CN108341528A - The method that fouling membrane is reduced in the processing method and water treatment procedure of tap water - Google Patents
The method that fouling membrane is reduced in the processing method and water treatment procedure of tap water Download PDFInfo
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- CN108341528A CN108341528A CN201810169756.7A CN201810169756A CN108341528A CN 108341528 A CN108341528 A CN 108341528A CN 201810169756 A CN201810169756 A CN 201810169756A CN 108341528 A CN108341528 A CN 108341528A
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- ultrafiltration
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 246
- 239000012528 membrane Substances 0.000 title claims abstract description 188
- 238000000034 method Methods 0.000 title claims abstract description 99
- 239000008399 tap water Substances 0.000 title claims abstract description 28
- 235000020679 tap water Nutrition 0.000 title claims abstract description 28
- 238000003672 processing method Methods 0.000 title claims abstract description 13
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 151
- 238000012545 processing Methods 0.000 claims abstract description 59
- 230000008569 process Effects 0.000 claims abstract description 45
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 18
- 238000002203 pretreatment Methods 0.000 claims abstract description 17
- 238000001914 filtration Methods 0.000 claims description 48
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 33
- 238000001179 sorption measurement Methods 0.000 claims description 33
- 230000001112 coagulating effect Effects 0.000 claims description 32
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 28
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 16
- 230000003647 oxidation Effects 0.000 claims description 16
- 238000007254 oxidation reaction Methods 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 10
- 238000004062 sedimentation Methods 0.000 claims description 5
- 238000001471 micro-filtration Methods 0.000 claims description 2
- 238000001728 nano-filtration Methods 0.000 claims description 2
- 238000001223 reverse osmosis Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 13
- 238000005516 engineering process Methods 0.000 abstract description 12
- 244000005700 microbiome Species 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000001954 sterilising effect Effects 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 65
- 238000004140 cleaning Methods 0.000 description 55
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 49
- 238000004659 sterilization and disinfection Methods 0.000 description 42
- 239000000126 substance Substances 0.000 description 35
- 239000000460 chlorine Substances 0.000 description 33
- 229910052801 chlorine Inorganic materials 0.000 description 32
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 31
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 28
- 239000004576 sand Substances 0.000 description 27
- 239000006004 Quartz sand Substances 0.000 description 26
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 24
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 22
- 229910052782 aluminium Inorganic materials 0.000 description 20
- 239000000701 coagulant Substances 0.000 description 20
- 229910052799 carbon Inorganic materials 0.000 description 19
- 238000010926 purge Methods 0.000 description 19
- 239000004411 aluminium Substances 0.000 description 18
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 18
- 238000005259 measurement Methods 0.000 description 16
- 239000000523 sample Substances 0.000 description 16
- 238000011109 contamination Methods 0.000 description 15
- 239000002033 PVDF binder Substances 0.000 description 14
- 239000003814 drug Substances 0.000 description 14
- 229920001282 polysaccharide Polymers 0.000 description 14
- 239000005017 polysaccharide Substances 0.000 description 14
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 14
- 239000000463 material Substances 0.000 description 13
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 12
- 238000009287 sand filtration Methods 0.000 description 12
- 230000000813 microbial effect Effects 0.000 description 11
- 108090000623 proteins and genes Proteins 0.000 description 11
- 239000003610 charcoal Substances 0.000 description 10
- 102000004169 proteins and genes Human genes 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- 235000015165 citric acid Nutrition 0.000 description 8
- 239000011159 matrix material Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 238000012544 monitoring process Methods 0.000 description 7
- 239000006228 supernatant Substances 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 125000001309 chloro group Chemical group Cl* 0.000 description 6
- 238000005345 coagulation Methods 0.000 description 6
- 230000015271 coagulation Effects 0.000 description 6
- 239000002131 composite material Substances 0.000 description 6
- 235000020188 drinking water Nutrition 0.000 description 6
- 239000003651 drinking water Substances 0.000 description 6
- 230000004907 flux Effects 0.000 description 6
- 239000008187 granular material Substances 0.000 description 6
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 6
- 229910052742 iron Inorganic materials 0.000 description 6
- 230000001678 irradiating effect Effects 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000012286 potassium permanganate Substances 0.000 description 6
- 241000894007 species Species 0.000 description 6
- 238000012360 testing method Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000001514 detection method Methods 0.000 description 5
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- 231100000719 pollutant Toxicity 0.000 description 5
- 230000002787 reinforcement Effects 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 210000004027 cell Anatomy 0.000 description 4
- 230000035622 drinking Effects 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
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- 239000000047 product Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 230000000274 adsorptive effect Effects 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000011001 backwashing Methods 0.000 description 3
- 230000027455 binding Effects 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
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- 238000011161 development Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 150000004676 glycans Chemical class 0.000 description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- -1 oxygen Anion Chemical class 0.000 description 3
- 238000001878 scanning electron micrograph Methods 0.000 description 3
- 238000012163 sequencing technique Methods 0.000 description 3
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- 108091032973 (ribonucleotides)n+m Proteins 0.000 description 2
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- 238000007400 DNA extraction Methods 0.000 description 2
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- 238000000246 agarose gel electrophoresis Methods 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
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- 230000034994 death Effects 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000249 desinfective effect Effects 0.000 description 2
- YJHDFAAFYNRKQE-YHPRVSEPSA-L disodium;5-[[4-anilino-6-[bis(2-hydroxyethyl)amino]-1,3,5-triazin-2-yl]amino]-2-[(e)-2-[4-[[4-anilino-6-[bis(2-hydroxyethyl)amino]-1,3,5-triazin-2-yl]amino]-2-sulfonatophenyl]ethenyl]benzenesulfonate Chemical compound [Na+].[Na+].N=1C(NC=2C=C(C(\C=C\C=3C(=CC(NC=4N=C(N=C(NC=5C=CC=CC=5)N=4)N(CCO)CCO)=CC=3)S([O-])(=O)=O)=CC=2)S([O-])(=O)=O)=NC(N(CCO)CCO)=NC=1NC1=CC=CC=C1 YJHDFAAFYNRKQE-YHPRVSEPSA-L 0.000 description 2
- 238000010828 elution Methods 0.000 description 2
- MHMNJMPURVTYEJ-UHFFFAOYSA-N fluorescein-5-isothiocyanate Chemical compound O1C(=O)C2=CC(N=C=S)=CC=C2C21C1=CC=C(O)C=C1OC1=CC(O)=CC=C21 MHMNJMPURVTYEJ-UHFFFAOYSA-N 0.000 description 2
- 229910052740 iodine Inorganic materials 0.000 description 2
- 239000011630 iodine Substances 0.000 description 2
- PNDPGZBMCMUPRI-UHFFFAOYSA-N iodine Chemical compound II PNDPGZBMCMUPRI-UHFFFAOYSA-N 0.000 description 2
- 230000002934 lysing effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000002906 microbiologic effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000004759 spandex Substances 0.000 description 2
- 238000004611 spectroscopical analysis Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 108020004465 16S ribosomal RNA Proteins 0.000 description 1
- QKNYBSVHEMOAJP-UHFFFAOYSA-N 2-amino-2-(hydroxymethyl)propane-1,3-diol;hydron;chloride Chemical compound Cl.OCC(N)(CO)CO QKNYBSVHEMOAJP-UHFFFAOYSA-N 0.000 description 1
- 229920000936 Agarose Polymers 0.000 description 1
- 241000223935 Cryptosporidium Species 0.000 description 1
- 230000004568 DNA-binding Effects 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- 241000224467 Giardia intestinalis Species 0.000 description 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
- LPSCRKGVODJZIB-UHFFFAOYSA-N [I].[C] Chemical group [I].[C] LPSCRKGVODJZIB-UHFFFAOYSA-N 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 239000012491 analyte Substances 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
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- 108020004707 nucleic acids Proteins 0.000 description 1
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- 150000007523 nucleic acids Chemical class 0.000 description 1
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- 239000010802 sludge Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- UIIMBOGNXHQVGW-UHFFFAOYSA-M sodium bicarbonate Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 239000012064 sodium phosphate buffer Substances 0.000 description 1
- 238000011895 specific detection Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 235000013547 stew Nutrition 0.000 description 1
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Classifications
-
- 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
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses the method for reducing fouling membrane in a kind of processing method of tap water and water treatment procedure, this method includes carrying out ultraviolet treatment with irradiation, hyperfiltration treatment, chlorination processing successively after pre-treatment to raw water.The method of the present invention has adjusted ultrafiltration and ultraviolet process sequences in original water treatment technology; both the sterilizing function of ultraviolet irradiation control microorganism had been remained; increase the effect of protection ultrafiltration membrane again simultaneously; reduce the fouling membrane of ultrafiltration membrane in process of ultrafiltration treatment; operation energy consumption is reduced, the service life of film during film process is significantly improved, reduces the processing cost of tap water; achieve the purpose that " energy-saving and emission-reduction ", the high fit environmental protection concept of " friendly process ".
Description
Technical field
The present invention relates to a kind of processing method of water resource, more particularly to one kind drinking water purification method, belongs to Shui Chu
Reason field.
