CN102826686B - Double-membrane treatment method of iron and steel industrial wastewater - Google Patents
Double-membrane treatment method of iron and steel industrial wastewater Download PDFInfo
- Publication number
- CN102826686B CN102826686B CN201210343827.3A CN201210343827A CN102826686B CN 102826686 B CN102826686 B CN 102826686B CN 201210343827 A CN201210343827 A CN 201210343827A CN 102826686 B CN102826686 B CN 102826686B
- Authority
- CN
- China
- Prior art keywords
- wastewater
- waste water
- reverse osmosis
- water
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims abstract description 63
- 238000011282 treatment Methods 0.000 title claims abstract description 62
- 229910000831 Steel Inorganic materials 0.000 title claims abstract description 55
- 239000010959 steel Substances 0.000 title claims abstract description 55
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 21
- 239000010842 industrial wastewater Substances 0.000 title abstract 2
- 239000002351 wastewater Substances 0.000 claims abstract description 220
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 178
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 147
- 238000001914 filtration Methods 0.000 claims abstract description 36
- 239000000701 coagulant Substances 0.000 claims abstract description 25
- 230000002829 reductive effect Effects 0.000 claims abstract description 23
- 238000000108 ultra-filtration Methods 0.000 claims description 59
- 238000012545 processing Methods 0.000 claims description 46
- 230000008569 process Effects 0.000 claims description 42
- 239000003795 chemical substances by application Substances 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 28
- 238000003672 processing method Methods 0.000 claims description 26
- 238000005273 aeration Methods 0.000 claims description 23
- 238000002203 pretreatment Methods 0.000 claims description 23
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical group [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 22
- 238000005189 flocculation Methods 0.000 claims description 20
- 230000016615 flocculation Effects 0.000 claims description 20
- 239000002455 scale inhibitor Substances 0.000 claims description 19
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 18
- 125000001309 chloro group Chemical group Cl* 0.000 claims description 17
- 230000009467 reduction Effects 0.000 claims description 14
- 239000012752 auxiliary agent Substances 0.000 claims description 11
- 229920002401 polyacrylamide Polymers 0.000 claims description 11
- 230000000844 anti-bacterial effect Effects 0.000 claims description 10
- 239000003899 bactericide agent Substances 0.000 claims description 10
- 230000001590 oxidative effect Effects 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000003206 sterilizing agent Substances 0.000 claims description 7
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 229920000642 polymer Polymers 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims description 6
- 241000195493 Cryptophyta Species 0.000 claims description 5
- 241000242583 Scyphozoa Species 0.000 claims description 5
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 5
- -1 PDMDAAC Polymers 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- IXPNQXFRVYWDDI-UHFFFAOYSA-N 1-methyl-2,4-dioxo-1,3-diazinane-5-carboximidamide Chemical compound CN1CC(C(N)=N)C(=O)NC1=O IXPNQXFRVYWDDI-UHFFFAOYSA-N 0.000 claims description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 3
- MDNWOSOZYLHTCG-UHFFFAOYSA-N Dichlorophen Chemical group OC1=CC=C(Cl)C=C1CC1=CC(Cl)=CC=C1O MDNWOSOZYLHTCG-UHFFFAOYSA-N 0.000 claims description 3
- 241000790917 Dioxys <bee> Species 0.000 claims description 3
- 239000001828 Gelatine Substances 0.000 claims description 3
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 3
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 3
- 238000013019 agitation Methods 0.000 claims description 3
- 239000004411 aluminium Substances 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- KHSLHYAUZSPBIU-UHFFFAOYSA-M benzododecinium bromide Chemical compound [Br-].CCCCCCCCCCCC[N+](C)(C)CC1=CC=CC=C1 KHSLHYAUZSPBIU-UHFFFAOYSA-M 0.000 claims description 3
- OTPBAANTTKRERC-UHFFFAOYSA-N benzyl(dodecyl)azanium;chloride Chemical compound Cl.CCCCCCCCCCCCNCC1=CC=CC=C1 OTPBAANTTKRERC-UHFFFAOYSA-N 0.000 claims description 3
- 125000004093 cyano group Chemical group *C#N 0.000 claims description 3
- 229960003887 dichlorophen Drugs 0.000 claims description 3
- 229920000159 gelatin Polymers 0.000 claims description 3
- 235000019322 gelatine Nutrition 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 claims 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 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- MGIYRDNGCNKGJU-UHFFFAOYSA-N isothiazolinone Chemical compound O=C1C=CSN1 MGIYRDNGCNKGJU-UHFFFAOYSA-N 0.000 claims description 3
- 150000002978 peroxides Chemical class 0.000 claims description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- UEZVMMHDMIWARA-UHFFFAOYSA-M phosphonate Chemical compound [O-]P(=O)=O UEZVMMHDMIWARA-UHFFFAOYSA-M 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- GRLPQNLYRHEGIJ-UHFFFAOYSA-J potassium aluminium sulfate Chemical compound [Al+3].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GRLPQNLYRHEGIJ-UHFFFAOYSA-J 0.000 claims description 3
- QLNJFJADRCOGBJ-UHFFFAOYSA-N propionamide Chemical compound CCC(N)=O QLNJFJADRCOGBJ-UHFFFAOYSA-N 0.000 claims description 3
- 235000010413 sodium alginate Nutrition 0.000 claims description 3
- 239000000661 sodium alginate Substances 0.000 claims description 3
- 229940005550 sodium alginate Drugs 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 4
- 125000004122 cyclic group Chemical group 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 abstract description 3
- 238000003756 stirring Methods 0.000 abstract description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract 1
- 229910001882 dioxygen Inorganic materials 0.000 abstract 1
- 239000008394 flocculating agent Substances 0.000 abstract 1
- 230000003068 static effect Effects 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 35
- 238000004140 cleaning Methods 0.000 description 34
- 239000003513 alkali Substances 0.000 description 28
- 239000000243 solution Substances 0.000 description 24
- 239000002253 acid Substances 0.000 description 19
- 239000002245 particle Substances 0.000 description 17
- 239000011347 resin Substances 0.000 description 15
- 229920005989 resin Polymers 0.000 description 15
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 14
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 14
- 239000000126 substance Substances 0.000 description 14
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 11
- 239000000084 colloidal system Substances 0.000 description 10
- 239000003814 drug Substances 0.000 description 10
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 9
- 230000001276 controlling effect Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 8
- 239000003729 cation exchange resin Substances 0.000 description 8
- 238000011010 flushing procedure Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 8
- 230000003647 oxidation Effects 0.000 description 8
- 238000007254 oxidation reaction Methods 0.000 description 8
- 239000006004 Quartz sand Substances 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 238000003723 Smelting Methods 0.000 description 7
- 238000005096 rolling process Methods 0.000 description 7
- 230000002000 scavenging effect Effects 0.000 description 7
- 238000004065 wastewater treatment Methods 0.000 description 7
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 6
- 238000011109 contamination Methods 0.000 description 6
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 6
- 230000008929 regeneration Effects 0.000 description 6
- 238000011069 regeneration method Methods 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
- 239000011162 core material Substances 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 230000000813 microbial effect Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000005086 pumping Methods 0.000 description 5
- 239000008237 rinsing water Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000001954 sterilising effect Effects 0.000 description 5
- 150000001450 anions Chemical class 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 230000008595 infiltration Effects 0.000 description 4
- 238000001764 infiltration Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 238000005554 pickling Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 238000004659 sterilization and disinfection Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 3
- 229940120146 EDTMP Drugs 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 230000001112 coagulating effect Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- NFDRPXJGHKJRLJ-UHFFFAOYSA-N edtmp Chemical compound OP(O)(=O)CN(CP(O)(O)=O)CCN(CP(O)(O)=O)CP(O)(O)=O NFDRPXJGHKJRLJ-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000007667 floating Methods 0.000 description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000009991 scouring Methods 0.000 description 3
- 230000032258 transport Effects 0.000 description 3
- 238000003911 water pollution Methods 0.000 description 3
- CHRJZRDFSQHIFI-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;styrene Chemical compound C=CC1=CC=CC=C1.C=CC1=CC=CC=C1C=C CHRJZRDFSQHIFI-UHFFFAOYSA-N 0.000 description 2
- 229940124321 AIDS medicine Drugs 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- YDONNITUKPKTIG-UHFFFAOYSA-N [Nitrilotris(methylene)]trisphosphonic acid Chemical compound OP(O)(=O)CN(CP(O)(O)=O)CP(O)(O)=O YDONNITUKPKTIG-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000007334 copolymerization reaction Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000011033 desalting Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000009472 formulation Methods 0.000 description 2
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 235000006408 oxalic acid Nutrition 0.000 description 2
- 229920001155 polypropylene Polymers 0.000 description 2
- 238000000247 postprecipitation Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 235000019832 sodium triphosphate Nutrition 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- UBXAKNTVXQMEAG-UHFFFAOYSA-L strontium sulfate Chemical compound [Sr+2].[O-]S([O-])(=O)=O UBXAKNTVXQMEAG-UHFFFAOYSA-L 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 241000387312 Hemiberlesia lataniae Species 0.000 description 1
- 101710194948 Protein phosphatase PhpP Proteins 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- 229910000754 Wrought iron Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000011021 bench scale process Methods 0.000 description 1
- 239000013590 bulk material Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000009749 continuous casting Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004070 electrodeposition Methods 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000009713 electroplating Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 230000002070 germicidal effect Effects 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 229920000592 inorganic polymer Polymers 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 235000014380 magnesium carbonate Nutrition 0.000 description 1
- 229960001708 magnesium carbonate Drugs 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000000873 masking effect Effects 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- RECVMTHOQWMYFX-UHFFFAOYSA-N oxygen(1+) dihydride Chemical compound [OH2+] RECVMTHOQWMYFX-UHFFFAOYSA-N 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- HWGNBUXHKFFFIH-UHFFFAOYSA-I pentasodium;[oxido(phosphonatooxy)phosphoryl] phosphate Chemical compound [Na+].[Na+].[Na+].[Na+].[Na+].[O-]P([O-])(=O)OP([O-])(=O)OP([O-])([O-])=O HWGNBUXHKFFFIH-UHFFFAOYSA-I 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000012256 powdered iron Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 125000001453 quaternary ammonium group Chemical group 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000011257 shell material Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000009865 steel metallurgy Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- UNXRWKVEANCORM-UHFFFAOYSA-I triphosphate(5-) Chemical compound [O-]P([O-])(=O)OP([O-])(=O)OP([O-])([O-])=O UNXRWKVEANCORM-UHFFFAOYSA-I 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a double-membrane treatment method of iron and steel industrial wastewater. The method comprises the following steps that the pH value of the wastewater is regulated to be greater than 7, and then, oxygen gas is introduced into the wastewater until the total iron content in the wastewater is reduced to a value smaller than 0.5mg/l; the pH value of the wastewater is regulated to 8.0 to 8.5, flocculating agents and coagulant aids are added into the wastewater under the stirring condition, and then, the static settlement is carried out; the wastewater subjected to preliminary treatment is subjected to filtering treatment in a filter so that the water outlet turbidity of the wastewater is smaller than 2NTU; the wastewater subjected to filtering treatment is subjected to full flow filtering treatment; the wastewater subjected to pretreatment is subjected to two-stage reverse osmosis treatment; and the wastewater subjected to the two-stage reverse osmosis treatment is subjected to fine treatment through a mixing bed. The double-membrane treatment method has the advantages that the treated wastewater reaches the demineralized water standard, the cyclic utilization rate of water resources is improved, the consumption of new water is saved, and the outward discharge water of a ton of steel is reduced.
