CN107226581A - A kind of zinc-containing water processing method, processing system and application - Google Patents

Abstract

The present invention provides a kind of zinc-containing water processing method, it is characterised in that the processing method sequentially includes：(1) zinc-containing water is pre-processed, obtains pretreated water；(2) pretreated water for obtaining step (1) carries out biochemical treatment, obtains biochemical treatment water；(3) the biochemical treatment water for obtaining step (2) carries out concentration, obtains concentration high salt concentrated water and recycle-water；(4) the concentration high salt concentrated water that step (3) is obtained is evaporated crystallization treatment, obtains recycle-water and crystal；Wherein recycle water standard is：PH 68, electrical conductivity≤50, COD≤30, turbidity≤1；This method is simple to operate, stable, with low cost, treatment effeciency is high, so that the zero-emission or low emission of plating production zinc-containing water are reached, while realizing the recovery of higher degree to each metal ion in waste water.

Description

A kind of zinc-containing water processing method, processing system and application

Technical field

The present invention relates to a kind of processing method of waste water and processing system, and in particular to a kind of electroplating industry zinc-containing water Processing method, have been used to the system handled electroplating industry zinc-containing water and this method or the system of this method with Application in processing electroplating industry zinc-containing water.

Background technology

Zinc-containing electroplating wastewater treatment is in handling process often using the processing such as chemical method, electrolysis, conventional ion exchange process Method.Above processing method has some limitations and can not accomplish zero-emission.Chemical method is that present processing complexing plating is useless The widely used method of water, needs to add substantial amounts of soda acid in process of production, while needing to add ferrous sulfate, polyaluminium Aluminium, adds the saliferous rate of water discharge, and the metal ion remained in water is still difficult to reach discharge standard；Due to discharge of wastewater Controlled substance content is extremely low as defined in standard, to reach that discharge standard needs to put into the chemicals of excess, cost is higher, and waste water It can not reclaim and use as process water；It is stable and electrolysis handling process is ripe, but due to as defined in discharge standard by Control thing content extremely low, so power consumption is larger during electrolysis wastewater, processing cost is high, and is also easy to produce toxic gas, it is difficult to handle To qualified discharge；Conventional ion exchange process can effectively be removed various harmful in waste water using organic backbone ion exchange resin Ion, while water can be with reuse, but resin demand is big, and regenerated liquid processing is difficult, need to consume substantial amounts of soda acid, and processing cost is high； And resin is in regenerative process, due to a large amount of ruptures shunk with expanding and causing resin of regeneration, the generation of resin, economy It is not high.Also some processing methods use reverse osmosis membrane concentration electroplating wastewater, while by pure water reuse, but the technique can not Technological requirement is reached, using there is its limitation.

As can be seen that there are problems in the various processing methods currently for zinc-containing water, even if to each Electroplate Factory Existing equipment make full use of the largely or entirely reuse for being still unable to reach waste water, and to the valuable gold in waste water Category can not be effectively separated and reclaim.

The content of the invention

It is an object of the invention to overcome produced problem in the prior art and defect, there is provided a kind of simple to operate, operation Stable, with low cost, treatment effeciency high zinc-containing water processing method and corresponding processing system, so as to reach that plating production contains The zero-emission or low emission of zinc waste water, while realizing the recovery of higher degree to each metal ion in waste water, save electroplating industry Industrial water amount, substantially reduces pollution of the electroplating industry to environment, reduces the usage amount of soda acid, can effectively save resource reduction life Production cost and the recovery for realizing equipment investment, promote and promote cleanly production and the sustainable development of electroplating industry.

The purpose of the present invention is achieved through the following technical solutions：

The present invention provides a kind of zinc-containing water processing method, it is characterised in that the processing method sequentially includes：

(1) zinc-containing water is pre-processed, obtains pretreated water；

(2) pretreated water for obtaining step (1) carries out biochemical treatment, obtains biochemical treatment water；

(3) the biochemical treatment water for obtaining step (2) carries out concentration, obtains concentration high salt concentrated water and reuse Water；

(4) the concentration high salt concentrated water that step (3) is obtained is evaporated crystallization treatment, obtains recycle-water and crystallization Thing；

Wherein recycle water standard is：PH 6-8, electrical conductivity≤50, COD≤30, turbidity≤1.

Preferably, in the step (1),

The zinc-containing water pH 6-8, it includes the pollutants such as zinc ion, SS and COD；Wherein, in the zinc-containing water Zn²⁺For 30-50mg/L；

Preferably, the step of pretreatment is：

Zinc-containing water is introduced broken zinc pond by (1-1), and it is 2-3 that sulfuric acid is added in broken zinc pond to pH, and sodium hypochlorite is added afterwards It is 300-400mv to ORP value, carries out broken zinc reaction；

Waste water after step (1-1) processing is introduced pH regulating reservoirs by (1-2), and addition sodium hydroxide to pH is 8.5-9.5；

Waste water after step (1-2) processing is introduced chemical reaction pond by (1-3), adds coagulant, flocculant is added afterwards, is stirred Mix 20-30min；

Waste water after step (1-3) processing is introduced accurate control High-rate sedimentation system by (1-4)；

Preferably, in the step (1-1), it is 10% sulfuric acid solution regulation pH to add concentration；Preferably, concentration is added ORP value is adjusted for 10% liquor natrii hypochloritis；

Preferably, the broken zinc reaction time of the step (1-1) is 20-30min；

Preferably, in the step (1-2), it is 10% sodium hydroxide solution regulation pH to add concentration；

Preferably, in the step (1-3), the coagulant is inorganic coagulant, more preferably PAC；Preferably, it is described Flocculant is organic flocculant, more preferably PAM；Preferably, the time interval between the addition coagulant and flocculant is 20-40min；

Preferably, the wastewater pH handled through step (1-3) is 8-9；

Preferably, in the step (1-4), the accurate control High-rate sedimentation system by water distribution system, precipitation process pond, Inclined tube, effluent weir, sludge bucket are sequentially connected composition；Preferably, the waste water after step (1-3) processing is introduced into the water distribution successively System, precipitation process pond, inclined tube；Supernatant after above-mentioned processing obtains pretreated water into effluent weir, and obtained sludge sinks Enter sludge bucket；Preferably, the pressure in the precipitation process pond is 2-3Mpa.

Preferably, in the step (2), the biochemical treatment step is：The pretreated water that step (1) is obtained enters successively Enter anaerobic pond, Aerobic Pond, membrane bioreactor；

Preferably, anaerobic bacteria is included in the anaerobic pond；Preferably, the anaerobic bacteria is selected from saccharomycete, nitrate bacterium, shuttle One or more in bacillus or bacteroid；

Preferably, the saccharomycete, nitrate bacterium, Fusobacterium or bacteroid make it have salt tolerance through domestication；

Preferably, aerobic microbiological is included in the Aerobic Pond；

Preferably, one or more of the oxygen animalcule in bacillus, rhizobium, nitrifier or mould；

Preferably, the bacillus, rhizobium, nitrifier or mould make it have salt tolerance through domestication；

Preferably, the membrane bioreactor is made up of hollow fiber film assembly and membrane cisterna；Preferably, the doughnut Membrane module is located in the membrane cisterna；

Preferably, the doughnut membrane aperture is 0.01-0.1 μm；

Preferably, pH is 6-8 after the biochemical treatment.

