CN105540967B - A kind of organic wastewater minimizing, recycling processing method and processing system - Google Patents

A kind of organic wastewater minimizing, recycling processing method and processing system Download PDF

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Publication number
CN105540967B
CN105540967B CN201510906365.5A CN201510906365A CN105540967B CN 105540967 B CN105540967 B CN 105540967B CN 201510906365 A CN201510906365 A CN 201510906365A CN 105540967 B CN105540967 B CN 105540967B
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unit
reverse osmosis
processing
water
nanofiltration
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CN105540967A (en
Inventor
李春启
梅长松
刘学武
岳培恒
段世慈
康善娇
牟伟腾
张文博
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Datang International Chemical Technology Research Institute Co Ltd
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Datang International Chemical Technology Research Institute Co Ltd
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    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • 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
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • 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
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • 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
    • C02F1/52—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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological 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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes

Abstract

The present invention provides a kind of organic wastewater minimizing, recycling processing method, including step：(1) waste water is subjected to pre-treatment, obtains the water outlet after pre-treatment；(2) solid-liquid separation treatment is carried out to the water outlet that step (1) obtains；(3) separation of solid and liquid is discharged and carries out nanofiltration processing；(4) nanofiltration concentrated water processing is carried out to the nanofiltration concentrated water that step (3) obtains, obtains the processing water outlet of nanofiltration concentrated water, nanofiltration concentrated water processing water outlet return to step (3) is mixed with separation of solid and liquid water outlet, carries out nanofiltration processing；(5) the first reverse-osmosis treated is carried out to the nanofiltration production water that step (3) obtains；(6) the second reverse-osmosis treated is carried out to the first reverse osmosis concentrated water that step (5) obtains；(7) reverse osmosis concentrated liquid obtained to step (6) is evaporated crystallization treatment, obtains crystal salt and evaporation condensate.The present invention also provides the processing systems for implementing this method.By the method and system of the present invention, minimizing, the recycling of sewage are really realized.

Description

A kind of organic wastewater minimizing, recycling processing method and processing system
Technical field
The present invention relates to technical field of waste water processing, more particularly to a kind of organic wastewater minimizing, the processing of recycling Method and for implementing the organic wastewater minimizing of this method, recycling treatment system.
Background technology
At present, the discharge standard of the industries such as coal chemical industry, petrochemical industry, printing and dyeing is increasingly stringent, sewage minimizing, recycling by Gradually become the inevitable choice of all industries and society.In actual process, because being subject to processing the factors such as technology and processing cost Restriction, processing procedure generate middle water be broadly divided into two kinds：Water is the filtering water outlet after biochemical treatment in the first, this Middle water can be sub-divided into multi-medium filtering water outlet, micro-filtration water outlet and ultra-filtration water, and the difference of three is mainly suspended matter and turbidity Difference；Water is the production water that water obtains again through reverse-osmosis treated in the first in second.Water is more because remaining in the first Macromolecular hardly degraded organic substance, multivalent ion, in actual use there are foam it is more, have peculiar smell, corrosivity and/or fouling Property various problems, the use scope such as strong be very limited.Water is reverse osmosis produced water in second, and water quality is preferable, but is handled It is expensive, and a large amount of concentration organic wastewaters of reverse osmosis generation, all kinds of pollutant concentrations are higher, can not discharge.
Film concentration technology " nanofiltration with high salt is used currently for the concentration organic wastewater of the reverse osmosis discharge of intermediate water reuse system more + reverse osmosis " further concentrate, the organic concentrate of height with high salt of nanofiltration and reverse osmosis discharge enters vapo(u)rization system concentration, crystallization.By Organic matter and salinity are very high in the concentrate, and vapo(u)rization system is caused to generate serious fouling, flies that material, foam be more, crystal salt Middle organic concentration height, evaporation condensate COD high, the problems such as conductivity is high, seriously affect the operation of vapo(u)rization system.In addition, In actual motion, after reverse osmosis concentrated water enters film concentrated water system with high salt, due to the further concentration of organic matter and salinity, fouling and Etching problem seriously affects the safe and stable operation of system, the service life of film greatly shortens, and invests and runs than more prominent Cost is very high.
Chinese patent CN201510189929 discloses a kind of printing and dyeing wastewater recovery and disposal method, and the invention is using adjusting Pond, coagulative precipitation tank, composite aeration activated sludge reaction pond, hydrolysis acidification pool, contact-oxidation pool, secondary settling tank, membrane biological reaction Pond and reverse osmosis reaction tank, are recycled.Since the biodegradability of dyeing waste water is poor, there are still more after biochemical treatment Solubilised state hardly degraded organic substance, and ultrafiltration membrane is very low to the organic removal rate of solubilised state in real process, it is almost nil；Though It is so reverse osmosis to have very high removal rate to this partial organic substances, but produced during reverse osmosis concentration a large amount of high saliferous and The concentrated water of organic matter, it is clear that waste water as discharge does not meet environmental requirement, and the multivalent ion in organic matter and water Serious fouling membrane can be caused, influences the operation of system.
Chinese patent CN201210057639 discloses a kind of system for recycling and treating coking wastewater and method, which includes Coagulating basin, inclined-plate clarifying basin, ultrafiltration apparatus, ultrafiltration production pond, first pump housing, first filter, the second filter, the second pump Body, nanofiltration device, nanofiltration production pond, the third pump housing, third filter, reverse osmosis unit and reverse osmosis produced pond, nanofiltration are dense Water makees sintering processes, and reverse osmosis concentrated water makees evaporation process.Although the technique proposes place to nanofiltration concentrated water and reverse osmosis concentrated water Reason method, but since nanofiltration concentrated water amount and reverse osmosis concentrated water are larger, nanofiltration concentrated water organic concentration is low, calorific value is low, adopts With sintering processes, processing cost costliness；Although reverse osmosis concentrated water have passed through concentration, but salt content is still relatively low, if using steaming Hair processing, processing cost are high.
Invention content
In order to overcome the above problem and defect of the prior art, the present invention provides a kind of stable, of low cost And the good organic wastewater minimizing for the treatment of effect, recycling processing method and its processing system, it is achieved thereby that wastewater minimisation Change, recycling.
