CN106517598A - Treating method and treating device for zero discharging of desulfurization wastewater - Google Patents
Treating method and treating device for zero discharging of desulfurization wastewater Download PDFInfo
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- CN106517598A CN106517598A CN201611234872.XA CN201611234872A CN106517598A CN 106517598 A CN106517598 A CN 106517598A CN 201611234872 A CN201611234872 A CN 201611234872A CN 106517598 A CN106517598 A CN 106517598A
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- desulfurization wastewater
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- 239000002351 wastewater Substances 0.000 title claims abstract description 65
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 51
- 230000023556 desulfurization Effects 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000007599 discharging Methods 0.000 title abstract 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 202
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 51
- 238000001728 nano-filtration Methods 0.000 claims abstract description 48
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 25
- 238000005345 coagulation Methods 0.000 claims abstract description 21
- 230000015271 coagulation Effects 0.000 claims abstract description 21
- 150000003839 salts Chemical class 0.000 claims abstract description 19
- 238000005342 ion exchange Methods 0.000 claims abstract description 12
- 239000013078 crystal Substances 0.000 claims abstract description 5
- 230000008569 process Effects 0.000 claims description 28
- 238000002425 crystallisation Methods 0.000 claims description 27
- 230000008025 crystallization Effects 0.000 claims description 27
- 238000003672 processing method Methods 0.000 claims description 27
- 150000002500 ions Chemical class 0.000 claims description 25
- 230000001112 coagulating effect Effects 0.000 claims description 21
- 239000002244 precipitate Substances 0.000 claims description 20
- 238000012545 processing Methods 0.000 claims description 17
- 239000012528 membrane Substances 0.000 claims description 15
- 230000033228 biological regulation Effects 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- 229910052799 carbon Inorganic materials 0.000 claims description 12
- 230000018044 dehydration Effects 0.000 claims description 12
- 238000006297 dehydration reaction Methods 0.000 claims description 12
- 239000010802 sludge Substances 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 10
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 7
- 230000016615 flocculation Effects 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 229910052742 iron Inorganic materials 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 5
- 239000004902 Softening Agent Substances 0.000 claims description 5
- 239000000956 alloy Substances 0.000 claims description 5
- 229910045601 alloy Inorganic materials 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical group [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 4
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 4
- 239000007800 oxidant agent Substances 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical group [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000013535 sea water Substances 0.000 claims description 3
- 239000012028 Fenton's reagent Substances 0.000 claims description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 2
- 239000000292 calcium oxide Substances 0.000 claims description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 2
- 239000000395 magnesium oxide Substances 0.000 claims description 2
- 230000014759 maintenance of location Effects 0.000 claims description 2
- 229920002401 polyacrylamide Polymers 0.000 claims description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 31
- 239000011780 sodium chloride Substances 0.000 abstract description 13
- 230000000694 effects Effects 0.000 abstract description 9
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- 238000005273 aeration Methods 0.000 abstract 2
- 238000004062 sedimentation Methods 0.000 abstract 2
- 238000004064 recycling Methods 0.000 abstract 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 50
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 31
- 229910001425 magnesium ion Inorganic materials 0.000 description 31
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 29
- 229910001424 calcium ion Inorganic materials 0.000 description 29
- 239000000377 silicon dioxide Substances 0.000 description 27
- 229910052681 coesite Inorganic materials 0.000 description 25
- 229910052906 cristobalite Inorganic materials 0.000 description 25
- 229910052682 stishovite Inorganic materials 0.000 description 25
- 229910052905 tridymite Inorganic materials 0.000 description 25
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 7
- 238000001764 infiltration Methods 0.000 description 6
- 239000011734 sodium Substances 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 229910001385 heavy metal Inorganic materials 0.000 description 5
- 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 4
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 4
- 229910052788 barium Inorganic materials 0.000 description 4
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 239000003456 ion exchange resin Substances 0.000 description 4
- 229920003303 ion-exchange polymer Polymers 0.000 description 4
- 229910052748 manganese Inorganic materials 0.000 description 4
- 239000011572 manganese Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000010908 plant waste Substances 0.000 description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 description 4
- 235000011152 sodium sulphate Nutrition 0.000 description 4
- 229910052712 strontium Inorganic materials 0.000 description 4
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 description 4
- 239000003643 water by type Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process 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
- 239000012535 impurity Substances 0.000 description 2
- 235000011147 magnesium chloride Nutrition 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 2
- 239000008234 soft water Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000004317 sodium nitrate Substances 0.000 description 1
- 235000010344 sodium nitrate Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
- C02F1/766—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens by means of halogens other than chlorine or of halogenated compounds containing halogen other than chlorine
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a treating method and a treating device for zero discharging of desulfurization wastewater. The treating method comprises the following steps: (1) performing aeration treatment and pre-sedimentation treatment on the desulfurization wastewater and collecting a first effluent; (2) performing coagulation treatment and softening treatment on the first effluent in turn, thereby obtaining a second effluent; (3) performing ultra-filtration treatment and ion exchange treatment on the second effluent in turn and collecting a third effluent; (4) performing nano-filtration treatment on the third effluent and collecting clean water; (5) performing reverse osmosis treatment on the clean water, thereby obtaining second concentrated water; (6) performing crystallizing treatment on the second concentrated water, thereby obtaining a crystal salt, and meanwhile, collecting the water generated in the steps (5) and (6), thereby obtaining water meeting standard. The device comprises an aeration adjusting device, a pre-sedimentation device, a coagulation treatment device, a softening treatment device, an ultra-filtration device, an ion exchange device, a nano-filtration device, a reverse osmosis device and a crystallizing device. The device has the advantages of running stability, good wastewater treatment effect and high recycling purity of sodium chloride.
