CN104230076B - The treatment process of reverse osmosis concentrated water in a kind of urban sewage recycling process - Google Patents
The treatment process of reverse osmosis concentrated water in a kind of urban sewage recycling process Download PDFInfo
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- CN104230076B CN104230076B CN201310232670.1A CN201310232670A CN104230076B CN 104230076 B CN104230076 B CN 104230076B CN 201310232670 A CN201310232670 A CN 201310232670A CN 104230076 B CN104230076 B CN 104230076B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
The invention discloses the treatment process of reverse osmosis concentrated water in a kind of urban sewage recycling process, comprise the following steps: (1) regulates reverse osmosis concentrated water pH and is heated to certain temperature; (2) be delivered in hydrophobic film assembly and carry out concentration; (3) proceed to concentrate after hard through " alkali tune-gravity settling separation-micro-filtrate membrane filtration "; (4) carry out solid-liquid separation after gravity settling, the mother liquor after separation carries out drying and other treatment, the reverse osmosis concentrated water of municipal effluent after two film process can be realized " zero release ".The invention solves reverse osmosis concentrated water that municipal effluent produces in two film treatment for reuse process cannot the problem of qualified discharge, the steam latent heat simultaneously produced by membrane distillation process and industrial low-grade heat source, effective utilization and saved the energy and running cost, present invention process possess skills advanced person, effluent quality is good, processing efficiency is high, the water resources rate of recovery is high, waste water heat utilization ratio advantages of higher.
Description
Technical field
The present invention relates to a kind for the treatment of process of reverse osmosis concentrated water, particularly membrane technique is adopted to carry out the treatment process of a small amount of dense water produced in advanced treatment engineering as second water source municipal effluent, namely film distillation technology is adopted to carry out the method for reverse osmosis concentrated water in city sewage deep reuse technology, more particularly, a kind of method utilizing the reverse osmosis concentrated water of vacuum membrane distillation technical finesse municipal effluent is related to.Belong to the further treatment technique field of municipal effluent.
Background technology
Shortage of water resources is one of the resource problem the severeest of 21 century facing mankind.The whole world only has 1/4 population to drink standard compliant clear water, and 1/3 population can not get safe water, and the situation of lack of water is on the rise.In the face of increasingly serious shortage of water resources problem, new way is all being explored energetically to obtain enough Freshwater resources in the whole world.Interbasin water transfer, sea water desaltination, reusing sewage and rain-water accumulating are with being the measure of increasing income generally come into one's own at present, they can alleviate the contradiction of supply and demand for the water resource to a certain extent, but Treated sewage reusing is often by as preferred option, very important reason is that water resource of reclaimed water can obtain nearby, the water yield is stablized, can not occur to disaccord with neighbour, the not impact of climate.
Along with Chinese society expanding economy, shortage of water resources problem becomes increasingly conspicuous.Development " waste water treating and reutilizing " is clearly write in " national economy and social development 10th Five-Year Plan outline " to realize " sustainable use of water resources ".Municipal middle water reuse is an effective behave of water saving pollution treatment, is again the functional sunrise industry of water resources sustainable development simultaneously.
In recent years, the outstanding problem having become puzzlement China socio-economic development in short supply of water resources.Special in populous city, being the high-pressure of water resources on the one hand, is that productive life creates a large amount of sewage and causes serious threat to ecotope on the other hand.Waste water is back to after process up to standard and Treatment for Reuse production system or life to use mixedly and be called as reusing sewage.The wide range of reusing sewage, from supplementary feed and the domestic water of industrial recycling water body.Reusing sewage both can have been saved and utilize limited to Freshwater resources that are preciousness effectively, the quantity discharged of sewage or waste water can be reduced again, alleviate the pollution of water surrounding, the excess load phenomenon of urban discharging pipeline can also be alleviated, there is obvious social benefit, environmental benefit and economic benefit.
Municipal wastewater is the general designation that city and organic town enter the water of sewerage system, the rainwater comprising sanitary sewage, factory effluent and dam in combined drainage system.The amount of municipal wastewater is general comparatively large, can reach more than ton every day.Generally reach country-level or secondary discharge standard after treatment, enter river course or ocean.Municipal effluent, for the shortage of alleviation lack of water city water resource, reduces urban water resource and pollutes significant.
Within 2010, National urban water displacement will reach 600 × 10
8m
3, the sewage average treatment rate of national the planned city is not less than 50%, key cities' wastewater reusing treatment rate 70%.This just creates primary condition to reusing sewage.If whole nation reusing sewage rate on average reaches 20%, year reuse amount can reach 40 × 10
8m
3, be normal year in time lack of water 60 × 10
8m
367%, namely by reusing sewage, the more than half part of National urban water deficit can be solved, reuse scale and reuse potentiality big, can to alleviate the water supply gets situation in large quantities of lack of water city.
Current recycling municipal sewage, major part is as Treated sewage reusing in landscape water, or industrial cooling circulating water.In a lot of area, because saltiness in sewage is high or organism, suspension content are high, permitted discharge still cannot meet reuse water quality requirement through simple Treatment for Reuse, as the water quality requirement of circulating cooling make-up water, boiler replenishing water.Now need to carry out further advanced treatment to permitted discharge.In the further treatment technique of sewage, the two membrane technique of ultra filtering reverse osmosis is current the most economically viable method.