Description
Technical field
The present invention relates to a kind of Wastewater Of Steel Industry treatment process, especially a kind of Wastewater Of Steel Industry double membrane processing method that adopts ultra-filtration membrane and reverse osmosis membrane to carry out.
Background technology
Over nearly 30 years, the development of ultra-filtration technique is very rapid, not only aspect the separation of singular solution, is having original effect, and application aspect Waste Water Reuse is also more and more, Chang Zuowei pre-processing device, guarantees the long-term safety steady running of the follow-up equipments such as reverse osmosis.
Ultrafiltration is a kind of membrane separation technique, and its film is porousness unsymmetrical structure.Filtration procedure is taking both sides differential pressure of membrane as motivating force, and taking mechanical grading principle as basic a kind of solution separating process, working pressure is generally 0.03～0.6MPa, and screening aperture is from 0.005～0.1 μ m, and molecular weight cut-off is 1000～500,000 dalton left and right.One of its topmost form is hollow-fibre membrane, is capillary, forms through spray silk spinning system.Its internal surface or outside surface are tight zone, or claim active coating, and inside is porous supporting mass.
The principle of reverse osmosis desalination is: in water salty (Ru Yuanshui), impose than naturally osmotic and press larger pressure, infiltration is carried out round about, water molecules in former water is pressed onto to the other side of film, become clean water (de-mineralized water), thereby reach the object except the middle salinity that anhydrates.Separation method with other is compared, and reverse osmosis has significant advantage: do not undergo phase transition, do not produce secondary pollution, need not heat, equipment is simple, efficiency is high, take up an area less, energy consumption is low, simple to operate, flexible etc.Within the scope of higher salt concentration, reverse osmosis has lower energy consumption than the desalting process such as ion-exchange and electrodialysis, and also constantly mechanize, automatization of masking technique.
Reverse osmosis technology just began one's study in the fifties, make the reverse osmosis membrane with industrial value to the end of the sixties, within 1971, start to have industrialness reverse osmosis unit to put into operation in power plant, adopt now reverse osmosis method to carry out water treatment and spread all over the countries such as the U.S., Japan, France, Italy.China starts to introduce reverse osmosis unit in the water treatment in power station the end of the seventies, the nineties the developing and become focus of reverse osmosis membrane, reverse osmosis technology is mainly used in the wastewater treatments such as sea water desaltination, pure water and ultrapure water preparation, city water processing, municipal sewage treatment and application, industrial electro waste electroplating and pulp and paper industry wastewater treatment, chemical wastewater treatment, foodstuffs industry, medicine industry now.This has fully proved that reverse osmosis technology is reliable in the technology maturation of reusing sewage processing.
Due to complicacy and the unstable of steel wastewater, embrane method technology is also not popularization and application in recycling of wastewater from steel field, does not occur ripe Technology at present.
Summary of the invention
Technical problem to be solved by this invention is: the defect that overcomes existing steel wastewater treatment process and can not reach de-mineralized water standard, providing a kind of adopts two Membrane Separation for Water Treatments to process the method that reclaims Iron and Steel Production waste water, waste water after treatment reaches de-mineralized water standard, improve water resources cyclic utilization rate, save new water consumption, reduced the outer draining of ton steel.
The present invention is directed to steel rolling, smelting wastewater water quality characteristics, reasonable, efficient, the energy-conservation pre-treatment and the pretreatment technology flow process that adopt, be the operations such as aeration, clorox sterilization, coagulating sedimentation, multi-medium filtering, ultrafiltration, waste water has reached the influent quality standard of reverse osmosis unit requirement after treatment.In addition, optimization of the present invention adds auxiliary agent kind, adds auxiliary agent point, adds assistant concentration, and process efficiency is further improved, and has guaranteed reverse osmosis system steady running.
In order to solve the problems of the technologies described above, the first technical scheme provided by the invention is, a kind of Wastewater Of Steel Industry double membrane processing method, and the method comprises:
B. pre-treatment
A1) aeration oxide treatment: waste water ph is adjusted to and is greater than 7, then pass into oxygen in waste water, until total iron content drops to < 0.5mg/L in waste water;
A2) automatic reaction, precipitation process: waste water ph is adjusted to 8.0-8.5, adds flocculation agent and coagulant aids under agitation condition in waste water, then staticly settle, wastewater effluent turbidity is reached below 5NTU;
B. pre-treatment
B1) filtration treatment: the waste water after pre-treatment is carried out in strainer to filtration treatment, so that wastewater effluent turbidity is less than 2NTU;
B2) uf processing: the waste water after filtration treatment is carried out to grossflow filtration processing, make pollution index≤3 of the waste water after uf processing;
C. double-stage reverse osmosis processing, carries out two steps ro processing by pretreated waste water;
D. precision processing, adopts mixed bed to carry out precision processing waste water after treatment double-stage reverse osmosis.
Aforesaid Wastewater Of Steel Industry double membrane processing method, at step a2) in, described flocculation agent is polymerize aluminum chloride, polyaluminium sulfate, polymer phosphate aluminium, bodied ferric sulfate, poly-ferric chloride or polymer phosphate iron; Described coagulant aids is polyacrylamide, PDMDAAC, gelatine or sodium alginate; Preferably, flocculation agent is polymerize aluminum chloride, taking wastewater volume flocculant addition as 20-30mg/L; Coagulant aids is polyacrylamide, taking wastewater volume coagulant aids add-on as 0.1-0.2mg/L.
Aforesaid Wastewater Of Steel Industry double membrane processing method, at step a2) taking a step forward comprises degerming algae treatment step: in the waste water after aeration oxide treatment, adding chlorine residue in the water outlet of chloro sterilizing agent control settling tank is 1.2-1.5mg/L, and described chloro sterilizing agent is clorox, liquid chlorine or dioxide peroxide.
Aforesaid Wastewater Of Steel Industry double membrane processing method, at step b1) in, described strainer is more medium filter, waste water flow velocity is 6-10m/h.
Aforesaid Wastewater Of Steel Industry double membrane processing method, at step b2) in, the membrane pore size of described ultrafiltration apparatus is 0.03-0.1 μ m, it is more than 20,000 filtering molecular weight.
Aforesaid Wastewater Of Steel Industry double membrane processing method, pretreated waste water, carrying out before first-stage reverse osmosis processing, regulates waste water ph to 6.5-7.5.
Aforesaid Wastewater Of Steel Industry double membrane processing method, pretreated waste water is carrying out, before first-stage reverse osmosis processing, adding Scale inhibitors organic phosphonate, taking wastewater volume Scale inhibitors add-on as 3.5-5mg/L.
Aforesaid Wastewater Of Steel Industry double membrane processing method, pretreated waste water is carrying out before first-stage reverse osmosis processing, and adding reductive agent to waste water is 200mV ± 10mV in redox potential (ORP); Described reductive agent is sub-sodium pyrosulfate, potassium aluminium sulfate, S-WAT or sodium bisulfite.
Aforesaid Wastewater Of Steel Industry double membrane processing method, first-stage reverse osmosis waste water after treatment, carrying out before two-pass reverse osmosis processing, regulates waste water ph to 7-8.
Aforesaid Wastewater Of Steel Industry double membrane processing method, the intersegmental pressure reduction of first-stage reverse osmosis is controlled at below 0.3MPa, and the intersegmental pressure reduction of two-pass reverse osmosis is controlled at below 0.2MPa.
Aforesaid Wastewater Of Steel Industry double membrane processing method, adopts the each auxiliary agent of computer control to add volume pump and corresponding technical process pump interlocking start and stop.
Aforesaid Wastewater Of Steel Industry double membrane processing method, pretreated waste water is carrying out before double-stage reverse osmosis processing, adopt cartridge filter to carry out filtration treatment, and two-stage hoisting pump frequency conversion and ultrafiltration product jellyfish pipe pressure is chain, ensures that waste water reaches the pressure requirement of cartridge filter.
Aforesaid Wastewater Of Steel Industry double membrane processing method, periodically in pretreated waste water, add non oxidizing bactericide, wherein said non oxidizing bactericide is dichlorophen, dioxy cyano group methane, isothiazolinone, dodecylbenzyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide or 2,2-, bis-bromos-3-nitrilo propionic acid amide.
Adopt the two Membrane Separation for Water Treatments of the present invention to process and reclaim high pollution Iron and Steel Production waste water, process and reach de-mineralized water standard, improved water resources cyclic utilization rate, reduced new water consumption, reduced the outer draining of ton steel.
Brief description of the drawings
It described in Fig. 1, is process flow sheet of the present invention.
Embodiment
For fully understanding object, feature and effect of the present invention, by following concrete embodiment, the present invention is elaborated.
The steel rolling of processing of the present invention, smelt and produce the waste water producing, its pollutant component complexity, in waste water, electricity is led, hardness, bacterium, microorganism, organic content is high and fluctuation is large, and water quality is quite severe, and it processes quite difficulty.
The present invention is directed to steel rolling, smelting wastewater water quality characteristics, reasonable, efficient, the energy-conservation pre-treatment and the pretreatment technology flow process that adopt, be the operations such as aeration, sterilization, coagulating sedimentation, multi-medium filtering, ultrafiltration, waste water has reached the influent quality standard of reverse osmosis unit requirement after treatment, system run all right, reliable.In addition, optimization of the present invention adds auxiliary agent kind, adds auxiliary agent point, adds assistant concentration, and process efficiency is further improved, and has guaranteed reverse osmosis system steady running.
