CN100450946C - Printing and dyeing waste water treatment method based on film technology - Google Patents
Printing and dyeing waste water treatment method based on film technology Download PDFInfo
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- CN100450946C CN100450946C CNB2007100086430A CN200710008643A CN100450946C CN 100450946 C CN100450946 C CN 100450946C CN B2007100086430 A CNB2007100086430 A CN B2007100086430A CN 200710008643 A CN200710008643 A CN 200710008643A CN 100450946 C CN100450946 C CN 100450946C
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Abstract
The invention discloses a disposing method of textile printing waste water based on film technology involving a waste water disposing method, which comprises the following steps: adjusting pH and COD value of integrated waste water; pumping into flocculate tank; adding into flocculant; pumping into flocculating setting vessel; getting clarified solution; pumping into membrane biological reactor; proceeding biological treatment; getting dialysate; pumping into counter osmotic separating system; proceeding counter osmotic separation; getting reverse osmosis dialysate; recycling; making concentrated liquid flow into oxide adsorbing tank; refluxing into flocculating setting disposal process; proceeding twice flocculating setting dispose; reaching to two grade emission standard; discharging the eligible reverse osmosis dialysate; adding ClO2 to oxide ineligible reverse osmosis dialysate; adsorbing with activated char; adjusting pH value with alkali liquor; depositing in storing tank.
Description
Technical field
The present invention relates to a kind of wastewater treatment method, particularly relate to a kind of treatment method of printing and dying wastewater of the middle water reuse based on membrane technique.
Background technology
Textile industry is the traditional mainstay industry of China, generally includes 5 parts such as weaving, printing and dyeing, chemical fibre, the manufacturing of clothing and textile specific equipment.Along with fast development of national economy, the dyeing industry of China has also entered high-speed development period, and equipment and state of the art obviously promote, and production technique and equipment are brought in constant renewal in and regenerated, and the especially private printing and dyeing enterprise development of printing and dyeing enterprise is very rapid.Dyeing and printing process refers in process of production all kinds of textile materialss (fiber, yarn, fabric) be carried out physics and chemically treated general name, comprises pre-treatment, dyeing, stamp and back arrangement process to textile materials, is referred to as dyeing and printing process.
Along with the development of printing and dyeing industry, its factory effluent has become one of current topmost pollution source of water body.Printing and dyeing are as the characteristics of the important source of pollution of environment, at first be that contamination level is big, the annual production of world's printing and dyeing at present is about 80～900,000 tons, and China's printing and dyeing annual production reaches 150,000 tons, occupy prostatitis, the world, in printing and dyeing are produced and used, have 10%～15% printing and dyeing component to enter environment approximately with waste water.Printing and dyeing industry of China and textile printing and dyeing industry prosperity, dyeing waste water is even more serious to the pollution of environment, and according to the data of environment communique in 1998, China's industrial wastewater treatment rate is about 87.4% at present, administers qualification rate and only handles 63% of total amount for existing device.The secondth, as many, the complex structure of printing and dyeing kind of environmental pollutant.The synthetic printing and dyeing that the whole world is used reach kind more than 30,000, and the printing and dyeing more than 80% are the complex organic compound that contains azo bond, poly aromatic nucleus.Printing and dyeing industry is one of extremely serious industry of environmental pollution in the chemical industry, and dyeing waste water colourity is big; The organic concentration height, the component complexity; Recalcitrant substance is many; Contain a large amount of inorganic salt, sulfide etc., belong to unmanageable trade effluent.Remove because the printing and dyeing molecule has complicated aromatic hydrocarbon molecular structure and is difficult to more, this is in water surrounding or in illumination with stable existence under the condition of oxygenant is arranged when manufacturing and designing for these structures.The 3rd is that most printing and dyeing are poisonous hardly degraded organic substance, and chemical stability is strong, has carcinogenic, teratogenesis and mutagenic " three cause " effect.Even printing and dyeing component concentration remaining in the waste water is very low, enters water body and also can cause the water body transmittance to reduce the destruction that causes water ecosystem.Therefore, dyeing waste water effectively is treated as important problem.
The water quality of dyeing waste water have Pollutant levels height, kind many, contain characteristics such as poisonous objectionable constituent and colourity height, at present both at home and abroad in this class wastewater treatment treatment process commonly used mainly contain multiple treatment technologies such as physics method, chemical method, biological process.