Two membrane technique be ultrafiltration/micro-filtration (UF/MF) technology is combined with reverse osmosis (RO) technology together with technique.Wherein, reverse osmosis technology is most advanced and the most energy-conservation effective membrane separation technique now.Its principle is under the effect higher than solution osmotic pressure, these materials and water can not be separated according to other materials through semi-permeable membranes.Because the membrane pore size of reverse osmosis membrane is very little, be only about 1nm, therefore, it is possible to effectively remove dissolved salts, colloid, microorganism, organism etc. in water, clearance is up to 97 ~ 99%.Reverse osmosis membrane system have water quality good, consume energy low, pollution-free, technique is simple, the advantage such as easy and simple to handle, but because two membranous system belongs to physical filtering process, due to the restriction of the rate of recovery in reusing sewage process, the rate of recovery is 60 ~ 80% under normal circumstances, and the reverse osmosis concentrated water always having 20 ~ 40% can not effectively be disposed because of the concentrated saltiness high containing more former water and pollutent.
Chinese patent CN102408165A discloses a kind of deep treatment method of municipal wastewater up to standard.Advanced treatment process of municipal wastewater up to standard described in this patent comprises flocculation sediment, sterilization, video disc filtration, immersion ultrafiltration, the several step of reverse osmosis.Reverse osmosis produced water water quality reaches reuse requirement.Reverse osmosis concentrated water and other a large amount of permitted discharge are blent rear discharge or are processed further and reach emission standard.Although this patented technology refer to the discharging modes of reverse osmosis concentrated water, only belonging to comparatively simple processing mode because blending discharge, failing in actual procedure to the abatement of the principal pollutant in dense water as total dissolved solidss, organic content etc.
Chinese patent ZL201010517699.0 discloses a kind for the treatment of process of municipal middle water, and particularly a kind of municipal middle water is used for the deep treatment method of power plant's cooling water.The advanced treatment method for urban water of electric power plant of this invention, adopts following steps: Air Exposure, filters; Add slaked lime, coagulant polymeric ferric sulfate and high-efficient coagulant aide; Add sterilant and carry out sterilization; Add composite scale-inhibiting corrosion inhibitor, after mixing, be added to power plant's cycling use of water.This patent of invention only adopts comparatively simple treatment process to carry out reasonable sanding to municipal middle water, does not relate to related film Technology.
Chinese patent CN 102180552A discloses a kind of urban sewage recycling in the method for recirculated cooling water and boiler water feeding, comprise the steps: that the externally discharged waste water that municipal sewage plant meets emission standard after secondary biochemical treatment enters MBBR, in MBBR, BOD and ammonia nitrogen are degraded, water after MBBR process introduces rapidly miscible pool, with coagulating agent short mix in rapidly miscible pool, flocculation basin is entered with the water of coagulating agent short mix, water after flocculation treatment enters Airfloat filtering pond, carry out air-dissolving air-float and multi-medium filtering process, water after air-dissolving air-float and multi-medium filtering process enters into ultra-filtration membrane, and carry out the roughing out of film, the water of the roughing out through film is introduced in first-stage reverse osmosis equipment and carries out a membrane sepn, water after a membrane separation is introduced in second-level reverse osmosis device and carried out secondary membrane separation and by the water after process for oiler feed provides.This patent of invention adopts biochemical method to carry out the pre-treatment of ultrafiltration and reverse osmosis membrane Technology for standard discharge municipal effluent after secondary biochemical treatment again, one sewage after secondary biochemical treatment itself does not have biodegradability substantially, again carry out biochemical pre-treatment and not only increase investment running cost, and bring bad result for the operation of subsequent film technique, two carry out this patent does not define the process of the dense water of reverse osmosis process.
Chinese patent CN101209886 discloses a kind of advanced treatment recycling technique of urban sewage adopting membrane bioreactor and reverse osmosis coupling.Be former water with the secondary effluent of municipal effluent after Sewage Plant process, or by municipal effluent through process reach secondary effluent after water be former water, enter membrane bioreactor MBR system and carry out biochemical pre-treatment, remove BOD, COD, SS, the ammonia nitrogen in water, the water after process is made to reach feed water by reverse osmosis water quality requirement, again through the further advanced desalination process of reverse osmosis system, required reuse water can be obtained.This patent only limits from sewage deep reuse angle, does not limit the processing mode of the reverse osmosis concentrated water produced in reuse technology process.
Chinese patent CN1796314 discloses a kind of method of city sewage deep treatment, the method comprises employing coagulation and filtration, ozone oxidation, bio-oxidation, advanced treatment is carried out to municipal effluent, to remove difficult degradation micro-content organism, bacterium, virus etc. remaining in municipal effluent secondary effluent, decolouring, except smelling, reaches the object of safe reuse.It is that water source carries out degree of depth reuse with municipal effluent that this patent does not relate to related film Technology.
The mode that the existing major part of the Patents for city standard discharge advanced treatment of wastewater reuse adopts biochemistry, pre-treatment and two membrane process to combine carries out processing rear reuse technology.Foregoing invention patent adopts different process to carry out the restriction of appropriate reuse and degree of depth reuse to municipal effluent up to standard, as recirculated cooling water and boiler replenishing water, but does not define the treatment technology of this technique reverse osmosis concentrated water.Although related to the qualified discharge mode of reverse osmosis concentrated water in CN102408165A, namely reverse osmosis concentrated water and other a large amount of permitted discharge are blent rear discharge or are processed further and reach emission standard, but it refer to reverse osmosis concentrated water and other a large amount of permitted discharge to be blent rear discharge or process further and reaches emission standard, only give suggestion to the qualified discharge of reverse osmosis concentrated water, and do not carry out limiting and play-by-play for the technical side's rule how above-mentioned reverse osmosis concentrated water makes advanced treatment.