The present invention provides a kind of organic wastewater minimizing, recycling processing method, this method includes sequentially following Step：
(1) pre-treatment is carried out to organic wastewater, obtains the water outlet after pre-treatment；Wherein, the pre-treatment is selected from pretreatment And/or biochemical treatment and/or advanced treating；Wherein, the pretreatment is in coagulation, oil removal, air supporting, precipitation, filtering, stripping It is one or more；The one kind or more of the advanced treating in coagulating sedimentation, absorption, advanced oxidation, biofilter processing Kind；
(2) solid-liquid separation treatment is carried out to the water outlet that step (1) obtains, obtains separation of solid and liquid water outlet；
(3) nanofiltration processing is carried out to the separation of solid and liquid water outlet that step (2) obtains, obtains nanofiltration production water and nanofiltration concentrated water；
(4) nanofiltration concentrated water processing is carried out to the nanofiltration concentrated water that step (3) obtains, obtains the water outlet of nanofiltration concentrated water processing, receive The water outlet of filter concentrated water processing is back to step (3) and is mixed with separation of solid and liquid water outlet, carries out nanofiltration processing；Wherein, the nanofiltration Concentrated water processing is one or more in biochemical optimization processing, sofening treatment, MBR processing；
(5) the first reverse-osmosis treated is carried out to the nanofiltration production water that step (3) obtains, obtains the first reverse osmosis produced water and first Reverse osmosis concentrated water；Preferably, the part for nanofiltration production water step (3) obtained is drawn, to carry out reuse/discharge or be used as The raw water of advanced purification system；
(6) the second reverse-osmosis treated is carried out to the first reverse osmosis concentrated water that step (5) obtains, obtains the second reverse osmosis produced water With the second reverse osmosis concentrated water；
(7) the second reverse osmosis concentrated water obtained to step (6) is evaporated crystallization treatment, obtains crystal salt and evaporative condenser Liquid.
According to the method for the present invention, wherein, organic wastewater include but not limited to coal chemical industry, petrochemical industry, pharmacy, printing and dyeing, The industrial organic waste water and sanitary sewage of food service industry discharge.
According to the method for the present invention, wherein, in the method step (1), pre-treatment can go the overwhelming majority in water removal Organic matter, ammonia nitrogen, oil, nitrate nitrogen, phosphate, suspended matter.The biochemical processing method includes but not limited to Anaerobic Treatment, water Solve acidification, anoxic treatment, Aerobic Process for Treatment and combinations thereof；Wherein Anaerobic Treatment includes anaerobic filter processing, up-flow anaerobism Sludge Bed processing, anaerobic fluidized bed processing and combinations thereof；Aerobic Process for Treatment includes contact-oxidation pool and handles, at biological aerated filter It is one or more in reason, activated sludge tank processing.Advanced treating includes but not limited to coagulating sedimentation, absorption, advanced oxidation, life Object filter tank processing and combinations thereof, wherein advanced oxidation include ozone oxidation, Fenton (Fenton) oxidation, fenton-type reagent and its Combination.
According to the method for the present invention, wherein, in the method step (2), it is heavy to be used by the water outlet that step (1) obtains Shallow lake, coagulating sedimentation, air supporting, filtering, UF membrane and combinations thereof carry out separation of solid and liquid, with go in water removal most suspended matter and Turbidity.Preferably, membrane separating method includes micro-filtration UF membrane and/or Ultra filtration membrane, solid reuse after separation of solid and liquid or into Disposition is transported outward after the dehydration of one step.A concentration of 0~the 100mg/L, preferably 0~50mg/L of the suspended matter of separation of solid and liquid production water；It is turbid It spends for 0~100NTU, preferably 0~50NTU.
According to the method for the present invention, wherein, in the method step (3), water is produced to the separation of solid and liquid that step (2) obtains With step (4) return nanofiltration concentrated water carry out nanofiltration processing, by most of organic matter, hardness, two level and the multivalence in water from Son, partial solubility total solid (TDS) are detached and are concentrated.Wherein, nanofiltration processing is carried out using nano filter membrance device；Preferably, exist Cartridge filter is set before nanofiltration device；NF membrane is sulfonated polyether sulfone film and/or polyamide composite film.Nanofiltration production water recycling Rate is 60~95%, preferably 70~90%；Salt rejection rate 5~60%, preferably 10~50%；Organic removal rate 30~ 100%, preferably 50~90%；Divalent and multivalent ion removal rate 20~100%, preferably 40~98%.
According to the method for the present invention, wherein, in the method step (4), the nanofiltration concentrated water that step (3) obtains is carried out Nanofiltration concentrated water processing, to remove most of organic matter, divalent and the multivalent ion and hardness in water removal.Preferably, biochemical optimizes Processing includes absorption, advanced oxidation, hydrolysis acidification, other change Organic substance in water molecular structures and composition to improve biochemical sewage It is one or more in the method for property.It is highly preferred that advanced oxidation includes ozone oxidation, Fenton oxidation, fenton-type reagent And combinations thereof.Sofening treatment includes one or more in lime softening, carbonate deposition, ion exchange；Further, lime is soft Turn to white lime softening and/or quick lime softening；The carbonate used in carbonate deposition is sodium carbonate and/or sodium bicarbonate； Ion exchange includes one or more during cation bed ion exchange, anion bed ion exchange and mixed bed ion exchange.MBR processing It is carried out using micro-filtration MBR membrane bioreactors and/or ultrafiltration MBR membrane bioreactors.The organic matter of nanofiltration concentrated water processing water outlet Removal rate 70~95%, preferably 80~90%；Hardness removal rate is 80~95%, preferably 85~90%.
According to the method for the present invention, wherein, in the method step (5), the nanofiltration production water that step (3) obtains is carried out First reverse-osmosis treated, with the total dissolved solid of the removal overwhelming majority and remaining organic matter.Preferably, the first reverse-osmosis treated It is carried out using reverse osmosis membrane；Preferably, cartridge filter is set before reverse osmosis membrane.It is highly preferred that reverse osmosis membrane is acetic acid Cellulose membrane and/or polyamide composite film.
The rate of recovery of first reverse osmosis produced water is 50~80%, preferably 55~75%；Salt rejection rate 80~99%, preferably 90~98.5%；Organic removal rate 80~100%, preferably 90~98%.
According to the method for the present invention, wherein, in the method step (6), step (5) is obtained first reverse osmosis concentrated Water carries out the second reverse-osmosis treated, further to concentrate total dissolved solid and organic matter, and generates less salt production water.Preferably, Second reverse-osmosis treated is carried out using reverse osmosis membrane apparatus；Preferably, cartridge filter is set before reverse osmosis membrane apparatus；More Preferably, reverse osmosis membrane is pollution-resistant brackish water desalination film and/or pollution-resistant sea water desalination membrane.
The second reverse osmosis produced water rate of recovery is 40~75%, preferably 50~70%；Salt rejection rate 80~99%, preferably 90 ~98.5%；Organic removal rate 80~100%, preferably 90~98%.
According to the method for the present invention, wherein, in the method step (7), step (6) is obtained second reverse osmosis concentrated Water is evaporated crystallization treatment, to generate crystal salt, and recycles condensate liquid.Preferably, evaporative crystallization processing is using evaporator, knot One or more progress in brilliant device, crystal salt separator.It is highly preferred that evaporator is MVR evaporators or multi-effect evaporator；Knot Brilliant device is crystallizing evaporator or cooler crystallizer；Crystal salt separator is centrifuge.Crystal salt includes but not limited to sodium chloride, sulphur It is one or more in sour sodium, magnesium sulfate, sodium nitrate.