Preferably, in the step (3), the concentration step is：The biochemical treatment water that step (2) is obtained is successively By one-level nanofiltration system, first-stage reverse osmosis system, two-stage reverse osmosis system；

Preferably, the one-level nanofiltration system is sequentially connected and constituted by accurate filter and one-level NF membrane；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the one-level NF membrane is technical grade equipment with high desalinization NF membrane；

Preferably, the aperture of the one-level NF membrane is 1-2nm；

Preferably, the one-level NF membrane is 50-70% to the rejection of sodium ion；

Preferably, the rejection ＞ 97% of the one-level NF membrane heavy metal ion and salinity；

Preferably, the film pressure of entering of the one-level nanofiltration system is 1.0-1.5Mpa；

Preferably, the relative molecular mass retention scope of the one-level nanofiltration system is 150-300 dalton；

Preferably, the pH of the water of the entrance one-level nanofiltration system is 6-8；

Preferably, the permeate of the one-level nanofiltration system can be used as recycle-water；

Preferably, the concentrate of the one-level nanofiltration system enters first-stage reverse osmosis system.

Preferably, in the step (3), the first-stage reverse osmosis system by accurate filter and first-stage reverse osmosis film successively Connection composition；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the first-stage reverse osmosis film is bitter reverse osmosis membrane；

Preferably, the rejection ＞ 98% of the first-stage reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the first-stage reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the first-stage reverse osmosis system is 1.8Mpa；

Preferably, the pH of the water of the entrance first-stage reverse osmosis system is 5-6；

Preferably, pH is adjusted by adding hydrochloric acid in the first-stage reverse osmosis system；

Preferably, the salt acid for adjusting pH that concentration is 0.2-0.5% is added；

Preferably, the permeate of the first-stage reverse osmosis system returns to one-level nanofiltration system；

Preferably, the concentrate of the first-stage reverse osmosis system enters two-stage reverse osmosis system.

Preferably, in the step (3), the two-stage reverse osmosis system by accurate filter and two-pass reverse osmosis film successively Connection composition；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the two-pass reverse osmosis film is seawater reverse osmosis membrane；

Preferably, the rejection ＞ 99.5% of the two-pass reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the two-pass reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the two-stage reverse osmosis system is 4-5Mpa；

Preferably, the pH of the water of the entrance two-stage reverse osmosis system is 6-8；

Preferably, pH is adjusted by adding hydrochloric acid in the two-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%；

Preferably, the permeate of the two-stage reverse osmosis system returns to one-level nanofiltration system；

Preferably, the concentrate of the two-stage reverse osmosis system is the high salt concentrated water.

Preferably, in the step (4), the evaporative crystallization process step is：The high salt concentrated water that step (3) is obtained according to Secondary process heat exchanger, concentration evaporator, crystallizing evaporator；

Preferably, the operation temperature of the heat exchanger is 80-100 DEG C；

Preferably, the operating pressure of the heat exchanger is 0.05-0.1MPa；

Preferably, the concentration evaporator is sequentially connected group by heating chamber, separation chamber, circular chamber, liquid distributor, demister Into；

Preferably, the crystallizing evaporator is sequentially connected and constituted by separation chamber, salt leg, thickener, crystallization kettle；

Preferably, condensed water of the high salt concentrated water after concentration evaporator returns to the two-stage reverse osmosis system；

Preferably, the high salt concentrated water obtains concentrating high salt concentrated water after concentration evaporator；

Preferably, the salt content of the concentration high salt concentrated water is 30-35%；

Preferably, the concentration high salt concentrated water obtains crystal and condensed water after crystallizing evaporator；Preferably, it is described Crystal is sodium sulphate and/or sodium chloride；Preferably, the condensed water is used as recycle-water.

The present invention also provides a kind of processing system of zinc-containing water processing method of the present invention, it is characterised in that described System includes pretreatment unit, biochemical treatment unit, concentration unit and the evaporative crystallization processing unit being sequentially communicated.

Preferably, the pretreatment unit includes the broken zinc pond being sequentially communicated, pH regulating reservoirs, chemical reaction pond, accurate control High-rate sedimentation system processed；The accurate control High-rate sedimentation system is by water distribution system, precipitation process pond, inclined tube, effluent weir, sludge Bucket is sequentially connected composition.

Preferably, the biochemical treatment unit includes anaerobic pond, Aerobic Pond, the membrane bioreactor being sequentially communicated；

Preferably, the membrane bioreactor is made up of hollow fiber film assembly and membrane cisterna；

Preferably, the hollow fiber film assembly is located in the membrane cisterna；

Preferably, the doughnut membrane aperture is 0.01-0.1 μm.

Preferably, the concentration unit include be sequentially communicated one-level nanofiltration system, first-stage reverse osmosis system, two grades Counter-infiltration system.

Preferably, the one-level nanofiltration system is sequentially connected and constituted by accurate filter and one-level NF membrane；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

The one-level NF membrane is technical grade equipment with high desalinization NF membrane；

Preferably, the aperture of the one-level NF membrane is 1-2nm；

Preferably, the one-level NF membrane is 50-70% to the rejection of sodium ion；Preferably, the one-level NF membrane The rejection ＞ 97% of heavy metal ion and salinity；

Preferably, the film pressure of entering of the one-level nanofiltration system is 1.0-1.5Mpa；

Preferably, the relative molecular mass retention scope of the one-level nanofiltration system is 150-300 dalton；

Preferably, the pH of the water of the entrance one-level nanofiltration system is 6-8.

Preferably, the first-stage reverse osmosis system is sequentially connected and constituted by accurate filter and first-stage reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

Preferably, the first-stage reverse osmosis film is bitter reverse osmosis membrane；

Preferably, the rejection ＞ 98% of the first-stage reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the first-stage reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the first-stage reverse osmosis system is 1.8Mpa；

Preferably, the pH of the water of the entrance first-stage reverse osmosis system is 5-6；

Preferably, pH is adjusted by adding hydrochloric acid in the first-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

Preferably, the two-stage reverse osmosis system is sequentially connected and constituted by accurate filter and two-pass reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

Preferably, the two-pass reverse osmosis film is seawater reverse osmosis membrane；

Preferably, the rejection ＞ 99.5% of the two-pass reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the two-pass reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the two-stage reverse osmosis system is 4-5Mpa；

Preferably, the pH of the water of the entrance two-stage reverse osmosis system is 6-8；

Preferably, pH is adjusted by adding hydrochloric acid in the two-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

Preferably, the evaporative crystallization unit includes heat exchanger, concentration evaporator, the crystallizing evaporator being sequentially communicated；

Preferably, the operation temperature of the heat exchanger is 80-100 DEG C；

Preferably, the operating pressure of the heat exchanger is 0.05-0.1MPa；

Preferably, the concentration evaporator is sequentially connected group by heating chamber, separation chamber, circular chamber, liquid distributor, demister Into；

Preferably, the crystallizing evaporator is sequentially connected and constituted by separation chamber, salt leg, thickener, crystallization kettle.

The processing system of zinc-containing water processing method of the present invention or zinc-containing water processing method of the present invention is at place Manage the application in zinc-containing water.

