CN109437455A - The processing equipment and method of secondary clarifier effluent Treated sewage reusing - Google Patents
The processing equipment and method of secondary clarifier effluent Treated sewage reusing Download PDFInfo
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- CN109437455A CN109437455A CN201811594830.6A CN201811594830A CN109437455A CN 109437455 A CN109437455 A CN 109437455A CN 201811594830 A CN201811594830 A CN 201811594830A CN 109437455 A CN109437455 A CN 109437455A
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- 238000012545 processing Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000010865 sewage Substances 0.000 title claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 201
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 58
- 239000002351 wastewater Substances 0.000 claims abstract description 31
- 239000013505 freshwater Substances 0.000 claims abstract description 30
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 14
- 239000012528 membrane Substances 0.000 claims description 87
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 83
- 238000004062 sedimentation Methods 0.000 claims description 35
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 32
- 239000002033 PVDF binder Substances 0.000 claims description 30
- 230000008676 import Effects 0.000 claims description 24
- 239000006228 supernatant Substances 0.000 claims description 22
- 239000000843 powder Substances 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 14
- 238000005266 casting Methods 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 230000001376 precipitating effect Effects 0.000 claims description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 8
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- 238000007634 remodeling Methods 0.000 claims description 6
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 5
- 239000002202 Polyethylene glycol Substances 0.000 claims description 5
- 229920001223 polyethylene glycol Polymers 0.000 claims description 5
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims description 4
- 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 claims description 4
- 230000001112 coagulating effect Effects 0.000 claims description 4
- 239000008367 deionised water Substances 0.000 claims description 4
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- 238000001035 drying Methods 0.000 claims description 4
- 239000013618 particulate matter Substances 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 239000011734 sodium Substances 0.000 claims description 4
- 229910052708 sodium Inorganic materials 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 238000007711 solidification Methods 0.000 claims description 4
- 230000008023 solidification Effects 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- AEQDJSLRWYMAQI-UHFFFAOYSA-N 2,3,9,10-tetramethoxy-6,8,13,13a-tetrahydro-5H-isoquinolino[2,1-b]isoquinoline Chemical compound C1CN2CC(C(=C(OC)C=C3)OC)=C3CC2C2=C1C=C(OC)C(OC)=C2 AEQDJSLRWYMAQI-UHFFFAOYSA-N 0.000 claims description 3
- 229920000388 Polyphosphate Polymers 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 claims description 3
- 230000008025 crystallization Effects 0.000 claims description 3
- ATHHXGZTWNVVOU-UHFFFAOYSA-N monomethyl-formamide Natural products CNC=O ATHHXGZTWNVVOU-UHFFFAOYSA-N 0.000 claims description 3
- 239000003960 organic solvent Substances 0.000 claims description 3
- 239000001205 polyphosphate Substances 0.000 claims description 3
- 235000011176 polyphosphates Nutrition 0.000 claims description 3
- 229920000036 polyvinylpyrrolidone Polymers 0.000 claims description 3
- 239000001267 polyvinylpyrrolidone Substances 0.000 claims description 3
- 235000013855 polyvinylpyrrolidone Nutrition 0.000 claims description 3
- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 claims description 3
- 239000000176 sodium gluconate Substances 0.000 claims description 3
- 235000012207 sodium gluconate Nutrition 0.000 claims description 3
- 229940005574 sodium gluconate Drugs 0.000 claims description 3
- 239000004698 Polyethylene Substances 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- 239000000835 fiber Substances 0.000 claims description 2
- 239000001509 sodium citrate Substances 0.000 claims description 2
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 claims description 2
- 239000002904 solvent Substances 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 abstract description 12
- 239000000126 substance Substances 0.000 abstract description 11
- 238000005370 electroosmosis Methods 0.000 abstract description 10
- 230000003647 oxidation Effects 0.000 abstract description 10
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- 238000011282 treatment Methods 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 6
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- 230000008020 evaporation Effects 0.000 abstract description 5
- 239000010893 paper waste Substances 0.000 abstract description 5
- 238000011033 desalting Methods 0.000 abstract description 3
- 150000003839 salts Chemical class 0.000 abstract description 3
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
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- 238000013508 migration Methods 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 9
- 238000001728 nano-filtration Methods 0.000 description 8
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 7
- 229910001424 calcium ion Inorganic materials 0.000 description 7
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 5
- 230000000903 blocking effect Effects 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 5
- 229910001425 magnesium ion Inorganic materials 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000003756 stirring Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000013049 sediment Substances 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000007792 addition Methods 0.000 description 2
- 239000003011 anion exchange membrane Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 2
- 238000005341 cation exchange Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000004043 dyeing Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
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- 238000003825 pressing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000010148 water-pollination Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 244000248349 Citrus limon Species 0.000 description 1
- 235000005979 Citrus limon Nutrition 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- YZCKVEUIGOORGS-IGMARMGPSA-N Protium Chemical compound [1H] YZCKVEUIGOORGS-IGMARMGPSA-N 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
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- 230000002378 acidificating effect Effects 0.000 description 1
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- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- MMCOUVMKNAHQOY-UHFFFAOYSA-N carbonoperoxoic acid Chemical compound OOC(O)=O MMCOUVMKNAHQOY-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
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- 238000006731 degradation reaction Methods 0.000 description 1
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- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- -1 has physical method Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
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- 238000001471 micro-filtration Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
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- 230000020477 pH reduction Effects 0.000 description 1
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- 239000000047 product Substances 0.000 description 1
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- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 150000003462 sulfoxides Chemical class 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000003643 water by type Substances 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
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4612—Controlling or monitoring
- C02F2201/46125—Electrical variables
- C02F2201/4613—Inversing polarity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/29—Chlorine compounds
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to technical field of waste water processing, the specially a kind of processing equipment and method of secondary clarifier effluent Treated sewage reusing.The present invention carries out desalting processing to the secondary settling tank waste water that papermaking generates using EDR, sulfate radical in water, the removal rate of chloride ion has reached 90% or more, the reclamation rate of water has reached 75% or more, using frequently pole-reversing electroosmosis, the technologies such as ultrafiltration, the processing capacity to secondary settling tank water can greatly be improved, equipment operation is easy to use, energy consumption is lower, without building more infrastructure, simultaneously, frequently pole-reversing electroosmosis technology has only carried out migration to the salt in water, COD substance is not migrated, the Advanced Oxidation Technics in Dealing to concentrated water can be removed from, it is convenient for subsequent evaporation processing, production cost is greatly saved, treated, and fresh water is recycled, greatly reduce the discharge amount of paper waste, the utilization rate of water resource is improved simultaneously, not only realize clean and environmental protection processing, also greatly Simplify original treatment process, reduce whole cost for wastewater treatment.