20~500 μ s/cm of conductivity of condensate liquid, preferably 30~200 μ s/cm；A concentration of the 10 of total dissolved solid ~300mg/L, preferably 20~100mg/L；A concentration of 1~50mg/L of TOC (total organic carbon), preferably 2~30mg/L； COD is 5~100mg/L, preferably 10~50mg/L.
According to the method for the present invention, wherein, the production water of processing method of the invention and processing system is included by present invention side The water outlet of separation of solid and liquid that the step of method (2) obtains, the nanofiltration production water obtained by (3) the step of the method for the present invention, by present invention side The first reverse osmosis produced water that the step of method (5) obtains, the second reverse osmosis produced water obtained by (6) the step of the method for the present invention, by The evaporation condensate that the step of the method for the present invention (7) obtains.These production water can be with reuse/discharge or as advanced purification system Raw water.
The present invention also provides a kind of for implementing the processing system of the organic wastewater minimizing of the method for the present invention, recycling System, the processing system include the pretreatment unit being in fluid communication successively, solid-liquid separation unit, nano-filtration unit, are connected to nanofiltration list Member concentrated water water outlet and solid-liquid separation unit water outlet between nanofiltration concentrated water processing unit, the first reverse osmosis units, second Reverse osmosis units and evaporative crystallization unit.
Wherein, solid-liquid separation unit receives the water outlet from pretreatment unit, and after carrying out solid-liquid separation treatment, what is obtained consolidates Liquid separation water outlet is sent to nano-filtration unit.
Nano-filtration unit receives the separation of solid and liquid water outlet from solid-liquid separation unit, after carrying out nanofiltration processing, obtains nanofiltration production Water and nanofiltration concentrated water send nanofiltration concentrated water to nanofiltration concentrated water processing unit.
Nanofiltration concentrated water processing unit receives the nanofiltration concentrated water from nano-filtration unit, after carrying out nanofiltration concentrated water processing, is received Filter the water outlet of concentrated water processing unit；After the water outlet of nanofiltration concentrated water processing unit is mixed with separation of solid and liquid water outlet, nanofiltration list is sent back to Member.
First reverse osmosis units receive the nanofiltration production water from nano-filtration unit, after carrying out the first reverse-osmosis treated, obtain the One reverse osmosis produced water and the first reverse osmosis concentrated water；First reverse osmosis concentrated water is sent to the second reverse osmosis units.
Second reverse osmosis units receive the first reverse osmosis concentrated water from the first reverse osmosis units, carry out the second reverse osmosis place After reason, the second reverse osmosis produced water and the second reverse osmosis concentrated water are obtained；Second reverse osmosis concentrated water is sent to evaporative crystallization unit.
Evaporative crystallization unit receives the second reverse osmosis concentrated water from the second reverse osmosis units, through evaporative crystallization, is tied Brilliant salt and evaporation condensate.
Preferably, in processing system of the present invention, solid-liquid separation unit, nano-filtration unit, the first reverse osmosis units, The production water of second reverse osmosis units and evaporative crystallization unit send to reuse/discharge or send to advanced purification system as raw water.
Preferably, in processing system according to the present invention, pretreatment unit includes pretreatment unit and/or biochemical treatment Unit and/or advanced treatment unit.It is highly preferred that pretreatment unit includes but not limited to coagulation, oil removal, air supporting, precipitation, mistake It is one or more in filter, stripping.Preferably, biochemical treatment unit includes but not limited to Anaerobic Treatment unit and/or hydrolysis acid Change and/or anoxic treatment unit and/or aerobic treatment unit；It is highly preferred that Anaerobic Treatment unit includes but not limited to anaerobism filter Pond, upflow anaerobic sludge blanket process, anaerobic fluidized bed and combinations thereof；Aerobic treatment unit includes but not limited to contact-oxidation pool, exposes It is one or more in gas biofilter, activated sludge tank.Preferably, advanced treatment unit includes but not limited to coagulating sedimentation list Member, absorbing unit, advanced oxidation unit, biofilter and combinations thereof；It is highly preferred that advanced oxidation unit includes ozone oxidation list Member, Fenton oxidation unit, fenton-type reagent unit and combinations thereof.
Preferably, in processing system according to the present invention, solid-liquid separation unit includes precipitation unit, coagulating sedimentation list Member, air flotation cell, filter element, film separation unit and combinations thereof；It is highly preferred that film separation unit includes micro-filtration film separation unit And/or Ultra filtration membrane unit.
Preferably, in processing system according to the present invention, nano-filtration unit is nano filter membrance device；It is highly preferred that nanofiltration list Member further includes the cartridge filter before being arranged on nano filter membrance device.It is highly preferred that NF membrane is sulfonated polyether sulfone film and/or gathers Amide composite membrane.
Preferably, in processing system according to the present invention, nanofiltration concentrated water processing unit include biochemical optimization unit and/ Or pliable cell and/or MBR unit.It is highly preferred that biochemical optimization unit includes absorbing unit, advanced oxidation unit, hydrolysis The one kind being acidified in unit or other processing units for changing Organic substance in water molecular structure and composition to improve biochemical sewage It is or a variety of.More preferably, advanced oxidation unit includes ozone oxidation unit, Fenton oxidation unit, fenton-type reagent unit And combinations thereof.Preferably, pliable cell is lime pliable cell, carbonate deposition unit, ion-exchange unit and combinations thereof；More Preferably, lime pliable cell is white lime pliable cell and/or quick lime pliable cell；Carbonate deposition unit includes carbonic acid Sodium and/or sodium bicarbonate precipitation unit；Ion-exchange unit is cation bed ion-exchange unit, anion bed ion-exchange unit, mixed bed Ion-exchange unit and combinations thereof.It is highly preferred that MBR unit is given birth to for micro-filtration MBR membrane biological reactions unit and/or ultrafiltration MBR films Object reaction member.
Preferably, in processing system according to the present invention, the first reverse osmosis units are reverse osmosis membrane apparatus；More preferably Ground, the first reverse osmosis units further include the cartridge filter before being arranged on the first reverse osmosis unit.It is highly preferred that the first reverse osmosis Reverse osmosis membrane in saturating unit is cellulose acetate film and/or polyamide composite film.
Preferably, in processing system according to the present invention, the second reverse osmosis units are reverse osmosis membrane apparatus；More preferably Ground, the second reverse osmosis units further include the cartridge filter before being arranged on anti-second reverse osmosis units.It is highly preferred that second is anti- Reverse osmosis membrane in permeation unit is pollution-resistant brackish water desalination film and/or pollution-resistant sea water desalination membrane.
Preferably, in processing system according to the present invention, evaporative crystallization unit includes evaporator, crystallizer, crystal salt Separator.It is highly preferred that evaporator is MVR evaporators or multi-effect evaporator；Crystallizer includes crystallizing evaporator, crystallisation by cooling Device；Crystal salt separator is centrifuge.
