CN104276702B - A kind of oil gas field waste water desalination treatment process - Google Patents
A kind of oil gas field waste water desalination treatment process Download PDFInfo
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- CN104276702B CN104276702B CN201410589996.4A CN201410589996A CN104276702B CN 104276702 B CN104276702 B CN 104276702B CN 201410589996 A CN201410589996 A CN 201410589996A CN 104276702 B CN104276702 B CN 104276702B
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- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000002351 wastewater Substances 0.000 title claims abstract description 25
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 128
- 238000001728 nano-filtration Methods 0.000 claims abstract description 48
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 23
- 239000000047 product Substances 0.000 claims abstract description 22
- 239000006228 supernatant Substances 0.000 claims abstract description 19
- 238000001914 filtration Methods 0.000 claims abstract description 17
- 239000012528 membrane Substances 0.000 claims abstract description 17
- 238000000909 electrodialysis Methods 0.000 claims abstract description 12
- 230000001112 coagulant Effects 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 230000001376 precipitating Effects 0.000 claims abstract description 8
- 238000003825 pressing Methods 0.000 claims abstract description 8
- 239000010802 sludge Substances 0.000 claims abstract description 8
- 238000002425 crystallisation Methods 0.000 claims abstract description 7
- 230000005712 crystallization Effects 0.000 claims abstract description 7
- 239000006200 vaporizer Substances 0.000 claims abstract description 7
- 238000000502 dialysis Methods 0.000 claims abstract description 4
- 238000009376 nuclear reprocessing Methods 0.000 claims abstract description 4
- 239000002244 precipitate Substances 0.000 claims abstract description 4
- 238000000108 ultra-filtration Methods 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 16
- VSCWAEJMTAWNJL-UHFFFAOYSA-K Aluminium chloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 230000015271 coagulation Effects 0.000 claims description 10
- 238000005345 coagulation Methods 0.000 claims description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 238000007792 addition Methods 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-M chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 239000000701 coagulant Substances 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 4
- 239000003814 drug Substances 0.000 claims description 4
- 238000005370 electroosmosis Methods 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 230000001954 sterilising Effects 0.000 claims description 3
- 238000004659 sterilization and disinfection Methods 0.000 claims description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910001424 calcium ion Inorganic materials 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 239000000243 solution Substances 0.000 abstract description 10
- 239000012267 brine Substances 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 6
- 238000011105 stabilization Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 22
- 230000000694 effects Effects 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 235000019600 saltiness Nutrition 0.000 description 4
- 241000276438 Gadus morhua Species 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 235000019516 cod Nutrition 0.000 description 3
- 238000011033 desalting Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000003672 gas field water Substances 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000000149 penetrating Effects 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000026676 system process Effects 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000003750 conditioning Effects 0.000 description 1
- 230000000875 corresponding Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000005429 turbidity Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention discloses a kind of oil gas field waste water desalination treatment process, comprising: the former water of saliferous carries out coagulating treatment and precipitates, and obtains supernatant liquor and precipitating sludge; Precipitating sludge plate-and-frame filter press carries out press filtration, obtains pressing filtering liquid and landfill mud, and pressing filtering liquid sends former pond back to for reprocessing; Supernatant liquor carries out uf processing and obtains pretreated water; Pretreated water carries out nanofiltration process and obtains nanofiltration membrane product water and concentrated solution, and concentrated solution is sent back in settling tank after sofening treatment, for again processing; Nanofiltration membrane is produced water and is carried out electrodialytic membranes process, obtains the dense water of electric osmose division power and water dialysis, and the dense water of electrodialysis is by mechanical steam recompression (MVR) vaporizer and crystallizer solidifies further, crystallization; And electric osmose division water carries out reverse-osmosis treated, obtain reverse osmosis produced water and the reverse osmosis concentrated water of standard discharge, reverse osmosis concentrated water is sent in nanofiltration product pond and again processes.Present method can realize low cost, stabilization treatment to brine waste.
Description
Technical field
The present invention relates to oil gas field waste water-treatment technology field, be specifically related to a kind of oil gas field waste water desalination treatment process.
Background technology
Natural gas field exploitation can produce a large amount of gas-field waters, gas-field water mainly refers to the local water taken out of from gas well with Sweet natural gas in gas recovery and the condensation water produced by separator because of pressure change at collection, gas recovery Raw gas, its notable feature is that saltiness is higher, and in the every premium on currency in certain areas, salts contg is up to milligram up to a million.