Description
Technical field
The invention belongs to technical field of waste water processing, specially a kind of method of secondary settling tank water depth processing.
Background technique
Membrane separation technique is a kind of emerging fluid separation techniques, can be divided mainly into pressure-driven by motive force to classify
Film and electric drive film.Pressure drive membrane can be divided into micro-filtration, ultrafiltration, nanofiltration, reverse osmosis these types by molecular cut off size again.It is super
The molecular cut off range of filter is often applied in pretreating process in 1000-100 ten thousand or so, and main trapped substance is
The impurities in water such as suspended matter, organism, colloid, bacterium, virus can effectively reduce the water quality indicators such as turbidity, COD, TOC, SDI.
Electric drive film has selective permeability, under the action of electric dialyzator DC electric field, ion selectivity to the ion in water
Through amberplex, so that electrolyte ion be separated from solution.
The industrial wastewaters such as papermaking, printing and dyeing are that a kind of water is big, waste water of complicated components, and paper waste is arranged again by pretreatment
Sewage quality can be improved by putting.
The processing method of paper waste mainly has physical method, chemical oxidization method and bioremediation at present.Physical method
Mainly there are the methods of absorption, air bearing, flocculation, belong to the primary treatment range of water quality, mainly removes the sundries in waste water and hang
Floating object to mitigate the load of subsequent treatment process, while providing service condition for subsequent technique.Chemical oxidization method mainly passes through
Chemical method converts, separates, recycles some substances in waste water.Its service condition is more demanding, often in high-temperature and high-pressure conditions
Under waste water is aoxidized, small, complicated component the water quality suitable for some waters.Bioremediation is that will have using microorganism
Machine object metabolic degradation is inorganic matter to handle waste water, can be divided mainly into aerobic method, anaerobic process, biological enzyme.Work in aerobic method
Property sludge using very extensive, operating cost is more cheap, and the secondary clarifier effluent amount of technique end is big but water quality is unstable
It is fixed, it is only capable of reaching discharge standard, water quality reuse still needs to further advanced treating.
In the prior art, after paper waste, treatment of dyeing wastewater are up to standard after direct emission or paper industry wastewater treatment
Only meet the requirement of slurrying industrial water, serious waste of resources.
Therefore, secondary settling tank water depth processing technique is researched and developed, the quality of recycle-water is improved, is allowed to meet in paper making process
Multi-faceted water demand is research staff's urgent problem.
Summary of the invention
The present invention is the deficiency in order to solve above-mentioned technology, provides a kind of conductivity, chloride ion and sulfate radical for reducing water
The method of the secondary settling tank water depth processing of ion concentration.
The technical solution adopted by the present invention to solve the technical problems is:
A kind of processing equipment of secondary clarifier effluent Treated sewage reusing, the processing equipment include the decalcification dress for being sequentially connected in series setting
It sets, ultrafiltration apparatus and EDR device (i.e. frequently pole-reversing electroosmosis system)；
The decalcification device includes sedimentation basin, dosing pump and immersible pump, and one end of the dosing pump is through conduit and to dosing
The conduit that product Chi Liantong, the other end connect extends in sedimentation basin, and the immersible pump is arranged in sedimentation basin, and the immersible pump connects
The import of the outlet pipe and ultrafiltration apparatus that connect connects；The bottom of the sedimentation basin is equipped with the discharge nozzle with valve；
The ultrafiltration apparatus includes at least one hyperfiltration membrane assembly, and the outlet of the hyperfiltration membrane assembly connects EDR device；Institute
It states setting water storage box and water pump, the water pump between hyperfiltration membrane assembly and decalcification device and is separately connected water storage box and ultrafiltration membrane group
Part；The import of the ultrafiltration apparatus is set on water storage box, is connected with outlet pipe；
The EDR device includes membrane stack, fresh water import, concentrated water import, pole water inlet, water outlet, concentrated water outlet and pole
Water out, inlet and outlet are equipped in pairs on membrane stack；The outlet of the hyperfiltration membrane assembly is separately connected the first pipe
Road and the second pipeline are successively arranged water tank, delivery pump and heat exchanger in first pipeline, the second pipeline and pole water lines,
And first pipeline, the second pipeline and pole water lines are separately connected the fresh water import of EDR device, concentrated water after respective heat exchanger
Import and pole water inlet, three water outlets on membrane stack are respectively water outlet, concentrated water outlet and pole water out.