Background technology
Drinking water refers to can be without handling, directly feed the water that human body drinks.Water is the main composition portion of human body fluid
Point, it is the important substance for constituting cell, tissue fluid, blood plasma etc..Medium of the water as all chemical reactions in vivo, is various nutrition
The platform of element and matter transportation.
The purifying treatment method of drinking water is general at present with the following method：Raw water then passes through after coagulating kinetics
After two or more processing in filtering, ozone oxidation, adsorption filtration or hyperfiltration treatment, then carry out it is ultraviolet or it is ultraviolet and
Sodium hypochlorite sequence sterilizes, and finally enters clear water reserviors, wherein：Coagulant during coagulating kinetics is used to be added in combined shaft
Aluminium polychloride adds the dosing method of ferric trichloride in mechanical accelerating purifying pool, or adds ferric trichloride in combined shaft,
Aluminium polychloride is added in mechanical accelerating purifying pool；Either only aluminium polychloride or ferric trichloride are added in combined shaft；Or
It is to add ferric trichloride in potassium permanganate composites, colloidal particle and small suspended contamination in raw water is removed using coagulating sedimentation；
Ozone Oxidation Treatment is to make organic pollutants oxidative degradation, and part macromolecular organic pollution is decomposed into and is easily dropped by biology
Solution or the small organic molecule being easily tightly held by activated carbon；Use upper layer for activity in charcoal sand adsorption tank during charcoal sand adsorption treatment
Charcoal particle, lower layer are quartz sand, and the organic pollution in aqueous to entering adsorption tank carries out physics, chemisorption and biology and drops
Solution, absorbs and filter particulate matter in water.
Ultraviolet light is commonly used in sterilizing, and principle is the ultraviolet light using appropriate wavelength, is destroyed in microbial cell
The molecular structure of DNA and RNA causes to be cross-linked to form photoproducts between nucleic acid key and chain break, stock, blocks its reproduction process,
It in turn results in growth cell death or reproducibility is dead, to achieve the effect that sterilizing.
Another action principle of ultraviolet-sterilization disinfection is water and dissolved oxygen therein under ultraviolet irradiation, generates super oxygen
Anion (O2 -), excitation ground state oxygen molecule (O2 *), hydrogen peroxide (H2O2), the oxidisability such as hydroxyl radical free radical (OH) are extremely strong to swash
State substance is sent out, these substances have destructive destruction to microbial pathogens in water, live by changing DNA in microbial body
Property, reproduction process is destroyed, causes cell metabolism to get muddled so as to cause death, reaches sterilisation purpose.
Although in recent years use ultraviolet technique treated sewage processing and drinking water treatment have wide application, its
The sterilisation stage of subsequent technique is also only limitted in terms of drinking water treatment, it is micro- for removing the bacterium in tap water, virus, fungi etc.
Biology.
Invention content
The purpose of the present invention is in coagulation, filtering and the hyperfiltration treatment technique in existing tap water production process for existing
Technological deficiency, the processing side of the method and tap water of the fouling membrane that membrane separation is reduced in a kind of water treatment procedure is provided
Method, the method for the present invention has adjusted ultrafiltration and ultraviolet process sequences in original water treatment technology, right before carrying out hyperfiltration treatment
Aqueous carries out ultraviolet treatment with irradiation, has not only remained the sterilizing function of ultraviolet irradiation control microorganism, but also increases protection
The effect of ultrafiltration membrane reduces the fouling membrane of ultrafiltration membrane in process of ultrafiltration treatment, and then reduces the operation energy consumption of ultrafiltration membrane, extends
The physics of ultrafiltration membrane and chemical cleaning period reduce physics and the number of chemical cleaning, reduce the discharge capacity of chemical cleaning water, reach
To the purpose of " energy-saving and emission-reduction ", the high fit environmental protection concept of " friendly process ".
To achieve the purpose of the present invention, one aspect of the present invention provides a kind of processing method of tap water, including to tap water
Factory's raw water carries out ultraviolet treatment with irradiation, hyperfiltration treatment, chlorination processing.
Wherein, further include then carrying out ultraviolet treatment with irradiation successively, at ultrafiltration to raw water of waterworks after pre-treatment
Reason, chlorination processing.
Wherein, water temperature is 0-40 DEG C, preferably 0-30 DEG C in decontamination process.
Wherein, it is 40-300mJ/cm that ultraviolet irradiating dose is controlled during the ultraviolet treatment with irradiation2, preferably
40-100mJ/cm2, further preferably 40-80mJ/cm2。
In particular, the temperature for controlling flow during the ultraviolet treatment with irradiation is 0-40 DEG C, preferably 0-30 DEG C；Control
Flow rate of water flow processed is 0.1-3m/s, preferably 0.5-2m/s.
Especially, it is 0.1-2s that the ultraviolet treatment with irradiation time is controlled during the ultraviolet treatment with irradiation.
In particular, when the ultraviolet treatment with irradiation selection cavity type UV disinfection system, ultraviolet treatment with irradiation is controlled
Time is 0.1-1s, preferably 0.5s；When selecting open tunnel type UV disinfection system, the control ultraviolet treatment with irradiation time is 1-
2s, preferably 1.5s.
Wherein, the membrane aperture of ultrafiltration membrane is 0.01-0.1 μm in the process of ultrafiltration treatment.
In particular, in the process of ultrafiltration treatment control hyperfiltration treatment operating pressure be 0.01-0.15MPa；Control
Water temperature is 0-40 DEG C, preferably 0-30 DEG C.
Especially, use the operating pressure of immersed ultrafiltration membrane pond progress hyperfiltration treatment for 0.03-0.06MPa, preferably
0.04-0.05MPa；Use the operating pressure of pressure type ultrafiltration membrane pool progress hyperfiltration treatment for 0.01-0.15MPa, preferably
0.05-0.09MPa。
Wherein, the ultrafiltration membrane is using PVC, PVDF, PVDF reinforcement or PS membrane etc..
In this field water supply plant it is existing it is known, any for water treatment ultrafiltration membrane (such as membrane material be PVDF,
PVDF reinforcements etc., membrane aperture are 0.01-0.1 μm) it is suitable for the present invention.
Wherein, the chlorination processing is to add sodium hypochlorite in the water outlet after ultrafiltration membrane treatment.
In particular, the dosage of the sodium hypochlorite is 2-10mg/L, preferably 5mg/L (adds time chlorine in i.e. every 1L water
Sour sodium 2-10mg).
Wherein, the pre-treatment include to raw water carry out coagulating kinetics, ozone Oxidation Treatment, adsorption filtration processing,
It is one or more in filtration treatment.
In particular, turbidity (NTU)≤3.0 of the raw water pre-treatment to water outlet；CODMn≤5.0mg/L；The concentration of Fe (total iron)<
0.30mg/L；The concentration of Al (total aluminium)<0.20mg/L；PH is 7.00-8.50.
Especially, the turbidity of raw water pre-treatment to water outlet is preferably≤1.0NTU；CODMnPreferably≤3.0mg/L；Fe is (total
Iron) concentration be preferably<0.3mg/L；The concentration of Al (total aluminium) is preferably<0.2mg/L；PH is 7.50-8.50.
The pre-treatment typically refers to Technology development in water supply plant water treatment technology, Technology development+depth
Treatment technology or Technology development+further treatment technique+hyperfiltration treatment.Wherein, conventional treatment process (such as coagulating sedimentation-
Quartz sand filtration, coagulating sedimentation-anthracite quartz sand double-layer filter material filtering etc.)；Advanced treatment process (such as ozone oxidation-work
Property charcoal absorption, the adsorption filtration of ozone oxidation-charcoal sand, activated carbon adsorption filtering etc.).
Wherein, the coagulating kinetics are that coagulant is added into aqueous, after being mixed evenly, the impurity in aqueous
It is precipitated after forming flco with coagulant, reaches separation.
In particular, the coagulant that the coagulating treatment adds is ferric trichloride, aluminium polychloride, bodied ferric sulfate or sulfuric acid
It is one or more in aluminium.
In particular, the dosage of coagulant is 5-50mg/L；The coagulating treatment time is 60-120min, preferably 90min.
The existing known any coagulating treatment equipment of water supply plant, coagulation method are suitable for the invention coagulation in this field
Processing.
Wherein, the ozone Oxidation Treatment is that aqueous is passed through ozone contact tank, carries out ozone oxidation.
In particular, the dosage of ozone is 0-2mg/L, preferably 0.5mg/L during the ozone Oxidation Treatment；Ozone
Time of contact is 5-12min, preferably 10-12min, further preferably 11.69min.
Wherein, filter cycle is 36-48h in the adsorption filtration processing procedure；Absorption time of contact is 2-20min, excellent
It is selected as 10-13min.
In particular, carry out the adsorption filtration processing using Carbon-sand filter, the filtering layer in filter tank is activated carbon and quartz sand,
It is at the middle and upper levels granular active carbon, and lower layer is quartz sand.
Wherein, the granular active carbon is cylindric, carbon granule a diameter of 1-2mm, preferably 1.5mm；Carbon granule pillar height is
2-3mm；Iodine sorption value >=900mg/g of activated carbon；Methylenum careuleum adsorptive value >=180mg/g of activated carbon.
