sterilizing agent 2a remaining in the water to be treated 100c after sterilization.
- the apparatus 7 can decompose the bactericide 2a and thus the organic matter. That is, the sterilization and the decomposition of the organic matter, which are the original purpose of injecting the sterilizing agent 2a, can be compatible.
- the sterilizing agent 2a can be effectively decomposed by the catalyst. That is, since the water to be treated 100c passes through the filter media 7b, 7c, 7d in a relatively long time, the sterilizing agent 2a remaining in the water to be treated 100c and the catalyst loaded with the filter media 7b, 7c, 7d The contact time can be extended, and the catalyst can effectively decompose the bactericide 2a and hence the organic matter.
- the MCF 10 is disposed between the sand filtration unit 7 and the one-stage RO membrane module 12, even if the catalyst is peeled off from the filter media 7b, 7c, 7d of the sand filtration unit 7, the peeled catalyst is 1 Before reaching the stage RO membrane modules 12 and 13, they are trapped by the MCF 10. Also, for example, even if the catalyst is exfoliated from the anthracite 7b, the anthracite 7b downstream of the anthracite 7b from which the catalyst exfoliated, sand 7c, or the catalyst exfoliated by the gravel 7d is trapped (that is, the exfoliated catalyst Are also trapped inside the sand filtration device 7). Therefore, it is possible to prevent the peeled catalyst from adhering to the one-stage RO membrane module 12 and lowering the processing performance of the one-stage RO membrane module 12.
- the catalyst is selected from iron, cobalt, nickel, magnesium, calcium, strontium, barium, and hydroxides, oxides, carbonates and sulfates of these metals, these metals or metal compounds Is easy to obtain and inexpensive, so the cost increase associated with the use of the catalyst can be suppressed.
- the catalyst is supported on each of the filter media of anthracite 7b, sand 7c and gravel 7d of the sand filtration device 7, but the catalyst is at least a part of these filter media 7b, 7c and 7d. It is sufficient if it is carried. Therefore, for example, among the filter media 7b, 7c and 7d, the catalyst may be supported only on the anthracite 7b, the catalyst may be supported only on the sand 7c, or the catalyst may be supported only on the gravel 7d. good.
- the catalyst may be supported only on a part of anthracite 7b forming the first filtration layer, or on a part of sand 7c of the sand 7c forming the second filtration layer.
- the catalyst may be supported only on a part of the gravel 7d of the gravel 7d that forms the third filtration layer.
- the catalyst is supported on the filter media 7b, 7c, 7d of the sand filtration device 7.
- the catalyst may be supported on the cartridge filter 10 a of the MCF 10.
- FIG. 3A is a schematic cross-sectional view showing the configuration of the sand filtration device according to the second embodiment of the present invention and the periphery thereof
- FIG. 3B is an enlarged view of a portion A of FIG. 3A.
- the catalyst is fixed to the filter media 7b, 7c and 7d inside the sand filtration device 7, whereas in the seawater desalination plant of the present embodiment, the catalyst is It changes to filter media 7b, 7c, and 7d, and is fixing to the inner skin of supply piping 20ca which supplies treated water to sand filtration device 17.
- supply piping 20ca and sand filtration apparatus 17 which concern on this embodiment are demonstrated in detail.
- the supply piping 20ca is provided with a catalyst coating layer 20cb on the inner peripheral surface thereof.
- the catalyst coating layer 20cb is formed over the entire circumference of the inner peripheral surface of the supply pipe 20ca and is formed over the entire length.
- the catalyst contained in the catalyst coating layer 20cb causes a decomposition reaction to occur in the sterilizing agent 2a contained in the treated water 100c flowing through the supply pipe 20ca, and generates active oxygen radicals.
- the active oxygen radical can decompose the organic matter contained in the water to be treated 100c.
- the metals or metal compounds that can be contained as a catalyst in the catalyst coating layer 20cb are the same as in the first embodiment.
- the to-be-processed water 100c which passed supply piping 20ca is set to the to-be-processed water 100ca from which the disinfectant 2a and the organic substance were removed.
- the sand filtration apparatus 17 includes, from the top, a first filtration layer 17B formed of anthracite (hereinafter, also referred to as filter material) 17b, a second filtration layer 17C formed of sand (hereinafter, also referred to as filter material) 17c, and gravel
- the third filtration layer 17D formed of the filter material 17d is also provided in the stacked state in this order.
- a net 7E is provided below the interior of the sand filtration device 17 so as to cover the entire cross section of the sand filtration device 17, and the third filtration layer 17D is supported by the net 7E from below.
- the filter media 17b, 17c, and 17d do not carry a catalyst.
- the filter media 17b, 17c and 17d are the same as the filter media 7b, 7c and 7d of the first embodiment except that the catalyst is not supported, and the filter media 17b, 17c and 17d are the filter media 17b, 17c and 17d.
- the filter layers 7B, 7C, and 7D of the first embodiment except that the catalyst does not support the catalyst.
- the other structure of the seawater desalination plant is the same as that of 1st Embodiment, description is abbreviate
- the desalination process according to the present embodiment will be described with reference to FIGS. 3A and 3B.
- the to-be-processed water 100c which flows through the inside of supply piping 20ca contains bactericidal agent 2a, organic substance, and the condensed turbid substance.
- the bactericidal agent 2a is decomposed by the action of the catalyst coating layer 20cb on the inner circumferential surface of the supply pipe 20ca, and the organic matter is decomposed by active oxygen radicals generated during the decomposition of the bactericidal agent 2a.
- the to-be-processed water 100c turns into the to-be-processed water 100ca from which bactericidal agent 2a and organic substance were removed in the middle of flowing through the inside of supply piping 20ca.
- the water to be treated 100ca forms an aqueous layer 100CA once on the filtration layer 17B, and then passes sequentially through the filtration layers 17B, 17C, and 17D, and the suspended matter condensed at this time is trapped, and the sterilizing agent 2a, organic matter And it becomes 100 d of treated water from which the condensed suspended matter was removed.