The present invention for overcome defect present in the processing of zinc-containing water in the prior art there is provided zinc-containing water processing side Method is：

Zinc-containing water pollutant sources analysis of the present invention：Zinc-containing water of the present invention is mainly after electroplating technology The process such as the plating piece passivation such as plating piece cleaning, pole plate cleaning, zinc, stainless steel electrolytic polishing, alumilite process, plating piece processing produced Raw waste water, pH 6-8, it includes the pollutants such as zinc, SS and COD；

Zinc-containing water processing method and processing system of the present invention by " effluent segregation, classification processing, waste water recycling, The technology path of resource reclaim ", is concentrated using the high-precision removal technology of heavy metal, high salinity wastewater biochemical technology, special membrane The fully recovering after processing, in production, realizes waste water by electroplated heavy metals zinc-containing water for technology and mechanical negative pressure evaporation crystallization technique Zero-emission, 99.67% is brought up to by wastewater recycle rate, and recycling for water resource is realized to greatest extent, by waste water Pollutant is converted into solid recycling, thoroughly realizes the zero-emission of waste water.

Zinc-containing water pretreating process of the present invention：1st, zinc-containing water is introduced into broken zinc pond, sulphur is added in broken zinc pond Acid is to pH 2-3, and rear sodium hypochlorite to the ORP value that adds is 300-400mv, after waste water is introduced into pH regulating reservoirs, add sodium hydroxide It is 8.5-9.5 to pH；2nd, waste water is introduced into chemical reaction pond again, in order to accelerate coagulating, adds coagulant, it is rear to add flocculation Agent, stirs 20-30min, is allowed to form larger alumen ustum (0.6-1.0mm), so as to accelerate precipitation, realizes and divides in flocculation process Period adds coagulant and flocculant, both is in the optimal reaction time, and flocculation reaction system uses mechanical agitation, reacts Speed is fast, effect is good, less developer, there is higher removal effect to phosphorus, fluorine, COD while removing heavy metals are removed；3rd, draw after Enter accurate control High-rate sedimentation system；The accurate control High-rate sedimentation system by water distribution system, precipitation process pond, inclined tube, go out Mill weir, sludge bucket are sequentially connected composition；Waste water after processing is introduced into the water distribution system, precipitation process pond, inclined tube successively；Through Supernatant after above-mentioned processing obtains pretreated water into effluent weir, and sludge sinks to sludge bucket；Above-mentioned accurate control High-rate sedimentation System shortens the sedimentation time to increase desilting area, improves deposition efficiency, passes through the waterpower of accurate control High-rate sedimentation system Water distribution, high-efficiency sedimentation etc. are acted on, efficient precipitation flco and SS, while in setting the inclined tube in pond, make jetsam not by The interference of current stabilization influence, reaches rapid precipitation effect, and the disposal ability of the accurate control High-rate sedimentation system is sunk than general Shallow lake pond is big 3-7 times, and the sludge of bottom of pond is discharged into sludge-tank by the static pressure mud discharging device of setting and further concentrated, and is then pumped into sludge Filter press press filtration, mud cake is reprocessed according to property, can remove about 80% suspension, 40-70% oils, and makes delivery turbidity <30NTU, COD decline 40-60% etc.；

Zinc-containing water biochemical processing process of the present invention：Pretreated water is sequentially entered into anaerobic pond, Aerobic Pond, film biological Reactor；By A/O/MBR biodegradation, the material such as most COD, ammonia nitrogen and SS in waste water is removed；The present invention The anaerobic technique is under without dissolved oxygen conditions or under anoxia condition, using the effect of anaerobic bacteria, organic matter is occurred hydrolysis, acid Change, remove the organic matter in waste water, improve the biodegradability of sewage, be conducive to follow-up aerobic treatment process；It is of the present invention Aerobic process is organic matter oxidation Decomposition in the presence of aerobic microbiological under aerobic conditions, and organic concentration declines, micro- life Organic matter in object amount increase, sewage, is attracted to activated sludge and biofilm surface, and connect with microbial cell surface first Touch, the organic matter of small molecule can be directed through cell membrane and enter in microbial body, and larger molecular organicses then must be in cell It is hydrolyzed to after small molecule be taken in cell body by microorganism again in the presence of exoenzyme-hydrolase.Organic matter is finally broken down into CO₂And H₂O；Membrane bioreactor of the present invention is made up of hollow fiber film assembly and membrane cisterna；Preferably, the doughnut Membrane module is located in the membrane cisterna；Membrane module is positioned in membrane cisterna, is aerated in pond, because hollow-fibre membrane is less than 0.1 Zoogloea and free bacteria, all can be retained in membrane cisterna by the aperture of micron, so that mud-water separation is reached, various suspensions Grain, bacterium, algae, turbidity and organic matter are effectively removed, it is ensured that go out aqueous suspension close to zero excellent water outlet water Matter.The efficient crown_interception of membrane bioreactor, can be smoothed out nitration reaction with effectively catching nitrifier, effectively remove Ammonia nitrogen；The larger molecular organicses for being difficult to degraded can be retained simultaneously, are extended its residence time in biochemical reaction tank, are allowed to Decomposition to the limit.

Zinc-containing water concentration technique of the present invention：Biochemical treatment water is sequentially passed through into one-level nanofiltration system, one-level Counter-infiltration system, two-stage reverse osmosis system；The present invention is to realize the zero-emission of zinc-containing water, is set in biochemical treatment system rear end Concentrating and treating system, for handling the strong brine of biochemical treatment system generation；Concentrating and treating system of the present invention is multistage dense The technique that contracting, nanofiltration/reverse osmosis concentration are combined, by the concentration step by step of film, making the water of high content of salt waste water gradually reduces (institute The high salt concentrated water salt content of acquisition is 40-60g/L) so as to reduce investment and the operating cost of subsequent evaporation crystal system；Should Concentration technique to need strong brine to be processed in follow-up evaporation and crystallization system, reduced than conventional concentrating and treating system 80%, making the cost of investment of whole Waste Water Treatment reduces 20-30%, the operating cost of wastewater treatment reduces 30- 40%, improve the automaticity of system.

Zinc-containing water evaporative crystallization handling process of the present invention：The high salt concentrated water that concentration is obtained, which is sequentially passed through, changes Hot device, concentration evaporator, crystallizing evaporator；Fully recovering after wastewater treatment to evaporative crystallization stage is accomplished to contain zinc by the present invention The zero-emission of waste water；Waste water is introduced into the heat exchanger in the evaporation and crystallization system, by heat exchange, removes the O in waste water₂ And CO₂Gas, the waste water after heat exchange, which enters in concentration evaporator, is evaporated concentration, when waste water salt concentration is to 30-35% I.e. before sodium sulphate and sodium chloride crystallization is produced, the waste water is delivered into crystallizing evaporator, crystal and condensed water is obtained, condensed Water is used as recycle-water.Evaporation and crystallization system of the present invention causes the negative of waste water evaporation section using mechanical temperature raising device Pressure, can save the energy, and the waste steam through overcompression heats supercharging and entered outside the pipe of concentration evaporator, and latent heat is passed to Pipe, itself condenses into condensed water, while the brine waste evaporation in pipe.The characteristics of evaporation and crystallization system of the present invention is Small volume, takes up an area less, energy consumption is low, and the thermal efficiency is high, and the power consumption of general one ton of waste water is 16-20kwh, and its thermal efficiency is that single-action is dodged 27 times of steaming system, are 7 times of quadruple effect flash system, are current state-of-the-art evaporation concentration system, the crystal produced by it Can be through handling or sending relevant departments' purification to utilize, its main component is sodium sulphate and sodium chloride.