Summary of the invention
The invention discloses the treatment process of reverse osmosis concentrated water in a kind of urban sewage recycling process, be intended to for the deficiencies in the prior art, provide a kind of municipal effluent up to standard to adopt remaining reverse osmosis concentrated method for deeply treating water after two membrane technique process.This treatment process main purpose is a small amount of reverse osmosis concentrated water processing reverse osmosis units generation further, organism, inorganic salt etc. in further removal reverse osmosis concentrated water, improve the utilization ratio of municipal effluent, reduce wastewater discharge to greatest extent, make full use of waste water residual heat, to greatest extent recycle-water resource and heat energy.
The present invention adopts following technical scheme to realize:
The reverse osmosis concentrated water water quality principal character of municipal effluent of the present invention after two film process is: pH is 7.0 ~ 8.5, colourity 30 ~ 60 times, dense water power leads 5000 ~ 7000 μ s/cm, COD 200 ~ 400mg/L, TOC 50 ~ 100mg/L, with calcium carbonate hardness 1000 ~ 1500mg/L, with calcium carbonate methyl orange alkalinity 1200 ~ 1600mg/L, Cl
-600 ~ 1000mg/L, NH
4 +-N 60 ~ 150mg/L, SO
4 2-600 ~ 1200mg/L, total iron 0.2 ~ 0.5mg/L.
A treatment process for reverse osmosis concentrated water in urban sewage recycling process, comprises the following steps:
(1) reverse osmosis concentrated water of municipal effluent after two film process, enters RO dense water pH regulator pond, regulates pH and adopts the mode of heating or heat exchange to be heated to certain temperature;
(2) by the reverse osmosis concentrated water after heating in step (1), through raw water pump, be delivered in hydrophobic film assembly, hydrophobic film assembly has specific placement form, in this process, by by-pass valve after pump and dense penstock, regulate hydrophobic film assembly feed liquid side feed pressure and feed liquid side crossflow velocity;
(3) hydrophobic film module permeate side in the step (2), adopts the mode vacuumized that the steam after infiltration is formed membrane distillation through condensation and produces water, and this product water can direct reuse or mix rear reuse with reverse osmosis produced water;
(4) adopt the mode of the dense water cycle of part that the dense water of the generation in step (3) is concentrated, reach certain cycles of concentration, to send into close to saturated or oversaturated dense water and add alkali pH regulator unit, and after being adjusted to suitable pH, entering gravity separator and be separated;
(5) by the supernatant liquid in step (4) after gravity settling separation, through fresh feed pump, send into microfiltration membrane unit, to remove the suspended substance of trace, the product water of microfiltration membrane unit is incorporated to RO dense water pH regulator pond, carries out advanced treatment;
(6) by the waste water being rich in a large amount of suspended substance after the gravity settling in step (4), send into centrifuge separator and carry out solid-liquid separation, the mother liquor after separation is delivered to spraying dry unit and carries out drying and other treatment.
Can realize like this " zero release " of the reverse osmosis concentrated water of municipal effluent after two film process.
Technical characteristics of the present invention comprises following content:
Reverse osmosis concentrated water pH regulator in step (1) is pH6 ~ 8, and preferred pH is 6.5 ~ 7.5.
In step (1), acid adding is for regulating reverse osmosis concentrated water pH, and can adopt strong acid and the middle strong acid such as sulfuric acid, hydrochloric acid, oxalic acid, wherein the concentration of all kinds of acid is unrestricted.
Be direct heating or heat exchange to the type of heating of reverse osmosis concentrated water in step (1), exhaust steam heat, electrically heated, industrial waste heat or sun power etc. can be adopted to be thermal source, or the combination of these thermals source; Heating temperature is 40 ~ 90 DEG C, is preferably 60 ~ 85 DEG C.
Hydrophobic film assembly in step (2) can adopt hollow fiber form assembly, plate and frame assembly or wound module.
Hydrophobic membrane materials in step (2) is the organic polymer material of polyvinylidene difluoride (PVDF), polysulfones, polypropylene, tetrafluoroethylene; The pore diameter range of hydrophobic film is 0.1 ~ 0.5 μm, and optimum is 0.15 ~ 0.2 μm.
The specific placement form of hydrophobic film assembly in step (2), can adopt standing manner or have the flat manner at certain angle of inclination; Angle of inclination in flat manner situation is 5 ~ 60 °, and preferred angle of inclination is 15 ~ 30 °.
In step (2), the feed liquid side feed pressure of hydrophobic film assembly is 0.005 ~ 0.03MPa, and preferred feed pressure is 0.015 ~ 0.025MPa; Crossflow velocity 0.6 ~ 1.0m/s, is preferably 0.7 ~ 0.9m/s.
The form that reverse osmosis concentrated water in step (2) enters hydrophobic hollow fiber membrane module can adopt the mode of interior pressure or external pressure.
In step (2), the length of single hollow fiber film assembly is 50 ~ 150cm, is preferably 80 ~ 100cm; The packing factor of single hollow fiber film assembly is 30 ~ 70%, is preferably 40 ~ 60%.
In step (3), the vacuum tightness of hydrophobic film module permeate side is 0.06 ~ 0.1MPa, is preferably 0.08 ~ 0.098MPa.
In step (3), the flux of hydrophobic film assembly film is 10 ~ 40L/m
2h, is preferably 15 ~ 35L/m
2h.
In step (3), the condensing mode of penetrating fluid can adopt indirectly water-cooled, refrigerant form air-cooled or capable of circulation.
Steam after infiltration in step (3), can be used for carrying out thermal exchange with the mode of reverse osmosis concentrated water heat exchange, realizes effective utilization of the latent heat of vaporization.