Separation of solid and liquid from processing unit is produced water, nanofiltration production water, the first reverse osmosis produced water, the second reverse osmosis produced water, is steamed It feels cold lime set, qualified discharge or requires to carry out reasonable reuse or as advanced purification system according to water spot water water quality, water Raw water.
The processing method and processing system of the present invention has but is not limited to following advantageous effect：
1. using nanofiltration as reverse osmosis pre-treating technology, most organic matter and two in water is produced in retention removal nanofiltration Valency and multivalent ion, hardness reduce the risk of the first reverse osmosis units and follow-up second reverse osmosis units fouling and pollution, can The rate of recovery of reverse osmosis units is improved, extends the service life of reverse osmosis units, ensures the safe and stable operation of reverse osmosis units, And reduce intractability, processing load and equipment investment and the operating cost of follow-up strong brine.
2. using nanofiltration concentrated water processing unit processes nanofiltration concentrated water, the production water of nanofiltration concentrated water processing unit returns to nano-filtration unit The treatment process reprocessed, the processing system for realizing the present invention are generated without nanofiltration concentrated water, improve the recycling of system water Rate.
3. the difficult drops of remnants most in water removal can not only be gone using nanofiltration concentrated water processing unit processes nanofiltration concentrated water Organic matter is solved, and the most divalent and multivalent ion in water removal can be gone, reduces nanofiltration by organic pollution and knot The risk of dirt.
Water during 4. the present invention is used as using nanofiltration production water, production water quality is significantly better than solid-liquid separation unit production water quality, And its cost of water treatment per ton is substantially less than reverse osmosis produced water.Water during nanofiltration production water is used as, big especially as water consumption During recirculating cooling water system moisturizing, there is solid-liquid separation unit and the incomparable advantage of reverse osmosis produced water, not only it is processed into This is low, and its organic matter, hardness content are very low, are conducive to the safe and stable operation of circulation.
5. the processing method and processing system of the present invention are further to the first reverse osmosis concentrated water using the second reverse-osmosis treated The second reverse osmosis produced water is recycled in concentration, using evaporative crystallization unit to the second reverse osmosis concentrated water condensing crystallizing, extracts crystal salt, And evaporation condensate is recycled, really realize the zero-emission of waste water.
6. the present invention carries out reuse by the processing different degrees of to organic wastewater, and by quality and purposes, really realize The minimizing of sewage, recycling, energy-saving purpose.
Description of the drawings
Hereinafter, carry out the embodiment that the present invention will be described in detail with reference to attached drawing, wherein：
Fig. 1 show organic wastewater minimizing of the present invention, recycling processing method an embodiment technological process Schematic diagram；
Fig. 2 shows organic wastewater minimizing of the present invention, the schematic diagrames of an embodiment of recycling treatment system；
Fig. 3 shows that the present invention is used for the organic wastewater minimizing of crushed coal pressure gasifying wastewater treatment, recycling treatment system The schematic diagram of system；
Fig. 4 shows that the present invention is used for the organic wastewater minimizing of crushed coal pressure gasifying wastewater treatment, recycling treatment system The detail drawing of system；
Fig. 5 shows organic wastewater minimizing of the present invention for petroleum asphaltene processing, recycling treatment system Schematic diagram；
Fig. 6 shows organic wastewater minimizing of the present invention for petroleum asphaltene processing, recycling treatment system Detail drawing；
Fig. 7 shows the present invention for the organic wastewater minimizing for the treatment of of dyeing wastewater, the signal of recycling treatment system Figure；And
Fig. 8 shows the present invention for the organic wastewater minimizing for the treatment of of dyeing wastewater, the detail drawing of recycling treatment system.
Specific embodiment
It is further illustrated the present invention below by specific embodiment, it should be understood, however, that, these embodiments are only It is used for specifically describing in more detail, and is not to be construed as limiting the present invention in any form.
This part carries out general description to the material and test method that are arrived used in present invention experiment.Although it is It is it is known in the art that still the present invention still uses up herein to realize many materials and operating method used in the object of the invention It may detailed description.It will be apparent to those skilled in the art that within a context, if not specified, material therefor of the present invention and behaviour It is well known in the art as method.
Embodiment 1
The present embodiment is used for the crushed coal pressure gasifying wastewater reduction, recycling processing method and its processing that illustrate the present invention System.
Crushed coal pressure gasifying wastewater reduction as shown in Figure 1, recycling treatment system, the processing system mainly include Pretreatment unit, solid-liquid separation unit, nano-filtration unit, the first reverse osmosis units, the second reverse osmosis list being sequentially in fluid communication Member, evaporative crystallization unit and the nanofiltration being connected between the concentrated water water outlet of nano-filtration unit and solid-liquid separation unit water outlet Concentrated water processing unit.
The technical data setting of the processing system is as follows：
Pretreatment unit
Each subelement of pretreatment unit is followed successively by：Pretreatment system and biochemical treatment system.
Each subsystem of pretreatment system is followed successively by：Tube separators, cavitation air flotation pond, each subsystem of biochemical treatment unit according to It is secondary to be：Anaerobic pond, anoxic pond, aerobic tank.
Each major parameter：
The hydraulic detention time of Tube separators：1h
The hydraulic detention time of cavitation air flotation system：30min
The hydraulic detention time of anaerobic pond reaction zone is for 24 hours
The hydraulic detention time of anoxic pond reaction zone is 10h
The hydraulic detention time of aerobic tank reaction zone is 36h
(1) solid-liquid separation unit
Each subelement of solid-liquid separation unit is followed successively by：Coagulating sedimentation, filtering, ultrafiltration, each major parameter：
The hydraulic detention time 3h of coagulating sedimentation system
5~10m/h of filtering velocity of filtration system
Ultrafiltration membrane is PVDF external pressure hollow-fibre membranes
(2) nano-filtration unit
Each subsystem of nano-filtration unit is followed successively by：Cartridge filter, nanofiltration, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Nanofiltration film type is polyamide composite film
(3) nanofiltration concentrated water processing unit
Each subelement of nanofiltration concentrated water processing unit is followed successively by：Biochemical optimization system, melded system, MBR system, it is each main Parameter：
Biochemical optimization system be Fenton oxidation system, Fenton reaction time 3h
Melded system is " lime melded system+carbonate melded system "
MBR system be " anoxic+aerobic+built-in ultrafiltration membrane system ", 6000~12000mg/L of sludge concentration
(4) first reverse osmosis units
Each subsystem of first reverse osmosis units is followed successively by：Cartridge filter, first reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant brackish water desalination reverse osmosis membrane original paper
(5) second reverse osmosis units
Each subsystem of second reverse osmosis units is followed successively by：Cartridge filter, second reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant seawater desalination reverse osmosis film original paper
(6) evaporative crystallization unit
Each subsystem of evaporative crystallization unit is followed successively by：Vapo(u)rization system, crystal system, crystal salt piece-rate system, each main ginseng Number：
Vapo(u)rization system is triple effect evaporation system
Crystal system is evaporation and crystallization system
Crystal salt piece-rate system is centrifugal separation system
Crystal salt is mainly sodium chloride
50 μ s/cm of evaporation condensate conductivity
Crushed coal pressure gasifying waste water, pH value be 8~9, COD 4000mg/L, a concentration of 400mg/L of volatile phenol, ammonia A concentration of 250mg/L of nitrogen, a concentration of 70mg/L of petroleum substance.