The advantage of above-mentioned evaporation and crystallization system is as follows：(1) system makes identical water tonnage device of making using mixed journey feedwater Ton water power consumes more external technique and reduces 40-50%；(2) it is dense by the high salt of concentrating and treating system because the system mixes journey feedwater Water sequentially enters low temperature effect from the high temperature effect of evaporation and crystallization system, and concentration is gradually risen, and temperature is gradually reduced.Avoid external work In skill, imitated from low temperature to being raised caused by high temperature effect make-up cooling water in high temperature effect feed water concentration, be effectively reduced the knot of high temperature effect Dirt and corrosion condition；(3) it is evenly distributed by the high salt concentrated water of concentrating and treating system on concentration evaporator, it is to avoid existing steaming Send out the uneven susceptible to plugging shortcoming of spray nozzle type feedwater in crystal system；(4) vacuum system uses differential pressure air extractor, accurate between each effect Really form design pressure difference so that the system run all right is reliable.

The processing system of zinc-containing water processing method of the present invention, using programmable logic controller (PLC), while realizing electricity Gas and instrument automatic control and monitoring, using industrial computer, operation process state and operational factor to system are monitored.This Outside, the membranous system in the system periodically uses permeate to rinse to rinse the pollutant of film surface, diaphragm；And set up online Chemical cleaning system, it is ensured that system is long-term, stably, Effec-tive Function.

At present, the Technology development in the prior art on zinc-containing water has chemical precipitation technology, biologic treating technique And membrane separation technique, routine techniques essentially according to " qualified discharge " highway route design, with the present invention compared with have the following disadvantages：

(1) routine techniques system wastewater recycle rate is 60%, wherein, water resource is not recycled fully, after wastewater treatment Discharge adds the load of surrounding enviroment；

(2) microorganism is to the poor resistance of salinity in routine biochemistry treatment technology, and sludge concentration is generally 3000mg/L, this The sludge concentration of inventive technique mesophytization system is 7000-8000mg/L.

(3) heavy metal ion not yet 100% is removed, and environmental pollution is still present；

(4) concentrated water that film concentration systems are produced need to be handled again, otherwise can cause two layers of pollution；

(5) routine techniques reuse water conductivity is 200-300 μ S/cm, the μ S/ of the technology of the present invention reuse water conductivity≤50 cm。

Zinc-containing water processing method of the present invention, the beneficial effect of processing system：

(1) condition that zinc-containing water pretreating process of the present invention reacts according to various heavy metal ion is different, uses The online monitoring instruments such as pH, ORP, automatically control measuring pump quantitative dosing, add medicament and are fully reacted with waste water, and pass through precision High-rate sedimentation system is controlled to carry out separation of solid and liquid processing, removal of heavy metal ions rate is up to 99.99%.

(2) zinc-containing water biochemical process of the present invention uses A/O/MBR techniques, and system is by biochemistry pool, membrane module and film Pond is constituted, and can be all retained in activated sludge in membrane cisterna, the various pollutants such as various suspended particulates, bacterium, organic matter stop Stay the time long, so as to be sufficiently removed, it is ensured that effluent quality is excellent, SS is almost nil.This process volume load is high, to water quality Water adaptive faculty is strong, is gone using through taming waste water of the extraordinary microorganism with salt tolerant to salt content height and containing difficult degradation COD Except efficiency high, denitrification effect is good.

(3) zinc-containing water concentration technology of the present invention uses special membrane concentration technique by the salinity in waste water according to desalination The technology that concentration and smart desalination and concentration are combined by more than 30 times of Waste water concentrating, the production water of advanced treatment system can direct reuse in life Production.Special membrane concentration technique still has efficient salt rejection rate, with higher mechanical strength and service life, energy under with high flow rate Good, the characteristics of cost performance is high of waving function, chemical stability is being issued compared with low operating pressure.

(4) zinc-containing water evaporative crystallization of the present invention is using the extraordinary both vapor compression technology of Germany, by distillation hydrothermal exchange Device, concentration evaporator, crystallizer and centrifuge etc. are constituted, and when evaporator handles waste water, the heat energy needed for evaporating waste water steams again Release heat energy is provided when vapour condenses and condenses water cooling, and in the process of running, the loss without latent heat makes waste water realize low temperature Negative pressure evaporation.In compressor compresses, pressure and temperature is lifted, and high enthalpy steam can fully reclaim distilled water as thermal source again With dope heat, energy consumption is saved.Evaporated during evaporation using pipe is outer, not only never incrustation in efficiency high and pipe.

Brief description of the drawings

Hereinafter, embodiment of the present invention is described in detail with reference to accompanying drawing, wherein：

Fig. 1 is zinc-containing water processing system schematic diagram of the present invention.

Embodiment

Illustrate the present invention referring to specific embodiment.It will be appreciated by those skilled in the art that these embodiments are only For illustrating the present invention, it does not limit the scope of the present invention in any way.

Experimental method in following embodiments, is conventional method unless otherwise specified.Original used in following embodiments Material, reagent material etc., unless otherwise specified, are commercially available products.

Zinc-containing water pollutant sources analysis of the present invention：Zinc-containing water of the present invention is mainly after electroplating technology The process such as the plating piece passivation such as plating piece cleaning, pole plate cleaning, zinc, stainless steel electrolytic polishing, alumilite process, plating piece processing produced Raw waste water, pH 6-8, it includes the pollutants such as zinc, SS and COD；

Zinc-containing water pretreating process of the present invention：1st, zinc-containing water is introduced into broken zinc pond, sulphur is added in broken zinc pond Acid is to pH, and rear sodium hypochlorite to the ORP value that adds is 300-400mv, after waste water is introduced into pH regulating reservoirs, add sodium hydroxide to pH For 8.5-9.5；2nd, waste water is introduced into chemical reaction pond again, in order to accelerate coagulating, adds coagulant, flocculant is added afterwards, 20-30min is stirred, is allowed to form larger alumen ustum (0.6-1.0mm), so as to accelerate precipitation, timesharing is realized in flocculation process Section adds coagulant and flocculant, both is in the optimal reaction time, and flocculation reaction system uses mechanical agitation, reaction speed Degree is fast, effect is good, less developer, there is higher removal effect to phosphorus, fluorine, COD while removing heavy metals are removed；3rd, it is rear to introduce Precision control High-rate sedimentation system；Preferably, the accurate control High-rate sedimentation system is by water distribution system, precipitation process pond, tiltedly Pipe, effluent weir, sludge bucket are sequentially connected composition；By the waste water after processing introduce successively the water distribution system, precipitation process pond, tiltedly Pipe；Supernatant after above-mentioned processing obtains pretreated water into effluent weir, and sludge sinks to sludge bucket；Above-mentioned accurate control is efficient Settling system shortens the sedimentation time to increase desilting area, improves deposition efficiency, passes through accurate control High-rate sedimentation system Waterpower water distribution, high-efficiency sedimentation etc. are acted on, efficient precipitation flco and SS, while in setting the inclined tube in pond, making jetsam The interference not influenceed by current stabilization, reaches rapid precipitation effect, the disposal ability of the accurate control High-rate sedimentation system is than general Sedimentation basin it is big 3-7 times, the sludge of bottom of pond is discharged into sludge-tank by the static pressure mud discharging device of setting and further concentrated, and is then pumped into Sludge filter press press filtration, mud cake is reprocessed according to property, can remove about 80% suspension, 40-70% oils, and makes water outlet Turbidity<30NTU, COD decline 40-60% etc.；