- the other desalination process is the same as that of the first embodiment, so the description will be omitted.
- the catalyst coating layer 20cb is formed on the entire circumference of the inner peripheral surface of the supply pipe 20ca and is formed over the entire length, but the organic substance and the sterilizing agent 2a contained in the water to be treated 100c are effectively If it can be disassembled, it may be formed only on a part of the inner circumferential surface of the supply pipe 20ca.
- the catalyst coating layer 20cb may be formed only on the lower half of the inner circumferential surface of the supply pipe 20ca or only on the portion disposed inside the sand filter 7.
- 3-1 Composition of seawater desalination plant
- the catalyst is coated on the inner peripheral surface of the supply pipe 20ca for supplying the water to be treated to the sand filtration device 17;
- a catalyst is changed to the inner peripheral surface of the supply piping 20c, and is coated on the reticulated body 27a provided in the sand filtration apparatus 27.
- supply piping 20c and sand filtration device 27 concerning this embodiment are explained.
- the feed pipe 20c and the sand filtration device 27 shown in FIG. 4 are used in place of the feed pipe 20ca and the sand filtration device 17 of the second embodiment shown in FIGS. 3A and 3B in the seawater desalination plant of the second embodiment. Be done.
- the passing amount per unit time of the water to be treated 100c in the filtration layers 17B, 17C, 17D is small. For this reason, the to-be-processed water 100c supplied from the flow path 20c in the sand filtration apparatus 27 once forms the water layer 100C on the 1st filtration layer 17B.
- the net-like body 27a is disposed so as to be submerged in the water layer 100C and at a predetermined distance above the first filtration layer 17B, and is disposed so as to cover the entire cross section of the sand filtration device 27.
- the net-like body 27a is formed in a grid shape by wires made of metal, plastic or the like, and the entire surface thereof is coated with a catalyst.
- This catalyst causes a decomposition reaction to occur in the bactericide 2a contained in the aqueous layer 100C (water to be treated 100c) to generate active oxygen radicals.
- the metals or metal compounds that can be used as a catalyst are the same as in the first and second embodiments.
- the height of the water layer 100C is determined by the supply amount of the water to be treated 100c per unit time, the passage amount of the water to be treated 100c in the filtration layers 17B, 17C, and 17D per unit time, and the cross sectional area of the upper space 7A. It can be predicted in advance based on Based on the predicted height of the water layer 100C, the installation position of the mesh body 27a can be set to a position where the water layer 100C is submerged.
- the desalination process according to the present embodiment will be described with reference to FIG.
- the to-be-processed water 100c which forms the water layer 100C contains the disinfectant 2a, the organic substance, and the condensed suspended matter.
- the germicide 2a is decomposed by the action of a catalyst coated on the surface of the network 27a, and the organic matter is decomposed by active oxygen radicals generated during the decomposition of the germicide 2a. That is, the bactericidal agent 2a and the organic matter are removed from the water layer 100C of the water to be treated 100c.
- the treated water from which the bactericidal agent 2a and the organic matter have been removed is filtered from suspended matter when passing through the filter layers 17B, 17C, 17D, and the bactericidal agent 2a, the treated water from which the organic matter and the suspended matter are removed and 100d. Become.
- the other desalination process is the same as that of each of the above-described embodiments, and hence the description thereof is omitted.
- the following effects can be obtained. That is, since the reticulated body 27a coated with the catalyst is only provided as compared with the case where the catalyst is supported on the fine filter media 7b, 7c and 7d as in the first embodiment, the catalyst is fixed in the flow path of the water to be treated. It is easy. In addition, in order to obtain the same configuration as that of the seawater desalination plant of this embodiment by modifying the existing seawater desalination plant, it is only necessary to add the reticulated body 27a, so that remodeling is easy. There is also an advantage.
- the contact time between the catalyst coated on the reticulated body 27a and the water 100c forming the aqueous layer 100C can be long, and the action of the catalyst Removal of the bactericide 2a and the organic matter can be effectively performed.
- the reticulated body 27a is disposed above the filtration layer 17B at a predetermined interval. However, the reticulated body 27a may be placed on the upper surface of the filtration layer 17B.
- the catalyst is coated on the entire surface of the reticulated body 27a, but a part of the surface of the reticulated body 27a may be coated (or except for a part of the surface of the reticulated body 27a) .
- the net-like body 27a is formed in a lattice shape (that is, a configuration in which the wires aligned in one direction cross the wires aligned in the other direction) using the wires. It may be arranged side by side.
- the net-like body 27a is formed using a wire.
- the net-like body 27a may be formed of a punching metal in which a plurality of openings are provided in a plate material.
- the net-like body in the present invention includes such a punching metal shape.
- the reticulated body 27a is submerged in the water layer 100C, but the reticulated body 27a may be disposed above the water layer 100C.
- the opening area of the netting body 27a is made smaller than that in the water layer 100C, for example, by forming the netting body 27a in a punching metal shape so that the contact time between the netting body 27a and the treated water 100c is long.
- the water layer 100C is formed on the reticulated body 27a.
- FIG. 5 is a schematic cross-sectional view showing the configuration of a sand filtration device according to a fourth embodiment of the present invention and the periphery thereof.
- the catalyst is coated on the inner peripheral surface of the supply pipe 20ca for supplying the water to be treated to the sand filtration device 17, whereas in the seawater desalination plant of the present embodiment, the powdery or granular catalyst is supplied to the inside of the sand filter 17 through the supply pipe 20c.
- the sand filtration apparatus 17 which concerns on this embodiment, and the structure of the periphery of it are demonstrated.
- the sand filtration apparatus 17 according to the present embodiment shown in FIG. 5 has the same configuration as the sand filtration apparatus 17 of the second embodiment shown in FIG. 3A, but the supply piping of the water 100C to be treated outside the sand filtration apparatus 17 A catalyst is supplied from a catalyst supply device (catalyst supply means) 30 to 20c.