In particular, the thickness of the active carbon layer and quartz sand layer is 0.3-0.6：1, preferably 0.5:1.
Wherein, filter cycle is 16-36h in the filter process；Filtering rate is 2-15m/h, preferably 8-9m/
h。
The existing known any adsorption filtration device and method of water supply plant are suitable for the present invention, generally use in this field
Carbon-sand filter or activated carbon filter etc.；The existing known any filter plant of water supply plant and method are suitable for the present invention, usually
Using quartzy sand filter or anthracite-quartz sand double-bed filter etc..
The method that another aspect of the present invention provides the fouling membrane that membrane separation is reduced in a kind of water treatment procedure, to aqueous
It carries out ultraviolet treatment with irradiation and then membrane separation is carried out to aqueous.
Wherein, it is 40-300mJ/cm that ultraviolet irradiating dose is controlled during the ultraviolet treatment with irradiation2, preferably
40-100mJ/cm2, further preferably 40-80mJ/cm2。
In particular, the temperature for controlling flow during the ultraviolet treatment with irradiation is 0-40 DEG C, preferably 0-30 DEG C；Control
Flow rate of water flow processed is 0.1-3m/s, preferably 0.5-2m/s；The control ultraviolet treatment with irradiation time is 0.1-2s.
Especially, it is using cavity type ultraviolet treatment with irradiation, control ultraviolet treatment with irradiation time in water treatment procedure
0.1-1s, preferably 0.5s；Open tunnel type ultraviolet treatment with irradiation is used in water treatment procedure, then when controlling ultraviolet treatment with irradiation
Between be 1-2s, preferably 1.5s.
Wherein, at the membrane separation selection ultrafiltration membrane treatment, micro-filtration film process, nanofiltration membrane treatment or reverse osmosis membrane
Reason, preferably ultrafiltration membrane treatment.
In particular, the membrane aperture of ultrafiltration membrane is 0.01-0.1 μm during the ultrafiltration membrane treatment.
Especially, in the process of ultrafiltration treatment control hyperfiltration treatment operating pressure be 0.01-0.15MPa；Control
Water temperature is 0-40 DEG C, preferably 0-30 DEG C.
Wherein, use the operating pressure of immersed ultrafiltration membrane pond progress hyperfiltration treatment for 0.03-0.06MPa, preferably
0.04-0.05MPa；Use the operating pressure of pressure type ultrafiltration membrane pool progress hyperfiltration treatment for 0.01-0.15MPa, preferably
0.05-0.09MPa。
In particular, the ultrafiltration membrane is using PVC, PVDF, PVDF reinforcement or PS membrane etc..
In this field water supply plant it is existing it is known, any for water treatment ultrafiltration membrane (such as membrane material be PVDF,
PVDF reinforcements etc., membrane aperture are 0.01-0.1 μm) it is suitable for the present invention.
In particular, further including carrying out pre-treatment to aqueous before carrying out ultraviolet treatment with irradiation to aqueous.
Wherein, the pre-treatment includes at raw water progress coagulating kinetics, ozone Oxidation Treatment, adsorption filtration
It is one or more in reason, filtration treatment.
In particular, turbidity (NTU)≤3.0 of the raw water pre-treatment to water outlet；CODMn≤5.0mg/L；Fe (total iron) concentration≤
1.0mg/L；Al (total aluminium) concentration≤1.0mg/L；PH is 7.00-8.50.
Especially, the turbidity of raw water pre-treatment to water outlet is preferably≤1.0NTU；CODMnPreferably≤3.0mg/L；Fe is (total
Iron) concentration preferably≤0.3mg/L；Al (total aluminium) concentration is preferably≤0.2mg/L.
In particular, the coagulating kinetics are that coagulant is added into aqueous, it is miscellaneous in aqueous after being mixed evenly
Matter precipitates after forming flco with coagulant, reaches separation.
Especially, the coagulant that the coagulating treatment adds is ferric trichloride, aluminium polychloride, bodied ferric sulfate or sulfuric acid
It is one or more in aluminium.
In particular, the dosage of coagulant is 5-50mg/L；The coagulating treatment time is 60-120min, preferably 90min.
The existing known any coagulating treatment equipment of water supply plant, coagulation method are suitable for the invention coagulation in this field
Processing.
Wherein, the ozone Oxidation Treatment is that aqueous is passed through ozone contact tank, carries out ozone oxidation.
In particular, the dosage of ozone is 0-2mg/L, preferably 0.5mg/L during the ozone Oxidation Treatment；Ozone
Time of contact is 5-12min, preferably 10-12min, further preferably 11.69min.
Wherein, filter cycle is 36-48h in the adsorption filtration processing procedure；Absorption time of contact is 2-20min, excellent
It is selected as 10-13min.
In particular, carry out the adsorption filtration processing using Carbon-sand filter, the filtering layer in filter tank is activated carbon and quartz sand,
It is at the middle and upper levels granular active carbon, and lower layer is quartz sand.
Wherein, the granular active carbon is cylindric, carbon granule a diameter of 1-2mm, preferably 1.5mm；Carbon granule pillar height is
2-3mm；Iodine sorption value >=900mg/g of activated carbon；Methylenum careuleum adsorptive value >=180mg/g of activated carbon.
In particular, the thickness of the active carbon layer and quartz sand layer is 0.3-0.6：1, preferably 0.5:1.
Wherein, filter cycle is 16-36h in the filter process；Filtering rate is 2-15m/h, preferably 8-9m/
h。
Domestic more complete more advanced handling technology of water supply includes at present：Coagulating sedimentation-filtering-ozone-active carbon absorption-
Ultrafiltration-is ultraviolet-chlorination, wherein coagulating sedimentation-filtering-ozone-active carbon absorption-ultrafiltration is water main process, ultraviolet-
Chlorination is to be disinfected before dispatching from the factory, and usually carry out disinfection after main process processing again, and the present invention is by adjusting net
The sequencing of ultrafiltration in change processing and the ultraviolet technique in disinfecting provide it is a kind of not only having retained former process effect but also
The method that Pollution of Ultrafiltration Membrane in water treatment technology can be reduced.
Compared with prior art, the method for the present invention has the following advantages that：
1, the purifying treatment method of tap water of the invention is that ultraviolet and ultrafiltration work is adjusted in handling technology of water supply flow
Skill sequence first carries out aqueous ultraviolet treatment with irradiation and then carries out ultrafiltration membrane treatment again, and the method for the present invention remains ultraviolet light
The function of microorganism is controlled, while increasing the effect of protection ultrafiltration membrane again, fouling membrane is reduced, reduces ultrafiltration membrane transmembrane pressure
Difference reduces water process energy, has more given full play to the effect of ultraviolet processing.
Ultraviolet disinfection processing is being carried out usually after ultrafiltration membrane treatment in existing water supply industry, it can be effective using ultraviolet disinfection
Control the microorganisms such as giardia lamblia stiles and Cryptosporidium.The method of the present invention adjusts ultraviolet light irradiation to before ultrafiltration membrane treatment,
The effect of ultraviolet control Pollution of Ultrafiltration Membrane is increased, and then protects ultrafiltration membrane operation, it is important to instructing water factory's technological design to have
Meaning possesses wide future in engineering applications.
2, the method for the present invention can both reduce ultrafiltration membrane energy consumption, reduce the row of ultrafiltration membrane chemical cleaning number and chemical cleaning water
High-volume, achieve the purpose that " energy-saving and emission-reduction ", the high fit environmental protection concept of " friendly process "；Moreover, after ultrafiltration membrane treatment
Chlorination processing is directly carried out, the treatment process for needing to carry out ultraviolet disinfection in more advanced handling technology of water supply is saved.
3, the method for the present invention does not increase any substance in the decontamination process of tap water, there is no need to chemicals,
Without other side effects, THMs class disinfection by-products will not be generated, ultraviolet processing is with safe to use, effect is extensive, disinfection
Steady performance.
4, the method for the present invention high degree of automation, operation is easy, and management is simple, and sterilization of high efficiency, sterilization are rapid, thorough.
5, the method for the present invention reduces in water treatment procedure fouling membrane in membrane separation, the service life of extended film,
Film process ability is improved, transmembrane pressure and operation energy consumption is reduced, has saved cost of water treatment.
Fouling membrane is the biggest obstacle that ultrafiltration membrane is used for clean water treatment, refers to particle, the colloidal particle handled in material
Or solute transportation deposited due to absorption in film surface or fenestra caused by membrane aperture become smaller or block, so that film is generated through stream
The irreversible change phenomenon of amount and stalling characteristic.Fouling membrane from pollutant type point include mainly inorganic pollution, organic contamination and
Microbial contamination.Fouling membrane can shorten the service life of film, reduce the processing capacity of film, increase operation energy consumption.
Description of the drawings
Fig. 1 is the flow diagram of water treatment of the present invention；
Fig. 2 is the LSCM observation charts of the protein contamination of ultrafiltration membrane surface；
Fig. 3 is the LSCM observation charts of β-polysaccharide pollution of ultrafiltration membrane surface；
Fig. 4 is the LSCM observation charts of α-polysaccharide pollution of ultrafiltration membrane surface；
Fig. 5 is the LSCM observation charts of the microbial contamination of ultrafiltration membrane surface；
Fig. 6 is the SEM observation charts of ultrafiltration membrane surface inorganic pollution；
Fig. 7 is that Venn figures are analyzed in ultrafiltration membrane surface biocoene species composition；
Fig. 8 is transmembrane pressure test result figure in process of ultrafiltration treatment.