Because saltiness is very high, intractability is large, in the past for the most of way adopted with layer re-injection of process of gas field wastewater, but owing to there is certain potential safety hazard in this mode, and re-injection is again by the impact of stratum bit selecting and the factor such as re-injection is limited in one's ability, therefore this processing mode is difficult to large-scale promotion in practical engineering application.
For brine waste, common processing mode mainly contains reverse osmosis method, distillation method, but the brine waste of the reverse osmosis method process of routine, saltiness is no more than 40000mg/L, and the rate of recovery is not high, produces a large amount of dense water, there is the problem of dense water secondary treatment.
Distillation method does not limit by water quality substantially, but due to chloride ion content in gas-field water general higher, require high to equipment corrosion resistance nature, therefore the overall cost of ownership of distillation method is comparatively large, and there are certain requirements heat supply source, floor space is large, and running cost is high.
Summary of the invention
The object of this invention is to provide a kind of oil gas field waste water desalination treatment process, realize the low cost to brine waste, stabilization treatment.
An embodiment provides a kind of oil gas field waste water desalination treatment process, comprise the following steps:
1) former for saliferous water is delivered to coagulation reaction tank from former pond, the former water of saliferous carries out coagulating treatment in coagulation reaction tank, and precipitates in settling tank, obtains supernatant liquor and precipitating sludge;
2) precipitating sludge plate-and-frame filter press carries out press filtration, obtains pressing filtering liquid and landfill mud, and pressing filtering liquid sends former pond back to for reprocessing, and landfill mud carries out landfill disposal;
3) supernatant liquor carries out uf processing in ultrafiltration product pond, obtains pretreated water;
4) pretreated water produces in pond in nanofiltration and carries out nanofiltration process, and obtain nanofiltration membrane and produce water and concentrated solution, concentrated solution is sent back in settling tank in softening pond after sofening treatment, for again processing;
5) nanofiltration membrane product water carries out electrodialytic membranes process in electric osmose division pond, obtains the dense water of electric osmose division power and water dialysis, and the dense water of electrodialysis is by mechanical steam recompression (MVR) vaporizer and crystallizer solidifies further, crystallization; And
6) electric osmose division water carries out reverse-osmosis treated, obtains reverse osmosis produced water and the reverse osmosis concentrated water of standard discharge, and reverse osmosis concentrated water is sent in nanofiltration product pond and again processes.
Oil gas field waste water desalination treatment process provided by the invention, has following beneficial effect:
1. for the high rigidity speciality of gas field wastewater, adopt nanofiltration technique except hard, effectively can ensure that the long-term stability of follow-up electrodialysis and reverse osmosis membrane is run, reduce fouling risk, and introduce reverse osmosis system advanced desalination when former water saltiness is reduced to 5000mg/L by electrodialysis, the water conditioning of final outflow water can be ensured, significantly can reduce overall cost of ownership again.
2. realized the minimizing of gas field wastewater by nanofiltration system, electrodialysis and reverse osmosis system combination process, there is good stability, low dirt is stifled, Water Sproading rate advantages of higher, the gas field wastewater desalting treatment rate of recovery can reach more than 70%.
Accompanying drawing explanation
Figure 1 shows that a kind of oil gas field waste water desalination treatment system adopting embodiments of the invention 1 method.
Embodiment
For making the object, technical solutions and advantages of the present invention clearly, below in conjunction with the specific embodiment of the invention and corresponding accompanying drawing, technical solution of the present invention is clearly and completely described.
Note: the reaction tank in each embodiment that the present invention is following, pond, settling tank are square or circular antiseepage pond.