1. physics method
Mainly comprise methods such as absorption (air supporting) method, membrane separation process, supersonic gas vibrating method.What application was maximum in physical treatment process is absorption method.At present, the external main active carbon adsorption that adopts, this method is very effective to dissolved organic matter in the removal water, but it can not remove colloid and hydrophobicity printing and dyeing in the water, and water-soluble printing and dyeing such as positively charged ion printing and dyeing, direct printing, acid printing and dyeing, active printing and dyeing are had absorption property preferably.Newborn MnO
2To the absorption accords with Langmuir adsorption isotherm of tropeolin-D, adsorption rate is big, can make the tropeolin-D percent of decolourization reach 99%.The adsorbed gas float glass process is exactly printing and dyeing ion and other soluble substances of at first using in powdery inorganic adsorbent (as wilkinite, kaolin etc.) the absorption waste water of some high dispersing, add gas floatation agent then, change it into hydrophobic particle, remove by air supporting, clearances such as acidity printing and dyeing, positively charged ion printing and dyeing and direct printing are reached more than 92%.The membrane technique that is applied to treatment of dyeing wastewater mainly contains ultra-filtration and reverse osmosis.The ultra-filtration technical finesse contains and disperses the decolorizing printing and dyeing waste water rate is 80%～97%, and the TOC clearance is 60%～85%.The clearance of reverse osmosis method dissolved solids reaches 85%～99%, and the printing and dyeing average recovery rate is 75%～85%.
Can make ultrasonic technology become the effective ways of wastewater treatment by control frequency of ultrasonic and saturated gas.Nine divisions of China in remote antiquity, Zhangjagang City fine chemistry industry station-service is according to the FBZ sewage treatment equipment treatment of dyeing and printing of supersonic gas vibrating technical project, and the colourity average removal rate is 97%, COD
CrClearance is 90.6%, and gross contamination load reduction rate is 85.9%.
2. chemical method
Chemical method mainly comprises methods such as chemical coagulation process, chemical oxidization method, photochemical catalysis oxidation style, electrochemical process.Chemical coagulation process is the common method of treatment of dyeing and printing, once is considered to one of effective, the most most economical decolouring technology.Used coagulating agent can be divided into inorganic coagulant, multifunctional efficient compound coagulant, organic polymer coagulating agent etc. at present.Once with coagulating agent such as ferrous sulfate, polymerize aluminum chlorides active dyeing waste water coagulating treatment was studied, the result shows that ferrous sulfate is the optimal coagulation agent, and the clearance of colourity can reach 75% to 94% respectively.Chemical oxidization method is one of main method of decolorizing printing and dyeing waste water, is to utilize the various oxidation means chromophoric group of will printing and dyeing to destroy and decolour.Press the different of oxygenant and oxidizing condition, chemical oxidization method can be divided into ozone oxidation method, deep oxidation method.The photochemical catalysis oxidation style developed rapidly in recent years as a kind of deep oxidation technology of degradation of organic substances.Zhang Guilan (Zhang Guilan, the degraded of dye wastewater in open rotation photo catalysis reactor, textile journal, 2005,26 (3), 109-111) make the dyeing waste water of degrading in this way obtain good decolorizing effect.Electrochemical process is by electrode reaction dyeing waste water to be purified.Micro-electrolysis method is to utilize iron-carbon filling material to corrode in electrolyte solution to form the electrochemical techniques that countless small galvanic cells are handled waste water, and it is that multiple physics chemical action such as a kind of current collection is separated, coagulation, electricity flocculation, absorption are in the method for wastewater treatment of one.In treatment process of dyeing and printing, the printing and dyeing molecule is adsorbed to carbon surface earlier, and oxidation or reduction reaction take place at the two poles of the earth then.Also can utilize electrode to carry out electrolysis, Jia Jin equality (Jia Jinping, Shen Zhemin, Wang Wenhua, the present situation of waste water containing dye treatment process and progress, 2000,19 (1), 26-29) utilize the over-all propertieies such as conduction, absorption, catalysis, redox and air supporting of electrode to realize absorption-electrode reaction-flocculation desorption one continuous line technology with activated carbon fiber as electrode, percent of decolourization reaches 98%, COD
CrClearance is greater than 80%.Also have other many employing electrochemical processes to handle the report that contains dyeing waste water simultaneously.
3. biochemical process
The dyeing waste water biodegradability is poor, can be by improving active sludge MLSS and improving the sludge activity biochemical property or select for use high-efficiency strain to improve biochemical effect if want to adopt biochemical process to handle.Wherein seed selection and the good decolouring flora of cultivation are important development directions of biochemical process.Carry out utilizing technology such as selection by mutation, protoplastis fusion, genetically engineered abroad, set up the research of the efficient printing and dyeing decolouring engineering bacteria that has a plurality of plasmids.Studies show that in recent years, dominant bacterias such as false single-cell bacteria, sphaerotilus natans bacterium, Arthrobacter, withered grass bacterium, oxidation yeast have suitable effect to the printing and dyeing degraded.
Though above-mentioned the whole bag of tricks all has good treatment effect, also there is following problem.
Aspect materialization, though gac has the characteristics of advantages of good adsorption effect, the regeneration of activated carbon difficulty, the cost height is restricted its application.The sorbent material that many enterprises turn to other low prices, material to be easy to get respectively.Though electrolytic process, oxidation style have certain effect in the colourity of removing dyeing waste water, often the COD removal is unsatisfactory, and the cost of handling medicament is also higher relatively, and many novel oxidation means also are in experimental study stage, not industrialization.