- This catalyst causes a decomposition reaction to occur in the bactericidal agent 2a contained in the water to be treated 100c to generate active oxygen radicals as in the above embodiments, and metals or metal compounds that can be used as a catalyst are also each of the above-mentioned respective embodiments. It is the same as the embodiment.
- the catalyst supply device 30, as shown in FIG. 5, includes a catalyst storage portion 31 in which a powdery or granular catalyst is stored, a pipe 32, and a valve 33 provided in the middle of the pipe 32. ing.
- the catalyst storage portion 31 is disposed vertically above the supply pipe 20 c, and an internal space for storing the catalyst is connected in communication with the inside of the supply pipe 20 c via the pipe 32.
- the valve 33 When the valve 33 is opened, the catalyst in the catalyst storage portion 31 falls in the pipe 32 by gravity and is supplied into the supply pipe 20c. There is.
- the catalyst supplied into the supply pipe 20c is supplied into the sand filter 17 together with the water 100c flowing through the supply pipe 20c.
- Most of the catalyst is disposed in the sand filtration apparatus 17 in a form that diffuses or deposits on the upper surface of the first filtration layer 17B in the aqueous layer 100C, and a part thereof is in each of the filtration layers 17B, 17C, 17D. It will be arrange
- the valve 33 may be either of a type in which the opening and closing operation is manually performed or a type in which the operation is performed automatically. Further, the valve 33 may be either of a type in which the opening degree can be adjusted continuously or stepwise, or a type in which the valve can only be operated fully closed or fully opened (that is, an open / close valve). Further, the supply of the catalyst may be appropriately performed as needed, may be intermittently performed at predetermined time intervals, or may be performed continuously at all times.
- the catalyst one having a specific gravity larger than the specific gravity (1.40 to 1.60 g / cm 3 ) of the anthracite 17b is used. This is to prevent the catalyst from being discharged from the sand filter 17 together with the backwash water when the sand filter 17 is backwashed. That is, since the water pressure of the backwash water is set to a pressure at which the anthracite 17b having the smallest specific gravity among the filter media 17b, 17c, 17d is not discharged together with the backwash water, the catalyst having a heavier specific gravity than the anthracite 17b is used. If used, the catalyst is not discharged from the sand filter 17 together with the backwash water.
- the other configuration is the same as that of the seawater desalination plant of the second embodiment, and thus the description thereof is omitted.
- the desalination process according to the present embodiment will be described with reference to FIG.
- the bactericidal agent 2a contained in the water to be treated 100c is decomposed by the action of the catalyst supplied from the catalyst supply device 30 into the sand filter 17.
- the organic matter contained in the water to be treated 100c is decomposed as a result of the bactericidal agent 2a. It is decomposed by active oxygen radicals generated during the
- the other desalination process is the same as that of each embodiment described above, and therefore the description thereof is omitted.
- the catalyst since the catalyst is supplied to the feed pipe 20c for supplying the water to be treated 100c to the sand filtration device 17, the supplied catalyst passes through the sand filtration device 17 due to the presence of the filter media 17b, 17c, 17d and the RO membrane It does not reach 12b and 13b. Accordingly, it is possible to prevent the performance of the RO films 12b and 13b from being degraded by the catalyst adhering to the RO films 12b and 13b. Furthermore, since the specific gravity of the catalyst is heavier than the specific gravity of the anthracite 17b, the catalyst is not discharged from the sand filter 17 together with the backwash water at the time of backwashing, so unnecessary discharge of the catalyst is prevented and running The cost increase can be suppressed.
- the catalyst supply means of the present invention is constituted by the catalyst supply device 30 shown in FIG. 5, but the configuration of the catalyst supply means of the present invention is not limited to this catalyst supply device 30.
- the catalyst storage unit 31 can be omitted from the catalyst supply device 30 (that is, only a seat for supplying the catalyst may be provided on the supply pipe 20c).
- the valve 33 may be opened and then the catalyst may be manually introduced into the pipe 33.
- the catalyst in the catalyst storage portion 31 is dropped by gravity and supplied to the supply pipe 20c.
- the catalyst supply device 30 may be configured to pressure-feed the pressure fluid and supply the same to the supply pipe 20c.
- the location of the catalyst in the water treatment apparatus of the present invention is not limited to that of the above embodiments, and the flow between the injection position 2A of the bactericidal agent 2a to the water to be treated and the one-stage RO membrane 12b It is good if it is a road. However, if the arrangement location of the catalyst is too close to the injection position 2A of the sterilizing agent 2a, the sterilizing agent 2a is decomposed before sterilization of the water 100a to be treated is not sufficiently performed. Therefore, in anticipation of a distance where sterilization of the water to be treated 100a is sufficiently performed, it is preferable to install the catalyst at a position separated from the injection position 2A of the germicide 2a than this distance.
- the catalyst it is preferable to install the catalyst after mixing of the water to be treated 100a and the sterilizing agent 2a by the mixer 6 (that is, downstream of the mixer 6).
- the mixer 6 that is, downstream of the mixer 6
- the catalyst adheres to the RO films 12b and 13b there is a possibility that the processing performance of the RO films 12b and 13b may be reduced. Therefore, even if the catalyst peels off and flows to the downstream side It is preferable to place the catalyst upstream of the MCF 10 so as to be removed before reaching the RO membranes 12b, 13b.
- the inner surface of the side wall and the inner surface of the bottom wall of the casing for housing the net 7E of the sand filtering devices 7, 17 and 27, the inner wall surface of the tank 8, etc. are exemplified.
- the catalyst may be disposed in the flow path by any one of fixing the position by coating or the like, and moving with the flow in the flow path.
- each said embodiment may be combined suitably, for example, all the said each embodiment may be combined. That is, the filter media 7b, 7c, 7d supporting the catalyst are used, the catalyst is fixed in the flow path 20, the reticulated body 27a supporting the catalyst is disposed in the water layer formed on the filter media 7b, and the catalyst is supplied
- the apparatus 30 may be provided to supply the catalyst to the flow path 20.
- the water treatment apparatus is described as a seawater desalination plant that desalinates and desalinates seawater using an RO membrane, but the water treatment apparatus of the present invention is not limited to this.