After premenstrual processing unit processes, it is discharged COD≤200mg/L, concentration≤1mg/L of volatile phenol, the concentration of ammonia nitrogen≤ 5mg/L, pH value 7~8, oil content≤5mg/L.
Waste water after pre-treatment produces water COD≤150mg/L, concentration≤5mg/ of ammonia nitrogen after solid-liquid separation unit is handled L, pH value 7~8,0.05~1.0NTU of turbidity, the μ s/cm of conductivity≤1500, salt content≤1000mg/L, total hardness≤300mg/ L, concentration≤120mg/L of sulfate radical.
Solid-liquid separation unit processing gained waste water is after nano-filtration unit is handled, the production water rate of recovery >=95%, and production water COD≤ 50mg/L, the μ s/cm of conductivity≤1000, salt content≤800mg/L, total hardness≤40mg/L, concentration≤5mg/L of sulfate radical, Concentrated water COD >=1000mg/L, the μ s/cm of conductivity >=8000, salt content >=5000mg/L, total hardness >=2200mg/L, sulfate radical Concentration >=1100mg/L.
Nano-filtration unit processing gained nanofiltration concentrated water produces water COD≤100mg/L, electricity after nanofiltration concentrated water processing unit processes The μ s/cm of conductance≤4500, salt content≤3000mg/L, total hardness≤20mg/L.
Nanofiltration production water produces the water rate of recovery after the processing of the first reverse osmosis units obtained by nanofiltration concentrated water processing unit processes 75%, produce water TOC≤5mg/L, the μ s/cm of conductivity≤30, salt content≤25mg/L, concentrated water COD >=180mg/L, conductivity >= 3900 μ s/cm, salt content >=3100mg/L, total hardness >=160mg/L, concentration >=20mg/L of sulfate radical.
First reverse osmosis concentrated water of the first reverse osmosis units processing gained is after the processing of the second reverse osmosis units, production water recycling Rate 70% produces water TOC≤10mg/L, the μ s/cm of conductivity≤100, salt content≤70mg/L, concentrated water COD >=500mg/L, conductance The μ s/cm of rate >=13000, salt content >=10000mg/L, total hardness >=530mg/L, concentration >=60mg/L of sulfate radical.
Second reverse osmosis concentrated water of the second reverse osmosis units processing gained is after evaporative crystallization cell processing, condensate liquid recycling Rate 90% produces water TOC≤10mg/L, and the μ s/cm of conductivity≤100, salt content≤70mg/L, crystal salt is sodium chloride.
Nanofiltration production water meets recirculating cooling water system moisturizing water quality requirement, partly as recirculated cooling water moisturizing.First is anti- Infiltration production water, the second reverse osmosis produced water and evaporation condensate are used as power chemical water treatment system make-up water source.
Embodiment 2
The present embodiment is used for the petroleum asphaltene minimizing, recycling processing method and its processing system that illustrate the present invention System.
Petroleum asphaltene minimizing as shown in Figure 2, recycling treatment system, the processing system are mainly included successively The pretreatment unit of fluid communication, solid-liquid separation unit, nano-filtration unit, the first reverse osmosis units, the second reverse osmosis units, evaporation Crystalline element and the nanofiltration concentrated water processing being connected between the concentrated water water outlet of nano-filtration unit and solid-liquid separation unit water outlet Unit.The technical data setting of processing system described in the present embodiment is as follows：
(1) pretreatment unit
Each subelement of pretreatment unit is followed successively by：Pretreatment system, biochemical treatment system and advanced treating system
System.
Each subsystem of pretreatment system is followed successively by：Tube separators, cavitation air flotation pond, each subsystem of biochemical treatment unit according to It is secondary to be：Anaerobism, anoxic, aerobic, sedimentation basin, each subsystem of advanced treatment system are followed successively by：Coagulation and filtration system, ozone oxidation system System, biological activated carbon system, each major parameter：
The hydraulic detention time of oil separator：1h
The hydraulic detention time of cavitation air flotation system：30min
The hydraulic detention time of air-dissolving air-float system：20min
The hydraulic detention time of anoxic pond reaction zone is 12h
The hydraulic detention time of aerobic tank reaction zone is for 24 hours
The hydraulic detention time of sedimentation basin is 4h
The filtering velocity of coagulation and filtration system is 5~10m/h, 5~10mg/L of PAC dosages
The ozone dosage of ozone oxidation system is 10~20mg/L
Biological activated carbon system hydraulic detention time is 1h
(2) solid-liquid separation unit
Each subelement of solid-liquid separation unit is followed successively by：Cartridge filter, ultrafiltration, each major parameter：
Cartridge filter filtering accuracy is 100 μm
Ultrafiltration membrane is PVDF external pressure hollow-fibre membranes
(3) nano-filtration unit
Each subsystem of nano-filtration unit is followed successively by：Cartridge filter, nanofiltration, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Nanofiltration film type is polyamide composite film
(4) nanofiltration concentrated water processing unit
Each subelement of nanofiltration concentrated water processing unit is followed successively by：Biochemical optimization system, melded system, MBR system, it is each main Parameter：
Biochemical optimization system be ozone oxidation system, oxidization time 2h
Melded system is " lime softening+carbonate softening "
The treatment process of MBR system be " anoxic+ultrafiltration membrane MBR membrane bioreactor systems ", sludge concentration 6000~ 12000mg/L
(5) first reverse osmosis units
Each subsystem of first reverse osmosis units is followed successively by：Cartridge filter, first reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant brackish water desalination reverse osmosis membrane original paper
(6) second reverse osmosis units
Each subsystem of second reverse osmosis units is followed successively by：Cartridge filter, second reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant bitter reverse osmosis membrane original paper
(7) evaporative crystallization unit
Each subsystem of evaporative crystallization unit is followed successively by：Vapo(u)rization system, crystal system, crystal salt piece-rate system, each main ginseng Number：
Vapo(u)rization system is four-effect evaporator system
Crystal system is evaporation and crystallization system
Crystal salt piece-rate system is centrifugal separation system
Crystal salt is mainly sodium chloride
50 μ s/cm of evaporation condensate conductivity
Petroleum asphaltene, pH value is 8~9, a concentration of 100mg/L, the ammonia nitrogen of COD 1000mg/L, volatile phenol A concentration of 300mg/L of a concentration of 80mg/L, petroleum substance.
After premenstrual processing unit processes, COD≤60mg/L of water outlet, concentration≤1mg/L of volatile phenol, the concentration of ammonia nitrogen≤ 5mg/L, pH value 7~8, oil content≤5mg/L.