Aspect biochemical, printing and dyeing are typical fine chemical products, characteristics with short run and many kinds, its complex structure, Production Flow Chart is long, expect that from former finished product often is attended by unit operations such as nitrated, condensation, reduction, oxidation, diazotization, coupling, by-product should be many, and product yield is low, the wastewater through organic matter complicated component, process operations such as printing and dyeing are produced chemical reaction process and separated, make with extra care, washing all are to be solvent with water, and water consumption is big.Though the biochemical process treatment of dyeing and printing has the advantage of less investment, but still there is the difficult dyeing waste water that adapts to of microorganism, shortcoming such as variation water quality is big, toxicity is big, and have problems such as the processing of biogas of sludge disposal, anaerobism section and complex management.Treatment of dyeing wastewater adopts single treatment process often to be difficult to get a desired effect.Conventional method is with the way of each treatment process combination, exists technical process long, running cost height, defectives such as effluent characteristics instability.
Summary of the invention
The object of the invention is at existing a series of problems in the existing treatment method of printing and dying wastewater, providing a kind of combines with dyeing waste water conventional processing technology based on membrane technique, low cost, high-effect, the treatment method of printing and dying wastewater of the secondary discharge standard of water reuse in making it to reach.
The present invention includes following steps:
1. filter: will be stored in dyeing waste water in the waste water basin and sanitary wastewater (20～25) by volume: 1 mixes after slag filters filter, removes suspended substance wherein, filtered liquid store in the comprehensive pond of waste water comprehensive wastewater.
2. comprehensive adjustment: measure the pH and the COD value of comprehensive wastewater, regulating its pH value is 6～9, and the COD value is 2000～4000mg/L.
3. flocculating settling: comprehensive wastewater is pumped in the flocculation jar, add and pump into the interior sedimentation of flocculating settling container (settling bowl or slurry tank etc.) after 3 kinds of different flocculation agents mix and get clear liquor, the add-on of flocculation agent must be as the criterion less than 1600mg/L with the COD of clear liquor behind flocculating settling, the sewage of the sediment in the flushing flocculating settling pond pumps into sand filtration in the sewage sand filter, and filtrate enters the circulation of comprehensive pond.
4. biochemical treatment: the clear liquor behind the flocculating settling is pumped into membrane bioreactor system carry out biochemical treatment and get dialyzate, the microfiltration membrane that membrane bioreactor adopts is that the aperture is hollow-fibre membranes such as the polyvinylidene difluoride (PVDF), polyethersulfone, cellulose acetate of 0.1～0.4 μ m.
5. reverse osmosis isolation: the dialyzate of membrane bioreactor gained is pumped into the reverse osmosis isolation system carry out reverse osmosis isolation and get the reverse osmosis dialyzate, the reverse osmosis dialyzate carries out the middle water reuse of FEOL, concentrated solution flows into the oxidation adsorption tank and handles, and concentrated solution passes back into the flocculating settling treatment process to carry out the secondary flocculating settling and handle and reach the secondary discharge standard discharging.
6. oxidation and adsorption bleaching: will enter the reverse osmosis dialyzate sampling analysis in the oxidation adsorption tank, eligible directly discharges.The failure adds the ClO of reasonable amount
2Oxidation is regulated pH to 6～9 through the charcoal absorption processing and with alkali lye, fully precipitation clarification in storagetank.
7. detect and discharging: will be through oxidation and absorption and after testing through the reverse osmosis waste water of precipitation process, meet the discharging of sewage second-level emission standard (GB8978-96) back.
In step 2, described comprehensive adjustment can add the waste water of alkali lye or low COD and regulate its pH value and COD.In step 3, before flocculating settling is handled, to get the waste water sample and carry out lab scale with 3 kinds of flocculation agents respectively, thereby determine the flocculation agent kind selected for use, flocculation agent is selected from ferrous salt, sodium polyacrylate, polyaluminium sulfate.In step 4, the oxygen+aerobic treatment process of holding concurrently is adopted in biochemical treatment, and aerobic treatment process adopts activated sludge process.When bringing into operation, in the aeration tank, be full of earlier sewage, add bacterial classification mud and carry out aeration, turn out active sludge.After producing active sludge, will be through satisfying the waste water that biological treatment water quality requires after the suitable pre-treatment, and enter the aeration tank after returned sluge mixes, and in the pond abundant aeration.The water outlet of Aerobic Pond method enters reaction tank through post precipitation, and mud is back to Aerobic Pond in the aerobic settling bowl.In step 5, the reverse osmosis membrane that the reverse osmosis isolation system adopts is preferably the polyamide membrane of 99.8% magnesium sulfate rejection rate.The treatment method of printing and dying wastewater of this membrane technique also comprises an anti-load impact part, and it is made up of technologies such as oxidation and adsorption bleachings and (sees step 6).