In step (4), the cycles of concentration of reverse osmosis concentrated water is 10 ~ 40 times, preferably 15 ~ 35 times.
In step (4), the pH regulator of the dense water of membrane distillation is 8 ~ 9.5, and preferred pH is 8.5 ~ 9.0.
Be 15 ~ 120min in the residence time of gravity separator in step (4), be preferably 30 ~ 90min.
Microfiltration membrane unit in step (5), comprise pressure type or immersed microfiltration membrane filtration, the form of membrane module can adopt following in one or more: hollow fiber film assembly, tubular membrane component or curtain type film assembly, optimum is hollow fiber film assembly or tubular membrane component;
The organic film material of the microfiltration membrane unit membrane assembly in step (5) adopt in polysulfones, polyolefins or polyvinylidene difluoride (PVDF) class one or more; Preferred polyvinylidene difluoride (PVDF), polyethersulfone or polypropylene; Membrane pore size is 0.1 ~ 0.3 μm, and optimum is 0.15 ~ 0.25 μm;
The operation scheme of the microfiltration membrane unit membrane assembly in step (5) is cross flow filter or dead-end filtration technique, and wherein dead-end filtration technique can realize go-and-retum every water inlet, and optimum is cross-flow technique;
Can realize in the automatic operational process of the microfiltration membrane unit membrane assembly in step (5) disperseing to wash, strengthen washing and soak the periodical operation washed, wherein dispersion is washed and can be realized two ends alternately water inlet, the water inlet cycle is respectively 15 ~ 30 minutes, and optimum is 20 ~ 25 minutes; Backwashing time is 60 ~ 120 seconds; Operating flux in microfiltration membrane unit operational process is 85 ~ 180L/ (m
2h), optimum is 120 ~ 150L/ (m
2h);
Microfiltration membrane unit in step (5), cleaning microfiltration membranes mode can select one or more of following manner: wash online, off-line washes or steam-water mixing is washed, and optimumly washes for steam-water mixing; The reinforcement of filtering system film is washed and the pickling of soaking in washed journey can be selected in following acid one or more, described acid comprises HCl, oxalic acid, citric acid, nitric acid, sulfuric acid and cleans with the acid of the composite clean-out system of EDTA;
Spraying dry unit operation in step (6), kiln temperature in is 200 ~ 250 DEG C, and kiln temperature out is 90 ~ 100 DEG C.
The essential distinction of the present invention and prior art is, the present invention relates to the deep treatment method of the reverse osmosis concentrated water of a kind of municipal effluent after two film process.The present invention is intended to carry out further advanced treatment and reuse for the reverse osmosis concentrated water of standard discharge municipal effluent after two film process, with recycle-water resource to greatest extent, reduces wastewater discharge, improves Waste Heat Reuse efficiency.Although refer in publication CN102408165 A in the introduction reverse osmosis concentrated water and other a large amount of permitted discharge to be blent rear discharge or process further and reach emission standard, but it only gives suggestion to the qualified discharge of reverse osmosis concentrated water, the further treatment technique for above-mentioned reverse osmosis concentrated water does not but carry out limiting and play-by-play.With the reverse osmosis concentrated water technology technology of the municipal effluent related in the present invention after two membrane technique process, there is essential distinction.
The present invention can produce following beneficial effect:
1, because the reverse osmosis concentrated water saltiness of city standard discharge sewage after two membrane process process is very high, relatively high general 5000 ~ 7000 μ s/cm of conductance, and containing a small amount of small organic molecule, COD is 200 ~ 400mg/L, therefore, the equipment with high desalinization of membrane distillation system, high organic removal rate advantage can be made full use of, high enrichment process is carried out to waste water;
2, method of the present invention is adopted, substantially the reverse osmosis concentrated water discharge difficulty of city standard discharge sewage after two membrane process process or the practical problems of dilution qualified discharge can be solved, and the height achieving municipal effluent up to standard is recycled, reclaimed water resources to greatest extent, combination pre-treatment and two membrane technique can realize " zero release " of city permitted discharge.
3, the reverse osmosis concentrated water of art breading city of the present invention standard discharge sewage after two membrane process process is adopted, membrane distillation produces water power and leads≤30 μ S/cm, produce water TOC≤10mg/L, Water Sproading rate is higher than 90%, membrane distillation produces water can be back to production technique water, highly achieves the recycling of waste water.
The inventive method solves reverse osmosis concentrated water that municipal effluent produces in two film treatment for reuse process cannot the problem of qualified discharge, can by realization " zero release " after the reverse osmosis concentrated water treatment of municipal effluent after two film process.Adopt technique of the present invention can to direct reuse after the reverse osmosis concentrated water advanced treatment of municipal effluent after two membrane process process, the steam latent heat simultaneously produced by membrane distillation process and industrial low-grade heat source, effective utilization and saved the energy and running cost, present invention process possess skills advanced person, effluent quality is good, processing efficiency is high, the water resources rate of recovery is high, waste water heat utilization ratio advantages of higher.
Accompanying drawing explanation
Fig. 1 is present invention process general flow chart;
Fig. 2 is the present invention's each cell process operating process schematic diagram,
Figure acceptance of the bid score not Biao Shi:
1-RO dense water pH regulator pond, 2-interchanger, 3-raw water pump, 4-hydrophobicity membrane component,
5-condenser, 6-produce water tank, 7-vacuum pump, 8-outer working shaft, 9-add alkali pH regulator pond,
10-gravity separator, 11-fresh feed pump, 12-microfiltration membrane unit, 13-centrifuge separator,
14-spray-dryer.