In the two membrane process crafts of the present invention, between ultrafiltration and reverse osmosis, do not set up intermediate water tank, produce jellyfish pipe pressure by two-stage hoisting pump frequency conversion and ultrafiltration chain, ensure the pressure of 0.21MPa, reduce the investment of a water tank and lift pump, saved operation energy consumption cost simultaneously.
The present invention is directed in steel wastewater water quality characteristics water organic content high, bacterium, content of microorganisms are high, breed fast feature, after reductive agent dispensing point, increase again non oxidizing bactericide dosing system, regularly reverse osmosis has been carried out to sterilization, avoided microbial contamination stifled to the dirt of film.
In reusing sewage, ultrafiltration all adopted cross flow filter in the past, in sewage disposal and the ultrafiltration producer suggestion hyperfiltration reverse-rinsing cycle between 20-40min, flux is 45L/m
2h left and right.And ultrafiltration has adopted full filtration filter in the present invention, design long 72min of hyperfiltration reverse-rinsing cycle, effectively promote the rate of recovery of ultrafiltration; Meanwhile, ultrafiltration adopts large flux design 56.8L/m
2h.
The handled waste water of the present invention is the mixing water that Iron and Steel Production is rolled district and two kinds of waste water of smelting.Rolling effluent comprises: in hot-rolled process, need use water cooling roll by pricking roller when steel ingot is rolled into various steel (steel plate, rod iron, rail etc.), flushing iron scale and the waste water that produces; Diluted acid water, nitration mixture, the alkali oil waste water etc. that rolling system produces is to neutralization station and the waste water of rear generation; Pipeline transports the waste water that powdered iron ore produces; The all waste water of rolling system such as continuous casting system is clean, turbid circulating water sewer.Smelting wastewater comprises: circulation water of blast furnace draining, Coal-gas Washing Water Using, blast furnace water-break, grain slag, sintering, the smelting system waste water such as coking.
By the macrocyclic statistical study to steel wastewater water quality data, in conjunction with existing water technology, by bench-scale testing repeatedly, by continuous process modification, form technique of the present invention.First-stage reverse osmosis ability of the present invention is 1400m
3/ h, whole process system is divided into: pre-treatment, pre-treatment, double-stage reverse osmosis and precision processing four parts.The present invention is taking reverse osmosis desalination as core, and pre-treatment comprises aeration oxide treatment and automatic reaction precipitation, and pre-treatment comprises that more medium filter filters and ultrafiltration, and precision processing comprises mixed bed processing.The present invention ensures that process system produces the requirement that water meets boiler feed water.
Describe steel wastewater treatment process of the present invention and related equipment in detail below in conjunction with Fig. 1.
1. pre-treatment
The main purpose of pre-treatment steel wastewater is most of iron, manganese, suspended substance, colloid and the partial organic substances of removing in waste water, alleviates the burden of pretreatment system and improves it and produce water water quality.Pretreating device mainly comprises the aeration oxidation pond, automatic reaction settling tank and the inclined-plate clarifying basin that connect successively.This pretreating device further comprises: mechanical grille, clorox medicine machine, flocculation agent medicine machine and coagulant aids medicine machine.Mechanical grille is arranged on before aeration oxidation pond, and clorox medicine machine is connected with aeration oxidation pond, and flocculation agent medicine machine is connected with automatic reaction settling tank with coagulant aids medicine machine.
1.1 aeration oxide treatment
Waste water ph is adjusted to and is greater than 7, then in waste water, pass into oxygen, until total iron content drops to < 0.5mg/L in waste water.
Concrete, this aeration oxidation operation mainly carries out in aeration oxidation pond.In waste water, iron is with Fe
2+form exist, can not be removed, the present invention adds alkali in waste water, conventional mineral alkali such as such as sodium hydroxide, potassium hydroxide etc., is adjusted to > 7 by waste water ph.Then, oxygen is passed in waste water, (CO leaves simultaneously preferably to adopt conventional air aeration method
2), airborne oxygen is by the Fe in waste water
2+be oxidized to Fe
3+, and form Fe (OH)
3colloid.This Fe (OH)
3colloid can be removed in post precipitation is processed.To the time that passes into oxygen in waste water for until in waste water total iron content drop to < 0.5mg/L, this residence time is about 20 minutes conventionally.
Steel wastewater iron-holder is 1-15mg/L, with the coagulating sedimentation+more medium filter of operation sewage employing forward, can only remove a small part iron.The present invention adopts aeration oxide treatment, total iron content can be dropped to < 0.5mg/L.
1.2 automatic reactions, precipitation process
Waste water ph is adjusted to 8.0-8.5 (preferably 8.2), under agitation condition, in waste water, adds flocculation agent and coagulant aids, then staticly settle.
Automatic reaction precipitation process is in order to remove iron, manganese, the calcium ion in waste water.Concrete, after aeration oxide treatment, waste water is delivered in automatic reaction pond, preferably adopt one-level lift pump that waste water is delivered to automatic reaction pond.Before waste water enters automatic reaction pond, add alkali, conventional mineral alkali such as such as sodium hydroxide, potassium hydroxide etc., is adjusted to 8.0-8.5 (preferably 8.2) by waste water ph.
In automatic reaction pond, adopt stirrer, medicament (flocculation agent and coagulant aids) and waste water are fully mixed.Preferably, in automatic reaction pond, adopt many group stirrers, and the stirring velocity of these stirrers reduces to discharge port from fast to slow gradually from mechanical reaction tank opening for feed, medicament (flocculation agent and coagulant aids) and waste water are fully mixed.For example, automatic reaction pond is made up of three groups of stirrers (4 every group), and rotating speed reduces to discharge port from fast to slow gradually from mechanical reaction tank opening for feed, and the impeller middle line speed of three groups of stirrers is respectively 0.54m/s, 0.35m/s, 0.15m/s.
In automatic reaction pond waste water with add flocculation agent and coagulant aids mix after from flow into settling tank leave standstill, most suspended substances is removed in settling tank, delivery turbidity reaches below 5NTU.The present invention preferably adopts conventional radial-flow inclined-plate clarifying basin, and quantity and the size of the present invention to radial-flow inclined-plate clarifying basin do not have particular requirement, and the wastewater flow rate that can process as required determines, for example adopting 2 diameters is the radial-flow inclined-plate clarifying basin of 29 meters.
The flocculation agent that the present invention preferably uses is inorganic polymer flocculant, for example polymerize aluminum chloride (PAC) polyaluminium sulfate (PAS), polymer phosphate aluminium (PAP), bodied ferric sulfate (PFS), poly-ferric chloride (PFC), polymer phosphate iron (PFP), more preferably adopt polymerize aluminum chloride as flocculation agent, particularly containing 30wt%Al
2o
3solid polyaluminium chloride as flocculation agent, in wastewater volume, the concentration that adds of polymerize aluminum chloride is 20-30mg/L.The coagulant aids that the present invention preferably uses is organic polymer coagulant aids, for example polyacrylamide, and PDMDAAC, gelatine, sodium alginate, more preferably polyacrylamide is as coagulant aids, and the concentration that adds of polyacrylamide is 0.1-0.2mg/L.
Preferably, pre-treatment of the present invention further comprises the steps:
1.3 water intakings are processed
Before waste water enters aeration oxide treatment, with large floating matter in grid interception waste water.For example, during from water reservoir water intaking (rolling effluent and smelting wastewater), at intake, grid is set, large floating matter in interception waste water.
1.4 degerming algae processing
Before automatic reaction, precipitation process, in the waste water after aeration oxide treatment, add chloro sterilizing agent, control settling tank water outlet chlorine residue 1.2-1.5mg/L.Described chloro sterilizing agent is clorox, liquid chlorine or dioxide peroxide.
Because organic content in waste water is 40-80mg/L, and ammonia nitrogen is up to 18mg/L, and wastewater temperature is between 15-28 DEG C.Under such condition, be applicable to the growth of bacterium algae, in especially summer, the microbial contamination of waste water is serious.Enter post-order process step and form biological clay pollution for fear of bacterium algae, and for fear of the safe and stable operation that affects ultrafiltration, reverse osmosis membrane, in waste water after aeration oxide treatment, add chloro sterilizing agent, the clorox that for example effective chlorine density is 10-15mg/L, and control settling tank water outlet chlorine residue 1.2-1.5mg/L, and follow-up ultrafiltration water outlet chlorine residue is between 0.5-0.8mg/L.
2. pre-treatment
The main purpose of pre-treatment steel wastewater is further to remove suspended substance in waste water, colloid, colourity, turbidity, organism etc. to hinder the impurity of follow-up reverse-osmosis treated.Pretreatment unit mainly comprises the more medium filter and the ultrafiltration apparatus that connect successively.Pretreatment unit further comprises filter backwash pump, filter backwash water tank, roots blower, hyperfiltration reverse-rinsing pump, hyperfiltration reverse-rinsing water pot, ultrafiltration cleaning system and clorox medicine system.Filter backwash water tank is connected successively with filter backwash pump, and is connected with more medium filter, and roots blower is connected with more medium filter.Hyperfiltration reverse-rinsing water pot is connected successively with hyperfiltration reverse-rinsing pump, and is connected with ultrafiltration apparatus, and clorox medicine system is connected with hyperfiltration reverse-rinsing water pot.Ultrafiltration cleaning system is connected with ultrafiltration apparatus.
2.1 filtration treatment
Waste water after pre-treatment enters two-stage hoisting pump water tank from settling tank, then adopts secondary deduction pump that the waste water after pre-treatment is added and is sent in strainer.Waste water after pre-treatment is carried out in strainer to filtration treatment, so that wastewater effluent turbidity is less than 2NTU.
Preferably, adopt conventional more medium filter to carry out filtration treatment, waste water flow velocity is 6-10m/h (preferably 9m/h), and pressure is for being greater than 0.2MPa.More medium filter is mainly held back and is removed most suspended substances and colloid in water by filtering layer.Preferably, the filler of more medium filter adopts hard coal, quartz sand and pebbles, for example following filling-material structure: (1) hard coal (upper strata): particle diameter: 0.8-1.2mm, thickness: 400mm; (2) quartz sand (lower floor): particle diameter: 0.5-0.8mm, thickness: 700mm; (3) quartz sand (bed course): particle diameter: 3.0-4.0mm, thickness: 100mm; (4) quartz sand (bed course): particle diameter: 4.0-8.0mm, thickness: 100mm; (5) pebbles (bed course): particle diameter: 6.0-12.0mm, thickness: 100mm; (6) pebbles (bed course): particle diameter: 12.0-18.0mm, thickness: 100mm; (7) pebbles (bed course): particle diameter: 18.0-25.0mm, thickness: 100mm.