Preferably, being equipped with agitating paddle in the sedimentation basin, the agitating paddle is located at the fulcrum at the top of sedimentation basin for precipitating
The center in pond, distance of the agitating paddle away from precipitating bottom of pond portion is in 1/5~1/2 range of sedimentation basin total height；It is described
Distance of the immersible pump away from precipitating bottom of pond portion is in 1/4~1/3 range of sedimentation basin total height.
Preferably, the ultrafiltration membrane in the hyperfiltration membrane assembly is external-compression type PVDF hollow-fibre membrane, the retention molecule of film
Amount is 5000-10 ten thousand；Film in the membrane stack is amberplex, membrane material PES, PVC, PE, PS or PP.
Preferably, the connecting pipe between the hyperfiltration membrane assembly and EDR device is equipped with flowmeter.
Another object of the present invention is to provide a kind of secondary settling tank method for deeply treating water using above-mentioned processing equipment, should
Method includes the following steps:
NaOH is added in S1, the secondary settling tank water to be processed into sedimentation basin and softens waste water, isolates supernatant after precipitating is complete
Liquid, the pH that acid adding adjusts supernatant is 5~6, and antisludging agent is added；
S2, by the hyperfiltration membrane assembly in ultrafiltration apparatus, big in water will be removed through the processed supernatant of step S1
Grain substance, reduces the SS value of water quality；
S3, the processed waste water of step S2 is sent into the membrane stack of EDR device by fresh water import and concentrated water import, is passed through
Pole water inlet is sent into NaCl solution into membrane stack, and chloride ion and sulfate ion are enriched in concentrated water；Membrane stack exports dense
Water is evaporated crystallization, fresh water direct reuse, and pole water is back to use again in EDR device.
Preferably, when bicarbonate radical content is not higher than 400mg/L in secondary clarifier effluent, being needed simultaneously in step S1
NaOH is added and carbonate softens waste water.It can be only when bicarbonate radical content is higher than 400mg/L in secondary clarifier effluent
NaOH solution is added.Due to containing a large amount of bicarbonate radical in papermaking deep waste water secondary settling tank water, production is reacted with hydroxyl
Carbonate, carbonate react to form sediment with calcium ions and magnesium ions again, this is made full use of the bicarbonate radical in water quality, section
The dosage of softening medicament is saved.And the cost of NaOH is lower than carbonate, therefore can reduce processing cost.But secondary clarifier effluent
When middle bicarbonate radical content is not higher than 400mg/L, the simple bicarbonate radical carried by NaOH in secondary clarifier effluent is not enough to soft
Change waste water, it is therefore desirable in addition add carbonate and be assisted.
Preferably, NaOH described in step S1 is the NaOH solution that mass fraction is 25%~35%, the acid is matter
The hydrochloric acid that score is 20%~30% is measured, the antisludging agent is EDTA, polyphosphate sodium, sodium gluconate or the lemon of 0.1~1mg/L
Lemon acid sodium solution.Subsequent EDR frequently pole-reversing electroosmosis needs are run under the conditions of weakly acidic, select hydrochloric acid as acidification medicine
Agent is also easy to produce scale formation because the sulfate radical that nitric acid introduces after there is strong oxidizing property, sulfuric acid to be added can be reacted with calcium ion,
Hydrochloric acid, which is added, adjusts pH cleanliness without any pollution；The alkali number being added in waste water is lower, and water pH value 8 or so, can only greatly reduce
For the dosage of the alkali and acid that neutralize, while unit price is relatively low, reduces costs.
Preferably, the inflow temperature of EDR device needs to control by heat exchanger at 35 DEG C~40 DEG C in step S3.
Preferably, ultrafiltration system described in step S2 uses modified PVDF ultrafiltration membrane, the modified PVDF ultrafiltration membrane
The preparation method comprises the following steps:
1) PVDF powder is added in the alcoholic solution of NaOH and is stirred 1~2 hour, the alcohol of the quality g and NaOH of PVDF powder are molten
The volume mL ratio of liquid is (0.1~0.5): (3.1~4), is filtered 5~10 times, is dried in 60 DEG C of baking oven after washing to constant weight,
It is spare；
2) by PVDF powder, the Nano-meter SiO_2 after drying2, neopelex and pore-foaming agent be added it is enough organic molten
In agent, stirred in water bath 20~24 hours of 60~80 DEG C casting solution, room temperature deaeration 24 hours；
3) casting solution is poured on non-woven fabrics, the film of 0.1mm~0.3mm is scraped with film-casting machine, and non-woven fabrics is soaked
It steeps into 25~30 DEG C of coagulating bath, is cleaned up after solidification with deionized water up to remodeling PVDF ultrafiltration membrane.
By above-mentioned chemistry remodeling, modified PVDF ultrafiltration membrane is obtained, there is good hydrophily, resistance to oxidation, antipollution etc.
Strainability.