Embodiment 1: oil gas field waste water desalination treatment process can comprise the following steps:
1) former for saliferous water is delivered to coagulation reaction tank from former pond, the former water of saliferous carries out coagulating treatment in coagulation reaction tank, and precipitates in settling tank, obtains supernatant liquor and precipitating sludge;
2) precipitating sludge plate-and-frame filter press carries out press filtration, obtains pressing filtering liquid and landfill mud, and pressing filtering liquid sends former pond back to for reprocessing, and landfill mud carries out landfill disposal;
3) supernatant liquor carries out uf processing in ultrafiltration product pond, obtains pretreated water;
4) pretreated water produces in pond in nanofiltration and carries out nanofiltration process, and obtain nanofiltration membrane and produce water and concentrated solution, concentrated solution is sent back in settling tank in softening pond after sofening treatment, for again processing;
5) nanofiltration membrane product water carries out electrodialytic membranes process in electric osmose division pond, obtains the dense water of electric osmose division power and water dialysis, and the dense water of electrodialysis is by mechanical steam recompression (MVR) vaporizer and crystallizer solidifies further, crystallization; And
6) electric osmose division water carries out reverse-osmosis treated, obtains reverse osmosis produced water and the reverse osmosis concentrated water of standard discharge, and reverse osmosis concentrated water is sent in nanofiltration product pond and again processes.
Embodiment 2: the supernatant liquor in embodiment 1 produces pond in ultrafiltration and carries out uf processing, and the step obtaining pretreated water can comprise:
Supernatant liquor by topping-up pump water suction and high-pressure pump draw water enter ultrafiltration product pond carry out uf processing, produce between pond at settling tank and ultrafiltration and be provided with supernatant liquor pipeline, supernatant liquor carries out self-cleaning filtering process in supernatant liquor pipeline, remove the impurity of more than 200 microns, then sterilization agent-feeding treatment is carried out, prevent from producing biological bacterium in a large number, adhere to ultrafiltration system, affect uf processing effect.
Embodiment 3: in embodiment 1 or 2, pretreated water produces in pond in nanofiltration and carries out nanofiltration process, obtain nanofiltration membrane to produce in the step of water and concentrated solution and can comprise: described pretreated water is drawn water by topping-up pump water suction and high-pressure pump and enters nanofiltration product pond and carry out nanofiltration process, produce between pond and nanofiltration product pond in ultrafiltration and be provided with pretreated water pipeline, pretreated water carries out dirty removing processing in described pretreated water pipeline, ensure that the content of calcium ion in pretreated water is not higher than 50 mg/litre, then carry out the process of adjustment pH value, ensure that the pH value of pretreated water is between 6.0 ~ 7.5.
Embodiment 4: be provided with line mixer in the pretreated water pipeline in embodiment 3, pretreated water also enters nanofiltration system after carrying out filtration treatment by the cartridge filter that nanofiltration system is preposition after mixing in line mixer.
Embodiment 5: the coagulating agent that in embodiment 1 or 2, coagulating is used is polymerize aluminum chloride or iron(ic) chloride, and addition is 10 mg/litre, is provided with whipping appts in coagulation reaction tank, starts speed of response and reaction effect that whipping appts can strengthen brine waste.
Embodiment 6: the coagulating agent that in embodiment 1 or 2, coagulating is used is polymerize aluminum chloride or iron(ic) chloride, and addition is 50 mg/litre, is provided with whipping appts in coagulation reaction tank, starts speed of response and reaction effect that whipping appts can strengthen brine waste.
Embodiment 7: the tenderizer that in embodiment 1 or 2, sofening treatment is used is sodium hydroxide or sodium carbonate, addition is 10 mg/litre.
Embodiment 8: the tenderizer that in embodiment 1 or 2, sofening treatment is used is sodium hydroxide or sodium carbonate, addition is 30 mg/litre.
Embodiment 9: in embodiment 1 or 2, the water treatment of nanofiltration membrane product can adopt the method for frequently pole-reversing electroosmosis to process, and the interpolar that falls is divided into 0.3h, and operating pressure is 0.005MPa.
Embodiment 10: in embodiment 1 or 2, the water treatment of nanofiltration membrane product can adopt the method for frequently pole-reversing electroosmosis to process, and the interpolar that falls is divided into 0.8h, and operating pressure is 0.20MPa.
Embodiment 11: be provided with line mixer between the former pond in embodiment 5 and coagulating, the former water of saliferous adds 10ppm polymerize aluminum chloride or iron(ic) chloride by former pond after pump promotes, the micro-vortex utilizing line mixer to produce make medicament quick, evenly spread to water body.