Description
Technical field
The invention belongs to technical field of waste water processing, and in particular to a kind of processing method and dress of desulfurization wastewater zero-emission
Put.
Background technology
The water that desulfurization wastewater is arranged from absorption tower China and foreign countries in being mainly boiler smoke process of wet desulphurization, which has composition multiple
The characteristics of miscellaneous, water quality and the water yield larger, suspension content of fluctuation and high hardness, this causes its intractability larger, processing procedure
In easily fouling, affect being smoothed out for processing procedure.The process country of desulfurization wastewater there is no the experience of maturation at present, external coal-fired
Evaporation and crystallization processes are employed in the desulfurization wastewater processing procedure of thermal power plant, mixed salt has been finally given, but by above-mentioned
The solid matter that technique is produced is sodium sulphate and the mixed salt of sodium chloride, and mixed salt is defined as hazardous waste, and intractability is big, cost
It is high.
In order to, while waste water is processed, can also separate mixed salt, prior art employ nanofiltration system, counter-infiltration system and
Evaporation and crystallization system, final separation have obtained sodium sulphate and sodium chloride.As 104692574 A of Chinese patent literature CN is disclosed
A kind of processing method of high slat-containing wastewater.High-salt wastewater is passed sequentially through regulating reservoir, potassium permanganate composites, V-type filter tank by the method
With first time ion exchange resin system, soft water is obtained；Then soft water is through first paragraph counter-infiltration system, second segment ion exchange
Resin system and high pressure nanofiltration system, obtain producing water and concentrated water；Again by concentrated water second segment high-pressure flat plate membranous system, freezing and crystallizing system
System, obtains technical grade saltcake, will produce water and tie through second segment counter-infiltration system, first paragraph high-pressure flat plate membranous system and MVP evaporation
Crystallographic system is united, and obtains industrial chlorinations sodium.Above-mentioned technology has reclaimed sodium chloride and sodium sulphate in high-salt wastewater, with preferable economy
Benefit and social benefit.
But, above-mentioned technology is passed directly into the waste water from V-type filter tank out in first time ion exchange resin system,
Impurity and suspension in waste water can cause resin stain and exchange bed blocking, affect the stable fortune of ion exchange resin system
OK, cause water treatment effect poor；Furthermore, then above-mentioned technology is passed through again first using the first counter-infiltration system to Waste water concentrating
High pressure nanofiltration system carries out a point salt, because divalence sulfate ion content is high in waste water, fouling risk easily occurs, affects counter-infiltration system
The stable operation of system, while also can pollute to corresponding membranous system, affects water treatment effect.
The content of the invention
For this purpose, to be solved by this invention is that existing desulfuration waste water treatment process and device have operation stability and process
The defect of effect difference, and then a kind of operation stability and high treating effect, low cost, sodium chloride recovery purity height, zero-emission are provided
The processing method and processing device of the desulfurization wastewater put
To solve above-mentioned technical problem, the technical solution used in the present invention is as follows：
The processing method of desulfurization wastewater provided by the present invention, comprises the steps：
(1) Air Exposure is carried out to desulfurization wastewater and preformed precipitate is processed, collect the first water outlet；
(2) coagulating treatment and sofening treatment are carried out successively to first water outlet, obtains the second water outlet；
(3) hyperfiltration treatment and ion-exchange treatment are carried out to second water outlet successively, the 3rd water outlet is collected；
(4) nanofiltration process is carried out to the 3rd water outlet, clear water is collected；
(5) reverse-osmosis treated is carried out to the clear water, obtains the second concentrated water；
(6) crystallization treatment is carried out to second concentrated water, obtains crystal salt, and collection step (5) and the product water in (6),
Obtain water up to standard.
In step (2), oxidant, flocculant and flocculation aid in the coagulating treatment, have been added；
Softening agent, desiliconizing agent, flocculant and flocculation aid have been added in the sofening treatment.
Further, in step (4), also the first concentrated water of gained is processed including collecting the nanofiltration, and by itself and step (1)
Described in desulfurization wastewater the step of mix.
Further, in step (4), before the nanofiltration is processed, also include carrying out at except carbon the 3rd water outlet
The step of reason.
Further, in step (1) and (2), also including collect the preformed precipitate process, the coagulating treatment and described soft
Change and process gained sludge, and which is concentrated and is dehydrated, obtain mud cake, and will produce obtained by the concentration and the dehydration water and
The step of desulfurization wastewater mixes.
Preferably, the oxidant is sodium hypochlorite and/or Fenton reagent；
The softening agent is at least one in sodium carbonate, calcium oxide or NaOH；
The desiliconizing agent is magnesia and/or magnesium chloride；
The flocculant is AlSnSi alloy and/or iron-based flocculating agent；
The flocculation aid is lime and/or polyacrylamide.