Specific implementation mode
The invention will now be further described with reference to specific embodiments, the advantages and features of the present invention will be with description and
It is apparent.But examples are merely exemplary for these, and it is not intended to limit the scope of the present invention in any way.People in the art
Member it should be understood that without departing from the spirit and scope of the invention can to the details of technical solution of the present invention and form into
Row modifications or substitutions, but these modifications and replacement are each fallen in protection scope of the present invention.
Method in following embodiments, no special instruction are conventional method.
In the embodiment of the present invention purified treatment is carried out by raw material of the raw water of the water treatment technique of regular tap water factory
For illustrate, raw water quality is as follows：Turbidity≤50.0, coloration≤50 degree, CODMn≤ 20mg/L, pH value 7.00-9.00.
The tap water purifying processing method of the present invention is carried out according to flow chart as shown in Figure 1.In addition to above-mentioned processing water,
Except raw water quality, water treatment technique, water quality, the water of other waterworks are suitable for the present invention.
Embodiment 1
1, raw water pre-treatment
Raw water is passed through potassium permanganate composites, ozone contact tank, Carbon-sand filter successively, carries out coagulating kinetics, smelly successively
Oxygen oxidation processes, adsorption filtration processing；Wherein：Dosing coagulant tri-chlorination in potassium permanganate composites during coagulating kinetics
Iron, dosage of PAC 10-40mg/L；The coagulating treatment time is 90min (being usually 60-120min), and water temperature is 10 DEG C (usual
It is 0-40 DEG C, preferably 0-30 DEG C)；It (is usually 0-2mg/ that the dosage of ozone, which is 0.5mg/L, during ozone Oxidation Treatment
L)；Ozone contact time is 11.69min (be usually 5-12min), water temperature be 10 DEG C (be usually 0-40 DEG C, preferably 0-30
℃)；Carbon-sand filter 36-48h filter cycle；Time of contact is 12.8min (being usually 2-20min)；The backwash of Carbon-sand filter is strong
Spend 12-19L/m2·s；The filtering layer of Carbon-sand filter is activated carbon and quartz sand, is at the middle and upper levels granular active carbon, lower layer is stone
Sand, granular active carbon are cylindric, carbon granule a diameter of 1-2mm, preferably 1.5mm；Carbon granule pillar height is 2-3mm；Activated carbon
Iodine sorption value >=900mg/g；Methylenum careuleum adsorptive value >=180mg/g of activated carbon；The thickness of active carbon layer and quartz sand layer is
0.5:1 (is usually 0.3-0.6：1).
By the filtered effluent quality of charcoal sand according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.30 CODMn(mg/L)：<2.0 pH：7.50-8.50
Fe(mg/L)：<0.30 Al(mg/L)：<0.01
Coagulating sedimentation is said so that the conventional use of ferric trichloride in waterworks is coagulant as an example in the embodiment of the present invention
It is bright, corresponding dosage of coagulant (such as aluminium polychloride, bodied ferric sulfate, aluminum sulfate etc.) that other waterworks use etc.
It is suitable for the present invention；The embodiment of the present invention is illustrated by taking potassium permanganate composites as an example, existing known in other this fields
The coagulation-sedimentation equipment (such as inclined-plate clarifying basin, mechanical accelerating purifying pool, Actiflo add sand sedimentation basin etc.) that waterworks uses
It is suitable for the present invention.
2, ultraviolet irradiation is handled
Water outlet after the adsorption filtration of charcoal sand is entered into waterworks water process cavity type ultraviolet disinfection system by water pump
System (is discharged in the pipeline flowed through and UV disinfection system is housed, ultraviolet light generating system is mounted on inside water pipe), the absorption of charcoal sand
It filters out water and flows through UV disinfection system, ultraviolet generator is discharged adsorption filtration and carries out ultraviolet treatment with irradiation, wherein controlling
Ultraviolet irradiating dose is 40mJ/cm2(it is usually 40-100mJ/cm2, preferably 40-80mJ/cm2)；Water temperature is 10 DEG C (usual
It is 0-40 DEG C, preferably 0-30 DEG C)；Water velocity is 1m/s (being usually 0.1-3m/s, preferably 0.5-2m/s)；Ultraviolet light shines
It is 0.5s (being usually 0.1-2s) to penetrate processing time.
In the embodiment of the present invention ultraviolet irradiation processing using cavity type ultraviolet disinfection (other than cavity type ultraviolet disinfection,
Open tunnel type UV disinfection system is also applied for the present invention).
UV disinfection system is purchased from Te Jiean companies, model PRO10 in the embodiment of the present invention.Ultraviolet ray disinfecting system is set
It is standby should include ultraviolet ray disinfector, it is power distribution control system, uv dosage on-line detecting system, on-line auto-cleaning system, automatic
Change monitoring system.It is existing known for tap water ultraviolet disinfection in this field other than the UV disinfection system
Ultraviolet system is suitable for the present invention.
3, hyperfiltration treatment
Aqueous by ultraviolet treatment with irradiation flows into immersed ultrafiltration membrane pond, carries out super-filtration purifying processing, wherein ultrafiltration
The membrane material of film is PVC, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 1.0/2.0mm.Membrane flux 45LMH, membrane area 30m2,
Water temperature is 10 DEG C (being usually 0-40 DEG C, preferably 0-30 DEG C), and the operating pressure 0.03MPa of ultrafiltration membrane treatment (is usually 0.03-
0.06MPa)；Physical cleaning and chemical cleaning are carried out in process of ultrafiltration treatment, wherein：Physical cleaning period 120min is (usually
For 30-120min), physical cleaning carries out for air purge and water recoil joint, wherein：Water backwash intensity 1.2m3/ h (is usually 1.2-
1.8m3/ h), the water backwashing time is 60s/ times (being usually 30-120s/ times)；Air purge intensity is 0.055m3/min(0.055-
0.080m3/ min), air purge time 60s/ times (being usually 30-120s/ times)；Chemical cleaning medicament NaClO (be usually NaClO,
HCl, citric acid or NaOH), medicament cleans concentration 200ppm (being usually 100-2000ppm), and 90 days chemical cleaning periods are (usually
It is 30-90 days/time), the chemical cleaning time is 2-3h/ times (being usually 2-12h/ times)；
In the embodiment of the present invention in ultrafiltration membrance filter processing ultrafiltration membrane material by taking membrane aperture is 0.01 μm of PVC film as an example into
Row explanation, it is as known in the art, any for water treatment ultrafiltration membrane (such as membrane material be PVDF, PVDF reinforcement etc.,
Membrane aperture is 0.01-0.1 μm) it is suitable for the present invention.
4, chlorination is handled
Sodium hypochlorite is added in being discharged to ultrafiltration membrane pool, dosage is that 2mg/L (adds sodium hypochlorite in i.e. every 1L water
2mg), it is added after sodium hypochlorite being configured to the liquor natrii hypochloritis that mass percent concentration is 10%, toss area is respectively clear
Pond water inlet (throw chlorine point) and clear water reserviors water outlet (mending chlorine point), water temperature be 10 DEG C (usually 0-40 DEG C, preferably 0-30
DEG C), subsequently into clear water reserviors, fully reaction disinfection, residence time in clear water reserviors>2h, when water outlet according to residual chlorine amount in water into
Row mends chlorine, mends chlorine dose 0-1mg/L so that output water contents of residual chlorine reaches 0.7-1.0mg/L, obtains and goes out for the water supply plant drunk
Factory's water.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.015 CODMn(mg/L)：0.5-1.2 pH：7.80-8.10
Fe(mg/L)：<0.30 Al(mg/L)：<0.01
The dosage of sodium hypochlorite is illustrated by taking 2mg/L as an example in chlorination processing in the embodiment of the present invention, other are certainly
The sodium hypochlorite dosage (such as 1-10mg/L) for carrying out water factory's chlorination processing is suitable for the present invention.
Embodiment 2
1, raw water pre-treatment
Raw water passes through potassium permanganate composites, quartzy sand filter successively, carries out coagulating kinetics, sand filtration treatment successively；
Wherein, the dosage of the potassium permanganate composites dosing coagulant ferric trichloride of coagulating kinetics, coagulant is 10-50mg/L, is mixed
Solidifying processing time is 90min, and water temperature is 20 DEG C；Quartz sand filter period 24-36h (being usually 16-36h), filtering rate
For 8.45m/h (being usually 2-15m/h, preferably 8-9m/h)；The backwash intensity 15L/m of quartzy sand filter2S (is usually 12-
19L/m2·s)；
Effluent quality after quartz sand filter according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.50 CODMn(mg/L)：<2.0 pH：7.50-8.50
Fe(mg/L)：<0.30 Al(mg/L)：<0.01
2, ultraviolet irradiation is handled
Water outlet after the adsorption filtration of charcoal sand is entered to the cavity type ultraviolet disinfection of waterworks water process by water pump
System, quartz sand filtration water outlet flow through UV disinfection system, and ultraviolet generator is discharged filtering and carries out ultraviolet treatment with irradiation,
Middle-ultraviolet lamp exposure dose is 80mJ/cm2；20 DEG C of water temperature；Water velocity is 0.5m/s；The ultraviolet treatment with irradiation time is 1s.