The present invention is made up of three parts, and first part promptly filters, the pre-treatment part of mixing, oxidation and coagulant precipitation.This part can be decomposed sedimentation and be removed most of mud, organism and salt, and the COD index is reduced to below the 1600mg/L by 2000～4000mg/L, can move steadily in the long term to guarantee film system (second section).Second section is the core of technical process, be membrane bioreactor and reverse osmosis part, membrane bioreactor system is further removed the macromolecular colloid material, guaranteeing that reverse osmosis system further removes small molecules COD material and pigment that oxidation, coagulation are difficult to remove, thereby make the waste water quality of processing reach the secondary discharge standard of national regulation.In addition, the present invention also has one to be the oxidation absorbing process that is provided with when the waste water impact load occurring, and the waste water of discharging is reached within the secondary discharge standard of national regulation all the time.
The outstanding advantage that the present invention has is: the water treatment effect that has both overcome conventional dyeing waste water method is undesirable, discharges little critical defect up to standard, has overcome single with film processing or the too high defective of adsorption treatment cost again.
Description of drawings
Fig. 1 is the process flow diagram of the embodiment of the invention
Embodiment
Fig. 1 provides the process flow diagram of the embodiment of the invention, the present invention is a treatment process design of finishing its dyeing waste water after the comparative study of composition, character and the existing processing scheme of dyeing waste water being goed deep into system, and waste water is by 7 unit combination utilizations such as grid wastewater equalization pond, flocculation hybrid reaction jar, settling bowl, membrane bioreactor cycling element, reverse osmosis cycling element, adsorption bleaching unit and system's electrical control units.Thereby form a kind of very difficult treatment method of printing and dying wastewater and device up to standard of sewage water treatment method routinely that be particularly suitable for.
Be stored in dyeing waste water in the waste water basin 1 and sanitary wastewater (20～25) by volume: 1 mixes after filter in slag filter tank 2, removes suspended substance wherein, filtered liquid store in the comprehensive pond 3 of waste water comprehensive wastewater.Measure the pH and the COD value of comprehensive wastewater, regulating its pH value is 6～9, and the COD value is 2000～4000mg/L.Comprehensive wastewater is pumped in the flocculation jar 14, add and pump into after 3 kinds of different flocculation agents mix that sedimentation gets clear liquor in the flocculating settling pond 5 in flocculation agent configured slot 4, the add-on of flocculation agent must be as the criterion less than 1600mg/L with the COD of clear liquor behind flocculating settling, the sewage of the sediment in the flushing flocculating settling pond pumps into sand filtration in the sewage sand filter, and filtrate enters the circulation of comprehensive pond.Clear liquor behind the flocculating settling is pumped into membrane bioreactor system 7 carry out biochemical treatment and get dialyzate, the microfiltration membrane that membrane bioreactor adopts is that the aperture is hollow-fibre membranes such as the polyvinylidene difluoride (PVDF), polyethersulfone, cellulose acetate of 0.1～0.4 μ m.The dialyzate of membrane bioreactor gained is pumped into reverse osmosis isolation system 6 to carry out reverse osmosis isolation and gets the reverse osmosis dialyzate, the reverse osmosis dialyzate carries out the middle water reuse of FEOL, concentrated solution flows into oxidation pond system 11 and handles, the oxidation pond system comprises oxidation pond 11A, adsorption tank 11B and storagetank 11C, and concentrated solution passes back into the flocculating settling treatment process to carry out the secondary flocculating settling and handle and to reach the secondary discharge standard discharging.With the reverse osmosis dialyzate sampling analysis that enters among oxidation pond 11A and the adsorption tank 11B, eligible directly discharges.The failure adds the ClO of reasonable amount
2Oxidation is regulated pH to 6～9 through the charcoal absorption processing and with alkali lye, fully precipitation clarification in storagetank 11C.Will be through oxidation and absorption and after testing through the reverse osmosis waste water of precipitation process, meet the discharging of sewage second-level emission standard (GB8978-96) back.
The adjusting of wastewater pH can be carried out in pH regulator pond 13.Before flocculating settling is handled, to get the waste water sample and carry out lab scale with 3 kinds of flocculation agents respectively, thereby determine the flocculation agent kind selected for use, flocculation agent is selected from ferrous salt, sodium polyacrylate, polyaluminium sulfate.Biochemical treatment can be adopted double oxygen+aerobic treatment process, and aerobic treatment process adopts activated sludge process.When bringing into operation, in the aeration tank, be full of earlier sewage, add bacterial classification mud and carry out aeration, turn out active sludge.After producing active sludge, will be through satisfying the waste water that biological treatment water quality requires after the suitable pre-treatment, and enter the aeration tank after returned sluge mixes, and in the pond abundant aeration.The water outlet of Aerobic Pond method enters reaction tank through post precipitation, and mud is back to Aerobic Pond in the aerobic settling bowl.The reverse osmosis membrane that the reverse osmosis isolation system adopts is preferably the polyamide membrane of 99.8% magnesium sulfate rejection rate.
Below provide the concrete operations operation.