Present invention also offers for the processing meanss of above-mentioned processing method, including the aerating regulation device being sequentially communicated,
Preformed precipitate device, coagulation treatment device, sofening treatment device, ultrafiltration apparatus, ion interchange unit, nanofiltration device, counter-infiltration dress
Put and crystallization apparatus.
Preferably, the molecular cut off of the NF membrane in the nanofiltration device be 150-300 dalton, bivalent ions section
Stay rate ＞ 98%；
Reverse osmosis membrane in the reverse osmosis unit is seawater reverse osmosis membrane and/or disc tube reverse osmosis (dt-ro) film；
The concentrated water outlet of the nanofiltration device is connected with the water inlet of the aerating regulation device.
Further, also include,
Carbon removing device, its water inlet, delivery port delivery port respectively with the ion interchange unit, the nanofiltration device
Water inlet is connected；
The enrichment facility being sequentially communicated and dehydration device, the sludge import of the enrichment facility are filled with the preformed precipitate respectively
Put, the coagulation treatment device is connected with the sludge outlet of the sofening treatment device, the enrichment facility and the dehydration are filled
That what is put produces inlet communication of the water out with the aerating regulation device.
Further, also include,
First water tank, its water inlet, delivery port delivery port respectively with the coagulation treatment device, sofening treatment dress
The water inlet connection put；
Second water tank, its water inlet, delivery port delivery port respectively with the sofening treatment device, the ultrafiltration apparatus
Water inlet is connected；
Three-tank, its water inlet, delivery port delivery port respectively with the carbon removing device, the water inlet of the nanofiltration device
Mouth connection；
4th water tank, its water inlet, delivery port delivery port respectively with the ultrafiltration apparatus, the ion interchange unit
Water inlet is connected；
5th water tank, its water inlet are connected with the delivery port of the reverse osmosis unit and the crystallization apparatus respectively.
Compared with prior art, the present invention has the advantages that：
1) processing method of the desulfurization wastewater provided by the embodiment of the present invention, processed by Air Exposure, preformed precipitate first,
Coagulating treatment and sofening treatment, remove desulfurization wastewater in COD, sulfate ion, calcium ions and magnesium ions, silica and 95% with
On suspension etc., it is to avoid these impurity are dirty to the film caused by subsequent ultrafiltration film, amberplex, NF membrane and reverse osmosis membrane
Dye, solves the problems, such as the fouling in film concentration process, it is ensured that the stable operation of subsequent handling；Then to desulfurization wastewater successively
Hyperfiltration treatment, ion-exchange treatment, nanofiltration process and reverse-osmosis treated are carried out, oil removal is gone by hyperfiltration treatment, it is to avoid be outstanding
Float pollutes and plug ion exchange membrane, improves the stability of process operation, reduces waste water hardness by ion-exchange treatment, carries
Highly crystalline product salt quality, delays or eliminates the scale formation of subsequent technique, the sulfate radical in waste water after ion-exchange treatment
Ion reduces more than 93%, then processes separation monovalent salt and divalent salts, such as monovalent salt, sodium chloride and sodium nitrate etc. by nanofiltration
Into in clear water, divalent salts, such as sodium sulphate are entered in the first concentrated water, because divalent ion mostly is the ion of fouling tendency, including negative and positive
Ion, is isolated in advance, it is to avoid scale formation is occurred during reverse-osmosis treated, is enable reverse-osmosis treated stable operation；
Finally, crystallization treatment is carried out to the second concentrated water directly, obtains the NaCl crystal salts of purity ＞ 99.5%, the crystal salt can reach
《Nacl》Refining industrial salt (industrial dry salt) primary standard in (GB/T 5462-2015) standard, which can directly carry out market pin
Sell, the effect of cooperating between above-mentioned each technique, it is ensured that the stable operation of above-mentioned processing method, while improve wastewater treatment
Effect, after testing, finally, COD in water up to standard<8mg/L、TDS 700-800mg/L、Na+230-250mg/L、Cl-380-
400mg/L、SO4 2-<0.5mg/L、SiO2<0.2mg/L、TSS<0.05mg/L。
2) processing method of the desulfurization wastewater provided by the embodiment of the present invention, before coagulating treatment, is first carried out at preformed precipitate
Reason, can be greatly reduced the chemical feeding quantity of follow-up coagulating treatment and sofening treatment；Oxidant and flocculant are added in coagulating treatment, with
Organic matter, sulfate ion and magnesium ion in removal desulfurization wastewater；Softening agent, desiliconizing agent, flocculant are added in sofening treatment
And flocculation aid, to remove the calcium ion in desulfurization wastewater and silica etc..
3) processing method of the desulfurization wastewater provided by the embodiment of the present invention, collects nanofiltration and processes the first concentrated water of gained, and
Which is mixed with the desulfurization wastewater in step (1), the SO in the first concentrated water4 2-With the Ca in follow-up coagulating treatment2+Reaction generates micro-
Molten calcium sulfate precipitation, the SO in desulfurization wastewater4 2-With Ca2+Reach ionization equilibrium, it is to avoid SO4 2-It is enriched with system, it is sl. sol.
CaSO4It is trapped into the first concentrated water in nanofiltration is processed, then flows back and mix with the desulfurization wastewater in step (1), until which is full
And Precipitation, drain into the external world, it is ensured that the purity and quality of later crystallization salt, the process of nanofiltration concentrated water is solved by the operation
Problem, realizes real zero-emission, meanwhile, investment and the operating cost of system are greatly reduced, the practicality of technique is improve.