3, hyperfiltration treatment
Aqueous by ultraviolet treatment with irradiation flows into ultrafiltration membrane pool, carries out super-filtration purifying processing, the wherein film of ultrafiltration membrane
Material is PVC, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 1.0/2.0mm.Membrane flux 45LMH, membrane area 30m2, water temperature is
20 DEG C, the operating pressure of ultrafiltration membrane treatment is 0.04MPa；Physical cleaning and chemical cleaning are carried out in process of ultrafiltration treatment,
In：Physical cleaning period 120min (being usually 30-120min), physical cleaning carry out for air purge and water recoil joint, wherein：Water
Backwash intensity 1.2m3/ h (is usually 1.2-1.8m3/ h), backwash time 60s/ times；Air purge intensity is 0.055m3/min(0.055-
0.080m3/ min), air purge time 60s/ times；Chemical cleaning medicament NaClO (being usually NaClO, HCl, citric acid or NaOH),
Medicament cleans concentration 400ppm, 80 days chemical cleaning periods (being usually 30-90 days/time)；
4, chlorination is handled
Sodium hypochlorite is added in being discharged to ultrafiltration membrane pool, dosage is that 5mg/L (adds sodium hypochlorite in i.e. every 1L water
5mg), concentration 10% is added, toss area is respectively clear water reserviors water inlet (throwing chlorine point) and clear water reserviors water outlet (mending chlorine point), water temperature
It is 20 DEG C, subsequently into clear water reserviors, fully reaction disinfection, residence time in clear water reserviors>2h, according to residual chlorine amount in water when water outlet
Benefit chlorine is carried out, chlorine dose 0-1mg/L is mended so that output water chlorine residue 0.7-1.0mg/L obtains the water supply plant output water for drinking.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.015 CODMn(mg/L)：0.5-1.2 pH：7.80-8.10
Fe(mg/L)：<0.30 Al(mg/L)：<0.01
Embodiment 3
1, raw water pre-treatment
Raw water passes through combined shaft, mechanical accelerating purifying pool, quartzy sand filter successively；Coagulating kinetics, stone are carried out successively
Sand filtration treatment, wherein dosing coagulant aluminium polychloride in combined shaft during coagulating kinetics, the dosage of coagulant
For 10-40mg/L；Mechanical accelerating purifying pool total residence time 90min, i.e. coagulating treatment time are 90min；Water temperature is 30 DEG C；Stone
Sand filter period 16-24h；Filtering rate is 8.45m/h (being usually 2-10m/h)；The backwash intensity of quartzy sand filter
12-19L/m2·s；
Effluent quality after quartz sand filtration according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.50 CODMn(mg/L)：<2.0 pH：7.50-8.50
Fe(mg/L)：<0.05 Al(mg/L)：<0.20
2, ultraviolet irradiation is handled
Water outlet after quartz sand filtration is entered to the open tunnel type ultraviolet disinfection system of waterworks water process by water pump
System (i.e. quartz sand filtration water outlet flows through conveyance canal), open tunnel type UV disinfection system uses modularized design, each ultraviolet disinfection
Module is by stainless steel lamp bracket, several ultraviolet lamp tubes, high-transmission rate quartz socket tube, automatic cleaning system, distribution system and data
Acquisition system forms.Its middle-ultraviolet lamp generating system is installed in conveyance canal, and the water body to flowing through conveyance canal is irradiated disinfection.
Quartz sand filtration water outlet flows through conveyance canal, and ultraviolet lamp, which is discharged filtering, carries out ultraviolet treatment with irradiation, and middle-ultraviolet lamp irradiates agent
Amount is 60mJ/cm2；30 DEG C of water temperature；Water velocity is 0.5m/s；The ultraviolet treatment with irradiation time is 1.5s (being usually 1-2s).
3, hyperfiltration treatment
Aqueous by ultraviolet treatment with irradiation flows into immersed ultrafiltration membrane pond, carries out super-filtration purifying processing, wherein ultrafiltration
The membrane material of film is PVDF, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 1.0/2.0mm.Membrane flux 45LMH, membrane area
30m2, water temperature is 30 DEG C, and the operating pressure of ultrafiltration membrane treatment is 0.035MPa；In process of ultrafiltration treatment carry out physical cleaning and
Chemical cleaning, wherein：Physical cleaning period 90min (be usually 30-120min), physical cleaning is air purge and water recoil combine into
Row, wherein：Water backwash intensity 1.2m3/ h (is usually 1.2-1.8m3/ h), it (is usually 30-60s/ that the backwash time, which is 60s/ times,
It is secondary)；Air purge intensity is 0.055m3/min(0.055-0.080m3/ min), air purge time 60s/ times (being usually 30-60s/ times).
Chemical cleaning medicament NaOH (being usually NaClO, HCl, citric acid or NaOH), medicament clean concentration 500ppm, chemical cleaning week
90 days/time of phase；
4, chlorination is handled
Sodium hypochlorite is added in being discharged to ultrafiltration membrane pool, dosage is that 2mg/L (adds sodium hypochlorite in i.e. every 1L water
2mg), that is, concentration 10% is added, toss area is respectively clear water reserviors water inlet (throwing chlorine point) and clear water reserviors water outlet (mending chlorine point), water
Temperature is 30 DEG C (being usually 0-40 DEG C, preferably 0-30 DEG C), and subsequently into clear water reserviors, fully reaction disinfection, stops in clear water reserviors
Stay the time>2h；Benefit chlorine is carried out according to residual chlorine amount in water when water outlet, mends chlorine dose 0-1mg/L so that output water chlorine residue 0.7-1.0mg/
L obtains the water supply plant output water for drinking.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.015 CODMn(mg/L)：0.5-1.2 pH：7.80-8.10
Fe(mg/L)：<0.05 Al(mg/L)：<0.20
Embodiment 4
1, raw water pre-treatment
Raw water passes through combined shaft, mechanical accelerating purifying pool, quartzy sand filter successively；Coagulating kinetics, stone are carried out successively
Sand filtration treatment, wherein the dosage of dosing coagulant aluminium polychloride in combined shaft, coagulant is 20mg/L；Machinery accelerates
Clarifying basin total residence time 90min, i.e. coagulating treatment time are 90min；Water temperature is 5 DEG C；Quartz sand filter period 24-
36h, filtering rate 8.45m/h；The backwash intensity 15L/m of quartz sand2·s；
Effluent quality after quartz sand filtration according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.50 CODMn(mg/L)：<2.0 pH：7.50-8.50
Fe(mg/L)：<0.05 Al(mg/L)：<0.20
2, ultraviolet irradiation is handled
Water outlet after the adsorption filtration of charcoal sand is entered to the cavity type ultraviolet disinfection of waterworks water process by water pump
System, quartz sand filtration water outlet flow through UV disinfection system, and ultraviolet generator is discharged adsorption filtration and carries out at ultraviolet light irradiation
Reason, wherein ultraviolet irradiating dose are 40mJ/cm2；30 DEG C of water temperature；Water velocity is 2m/s；The ultraviolet treatment with irradiation time is
0.1s。
3, hyperfiltration treatment
Aqueous feed pressure formula (internal pressure) ultrafiltration membrane pool by ultraviolet treatment with irradiation carries out super-filtration purifying processing,
The membrane material of middle ultrafiltration membrane is PVDF, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 0.7/1.3mm.Membrane flux 45LMH, film surface
Product 50m2, water temperature is 5 DEG C (being usually 0-40 DEG C, preferably 0-30 DEG C), and the operating pressure of ultrafiltration membrane treatment is 0.07MPa (logical
It is often 0.01-0.15MPa, preferably 0.05-0.09MPa)；Physical cleaning and chemical cleaning are carried out in process of ultrafiltration treatment,
Wherein：Physical cleaning period 50min, physical cleaning carry out for air purge and water recoil joint, wherein：Water backwash intensity is 2.5m3/
H (is usually 2.5-4m3/ h), backwash takes 60s/ times (being usually 30-60s/ times)；Air purge intensity is 0.055m3/min
(0.055-0.080m3/ min), air purge time 60s/ times (being usually 30-60s/ times)；Chemical cleaning medicament NaOH is (usually
NaClO, HCl, citric acid or NaOH), medicament cleaning concentration 500ppm, 90 days chemical cleaning periods (usually 30-90 days/
It is secondary)；
4, chlorination is handled
Sodium hypochlorite is added in being discharged to ultrafiltration membrane pool, dosage is that 2mg/L (adds sodium hypochlorite in i.e. every 1L water
2mg), concentration 10% is added, toss area is respectively clear water reserviors water inlet (throwing chlorine point) and clear water reserviors water outlet (mending chlorine point), water temperature
It is 30 DEG C, subsequently into clear water reserviors, fully reaction disinfection, residence time in clear water reserviors>2h, according to residual chlorine amount in water when water outlet
Benefit chlorine is carried out, chlorine dose 0-1mg/L is mended so that output water chlorine residue 0.7-1.0mg/L obtains the water supply plant output water for drinking.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.015 CODMn(mg/L)：0.5-1.2 pH：7.50-8.10
Fe(mg/L)：<0.05 Al(mg/L)：<0.20
Embodiment 5
1, raw water pre-treatment
Raw water passes through combined shaft, mechanical accelerating purifying pool, quartzy sand filter, ozone contact tank, activated carbon filter successively, according to
Secondary progress coagulating kinetics, quartz sand filtration processing, ozone Oxidation Treatment, activated carbon adsorption filtration treatment；Wherein, coagulation is heavy
Shallow lake uses ferric trichloride and aluminium polychloride for coagulant, and the dosage of ferric trichloride is 10-40mg/L, the dosage of aluminium polychloride
For 5-10mg/L；Mechanical accelerating purifying pool total residence time 90min (i.e. the coagulating treatment time is 90min)；Water temperature is 10 DEG C；Stone
Sand filter period 24-36h, filtering rate 8.45m/h；The backwash intensity 15L/m of quartzy sand filter2·s；Ozone oxygen
The dosage for changing ozone in processing procedure is 0.5mg/L, and ozone contact time 12min, water temperature is 10 DEG C；Activated carbon filter mistake
Filter period 36-48h；Time of contact is 12.8min, the backwash intensity 19L/m of activated carbon filter2S (is usually 12-19L/m2·
s)。
Effluent quality after activated carbon adsorption according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.30 CODMn(mg/L)：<1.8 pH：7.50-8.50
Fe(mg/L)：<0.30 Al(mg/L)：<0.20
2, ultraviolet irradiation is handled
Disappear the cavity type for entering by water pump waterworks water process by the filtered water outlet of activated carbon adsorption is ultraviolet
Malicious system, activated carbon adsorption filter out water and flow through UV disinfection system, and ultraviolet generator is discharged adsorption filtration and carries out ultraviolet light
Treatment with irradiation, wherein control ultraviolet irradiating dose is 40mJ/cm2；Water temperature is 10 DEG C；Water velocity is 0.5m/s；Ultraviolet light
The treatment with irradiation time is 1s (being usually 0.1-1s).