The backwash cycle of strainer is determined according to Inlet and outlet water pressure reduction or accumulated running time, and for example specification φ 5000 processes flow 194m
3/ h, carries out backwash after 24 hours working times of strainer of flow velocity 9.0m/h.Backwash water adopts strainer to produce water, and the strainer in filter backwash water tank produces water under filter backwash pumping action, according to backwash intensity 8-12L/m
2.s (preferably 10L/m
2.s) strainer is carried out to backwash.After backwash, water enters steel wastewater pond, again enters pre-treatment.Adopt roots blower to carry out gas scouring, and gas scouring intensity is 8-12L/m
2.s (preferably 10L/m
2.s).
2.2 uf processing
Waste water after filtration treatment is carried out to grossflow filtration (full dose filtration) to be processed.Ultrafiltration of the present invention adopts large flux design, and permeant flux is 56.8L/m
2h, is greater than the permeant flux 45L/m of common Wastewater Treatment Design
2h.
The effect of uf processing (UF) waste water is to remove the impurity such as particle in waste water, suspended substance, colloid, organism, ensures to produce water pollution index (SDI)≤3, meets the requirement of reverse osmosis unit.Uf processing waste water reclamation rate of the present invention is >=90%.
Ultrafiltration apparatus preferred film aperture is that (preferably 0.03 μ film m), its material can be conventional ultrafiltration membrane material to 0.03-0.1 μ m, for example polyvinylidene difluoride (PVDF) (PVDF).Its film silk inside/outside footpath of preferred ultra-filtration membrane is 0.6-0.8/1.2-1.4mm (preferably 0.7/1.3mm), filtration cycle >=72min.According to wastewater flow, ultrafiltration apparatus can be selected many cover membrane modules, for example, select 12 cover ultrafiltration apparatuss, and every cover comprises 64 membrane modules, and every covering device designing treatment amount is 189m
3/ h.
Ultrafiltration apparatus operation for some time, need to carry out backwash processing.Backwash water water source adopts ultrafiltration to produce water, adds clorox sterilization in backwash water, and in backwash water, the concentration of clorox is 30-40mg/L.Backwash pressure reduction is increased to maximum operating pressure differential, and backwash intensity is 100-150L/m
2h.The ultrafiltration that clorox medicine system joins clorox in hyperfiltration reverse-rinsing water pot is produced in water, and the ultrafiltration product water under hyperfiltration reverse-rinsing pumping action in hyperfiltration reverse-rinsing water pot enters ultrafiltration apparatus and carries out backwash.The backwash of ultra-filtration equipment (SFR) adopts the mode of gas-water associating, and every operation backwash in 72 minutes once.
Water production rate is little or while reaching 2 months working time, need to carry out matting to ultrafiltration apparatus.In hyperfiltration membrane assembly During Process of Long-term Operation, the various detrimental impurity that film surface can be held back by it covers and forms cake layer, and even fenestra also can be stopped up by more tiny impurity, and the permeable membrane pressure of waste water is increased.The quality of useless pretreatment quality, can only solve the speed problem of the contaminated speed of film, and contaminated solution problem fundamentally needs regularly ultrafiltration apparatus to be carried out to matting for this reason.The cleaning interval of ultrafiltration apparatus is subject to the impact of itself material capability parameter, operational conditions (as temperature, pressure etc.).
When cleaning organic matter and microbial contamination, the chemical formulation of the cleaning ultrafiltration apparatus that the present invention adopts is NaOH and the 0.15-0.25wt%NaClO of the aqueous solution that comprises following material: 0.03-0.07wt%, preferably 0.05wt%NaOH+0.2wt%NaClO.In this cleaning process by adding pH that alkali ensures matting water at 11-12.
While cleaning the dirty stifled and part colloid of iron pollution, carbonate crystallization, the chemical formulation of the cleaning ultrafiltration apparatus that the present invention adopts is the citric acid solution of the oxalic acid solution of concentration 1.5-2.5wt% or the hydrochloric acid of concentration 0.3-0.5wt% or concentration 1.5-2.5wt%, the hydrochloric acid of the oxalic acid solution of preferred concentration 2wt% or concentration 0.4wt% or the citric acid solution of concentration 2wt%.The pH that ensures matting water by acid adding in this cleaning process is at 1.5-2.0.
3. double-stage reverse osmosis processing
Adopt one-level high-pressure pump to deliver to double-stage reverse osmosis device pretreated waste water and carry out two steps ro processing.Wherein the intersegmental pressure reduction of first-stage reverse osmosis is controlled at below 0.3MPa, and the intersegmental pressure reduction of two-pass reverse osmosis is controlled at below 0.2MPa.One-level infiltration of the present invention and secondary infiltration form by multistage.Intersegmental pressure reduction refers to: the pressure reduction between the water inlet of certain section and this section of dense water.The waste water reclamation rate of double-stage reverse osmosis processing of the present invention is 75%, and this lower waste water reclamation rate is easy to prevent that fouling and film from polluting.
Double-stage reverse osmosis device of the present invention mainly comprises one-level high-pressure pump, first-stage reverse osmosis device, secondary high-pressure pump, second level reverse osmosis apparatus, first-stage reverse osmosis water tank and two-pass reverse osmosis water tank.The effect of pretreated waste water process one-level high-pressure pump is sent in first-stage reverse osmosis device, a first-stage reverse osmosis device water outlet part enters associating pumping plant, outer for de-mineralized water user, it is personal that a part enters first-stage reverse osmosis water tank, a part enters in second level reverse osmosis apparatus via the effect of secondary high-pressure pump, then enters two-pass reverse osmosis water tank.Describe the waste water through two-pass reverse osmosis processing below in detail.
The main purpose of reverse-osmosis treated is to remove dissolved salts in waste water, removes small-particle that some macromole and last stage do not remove etc. simultaneously.According to the difference of wastewater flow, can select the quantity of reverse osmosis unit.Preferably, select low pressure pollution resistant composite film (BW30-365FR and BW30-400FR) as reverse osmosis membrane of the present invention, single film ratio of desalinization reaches more than 99.5%.
Preferably, first-stage reverse osmosis device comprises 7 covers, and it is 32:16 that 1#-4# unit pressurized vessel is arranged, every cover adopts 336 membrane elements, and it is 36:18 that 5#-6# unit pressurized vessel is arranged, and every cover adopts 324 membrane elements, it is 30:15 that 0# unit pressurized vessel is arranged, and adopts 315 membrane elements.In the time that reverse osmosis equipment temperature is 20 DEG C, the every cover of first-stage reverse osmosis device is exerted oneself as 235m
3/ h, the rate of recovery is 75%, and ratio of desalinization is not less than 97%.
Second level reverse osmosis apparatus further removes first-stage reverse osmosis and produces the salt in water, extends the regeneration period of mixed bed.Preferably, second level reverse osmosis apparatus comprises 3 covers, and it is 11:4 that unit pressurized vessel is arranged, and every cover adopts 90 membrane elements.
First-stage reverse osmosis device water production rate is 1400m
3/ h, second level reverse osmosis apparatus water production rate is 300m
3/ h.One-level high-pressure pump and secondary high-pressure pump provide enough pressure to reverse osmosis unit, according to the situation of actual reverse osmosis unit and waste water, can adjust the force value that one-level high-pressure pump and secondary high-pressure pump provide, for example in an embodiment, one-level high-pressure pump and secondary high-pressure pump provide the pressure of 1MPa.Waste water under the effect of one-level high-pressure pump after ultrafiltration enters first-stage reverse osmosis device, and under the effect of secondary high-pressure pump, first-stage reverse osmosis device waste water after treatment enters second level reverse osmosis apparatus.
Reverse osmosis unit must not be stopped transport for a long time, and at least move 2 hours every day.If prepare to shut down more than 72 hours,, protect implementing to the sodium sulfite solution that punching dress concentration is 1wt% in assembly with chemical cleaning system.The each start of reverse osmosis unit (RO) all should be less than under 0.5MPa condition and rinse 5-10 minute at intake pressure.Block up for the dirt of effectively eliminating, alleviate film, reverse osmosis unit film unit was carried out to big yield flushing once in every 24 hours.
Reverse osmosis unit is normally in service, membrane element can be subject to the flushing of infiltration water, so only decline more than 10% at reverse osmosis unit (RO) aquifer yield in theory, pressure drop increase more than 15%, ratio of desalinization obviously descend in degradation situation, just need to carry out matting to reverse osmosis unit.But in order to ensure the long safe operation of reverse osmosis unit, common 1 month matting reverse osmosis unit once.When cleaning, need segmented cleaning, clean direction identical with the direction of operation, do not allow reverse cleaning, to avoid film and roll up and stretch out and damage membrane element.
When matting, working pressure control is: meeting under the prerequisite of water production rate and water quality, get low force value as far as possible; Quantity discharged control: due to the variation of the factor such as water temperature, working pressure, make the water production rate of device that corresponding variation also occur, at this moment tackle quantity discharged adjustment, control between quantity discharged and water production rate than being 1:3.
Be in operation, RO film may be polluted by inorganics dirt, colloid, microorganism, metal oxide etc. or block.These electrodeposition substances, on film surface, will cause that RO film transit dose declines and ratio of desalinization reduces.Therefore,, in order to recover transit dose and the desalting performance of RO film, need to carry out termly matting to RO.
Alkali cleaning is applicable to organism and microbial contamination, the chemical cleaning solution of the alkali cleaning reverse osmosis unit that the present invention adopts is the solution that comprises following composition: 1.5-2.5wt% (preferably 2wt%) ethylenediamine tetraacetic acid (EDTA) (EDTA), 1.5-2.5wt% (preferably 2wt%) tripoly phosphate sodium STPP, 0.120-0.130wt% (preferably 0.125wt%) dodecane.In cleaning process, such as, ensure that by adding alkali (conventional alkali such as sodium hydroxide, potassium hydroxide etc.) pH is at 11-12.