- it can be applied to a water treatment apparatus that desalinates and desalinates lake water of salt lake with an RO membrane, and can also be applied to a water treatment apparatus that separates impurities from water of rivers and lakes with an RO membrane.
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Abstract
Description
特許文献2には、逆浸透膜を使用するものではないが、有機物を含有する被処理水に塩素系酸化剤を添加し、マンガン系濾過材に通水して有機物を接触酸化分解する技術が記載されている。
つまり、(1)注入装置が故障して被処理水にSBSが注入されない場合、(2)被処理水にSBSを注入してもSBSが被処理水内で十分に撹拌されない場合、(3)SBSの注入量が殺菌剤の量に対して不十分である場合には、被処理水中に殺菌剤が残留し、この残留した殺菌剤によって逆浸透膜が酸化劣化してしまう。このため、逆浸透膜を透過した被処理水の水質の低下をまねいてしまう。
さらには、SBSを注入するためのイニシャルコスト及びランニングコストが掛かるという課題がある。
前記流路内には、前記注入位置と前記逆浸透膜モジュールとの間において、以下の(1),(2)及び(3)に記載された金属又は金属化合物の中から選択された少なくとも1種類の金属又は金属化合物が、触媒として配置される。
(1)8族元素,9族元素及び10族元素に属する金属
(2)2族元素に属する金属
(3)前記(1),(2)に記載された各金属の金属化合物である水酸化物,酸化物,炭酸塩及び硫酸塩
[7]前記網状体が、前記ろ材の上に前記被処理水によって形成される水層に水没するように配置されることが好ましい。
[9]前記流路には、前記混合促進手段と前記逆浸透膜モジュールとの間にろ材が備えられ、前記触媒供給手段により、前記流路の前記ろ材へ前記被処理水を供給する部分に、前記触媒を供給することが好ましい。
[10]前記触媒は、前記ろ材よりも比重が重いことが好ましい。
また、流路内に触媒を配置する態様としては、コーティングなどにより触媒を流路に固定する態様に限らず、流路に触媒を投入して触媒が流路内で移動するような、触媒が完全に流路に固定されないよう態様なども含むものである。
水中生物の除去のために従来から被処理水に注入されていた殺菌剤を利用して、流路内に触媒を配置するといった簡素な構成で有機物を分解することができ、しかも、塩素系の殺菌剤が触媒の作用により分解するので従来使用されていた塩素系の殺菌剤を除去するための設備を省略しても逆浸透膜の劣化を防止することができる。
したがって、大幅なコストアップを要することなく逆浸透膜の劣化及び逆浸透膜への有機物の付着を防止できる。
また、以下の説明において、上流,下流といった場合には被処理水の流通方向における上流,下流を意味するものとする。
本発明の水処理装置の第1実施形態としての海水淡水化プラント1について、図1及び図2を用いて説明する。
図1は、本実施形態に係る水処理装置の全体構成を示す模式図である。
図2は、本実施形態に係る砂ろ過装置及びその周辺の構成を示す模式的な断面図である。
先ず、海水淡水化プラント1の全体構成を説明すると、海水淡水化プラント1は、図1に示すように、上流側から、海水供給ポンプ3,混合促進手段の一例であるミキサ6,砂ろ過装置7,タンク8,送水ポンプ9,MCF(Micron Cartridge Filter)10,高圧ポンプ11,1段逆浸透膜モジュール(以下、1段RO膜モジュールという)12,2段逆浸透膜モジュール(以下、2段RO膜モジュールという)13及び淡水タンク14が、この順に並べられて構成されている。
海水供給ポンプ3の上流側には、被処理水の原水である海水(以下、被処理水ともいう)100aを取り込む流路(以下、取水路ともいう)20aが備えられ、構成機器3,6~14の各相互間には、被処理水100b~100gが流通する流路20b~20jがそれぞれ備えられている。流路20a~20jは配管や開渠などにより構成されている。
なお、図1では簡略化して示しているが、砂ろ過装置7は並列に複数設けられている。砂ろ過装置7を並列に複数設けることで、一つの砂ろ過装置7が逆洗やメンテナンスのため使用できないときでも、他の砂ろ過装置7に切り替えることで海水淡水化プラント1の運転を継続して行えるようにしている。
以下、流路20a~20jを特に区別しない場合には流路20といい、被処理水100a~100gを特に区別しない場合には被処理水100という。
殺菌剤注入装置2aは、取水路20aより取り込まれた海水100aに、注入位置2Aにおいて塩素系の殺菌剤2aを注入する。これにより、海水100aに含まれる微生物や貝類などの海洋生物が、流路20や各構成機器3,6~14の流通部に付着してこれらを閉塞させてしまうことが防止される。塩素系の殺菌剤2aは、ここでは次亜塩素酸ソーダ(NaClO)であり、以下、次亜塩素酸ソーダ2aとも表記する。
海水電解槽に供給する塩分を含む水は、流路20a~20i(処理水の塩分濃度の高い流路20a~20hが好ましい)から取り込むようにしても良いし、流路20とは別ラインにより海から海水を直接取り込むようにしても良いし、或いは、RO膜モジュール12,13により分離された塩分の濃い濃縮水を取り込むようにしても良い。
pH調整剤注入装置4は、流路20bを流通する被処理水100bにpH調整剤(ここでは硫酸)4aを注入し、凝集剤注入装置5は、被処理水100bにpH調整剤4aの注入位置よりも下流側で凝集剤(ここでは塩化鉄)5aを注入する。凝集剤5aを注入することにより、被処理水100bに含まれる濁質を凝集させて、その下流側の砂ろ過装置7により濁質を効率的にトラップできるようにしている。凝集剤5aによる凝集効果は、被処理水100bのpHに影響を受けるので、pH調整剤4aを注入して被処理水100bのpHを最適化している。