1. filter
1. clear way valve V01 (or V02), V03 and V04, ejector priming P01, the impact flow velocity in the time of should preventing to start shooting after stable dashes filtering layer, destroys filtering layer.
2. when filtering flow velocity, answer variable valve to make liquid level, prevent to overflow all the time a little less than the filter tank bead less than the flow of pump.
3. according to the equalizing tank ratio requirement, need stop press filtration water enters, when changing composite wastewater, stop pump P01, shut-off valve V01 (or V02) opens 50% aperture with valve V07, ejector priming P02, when stable back clear way valve V07 (purpose is that the impact flow velocity when preventing to start shooting dashes filtering layer the destruction filtering layer).
4. when slag filter tank 2 quits work, at first close pump P01 and P02, close all valves then.
5. when filtering flow velocity, change to another filtering basin work less than the flow handled.
6. blocked filter tank is stopped using, and oozes drop, scrapes off mud and blocked filtering layer after making sewage dehydration, sends to burning.The filter tank replenishes new＜2mm particle diameter cinder.
2. comprehensive adjustment
1) volume in pH regulator pond 13 is determined
1. measure the long 4.6m in low level pond * wide 3.2m * high 1.9m, by every 1m
3In the pond, do scale mark on the easy observed metope.
2. measure slag (sand) filter tank 2 total areas, by every 1m
3Continuation is done scale mark on former scale parallel direction.
2) COD index preparation
1. according to the highest COD index in pH regulator pond 13, go into press filtration waste water and comprehensive wastewater (at first by preparation in 1: 3) by 2 filters of slag filter tank respectively.
2. open valve V09, ejector priming P03 enters and mixes 15min.
3. sampling send analyzer room 12 to measure the COD index after mixing 15min.
3. flocculating settling
1) flocculation
(1) flocculation agent Preparation tank 4 volumes and mark are determined: the long 2.4m of measuring reservoir * wide 1m * high 1.2m, do scale mark on the easy observed side by every 40L in the pond.
(2) 10% flocculation agents preparation: open valve V33, in flocculation agent Preparation tank 4, add 1.8m
3No salt solution, open pump P04 and stir, add the 200kg flocculation agent then, stop pump P04 after stirring 30min, flocculation agent is stand-by.
(3) coagulation operating procedure flocculation:
1. open valve V08, shut-off valve V09, ejector priming P03 feed adjustment pond waste water when flocculation jar 14 internal volumes reach 50%, starts agitator and stirs.
2. continue feed adjustment pond waste water to a little less than in the jar during bead, stop to stir, calculate a waste water actual volume (this volume will be for preparing the benchmark of flocculation agent from now on) in the flocculation jar.
3. start and stir, open valve V10, put into 10% flocculation agent by 5%, close V10 after finishing, pour 10% coagulant aids (when needing) into by 0.1% according to the actual waste water volume according to a flocculation jar interior actual waste water volume.
4. continue to stir to shut down behind the 15min and stir, every batch of first jar of sampling send the laboratory to do sedimentation and COD, colorimetric detection.
5. open valve V11, ejector priming P05 sends the flocculation jar interior good waste water of coagulation into settling bowl 5.
6. after waste water is all squeezed into settling bowl 5, close pump P05,1. shut-off valve V11 repeats～5., and measures the adjustment of making the flocculation agent addition according to analyzer room 12.
2) sedimentation
(1) control of coagulant precipitation and suspended substance:
1. the waste water behind the coagulation flows in the process of outlet step by step through overflow port, the sludge settling situation in the waste water in the claire, when effect of settling occurring when not good, in time adjust flocculation blended ratio, to satisfy settled effect.
When 2. foreign material such as oils, external suspended substance appear in the waste water surface, be in time in advance to remove.
3. the waste water of discharging from settling bowl 5 outlets is answered clear, is not had muddy, suspended matter.
4. according to membrane bioreactor 7 transit dose variable valve V12 apertures the waste water in the membrane bioreactor 7 is in all the time near the canful state.
(2) spoil disposal technology:
1. when the sludge quantity in certain pond reaches 1/2 liquid level in the pond, open the mud valve V13 (or V14, V15) of this bottom, pond, variable valve V16 enters in the sand filter mud, flow is as the criterion not dashed sand bed, when penetrating, the full pond of mud in the sand filter or waste water closes mud valve V13 (or V14, V15), open another mud valve V14 (or V13, V15), by that analogy.
2. when spoil disposal speed can not satisfy sedimentation and needs the sludge discharged amount, the contaminated obstruction of filtering layer of sand filter be described, cause ability drop, drain the back in time interior mud of cleaning sand filter and blocked filtering layer.
4. biochemical treatment (using membrane bioreactor 7)
1) membrane bioreactor operating procedure
(1) opens valve V39, start gas blower P12, regulate the flow of air compressor machine, make the air pump flow reach 50m
3/ h (amount of looking dissolved oxygen in the membrane bioreactor is determined).