Zinc-containing water biochemical processing process of the present invention：Pretreated water is sequentially entered into anaerobic pond, Aerobic Pond, film biological Reactor；By A/O/MBR biodegradation, the material such as most COD, ammonia nitrogen and SS in waste water is removed；The present invention The anaerobic technique is under without dissolved oxygen conditions or under anoxia condition, using the effect of anaerobic bacteria, organic matter is occurred hydrolysis, acid Change, remove the organic matter in waste water, improve the biodegradability of sewage, be conducive to follow-up aerobic treatment process；It is of the present invention Aerobic process is organic matter oxidation Decomposition in the presence of aerobic microbiological under aerobic conditions, and organic concentration declines, micro- life Organic matter in object amount increase, sewage, is attracted to activated sludge and biofilm surface, and connect with microbial cell surface first Touch, the organic matter of small molecule can be directed through cell membrane and enter in microbial body, and larger molecular organicses then must be in cell It is hydrolyzed to after small molecule be taken in cell body by microorganism again in the presence of exoenzyme-hydrolase.Organic matter is finally broken down into CO₂And H₂O；Membrane bioreactor of the present invention is made up of hollow fiber film assembly and membrane cisterna；Preferably, the doughnut Membrane module is located in the membrane cisterna；Membrane module is positioned in membrane cisterna, is aerated in pond, because hollow-fibre membrane is less than 0.1 Zoogloea and free bacteria, all can be retained in membrane cisterna by the aperture of micron, so that mud-water separation is reached, various suspensions Grain, bacterium, algae, turbidity and organic matter are effectively removed, it is ensured that go out aqueous suspension close to zero excellent water outlet water Matter.The efficient crown_interception of membrane bioreactor, can be smoothed out nitration reaction with effectively catching nitrifier, effectively remove Ammonia nitrogen；The larger molecular organicses for being difficult to degraded can be retained simultaneously, are extended its residence time in biochemical reaction tank, are allowed to Decomposition to the limit.

Zinc-containing water concentration technique of the present invention：Biochemical treatment water is sequentially passed through into one-level nanofiltration system, one-level Counter-infiltration system, two-stage reverse osmosis system；The present invention is to realize the zero-emission of zinc-containing water, is set in biochemical treatment system rear end Concentrating and treating system, for handling the strong brine of biochemical treatment system generation；Concentrating and treating system of the present invention is multistage dense The technique that contracting, nanofiltration/reverse osmosis concentration are combined, by the concentration step by step of film, making the water of high content of salt waste water gradually reduces (institute The high salt concentrated water salt content of acquisition is 40-60g/L) so as to reduce investment and the operating cost of subsequent evaporation crystal system；Should Concentration technique to need strong brine to be processed in follow-up evaporation and crystallization system, reduced than conventional concentrating and treating system 80%, making the cost of investment of whole Waste Water Treatment reduces 20-30%, the operating cost of wastewater treatment reduces 30- 40%, improve the automaticity of system.

Zinc-containing water evaporative crystallization handling process of the present invention：The high salt concentrated water that concentration is obtained, which is sequentially passed through, changes Hot device, concentration evaporator, crystallizing evaporator；Fully recovering after wastewater treatment to evaporative crystallization stage is accomplished to contain zinc by the present invention The zero-emission of waste water；Waste water is introduced into the heat exchanger in the evaporation and crystallization system, by heat exchange, removes the O in waste water₂ And CO₂Gas, the waste water after heat exchange, which enters in concentration evaporator, is evaporated concentration, when waste water salt concentration is to 30-35% I.e. before sodium sulphate and sodium chloride crystallization is produced, the waste water is delivered into crystallizing evaporator, crystal and condensed water is obtained, condensed Water is used as recycle-water.Evaporation and crystallization system of the present invention causes the negative of waste water evaporation section using mechanical temperature raising device Pressure, can save the energy, and the waste steam through overcompression heats supercharging and entered outside the pipe of concentration evaporator, and latent heat is passed to Pipe, itself condenses into condensed water, while the brine waste evaporation in pipe.The characteristics of evaporation and crystallization system of the present invention is Small volume, takes up an area less, energy consumption is low, and the thermal efficiency is high, and the power consumption of general one ton of waste water is 16-20kwh, and its thermal efficiency is that single-action is dodged 27 times of steaming system, are 7 times of quadruple effect flash system, are current state-of-the-art evaporation concentration system, the crystal produced by it Can be through handling or sending relevant departments' purification to utilize, its main component is sodium sulphate and sodium chloride.

The technological process of following examples of the present invention, its basic handling flow is：Electroplate zinc-containing water → pretreating process → biochemical processing process → entrance anaerobic pond → entrance Aerobic Pond → membrane bioreactor → supercharging → one-level nanofiltration UF membrane → Supercharging → first-stage reverse osmosis UF membrane → supercharging → two-pass reverse osmosis UF membrane, high salt concentrated water enters evaporative crystallization system after separation System；In evaporation and crystallization system, high salt concentrated water handles the condensed water produced by concentration evaporator, can meet workshop recycle-water Water quality requirement.

Embodiment 1

(1) zinc-containing water is pre-processed, and obtains pretreated water

Zinc-containing water is taken first, and the zinc-containing water is mainly the plating such as plating piece cleaning, pole plate cleaning, zinc after electroplating technology The waste water produced by process such as part passivation, stainless steel electrolytic polishing, alumilite process, plating piece processing, pH 6-8, its comprising zinc, The pollutants such as SS and COD；

Zinc-containing water is introduced into broken zinc pond, the sulfuric acid solution of addition 10% is 2-3 to pH in broken zinc pond, and concentration is added afterwards To ORP value it is 300-400mv for 10% liquor natrii hypochloritis, carries out broken zinc reaction；Waste water is introduced into pH regulating reservoirs afterwards, added The sodium hydroxide solution of 10% concentration, regulation pH is 8.5-9.5, and waste water is re-introduced into chemical reaction pond, add coagulant PAC and Flocculant PAM, stirs 25min.Waste water is introduced into accurate control High-rate sedimentation system again.