砂ろ過装置7は、図2に示すように、配管により構成される流路(以下、供給配管ともいう)20cが、砂ろ過装置7の内部の上部空間7Aに挿入されている。この供給配管20cは、その下流端が閉塞されるとともに、砂ろ過装置7内への挿入部の円周面下部には、配管壁を貫通する噴射孔が複数設けられている。これにより、供給配管20cを流れてきた被処理水100cは、砂ろ過装置7の内部において各噴射孔から下方に向けて噴射される。
第2ろ過層7Cは、主体的に被処理水100cのろ過を行い、第1ろ過層7Bは比較的大きなものをトラップして第2ろ過層7Cの負担を軽減するものである。第3ろ過層7Dは、補助的なろ過層であり、ろ過層7B,7Cを下方から支持するとともに被処理水100cの流通や逆洗水の流通を均等にする役割を担っている。
砂7cは、これに限定されるものではないが、例えば有効径が0.6mmであって均等係数が1.4以下のものを使用することができる。
なお、砂ろ過装置には、逆洗時に逆洗水を排出する図示しない排出口が設けられている。
(1)8族元素,9族元素又は10族元素に属する金属
(2)2族元素に属する金属
(3)前記(1),(2)に記載された各金属の金属化合物である水酸化物,酸化物,炭酸塩及び硫酸塩
供給配管20cから砂ろ過装置7内に供給された被処理水100cは、第1ろ過層7Bの上で水層100Cを一旦形成したのち、各ろ過層7B,7C,7Dを順次通過する。この過程で、被処理水100cに残留する次亜塩素酸ソーダ2a(NaClO)は、各ろ材7b,7c,7dが担持している触媒と接触して、下の反応式[1]に示す分解反応を起こし、塩分と活性酸素ラジカルに分解される。
NaClO+CAT → NaCl+(O)〔CAT:触媒,(O):活性酸素ラジカル〕 …[1]
この活性酸素ラジカルが、被処理水100cに含まれる有機物と反応して、この有機物を酸化分解する。
MCF10は、内部にカートリッジフィルタ(ろ材)10aがセットされており、被処理水100dから、砂ろ過装置7によりトラップできなかった微細な濁質などを除去する。
なお、1段RO膜モジュール12と2段RO膜モジュール13との間にさらに高圧ポンプを設けて、この高圧ポンプにより2段RO膜モジュール13に浸透圧以上の圧力をかけるようにしても良い。このようにRO膜モジュール12,13の相互間に高圧ポンプを設けることで、高圧ポンプ11の一台だけで両RO膜モジュール12,13に浸透圧以上の圧力をかける場合よりも、高圧ポンプ11の吐出圧力を低くすることが可能となる。
浸透圧以上の圧力で1段RO膜12bに供給された被処理水100eは、1段RO膜12bを通過して脱塩された塩分の少ない被処理水(以下、中間生成水ともいう)100fと、1段RO膜12bの上流側に残留した塩分の多い濃縮水101aとに分離される。
中間生成水100fは、流路20iを介して2段RO膜モジュール13へ供給され、濃縮水101aは、殺菌剤注入装置2の海水電界層に供給されて次亜塩素酸ソーダ2aの生成に使用されるか、或いは、砂ろ過装置7やMCF10の逆洗に使用される。
浸透圧以上の圧力で2段RO膜13bに供給された中間生成水100fは、2段RO膜13bを通過して塩分を含まない最終生成水である被処理水(以下、淡水という)100gと、2段RO膜12bの上流側に残留した塩分を含む濃縮水101bとに分離される。
淡水100gは、流路20jを介して淡水タンク14に供給されて貯留され、濃縮水101bは、殺菌剤注入装置2の海水電界層に供給されて次亜塩素酸ソーダ2aの生成に使用されるか、或いは、砂ろ過装置7やMCF10の逆洗に使用される。
なお、一つのRO膜モジュールによる脱塩により淡水が得られるのであれば、RO膜モジュールは一段だけでも良い。
本実施形態の海水淡水化プラント1による海水の淡水化処理を図1及び図2を参照して説明する。
先ず、被処理水100に塩素系の殺菌剤である殺菌剤2a,pH調整剤4a及び凝集剤5aが注入された後、被処理水100はミキサ6により混合される。これにより、被処理水100が殺菌されると共に被処理水100に含まれる濁質が凝縮(フロック化)される。
ついで被処理水100は、凝縮した濁質が砂ろ過装置7によりろ過される。同時に、触媒を担持したろ材7b,7c,7dの作用により、被処理水100中に残留していた殺菌剤2aが分解反応を起こすとともに、この分解反応により発生した活性酸素ラジカルにより有機物が分解される。すなわち、被処理水100は、砂ろ過装置7を通過する過程で、濁質,有機物及び殺菌剤2aが同時に除去される。
第1実施形態の海水淡水化プラント1によれば、被処理水100に注入される殺菌剤2aが、砂ろ過装置7のろ材7b,7c,7dに担持された触媒の作用により分解反応を起こして、活性酸素ラジカルが発生し、この活性酸素ラジカルにより被処理水100中の有機物を酸化分解することができる。つまり、殺菌剤2aの除去と有機物の除去とを共に行うことができる。
これにより、殺菌剤2aによるRO膜12b,13bの劣化を防止できるとともに、海洋生物の除去のために従来から被処理水100に注入されていた殺菌剤2aを利用して有機物も除去することができ、さらには、従来技術で使用されていた塩素系の殺菌剤を除去するためのSBS注入設備を省略することができる。また、触媒をろ材に担持させるといった簡素な構成だけで有機物を除去することができる。
したがって、コストアップを抑えながら逆浸透膜の劣化及び逆浸透膜への有機物の付着を防止できる。
さらに、塩素系の殺菌剤2aによるRO膜12b,13bの劣化及び有機物の付着によるRO膜12b,13bの処理量の低下を防止できるので、RO膜12b,13bを新しいものに交換するまでのインターバルを長くすることができ、ランニングコストを抑えることができる。