Pickling is applicable to iron pollution, the dirty stifled and part colloid of carbonate crystallization, the chemical cleaning solution of the pickling reverse osmosis unit that the present invention adopts is: the citric acid solution of the hydrochloric acid of concentration 0.3-0.5wt% or concentration 1.5-2.5wt%, the citric acid solution of the hydrochloric acid of preferred concentration 0.4wt% or concentration 2wt%.The pH that ensures matting water by acid adding in this cleaning process is at 1.5-2.0.
The present invention generally adopts pickling after first alkali cleaning, according to pollution cause also can first pickling after alkali cleaning.For preventing that the pollutent of first-stage reverse osmosis device from entering second level reverse osmosis apparatus and causing second level reverse osmosis apparatus to pollute, clean and want partition running at first pass, first clean second level reverse osmosis apparatus and clean again first-stage reverse osmosis device.Before cleaning, must rinse reverse osmosis system 10～30 minutes with reverse osmosis water outlet.While cleaning second level reverse osmosis apparatus, adjust matting scavenging solution flow to 70～100m
3/ h, must ensure in whole cleaning process that pH is within the scope of 1.5-2.0, temperature≤38 DEG C, pressure reduction≤0.25MPa.When the cleaning flow of every pressurized vessel can reach 9m
3/ h, illustrates that second level reverse osmosis apparatus cleaning performance is good, can clean first-stage reverse osmosis device.
Cleaning first-stage reverse osmosis device adjustment matting scavenging solution flow is 100-150m
3/ h, notes ensureing that pH is within the scope of 11-12 in whole cleaning process temperature≤38 DEG C, △ P≤0.25MPa.When the cleaning flow of every pressurized vessel can reach 9m
3/ h, illustrates that first-stage reverse osmosis device cleaning performance is good, can finish to clean.
After each cleaning, all rinse reverse osmosis unit with reverse osmosis water outlet, until the dense water pH of reverse osmosis unit is while approaching the pH value of reverse osmosis unit water inlet waste water.
Preferably, adopt non-oxidiser to carry out recycling sterilizing.The pH value of a scavenging solution of mensuration per hour in whole cleaning process, the pH value of observing the color of scavenging solution and adjusting in time scavenging solution is to specialized range.In the time that scavenging solution darkens, should change scavenging solution, temperature of record per hour, inlet and outlet pressure and pressure reduction, flow, pH value etc.
Double-stage reverse osmosis device of the present invention further comprises that acid adds equipment, Scale inhibitors to add equipment, reductive agent to add equipment, cartridge filter and non oxidizing bactericide equipment.Acid adds equipment, Scale inhibitors to add equipment, reductive agent to add equipment and cartridge filter to be arranged on before one-level high-pressure pump.
Preferably, pretreated waste water is entering before first-stage reverse osmosis device, and (conventional mineral acid all can be applicable to the present invention to add equipment to add acid by acid, for example hydrochloric acid, sulfuric acid, phosphoric acid), in order to regulate waste water ph to 6.5-7.5, to reduce the trend of dense water side carbonate fouling.
Preferably, pretreated waste water is entering before first-stage reverse osmosis device, add equipment in feed water by reverse osmosis, to add Scale inhibitors by Scale inhibitors, the present invention's Scale inhibitors used is organic phosphonate, such as Amino Trimethylene Phosphonic Acid (ATMP), ethylene diamine tetra methylene phosphonic acid sodium (EDTMPS), ethylene diamine tetra methylene phosphonic acid (EDTMPA) etc., preferably can use the Flocon135 in commercially available U.S. big lake.3.5-5mg/L in the dosage of wastewater volume Scale inhibitors of the present invention, can prevent in reverse osmosis concentrated water side that difficulty (slightly soluble) salt such as calcium carbonate, magnesiumcarbonate, calcium sulfate, barium sulfate, Strontium Sulphate, Calcium Fluoride (Fluorspan) separate out fouling after concentrated, stop up reverse osmosis membrane, thereby damage the application characteristic of membrane element.
Preferably; for protecting follow-up reverse osmosis membrane; pretreated waste water is entering before first-stage reverse osmosis device; add equipment to add conventional water treatment reductive agent by reductive agent; for example sub-sodium pyrosulfate, potassium aluminium sulfate, S-WAT, sodium bisulfite; with the chlorine residue in reducing waste water, add-on control is 200mV left and right for adopting the redox potential in online ORP (redox potential) table detection water, and 10mV fluctuates.The preferred reductive agent of the present invention is sodium bisulfite.
Preferably, before waste water carries out reverse-osmosis treated, carry out secondary filter.Concrete, adopting cartridge filter, before this cartridge filter is arranged on RO, object is that the macrobead thing in anti-sealing enters reverse osmosis membrane, damages reverse osmosis membrane, to guarantee the normal operation of RO.The principle of work of cartridge filter is: utilize the hole of filter core 5 μ m to carry out mechanical filter, in waste water, remaining trace suspension particle, colloid, microorganism etc., be trapped or be adsorbed in cartridge surface and hole.The present invention adopts PLC to control technical process, produces jellyfish pipe pressure chain by two-stage hoisting pump frequency conversion and ultrafiltration, ensures that wastewater pressure reaches the requirement of cartridge filter pressure, the pressure of for example 0.21MPa.
Along with the growth for the treatment of time of water, filter core of security filter is because of the pollution of trapped substance, and its running resistance rises gradually, imports and exports differential water pressures while reaching 0.1MPa, more renew cartridge when moving to.Preferably, cartridge filter is vertical column equipment, in-built 101 long 40 inches filter cores of cartridge filter, and filtering accuracy is 5 μ m.
Preferably, add after equipment at reductive agent, in high-pressure pump back with water inlet line, increased non oxidizing bactericide adding equipment, regularly reverse osmosis membrane is carried out to germicidal treatment, to avoid microbial contamination stifled to the dirt of film.When season alternation, for the situation of severe contamination, every 2-3 days, add non oxidizing bactericide once spring and autumn, and each 2 hours, concentration was 200mg/L.For slight pollution or for the maintenance of reverse osmosis membrane, every 3 days, add non oxidizing bactericide once, each 2 hours, concentration was 100mg/L.Wherein said non oxidizing bactericide is dichlorophen, dioxy cyano group methane, isothiazolinone, dodecylbenzyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide or 2,2-, bis-bromos-3-nitrilo propionic acid amide.
4. precision processing
Adopt mixed bed to carry out precision processing waste water after treatment double-stage reverse osmosis.
Yin, yang ion, the CO in waste water can be further removed in mixed bed precision processing
2and SiO
2, ensure that effluent quality reaches product water water quality requirement.The positive and negative ion that in waste water, various inorganic salt ionization generates, when through resinbed, replaced by the hydroxide ion in hydrogen ion and resin anion(R.A) in resin cation (R.C.) respectively, enter hydrogen ion in water and hydroxide ion in conjunction with generating water molecules, thereby obtain the effect of removing inorganic salts in waste water.Preferably, waste water filtering speed is 30-45m/h.The present invention can select according to the flow of waste water quantity and the specification of mixed bed, for example, adopt 3 mixed beds, specification
every nominal output 150m
3/ h.The present invention's mixed bed used is the conventional commercially available mixed bed in this area, wherein resin anion(R.A) and resin cation (R.C.) are all conventional mixed bed sewage water filtration material, and for example resin anion(R.A) adopts 201 × 7 (on vinylbenzene-divinylbenzene copolymerization matrix with quaternary ammonium group (N (CH
3)
3oH), resin cation (R.C.) adopts 001 × 1 styrene type cation exchange resin, 001 × 2 styrene type cation exchange resin, 001 × 4 styrene type cation exchange resin, 001 × 7 styrene type cation exchange resin is (on vinylbenzene-divinylbenzene copolymerization matrix with sulfonic group (SO
3h)), 002 × 7 styrene type cation exchange resin, 003 × 7 styrene type cation exchange resin, 004 × 7 styrene type cation exchange resin.
Use after for some time, mixed bed needs regeneration, sun resin regeneration the regenerator having diluted from bottom to top reverse flow through resin layer, by the resin of the different attitudes of regenerating according to this from top to bottom, the regeneration of negative resin is the regenerator the having diluted resin layer of forward flowing through from top to bottom, by the resin of the different attitudes of regenerating according to this from top to bottom.Storng-acid cation exchange resin and strongly basic anion exchange resin are housed in mixed bed, and the filling ratio of Zeo-karb and anionite-exchange resin is 1:2, as the multiple bed unit of numerous series connection.H after exchanging by hybrid ionic in water
+and OH
-generate immediately the water molecules that degree of ionization is very low, the gegenion seldom may form positively charged ion or anionresin time, can make permutoid reaction carry out very thoroughly.
Reclaim equiment comprises sour high-order storage tank, the high-order storage tank of alkali, sour low level batch meter, alkali low level batch meter, injector and neutralization tank.
The material that the high-order storage tank of acid, the high-order storage tank of alkali adopt is respectively steel lining glue (acid) and steel is coated with epoxy resin (alkali), adopts ejector applications vacuum method to carry regenerator.
Acid low level batch meter, alkali low level batch meter adopt steel lining plastic container.Volume can meet respectively regeneration acid, alkali number once.Conventionally specification,
nominal output 150m
3the mixed bed of/h, acid solution (31%) primary recycling amount is 800L, alkali lye (40%) primary recycling amount is 700L.Acid, alkali are disposed to neutralization tank and carry out neutralizing treatment.
Mixed bed start-stop moves automatically according to mixed bed water outlet high water tank, also can manually control.The regeneration of mixed bed can manually be carried out also can automatically carrying out.
The feature of technique and device according to the present invention, preferably adopts PLC that each operation is realized automatically and being controlled.Meanwhile, the signal gathering by data collecting card, concentrates on and on upper computer, shows each processing parameter.Whole PLC Controlling System possesses the function of centralized supervisory control, warning, interlock protection, procedure operation.
PLC Controlling System can be carried out man-machine dialogue.By upper computer picture and mouse, whole waste water treatment process is monitored, all operating parameters, guard signal be printable record all.
Elaborate the principle of PLC Controlling System below.
PLC Controlling System adopts Siemens S7 series of PLC by the newly-built ultrafiltration of Ethernet (ICP/IP protocol), reverse osmosis system dispatch control system.PLC is programmable logic controller, it according to the program of establishment and adopt data message carry out logical operation, and operation result is outputed to topworks and is come the operation of control system equipment by signal.