Waste water after pre-treatment produces COD≤60mg/L of water, concentration≤5mg/ of ammonia nitrogen after solid-liquid separation unit is handled L, pH value 7~8,0.05~1.0NTU of turbidity, the μ s/cm of conductivity≤1200, salt content≤900mg/L, total hardness≤150mg/ L, concentration≤100mg/L of sulfate radical.
Solid-liquid separation unit processing gained waste water is after nano-filtration unit is handled, the production water rate of recovery >=95%, and production water COD≤ 20mg/L, the μ s/cm of conductivity≤900, salt content≤700mg/L, total hardness≤30mg/L, concentration≤2mg/L of sulfate radical are dense Water COD >=400mg/L, the μ s/cm of conductivity >=3900, salt content >=2700mg/L, total hardness >=1200mg/L, sulfate radical it is dense Degree >=980mg/L.
Nano-filtration unit processing gained nanofiltration concentrated water produces water COD≤60mg/L, conductance after nanofiltration concentrated water processing unit processes The μ s/cm of rate≤3800, salt content≤2400mg/L, total hardness≤20mg/L.
Nanofiltration production water obtained by nanofiltration concentrated water processing unit is after the processing of the first reverse osmosis units, the production water rate of recovery 75%, production Water TOC≤5mg/L, the μ s/cm of conductivity≤30, salt content≤25mg/L, concentrated water COD >=60mg/L, the μ s/ of conductivity >=3500 Cm, salt content >=2700mg/L, total hardness >=120mg/L.
First reverse osmosis concentrated water of the first reverse osmosis units processing gained is after the processing of the second reverse osmosis units, production water recycling Rate 75% produces water TOC≤10mg/L, the μ s/cm of conductivity≤100, salt content≤70mg/L, concentrated water COD >=450mg/L, conductance The μ s/cm of rate >=13700, salt content >=10600mg/L, total hardness >=480mg/L, concentration >=50mg/L of sulfate radical.
Second reverse osmosis concentrated water of the second reverse osmosis units processing gained is after evaporative crystallization cell processing, condensate liquid recycling Rate 95%, produces TOC≤10mg/L of water, and the μ s/cm of conductivity≤100, salt content≤70mg/L, crystal salt is sodium chloride.
The leading indicator of separation of solid and liquid production water reaches《Recirculated cooling water Standard of reclaimed water》(HGT3923-2007) In requirement, part nanofiltration production water be used as net circulation cooling water replenishment.First reverse osmosis produced water, the second reverse osmosis produced water and evaporation Condensate liquid is used as desalted water station make-up water source.
Embodiment 3
The present embodiment is used for the dyeing waste water minimizing, recycling processing method and its processing system that illustrate the present invention.
Dyeing waste water minimizing as shown in Figure 3, recycling treatment system, the processing system include what is sequentially connected Pretreatment unit, solid-liquid separation unit, nano-filtration unit, the first reverse osmosis units, the second reverse osmosis units, evaporative crystallization unit, And it is connected to the nanofiltration concentrated water processing unit between the concentrated water water outlet of nano-filtration unit and solid-liquid separation unit water outlet.This reality The technical data setting for applying the processing system of example is as follows：
(1) pretreatment unit
Each subsystem of pretreatment unit is followed successively by：Hydrolysis acidification pool, aerobic tank, each major parameter：
The hydraulic detention time of hydrolysis acidification pool is for 24 hours
The hydraulic detention time of aerobic tank reaction zone is 20h
(2) solid-liquid separation unit
Solid-liquid separation unit be micro-filtration film separation system, major parameter：
Film original paper is PVDF hollow-fibre membranes
(3) nano-filtration unit
Each subsystem of nano-filtration unit is followed successively by：Cartridge filter, nanofiltration, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Nanofiltration film type is polyamide composite film
(4) nanofiltration concentrated water processing unit
Each subelement of nanofiltration concentrated water processing unit is followed successively by：Biochemical optimization system, melded system, MBR system, it is each main Parameter：
Biochemical optimization system be Fenton oxidation system, Fenton reaction time 3h
Melded system is " lime softening+carbonate softening "
MBR system treatment process be " anoxic+aerobic+built-in mocromembrane system ", 6000~12000mg/L of sludge concentration
(5) first reverse osmosis units
Each subsystem of first reverse osmosis units is followed successively by：Cartridge filter, first reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant brackish water desalination reverse osmosis membrane original paper
(6) second reverse osmosis units
Each subsystem of second reverse osmosis units is followed successively by：Cartridge filter, second reverse osmosis, each major parameter：
Cartridge filter filtering accuracy is 5 μm
Reverse osmosis membrane type is polyamide composite film
Film original paper is pollution-resistant seawater desalination reverse osmosis film original paper
(7) evaporative crystallization unit
Each subsystem of evaporative crystallization unit is followed successively by：Vapo(u)rization system, crystal system, crystal salt piece-rate system, each main ginseng Number：
Vapo(u)rization system is MVR vapo(u)rization systems
Crystal system is evaporation and crystallization system
Crystal salt piece-rate system is centrifugal separation system
Crystal salt is mainly sodium chloride
50 μ s/cm of evaporation condensate conductivity
Dyeing waste water, pH value are 9~11, COD 1200mg/L, BOD5For 350mg/L, 900 times of coloration.
After premenstrual processing unit processes, it is discharged COD≤180mg/L, BOD5≤ 30mg/L, concentration≤5mg/L of ammonia nitrogen, pH Value 6~9, coloration≤50 times.
Waste water after pre-treatment produces water COD≤150mg/L, concentration≤5mg/ of ammonia nitrogen after solid-liquid separation unit is handled L, pH value 6~9, coloration≤50 times, 0.05~1.0NTU of turbidity, the μ s/cm of conductivity≤1600, salt content≤1100mg/L, always Hardness≤200mg/L, sulfate radical≤300mg/L.
Solid-liquid separation unit processing gained waste water is after nano-filtration unit is handled, the production water rate of recovery >=95%, and production water COD≤ 10mg/L, the μ s/cm of conductivity≤950, salt content≤700mg/L, total hardness≤30mg/L, concentration≤10mg/L of sulfate radical, Concentrated water COD >=1400mg/L, the μ s/cm of conductivity >=7450, salt content >=4700mg/L, total hardness >=1700mg/L, sulfate radical Concentration >=2900mg/L.
Nano-filtration unit processing gained nanofiltration concentrated water produces water COD≤100mg/L, electricity after nanofiltration concentrated water processing unit processes The μ s/cm of conductance≤5000, salt content≤3300mg/L, total hardness≤20mg/L.
Nanofiltration production water produces the water rate of recovery after the processing of the first reverse osmosis units obtained by nanofiltration concentrated water processing unit processes 75%, produce water TOC≤5mg/L, the μ s/cm of conductivity≤30, salt content≤25mg/L, concentrated water COD >=50mg/L, conductivity >= 3700 μ s/cm, salt content >=2700mg/L, total hardness >=120mg/L, concentration >=40mg/L of sulfate radical.