4) processing method of the desulfurization wastewater provided by the embodiment of the present invention, is concentrated using film and substitute completely evaporation and concentration,
It is Na that nanofiltration processes clear water side+、Cl-Deng monovalent ion, then the product water obtained by reverse-osmosis treated can reach reuse index, receive
After filter process, the amount of the second concentrated water of gained is less than the 1/5 of inflow, is greatly reduced into the desulfurization wastewater in crystallization treatment
Amount, meanwhile, the second concentrated water salt content is higher, and the water yield is less, can cancel waste water evaporation equipment, directly carries out crystallization treatment, significantly
Reduce investment and the operating cost of concentration.
5) processing method of the desulfurization wastewater provided by the embodiment of the present invention, before nanofiltration is processed, enters to the 3rd water outlet
Row carbon removal treatment, and with reference to the ion-exchange treatment of front and continued, further remove calcium ions and magnesium ions, heavy metal ion and titanium dioxide
Carbon；As collecting preformed precipitate process and sludge obtained by coagulating treatment, and which is concentrated and is dehydrated, obtained mud cake, and will be dense
Contracting and dehydration gained are produced and are mixed with desulfurization wastewater, have thoroughly processed desulfurization wastewater.
6) processing meanss of the desulfurization wastewater provided by the embodiment of the present invention, at operation stability height, desulfurization wastewater
The features such as reason effect is good, low cost, sodium chloride recovery purity is high.
Description of the drawings
In order to be illustrated more clearly that the specific embodiment of the invention or technical scheme of the prior art, below will be to concrete
Needed for embodiment or description of the prior art, accompanying drawing to be used is briefly described, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, can be with according to these other accompanying drawings of accompanying drawings acquisition.
Fig. 1 is the structural representation of the processing meanss of desulfurization wastewater in the embodiment of the present invention；
Reference：
1- aerating regulation devices；2- preformed precipitate devices；3- coagulation treatment devices；The first water tanks of 4-；5- sofening treatment devices；
The second water tanks of 6-；7- ultrafiltration apparatus；8- enrichment facilities；9- dehydration devices；The 4th water tanks of 10-；11- ion interchange units；12- is removed
Carbon device；13- three-tanks；14- nanofiltration devices；15- reverse osmosis units；16- crystallization apparatus；The 5th water tanks of 17-.
Specific embodiment
In order to the object, technical solutions and advantages of the present invention are better described, below in conjunction with specific embodiment to this
It is bright to be described further.The present invention can be embodied in many different forms, and should not be construed as limited to set forth herein
Embodiment.On the contrary, there is provided these embodiments so that the disclosure will be it is thorough and complete, and will the present invention design fill
Divide and convey to those skilled in the art, the present invention will only be defined by the appended claims.
Embodiment 1
Present embodiments provide a kind of processing method of desulfurization wastewater zero-emission.The processing method comprises the steps：
(1) certain Desulphurization for Coal-fired Power Plant waste water carries out Air Exposure into aerating regulation device, and the waste water after Air Exposure enters
Staticly settled in entering preformed precipitate device, collected the first water outlet, wherein, COD 1000mg/L, TDS in desulfurization wastewater
66800mg/L、Na+4600mg/L、Cl-13000mg/L、Mg2+44000mg/L、Ca2+2400mg/L、SO4 2-36000mg/L、
SiO2It is 752.8NTU that 250mg/L, TSS13000mg/L, pH are 6.5, turbidity, COD 186mg/L in the first water outlet,
TDS41000mg/L、Na+4000mg/L、Cl-8200mg/L、Mg2+23800mg/L、Ca2+1400mg/L、SO4 2-21200mg/L、
SiO2<135mg/L, TSS 708mg/L, turbidity are 23.71NTU, and turbidity removal rate reaches 96.9%；
(2) first water outlets carry out coagulating treatment in coagulation treatment device, and dosage has been added in coagulation treatment device
For the sodium hypochlorite of the polymeric iron of 1000mg/L, the PAMC of 2mg/L and 800mg/L, and adjust coagulating treatment
When pH be 10.5-10.6；Sofening treatment is carried out in entering back into sofening treatment device, in sofening treatment device, dosage has been added
For 300mg/L lime, 200mg/LMgO, 15g/L sodium carbonate, 50mg/L AlSnSi alloy, collect the second water outlet, it is therein
COD 143mg/L、TDS 17500mg/L、Na+6300mg/L、Cl-8230mg/L、Mg2+<60mg/L、Ca2+120mg/L、SO4 2-
2150mg/L、SiO2<5mg/L, TSS 1mg/L, turbidity are 2.56NTU；
(3) second water outlets carry out hyperfiltration treatment in ultrafiltration apparatus, and GE ZW500D ultrafiltration is used in ultrafiltration apparatus
Film；Hyperfiltration treatment water outlet carries out ion-exchange treatment in entering back into ion interchange unit, collect the 4th water outlet, COD therein
117mg/L、TDS 17400mg/L、Na+6300mg/L、Cl-8230mg/L、Mg2+<2mg/L、Ca2+<2mg/L、SO4 2-2150mg/
L、SiO2<5mg/L、TSS<1mg/L, turbidity are 0NTU；
(4) the 3rd water outlets carry out nanofiltration process in nanofiltration device, using GE in nanofiltration device, DK8040F NF membranes,
COD 35mg/L, TDS 13800mg/L, Na in clear water+5200mg/L、Cl-8100mg/L、Mg2+<0.01mg/L、Ca2+<
0.01mg/L、SO4 2-15mg/L、SiO2<5mg/L、TSS<0.05mg/L, turbidity are 0NTU, and the heavy metal ion such as barium, strontium, manganese contains
Amount is not detected；
(5) clear water carries out reverse-osmosis treated in reverse osmosis unit, and reverse osmosis unit adopts two-stage SWRO, collects second
Concentrated water, reverse-osmosis treated produce COD in water<8mg/L、TDS 367mg/L、Na+132mg/L、Cl-194mg/L、Mg2+<0.01mg/
L、Ca2+<0.01mg/L、SO4 2-0.5mg/L、SiO2<0.2mg/L、TSS<0.05mg/L, turbidity are 0NTU, magnesium ion and calcium from
Son is not detected, and it is high-quality recycle-water that reverse-osmosis treated produces water, can drain in the 5th water tank, can add in production technology；
(6) second concentrated waters carry out crystallization treatment in crystallization apparatus, are further purified by solventing-out, obtain purity
>99.5% NaCl, can sell as Nacl；The crystallization water is drained in the 5th water tank, after mixing with reverse-osmosis treated product water, is carried
Rise to each reuse water spot of plant area.