上記の第1実施形態では、砂ろ過装置7のアンスラサイト7b,砂7c及び砂利7dの各ろ材にそれぞれ触媒を担持させたが、触媒は、少なくともこれらのろ材7b,7c,7dの一部に担持されていれば良い。したがって、例えば、ろ材7b,7c,7dの内、アンスラサイト7bにのみ触媒を担持させても良いし、砂7cにのみ触媒を担持させても良いし、砂利7dにのみ触媒を担持させても良い。又は、第1ろ過層を形成するアンスラサイト7bの一部のアンスラサイト7bにのみ触媒を担持させても良いし、第2ろ過層を形成する砂7cの一部の砂7cにのみ触媒を担持させても良いし、第3ろ過層を形成する砂利7dの一部の砂利7dにのみ触媒を担持させても良い。
上記の第1実施形態では、砂ろ過装置7のろ材7b,7c,7dに触媒を担持させたが、ろ材7b,7c,7dに触媒を担持させる替わりに、又は、ろ材7b,7c,7dに触媒を担持させることに加えて、MCF10のカートリッジフィルタ10aに触媒を担持させるようにしても良い。
本発明の水処理装置の第2実施形態として海水淡水化プラントについて、図3A及び図3Bを参照して説明する。なお、第1実施形態と同一要素については同一の符号を付し、その説明を省略する。
図3Aは、本発明の第2実施形態に係る砂ろ過装置及びその周辺の構成を示す模式的な断面図であり、図3Bは図3AのA部拡大図である。
第1実施形態の海水淡水化プラント1では、触媒を、砂ろ過装置7の内部のろ材7b,7c,7dに固定していたのに対し、本実施形態の海水淡水化プラントでは、触媒を、ろ材7b,7c,7dに替えて、砂ろ過装置17に被処理水を供給する供給配管20caの内周面に固定している。
以下、本実施形態に係る供給配管20ca及び砂ろ過装置17について詳しく説明する。
図3A及び図3Bに示す供給配管20ca及び砂ろ過装置17は、図1及び図2に示す第1実施形態の海水淡水化プラント1における供給配管20c及び砂ろ過装置7に替えて使用される。
供給配管20caには、その内周面に触媒コーティング層20cbが備えられている。触媒コーティング層20cbは、ここでは供給配管20caの内周面の全周に形成され且つ全長に渡って形成されている。
供給配管20caを通過した被処理水100cは、殺菌剤2a及び有機物の除去された被処理水100caとされる。
ろ材17b,17c,17dは、第1実施形態のろ材7b,7c,7dとは異なり触媒が担持されていない。触媒を担持していない以外は、ろ材17b,17c,17dは、第1実施形態のろ材7b,7c,7dと同じであり、各ろ過層17B,17C,17Dは、そのろ材17b,17c,17dが触媒を担持していない以外は、第1実施形態の各ろ過層7B,7C,7Dと同じなので説明を省略する。
また、海水淡水化プラントのその他の構成は、第1実施形態と同様なので説明を省略する。
本実施形態に係る淡水化処理を、図3A及び図3Bを参照して説明する。
供給配管20ca内を流れる被処理水100cは、殺菌剤2a,有機物及び凝縮した濁質を含んでいる。殺菌剤2aは、供給配管20ca内周面の触媒コーティング層20cbの作用により分解され、有機物は、殺菌剤2aの分解の際に発生した活性酸素ラジカルにより分解される。すなわち、被処理水100cは、供給配管20ca内を流れる最中に殺菌剤2a及び有機物を除去された被処理水100caとなる。被処理水100caは、ろ過層17Bの上で一旦水層100CAを形成した後、ろ過層17B,17C,17Dを順次通過して、この際に凝縮した濁質がトラップされ、殺菌剤2a,有機物及び凝縮した濁質の除去された被処理水100dとなる。
この他の淡水化処理は第1実施形態と同様なので説明を省略する。
第2実施形態の海水淡水化プラントによれば、第1実施形態の海水淡水化プラントと同様の効果が得られることに加え、次のような効果が得られる。
つまり、第1実施形態のように細かなろ材7b,7c,7dに触媒を担持させるのに較べて、供給配管20caの内周面に触媒をコーティングするだけなので、被処理水の流路に触媒を固定するのが容易である。また、既存の海水淡水化プラントを改造して本実施形態の海水淡水化プラントと同様の構成を得ようとする場合には、供給配管20caのみを改造又は変更すれば良いので、既存の海水淡水化プラントからの改造が容易であるという利点もある。
上記第2実施形態では、触媒コーティング層20cbを供給配管20caの内周面の全周に形成し且つ全長に渡って形成したが、被処理水100cに含まれる有機物及び殺菌剤2aを効果的に分解できるのであれば、供給配管20caの内周面の一部にだけに形成しても良い。例えば、触媒コーティング層20cbを、供給配管20caの内周面の下半分だけ、又は、砂ろ過装置7の内部に配置された部分にだけ形成するようにしても良い。
本発明の水処理装置の第3実施形態として海水淡水化プラントについて、図4を参照して説明する。なお、上記の各実施形態と同一要素については同一の符号を付し、その説明を省略する。
図3A及び図3Bに示す第2実施形態の海水淡水化プラントでは、触媒を、砂ろ過装置17に被処理水を供給する供給配管20caの内周面にコーティングしていたのに対し、本実施形態の海水淡水化プラントでは、触媒を、供給配管20cの内周面に替えて、砂ろ過装置27内に設けた網状体27aにコーティングしている。
図4に示す供給配管20c及び砂ろ過装置27は、第2実施形態の海水淡水化プラントに対し、図3A及び図3Bに示す第2実施形態の供給配管20ca及び砂ろ過装置17に替えて使用される。
砂ろ過装置27内に供給される被処理水100cの単位時間当たりの供給量に較べると、ろ過層17B,17C,17Dにおける被処理水100cの単位時間当たりの通過量は少量である。このため、砂ろ過装置27内に流路20cから供給された被処理水100cは第1ろ過層17Bの上で水層100Cを一旦形成する。