Adopt a kind of oil gas field waste water desalination treatment system of embodiments of the invention 1 method as shown in Figure 1, the working process of native system is:
Pending waste water in former pond enters reaction tank by line mixer after coagulation dosing system dosing coagulant, the waste water that reaction tank stirs enters settling tank and clarifies, settling tank supernatant liquor enters self-cleaning filter and filters after sterilization medicine system chemicals addition control, water after filtration enters ultrafiltration system through ultrafiltration water transfer pump, water after ultrafiltration system process enters into ultrafiltration and produces water tank, the ultrafiltration water produced in water tank is delivered to cartridge filter through topping-up pump and is filtered, water after filter enters into nanofiltration system through high-pressure pump and carries out the degree of depth except hard, nanofiltration is produced water and is entered into nanofiltration product water tank, the nanofiltration water produced in water tank enters into electrodialysis system and carries out advanced desalination process after supercharging, the a small amount of dense water of electrodialysis enters MVR vaporizer and realizes crystallisation solidification, de-salted water enters electric osmose division water tank, electric osmose division water produces water again and carries out reuse or qualified discharge after reverse osmosis system process, a small amount of dense water then enters nanofiltration and produces water tank, do not produce the dense water of outer row.
Use the example of present method process oil-gas field waste water as follows:
Certain Sweet natural gas production wells, the pH of gas field wastewater is 6.00, and specific conductivity is 85000us/cm, and calcium hardness is 901mg/L, and magnesium hardness is 137mg/L, COD is 1800mg/L, and the water yield is 60m
3/ sky.This gas field wastewater desalinating process selects polymerize aluminum chloride to be coagulating agent, and sodium hydroxide and sodium carbonate are tenderizer.
The flooding velocity in former pond is 60m
3/ sky, pending waste water adds 10ppm polymerize aluminum chloride by former pond after pump promotes, the micro-vortex utilizing line mixer to produce make medicament fast, evenly spread to water body, be conducive to carrying out fast of flocculation reaction, after flocculation reaction, enter settling tank, settling tank supernatant liquor is transported to ultrafiltration system by topping-up pump.
Discharge 5m is produced in ultrafiltration
3/ h, produce water and enter ultrafiltration product water tank, ultra-filtration equipment backwash water produces water tank from ultrafiltration, and backwash water is disposed to former pond.Arrange cartridge filter before nanofiltration, ultrafiltration is produced water and is filtered through cartridge filter and after high-pressure pump supercharging, enter nanofiltration system and carry out desalting treatment, and nanofiltration system is exerted oneself 4.5m
3/ h, penetrating fluid 4m
3/ h, dense water 0.5m
3/ h.Nanofiltration Scale inhibitors chemical feeding quantity is 3ppm.
The penetrating fluid 4m is firmly removed through nanofiltration
3/ h enters electrodialysis system and carries out advanced desalination process, and electrodialysis is frequently pole-reversing electroosmosis, and the interpolar that falls is divided into 30min, and operating pressure is 0.03MPa ~ 0.07MPa, and running voltage is 25V, and electric current is 32A, 3.2m
3/ h electric osmose division water qualified discharge or reuse, 0.8m
3the dense water of/h can enter MVR vaporizer and carry out crystallisation solidification process.
Experiment effect: former water COD after uf processing is 1500mg/L, and turbidity is 0.3NTU, and calcium hardness is 901mg/L, and magnesium hardness is 137mg/L, and specific conductivity is 82000us/cm; Waste water after nanofiltration process, COD is 400mg/L, and the hardness of calcium is 82mg/L, and magnesium hardness is 11mg/L, and specific conductivity is 75680us/cm; Electric osmose division water conductivity is 700us/cm, and dense water conductivity is 126135us/cm, and electrodialytic desalting rate is 60%, MVR vaporizer discharge concentration is 70%, and feed liquid enters crystallizer and realizes complete crystallization.
Oil gas field waste water desalination treatment process of the present invention adopts nanofiltration, electrodialysis and reverse osmosis advanced desalination combination process can steady running, fouling risk is little, the membranous system cleaning interval is long, can stablize for high slat-containing wastewater system recoveries rate and remain on more than 60%, MVR evaporation then finally solves the dense water whereabouts of membranous system with crystal system, fundamentally realizes the complete desalination of gas field wastewater.
Although with above-mentioned preferred embodiment to invention has been detailed description, not limit the present invention with above-described embodiment.Those skilled in the art should recognize when the technical characteristic do not departed from given by technical solution of the present invention and scope, the increase done technical characteristic, with the replacement of some same contents of this area, all should belong to protection scope of the present invention.