(2) open valve V12, start import pump P06, make pump P06 in 40s, be raised to 30Hz automatically by 0Hz, stable back variable valve V12, (looking percolate flux and reverse osmosis system needs feed rate to determine), the feed liquor flow reaches 52m
3/ h.
(3) open valve V21, start outlet pump P11, make pump P11 be raised to 30Hz automatically by 0Hz in 40s, stable back variable valve V21 makes the effluent liquid flow reach 51.5m
3/ h.
(4) open valve V38, start sludge pump P10, make pump P10 be raised to 30Hz automatically by 0Hz in 40s, stable back variable valve V38 makes spoil disposal effluent liquid flow reach 0.5m
3/ h.(0.5m there is this moment
3The flow of/h flows out to settling bowl from valve V38 outlet).
(5) variable valve V12 and V21 repeatedly under the constant prerequisite of pressure when percolate flux needs feed rate less than reverse osmosis, improve the assembly top hole pressure and make it satisfied.
Stop pump P06 when (6) shutting down, pump P11, pump P10, pump P12 close V12, V21, V38 and V39, open V20 and V17, and ejector priming P06 and pump P11 are raised to 30Hz automatically by 0Hz in 40s.Take out when causing 1/4 liquid level when water in the CIP jar 10, shutdown is awaited orders.Open no brine valve V23, be full of CIP jar 10.
(7) close all valves.
Annotate: when not working more than one day, the film system will carry out matting, and protects with protective material.
2) cleaning operation technology
(1) when film system percolate flux can not satisfy the feed rate of reverse osmosis system needs, the film system entered the cleaning state.
(2) the total volume of water of mensuration system: all water in the emptying system, close all valves, in CIP jar 10, fill it up with deionized water, open valve V20, V17 and V23, ejector priming P06 makes pump P06 be raised to 30Hz automatically by 0Hz in 40s.Liquid levels descend in the CIP jar 10 at this moment, measure falling head and CIP jar 10 volumes, calculate total volume of water, before moisturizing extremely detects liquid level build-up in the CIP jar 10.
(3) the consoluet LC-01# clean-out system of the total volume of water 1% of adding system in CIP jar 10, wash cycles 20～40min.
(4) when flux recovers, finish to clean.When flux can not return to 85% when above of new membrane flux, scavenging period arrives 40min, opens valve V18, with the water in the CIP jar 10 with cleaning fluid discharge to settling bowl, moisturizings in time in the CIP jar 10 keep water level in the CIP jar.
(5) shut-off valve V18 slowly adds the LC-07# clean-out system in the CIP jar, control pH value is 2, wash cycles 40min, and operating parameters is constant.
(6) return to 85% when above of new membrane flux when cleaning the back percolate flux, open valve V18, clean-out system is discharged into settling bowl with the water in the CIP jar, moisturizings in time in the CIP jar 10, maintenance CIP jar 10 interior water levels, shutdown is awaited orders.
Annotate: when not working more than one day, enter film protection technology and carry out the film system protection.
3) film protection operating procedure
(1) the longest is 3 days (weekend)---according to total hold-up, with 0.1%w/w (lg/L) the sodium metabisulfite solution 15min that under 10～25 ℃ of conditions, circulates.
(2) the longest is 30 days (one month)---according to total hold-up, with 0.25%w/w (lg/L) the sodium sulfite solution 15min that under 10～25 ℃ of conditions, circulates.
(3) the longest is that 12 months (1 year) or equipment may be in freezing conditions any shutdown of following time (state in winter)---0.25%v/v Proxel Gxl (Zeneca Biocides produces) solution (2.5ml/L) adds the glycerine (98% SILVER REAGENT) of 18%v/v (180ml/L) again.When mixing fully, be adjusted to pH value 4.5～5.0 with dilute sulphuric acid or citric acid, 60min circulates under 10～25 ℃ of conditions.
(4) the same cleaning parameters of operating parameters stops pump P06 after operation is finished, and closes all valves.
5. reverse osmosis
1) reverse osmosis operating procedure
(1) open valve V25, V22, V27 and V28, ejector priming P07, after operating steadily, ejector priming P08 makes pump P08 be raised to 30Hz automatically by 0Hz in 40s.
(2) stable back variable valve V27 and frequency make the assembly intake pressure reach 18～20bar, and concentrated solution discharge reaches 20～24m
3/ h.
(3) variable valve V26 and V27 repeatedly under the constant prerequisite of pressure make concentrated solution discharge reach 23.7m
3/ h (has 0.3m this moment
3The flow of/h flows out to settling bowl from valve V26 outlet).
(4) when percolate flux during, should clean less than initial percolate flux 50%.
Stop pump P08 and P07 when (5) shutting down, close V25, V22 and V27, open V24 and V26, ejector priming P07, when water was evacuated to 1/4 liquid level in the CIP jar 10, shutdown was awaited orders.
(6) open no brine valve V23, be full of the CIP jar.
(7) close all valves.
Annotate: when not working more than one day, the film system will carry out matting, and protects with protective material.