網状体27aは、金属やプラスチック等により形成された線材により格子状に構成され、その全表面には触媒がコーティングされている。この触媒は、水層100C(被処理水100c)に含まれる殺菌剤2aに分解反応を生じさせ活性酸素ラジカルを発生させる。触媒として使用できる金属又は金属化合物は、第1及び第2実施形態と同じである。
本実施形態に係る淡水化処理を、図4を参照して説明する。
水層100Cを形成する被処理水100cは、殺菌剤2a,有機物及び凝縮した濁質を含んでいる。殺菌剤2aは、網状体27aの表面にコーティングされた触媒の作用により分解され、有機物は、殺菌剤2aの分解の際に発生した活性酸素ラジカルにより分解される。すなわち、被処理水100cは、水層100Cにおいて殺菌剤2a及び有機物が除去される。
この殺菌剤2a及び有機物が除去された被処理水は、ろ過層17B,17C,17Dを通過する際に濁質をろ過され、殺菌剤2a,有機物及び濁質の除去された被処理水100dとなる。
この他の淡水化処理は上記の各実施形態と同様なので説明を省略する。
第3実施形態の海水淡水化プラントによれば、第1実施形態の海水淡水化プラントと同様の効果が得られることに加え、次のような効果が得られる。
つまり、第1実施形態のように細かなろ材7b,7c,7dに触媒を担持させるのに較べて、触媒をコーティングした網状体27aを設けるだけなので、被処理水の流路に触媒を固定するのが容易である。また、既存の海水淡水化プラントを改造して本実施形態の海水淡水化プラントと同様の構成を得ようとする場合には、網状体27aを追加するだけで良いので、改造が容易であるという利点もある。
また、網状体27aを水層100Cに水没状態とするので、網状体27aにコーティングされた触媒と水層100Cを形成する被処理水100cとの接触時間を長く取ることができ、触媒の作用による殺菌剤2a及び有機物の除去を効果的に行うことができる。
上記第3実施形態では、網状体27aをろ過層17Bから上方に所定の間隔を空けて配置したが、網状体27aをろ過層17Bの上面に載置するようにしても良い。
上記第3実施形態では、網状体27aの全表面に触媒をコーティングしたが、網状体27aの表面の一部に(又は網状体27aの表面の一部を除いて)触媒をコーティングしても良い。
上記第3実施形態では、網状体27aを、線材を使用して格子状(すなわち一の方向に並ぶ線材と他の方向に並ぶ線材とを交差させる構成)としたが、全ての線材を一定方向に並べて構成しても良い。
また、上記第3実施形態では、網状体27aを水層100Cに水没状態とするようにしたが、網状体27aを水層100Cの上方に配置しても良い。この場合、網状体27aと被処理水100cとの接触時間が長くなるように、網状体27aをパンチングメタル形状にするなどして、その開口面積を水層100Cに水没状態とする場合よりも少なめにすることが好ましく、網状体27a上に水層100Cが形成されるようにするのが好ましい。
本発明の水処理装置の第4実施形態として海水淡水化プラントについて、図5を参照して説明する。なお、上記の各実施形態と同一要素については同一の符号を付し、その説明を省略する。
図5は、本発明の第4実施形態に係る砂ろ過装置及びその周辺の構成を示す模式的な断面図である。
第2実施形態の海水淡水化プラントでは、触媒を、砂ろ過装置17に被処理水を供給する供給配管20caの内周面にコーティングしていたのに対し、本実施形態の海水淡水化プラントでは、触媒を、供給配管20caにコーティングする替わりに、粉末状又は粒状の触媒を、供給配管20cを介して砂ろ過装置17の内部に供給するようにしている。
図5に示す本実施形態に係る砂ろ過装置17は、図3Aに示す第2実施形態の砂ろ過装置17と同一の構成であるが、砂ろ過装置17の外部において被処理水100Cの供給配管20cに、触媒供給装置(触媒供給手段)30から触媒が供給される。この触媒は、上記の各実施形態と同様に被処理水100cに含まれる殺菌剤2aに分解反応を生じさせ活性酸素ラジカルを発生させるものであり、触媒として使用できる金属又は金属化合物も上記の各実施形態と同じである。
供給配管20c内に供給された触媒は、供給配管20c内を流通する被処理水100cとともに砂ろ過装置17内に供給される。この触媒は、その大半が、水層100C内に拡散又は第1ろ過層17Bの上面に堆積する形態で砂ろ過装置17内に配置され、その一部が各ろ過層17B,17C,17D内に潜り込む形態で砂ろ過装置17内に配置されることとなる。
また、触媒の供給は、必要に応じて適宜行うようにしても良いし、所定の時間間隔ごとに間欠的に行うようにしても良いし、常時連続して行うようにしても良い。
この他の構成は、第2実施形態の海水淡水化プラントと同じであるので説明を省略する。
本実施形態に係る淡水化処理を、図5を参照して説明する。
被処理水100cが含んでいる殺菌剤2aは、触媒供給装置30から砂ろ過装置17内に供給された触媒の作用により分解され、被処理水100cが含んでいる有機物は、殺菌剤2aの分解の際に発生した活性酸素ラジカルにより分解される。
この他の淡水化処理は前記の各実施形態と同様なので説明を省略する。
第4実施形態の海水淡水化プラントによれば、第1実施形態の海水淡水化プラントと同様の効果が得られることに加え、次のような効果が得られる。
つまり、触媒が摩滅するなどして触媒量が減少しても、新たな触媒を適宜供給できるので、触媒による作用・効果(殺菌剤2aの分解、活性酸素ラジカルによる有機物の分解)を持続して得られる。
さらに、触媒の比重がアンスラサイト17bの比重よりも重いことから、逆洗時に逆洗水とともに触媒が砂ろ過装置17から排出されてしまうことがないため、不要な触媒の排出を防止してランニングコストの上昇を抑えることができる。