3, hyperfiltration treatment
Aqueous by ultraviolet treatment with irradiation flows into ultrafiltration membrane pool, carries out super-filtration purifying processing, the wherein film of ultrafiltration membrane
Material is PVDF, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 1.0/2.0mm.Membrane flux 45LMH, membrane area 50m2, water temperature
For 10 DEG C (being usually 0-40 DEG C, preferably 0-30 DEG C), the operating pressure of ultrafiltration membrane treatment is 0.03MPa；In hyperfiltration treatment mistake
Physical cleaning and chemical cleaning are carried out in journey, wherein：Physical cleaning period 90min (being usually 30-120min), physical cleaning is
Air purge and water recoil joint carry out, wherein：Water backwash intensity 1.2m3/ h (is usually 1.2-1.8m3/ h), the water backwashing time is
60s/ times；Air purge intensity is 0.055m3/ min, air purge time 60s/ times；Chemical cleaning medicament NaClO (be usually NaClO,
HCl, citric acid or NaOH), medicament cleans concentration 200ppm, 90 days chemical cleaning periods (being usually 30-90 days/time)；
4, chlorination is handled
Sodium hypochlorite is added in being discharged to ultrafiltration membrane pool, dosage 2mg/L adds concentration 10%, and toss area is respectively
Clear water reserviors water inlet (throw chlorine point) and clear water reserviors water outlet (mending chlorine point), water temperature be 10 DEG C (usually 0-40 DEG C, preferably 0-30
DEG C), subsequently into clear water reserviors, fully reaction disinfection, residence time in clear water reserviors>2h, when water outlet according to residual chlorine amount in water into
Row mends chlorine, mends chlorine dose 0-1mg/L so that output water chlorine residue 0.7-1.0mg/L obtains the water supply plant output water for drinking.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.015 CODMn(mg/L)：0.5-1.2 pH：7.80-8.10
Fe(mg/L)：<0.30 Al(mg/L)：<0.20
The ultrafiltration membrane process of 1 regular tap water treatment process of reference examples
1, raw water pre-treatment
Raw water passes through combined shaft, mechanical accelerating purifying pool, quartzy sand filter, ozone contact tank, activated carbon filter successively, according to
Secondary progress coagulating kinetics, quartz sand adsorption filtration processing, ozone Oxidation Treatment, activated carbon adsorption filtration treatment；Wherein, it mixes
Retrogradation shallow lake uses ferric trichloride and aluminium polychloride for coagulant, and the dosage of ferric trichloride is 10-40mg/L, aluminium polychloride
Dosage is 5-10mg/L；Mechanical accelerating purifying pool total residence time 90min；Water temperature is 10 DEG C；Quartz sand filter period 24-
36h, filtering rate are 8.45m/h (being usually 2-15m/h)；The backwash intensity 15L/m of quartzy sand filter2S (is usually 12-
19L/m2·s)；The dosage of ozone is 0.5mg/L during ozone Oxidation Treatment, and ozone contact time is that 12min (is usually
5-12min), water temperature is 10 DEG C；Activated carbon filter 36-48h filter cycle；Time of contact is that 12.8min (is usually 2-
20min), the backwash intensity 19L/m of activated carbon filter2S (is usually 12-19L/m2·s)。
After activated carbon adsorption effluent quality according to《People's Republic of China's tap water quality national standard》
(GB5749-2006) it is monitored, measurement result is as follows：
Turbidity (NTU)：<0.30 CODMn(mg/L)：<1.8 pH：7.50-8.50
Fe(mg/L)：<0.30 Al(mg/L)：<0.20
2, hyperfiltration treatment
Aqueous by activated carbon adsorption filtration treatment flows into immersed ultrafiltration membrane pond, carries out super-filtration purifying processing, wherein
The membrane material of ultrafiltration membrane is PVDF, and 0.01 μm of membrane aperture, film wire inner/outer diameter is 1.0/2.0mm.Membrane flux 45LMH, membrane area
50m2, water temperature is 10 DEG C, and ultrafiltration membrane exports operating pressure 0.05MPa；Physical cleaning and chemistry are carried out in process of ultrafiltration treatment
Cleaning, wherein：Physical cleaning period 30min (be usually 30-60min/ time), physical cleaning is air purge and water recoils combine into
Row, wherein：Water backwash intensity 1.8m3/ h (is usually 1.5-1.8m3/ h), the water backwashing time is 60s/ times；Air purge intensity is
0.080m3/min(0.07-0.080m3/ min), air purge time 60s/ times；Chemical cleaning medicament NaClO+ citric acids are (usually
NaClO, HCl, citric acid or NaOH), after first being cleaned with NaClO, then with citric acid cleaning, it is (logical that medicament cleans concentration 2000ppm
It is often 1000-2000ppm), 30 days/time of the chemical cleaning period (being usually 30-45 days/time)；
In order to reach identical treatment effect, needing frequently to carry out physics, chemical cleaning, physics, chemical cleaning period are short,
Wherein the physical cleaning period is usually 30-60min/ times；And water backwash intensity is high in physics, usually 1.5-1.8m3/h；Gas
It is 0.07-0.080m to wash intensity3/min.The chemical cleaning period is usually 30-45 days/time；And chemical cleaning medicament is dense
Degree is high, usually 1000-2000ppm.
And physical, chemical cleaning period are long during ultrafiltration membrane treatment in the method for the present invention, wherein physical cleaning is all
Phase is usually 30-120min/ times, preferably 90-120min/ times；And water backwash intensity is high in physics, usually 1.2-
1.8m3/h；Air purge intensity is 0.055-0.080m3/min.The chemical cleaning period is usually 30-90 days/time, preferably 60-90
Day/time；And the concentration of chemical cleaning medicament is high, usually 100-2000ppm, preferably≤500ppm, preferably 200-
500ppm。
3, ultraviolet disinfection is handled
Water outlet after hyperfiltration treatment is pumped into the cavity type UV disinfection system of waterworks water process by water pump,
Hyperfiltration treatment water outlet flows through UV disinfection system, and ultraviolet generator is discharged adsorption filtration and carries out ultraviolet treatment with irradiation, wherein
Control ultraviolet irradiating dose is 40mJ/cm2；Water temperature is 10 DEG C；Water velocity is 0.5m/s；The ultraviolet treatment with irradiation time is
1s (being usually 0.1-1s).
4, chlorination is handled
Sodium hypochlorite is added into the water outlet after ultraviolet disinfection, dosage 2mg/L adds concentration 10%, toss area point
Not Wei clear water reserviors water inlet (throw chlorine point) and clear water reserviors water outlet (mending chlorine point), water temperature be 10 DEG C (usually 0-40 DEG C, preferably
0-30 DEG C), subsequently into clear water reserviors, fully reaction disinfection, residence time in clear water reserviors>2h, according to chlorine residue in water when water outlet
Amount carries out benefit chlorine, mends chlorine dose 0-1mg/L so that output water chlorine residue 0.7-1.0mg/L obtains the water supply plant manufacture for drinking
Water.