Claims (8)
1. an oil gas field waste water desalination treatment process, is characterized in that, comprising:
1) former for saliferous water is delivered to coagulation reaction tank from former pond, the former water of saliferous carries out coagulating treatment in coagulation reaction tank, and precipitates in settling tank, obtains supernatant liquor and precipitating sludge;
2) described precipitating sludge plate-and-frame filter press carries out press filtration, obtains pressing filtering liquid and landfill mud, and described pressing filtering liquid sends former pond back to for reprocessing, and described landfill mud carries out landfill disposal;
3) described supernatant liquor carries out uf processing in ultrafiltration product pond, obtains pretreated water;
4) described pretreated water produces in pond in nanofiltration and carries out nanofiltration process, and obtain nanofiltration membrane and produce water and concentrated solution, described concentrated solution is sent back in settling tank in softening pond after sofening treatment, for again processing;
5) described nanofiltration membrane product water carries out electrodialytic membranes process in electric osmose division pond, and obtain the dense water of electric osmose division power and water dialysis, the dense water of described electrodialysis is by mechanical steam recompression (MVR) vaporizer and crystallizer solidifies further, crystallization; And
6) described electric osmose division water carries out reverse-osmosis treated, obtains reverse osmosis produced water and the reverse osmosis concentrated water of standard discharge, and described reverse osmosis concentrated water is sent in nanofiltration product pond and again processes.
2. method according to claim 1, it is characterized in that, described supernatant liquor by topping-up pump water suction and high-pressure pump draw water enter ultrafiltration product pond carry out uf processing, produce between pond at settling tank and ultrafiltration and be provided with supernatant liquor pipeline, supernatant liquor carries out self-cleaning filtering process in described supernatant liquor pipeline, remove the impurity of more than 200 microns, then carry out sterilization agent-feeding treatment.
3. method according to claim 1 and 2, it is characterized in that, described pretreated water by topping-up pump water suction and high-pressure pump draw water enter nanofiltration product pond carry out nanofiltration process, produce between pond and nanofiltration product pond in ultrafiltration and be provided with pretreated water pipeline, pretreated water carries out dirty removing processing in described pretreated water pipeline, ensure that the content of calcium ion in pretreated water is not higher than 50 mg/litre, then carries out adjust ph process, ensure that the pH value of pretreated water is between 6.0 ~ 7.5.
4. method according to claim 3, is characterized in that, described pretreated water carried out filtration treatment before entering nanofiltration product pond, was provided with line mixer in described pretreated water pipeline.
5. method according to claim 1 and 2, is characterized in that, described coagulating coagulating agent used is polymerize aluminum chloride or iron(ic) chloride, and addition is 10 ~ 50 mg/litre, is provided with whipping appts in described coagulation reaction tank.
6. method according to claim 1 and 2, is characterized in that, described sofening treatment tenderizer used is sodium hydroxide or sodium carbonate, and addition is 10 ~ 30 mg/litre.
7. method according to claim 1 and 2, is characterized in that, described nanofiltration membrane is produced water treatment and adopted the method for frequently pole-reversing electroosmosis to process, and the interpolar that falls is divided into 0.3-0.8h, and operating pressure is 0.005MPa ~ 0.20MPa.
8. method according to claim 5, it is characterized in that, be provided with line mixer between described former pond and coagulating, the former water of saliferous adds 10ppmPAC by former pond after pump promotes, the micro-vortex utilizing line mixer to produce make medicament quick, evenly spread to water body.
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| CN101955282A (en) * | 2010-10-18 | 2011-01-26 | 江苏省环境科学研究院 | Method for realizing zero emission of dyeing wastewater with high salinity in printing and dyeing enterprises |
| CN103342432A (en) * | 2013-07-23 | 2013-10-09 | 南京工业大学 | Near zero emission process of salt-containing waste water |
| CN103896437A (en) * | 2014-01-02 | 2014-07-02 | 杭州深瑞水务有限公司 | Zero emission treatment process of high-salinity wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955282A (en) * | 2010-10-18 | 2011-01-26 | 江苏省环境科学研究院 | Method for realizing zero emission of dyeing wastewater with high salinity in printing and dyeing enterprises |
| CN103342432A (en) * | 2013-07-23 | 2013-10-09 | 南京工业大学 | Near zero emission process of salt-containing waste water |
| CN103896437A (en) * | 2014-01-02 | 2014-07-02 | 杭州深瑞水务有限公司 | Zero emission treatment process of high-salinity wastewater |
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