Embodiment 2
Present embodiments provide a kind of processing method of desulfurization wastewater zero-emission.The processing method comprises the steps：
(1) certain Desulphurization for Coal-fired Power Plant waste water carries out Air Exposure into aerating regulation device, and the waste water after Air Exposure enters
Staticly settled in entering preformed precipitate device, collected the first water outlet, wherein, COD 1000mg/L, TDS in desulfurization wastewater
55800mg/L、Na+4300mg/L、Cl-12000mg/L、Mg2+40000mg/L、Ca2+2500mg/L、SO4 2-22000mg/L、
SiO2It is 752.8NTU that 250mg/L, TSS17000mg/L, pH are 6.0, turbidity, COD 140mg/L in the first water outlet,
TDS34260mg/L、Na+3741mg/L、Cl-7560mg/L、Mg2+21600mg/L、Ca2+1450mg/L、SO4 2-12980mg/L、
SiO2<130mg/L, TSS 900mg/L, turbidity are 23.6NTU；
(2) first water outlets carry out coagulating treatment in coagulation treatment device, and dosage has been added in coagulation treatment device
For the H of the polymeric iron of 1000mg/L, the lime of 2mg/L and 600mg/L2O2, Fe2+Mol ratio with hydrogen peroxide is 1:4, and adjust
PH during coagulating treatment is 8.5-9.5；Sofening treatment is carried out in entering back into sofening treatment device, has been added in sofening treatment device
Dosage is 300mg/L lime, 200mg/LMgO, 15g/L sodium carbonate, the AlSnSi alloy of 50mg/L, collects the second water outlet, its
In COD 143mg/L, TDS 14625mg/L, Na+5890mg/L、Cl-7560mg/L、Mg2+<54mg/L、Ca2+124mg/L、
SO4 2-1316mg/L、SiO2<4.8mg/L, TSS 1.26mg/L, turbidity are 2.50NTU；
(3) second water outlets carry out hyperfiltration treatment in ultrafiltration apparatus, and GE ZW500D ultrafiltration is used in ultrafiltration apparatus
Film；Hyperfiltration treatment water outlet carries out ion-exchange treatment in entering back into ion interchange unit, collect the 4th water outlet, COD therein
116mg/L、TDS 14535mg/L、Na+5886mg/L、Cl-7558mg/L、Mg2+<1.78mg/L、Ca2+<1.98mg/L、SO4 2-
1315mg/L、SiO2<4.8mg/L、TSS<1.25mg/L, turbidity are 0NTU；
(4) the 3rd water outlets carry out nanofiltration process in nanofiltration device, using GE in nanofiltration device, DK8040F NF membranes,
COD 34mg/L, TDS 11482mg/L, Na in clear water+4885mg/L、Cl-7437mg/L、Mg2+<0.008mg/L、Ca2+<
0.008mg/L、SO4 2-9.2mg/L、SiO2<4.5mg/L、TSS<0.06mg/L, turbidity are 0NTU, the heavy metal such as barium, strontium, manganese from
Sub- content is not detected, and nanofiltration processes gained concentrated water and is back in step (1), and mixes with desulfurization wastewater；
(5) clear water carries out reverse-osmosis treated in reverse osmosis unit, and reverse osmosis unit adopts two-stage SWRO, collects second
Concentrated water, reverse-osmosis treated produce COD in water<7.8mg/L、TDS 287mg/L、Na+117mg/L、Cl-186mg/L、Mg2+<
0.008mg/L、Ca2+<0.008mg/L、SO4 2-0.37mg/L、SiO2<0.2mg/L、TSS<0.05mg/L, turbidity be 0NTU, magnesium
Ion and calcium ion are not detected, and it is high-quality recycle-water that reverse-osmosis treated produces water, can drain in the 5th water tank, can add to production
In technique；
(6) second concentrated waters carry out crystallization treatment in crystallization apparatus, are further purified by solventing-out, obtain purity
>99.5% NaCl, can sell as Nacl；The crystallization water is drained in the 5th water tank, after mixing with reverse-osmosis treated product water, is carried
Rise to each reuse water spot of plant area.