Clear water reserviors effluent quality according to《People's Republic of China's tap water quality national standard》(GB5749-2006) it carries out
Monitoring, measurement result are as follows：
Turbidity (NTU)：0.003-0.025 CODMn(mg/L)：0.80-1.60 pH：7.80-8.10
Fe(mg/L)：<0.30 Al(mg/L)：<0.20
Reference examples 2
With the blank ultrafiltration membrane without any processing used in embodiment 1-5,1 ultrafiltration membrane pool of reference examples, as a contrast
Example 2.
1 ultrafiltration membrane surface organic pollution of test example, microorganism detection
Laser scanning co-focusing fluorescence microscope (LSCM) is a kind of to be obtained using computer, laser and image processing techniques
The analytical instrument of biological sample three-dimensional data, at present state-of-the-art molecular cytobiology.It is mainly used for observing living cells structure
And the biology variation of specific molecular, ion, quantitative analysis and real-time quantitative measurement etc..Specific detection operating method is as follows：
Ultrafiltration membrane in embodiment 5, the ultrafiltration membrane pool of reference examples 1 is run 20 days, is taken out ultrafiltration membrane film wire, is randomly selected
The film wire sample of film wire 6, every 10-20cm, the both ends of clip film wire and intermediate each about 2cm long, in room temperature (25 DEG C) darkroom
Lower to instill film surface with SYTO63 solution, room temperature shakes 30min, uses NaHCO3Buffer solution (0.1M) instills film surface；Again will
FITC solution (10g/L) instills film surface, places 1h at room temperature；ConA solution (0.2g/L) is instilled into film surface again, in room
Temperature is lower to place 30min；Calcofluor white solution is instilled into film surface again, places 30min at room temperature；It is buffered with PBS
Solution remove excess stain agent after, immediately use Lycra laser confocal scanning microscope (Lycra SP5 laser co-focusing systems,
Germany) observation of taking pictures is carried out to the film wire after dyeing.The excitation/emission wavelength of Calcofluor white is 400/410-
480nm (blue)；The excitation/emission wavelength of FITC probes is 488/500-540nm (green)；The excitation/emission wavelength of ConA
For 543/550-600nm (being selected as carmetta)；The corresponding excitation/emission wavelength 633/650-700nm (red) of SYTO63.Choosing
It selects one of sample constant brightness and no longer carries out brightness regulation later, to ensure to observe point of pollutant under conditions of unification
Cloth and quantization content situation.
The calculating for being carried out brightness value to collected picture using Matlab2015b platforms, is reacted each by brightness value
The content situation of a pollutant.It is first passed through headed by detailed process in Matlab2015b and reads picture from tape function imread, will schemed
Piece is converted into three-dimensional data, then obtained three-dimensional array is converted to two-dimensional array, later according to the calculating function of brightness again into
The brightness calculation of each point of row, the brightness that the brightness value of obtained each point progress average computation is finally obtained to picture are averaged
Value.
LSCM Observe and measures result is as shown in Fig. 2,3,4,5, wherein the protein organic contamination of ultrafiltration membrane surface is in laser
It scans under confocal fluorescent microscopic in green；In blue under the LSCM of β-polysaccharide organic pollution；α-polysaccharide organic pollution
It is in carmetta under LSCM；It takes on a red color under the LSCM of microbial contamination.Each point in figure is calculated into obtain brightness according to three primary colors rgb value
Value, counts and obtains mean fluorecence brightness value as shown in table 1,2.
Fig. 2 is the LSCM observation charts of the protein organic contamination of ultrafiltration membrane surface, and wherein a is embodiment 5, and b is reference examples
1；Fig. 3 is the LSCM observation charts of β-polysaccharide organic pollution of ultrafiltration membrane surface, and wherein a is embodiment 5, and b is reference examples 1；Fig. 4 is
The LSCM observation charts of the α of ultrafiltration membrane surface-polysaccharide organic pollution, wherein a are embodiment 5, and b is reference examples 1；Fig. 5 is ultrafiltration membrane
The LSCM observation charts of surface microorganism pollution, wherein a are embodiment 5, and b is reference examples 1.
The LSCM image fluorescent brightness result of calculations of 1 ultrafiltration membrane surface organic pollution of table
By Fig. 2-4, table 1 can be seen that：The protein of ultrafiltration membrane surface and β-polysaccharide organic pollutant subtract in embodiment 5
It is few, it is 14.8881 and 8.6803 respectively in fluorescent brightness value, is significantly lower than the protein of the ultrafiltration membrane surface of reference examples 1
It is 19.124 and 13.1313 respectively in fluorescent brightness value with β-polysaccharide organic pollution；It is attached with ultrafiltration membrane surface microorganism
It, biology starts high molecular polymer that metabolic secretion goes out, being wrapped in outside cell wall, i.e. Extracellular polymers (EPS).EPS master
There is an exoprotein, exocellular polysaccharide, DNA, the compositions such as lipid make fouling membrane degree become serious.
Ultraviolet processing can be such that the microbial contamination degree of ultrafiltration membrane surface reduces, therefore EPS (such as protein of film surface
And polysaccharide) quantity can also reduce；Protein and polysaccharide in addition, ultraviolet light processing can degrade in membrane cisterna water inlet etc. have
Machine object so that the organic contamination degree in film wire mitigates.
It can be seen that the control effect of protein of the ultraviolet processing to film surface, α-polysaccharide and β-polysaccharide organic object is preferable.
Ultraviolet processing has the organic pollution of ultrafiltration membrane surface certain control action, especially to protein and β-polysaccharide organic object
Control.
The LSCM image fluorescent brightness result of calculations of 2 ultrafiltration membrane surface microbial contamination of table
By Fig. 5, table 2 can be seen that：The ultrafiltration membrane surface fluorescent brightness highest of reference examples 1, and film surface red is uneven,
And brightness higher position almost joins together；The ultrafiltration membrane surface fluorescent brightness value of embodiment 5 is very low, and only 2.4910, it is red
Fluorescence is simultaneously uneven, is in spot block distribution.
It is ultraviolet to make cell by destroying genetic stew (DNA DNA and the Ribonucleic RNA) of microorganism
Fertility is lost, death is eventually led to；As it can be seen that ultraviolet have bactericidal effect, there is inhibition bacterium in the process with ultrafiltration membrane combination
In the effect of film surface growth, there is control action to the microbial contamination of ultrafiltration membrane surface.
2 ultrafiltration membrane surface inorganic pollution analyte detection of test example
The inorganic pollution of ultrafiltration membrane surface is detected using scanning electron microscope (SEM) method, the specific method is as follows：
The ultrafiltration membrane of embodiment 5 after running 20 days, reference examples 1, reference examples 2 is distinguished into vacuum dried processing for 24 hours, so
SEM is used to observe film surface pollution object morphosis afterwards；Scanning electron microscope is FEI Quanta 200FEG Flied emission scanning electron microscopies
Mirror.
Scanning electron microscope (SEM) testing result as shown in fig. 6, wherein 6a be embodiment 5 handle 20 days after ultrafiltration membrane surface
Inorganic pollution SEM image；6b is the SEM image of the inorganic pollution of the ultrafiltration membrane surface after reference examples 1 are handled 20 days；
6c is the SEM image of 2 blank ultrafiltration membrane of reference examples.Aqueous is shone by ultraviolet light in the embodiment of the present invention 5 known to being shown in figure
After penetrating processing, then hyperfiltration treatment is carried out, ultrafiltration membrane film wire surface is also relatively cleaner, pollutes obviously than reference examples 1 (i.e. without ultraviolet
Processing) ultrafiltration membrane surface it is few.
Ultrafiltration film surface is measured using energy depressive spectroscopy (2000 X-ray energy disperse spectroscopies (EDS) of model EDAX Genesis)
The front and back element composition of pollution, analysis result are as shown in table 3.
3 ultrafiltration film surface inorganic pollution EDAX results of table
As shown in Table 3：
1, the blank ultrafiltration membrane of reference examples 2 is mainly tri- kinds of elements of C, O and Cl, this is the main composition of PVC material film.Table
In it can be seen that, the EDAX results of embodiment 5 are close with blank film EDAX results, element composition approach；
2 and the EDAX results of reference examples 1 are shown, except film process C, O and tri- kinds of elements of Cl, also largely containing Fe,
Al, Ca, S, K and Si show that the ultrafiltration membrane surface pollutant without ultraviolet processing is more.
It can be seen that ultraviolet, treated that ultrafiltration membrane surface is cleaner, and ultraviolet processing is so that film surface Fe, Al, Ca, S, K and Si
Equal inorganic pollutions substantially reduce.