Further, organic solvent described in step 2) is N, N-2- methylformamide, N, N-2- methylacetamide, diformazan
Sulfoxide, N- methyl -2- are than pyrrolidone or acetone；The pore-foaming agent is polyethylene glycol or polyvinylpyrrolidone；In step 2)
PVDF powder, Nano-meter SiO_22, neopelex and pore-foaming agent mass ratio be (10~15): (1~4): (2~5): (1~
2)。
In secondary settling tank method for deeply treating water of the invention, after adding alkali to soften waste water in supernatant calcium ions and magnesium ions concentration
Lower than 80mg/L, equipment internal incrustation in subsequent technique, bacteria breed, amberplex blocking, pollution etc. can be effectively reduced
There is strainabilities, the additions of antisludging agent such as good hydrophily, resistance to oxidation, antipollution to avoid for problem, remodeling PVDF ultrafiltration membrane
Scale problems inside ERD system equipment, it is for ultrafiltration and the permanent of electrodialysis plant, efficient operation particularly significant.
Treated that the SS value of waste water can be dropped to 5mg/L hereinafter, can reduce the place of subsequent EDR by waste water for ultrafiltration system
Load is managed, while solving the problems, such as dirty stifled, so that desalination processes are highly efficient, the molecular cut off of PVDF ultrafiltration membrane is
50000~100000.
Material is handled by frequently pole-reversing electroosmosis (EDR) system, and the chloride ion, sulfate radical in fresh water are rich in concentrated water
Collection, fresh water enter circulating and recovering processing system, and concentrated water carries out oxidation evaporation and makees waste processing.Secondary settling tank water is carried out using EDR
When desalting processing, waste water calcium ions and magnesium ions and solid suspension content are low, and waste water desalination is more efficient, and fresh-water recovery rate is also higher.Through
Fresh water conductance after crossing EDR is 1.0mS/cm hereinafter, fresh water water quality meets reuse requirement at this time, while the rate of recovery of water can reach
75% or more.
The invention has the benefit that
Desalting processing is carried out to the secondary settling tank waste water that papermaking generates using EDR, the removal rate of sulfate radical, chloride ion in water
Reach 90% or more, the reclamation rate of water has reached 75% or more, using frequently pole-reversing electroosmosis technology, can greatly improve
To the processing capacity of secondary settling tank water, equipment operation is easy to use, and energy consumption is lower, without building more infrastructure, meanwhile,
Frequently pole-reversing electroosmosis technology has only carried out migration to the salt in water, does not migrate COD substance, can remove to concentrated water
Advanced Oxidation Technics in Dealing, be convenient for subsequent evaporation processing, greatly saved production cost, treated fresh water carries out
It recycles, greatly reduces the discharge amount of paper waste, while improving the utilization rate of water resource, not only realize cleaning
Environmental protection treatment also greatly simplifies original treatment process, reduces whole cost for wastewater treatment.
Detailed description of the invention
Fig. 1 is the overall flow schematic diagram of processing equipment of the present invention.
Fig. 2 is decalcification schematic device of the present invention.
Fig. 3 is ultrafiltration apparatus schematic diagram of the present invention.
Fig. 4 is EDR schematic device of the present invention.
Fig. 5 is the flow diagram of the method for secondary settling tank water depth of the present invention processing.
In figure: 1- decalcification device；11- sedimentation basin；12- blender；13- dosing pump；14- immersible pump；15- outlet pipe；16-
Discharge nozzle；2- ultrafiltration apparatus；21- water storage box；22- water pump；23- ultrafiltration module；3-EDR device；31- membrane stack；32- delivery pump；
33- heat exchanger；The first pipeline of 34-；The second pipeline of 35-；The pole 36- water lines；37- water tank；38-1- water outlet；38-2- concentrated water
Outlet；The pole 38-3- water out；39-1- fresh water import；39-2- concentrated water import；The pole 39-3- water inlet.
Specific embodiment
Technology contents of the invention are done further and illustrated combined with specific embodiments below.
As shown in figures 1-4, a kind of processing equipment of secondary clarifier effluent Treated sewage reusing, the processing equipment include being sequentially connected in series
Decalcification device 1, ultrafiltration apparatus 2 and the EDR device 3 of setting.
As shown in Fig. 2, decalcification device 1 includes sedimentation basin 11, dosing pump 13 and immersible pump 14, one end of dosing pump 13 is through leading
Pipe is connected to drug pond to be added, and the conduit of other end connection extends in sedimentation basin 11.NaOH can be placed in drug pond to be added
The reagents such as solution, antisludging agent.Immersible pump 14 is arranged in sedimentation basin 11.The outlet pipe 15 and ultrafiltration apparatus 2 that immersible pump 14 connects
Import connection, connect hose on immersible pump 14, can arbitrarily adjust the height of immersible pump 14.In general, immersible pump 14 is away from heavy
The distance of 11 bottom of shallow lake pond is in 1/4~1/3 range of 11 total height of sedimentation basin.The bottom of sedimentation basin 11 is equipped with going out with valve
Expects pipe 16 is additionally provided with agitating paddle 12 in sedimentation basin 11, and the fulcrum that agitating paddle 12 is located at 11 top of sedimentation basin is in sedimentation basin 11
Heart position, distance of the agitating paddle 12 away from 11 bottom of sedimentation basin are the 1/3 of 11 total height of sedimentation basin.