2) cleaning operation technology
(1) when film system percolate flux less than initial flux 50% the time, enter the cleaning state.
(2) the total volume of water of mensuration system: all water in the emptying system, close all valves, in the CIP jar, fill it up with deionized water, open valve V24, V27 and V26, ejector priming P07, the back ejector priming P08 that operates steadily makes pump P08 be raised to 30Hz automatically by 0Hz in 40s.This moment, the CIP tank level descended, and measured falling head and CIP tank volume, calculated total volume of water, before moisturizing returns to detection with the CIP tank level.
(3) stable back variable valve V27 and frequency make the assembly intake pressure reach 6bar, and concentrated solution discharge reaches 52m
3/ h.
(4) the consoluet LC-01# clean-out system of the total volume of water 1% of adding system in the CIP jar, wash cycles 20～40min.
(5) when flux recovers, finish to clean.When flux can not return to 85% when above of new membrane flux, scavenging period arrives 40min, opens valve V26, with the water in the CIP jar clean-out system is discharged into settling bowl 5, and moisturizing in time in the CIP jar keeps the interior water level of CIP jar.
(6) shut-off valve V26 slowly adds the LC-07# clean-out system in the CIP jar, control pH value is 2, wash cycles 40min, and operating parameters is constant.
(7) return to 85% when above of new membrane flux when cleaning the back percolate flux, open valve V26, clean-out system is discharged into settling bowl with the water in the CIP jar, moisturizing in time in the CIP jar, the interior water level of maintenance CIP jar, shutdown is awaited orders.
Annotate: when not working more than one day, enter film protection technology and carry out the film system protection.
3) film protection operating procedure
(1) protective material concentration and working time same ultrafiltration system.
(2) the same cleaning parameters of operating parameters stops pump P08 and P07 after operation is finished, and closes all valves.
In the reverse osmosis isolation system, can adopt reverse osmosis circulation tank 8.
6. oxidation and adsorption bleaching
1) oxidation
(1) in oxidation tank 9, adds 10% oxygenant.When needing with addition of consoluet 0.5% pro-oxygenic agent.
(2) open valve V31 and calculate adjusting proportioning flow through flow quantity and analyzer room's analysis proportioning according to reverse osmosis.
(3) shut-off valve V31 when reverse osmosis system is shut down.
(4) sampling analysis index and carry out source recording in the 3rd pond.
2) adsorption bleaching
(1) in adsorption tank 11B, adds the 10Kg granulated active carbon.
(2) will send into the adsorption tank 11B that granulated active carbon is housed through the waste water of oxide treatment and carry out adsorption bleaching.
3) the pH value is regulated
(1) liquid caustic soda of allotment 10% concentration in the liquid caustic soda jar.
(2) when the full pond of storage pool the 3rd lattice waste water, the pH value is surveyed in sampling, allocates ratio measuring and is mixed.
7. detect and discharging
1) sampling and measuring checking waste water ph, COD and colourity.
2), meet the discharging of sewage second-level emission standard (GB8978-96) back through oxidation and adsorption treatment.Mud is pressed the technological operation of settling bowl spoil disposal.
Claims (7)
1. treatment method of printing and dying wastewater based on membrane technique is characterized in that may further comprise the steps:
1) filter: will be stored in dyeing waste water in the waste water basin and sanitary wastewater (20～25) by volume: 1 mixes after slag filters filter, removes suspended substance wherein, filtered liquid store in the comprehensive pond of waste water comprehensive wastewater;
2) comprehensive adjustment: measure the pH and the COD value of comprehensive wastewater, regulating its pH value is 6～9, and the COD value is 2000～4000mg/L;
3) flocculating settling: comprehensive wastewater is pumped in the flocculation jar, add and pump into after 3 kinds of different flocculation agents mix that sedimentation gets clear liquor in the flocculating settling container, the add-on of flocculation agent must be as the criterion less than 1600mg/L with the COD of clear liquor behind flocculating settling, the sewage of the sediment in the flushing flocculating settling pond pumps into sand filtration in the sewage sand filter, and filtrate enters the circulation of comprehensive pond;
4) biochemical treatment: the clear liquor behind the flocculating settling is pumped into membrane bioreactor system carry out biochemical treatment and get dialyzate, the microfiltration membrane that membrane bioreactor adopts is that the aperture is polyvinylidene difluoride (PVDF), polyethersulfone or the cellulose acetate hollow-fibre membrane of 0.1～0.4 μ m;
5) reverse osmosis isolation: the dialyzate of membrane bioreactor gained is pumped into the reverse osmosis isolation system carry out reverse osmosis isolation and get the reverse osmosis dialyzate, the reverse osmosis dialyzate carries out the middle water reuse of FEOL, and concentrated solution flows into the oxidation adsorption tank and handles;
6) oxidation and adsorption bleaching: will enter the concentrated solution sampling analysis in the oxidation adsorption tank, eligible directly discharges, and the failure adds the ClO of reasonable amount
2Oxidation is regulated pH to 6～9 through the charcoal absorption processing and with alkali lye, fully precipitation clarification in storagetank;
7) detect and discharging: will be through oxidation and absorption and after testing through the reverse osmosis waste water of precipitation process, discharge after meeting the sewage second-level emission standard.