The analysis detection of 3 ultrafiltration membrane surface biology community structure of test example
Sample entrusts Shanghai Major Biological Medical Technology Co., Ltd. to detect.The specific method is as follows：
It is run 20 days in the ultrafiltration membrane of embodiment 5, reference examples 1, takes out film wire, randomly select film wire 6, every 10-
20cm；It takes 500ml sterile waters to rinse film surface sludge repeatedly respectively, collects muddy water mixed solution in clean sterile centrifuge tube
In, 4 DEG C, 12000r/min, centrifuge 10min.It abandons supernatant, after mixing sediment, the fresh sediments of 1g is taken to carry out carrying for DNA at once
It takes；
DNA extractions, specific steps are carried out using mp kits：500mg samples are added to Lysing Matrix E Tube,
978 μ l Sodium Phosphate Buffer and 122 μ l MT Buffer are added；The mixing 40s in Fastprep instruments；
14000XG centrifuges Lysing Matrix E Tubes 5-10min；Supernatant is transferred in a clean pipe of 2ml.It is added
250 μ lPPS reagents and mixing, shake with hands pipe 10 times；14000XG centrifuges 5min precipitations, and supernatant is transferred to one totally
15ml pipes in.1ml Binding Matrix Suspension are added in supernatant；It is placed on a circulator or by hand reversion
2min, allows DNA binding matrix.Pipe is put and stands 3min on frame, silica matrix is allowed to precipitate；500 μ l supernatants of careful removal, avoid
Meet the Binding Matrix of precipitation.Abandon supernatant.Binding Matrix are resuspended in remaining liquid.By about 600 μ l
Mixture be transferred to SPINTMFilter, 14000XG centrifuge 1min.Catch Tube are emptied, and remaining supernatant is added
To SPINTMCentrifugal filtration in Filter；Add 500 μ l SEWS-M to SPINTMFilter, 1min is in 14000XG for centrifugation.
Go out to flow through liquid and SPINTMFilter puts back to Catch Tube.14000XG centrifuges 2min, in clear dry SPINTMIn Filter
Remaining SEWS-M；Mobile SPINTMFilter air-dries 5min at room temperature to new Catch Tube；50-100 μ l DES are added
Resuspension gently is gently agitated for filter membrane and is flicked with pipette tips or finger, is resuspended and elutes silica matrix for efficient DNA.
14000XG centrifuges 1min, shifts DNA to the Catch Tube of elution.
Detect program：After genome DNA extraction, DNA is detected with 1% agarose gel electrophoresis.Using primer 515F_
907R carries out 16S rRNA gene pyramidings enzyme chain reaction (PCR) and expands.Whole samples are carried out according to formal experiment condition, each
3 repetitions of sample are detected after mixing the PCR product of same sample with 2% agarose gel electrophoresis, solidifying using AxyPrepDNA
Plastic recovery kit (AXYGEN companies) gel extraction PCR product, Tris_HCl elutions；2% agarose electrophoresis detects.With reference to electricity
It swims preliminary quantitative result, by PCR product QuantiFluorTM- ST blue-fluorescences quantitative system (Promega companies) is examined
Measured quantity utilizes Illumina Miseq later according to the requirement of the sequencing amount of each sample after carrying out the mixing of corresponding proportion
PE300 platforms carry out subsequent high pass amount sequencing analysis.
The biology of microbe colony after measurement embodiment 5,1 ultrafiltration membrane of reference examples are run 20 days in ultrafiltration membrane film surface is more
Sample, measurement result are as follows：
1, community diversity index
The diversity indices of 4 film surface pollutant sample of table
The diversity of microorganism can analyze reflection microbiologic population by the diversity (Alpha diversity) of single sample
Abundance and diversity, sobs indexes and ace indexes reflection group's richness (Community richness),
Shannoneven indexes reflect community evenness (Community evenness), and coverage indexes and simpson indexes are anti-
Reflect community diversity (Community diversity).
As can be seen from Table 4, the coverage indexes (coverage rate) of sample illustrate sample compared with Gao Jun 99.7% or more
The gene order measured can really reflect the biocenological feature of sample.Referred to using the Sob indexes and Ace of characterization group richness
Number estimates maximum OUT numbers, finds group's sum apparent less, Sobs indexes and the Ace indexes of ultraviolet-ultrafiltration membrane surface
Only it is the 30% of ultrafiltration.Simpson indexes reflect microbe species, and Simpson indexes are bigger to illustrate that microbe species are fewer.
As can be seen from the table, the Simpson indexes of ultraviolet-ultrafiltration (embodiment 5) are apparently higher than reference examples 1 (ultrafiltration).
As it can be seen that ultraviolet can inhibit film surface microbial contamination, film surface microbial count and type is made all to significantly reduce,
Wherein microorganism total amount reduces 30%.
2, species composition is analyzed
Venn schemes (Fig. 7), can be used for counting species (such as OTU) number common and exclusive in multigroup or multiple samples,
Species (such as OTU) the number compositional similarity and overlapping cases of environmental samples can more intuitively be showed.Under normal conditions, divide
The sample table for the OTU or other taxology level that similar level is 97% is selected when analysis.Venn figures are based on Shanghai Mei Ji biologies
Pharmaceutical Technology Co., Ltd automatically generates the detection data of sample on the data platform that the said firm provides.
It is intuitive anti-by Venn figures in order to illustrate the difference of microbiologic population between 1 two embodiment 5, reference examples samples
It reflects.Common to Fig. 7 has been counted in 1 two embodiment 5, reference examples samples and exclusive category kind number, it is demonstrated by two samples
Compositional similarity and overlapping cases.As shown in Figure 7, the ultrafiltration membrane micro- life in (ultrafiltration membrane without ultraviolet processing) surface of reference examples 1
The category kind of object is 208, and ultrafiltration membrane (i.e. the ultrafiltration membrane after ultraviolet processing) surface of embodiment 5 belongs to kind and significantly reduces, only
120, the two lap is 102.As it can be seen that retaining 49.0% micro- life by ultraviolet treated ultrafiltration membrane surface microorganism
Species group, and there is 50.9% to be got rid of by ultraviolet, illustrate that the ultraviolet type to ultrafiltration membrane surface microorganism has certain control to make
With.
4 ultrafiltration membrane transmembrane pressure of test example is analyzed
TMP is an important indicator of ultrafiltration membrane operation, that is, refers to ultrafiltration membrane intake pressure and produce the difference between water pressure,
It is the motive force for completing membrane filtration.TMP increases the raising for the energy consumption that ultrafiltration membrane can be caused to run, and operating cost also rises therewith
It is high.The transmembrane pressure (TMP) of ultrafiltration membrane is measured using pressure sensor, i.e., pressure sensor is installed in ultrafiltration membrane water outlet pipe part
Probe measures membrane module discharge pressure instantaneous value, and the difference of ultrafiltration membrane pool liquid level (steady state value) is TMP, unit kpa.Difference
Value storage takes a TMP in pressure sensor, per 60min.Pressure sensor has display screen, can site setup detection frequency etc.
Parameter can also be extracted from USB flash disk interface by data.
The transmembrane pressure of ultrafiltration membrane, measurement result such as Fig. 8 institutes are measured the ultrafiltration membrane of the embodiment of the present invention 5, reference examples 1
Show.
As shown in Figure 8, the transmembrane pressure average value of ultrafiltration membrane is 13.8kPa in the embodiment of the present invention 5, is surpassed in reference examples 1
The transmembrane pressure of filter membrane is 24.4kPa, is significantly higher than the transmembrane pressure of ultrafiltration membrane of the present invention.This is because by ultraviolet processing,
The fouling membrane (including inorganic pollution, organic contamination and microbial contamination) of ultrafiltration membrane is substantially reduced in embodiment 5, keeps TMP relatively low.
Claims (10)
1. a kind of processing method of tap water, characterized in that including carrying out ultraviolet treatment with irradiation, ultrafiltration to raw water of waterworks
Processing, chlorination processing.
2. processing method as described in claim 1, characterized in that control ultraviolet light during the ultraviolet treatment with irradiation and shine
It is 40-300mJ/cm to penetrate dosage2, preferably 40-100mJ/cm2。
3. processing method as claimed in claim 1 or 2, characterized in that control flow during the ultraviolet treatment with irradiation
Temperature be 0-40 DEG C, preferably 0-30 DEG C；Control flow rate of water flow is 0.1-3m/s, preferably 0.5-2m/s.
4. processing method as claimed in claim 1 or 2, characterized in that the membrane aperture of ultrafiltration membrane in the process of ultrafiltration treatment
It is 0.01-0.1 μm.
5. processing method as claimed in claim 1 or 2, characterized in that control is in hyperfiltration treatment in the process of ultrafiltration treatment
Pressure is 0.01-0.15MPa.
6. processing method as claimed in claim 1 or 2, characterized in that the pre-treatment includes carrying out coagulating sedimentation to raw water
It is one or more in processing, ozone Oxidation Treatment, adsorption filtration processing, filtration treatment.
7. processing method as claimed in claim 1 or 2, characterized in that the chlorination processing is after ultrafiltration membrane treatment
Sodium hypochlorite is added in water outlet.
8. a kind of method for reducing the fouling membrane of membrane separation in water treatment procedure, characterized in that carry out ultraviolet light to aqueous
Treatment with irradiation and then to aqueous carry out membrane separation.
9. method as claimed in claim 8, characterized in that membrane separation selection ultrafiltration membrane treatment, micro-filtration film process,
Nanofiltration membrane treatment or reverse osmosis membrane processing, preferably ultrafiltration membrane treatment.
10. method as claimed in claim 8 or 9, characterized in that control ultraviolet light during the ultraviolet treatment with irradiation and shine
It is 40-300mJ/cm to penetrate dosage2, preferably 40-100mJ/cm2。
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