Embodiment 3
Present embodiments provide a kind of processing method of desulfurization wastewater zero-emission.The processing method comprises the steps：
(1) certain Desulphurization for Coal-fired Power Plant waste water carries out Air Exposure into aerating regulation device, and the waste water after Air Exposure enters
Staticly settled in entering preformed precipitate device, collected the first water outlet, wherein, COD 1000mg/L, TDS in desulfurization wastewater
66800mg/L、Na+4600mg/L、Cl-13000mg/L、Mg2+44000mg/L、Ca2+2400mg/L、SO4 2-36000mg/L、
SiO2It is 752.8NTU that 250mg/L, TSS13000mg/L, pH are 6.5, turbidity, COD 180mg/L in the first water outlet,
TDS41000mg/L、Na+4000mg/L、Cl-8200mg/L、Mg2+23800mg/L、Ca2+1400mg/L、SO4 2-21200mg/L、
SiO2<135mg/L, TSS 708mg/L, turbidity are 23.71NTU；
(2) first water outlets carry out coagulating treatment in coagulation treatment device, and dosage has been added in coagulation treatment device
For the H of the iron-based flocculating agent of 1000mg/L, the PAMC of 2mg/L and 600mg/L2O2, Fe2+With rubbing for hydrogen peroxide
You are than being 1:3, and pH when adjusting coagulating treatment is 10.5-10.6；Sofening treatment is carried out in entering back into sofening treatment device, it is soft
Dosage is added in changing processing meanss for 300mg/L lime, 200mg/L magnesium chlorides, 15g/L sodium carbonate, the aluminium system of 60mg/L
Flocculant, in collection the second water outlet, and collection step (1) obtained by preformed precipitate process, the coagulating treatment and the sofening treatment
Sludge, and which is concentrated and is dehydrated, mud cake is obtained, and is given up water is produced obtained by the concentration and the dehydration with the desulfurization
Water mixes, COD 140mg/L, TDS17500mg/L, Na therein+6300mg/L、Cl-8230mg/L、Mg2+<60mg/L、Ca2+
120mg/L、SO4 2-2150mg/L、SiO2<5mg/L, TSS 1mg/L, turbidity are 2.56NTU；
(3) second water outlets carry out hyperfiltration treatment in ultrafiltration apparatus, and GE ZW500D ultrafiltration is used in ultrafiltration apparatus
Film；Hyperfiltration treatment water outlet carries out ion-exchange treatment in entering back into ion interchange unit, collect the 4th water outlet, COD therein
117mg/L、TDS 17400mg/L、Na+6300mg/L、Cl-8230mg/L、Mg2+<2mg/L、Ca2+<2mg/L、SO4 2-2150mg/
L、SiO2<5mg/L、TSS<1mg/L, turbidity are 0NTU；
(4) the 3rd water outlets carry out nanofiltration process in nanofiltration device, using GE in nanofiltration device, DK8040F NF membranes,
COD 35mg/L, TDS 13800mg/L, Na in clear water+5200mg/L、Cl-8100mg/L、Mg2+<0.01mg/L、Ca2+<
0.01mg/L、SO4 2-15mg/L、SiO2<5mg/L、TSS<0.05mg/L, turbidity are 0NTU, and the heavy metal ion such as barium, strontium, manganese contains
Amount is not detected, and nanofiltration processes gained concentrated water and is back in step (1), and mixes with desulfurization wastewater；
(5) clear water carries out reverse-osmosis treated in reverse osmosis unit, and reverse osmosis unit adopts two-stage SWRO, collects second
Concentrated water, reverse-osmosis treated produce COD in water<7mg/L、TDS 367mg/L、Na+132mg/L、Cl-194mg/L、Mg2+<0.01mg/
L、Ca2+<0.01mg/L、SO4 2-0.5mg/L、SiO2<0.2mg/L、TSS<0.05mg/L, turbidity are 0NTU, magnesium ion and calcium from
Son is not detected, and it is high-quality recycle-water that reverse-osmosis treated produces water, can drain in the 5th water tank, can add in production technology；
(6) second concentrated waters carry out crystallization treatment in crystallization apparatus, are further purified by solventing-out, obtain purity
>99.5% NaCl, can sell as Nacl；The crystallization water is drained in the 5th water tank, after mixing with reverse-osmosis treated product water, is carried
Rise to each reuse water spot of plant area.