Embodiment
Below, by reference to the accompanying drawings and specific embodiment, invention embodiment is further described.
As shown in figure 1 and 2, treatment process of the present invention comprises the following steps: (1) regulates reverse osmosis concentrated water pH and adopts the mode of heating or heat exchange that reverse osmosis concentrated water is heated to certain temperature; (2) reverse osmosis concentrated water after heating is delivered in the hydrophobic film assembly with specific placement form, adopts the mode of the dense water cycle of part to carry out concentration; (3) the dense water of membrane distillation proceeds to concentrate after hard through " alkali tune-gravity settling separation-micro-filtrate membrane filtration "; (4) waste water being rich in a large amount of suspended substance after gravity settling carries out solid-liquid separation through centrifuge separator, mother liquor after separation is delivered to spraying dry unit and is carried out drying and other treatment, the reverse osmosis concentrated water of municipal effluent after two film process can be realized " zero release ".
Embodiment 1
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH8.5, colourity 30 times, dense water power leads 5000 μ s/cm, COD 200mg/L, TOC 50mg/L, hardness (with calcium carbonate) 1000mg/L, methyl orange alkalinity (with calcium carbonate) 1200mg/L, Cl
-600mg/L, NH
4 +-N 60mg/L, SO
4 2-600mg/L, total iron 0.2mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density sulfuric acid to regulate feedwater pH to 8.0, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, used heat is utilized to be heated to 40 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter vertical placement, pore size is in the PVDF tubular fibre hydrophobic film assembly of 0.2 μm, the useful length of this hydrophobic membrane assembly is 50cm, and in single membrane module, the loading level of hollow-fibre membrane is 70%; Regulate the feed pressure of hydrophobic membrane assembly to be 0.03MPa by the by-pass valve of raw water pump 3, and regulate waste water to be 0.6m/s at the crossflow velocity of hollow-fibre membrane inner chamber; It is the condenser 5 of heat-eliminating medium that the water vapor produced through PVDF hydrophobic hollow fiber membrane assembly and a small amount of volatile organism enter with water under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.1MPa, and flux of membrane distillation is 10L/m
2h, it is 7.5 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft 8.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 40, the dense water of outer row then enters and adds alkali pH regulator pond 9, the dense water pH of membrane distillation is regulated to be 9.0 by adding certain density NaOH, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 100min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.1 μm of PVDF tubular fibre, and Membrane Filtration Flux is 90L/m
2h, adjustment micro-filtrate membrane filtration system recoveries rate is 80%, and the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and proceeded advanced treatment, dense water cycle to gravitational settling separator 10; The mode that micro-filtrate membrane filtration system adopts cross flow filter, two ends alternately intake, alternately flooding time is spaced apart a filtration cycle, the filtration cycle of micro-filtrate membrane filtration system is 25min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 25min enters backwash procedure, and the backwash time of this process is 60 seconds; After reaching 2 filtration cycles filtration cycle, program starts the dispersion adding hydrochloric acid and washes and soak washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 250 DEG C, kiln temperature out is obtain solid under the condition of 100 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
Embodiment 2
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH7.5, colourity 40 times, dense water power leads 6000 μ s/cm, COD 300mg/L, TOC 75mg/L, hardness (with calcium carbonate) 1200mg/L, methyl orange alkalinity (with calcium carbonate) 1400mg/L, Cl
-800mg/L, NH
4 +-N 100mg/L, SO
4 2-800mg/L, total iron 0.4mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density hydrochloric acid to regulate feedwater pH to 6.5, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, electrically heated is adopted to be heated to 60 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter hydrophobic membrane assembly and horizontal plane angle is that 15 ° are placed, pore size is in the PSF tubular fibre hydrophobic film assembly of 0.1 μm, the useful length of this hydrophobic membrane assembly is 80cm, and in single membrane module, the loading level of hollow-fibre membrane is 60%; Regulate the feed pressure of hydrophobic membrane assembly to be 0.025MPa by the by-pass valve of feedstock pump 3, and regulate waste water to be 0.7m/s at the crossflow velocity of hollow-fibre membrane shell side; It is the condenser 5 of heat-eliminating medium that the water vapor produced through PSF hydrophobic hollow fiber membrane assembly and a small amount of volatile organism enter with wind under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.098MPa, and flux of membrane distillation is 15L/m
2h, it is 7.4 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 15, and the dense water of outer row then enters and adds alkali pH regulator pond 9, by adding certain density NaCO
3the dense water pH of membrane distillation is regulated to be 8.0, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 120min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.3 μm of PES hollow-fibre membrane, and Membrane Filtration Flux is 180L/m
2h, adjustment micro-filtrate membrane filtration system recoveries rate is 90%, and the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and proceeded advanced treatment, dense water cycle to gravitational settling separator 10; The mode that micro-filtrate membrane filtration system adopts cross flow filter, two ends alternately intake, alternately flooding time is spaced apart a filtration cycle, the filtration cycle of micro-filtrate membrane filtration system is 15min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 15min enters backwash procedure, and the backwash time of this process is 120 seconds; After reaching 3 filtration cycles filtration cycle, program starts the dispersion adding sulfuric acid and washes and soak washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 230 DEG C, kiln temperature out is obtain solid under the condition of 95 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
Embodiment 3
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH8.0, colourity 50 times, dense water power leads 5500 μ s/cm, COD 250mg/L, TOC 63mg/L, hardness (with calcium carbonate) 1100mg/L, methyl orange alkalinity (with calcium carbonate) 1300mg/L, Cl
-700mg/L, NH
4 +-N 80mg/L, SO
4 2-700mg/L, total iron 0.3mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density hydrochloric acid to regulate feedwater pH to 7.5, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, industrial waste heat is adopted to be heated to 80 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter hydrophobic membrane assembly and horizontal plane angle is that 30 ° are placed, pore size is in the PP tubular fibre hydrophobic film assembly of 0.15 μm, the useful length of this hydrophobic membrane assembly is 100cm, and in single membrane module, the loading level of hollow-fibre membrane is 40%; Regulate the feed pressure of hydrophobic membrane assembly to be 0.015MPa by the by-pass valve of feedstock pump 3, and regulate waste water to be 0.8m/s at the crossflow velocity of hollow-fibre membrane tube side; It is the condenser 5 of cooling conditions that the water vapor produced through PP hydrophobic hollow fiber membrane assembly and a small amount of volatile organism enter with refrigerant under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.08MPa, and flux of membrane distillation is 35L/m