The condition of technology and equipment operation of the present invention is:
(1) satisfy condition: each auxiliary agent adds the low liquid level of the liquid level > of equipment
(2) operation form: operation automatically.
(3) system alarm: Interlock Status.
(4) interlocking of liquid level: it is main that the variation of high water tank is mainly realized reporting to the police, judges that by operator whether liquid level signal is true.
Elaborate PLC Controlling System adds equipment control to each auxiliary agent below.
The auxiliary agent that the present invention adds comprises the flocculation agent (for example polymerize aluminum chloride (PAC)) that reduces turbidity; Accelerate the unite coagulant aids (for example polyacrylamide (PAM)) of sedimentation of flco aggegation; Degrade former water bacteria, organic oxygenant (for example clorox); Prevent the Scale inhibitors of the dense water end (W.E.) fouling of reverse osmosis membrane; Prevent the reductive agent (for example sodium bisulfite) of reverse osmosis membrane oxidation; Regulate acid (for example hydrochloric acid), the alkali (for example sodium hydroxide) of one-level, second level reverse osmosis apparatus (RO) water inlet PH.
The add-on of each auxiliary agent is by volume pump control, each volume pump and corresponding technical process pump interlocking start and stop.
Concrete, the clorox volume pump of pretreatment procedure, flocculation agent volume pump, coagulant aids volume pump, alkali (preferably sodium hydroxide) volume pump and with the start and stop of pretreated waste water amount interlocking.
Clorox add-on is adjusted volume pump frequency automatically according to settling tank water outlet chlorine residue, control settling tank water outlet chlorine residue 1.2-1.5mg/L, coagulant aids add-on, flocculant addition are according to the automatic regulating frequency of wastewater flow rate, it is 20-30mg/L that control flocculation agent adds concentration, it is 0.1-0.2mg/L that coagulant aids adds concentration, alkali (preferably sodium hydroxide) adds concentration to pump water pH value according to two-stage hoisting automatically to adjust frequency, and controlling pH is about 8.0-8.5.
In addition, hyperfiltration reverse-rinsing clorox volume pump also with the start and stop of hyperfiltration reverse-rinsing interlocking.
Reductant metering pump and the chain start and stop of one-level high-pressure pump, reductive agent add-on is adjusted volume pump frequency automatically according to first-stage reverse osmosis device water-in, controls first-stage reverse osmosis device water-in at redox potential (ORP) 200mV, fluctuates 10.Preferably, operation 1-2 cover reverse osmosis unit, starts 1 volume pump automatically, and operation 3-4 cover reverse osmosis unit, starts 2 volume pumps automatically, and operation 5-6 cover reverse osmosis unit, starts 3 volume pumps automatically.
Scale inhibitors volume pump, sour volume pump and the chain start and stop of one-level high-pressure pump.Scale inhibitors add-on, according to the proportional automatic adjusting metering pump frequency of one-level high-pressure pump general import wastewater flow, is controlled scale inhibitor dosing amount 3.5-5mg/L.Preferably, operation 1-2 cover reverse osmosis unit, starts 1 volume pump automatically, and operation 3-4 cover reverse osmosis unit, starts 2 volume pumps automatically, and operation 5-6 cover reverse osmosis unit, starts 3 volume pumps automatically.Acid add-on is adjusted volume pump frequency automatically according to ultrafiltration water outlet pH, and the about 5-10mg/L of sour add-on is preferred, and operation 1-4 cover reverse osmosis unit, starts 1 volume pump automatically, and operation 5-6 cover reverse osmosis unit, starts 2 volume pumps automatically.
Alkali volume pump and the chain start and stop of secondary high-pressure pump, add-on is adjusted volume pump frequency automatically according to the secondary high-pressure pump PH of always intaking, and controls secondary high-pressure pump water inlet pH at 7-8, and alkali enters the about 5mg/L of dose, preferred, 2 volume pump the using and the reserved.
Two-stage hoisting pumping capacity realizes automatically and controlling according to ultrafiltration rising pipe upward pressure, ensures pressure-stabilisation.
Describe the control of more medium filter below in detail.
The control of more medium filter be ON/OFF, pump by controlling Pneumatic butterfly valve open/stop operation, backwash, the automatic operation process such as for subsequent use of realizing.The cycle of backwash is mainly to determine according to the accumulated running time of equipment and integrated flow.In addition, be provided with tensimeter in inlet pipe and each outlet of strainer, at the inlet flow rate meter of each strainer, flow signal sent into microcomputer and show, record, control.
Describe the control of ultra-filtration equipment below in detail.
Startup, operation, backwash, the air bump rinse operation of ultra-filtration equipment, just wash, shut down the process such as for subsequent use and all can realize automatically and controlling by PLC.Meanwhile, ultrafiltration system also arranges a local panel and a local operation dish, on local panel readable go out the relevant technological parameters of ultrafiltration, and can on local operation dish, operate relevant water pump and automatic valve.The important parameter of ultra-filtration equipment is equipped with to on-line detector table as pressure, flow etc., and is set with overload alarm function.
The backwash of ultrafiltration system is according to the backwash condition of working time as ultrafiltration system, generally every 72min backwash once; The mode that comes into operation of ultrafiltration system: specified operation time, use after the time automatically out of servicely, after backwash, automatically proceed to operation.The matting of ultrafiltration system can automatically also can be manual.
Describe the control of high-pressure pump below in detail.
The high-pressure pump of RO device is imported and exported low pressure and high voltage protective switch is housed.When service discharge deficiency makes the hydraulic pressure of high-pressure pump entrance lower than a certain set(ting)value (being generally 0.05MPa), can automatically send signal and stop high-pressure pump operation, protection high-pressure pump is not worked in idle running situation.When system is because of other reason or mishandle; while making the top hole pressure of high-pressure pump exceed certain set(ting)value (being generally 2.0MPa); the protection of high-pressure pump top hole pressure can be powered by automatic cut off high pump, the corresponding RO device of simultaneously stopping transport, and securing system equipment is without prejudice.
Describe the control of reverse osmosis unit (RO) below in detail.
The processes such as the startup of RO device, operation, flushing, shutdown are for subsequent use all can be realized automatically and being controlled by PLC.Meanwhile, RO system also arranges a local panel and a local operation dish, can read the relevant technological parameters of RO, as specific conductivity, flow, pressure etc. on local panel; And can be on local operation dish start and stop RO water inlet high-pressure pump and relevant automatic valve.
Stop using or move after 12-24 hour at RO, with product water to about reverse osmosis membrane assembly auto-flushing 10～30min, to avoid high concentration salts in dense water to affect the performance of film in the surface deposition fouling of RO film.The also pollution tendencies of contaminant reducing to reverse osmosis membrane of timing low-pressure washing.First-stage reverse osmosis (RO) device of operation carries out auto-flushing according to the big yield flushing cycle of setting, the longlyest can not exceed 24 hours, first-stage reverse osmosis (RO) device of stoppage in transit and second level reverse osmosis apparatus by operations staff according to working specification periodic flushing.
Set forth the present invention below by specific embodiment, one skilled in the art will appreciate that this should not be understood to the restriction to the claims in the present invention scope.
Embodiment
Embodiment 1
The waste water of using in embodiment is the mixing water that district and two kinds of waste water of smelting roll in Taiyuan Steel Plant, and concrete parameter is in table 1.
Table 1
(above-mentioned being up to refers to that index value can occur at short notice)
The performance index of each auxiliary agent of using in embodiment and interpolation situation are in table 2
Table 2
Adopt PLC that the each operation of the present embodiment is realized automatically and being controlled.
1. pre-treatment
Waste water pump in water reservoir is sent into aeration oxidation pond.Intake at water reservoir arranges grid, large floating matter in interception waste water.In aeration oxidation pond, in waste water, add the sodium hydroxide solution of concentration 30wt%, waste water ph is adjusted to and is greater than 7.Then, adopt conventional air aeration method, in waste water, pass into oxygen 20 minutes, sampling and measuring, in waste water, total iron content drops to < 0.5mg/L.In waste water after aeration oxide treatment, add clorox, by PLC, clorox add-on is adjusted clorox volume pump frequency automatically according to post precipitation pond water outlet chlorine residue 1.2-1.5mg/L, and in waste water, effective chlorine density is 10-15mg/L.
Adopt one-level lift pump that waste water is delivered to automatic reaction pond, before waste water enters automatic reaction pond, add the sodium hydroxide solution of concentration 30wt%, waste water ph is adjusted to 8.2 left and right.
The present embodiment automatic reaction pond is made up of three groups of stirrers (4 every group), and rotating speed reduces to discharge port from fast to slow gradually from mechanical reaction tank opening for feed, and the impeller middle line speed of three groups of stirrers is respectively 0.54m/s, 0.35m/s, 0.15m/s.Coagulant aids polyacrylamide (PAM) add-on, flocculant poly aluminum chloride PAC (aluminium sesquioxide is more than or equal to 29%) add-on regulate metering pump frequency automatically according to wastewater flow rate, it is 20-30mg/L that control flocculation agent adds concentration, and it is 0.1-0.2mg/L that coagulant aids adds concentration.
After in automatic reaction pond, waste water mixes with flocculation agent and coagulant aids, the radial-flow inclined-plate clarifying basin that certainly flows into 2 diameters and be 29 meters leaves standstill, sampling and measuring, and delivery turbidity is below 5NTU.
2. pre-treatment
Settling tank water outlet enters two-stage hoisting pump water tank, then by two-stage hoisting pump, waste water pressurization is sent into more medium filter.More medium filter main technical details is as follows:
Quantity: 13; Specification: φ 5000;
Bulk material: carbon steel; Inner anticorrosion: line with rubber
Design pressure: 0.6MPa; Operating pressure: be greater than 0.2Mpa
Working time: backwash in 24 hours once (is adjusted by actual), also can carry out backwash according to flow accumulation
The backwash time: 90min/ time; Turbidity: water outlet <5mg/L
Backwash intensity: 10L/m
2.s gas is cleaned intensity: 10L/m2.s
Operation flow velocity: 9.0m/h; Equipment is exerted oneself: normal 194m
3/ h
Filtrate is loaded grating:
(1) hard coal (upper strata): particle diameter: 0.8-1.2mm, thickness: 400mm; (2) quartz sand (lower floor): particle diameter: 0.5-0.8mm, thickness: 700mm; (3) quartz sand (bed course): particle diameter: 3.0-4.0mm, thickness: 100mm; (4) quartz sand (bed course): particle diameter: 4.0-8.0mm, thickness: 100mm; (5) pebbles (bed course): particle diameter: 6.0-12.0mm, thickness: 100mm; (6) pebbles (bed course): particle diameter: 12.0-18.0mm, thickness: 100mm; (7) pebbles (bed course): particle diameter: 18.0-25.0mm, thickness: 100mm.