(2) pretreated water is subjected to biochemical treatment, obtains biochemical treatment water

The pretreated water is sequentially entered into anaerobic pond, Aerobic Pond, membrane bioreactor；Wherein, include and detest in anaerobic pond Oxygen bacterium, one or more of the anaerobic bacteria in saccharomycete, nitrate bacterium, Fusobacterium or bacteroid；The saccharomycete, nitre Hydrochlorate bacterium, Fusobacterium or bacteroid make it have salt tolerance through domestication；Aerobic microbiological is included wherein in Aerobic Pond, the oxygen is micro- The biological one or more in bacillus, rhizobium, nitrifier or mould；The bacillus, rhizobium, nitrifier Or mould makes it have salt tolerance through domestication；Afterwards enter membrane bioreactor, the membrane bioreactor by hollow-fibre membrane (in The aperture of hollow fiber film be 0.01-0.1 μm) component and membrane cisterna composition；Membrane module is positioned in membrane cisterna, is aerated in pond, PH is 6-8 after the biochemical treatment, can remove the material such as most COD, ammonia nitrogen and SS in waste water；Anaerobism work of the present invention Skill is under without dissolved oxygen conditions or under anoxia condition, using the effect of anaerobic bacteria, organic matter is occurred hydrolysis, acidifying, removes useless Organic matter in water, improves the biodegradability of sewage, is conducive to follow-up aerobic treatment process；Aerobic process of the present invention is Under aerobic conditions, organic matter oxidation Decomposition in the presence of aerobic microbiological, organic concentration declines, microbial biomass increase, Organic matter in sewage, is attracted to activated sludge and biofilm surface, and contacted with microbial cell surface, small molecule first Organic matter can be directed through cell membrane into microbial body, and larger molecular organicses then must be in exoenzyme-hydrolysis It is hydrolyzed to after small molecule be taken in cell body by microorganism again in the presence of enzyme.Organic matter is finally broken down into CO₂And H₂O；This Invent the membrane bioreactor to be made up of hollow fiber film assembly and membrane cisterna, membrane module is positioned in membrane cisterna, carried out in pond Zoogloea and free bacteria, because hollow-fibre membrane is less than 0.1 micron of aperture, all can be retained in membrane cisterna by aeration, So as to reach mud-water separation, various suspended particulates, bacterium, algae, turbidity and organic matter are effectively removed, it is ensured that gone out Excellent effluent quality of the aqueous suspension close to zero.The efficient crown_interception of membrane bioreactor, can be made with effectively catching nitrifier Nitration reaction is smoothed out, and effectively removes ammonia nitrogen；The larger molecular organicses for being difficult to degraded can be retained simultaneously, extend it in biochemistry Residence time in reaction tank, it is allowed to be decomposed to greatest extent.

(3) the biochemical treatment water is subjected to concentration, obtains high salt concentrated water and recycle-water

Biochemical treatment water is sequentially passed through into one-level nanofiltration system, first-stage reverse osmosis system, two-stage reverse osmosis system；Described one Level nanofiltration system is sequentially connected and constituted by accurate filter and one-level NF membrane, and wherein the filter core of accurate filter is fusion-jet type PP Cotton, the aperture of precise microfiltration device is 5 μm, and the aperture of the one-level NF membrane is 1nm, and pending water passes through one-level NF membrane When, the rejection to sodium ion is 50%, and the rejection of heavy metal ion and salinity is 98%；Afterwards by one-level nanofiltration system System, pH is 6-8, enters film pressure for 1.5Mpa；The relative molecular mass retention scope of the one-level nanofiltration system is 300 dalton； The permeate of the one-level nanofiltration system can be continuing with through ion exchange as recycle-water；

Concentrate of the above-mentioned processing water Jing Guo one-level nanofiltration system enters first-stage reverse osmosis system, the first-stage reverse osmosis system System is sequentially connected composition by accurate filter and first-stage reverse osmosis film (bitter reverse osmosis membrane, aperture is 0.1-1nm), and one-level is anti- The film pressure of entering of osmosis system is 1.8Mpa, and it is 5-6 to adjust pH by 0.2% hydrochloric acid, by the first-stage reverse osmosis film, counterweight The rejection of metal ion and salinity is 99%；Permeate of the above-mentioned processing water Jing Guo first-stage reverse osmosis system returns to one-level nanofiltration System, its concentrate enters two-stage reverse osmosis system.The two-stage reverse osmosis system is by accurate filter and two-pass reverse osmosis film (seawater reverse osmosis membrane, aperture is 0.1-1nm) is sequentially connected composition；The film pressure of entering of two-stage reverse osmosis system is 5Mpa, is passed through 0.2% hydrochloric acid adjustment pH is 6-8, by the two-pass reverse osmosis film, and the rejection of heavy metal ion and salinity is 99.9%； Above-mentioned processing water returns to one-level nanofiltration system by the permeate of two-stage reverse osmosis system, and its concentrate is high salt concentrated water, high salt The salt content of concentrated water is 40g/L.

The present invention is to realize the zero-emission of zinc-containing water, sets concentrating and treating system in biochemical treatment system rear end, is used for Handle the strong brine that biochemical treatment system is produced；Concentrating and treating system of the present invention is multistage concentration, nanofiltration/reverse osmosis concentration With reference to technique, by the concentration step by step of film, making the water of high content of salt waste water gradually reduces (the high salt concentrated water saliferous obtained Measure as 40g/L) so as to reduce investment and the operating cost of subsequent evaporation crystal system；The concentration technique causes follow-up Strong brine to be processed is needed in evaporation and crystallization system, 80% is reduced than conventional concentrating and treating system, makes whole wastewater treatment The cost of investment of system reduces 30%, and the operating cost of wastewater treatment reduces 40%, improves the automaticity of system. Above-mentioned zinc-containing water concentration technique, carries out pre-concentration, by one-level nanofiltration system through accurate filter and one-level nanofiltration system The permeate of system can be used as recycle-water after ion exchange, and the concentrate of the one-level nanofiltration system enters first-stage reverse osmosis System；The permeate of the first-stage reverse osmosis system returns to one-level nanofiltration system, and the concentrate of the first-stage reverse osmosis system enters Enter two-stage reverse osmosis system；The permeate of the two-stage reverse osmosis system returns to one-level nanofiltration system, the two-pass reverse osmosis system The concentrate of system is the high salt concentrated water.

(4) the high salt concentrated water is evaporated crystallization treatment, obtains recycle-water and crystal

Above-mentioned high salt concentrated water is sequentially passed through into heat exchanger, concentration evaporator, crystallizing evaporator；The operation temperature of the heat exchanger Spend for 80-100 DEG C；The operating pressure of the heat exchanger is 0.05-0.1MPa；The concentration evaporator by heating chamber, separation chamber, Circular chamber, liquid distributor, demister are sequentially connected composition；The crystallizing evaporator by separation chamber, salt leg, thickener, crystallization kettle according to Secondary connection composition；Condensed water of the above-mentioned high salt concentrated water after concentration evaporator returns to above-mentioned two-stage reverse osmosis system；High salt is dense The concentrate that water is obtained after concentration evaporator is concentration high salt concentrated water, and salt content is 40-60g/L；The concentration high salt concentrated water Crystal and condensed water are obtained after crystallizing evaporator；Obtained crystal is sodium sulphate and/or sodium chloride；And condensed water is made Workshop is returned to for recycle-water to be continuing with.

Wherein, the concentration evaporator is made up of the multiple evaporators being serially connected, and (90 DEG C or so) heating of low temperature are steamed Vapour is introduced into the first effect, heats feed liquid therein, feed liquid is produced the almost equivalent evaporation lower than vapor (steam) temperature.The steam of generation The second effect is introduced into as heating steam, makes the feed liquid of the second effect with than the first effect lower temperature evaporation.This process is always Repeat to last effect.The solidifying water of first effect is returned at thermal source, and other each solidifying water of effect are exported after collecting as desalination water, a steaming Vapour is put into, and the water that can evaporate many times comes out.Meanwhile, feed liquid is passed through by the concentration successively of the first effect to most end effect, in most end Effect reaches supersaturation and crystallizes and separate out.It is achieved in the separation of solid and liquid of feed liquid.