2h, it is 7.6 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 35, the dense water of outer row then enters and adds alkali pH regulator pond 9, the dense water pH of membrane distillation is regulated to be 8.5 by adding certain density NaOH, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 60min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.2 μm of PVDF tubular fibre curtain type membrane, and Membrane Filtration Flux is 130L/m
2h, the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and is proceeded advanced treatment, dense water section is circulated to gravitational settling separator 10; Micro-filtrate membrane filtration system adopts the mode of dead-end filtration, the filtration cycle of micro-filtrate membrane filtration system is 20min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 20min enters backwash procedure, and the backwash time of this process is 110 seconds; After reaching 2 filtration cycles filtration cycle, program starts the dispersion adding oxalic acid and washes and soak washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 220 DEG C, kiln temperature out is obtain solid under the condition of 94 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
Embodiment 4
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH7.0, colourity 60 times, dense water power leads 6500 μ s/cm, COD 350mg/L, TOC 80mg/L, hardness (with calcium carbonate) 1400mg/L, methyl orange alkalinity (with calcium carbonate) 1500mg/L, Cl
-900mg/L, NH
4 +-N 120mg/L, SO
4 2-1000mg/L, total iron 0.4mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density oxalic acid to regulate feedwater pH to 6.0, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, the mode of solar heating is adopted to be heated to 85 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter hydrophobic membrane assembly and horizontal plane angle is that 60 ° are placed, pore size is in the PVDF tubular fibre hydrophobic film assembly of 0.3 μm, the useful length of this hydrophobic membrane assembly is 150cm, and in single membrane module, the loading level of hollow-fibre membrane is 30%; Regulate the feed pressure of hydrophobic membrane assembly to be 0.005MPa by the by-pass valve of feedstock pump 3, and regulate waste water to be 0.9m/s at the crossflow velocity of hollow-fibre membrane shell side; It is the condenser 5 of cooling conditions that the water vapor produced through PVDF hydrophobic hollow fiber membrane assembly and a small amount of volatile organism enter with refrigerant under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.06MPa, and flux of membrane distillation is 30L/m
2h, it is 7.6 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 30, and the dense water of outer row then enters and adds alkali pH regulator pond 9, by adding certain density NaCO
3the dense water pH of membrane distillation is regulated to be 8.0, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 90min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.15 μm of PP hollow-fibre membrane, and Membrane Filtration Flux is 120L/m
2h, adjustment micro-filtrate membrane filtration system recoveries rate is 95%, and the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and proceeded advanced treatment, dense water cycle to gravitational settling separator 10; The mode that micro-filtrate membrane filtration system adopts cross flow filter, two ends alternately intake, alternately flooding time is spaced apart a filtration cycle, the filtration cycle of micro-filtrate membrane filtration system is 23min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 23min enters backwash procedure, and the backwash time of this process is 90 seconds; After reaching 5 filtration cycles filtration cycle, the dispersion that program starts adding citric acid is washed and soaks washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 210 DEG C, kiln temperature out is obtain solid under the condition of 92 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
Embodiment 5
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH8.5, colourity 40 times, dense water power leads 7000 μ s/cm, COD 400mg/L, TOC 100mg/L, hardness (with calcium carbonate) 1500mg/L, methyl orange alkalinity (with calcium carbonate) 1600mg/L, Cl
-1000mg/L, NH
4 +-N 150mg/L, SO
4 2-1200mg/L, total iron 0.5mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density hydrochloric acid to regulate feedwater pH to 8.0, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, adopt electrically heated to be heated to 90 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter hydrophobic membrane assembly and horizontal plane angle is that 5 ° are placed, pore size is in the PTFE plate and frame hydrophobic film assembly of 0.1 μm; Regulate the feed pressure of hydrophobic membrane assembly to be 0.01MPa by the by-pass valve of feedstock pump 3, and regulate the crossflow velocity of waste water in PTFE plate and frame module to be 1.0m/s; It is the condenser 5 of cooling conditions that the water vapor produced through PTFE plate and frame hydrophobic membrane assembly and a small amount of volatile organism enter with heat-eliminating medium under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.09MPa, and flux of membrane distillation is 40L/m
2h, it is 7.5 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 10, the dense water of outer row then enters and adds alkali pH regulator pond 9, the dense water pH of membrane distillation is regulated to be 9.5 by adding certain density NaOH, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 15min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.25 μm of PVDF hollow-fibre membrane, and Membrane Filtration Flux is 150L/m
2h, adjustment micro-filtrate membrane filtration system recoveries rate is 95%, and the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and proceeded advanced treatment, dense water cycle to gravitational settling separator 10; The mode that micro-filtrate membrane filtration system adopts cross flow filter, two ends alternately intake, alternately flooding time is spaced apart a filtration cycle, the filtration cycle of micro-filtrate membrane filtration system is 20min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 20min enters backwash procedure, and the backwash time of this process is 100 seconds; After reaching 4 filtration cycles filtration cycle, program starts the dispersion adding hydrochloric acid and washes and soak washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 200 DEG C, kiln temperature out is obtain solid under the condition of 90 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
Embodiment 6
The advanced treatment process flow process of municipal effluent reverse osmosis concentrated water after two film process as depicted in figs. 1 and 2, RO dense water pH regulator pond 1 acid adding is sent under the effect of reverse osmosis concentrated water after two film process in overbottom pressure, wherein reverse osmosis concentrated water water quality significant parameter comprises: pH7.5, colourity 50 times, dense water power leads 6000 μ s/cm, COD 300mg/L, TOC 75mg/L, hardness (with calcium carbonate) 1200mg/L, methyl orange alkalinity (with calcium carbonate) 1400mg/L, Cl
-800mg/L, NH
4 +-N 100mg/L, SO
4 2-900mg/L, total iron 0.3mg/L.