Embodiment 4
Present embodiments provide a kind of processing method of desulfurization wastewater zero-emission.The processing method comprises the steps：
(1) certain Desulphurization for Coal-fired Power Plant waste water carries out Air Exposure into aerating regulation device, and the waste water after Air Exposure enters
Staticly settled in entering preformed precipitate device, collected the first water outlet, wherein, COD 1000mg/L, TDS in desulfurization wastewater
66800mg/L、Na+4600mg/L、Cl-13000mg/L、Mg2+44000mg/L、Ca2+2400mg/L、SO4 2-36000mg/L、
SiO2It is 752.8NTU that 250mg/L, TSS13000mg/L, pH are 6.5, turbidity, COD 180mg/L in the first water outlet,
TDS41000mg/L、Na+4000mg/L、Cl-8200mg/L、Mg2+23800mg/L、Ca2+1400mg/L、SO4 2-21200mg/L、
SiO2<135mg/L, TSS 708mg/L, turbidity are 23.71NTU；
(2) first water outlets carry out coagulating treatment in coagulation treatment device, and dosage has been added in coagulation treatment device
For the polymeric iron of 1000mg/L, the PAMC of 2mg/L and ... the sodium hypochlorite of mg/L, and adjusting at coagulation
PH during reason is 10.5-10.6；Sofening treatment is carried out in entering back into sofening treatment device, is added in sofening treatment device
Measure for 300mg/L lime, 200mg/LMgO, 15g/L sodium carbonate ... the AlSnSi alloy of mg/L, collect the second water outlet, and
Preformed precipitate process, the coagulating treatment and sludge obtained by the sofening treatment in collection step (1), and which is concentrated and is taken off
Water, is obtained mud cake, and is mixed water is produced obtained by the concentration and the dehydration with the desulfurization wastewater, COD 140mg/ therein
L、TDS 17500mg/L、Na+6300mg/L、Cl-8230mg/L、Mg2+<60mg/L、Ca2+120mg/L、SO4 2-2150mg/L、
SiO2<5mg/L, TSS 1mg/L, turbidity are 2.56NTU；
(3) second water outlets carry out hyperfiltration treatment in ultrafiltration apparatus, and GE ZW500D ultrafiltration is used in ultrafiltration apparatus
Film；Hyperfiltration treatment water outlet carries out ion-exchange treatment in entering back into ion interchange unit, collect the 4th water outlet, COD therein
117mg/L、TDS 17400mg/L、Na+6300mg/L、Cl-8230mg/L、Mg2+<2mg/L、Ca2+<2mg/L、SO4 2-2150mg/
L、SiO2<5mg/L、TSS<1mg/L, turbidity are 0NTU；
(4) the 3rd water outlets carry out carbon removal treatment in carbon removing device, remove removing carbon dioxide, delay subsequent film fouling；Again
Nanofiltration process is carried out in nanofiltration device, GE in nanofiltration device, is adopted, DK8040F NF membranes, COD 30mg/L in clear water,
TDS 13200mg/L、Na+5100mg/L、Cl-8000mg/L、Mg2+<0.01mg/L、Ca2+<0.01mg/L、SO4 2-12mg/L、
SiO2<3mg/L、TSS<0.03mg/L, turbidity are 0NTU, and the heavy metal ion content such as barium, strontium, manganese is not detected, and nanofiltration processes institute
Obtain concentrated water to be back in step (1), and mix with desulfurization wastewater；
(5) clear water carries out reverse-osmosis treated in reverse osmosis unit, and reverse osmosis unit adopts two-stage SWRO, collects second
Concentrated water, reverse-osmosis treated produce COD in water<5mg/L、TDS 330mg/L、Na+128mg/L、Cl-200mg/L、Mg2+<0.01mg/
L、Ca2+<0.01mg/L、SO4 2-0.3mg/L、SiO2<0.1mg/L、TSS<0.03mg/L, turbidity are 0NTU, magnesium ion and calcium from
Son is not detected, and it is high-quality recycle-water that reverse-osmosis treated produces water, can drain in the 5th water tank, can add in production technology；
(6) second concentrated waters carry out crystallization treatment in crystallization apparatus, are further purified by solventing-out, obtain purity
>99.6% NaCl, can sell as Nacl；The crystallization water is drained in the 5th water tank, after mixing with reverse-osmosis treated product water, is carried
Rise to each reuse water spot of plant area.
Embodiment 5
Present embodiments provide a kind of processing meanss of desulfurization wastewater zero-emission.The processing meanss, including what is be sequentially communicated
Aerating regulation device 1, preformed precipitate device 2, coagulation treatment device 3, sofening treatment device 5, ultrafiltration apparatus 7, ion interchange unit
11st, nanofiltration device 14, reverse osmosis unit 15 and crystallization apparatus 16.
By above-mentioned setting, make above-mentioned processing meanss that there is operation stability height, desulfurization wastewater high treating effect, cost
The features such as low, sodium chloride recovery purity is high.
Preferably, the molecular cut off of the NF membrane in nanofiltration device 14 be 150-300 dalton, bivalent ions retention
Rate ＞ 98%；
Reverse osmosis membrane in reverse osmosis unit 15 is seawater reverse osmosis membrane and/or disc tube reverse osmosis (dt-ro) film；
The concentrated water outlet of nanofiltration device 14 is connected with the water inlet of aerating regulation device 1.
On the basis of above-mentioned technical proposal, also include,
Carbon removing device 12, its water inlet, delivery port delivery port respectively with ion interchange unit 11, nanofiltration device 14 enter
The mouth of a river connects；
The enrichment facility 8 being sequentially communicated and dehydration device 9, the sludge import of enrichment facility 8 respectively with preformed precipitate device 2,
Coagulation treatment device 3 is connected with the sludge outlet of sofening treatment device 5, the product water out of enrichment facility 8 and dehydration device 9 with
The inlet communication of aerating regulation device 1.