The technical parameter of the evaporation and crystallization system processing concentrated water is as follows：

(1) desalination water salt content (TDS) is less than 10ppm

(2) ton desalination water steam consumption quantity=(1/ effect number)/90%t/t

(3) 2~4kwh/t of ton desalination water power consumption

A kind of zinc-containing water processing method of the present invention not only brings up to wastewater recycle rate relative to prior art 99.67%, while processing cost, the metal ion recycling reduced in solid waste yield and waste water can be greatly reduced, it is thoroughly real The zero-emission of existing waste water.

Comparative example 1

(1) zinc-containing water is taken first, and the zinc-containing water is mainly the cleaning of the plating piece after electroplating technology, pole plate cleaning, zinc Deng the waste water produced by the processes such as plating piece passivation, stainless steel electrolytic polishing, alumilite process, plating piece processing, pH 6-8, it is included The pollutants such as zinc, SS and COD；Zinc-containing water is introduced into pH regulating reservoirs, sodium hydroxide regulation pH to 10-11 is added, when it reacts Between be 20-25min；Waste water is introduced into chemical reaction pond afterwards, coagulant PAC and flocculant PAM is added, 25min is stirred.Again will be useless Water introduces settling system and carries out mud-water separation, and sludge enters sludge treating system, and supernatant enters biochemical system.

(2) pretreated water is sequentially entered into anaerobic pond, Aerobic Pond, biochemical sedimentation basin；Wherein, include and detest in anaerobic pond Aerobic microbiological is included in oxygen bacterium, wherein Aerobic Pond；Enter biochemical sedimentation basin afterwards, the biochemical sedimentation basin is by water distributing area, sludge Area, Disengagement zone and effluent weir composition；Biochemical sedimentation basin water outlet SS is 30mg/L, and COD is 50mg/L, and biochemistry pool water outlet 40% is up to standard Discharge, 60% enters film concentration systems.

(3) water outlet after biochemistry is sequentially passed through into accurate filter, reverse osmosis membrane apparatus；The filter core of wherein accurate filter is PP cottons, the aperture of precise microfiltration device is 5 μm；The film pressure of entering of counter-infiltration system is 1.2-1.6Mpa, is adjusted by hydrochloric acid PH is 5-6, by the reverse osmosis membrane, and the rejection of heavy metal ion and salinity is 99%；The concentrate of reverse osmosis membrane is returned Pretreatment system is handled again, reverse osmosis membrane permeate electrical conductivity 200-300 μ S/cm, accounts for the 60% of total waste water, permeate It is used as reuse Water circulation to production line.

In a word, specific description of embodiments of the present invention is not intended to limit the present invention for the above, and those skilled in the art can be with It is variously modified or is deformed according to the present invention, without departing from the spirit of the present invention, all should belong to right appended by the present invention will The scope asked.

Claims (16)

1. a kind of zinc-containing water processing method, it is characterised in that the processing method sequentially includes：

(1) zinc-containing water is pre-processed, obtains pretreated water；

(2) pretreated water for obtaining step (1) carries out biochemical treatment, obtains biochemical treatment water；

(3) the biochemical treatment water for obtaining step (2) carries out concentration, obtains concentration high salt concentrated water and recycle-water；

(4) the concentration high salt concentrated water that step (3) is obtained is evaporated crystallization treatment, obtains recycle-water and crystal；

Wherein recycle water standard is：PH 6-8, electrical conductivity≤50, COD≤30, turbidity≤1.

2. processing method according to claim 1, it is characterised in that in the step (1), the zinc-containing water pH 6- 8, it includes the pollutants such as zinc ion, SS and COD；Wherein, Zn in the zinc-containing water²⁺For 30-50mg/L；

Preferably, the step of pretreatment is：

Zinc-containing water is introduced broken zinc pond by (1-1), and it is 2-3 that sulfuric acid is added in broken zinc pond to pH, and the rear sodium hypochlorite that adds is to ORP It is worth for 300-400mv, the broken zinc reaction of progress；

Waste water after step (1-1) processing is introduced pH regulating reservoirs by (1-2), and addition sodium hydroxide to pH is 8.5-9.5；

Waste water after step (1-2) processing is introduced chemical reaction pond by (1-3), adds coagulant, flocculant is added afterwards, is stirred 20-30min；

Waste water after step (1-3) processing is introduced accurate control High-rate sedimentation system by (1-4)；

Preferably, in the step (1-1), it is 10% sulfuric acid solution regulation pH to add concentration；Preferably, adding concentration is 10% liquor natrii hypochloritis's regulation ORP value；

Preferably, the broken zinc reaction time of the step (1-1) is 20-30min；

Preferably, in the step (1-2), it is 10% sodium hydroxide solution regulation pH to add concentration；

Preferably, in the step (1-3), the coagulant is inorganic coagulant, more preferably PAC；Preferably, the flocculation Agent is organic flocculant, more preferably PAM；Preferably, the time interval added between coagulant and flocculant is 20- 40min；

Preferably, the wastewater pH handled through step (1-3) is 8-9；

Preferably, in the step (1-4), the accurate control High-rate sedimentation system is by water distribution system, precipitation process pond, tiltedly Pipe, effluent weir, sludge bucket are sequentially connected composition；Preferably, the waste water after step (1-3) processing is introduced described with water system successively System, precipitation process pond, inclined tube；Supernatant after above-mentioned processing obtains pretreated water into effluent weir, and obtained sludge is sunk to Sludge bucket；Preferably, the pressure in the precipitation process pond is 2-3Mpa.

3. processing method according to claim 1 or 2, it is characterised in that in the step (2), the biochemical treatment step Suddenly it is：The pretreated water that step (1) is obtained sequentially enters anaerobic pond, Aerobic Pond, membrane bioreactor；

Preferably, anaerobic bacteria is included in the anaerobic pond；Preferably, the anaerobic bacteria is selected from saccharomycete, nitrate bacterium, Fusobacterium Or the one or more in bacteroid；

Preferably, the saccharomycete, nitrate bacterium, Fusobacterium or bacteroid make it have salt tolerance through domestication；

Preferably, aerobic microbiological is included in the Aerobic Pond；

Preferably, one or more of the oxygen animalcule in bacillus, rhizobium, nitrifier or mould；

Preferably, the bacillus, rhizobium, nitrifier or mould make it have salt tolerance through domestication；

Preferably, the membrane bioreactor is made up of hollow fiber film assembly and membrane cisterna；Preferably, the hollow-fibre membrane group Part is located in the membrane cisterna；

Preferably, the doughnut membrane aperture is 0.01-0.1 μm；

Preferably, pH is 6-8 after the biochemical treatment.

4. processing method according to any one of claim 1 to 3, it is characterised in that described dense in the step (3) Contracting process step is：The biochemical treatment water that step (2) is obtained sequentially passes through one-level nanofiltration system, first-stage reverse osmosis system, two Level counter-infiltration system；

Preferably, the one-level nanofiltration system is sequentially connected and constituted by accurate filter and one-level NF membrane；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the one-level NF membrane is technical grade equipment with high desalinization NF membrane；

Preferably, the aperture of the one-level NF membrane is 1-2nm；

Preferably, the one-level NF membrane is 50-70% to the rejection of sodium ion；

Preferably, the rejection ＞ 97% of the one-level NF membrane heavy metal ion and salinity；

Preferably, the film pressure of entering of the one-level nanofiltration system is 1.0-1.5Mpa；

Preferably, the relative molecular mass retention scope of the one-level nanofiltration system is 150-300 dalton；

Preferably, the pH of the water of the entrance one-level nanofiltration system is 6-8；

Preferably, the permeate of the one-level nanofiltration system can be used as recycle-water；

Preferably, the concentrate of the one-level nanofiltration system enters first-stage reverse osmosis system.