The reverse osmosis concentrated water entering RO dense water pH regulator pond adopts certain density hydrochloric acid to regulate feedwater pH to 6.5, after the steam latent heat that first waste water after pH regulator adopt membrane distillation to produce carries out heat exchange, adopt exhaust steam to be heated to 60 DEG C to the reverse osmosis concentrated water after preheating, under the lifting of feedstock pump 3, enter upright placement, pore size is in the PTFE rolling hydrophobic film assembly of 0.4 μm; Regulate the feed pressure of hydrophobic membrane assembly to be 0.02MPa by the by-pass valve of feedstock pump 3, and regulate the crossflow velocity in waste water PTFE rolling hydrophobic film assembly to be 0.9m/s; It is the condenser 5 of cooling conditions that the water vapor produced through the hydrophobic rolled membrane module of PTFE and a small amount of volatile organism enter with refrigerant under the suction function of vacuum pump 7 after interchanger 2 is suitably lowered the temperature again, and then after being converted into liquid water, enter product water tank 6, wherein hydrophobic film module permeate side vacuum tightness is 0.095MPa, and flux of membrane distillation is 20L/m
2h, it is 7.5 that membrane distillation produces water pH, conductance≤20 μ S/cm, TOC≤10mg/L, Cl
-≤ 50mg/L, NH
4 +-N≤5mg/L, produces water by Liquid level membrane distillation and is delivered to middle low-pressure boiler water charging system through outer working shaft.
The cycles of concentration adopting the mode of part concentrate recirculation to regulate hydrophobic film to distill unit is 20, the dense water of outer row then enters and adds alkali pH regulator pond 9, the dense water pH of membrane distillation is regulated to be 9.3 by adding certain density NaOH, the dense water of membrane distillation after pH regulator enters gravity separator 10, after containing after pH regulator is stopped 30min compared with the suspension of the scale forming matters such as calcium polycarbonate in gravity separator 10, supernatant liquor is delivered to micro-filtrate membrane filtration unit 12 to remove the fouling tendency suspended substance of trace in supernatant liquor by overflow port through fresh feed pump 11
Microfiltration membrane under this condition selects 0.2 μm of PP tubular fibre curtain type membrane, and Membrane Filtration Flux is 85L/m
2h, the product water of micro-filtrate membrane filtration is delivered to after acid adding pH regulator pond 1 mixes with former water and is proceeded advanced treatment, dense water section is circulated to gravitational settling separator 10; Micro-filtrate membrane filtration system adopts the mode of dead-end filtration, the filtration cycle of micro-filtrate membrane filtration system is 30min, namely the working procedure opening and closing respective valves of microfiltration membrane immediately by PLC after carrying out the product water of 30min enters backwash procedure, and the backwash time of this process is 80 seconds; After reaching 2 filtration cycles filtration cycle, program starts the dispersion adding hydrochloric acid and washes and soak washed journey, regulating online administration timing of drug and chemical feeding quantity to control matting pH is 3, and soak time is 5min, proceeds normal operation after carrying out the flushing operation of 5 seconds afterwards; Above-mentioned washing, the chemical dispersion flow washed in the backwash process after washing with chemical immersion is 2 times of microfiltration membrane water production rate.
Aq suspension after gravity separator 10 sedimentation is after being pumped into centrifuge separator 13 and carrying out solid-liquid separation, a small amount of liquid sends into spraying dry unit 14, the temperature in controlling spraying dry unit is 240 DEG C, kiln temperature out is obtain solid under the condition of 96 DEG C, itself and centrifuge separator 13 gained solids mixing is disposed.
The foregoing is only better possible embodiments of the present invention, not thereby limit to the scope of the claims of the present invention, therefore the equivalence change that every utilization specification sheets of the present invention and accompanying drawing content are done, be all contained in protection scope of the present invention.