As shown in figure 3, ultrafiltration apparatus 2 includes two hyperfiltration membrane assemblies 23, the outlet of the hyperfiltration membrane assembly 23 connects EDR
Device is arranged water storage box 21 between hyperfiltration membrane assembly 23 and decalcification device 1 and water pump 22, water pump 22 is separately connected 21 He of water storage box
Hyperfiltration membrane assembly 23, the water storage box 21 and water pump 22 of setting are to control the flow that material enters ultrafiltration apparatus 2.Ultrafiltration apparatus
2 import is set on water storage box 21, is connected with outlet pipe 15.
As shown in figure 4, EDR device includes 31, three water inlets of membrane stack and three water outlets.Membrane stack is by anode, cathode, two
A clamping plate, anion-exchange membrane, cation-exchange membrane and concentrated water partition, diluted gasket composition, the concentrated water partition sequentially stacked,
Anion-exchange membrane, diluted gasket, cation-exchange membrane are laminated to few two groups of films as one group of membrane structure among two pieces of clamping plates
Structure.Inlet and outlet are arranged in pairs on the clamping plate of membrane stack, and three inlet and outlet are respectively used to fresh water, concentrated water and pole water
Pass in and out membrane stack.Water inlet is equipped with water outlet and membrane stack 31, and three water inlets are separately connected the first pipeline 34, the second pipeline
35 and pole water lines 36, water tank 37, delivery pump 32 and heat exchange are equipped in the first pipeline 34, the second pipeline 35 and pole water lines 36
Device 33, three water inlets are respectively fresh water import 39-1, concentrated water import 39-2 and pole water inlet 39-3, and three water outlets are respectively
Water outlet 38-1, concentrated water export 38-2 and pole water out 38-3.
The course of work of the present apparatus are as follows: squeeze into secondary clarifier effluent in sedimentation basin 11, by dosing pump 13 to sedimentation basin 11
Interior addition NaOH solution and antisludging agent open agitating paddle 12 and stir material, stand one hour after mixing evenly, keep calcium ions and magnesium ions heavy
It forms sediment completely, then opens immersible pump 14 for supernatant and be transferred to water storage box 21 through outlet pipe 15, the calcium and magnesium precipitating in sedimentation basin 11
It is discharged by discharge nozzle 16.Ultrafiltration apparatus 2 is run, ultrafiltration membrane is external pressing type hollow fibrous membrane, and the molecular cut off of film is 5000-10
Ten thousand, meanwhile, 2% NaCl solution is added into the water tank 37 of pole water lines 36, after ultrafiltration module 23, the SS value of supernatant drops
Low, supernatant after ultrafiltration is entered in water tank 37 by the first pipeline 34 and the second pipeline 35, opens simultaneously the first pipeline 34, the
The heat exchanger 33 and delivery pump 32 of two pipelines 35 and pole water lines 36, the temperature into the liquid of membrane stack 31 are controlled 35 DEG C~40
DEG C, the salinity in supernatant is concentrated into concentrated water, and fresh water, concentrated water, pole water are discharged respectively, fresh water direct reuse, concentrated water evaporation knot
Crystalline substance, pole water are back to use in EDR device, and membrane stack carries out down pole automatically, and the frequency of falling pole is hour/time 3-24.
The present invention further provides a kind of secondary settling tank method for deeply treating water using above-mentioned processing equipment below, specific
Process is as shown in figure 5, this method comprises the following steps:
NaOH is added in S1, the secondary settling tank water to be processed into sedimentation basin 11 and softens waste water.When carbonic acid in secondary clarifier effluent
When hydrogen radical content is higher than 400mg/L, NaOH can only be added, react it with the bicarbonate radical in secondary settling tank water and generate carbonic acid
Root carries out sofening treatment to water.If but when bicarbonate radical content is not higher than 400mg/L in secondary clarifier effluent, needing to add simultaneously
Enter NaOH and carbonate softens waste water.Agitating paddle 12 can be opened in softening process and stirs material, and stirring is after a certain period of time
It is staticly settled, supernatant is isolated after precipitating is complete, the pH that acid adding adjusts supernatant is 5~6.Finally, antisludging agent is added.
Wherein, NaOH is the NaOH solution that mass fraction is 25%~35%, and acid is the hydrochloric acid that mass fraction is 20%~30%, scale inhibition
Agent can be EDTA, polyphosphate sodium, sodium gluconate or the sodium citrate solution of 0.1~1mg/L.
S2, it, by the hyperfiltration membrane assembly 23 in ultrafiltration apparatus 2, will be removed big in water through the processed supernatant of step S1
Particulate matter reduces the SS value of water quality.Ultrafiltration membrane is external pressing type hollow fibrous membrane, and the molecular cut off of film is 5000-10 ten thousand.It is super
After filter, concentrated water discharge, supernatant is stored in water tank 37 by the first pipeline 34 and the second pipeline 35.
S3, by the processed waste water of step S2 in water tank 37, under the conveying of delivery pump 32 by fresh water import 39-1 and
Concentrated water import 39-2 is sent into the membrane stack 31 of EDR device 3, is sent into NaCl solution into membrane stack 31 by pole water inlet 39-3.And
In transmission process, need to open the heat exchanger 33 of the first pipeline 34, the second pipeline 35 and pole water lines 36, so that into membrane stack 31
Liquid temperature control at 35 DEG C~40 DEG C.In membrane stack 31, chloride ion and sulfate ion are enriched in concentrated water, supernatant
In salinity be concentrated into concentrated water after, fresh water, concentrated water, pole water are respectively from water outlet 38-1, concentrated water outlet 38-2 and pole water out
38-3 water outlet.Membrane stack 31 exports obtained concentrated water and is evaporated crystallization, fresh water direct reuse, and pole water is back to use EDR device 3 again
In.