On the basis of above-mentioned technical proposal, also include,
First water tank 4, its water inlet, delivery port delivery port respectively with coagulation treatment device 3, sofening treatment device 5
Water inlet is connected；
Second water tank 6, its water inlet, delivery port delivery port respectively with sofening treatment device 5, the water inlet of ultrafiltration apparatus 7
Mouth connection；
Three-tank 13, its water inlet, delivery port delivery port respectively with carbon removing device 12, the water inlet of nanofiltration device 14
Connection；
4th water tank 10, its water inlet, delivery port delivery port respectively with ultrafiltration apparatus 7, ion interchange unit 11 enter
The mouth of a river connects；
5th water tank 17, its water inlet are connected with the delivery port of reverse osmosis unit 15 and crystallization apparatus 16 respectively.
Obviously, above-described embodiment is only intended to clearly illustrate example, and the not restriction to embodiment.It is right
For those of ordinary skill in the art, can also make on the basis of the above description other multi-forms change or
Change.There is no need to be exhaustive to all of embodiment.And thus it is extended obvious change or
Among changing still in the protection domain of the invention.
Claims (10)
1. a kind of processing method of desulfurization wastewater zero-emission, comprises the steps：
(1) Air Exposure is carried out to desulfurization wastewater and preformed precipitate is processed, collect the first water outlet；
(2) coagulating treatment and sofening treatment are carried out successively to first water outlet, obtains the second water outlet；
(3) hyperfiltration treatment and ion-exchange treatment are carried out to second water outlet successively, the 3rd water outlet is collected；
(4) nanofiltration process is carried out to the 3rd water outlet, clear water is collected；
(5) reverse-osmosis treated is carried out to the clear water, obtains the second concentrated water；
(6) crystallization treatment is carried out to second concentrated water, obtains crystal salt, and collection step (5) and the product water in (6), obtain
Water up to standard.
2. processing method according to claim 1, it is characterised in that in step (2), add aerobic in the coagulating treatment
Agent, flocculant and flocculation aid；
Softening agent, desiliconizing agent, flocculant and flocculation aid have been added in the sofening treatment.
3. processing method according to claim 1 and 2, it is characterised in that in step (4), also including collecting the nanofiltration
Process gained the first concentrated water, and by its with described in step (1), desulfurization wastewater mixes the step of.
4. the processing method according to any one of claim 1-3, it is characterised in that in step (4), at the nanofiltration
Before reason, also include the step of carbon removal treatment is carried out to the 3rd water outlet.
5. the processing method according to any one of claim 1-4, it is characterised in that in step (1) and (2), also include
The preformed precipitate process, the coagulating treatment and sludge obtained by the sofening treatment are collected, and which is concentrated and is dehydrated, obtained
To mud cake, and will the concentration and product water obtained by the dehydration the step of mix with the desulfurization wastewater.
6. processing method according to claim 2, it is characterised in that the oxidant is sodium hypochlorite and/or Fenton
Reagent；
The softening agent is at least one in sodium carbonate, calcium oxide or NaOH；
The desiliconizing agent is magnesia and/or magnesium chloride；
The flocculant is AlSnSi alloy and/or iron-based flocculating agent；
The flocculation aid is lime and/or polyacrylamide.
7. the processing meanss of the processing method being used for any one of claim 1-6, it is characterised in that including being sequentially communicated
Aerating regulation device, preformed precipitate device, coagulation treatment device, sofening treatment device, ultrafiltration apparatus, ion interchange unit, receive
Filter device, reverse osmosis unit and crystallization apparatus.
8. processing meanss according to claim 7, it is characterised in that the retention molecule of the NF membrane in the nanofiltration device
Measure as 150-300 dalton, bivalent ions rejection ＞ 98%；
Reverse osmosis membrane in the reverse osmosis unit is seawater reverse osmosis membrane and/or disc tube reverse osmosis (dt-ro) film；
The concentrated water outlet of the nanofiltration device is connected with the water inlet of the aerating regulation device.
9. processing meanss according to claim 7 or 8, it is characterised in that also include,
Carbon removing device, its water inlet, delivery port delivery port respectively with the ion interchange unit, the water inlet of the nanofiltration device
Mouth connection；
The enrichment facility being sequentially communicated and dehydration device, the sludge import of the enrichment facility respectively with the preformed precipitate device,
The coagulation treatment device is connected with the sludge outlet of the sofening treatment device, the enrichment facility and the dehydration device
Produce inlet communication of the water out with the aerating regulation device.
10. processing meanss according to claim 9, it is characterised in that also include,
First water tank, its water inlet, delivery port delivery port respectively with the coagulation treatment device, the sofening treatment device
Water inlet is connected；
Second water tank, its water inlet, delivery port delivery port respectively with the sofening treatment device, the water inlet of the ultrafiltration apparatus
Mouth connection；
Three-tank, its water inlet, delivery port delivery port respectively with the carbon removing device, the water inlet of the nanofiltration device connect
It is logical；
4th water tank, its water inlet, delivery port delivery port respectively with the ultrafiltration apparatus, the water inlet of the ion interchange unit
Mouth connection；
5th water tank, its water inlet are connected with the delivery port of the reverse osmosis unit and the crystallization apparatus respectively.
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