Backwash water adopts strainer to produce water, adopts roots blower to carry out gas scouring.
Waste water after treatment more medium filter is sent into ultrafiltration apparatus.The main technical details of ultrafiltration apparatus is as follows:
Device quantity: 12 covers; Device is exerted oneself: Q=189m
3/ h/ cover;
Membrane module model: SFP2860; Membrane module quantity: 64/cover;
System recoveries rate: >=90%; Membrane pore size: 0.03 μ m;
Film silk inside/outside footpath: 0.7/1.3mm; Transmitance: 56.8L/m
2h
Filtration area: 52m
2/; Filter molecular weight: 20,000
Membrane material: PVDF (polyvinylidene difluoride (PVDF))
Maximum working pressure (MWP): 0.6MPa; Maximum operating pressure differential: 0.21Mpa
PH scope: 2～12 (when cleanings 1～12)
Maximum water inlet chlorine residue: 200mg/L (cleaning maximum tolerance chlorine content 5000mg/L) continuously
Working forms: grossflow filtration
Filtration cycle: >=72min
Water backwash intensity: 100-150L/m
2h
3. double-stage reverse osmosis processing
Add equipment in waste water, to add concentration 30wt% hydrochloric acid soln by acid, sour add-on is automatically adjusted acid according to ultrafiltration water outlet PH and is added volume pump frequency, and the about 5-10mg/L of sour add-on regulates waste water ph to 6.5-7.5.
Add equipment in waste water, to add Scale inhibitors Flocon135 by Scale inhibitors, dosage 3.5-5mg/L.Scale inhibitors add-on adds volume pump frequency according to the proportional automatic adjusting Scale inhibitors of one-level high-pressure pump general import wastewater flow.
Add equipment in waste water, to add sodium bisulfite by reductive agent, reductive agent add-on is automatically adjusted reductive agent according to first-stage reverse osmosis device water-in wastewater flow and is added volume pump frequency, control first-stage reverse osmosis device water-in in redox potential (ORP) at 200mV ± 10mV.
It is chain that jellyfish pipe pressure is produced in two-stage hoisting pump frequency conversion and ultrafiltration, ensures wastewater pressure 0.21MPa, and waste water is sent into cartridge filter.The main technical details of cartridge filter is as follows:
Quantity: 13; Specification: φ 1000 vertical cylinder;
Cylindrical shell material: stainless steel; Filter core material: polypropylene (PP);
Filtering accuracy: 5 μ m; Flow: 200m
3/ h;
Operating pressure: 0.4MPa; Front and back operting differential pressure: <0.3MPa
Flow condition: SDI<3; Turbidity <0.5mg/L
Waste water after treatment cartridge filter is delivered to first-stage reverse osmosis device by one-level high-pressure pump with the pressure pump of 1MPa and carry out filtration treatment.First-stage reverse osmosis device comprises 7 covers, and it is 32:16 that 1#-4# unit pressurized vessel is arranged, and every cover adopts 336 membrane elements, it is 36:18 that 5#-6# unit pressurized vessel is arranged, every cover adopts 324 membrane elements, and it is 30:15 that 0# unit pressurized vessel is arranged, and adopts 315 membrane elements.The intersegmental pressure reduction of first-stage reverse osmosis is controlled at below 0.3MPa.Select BW30-365FR and BW30-400FR composite membrane as reverse-osmosis treated film.In the time that reverse osmosis equipment temperature is 20 DEG C, the every cover of first-stage reverse osmosis device is exerted oneself as 235m
3/ h.A first-stage reverse osmosis device water outlet part enters associating pumping plant, and outer for de-mineralized water user, it is personal that a part enters first-stage reverse osmosis water tank, and a part is delivered in second level reverse osmosis apparatus with the pressure pump of 1MPa via secondary high-pressure pump.Alkali volume pump and the chain start and stop of secondary high-pressure pump, alkali (concentration 30wt% sodium hydroxide solution) add-on is adjusted alkali volume pump frequency automatically according to the secondary high-pressure pump PH of always intaking, and controls secondary high-pressure pump water inlet PH within the scope of 7-8.
Second level reverse osmosis apparatus comprises 3 covers, and it is 11:4 that unit pressurized vessel is arranged, and every cover adopts 90 membrane elements.First-stage reverse osmosis device water production rate is 1400m
3/ h, second level reverse osmosis apparatus water production rate is 300m
3/ h.The intersegmental pressure reduction of two-pass reverse osmosis is controlled at below 0.2MPa.
4. precision processing
Second level reverse osmosis apparatus waste water after treatment enters two-pass reverse osmosis and produces water tank, then under the effect of mixed bed lift pump, enters mixed bed, and waste water filtering speed is 40m/h.Mixed bed adopts 3 altogether, specification
every nominal output 150m
3/ h.It is 201 × 7 that mixed bed adopts resin anion(R.A), and resin cation (R.C.) is 001 × 7.Mixed bed water outlet after treatment enters mixed bed product water tank, supplies for outer.
The water outlet parameter that each operation stage records is as shown in table 3:
Table 3
Adopt of the present invention pair of embrane method treatment technology, at least there is following beneficial effect:
1. first-stage reverse osmosis output (de-mineralized water) 1400m in embodiment
3/ h, 2.5 yuan/ton of costs, 5.5 tons of de-mineralized water prices, year increase benefit:
1400m
3/ h × (5.5-2.5) unit/m
3× 24h × 365 day=3679.2 ten thousand yuan.
Save outer draining benefit: 1400m
3/ h × 0.5 yuan/ton × 24h × 365 day=613.2 ten thousand yuan.Amount to ten thousand yuan of year create beneficial result: 3679.2+613.2=4292.4.
2. the present invention has reclaimed trade effluent, has reduced outer row, has reduced water at low temperature rate of water make-up, has opened up a new water source for Iron And Steel Industry, has solved stainless steel system reform water shortage problem.The present invention meets national energy-saving and reduces discharging; the strategy of sustainable development; alleviate the situation of existing water resources critical shortage and water pollution, water pollution and environment protection have been produced to positive effect, and be worth for the innovation of China iron and steel metallurgy industry water technology provides the experience used for reference.
Claims (11)
1. a Wastewater Of Steel Industry double membrane processing method, the method comprises:
A. pre-treatment
A1) aeration oxide treatment: waste water ph is adjusted to and is greater than 7, then pass into oxygen in waste water, until total iron content drops to < 0.5mg/L in waste water;
A2) automatic reaction, precipitation process: waste water ph is adjusted to 8.0-8.5, adds flocculation agent and coagulant aids under agitation condition in waste water, then staticly settle, wastewater effluent turbidity is reached below 5NTU;
B. pre-treatment
B1) filtration treatment: the waste water after pre-treatment is carried out in strainer to filtration treatment, so that wastewater effluent turbidity is less than 2NTU;
B2) uf processing: the waste water after filtration treatment is carried out to grossflow filtration processing, make pollution index≤3 of the waste water after uf processing; Uf processing permeant flux is 56.8L/m
2h;
C. double-stage reverse osmosis processing
Pretreated waste water is carried out to two steps ro processing; Wherein, the intersegmental pressure reduction of first-stage reverse osmosis is controlled at below 0.3MPa, and the intersegmental pressure reduction of two-pass reverse osmosis is controlled at below 0.2MPa; First-stage reverse osmosis device comprises 7 covers, and it is 32:16 that 1#-4# unit pressurized vessel is arranged, and every cover adopts 336 membrane elements, it is 36:18 that 5#-6# unit pressurized vessel is arranged, every cover adopts 324 membrane elements, and it is 30:15 that 0# unit pressurized vessel is arranged, and adopts 315 membrane elements; Second level reverse osmosis apparatus comprises 3 covers, and it is 11:4 that unit pressurized vessel is arranged, and every cover adopts 90 membrane elements;
D. precision processing
Adopt mixed bed to carry out precision processing waste water after treatment double-stage reverse osmosis;
Wherein, pretreated waste water, carrying out before first-stage reverse osmosis processing, regulates waste water ph to 6.5-7.5; First-stage reverse osmosis waste water after treatment, carrying out before two-pass reverse osmosis processing, regulates waste water ph to 7-8.
2. Wastewater Of Steel Industry double membrane processing method according to claim 1, is characterized in that, at step a2) in, described flocculation agent is polymerize aluminum chloride, polyaluminium sulfate, polymer phosphate aluminium, bodied ferric sulfate, poly-ferric chloride or polymer phosphate iron; Described coagulant aids is polyacrylamide, PDMDAAC, gelatine or sodium alginate.
3. Wastewater Of Steel Industry double membrane processing method according to claim 2, is characterized in that, described flocculation agent is polymerize aluminum chloride, taking wastewater volume flocculant addition as 20-30mg/L; Described coagulant aids is polyacrylamide, taking wastewater volume coagulant aids add-on as 0.1-0.2mg/L.
4. Wastewater Of Steel Industry double membrane processing method according to claim 1 and 2, it is characterized in that, at step a2) taking a step forward comprises degerming algae treatment step: in the waste water after aeration oxide treatment, adding chlorine residue in the water outlet of chloro sterilizing agent control settling tank is 1.2-1.5mg/L, wherein, described chloro sterilizing agent is clorox, liquid chlorine or dioxide peroxide.
5. Wastewater Of Steel Industry double membrane processing method according to claim 1, is characterized in that, at step b1) in, described strainer is more medium filter, waste water flow velocity is 6-10m/h.
6. Wastewater Of Steel Industry double membrane processing method according to claim 1, is characterized in that, at step b2) in, it is 0.03-0.1 μ m that described ultra-filtration filters is processed the membrane pore size using, it is more than 20,000 filtering molecular weight.
7. Wastewater Of Steel Industry double membrane processing method according to claim 1, it is characterized in that, pretreated waste water, carrying out before first-stage reverse osmosis processing, regulates after pH value, add Scale inhibitors organic phosphonate, taking wastewater volume Scale inhibitors add-on as 3.5-5mg/L.