In addition, since sediment is more, being easy to happen fouling membrane or clogging in the treatment process of secondary settling tank waste water.
Therefore present invention is alternatively directed to it to be modified the ultrafiltration membrane in ultrafiltration system, filter its more hydrophilic, resistance to oxidation, antipollution etc.
Performance.The preparation method of modified PVDF ultrafiltration membrane can be in the following way:
1) PVDF powder is added in the alcoholic solution of NaOH and is stirred 1~2 hour, the alcohol of the quality g and NaOH of PVDF powder are molten
The volume mL ratio of liquid is (0.1~0.5): (3.1~4), is filtered 5~10 times, is dried in 60 DEG C of baking oven after washing to constant weight,
It is spare；
2) by PVDF powder, the Nano-meter SiO_2 after drying2, neopelex and pore-foaming agent be added it is enough organic molten
In agent, PVDF powder, Nano-meter SiO_22, neopelex and pore-foaming agent mass ratio be (10~15): (1~4): (2~
5): (1~2).Pore-foaming agent can be polyethylene glycol or polyvinylpyrrolidone, and organic solvent can be as N, N-2- methyl formyl
Amine, N, N-2- methylacetamide, dimethyl sulfoxide, N- methyl -2- are than pyrrolidone or acetone.Mixture is in 60~80 DEG C of water-bath
It stirs and obtains within 20~24 hours casting solution, room temperature deaeration 24 hours；
3) casting solution is poured on non-woven fabrics, the film of 0.1mm~0.3mm is scraped with film-casting machine, and non-woven fabrics is soaked
It steeps into 25~30 DEG C of coagulating bath, is cleaned up after solidification with deionized water up to remodeling PVDF ultrafiltration membrane.
Technical effect of the invention and specific implementation are further shown below by embodiment.The following example
In, the device that used device and i.e. Fig. 1~4 are shown, specific structure repeats no more.
Embodiment 1:
Chloride ion content is 375mg/L, sulfate ion content 272mg/L, conductivity in untreated secondary settling tank water
For 2000us/cm.
The method of secondary settling tank water depth processing includes the following steps:
S1, the NaOH solution softening waste water that mass fraction is 30%, lye reagent consumption amount are added into secondary settling tank water
0.8L/t, the content of waste water calcium ions and magnesium ions is 40mg/L after sofening treatment, precipitating completely after isolate supernatant, into supernatant
Adding mass fraction is 20% hydrochloric acid, and hydrochloric acid reagent consumption amount is 0.5L/t, and adjusting pH is 6.EDTA is added into material again to make
For antisludging agent, concentration of the EDTA in material is 0.1mg/L.
S2, will through the processed supernatant of step S1 by ultrafiltration system, the molecular cut off of ultrafiltration membrane is 50000~
100000, the large particulate matter in water is removed, the SS value of water quality is reduced.The ultrafiltration membrane the preparation method is as follows:
1) PVDF powder is added in the alcoholic solution of NaOH and is stirred 2 hours, the alcoholic solution of the quality g and NaOH of PVDF powder
Volume mL ratio is 1:4, is filtered 10 times, is dried in 60 DEG C of baking oven after washing to constant weight, spare；
2) by PVDF powder, the Nano-meter SiO_2 after drying2, neopelex and polyethylene glycol be added it is enough organic
In solvent N, N-2- methylformamide, stirred in water bath 20 hours of 60 DEG C casting solution, room temperature deaeration 24 hours, PVDF
Powder, Nano-meter SiO_22, neopelex and polyethylene glycol mass ratio be 10:1:3:2.
3) casting solution is poured on non-woven fabrics, the film of 0.1mm~0.3mm is scraped with film-casting machine, and non-woven fabrics is soaked
It steeps into 30 DEG C of coagulating bath, is cleaned up after solidification with deionized water up to modified PVDF ultrafiltration membrane, be assembled to ultrafiltration
In device.
S3, the processed material of step S2 is sent into EDR frequently pole-reversing electroosmosis system again, into the waste water temperature of membrane stack
Control is at 35 DEG C.Chloride ion and sulfate ion are enriched in concentrated water, and concentrated water carries out oxidation evaporation, fresh water direct reuse, pole water
Again reuse is to EDR.
Final reuse fresh water conductance is 300us/cm, and production water chloride ion content is 30mg/L, removal rate 92%, sulfate radical
The content of ion is 12mg/L, removal rate 95.6%, fresh-water recovery rate 78.9%, do not occur in experimentation fouling membrane with
The case where blocking.
Comparative example 1:
Chloride ion content is 375mg/L, sulfate ion content 272mg/L, conductivity in untreated secondary settling tank water
For 2000us/cm.
Secondary settling tank water is handled using conventional filtering and nanofiltration mode in this comparative example.In the advanced treating mistake of secondary settling tank water
Cheng Zhong, secondary settling tank water are filtered to remove macromolecule contaminant and suspended contamination in water first, and filtered water passes through at nanofiltration
Organic matter and partial salts substance of the reason by water middle-molecular-weihydroxyethyl greater than 200 remove, and nanofiltration produces water and carries out production reuse, nanofiltration concentrated water
Carry out Fenton oxidation processing.