上記の第4実施形態では、本発明の触媒供給手段を図5に示す触媒供給装置30により構成したが、本発明の触媒供給手段の構成はこの触媒供給装置30に限定されない。例えば、触媒供給装置30に対し触媒貯留部31を省略することもできる(つまり供給配管20cに触媒供給用の座を設けるだけでも良い)。この場合、バルブ33を開弁した上で人手により触媒を配管33内に投入すれば良い。また、触媒供給装置30は、触媒貯留部31内の触媒を重力で落下させて供給配管20cに供給する構成としたが、圧力流体により圧送して供給配管20cに供給する構成としても良い。
(1)本発明の水処理装置における触媒の配置箇所は、上記各実施形態のものに限定されず、被処理水への殺菌剤2aの注入位置2Aから1段RO膜12bとの間の流路であれば良い。
但し、触媒の配置箇所が、殺菌剤2aの注入位置2Aに近すぎると、被処理水100aの殺菌が十分に行われないうちに殺菌剤2aが分解されてしまう。したがって、被処理水100aの殺菌が十分に行われる距離を見込んで、この距離よりも殺菌剤2aの注入位置2Aから離隔した位置に触媒を設置するのが好ましい。或いは、ミキサ6により被処理水100aと殺菌剤2aとの混合が行われた後(つまりミキサ6よりも下流側)に触媒を設置するのが好ましい。
また、触媒がRO膜12b,13bに付着してしまうとRO膜12b,13bの処理性能を低下させてしまう可能性があるので、触媒が剥離するなどして下流側へと流れていってもRO膜12b,13bに到達するまえに除去されるようにMCF10よりも上流側に触媒を配置するのが好ましい。
2 殺菌剤注入装置
2a 殺菌剤〔次亜塩素酸ソーダ(NaClO)〕
6 ミキサ(混合促進手段)
7,17,27 砂ろ過装置
7B,17B 第1ろ過層
7C,17C 第2ろ過層
7D,17D 第3ろ過層
7b,17b アンスラサイト(ろ材)
7c,17c 砂(ろ材)
7d,17d 砂利(ろ材)
10 MCF
10a カートリッジフィルタ(ろ材)
12 1段逆浸透膜モジュール(1段RO膜モジュール)
12b 1段逆浸透膜(1段RO膜)
13 2段逆浸透膜モジュール(2段RO膜モジュール)
13b 2段逆浸透膜(2段RO膜)
20,20a~20j,20ca 流路
20cb 触媒コーティング層
27a 網状体
30 触媒供給装置(触媒供給手段)
100,100a~100g,100ca 被処理水
100C,100CA 水層
Claims (11)
- 被処理水が流通する流路と、
前記流路の注入位置において塩素系の殺菌剤を注入する殺菌剤注入手段と、
前記注入位置よりも前記被処理水の流通方向で下流側において前記流路に配置されるとともに、逆浸透膜を有する逆浸透膜モジュールとが備えられ、
前記流路内には、前記注入位置と前記逆浸透膜モジュールとの間において、以下の(1),(2)及び(3)に記載された金属又は金属化合物の中から選択された少なくとも1種類の金属又は金属化合物が、触媒として配置されたことを特徴とする、水処理装置。
(1)8族元素,9族元素及び10族元素に属する金属
(2)2族元素に属する金属
(3)前記(1),(2)に記載された各金属の金属化合物である水酸化物,酸化物,炭酸塩及び硫酸塩 - 前記流路には、前記注入位置と前記触媒との間に、前記殺菌剤と前記被処理水との混合を促進する混合促進手段が備えられた
ことを特徴とする、請求項1に記載の水処理装置。 - 前記流路には、前記混合促進手段と前記逆浸透膜モジュールとの間にろ材が備えられ、
前記触媒は、少なくとも、前記ろ材の一部に固定された
ことを特徴とする、請求項2に記載の水処理装置。 - 前記流路には、前記触媒と前記逆浸透膜モジュールとの間にろ材が備えられた
ことを特徴とする、請求項2又は3に記載の水処理装置。 - 前記流路には、前記混合促進手段と前記逆浸透膜モジュールとの間にろ材が備えられ、
前記触媒は、前記流路の前記ろ材へ前記被処理水を供給する部分に固定された
ことを特徴とする、請求項2~4の何れか1項に記載の水処理装置。 - 前記流路には、前記混合促進手段と前記逆浸透膜モジュールとの間にろ材が備えられ、
前記ろ材の上方に網状体が配置され、
前記触媒は前記網状体に固定された
ことを特徴とする、請求項2~5の何れか一項に記載の水処理装置。 - 前記網状体が、前記ろ材の上に前記被処理水によって形成される水層に水没するように配置された
ことを特徴とする、請求項6に記載の水処理装置。 - 前記触媒を前記流路に供給する触媒供給手段が備えられた
ことを特徴とする、請求項2~7の何れか一項に記載の水処理装置。 - 前記流路には、前記混合促進手段と前記逆浸透膜モジュールとの間にろ材が備えられ、
前記触媒供給手段により、前記流路の前記ろ材へ前記被処理水を供給する部分に、前記触媒を供給するようにした
ことを特徴とする、請求項8に記載の水処理装置。 - 前記触媒は、前記ろ材よりも比重が重い
ことを特徴とする、請求項9に記載の水処理装置。 - 前記8族元素に属する金属が鉄であり、前記9族元素に属する金属がコバルトであり、前記10族元素に属する金属がニッケルであり、前記2族元素に属する金属が、マグネシウム,カルシウム,ストロンチウム及びバリウムである
ことを特徴とする、請求項1~10の何れか1項に記載の水処理装置。
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CN107008480A (zh) * | 2017-03-30 | 2017-08-04 | 常州大学 | 一种碳酸钴复合碳酸镧光催化剂的制备方法 |
CN107096555A (zh) * | 2017-03-30 | 2017-08-29 | 常州大学 | 一种碳酸钴复合磷酸钴光催化剂的制备方法 |
JP2019076827A (ja) * | 2017-10-24 | 2019-05-23 | 住友電気工業株式会社 | 水処理設備及び水処理方法 |
CN108408996A (zh) * | 2018-04-25 | 2018-08-17 | 郑州德威机械设备有限公司 | 一种基于海水电解的生活污水处理装置 |
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