Claims (20)
1. the treatment process of reverse osmosis concentrated water in urban sewage recycling process, comprises the following steps:
(1) reverse osmosis concentrated water of municipal effluent after two film process, enters RO dense water pH regulator pond, regulates pH be 6 ~ 8 and be heated to 40 ~ 90 DEG C;
(2) by the reverse osmosis concentrated water after heating in step (1), be delivered in hydrophobic film assembly, in this process, regulate hydrophobic film assembly feed liquid side feed pressure to be 0.005 ~ 0.03MPa, feed liquid side crossflow velocity 0.6 ~ 1.0m/s;
(3) hydrophobic film module permeate side in step (2), adopts the mode vacuumized to be formed through condensation by the steam after infiltration and produces water, this product water direct reuse or reuse after mixing with reverse osmosis produced water;
(4) the dense water adopting the mode of the dense water cycle of part to make to produce in step (3) concentrates, cycles of concentration is 10 ~ 40 times, to send into close to saturated or oversaturated dense water and add alkali pH regulator unit, pH regulator is 8 ~ 9.5, enters gravity separator and is separated;
(5) by the supernatant liquid in step (4) after gravity settling separation, send into microfiltration membrane unit, to remove the suspended substance of trace, the product water of microfiltration membrane unit is incorporated to RO dense water pH regulator pond, carries out advanced treatment;
(6) by the waste water being rich in a large amount of suspended substance after the gravity settling in step (4), send into centrifuge separator and carry out solid-liquid separation, the mother liquor after separation is delivered to spraying dry unit and carries out drying and other treatment.
2. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, it is characterized in that, the water quality characteristic of described reverse osmosis concentrated water after two film process is: pH is 7.0 ~ 8.5, colourity 30 ~ 60 times, dense water power leads 5000 ~ 7000 μ s/cm, COD200 ~ 400mg/L, TOC 50 ~ 100mg/L, with calcium carbonate hardness 1000 ~ 1500mg/L, with calcium carbonate methyl orange alkalinity 1200 ~ 1600mg/L, Cl
-600 ~ 1000mg/L, NH
4 +-N 60 ~ 150mg/L, SO
4 2-600 ~ 1200mg/L, total iron 0.2 ~ 0.5mg/L.
3. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, it is characterized in that, the reverse osmosis concentrated water pH regulator in step (1) is 6.5 ~ 7.5.
4. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, it is characterized in that, described in step (1), Heating temperature is 60 ~ 85 DEG C.
5. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, is characterized in that, the hydrophobic film assembly in step (2) adopts hollow fiber form assembly, plate and frame assembly or wound module.
6. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, it is characterized in that, the hydrophobic membrane materials in step (2) is polyvinylidene difluoride (PVDF), polysulfones, polypropylene or tetrafluoroethylene; The pore diameter range of hydrophobic film is 0.1 ~ 0.5 μm.
7. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 6, it is characterized in that, the pore diameter range of hydrophobic film is 0.15 ~ 0.2 μm.
8. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, is characterized in that, in step (2), the placement form of hydrophobic film assembly adopts standing manner or angle of inclination to be the flat manner of 5 ~ 60 °.
9. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 8, it is characterized in that, the angle of inclination of described flat manner is 15 ~ 30 °.
10. the treatment process of reverse osmosis concentrated water in urban sewage recycling process according to claim 1, it is characterized in that, described in step (2), feed pressure is 0.015 ~ 0.025MPa, and described crossflow velocity is 0.7 ~ 0.9m/s.
In 11. urban sewage recycling processes according to claim 5, the treatment process of reverse osmosis concentrated water, is characterized in that, the length of single hollow fiber form assembly is 50 ~ 150cm, and the packing factor of single hollow fiber form assembly is 30 ~ 70%.
In 12. urban sewage recycling processes according to claim 11, the treatment process of reverse osmosis concentrated water, is characterized in that, the length of single hollow fiber form assembly is 80 ~ 100cm, and the packing factor of single hollow fiber form assembly is 40 ~ 60%.
In 13. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, in step (3), the vacuum tightness of hydrophobic film module permeate side is 0.06 ~ 0.1MPa.
In 14. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, in step (3), the flux of hydrophobic film assembly film is 10 ~ 40L/m
2h.
In 15. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, described in step (4), cycles of concentration is 15 ~ 35 times.
In 16. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, described in step (4), the pH regulator of the dense water of membrane distillation is 8.5 ~ 9.0.
In 17. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, in step (4), the residence time of gravity separator is 15 ~ 120min.
The treatment process of reverse osmosis concentrated water in 18. urban sewage recycling processes according to claim 1, it is characterized in that, the organic film material of the microfiltration membrane unit membrane assembly in step (5) adopt in polysulfones, polyolefins or polyvinylidene difluoride (PVDF) class one or more, membrane pore size is 0.1 ~ 0.3 μm.
The treatment process of reverse osmosis concentrated water in 19. urban sewage recycling processes according to claim 1, it is characterized in that, can realize in the automatic operational process of the microfiltration membrane unit membrane assembly in step (5) disperseing to wash, strengthen washing and soak the periodical operation washed, wherein dispersion is washed and can be realized two ends alternately water inlet, and the water inlet cycle is respectively 15 ~ 30 minutes; Backwashing time is 60 ~ 120 seconds; The operating flux of microfiltration membrane unit is 85 ~ 180L/ (m
2h).
In 20. urban sewage recycling processes according to claim 1, the treatment process of reverse osmosis concentrated water, is characterized in that, the spraying dry unit in step (6), and kiln temperature in is 200 ~ 250 DEG C, and kiln temperature out is 90 ~ 100 DEG C.
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| CN109499388A (en) | 2010-05-21 | 2019-03-22 | Z纳米有限责任公司 | Self assembly surfactant structure |
| CN106237649B (en) * | 2016-07-27 | 2019-03-26 | 大唐环境产业集团股份有限公司 | A kind of membrane distillation crystallization treatment device and method |
| CN108726636A (en) * | 2018-06-04 | 2018-11-02 | 中广核工程有限公司 | A kind of method and system of membrane distillation processing waste water |
| CN108975546B (en) * | 2018-09-25 | 2024-05-28 | 浙江金龙自控设备有限公司 | Fine filtering device for high-temperature water injection |
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