Compared with Example 1, the operating pressure of nanofiltration is higher for this comparative example, and the cost of operation also can be higher, and it is produced
The concentrated water amount generated in the process is larger, in the higher situation of producing water ratio, COD, SO of concentrated water4 2-、Ca2+Also higher, nanofiltration membrane is easy
Water fouling is produced, also pressure is larger for subsequent Fenton oxidation processing, and Fenton oxidation processing need to build job facilities and a large amount of medicines are added
Agent, higher cost.Since nanofiltration technique can only remove the impurity of 200 or more molecular weight, for Cl-、SO4 2-Plasma can not be gone
It removes, producing water can not be in line, can only also be used as industrial water reuse.
Comparative example 2:
Chloride ion content is 375mg/L, sulfate ion content 272mg/L, conductivity in untreated secondary settling tank water
For 2000us/cm.
Compared with Example 1, difference is not carry out step S2 this comparative example, i.e., secondary settling tank water passes through S1 sofening treatment
Afterwards, supernatant is separated, supernatant does not remove large particulate matter by ultrafiltration system, and SS value is greater than 50000 in water, is sent directly into frequency
Numerous pole-reversing electroosmosis system, remaining way are same as Example 1.The feelings of serious fouling membrane and blocking occur in experimentation
Condition, can not output recoverable fresh water.
It can be seen that reducing ultrafiltration system processing step in the present invention, serious fouling membrane and blocking, experiment has occurred
It can not be normally carried out.
Comparative example 3:
Chloride ion content is 375mg/L, sulfate ion content 272mg/L, conductivity in untreated secondary settling tank water
For 2000us/cm.
Compared with Example 1, difference is not carry out step S2 this comparative example, i.e., secondary settling tank water passes through S1 sofening treatment
Afterwards, supernatant is separated, by the unmodified common ultrafiltration system of pvdf membrane, ultrafiltration system treated material is sent into identical frequency
Numerous pole-reversing electroosmosis system, remaining way are same as Example 1.Final reuse fresh water conductance is 800us/cm, produce water chlorine from
Sub- content is 50mg/L, and removal rate 86.67%, the content of sulfate ion is 35mg/L, removal rate 87.13%, fresh water
The rate of recovery is 65.5%, and the frequency that fouling membrane or blocking occur in experimentation is 9.8%.
This comparative example compared with Example 1, shows under identical runing time, the production water chloride ion of final comparative example and
The content of sulfate ion is higher than embodiment, and fresh-water recovery rate 65.5% is lower than the 78.9% of embodiment, and working efficiency is too late
Not as good as scheme listed by embodiment.Therefore, modified pvdf membrane has substance to mention the performances such as the antipollution of ultrafiltration membrane in system
It rises.
Embodiment described above is preferred version of the invention, is not intended to limit the present invention in any form,
There are also other variants and remodeling on the premise of not exceeding the technical scheme recorded in the claims.
Claims (10)
1. a kind of processing equipment of secondary clarifier effluent Treated sewage reusing, which is characterized in that the processing equipment includes being sequentially connected in series to set
Decalcification device (1), ultrafiltration apparatus (2) and the EDR device (3) set；
The decalcification device (1) includes sedimentation basin (11), dosing pump (13) and immersible pump (14), one end of the dosing pump (13)
It is connected to through conduit with drug pond to be added, the conduit that the other end is connect extends in sedimentation basin (11), immersible pump (14) setting
In sedimentation basin (11), the outlet pipe (15) of immersible pump (14) connection is connect with the import of ultrafiltration apparatus (2)；The precipitating
The bottom in pond (11) is equipped with the discharge nozzle (16) with valve；
The ultrafiltration apparatus (2) includes at least one hyperfiltration membrane assembly (23), and the outlet of the hyperfiltration membrane assembly (23) connects EDR
Device (3)；Water storage box (21) and water pump (22), the water pump are set between the hyperfiltration membrane assembly (23) and decalcification device (1)
(22) water storage box (21) and hyperfiltration membrane assembly (23) are separately connected；The import of the ultrafiltration apparatus (2) is set to water storage box (21)
On, it is connected with outlet pipe (15)；
The EDR device (3) include membrane stack (31), fresh water import (39-1), concentrated water import (39-2), pole water inlet (39-3),
Water outlet (38-1), concentrated water outlet (38-2) and pole water out (38-3), inlet and outlet are equipped in pairs in film
On heap (31)；The outlet of the hyperfiltration membrane assembly (23) is separately connected the first pipeline (34) and the second pipeline (35), and described first
Water tank (37), delivery pump (32) and heat exchanger are successively arranged in pipeline (34), the second pipeline (35) and pole water lines (36)
(33), and the first pipeline (34), the second pipeline (35) and pole water lines (36) are separately connected after respective heat exchanger (33)
Fresh water import (39-1), concentrated water import (39-2) and the pole water inlet (39-3) of EDR device, three water outlets on membrane stack (31)
Respectively water outlet (38-1), concentrated water outlet (38-2) and pole water out (38-3).
2. the processing equipment of secondary clarifier effluent Treated sewage reusing according to claim 1, which is characterized in that the sedimentation basin
(11) agitating paddle (12) are equipped in, the agitating paddle (12) is located at the center that the fulcrum at the top of sedimentation basin (11) is sedimentation basin (11)
Position, distance of the agitating paddle (12) away from sedimentation basin (11) bottom are in 1/5~1/2 range of sedimentation basin (11) total height；
Distance of the immersible pump (14) away from sedimentation basin (11) bottom is in 1/4~1/3 range of sedimentation basin (11) total height.