First reverse osmosis concentrated water of the first reverse osmosis units processing gained is after the processing of the second reverse osmosis units, production water recycling Rate 75% produces water TOC≤5mg/L, the μ s/cm of conductivity≤100, salt content≤70mg/L, concentrated water COD >=170mg/L, conductivity >=14500 μ s/cm, salt content >=10700mg/L, total hardness >=480mg/L, concentration >=160mg/L of sulfate radical.
Second reverse osmosis concentrated water of the second reverse osmosis units processing gained is after evaporative crystallization cell processing, condensate liquid recycling Rate 95% produces water TOC≤10mg/L, and the μ s/cm of conductivity≤100, salt content≤70mg/L, crystal salt is sodium chloride.
Nanofiltration production water meets rinsing or dyeing with water water quality requirement, partly can be used as rinsing or dyeing water, the first reverse osmosis Production water, the second reverse osmosis produced water and evaporation condensate are used as boiler feed water make-up water source, also can be used for the processes such as dyeing thoroughly.
Although to present invention has been a degree of descriptions, it will be apparent that, do not departing from the spirit and scope of the present invention Under conditions of, the appropriate variation of each condition can be carried out.It is appreciated that the present invention is not limited to the embodiment, and it is attributed to power The range of profit requirement includes the equivalent replacement of each factor.

Claims (46)

1. a kind of minimizing of organic wastewater, recycling processing method, the treating method comprises following steps sequentially：
(1) pre-treatment is carried out to waste water, obtains the water outlet after pre-treatment；Wherein, the pre-treatment is selected from pretreatment and/or biochemistry Processing and/or advanced treating；The pretreatment is one or more in coagulation, oil removal, air supporting, precipitation, filtering, stripping； The advanced treating is one or more in coagulating sedimentation, absorption, advanced oxidation, biofilter processing；
(2) solid-liquid separation treatment is carried out to the water outlet that step (1) obtains, obtains separation of solid and liquid water outlet；
(3) nanofiltration processing is carried out to the separation of solid and liquid water outlet that step (2) obtains, obtains nanofiltration production water and nanofiltration concentrated water；
(4) nanofiltration concentrated water processing is carried out to the nanofiltration concentrated water that step (3) obtains, obtains the processing water outlet of nanofiltration concentrated water, the nanofiltration Concentrated water processing water outlet is back to step (3) and is mixed with separation of solid and liquid water outlet, carries out nanofiltration processing；Wherein, the nanofiltration concentrated water Biochemical optimization processing, sofening treatment and the MBR processing to carry out successively are handled, is inhaled wherein the biochemical optimization processing is selected from It is one or more in attached, advanced oxidation, hydrolysis acidification；
(5) the first reverse-osmosis treated is carried out to the nanofiltration production water that step (3) obtains, obtains the first reverse osmosis produced water and the first reverse osmosis Saturating concentrated water；
(6) the first reverse osmosis concentrated water obtained to step (5) carries out the second reverse-osmosis treated, obtains the second reverse osmosis produced water and the Two reverse osmosis concentrated waters；
(7) the second reverse osmosis concentrated water obtained to step (6) is evaporated processing, obtains evaporation concentrated solution and evaporation condensate；
Wherein, the industrial organic waste water that the organic wastewater is discharged selected from coal chemical industry, petrochemical industry, pharmacy, printing and dyeing, food service industry It is and one or more in sanitary sewage.
2. processing method according to claim 1, which is characterized in that in step (1), the biochemical treatment is selected from anaerobism It is one or more in processing, hydrolysis acidification processing, anoxic treatment, Aerobic Process for Treatment；Wherein Anaerobic Treatment is selected from anaerobic filter It is one or more in reason, upflow anaerobic sludge blanket process processing, anaerobic fluidized bed processing；Aerobic Process for Treatment is selected from contact-oxidation pool It is one or more in reason, biofilter processing, activated sludge tank processing.
3. processing method according to claim 2, which is characterized in that the advanced oxidation is selected from ozone oxidation, Fenton It is one or more in oxidation, fenton-type reagent.
4. processing method according to claim 2, which is characterized in that the biofilter processing is selected from ordinary biofilter It is one or more in processing, biological aerated filter processing, biological activated carbon filter processing.
5. processing method according to claim 1, which is characterized in that in step (2), the solid-liquid separation treatment is selected from It is one or more in precipitation, coagulating sedimentation, air supporting, filtering, UF membrane.
6. processing method according to claim 5, which is characterized in that the UF membrane is micro-filtration UF membrane and/or ultrafiltration UF membrane.
7. processing method according to claim 1, which is characterized in that in step (3), nanofiltration processing is filled using NF membrane Put progress.
8. processing method according to claim 7, which is characterized in that the NF membrane is sulfonated polyether sulfone film and/or gathers Amide composite membrane.
9. processing method according to claim 7, which is characterized in that cartridge filter is set before nanofiltration device.
10. processing method according to claim 1, which is characterized in that the advanced oxidation is selected from ozone oxidation, Fenton It is one or more in oxidation, fenton-type reagent.
11. processing method according to claim 1, which is characterized in that in step (4), the sofening treatment is selected from stone It is one or more in grey softening, carbonate deposition, ion exchange.
12. processing method according to claim 11, which is characterized in that lime softening for white lime softening and/or Quick lime softens；The carbonate used in the carbonate deposition is sodium carbonate and/or sodium bicarbonate；The ion exchange is selected from It is one or more in cation bed ion exchange, anion bed ion exchange, mixed bed ion exchange.
13. processing method according to claim 1, which is characterized in that in step (4), the MBR processing is using micro-filtration MBR membrane bioreactors and/or ultrafiltration MBR membrane bioreactors carry out.
14. processing method according to claim 1, which is characterized in that in step (5), nanofiltration that step (3) is obtained The part for producing water is drawn, to carry out reuse/discharge or the raw water as advanced purification system.
15. processing method according to claim 1, which is characterized in that in step (7), tied to evaporation concentrated solution Crystalline substance processing obtains crystal salt and crystallization concentrate.
16. according to the processing method described in any one of claim 1-15, which is characterized in that in step (5), the first reverse osmosis Processing is carried out using reverse osmosis membrane apparatus thoroughly.
17. processing method according to claim 16, which is characterized in that the setting security personnel filtering before reverse osmosis unit Device.
18. processing method according to claim 17, which is characterized in that the filtering accuracy of the cartridge filter is 5 μm.
19. processing method according to claim 16, which is characterized in that the reverse osmosis membrane in the first reverse-osmosis treated is vinegar Acid cellulose film and/or polyamide composite film.
20. according to the processing method described in any one of claim 1-15, which is characterized in that in step (6), the second reverse osmosis Processing is carried out using reverse osmosis membrane apparatus thoroughly.