8. Wastewater Of Steel Industry double membrane processing method according to claim 1, it is characterized in that, pretreated waste water before first-stage reverse osmosis processing, adds after Scale inhibitors carrying out, and adding reductive agent to waste water is 200mV ± 10mV in redox potential (ORP); Described reductive agent is sub-sodium pyrosulfate, potassium aluminium sulfate, S-WAT or sodium bisulfite.
9. Wastewater Of Steel Industry double membrane processing method according to claim 1, is characterized in that, adopts the each auxiliary agent of computer control to add volume pump and corresponding technical process pump interlocking start and stop.
10. Wastewater Of Steel Industry double membrane processing method according to claim 9, it is characterized in that, pretreated waste water is carrying out before double-stage reverse osmosis processing, adopt cartridge filter to carry out filtration treatment, and it is chain to adopt two-stage hoisting pump frequency conversion and ultrafiltration to produce jellyfish pipe pressure, ensures that waste water reaches the pressure requirement of cartridge filter.
11. Wastewater Of Steel Industry double membrane processing methods according to claim 1, it is characterized in that, periodically in pretreated waste water, add non oxidizing bactericide, wherein said non oxidizing bactericide is dichlorophen, dioxy cyano group methane, isothiazolinone, dodecylbenzyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide or 2,2-, bis-bromos-3-nitrilo propionic acid amide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210343827.3A CN102826686B (en) | 2012-09-17 | 2012-09-17 | Double-membrane treatment method of iron and steel industrial wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210343827.3A CN102826686B (en) | 2012-09-17 | 2012-09-17 | Double-membrane treatment method of iron and steel industrial wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102826686A CN102826686A (en) | 2012-12-19 |
| CN102826686B true CN102826686B (en) | 2014-07-30 |
Family
ID=47330034
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210343827.3A Active CN102826686B (en) | 2012-09-17 | 2012-09-17 | Double-membrane treatment method of iron and steel industrial wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102826686B (en) |
Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103693776A (en) * | 2013-11-29 | 2014-04-02 | 江苏蛟龙重工集团有限公司 | Sewage treatment equipment |
| CN103864251A (en) * | 2014-03-18 | 2014-06-18 | 北京林业大学 | Esterified wastewater recycling membrane treatment system |
| CN103922546A (en) * | 2014-04-29 | 2014-07-16 | 江苏科沛达环境工程科技有限公司 | Heavy metal wastewater treatment equipment and method |
| CN104014247B (en) * | 2014-05-21 | 2016-01-27 | 内蒙古伊泰煤制油有限责任公司 | A kind of method for disinfection preventing the stifled reverse osmosis membrane of microorganism dirt |
| CN105330004B (en) * | 2014-08-15 | 2018-07-13 | 新特能源股份有限公司 | A kind for the treatment of process of Treated sewage reusing |
| CN105366769A (en) * | 2014-08-25 | 2016-03-02 | 成都安捷宜康环保科技有限公司 | Method of treating urban sewage by using double-membrane process |
| CN104386790A (en) * | 2014-11-13 | 2015-03-04 | 无锡伊佩克科技有限公司 | Wastewater treatment reagent |
| CN104528995B (en) * | 2014-12-22 | 2017-01-04 | 中国神华能源股份有限公司 | The wastewater treatment equipment of aluminium oxide and method in a kind of acidity extraction flyash |
| CN104671499B (en) * | 2015-02-01 | 2016-04-27 | 山西太钢不锈钢股份有限公司 | Smelt composite wastewater advanced treatment separate-recycling method |
| CN105132210A (en) * | 2015-09-02 | 2015-12-09 | 西安热工研究院有限公司 | Cleaning formula for cartridge filter element |
| CN105540925A (en) * | 2015-12-31 | 2016-05-04 | 上海丰信环保科技有限公司 | Three-time sterilization technology for membrane-method recycling of printing and dyeing wastewater |
| CN106334453A (en) * | 2016-11-10 | 2017-01-18 | 山西太钢不锈钢股份有限公司 | Method for controlling microorganisms of smelting waste water treatment system |
| CN107215979A (en) * | 2017-06-02 | 2017-09-29 | 青岛百发海水淡化有限公司 | A kind of method for desalting seawater |
| CN107285523B (en) * | 2017-08-07 | 2018-10-09 | 徐州工程学院 | A kind of mine wastewater Intelligent treatment device and method |
| CN107473472A (en) * | 2017-09-29 | 2017-12-15 | 项心力 | A kind of method based on physical chemistry coacervation processing sewage |
| CN107879513A (en) * | 2017-11-30 | 2018-04-06 | 东南大学成贤学院 | A kind of device of the full-automatic softening of the reverse osmosis concentrated water process of high rigidity |
| CN108176229B (en) * | 2017-12-01 | 2020-12-15 | 大同煤矿集团有限责任公司 | Pollution control method for ultrafiltration filter element in water treatment |
| CN108840362A (en) * | 2018-09-30 | 2018-11-20 | 长江师范学院 | A method of using prepared from steel slag for precipitated calcium carbonate |
| CN109336333A (en) * | 2018-11-14 | 2019-02-15 | 湖南冠颜料有限公司 | A kind of ferric oxide red colorant producing wastewater treatment |
| CN111392923A (en) * | 2020-03-04 | 2020-07-10 | 首钢京唐钢铁联合有限责任公司 | Acid-containing wastewater treatment method, treatment system and application |
| CN112456722A (en) * | 2020-12-07 | 2021-03-09 | 西安华浦水处理设备有限公司 | Coal mine water treatment system |
| CN112759113A (en) * | 2020-12-14 | 2021-05-07 | 广西大学 | Zero discharge of iron phosphate production wastewater and recovery method of phosphate radical and sulfate radical |
| CN112794505A (en) * | 2020-12-30 | 2021-05-14 | 中冶赛迪工程技术股份有限公司 | An electric furnace short-flow iron and steel plant water treatment and wastewater zero discharge process |
| CN113501593A (en) * | 2021-07-05 | 2021-10-15 | 内蒙古金河环保科技股份有限公司 | Sub-osmosis membrane wastewater treatment system and process |
| CN115108612B (en) * | 2021-08-13 | 2023-12-12 | 上海三及新材料科技有限公司 | Method for reducing oxidation-reduction potential of electrodialysis anolyte and application thereof |
| CN115536195A (en) * | 2022-09-21 | 2022-12-30 | 宝钢工程技术集团有限公司 | Cooling water treatment system for reducing temperature of coal gas and using method thereof |
| CN115927838B (en) * | 2022-12-16 | 2024-11-29 | 阳春新钢铁有限责任公司 | Intelligent steel billet charging and intelligent scrap removal control system and method |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3338505B2 (en) * | 1993-03-15 | 2002-10-28 | ダイセル化学工業株式会社 | Method for membrane purification of surface water with improved recovery rate and method of operating the same |
| CN1262490C (en) * | 2004-04-09 | 2006-07-05 | 太原钢铁(集团)有限公司 | Reverse osmosis method for treating sewage |
| AU2008202302A1 (en) * | 2008-05-22 | 2009-12-10 | Al-Samadi, Riad Dr | High Water Recovery Membrane Purification Process |
| CN101475269B (en) * | 2009-01-20 | 2011-08-31 | 上海恒通先进水处理有限公司 | Comprehensive treating and recycling method for steel wastewater and apparatus thereof |
| CN101613158B (en) * | 2009-08-07 | 2011-08-17 | 山西太钢不锈钢股份有限公司 | Double-membrane water treatment method of water tank with no ultrafiltration products |
| CN102616996B (en) * | 2012-04-05 | 2014-03-26 | 山西太钢不锈钢股份有限公司 | Method and special system for treating mixed wastewater with high salt content |
-
2012
- 2012-09-17 CN CN201210343827.3A patent/CN102826686B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102826686A (en) | 2012-12-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102826686B (en) | Double-membrane treatment method of iron and steel industrial wastewater | |
| CN102417253B (en) | In-depth treatment zero-discharge recovery equipment for heavy metal waste water | |
| CN101723549B (en) | Coking wastewater recycling treatment method | |
| CN101074141B (en) | Low-concentration organic wastewater regeneration and reuse process | |
| CN201746400U (en) | Depth treatment system for reclaimed water recycling | |
| CN111423035A (en) | A process system and method for combined treatment of circulating water in a thermal power plant without chemical and chemical methods | |
| CN102627364A (en) | Process flow for recycling and treating reverse osmosis concentrated water | |
| CN101723551B (en) | Coking wastewater recycling treatment method | |
| CN107522340A (en) | A kind of system and method for recycling high villaumite sewage | |
| CN110330140A (en) | Saline and alkaline region water pollution improvement and system for regenerating and recycling and method | |
| CN201309875Y (en) | Recycling device of biological pharmaceutical wastewater | |
| CN101723550B (en) | System for treating recycling of coking wastewater | |
| CN105293787B (en) | A kind of cold rolling alkalescence waste discharge advanced treatment recycling technique system and method | |
| CN202265468U (en) | Equipment for deeply treating and recovering heavy metal waste water with zero discharge | |
| CN207108747U (en) | A kind of textile printing and dyeing wastewater processing system | |
| CN210656480U (en) | Adopt washing cigarette waste water retrieval and utilization processing apparatus of DTRO device | |
| CN109422383A (en) | A kind of Treated sewage reusing treatment process | |
| CN112321028A (en) | Zero outer system of arranging of thermal power plant's circulating water based on digital real time monitoring | |
| CN218089172U (en) | Photovoltaic fluorine-containing wastewater reclaimed water recycling system | |
| CN202829788U (en) | Treatment device for benzene-containing waste water | |
| CN216513312U (en) | Near zero discharge system of advanced treatment coking strong brine | |
| CN213596069U (en) | Water treatment device combining ozone tail gas with ceramic membrane | |
| CN214528464U (en) | Recycling system of coal chemical industry circulating sewage | |
| CN213680237U (en) | Zero-discharge treatment system for mixed wastewater in electroplating industry | |
| CN212334909U (en) | Zero discharge system of power plant's salt-containing wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP02 | Change in the address of a patent holder |
Address after: 030003, Shanxi, Taiyuan, pointed lawn area, lawn street, No. 2 Patentee after: Shanxi Taigang Stainless Steel Co.,Ltd. Address before: 030003 No. 2, sharp lawn, Taiyuan City, Shanxi Province Patentee before: Shanxi Taigang Stainless Steel Co.,Ltd. |
|
| CP02 | Change in the address of a patent holder |