3. the processing equipment of secondary clarifier effluent Treated sewage reusing according to claim 1, which is characterized in that the ultrafiltration membrane group
Ultrafiltration membrane in part (23) is external-compression type PVDF hollow-fibre membrane, and the molecular cut off of film is 5000-10 ten thousand；The membrane stack (31)
In film be amberplex, membrane material PES, PVC, PE, PS or PP.
4. the processing equipment of secondary clarifier effluent Treated sewage reusing according to claim 1, which is characterized in that the ultrafiltration membrane group
Connecting pipe between part (23) and EDR device (3) is equipped with flowmeter.
5. a kind of secondary settling tank method for deeply treating water using the processing equipment as described in claim 1-4 any one, feature
It is, described method includes following steps:
S1, NaOH softening waste water is added into the secondary settling tank water to be processed in sedimentation basin (11), isolates supernatant after precipitating is complete
Liquid, the pH that acid adding adjusts supernatant is 5~6, and antisludging agent is added；
S2, it will be removed big in water through the processed supernatant of step S1 by the hyperfiltration membrane assembly (23) in ultrafiltration apparatus (2)
Particulate matter reduces the SS value of water quality；
S3, the processed waste water of step S2 is sent into EDR device (3) by fresh water import (39-1) and concentrated water import (39-2)
In membrane stack (31), NaCl solution is sent into membrane stack (31) by pole water inlet (39-3), chloride ion and sulfate ion are dense
It is enriched in water；The concentrated water that membrane stack (31) outlet obtains is evaporated crystallization, fresh water direct reuse, and pole water is back to use EDR dress again
It sets in (3).
6. secondary settling tank method for deeply treating water according to claim 5, which is characterized in that in step S1, when secondary settling tank goes out
When bicarbonate radical content is not higher than 400mg/L in water, needs that NaOH is added simultaneously and carbonate softens waste water.
7. the method for secondary settling tank water depth according to claim 5 processing, which is characterized in that NaOH described in step S1 is
The NaOH solution that mass fraction is 25%~35%, the acid are the hydrochloric acid that mass fraction is 20%~30%, the antisludging agent
For the EDTA of 0.1~1mg/L, polyphosphate sodium, sodium gluconate or sodium citrate solution.
8. the method for secondary settling tank water depth processing according to claim 5, which is characterized in that EDR device (3) in step S3
Inflow temperature need by heat exchanger (33) control at 35 DEG C~40 DEG C.
9. the method for secondary settling tank water depth processing according to claim 5, which is characterized in that ultrafiltration system described in step S2
System using modified PVDF ultrafiltration membrane, the modified PVDF ultrafiltration membrane the preparation method comprises the following steps:
1) PVDF powder is added in the alcoholic solution of NaOH and is stirred 1~2 hour, the alcoholic solution of the quality g and NaOH of PVDF powder
Volume mL ratio is (0.1~0.5): (3.1~4), is filtered 5~10 times, is dried in 60 DEG C of baking oven after washing to constant weight, standby
With；
2) by PVDF powder, the Nano-meter SiO_2 after drying2, neopelex and pore-foaming agent be added in enough organic solvents,
Stirred in water bath 20~24 hours of 60~80 DEG C casting solution, room temperature deaeration 24 hours；
3) casting solution is poured on non-woven fabrics, the film of 0.1mm~0.3mm is scraped with film-casting machine, and non-woven fabrics is dipped into
In 25~30 DEG C of coagulating bath, cleaned up after solidification with deionized water up to remodeling PVDF ultrafiltration membrane.
10. the method for secondary settling tank water depth processing according to claim 9, which is characterized in that organic described in step 2)
Solvent is N, and N-2- methylformamide, N, N-2- methylacetamide, dimethyl sulfoxide, N- methyl -2- are than pyrrolidone or acetone；It is described
Pore-foaming agent is polyethylene glycol or polyvinylpyrrolidone；PVDF powder, Nano-meter SiO_2 in step 2)2, neopelex and cause
The mass ratio of hole agent is (10~15): (1~4): (2~5): (1~2).
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|---|---|---|---|---|
| CN110548601A (en) * | 2019-09-26 | 2019-12-10 | 广西森合高新科技股份有限公司 | Gold ore dressing agent, preparation method thereof and gold ore dressing method |
| CN112358096A (en) * | 2020-10-23 | 2021-02-12 | 重庆聚狮新材料科技有限公司 | Refining method for polyphenylene sulfide rectification recovered water |
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| CN110548601A (en) * | 2019-09-26 | 2019-12-10 | 广西森合高新科技股份有限公司 | Gold ore dressing agent, preparation method thereof and gold ore dressing method |
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| CN115920658A (en) * | 2023-01-15 | 2023-04-07 | 安徽科博瑞环境科技有限公司 | Low-surface-energy anti-pollution hollow fiber membrane and preparation method thereof |
| CN115920658B (en) * | 2023-01-15 | 2023-10-20 | 安徽科博瑞环境科技有限公司 | Low-surface-energy anti-pollution hollow fiber membrane and preparation method thereof |
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| CN109437455B (en) | 2024-05-31 |
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