21. processing method according to claim 20, which is characterized in that the setting security personnel filtering before reverse osmosis membrane apparatus Device.
22. processing method according to claim 21, which is characterized in that the filtering accuracy of the cartridge filter is 5 μm.
23. processing method according to claim 20, which is characterized in that the reverse osmosis membrane in the second reverse-osmosis treated is anti- Contamination type brackish water desalination film and/or pollution-resistant sea water desalination membrane.
24. according to the processing method described in any one of claim 1-15, which is characterized in that in step (7), evaporative crystallization Processing is using one or more progress in evaporator, crystallizer, crystal salt separator.
25. processing method according to claim 24, which is characterized in that evaporator is MVR evaporators or multi-effect evaporator； Crystallizer is crystallizing evaporator or cooler crystallizer；Crystal salt separator is centrifuge；Crystal salt is sodium chloride, sodium sulphate, sulphur It is one or more in sour magnesium, sodium nitrate.
26. a kind of for implementing the system of any one of the claim 1-25 processing methods, which includes fluid successively The pretreatment unit of connection, nano-filtration unit, is connected to the concentrated water water outlet of nano-filtration unit and separation of solid and liquid list at solid-liquid separation unit Nanofiltration concentrated water processing unit, the first reverse osmosis units, the second reverse osmosis units and evaporative crystallization unit between first water outlet；
Wherein, the pretreatment unit is pretreatment unit and/or biochemical treatment unit and/or advanced treatment unit, is pre-processed Unit is one or more in coagulating basin, oil separator, flotation tank, sedimentation basin, filtering ponds, stripping device；Advanced treating list Member is one or more in coagulating sedimentation unit, absorbing unit, advanced oxidation unit, biofilter；
Nanofiltration concentrated water processing unit includes the biochemical being in fluid communication successively optimization unit, pliable cell and MBR unit, wherein raw The property changed optimization unit is one or more in absorbing unit, advanced oxidation unit, hydrolysis acidification unit；
Solid-liquid separation unit receives the water outlet from pretreatment unit, after carrying out solid-liquid separation treatment, obtained solid-liquid separation Water is sent to nano-filtration unit；
Nano-filtration unit receive from solid-liquid separation unit separation of solid and liquid water outlet, carry out nanofiltration processing after, obtain nanofiltration production water and Nanofiltration concentrated water send nanofiltration concentrated water to nanofiltration concentrated water processing unit；
Nanofiltration concentrated water processing unit receives the nanofiltration concentrated water from nano-filtration unit, and after carrying out nanofiltration concentrated water processing, it is dense to obtain nanofiltration Water process is discharged；After nanofiltration concentrated water processing water outlet is mixed with separation of solid and liquid water outlet, nano-filtration unit is sent back to；
First reverse osmosis units receive the nanofiltration production water from nano-filtration unit, and after carrying out the first reverse-osmosis treated, it is anti-to obtain first Infiltration production water and the first reverse osmosis concentrated water；First reverse osmosis concentrated water is sent to the second reverse osmosis units；
Second reverse osmosis units receive the first reverse osmosis concentrated water from the first reverse osmosis units, carry out the second reverse-osmosis treated Afterwards, the second reverse osmosis produced water and the second reverse osmosis concentrated water are obtained；Second reverse osmosis concentrated water is sent to evaporative crystallization unit；
Evaporative crystallization unit receives the second reverse osmosis concentrated water from the second reverse osmosis units, through evaporative crystallization, obtains crystal salt And evaporation condensate.
27. system according to claim 26, which is characterized in that solid-liquid separation unit, nano-filtration unit, the first reverse osmosis list Member, the second reverse osmosis units and evaporative crystallization unit production water send to reuse/exhaust system or send to advanced purification system and be used as Raw water.
28. system according to claim 27, which is characterized in that biochemical treatment unit is Anaerobic Treatment unit and/or water Solution acidification and/or anoxic treatment unit and/or aerobic treatment unit.
29. system according to claim 28, which is characterized in that the Anaerobic Treatment unit is selected from anaerobic filter, up-flow Formula is anaerobic mud bed, it is anaerobic fluidized bed in it is one or more；Aerobic treatment unit is selected from contact-oxidation pool, aeration and biological is filtered It is one or more in pond, activated sludge tank.
30. system according to claim 26, which is characterized in that the advanced oxidation unit be selected from ozone oxidation unit, It is one or more in Fenton oxidation unit, fenton-type reagent unit.
31. system according to claim 26, which is characterized in that the solid-liquid separation unit is selected from precipitation unit, coagulation It is one or more in precipitation unit, air flotation cell, filter element, film separation unit.
32. system according to claim 31, which is characterized in that the film separation unit for micro-filtration film separation unit and/ Or Ultra filtration membrane unit.
33. system according to claim 26, which is characterized in that the nano-filtration unit is nano filter membrance device.
34. system according to claim 33, which is characterized in that the nano-filtration unit, which further includes, is arranged on nano filter membrance device Cartridge filter before.
35. system according to claim 33, which is characterized in that the NF membrane is sulfonated polyether sulfone film and/or polyamides Amine composite membrane.
36. system according to claim 26, which is characterized in that the pliable cell is lime pliable cell, carbonate It is one or more in precipitation unit, ion-exchange unit.
37. system according to claim 36, which is characterized in that the lime pliable cell is white lime pliable cell And/or quick lime pliable cell；Carbonate deposition unit is sodium carbonate and/or sodium bicarbonate precipitation unit；Ion-exchange unit It is one or more in cation bed ion-exchange unit, anion bed ion-exchange unit, mixed bed ion crosspoint.
38. system according to claim 26, which is characterized in that the MBR unit is micro-filtration MBR membrane biological reaction units And/or ultrafiltration MBR membrane biological reaction units.
39. system according to claim 26, which is characterized in that first reverse osmosis units are reverse osmosis membrane apparatus.
40. system according to claim 39, which is characterized in that first reverse osmosis units, which further include, is arranged on reverse osmosis Cartridge filter before permeable membrane device.
41. system according to claim 39, which is characterized in that the reverse osmosis membrane in first reverse osmosis units is vinegar Acid cellulose film and/or polyamide composite film.
42. system according to claim 26, which is characterized in that the second reverse osmosis units are reverse osmosis membrane apparatus.
43. system according to claim 42, which is characterized in that second reverse osmosis units, which further include, is arranged on reverse osmosis Cartridge filter before saturating unit.
44. system according to claim 42, which is characterized in that the reverse osmosis membrane in the second reverse osmosis units is antipollution Type brackish water desalination film and/or pollution-resistant sea water desalination membrane.
45. system according to claim 26, which is characterized in that evaporative crystallization unit is selected from evaporator, crystallizer, crystallization Salt separator.
46. system according to claim 45, which is characterized in that the evaporator is MVR evaporators or multi-effect evaporator； Crystallizer is crystallizing evaporator or cooler crystallizer；Crystal salt separator is centrifuge.
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