5. processing method according to any one of claim 1 to 4, it is characterised in that in the step (3), described one Level counter-infiltration system is sequentially connected and constituted by accurate filter and first-stage reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the first-stage reverse osmosis film is bitter reverse osmosis membrane；

Preferably, the rejection ＞ 98% of the first-stage reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the first-stage reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the first-stage reverse osmosis system is 1.8Mpa；

Preferably, the pH of the water of the entrance first-stage reverse osmosis system is 5-6；

Preferably, pH is adjusted by adding hydrochloric acid in the first-stage reverse osmosis system；

Preferably, the salt acid for adjusting pH that concentration is 0.2-0.5% is added；

Preferably, the permeate of the first-stage reverse osmosis system returns to one-level nanofiltration system；

Preferably, the concentrate of the first-stage reverse osmosis system enters two-stage reverse osmosis system.

6. processing method according to any one of claim 1 to 5, it is characterised in that in the step (3), described two Level counter-infiltration system is sequentially connected and constituted by accurate filter and two-pass reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the precise microfiltration device is 5 μm；

Preferably, the two-pass reverse osmosis film is seawater reverse osmosis membrane；

Preferably, the rejection ＞ 99.5% of the two-pass reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the two-pass reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the two-stage reverse osmosis system is 4-5Mpa；

Preferably, the pH of the water of the entrance two-stage reverse osmosis system is 6-8；

Preferably, pH is adjusted by adding hydrochloric acid in the two-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%；

Preferably, the permeate of the two-stage reverse osmosis system returns to one-level nanofiltration system；

Preferably, the concentrate of the two-stage reverse osmosis system is the high salt concentrated water.

7. processing method according to any one of claim 1 to 6, it is characterised in that in the step (4), described to steam Sending out crystallization treatment step is：The high salt concentrated water that step (3) is obtained sequentially passes through heat exchanger, concentration evaporator, crystallizing evaporator；

Preferably, the operation temperature of the heat exchanger is 80-100 DEG C；

Preferably, the operating pressure of the heat exchanger is 0.05-0.1MPa；

Preferably, the concentration evaporator is sequentially connected by heating chamber, separation chamber, circular chamber, liquid distributor, demister and constituted；

Preferably, the crystallizing evaporator is sequentially connected and constituted by separation chamber, salt leg, thickener, crystallization kettle；

Preferably, condensed water of the high salt concentrated water after concentration evaporator returns to the two-stage reverse osmosis system；

Preferably, the high salt concentrated water obtains concentrating high salt concentrated water after concentration evaporator；

Preferably, the salt content of the concentration high salt concentrated water is 30-35%；

Preferably, the concentration high salt concentrated water obtains crystal and condensed water after crystallizing evaporator；Preferably, the crystallization Thing is sodium sulphate and/or sodium chloride；Preferably, the condensed water is used as recycle-water.

8. the processing system of zinc-containing water processing method as any one of claim 1 to 7, it is characterised in that the system System includes pretreatment unit, biochemical treatment unit, concentration unit and the evaporative crystallization processing unit being sequentially communicated.

9. processing system according to claim 8, it is characterised in that the pretreatment unit includes the broken zinc being sequentially communicated Pond, pH regulating reservoirs, chemical reaction pond, accurate control High-rate sedimentation system；The accurate control High-rate sedimentation system is by with water system System, precipitation process pond, inclined tube, effluent weir, sludge bucket are sequentially connected composition.

10. processing system according to claim 8 or claim 9, it is characterised in that the biochemical treatment unit includes being sequentially communicated Anaerobic pond, Aerobic Pond, membrane bioreactor；

Preferably, the membrane bioreactor is made up of hollow fiber film assembly and membrane cisterna；

Preferably, the hollow fiber film assembly is located in the membrane cisterna；

Preferably, the doughnut membrane aperture is 0.01-0.1 μm.

11. the processing system according to any one of claim 8 to 10, it is characterised in that the concentration unit bag Include the one-level nanofiltration system being sequentially communicated, first-stage reverse osmosis system, two-stage reverse osmosis system.

12. the processing system according to any one of claim 8 to 11, it is characterised in that the one-level nanofiltration system by Accurate filter and one-level NF membrane are sequentially connected composition；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

The one-level NF membrane is technical grade equipment with high desalinization NF membrane；

Preferably, the aperture of the one-level NF membrane is 1-2nm；

Preferably, the one-level NF membrane is 50-70% to the rejection of sodium ion；Preferably, the one-level NF membrane counterweight The rejection ＞ 97% of metal ion and salinity；

Preferably, the film pressure of entering of the one-level nanofiltration system is 1.0-1.5Mpa；

Preferably, the relative molecular mass retention scope of the one-level nanofiltration system is 150-300 dalton；

Preferably, the pH of the water of the entrance one-level nanofiltration system is 6-8.

13. the processing system according to any one of claim 8 to 12, it is characterised in that the first-stage reverse osmosis system It is sequentially connected and is constituted by accurate filter and first-stage reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

Preferably, the first-stage reverse osmosis film is bitter reverse osmosis membrane；

Preferably, the rejection ＞ 98% of the first-stage reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the first-stage reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the first-stage reverse osmosis system is 1.8Mpa；

Preferably, the pH of the water of the entrance first-stage reverse osmosis system is 5-6；

Preferably, pH is adjusted by adding hydrochloric acid in the first-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

14. the processing system according to any one of claim 8 to 13, it is characterised in that the two-stage reverse osmosis system It is sequentially connected and is constituted by accurate filter and two-pass reverse osmosis film；

Preferably, the filter core of the accurate filter is fusion-jet type PP cottons；

Preferably, the filter core aperture of the accurate filter is 5 μm；

Preferably, the two-pass reverse osmosis film is seawater reverse osmosis membrane；

Preferably, the rejection ＞ 99.5% of the two-pass reverse osmosis film heavy metal ion and salinity；

Preferably, the aperture of the two-pass reverse osmosis film is 0.1-1nm；

Preferably, the film pressure of entering of the two-stage reverse osmosis system is 4-5Mpa；

Preferably, the pH of the water of the entrance two-stage reverse osmosis system is 6-8；

Preferably, pH is adjusted by adding hydrochloric acid in the two-stage reverse osmosis system；

Preferably, the concentration of the hydrochloric acid is 0.2-0.5%.

15. the processing system according to any one of claim 8 to 14, it is characterised in that the evaporative crystallization unit bag Include the heat exchanger being sequentially communicated, concentration evaporator, crystallizing evaporator；

Preferably, the operation temperature of the heat exchanger is 80-100 DEG C；

Preferably, the operating pressure of the heat exchanger is 0.05-0.1MPa；

Preferably, the concentration evaporator is sequentially connected by heating chamber, separation chamber, circular chamber, liquid distributor, demister and constituted；

Preferably, the crystallizing evaporator is sequentially connected and constituted by separation chamber, salt leg, thickener, crystallization kettle.

16. the processing any one of processing method or claim 8 to 15 as any one of claim 1 to 7 Application of the system in Treatment of Zinc-containing Wastewater.