2. a kind of treatment method of printing and dying wastewater based on membrane technique as claimed in claim 1 is characterized in that in step 2, and described comprehensive adjustment adds the waste water of alkali lye or low COD and regulates its pH value and COD.
3. a kind of treatment method of printing and dying wastewater based on membrane technique as claimed in claim 1 is characterized in that in step 3, before flocculating settling is handled, gets the waste water sample and carries out lab scale with 3 kinds of flocculation agents respectively, determines the flocculation agent kind of selecting for use.
4. as claim 1 or 3 described a kind of treatment method of printing and dying wastewater, it is characterized in that in step 3, flocculation agent is selected from ferrous salt, sodium polyacrylate or polyaluminium sulfate based on membrane technique.
5. a kind of treatment method of printing and dying wastewater based on membrane technique as claimed in claim 1 is characterized in that in step 4, and the oxygen+aerobic treatment process of holding concurrently is adopted in biochemical treatment, and aerobic treatment process adopts activated sludge process.
6. a kind of treatment method of printing and dying wastewater based on membrane technique as claimed in claim 5 is characterized in that described biochemical treatment is when bringing into operation, and is full of earlier sewage in the aeration tank, adds bacterial classification mud and carries out aeration, turns out active sludge; After producing active sludge, will be through satisfying the waste water that biological treatment water quality requires after the suitable pre-treatment, and enter the aeration tank after returned sluge mixes, and in the pond abundant aeration; The water outlet of Aerobic Pond method enters reaction tank through post precipitation, and mud is back to Aerobic Pond in the aerobic settling bowl.
7. a kind of treatment method of printing and dying wastewater based on membrane technique as claimed in claim 1 is characterized in that in step 5, and the reverse osmosis membrane that the reverse osmosis isolation system adopts is the polyamide membrane of 99.8% magnesium sulfate rejection rate.
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| CN102040301B (en) * | 2009-10-19 | 2013-04-17 | 中国科学院生态环境研究中心 | Method for treating municipal waste leachate membrane concentrated solution |
| JP5627322B2 (en) * | 2010-07-15 | 2014-11-19 | 株式会社日立製作所 | Waste water treatment system and waste water treatment method |
| CN102050555B (en) * | 2010-12-24 | 2012-07-25 | 波鹰(厦门)科技有限公司 | Device and method for treating and recycling printing and dyeing wastewater |
| FR2984874B1 (en) * | 2011-12-23 | 2014-01-10 | Degremont | PROCESS FOR TREATING INDUSTRIAL OR URBAN WASTEWATER FOR REUSE, AND INSTALLATION FOR CARRYING OUT SAID METHOD |
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| CN103304054B (en) * | 2013-06-16 | 2015-09-23 | 德州学院 | A kind for the treatment of process of dyeing waste water |
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| CN104829049A (en) * | 2015-04-21 | 2015-08-12 | 南通大恒环境工程有限公司 | Reusing treatment method for printing and dyeing wastewater |
| CN105417896A (en) * | 2016-01-07 | 2016-03-23 | 嘉兴瑞奕环保科技有限公司 | Printing and dyeing wastewater treatment system |
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| CN107857392A (en) * | 2017-11-21 | 2018-03-30 | 合肥创想能源环境科技有限公司 | A kind of method of integrated membrane separation technique processing dyeing waste water |
| CN110713282B (en) * | 2018-07-13 | 2023-10-24 | 中国石油化工股份有限公司 | Laboratory organic waste liquid treatment method and system |
| CN109650659A (en) * | 2019-01-10 | 2019-04-19 | 湖南工程学院 | A kind for the treatment of method of printing and dying wastewater |
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| CN1478737A (en) * | 2003-07-14 | 2004-03-03 | 宜兴鹏鹞阳光环保有限公司 | Garbage percolation liquid treatment process |
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Address after: Xiamen City, Fujian province Jimei 361022 central city Xinglin Sanda Technology Park Patentee after: Suntar Membrane Technology (Xiamen) Co., Ltd. Patentee after: Suntar Membrane Environment Technology Co., Ltd. Address before: Xiamen City, Fujian province Jimei 361022 central city Xinglin Sanda Technology Park Patentee before: Suntar Membrane Technology (Xiamen) Co., Ltd. Patentee before: Suntar(Xiamen) Environmental Engineering Co., Ltd. |
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Effective date of registration: 20121226 Address after: 361022 Fujian province Xiamen City Xinglin central city Sanda Technology Park Patentee after: Suntar Membrane Environment Technology Co., Ltd. Address before: Xiamen City, Fujian province Jimei 361022 central city Xinglin Sanda Technology Park Patentee before: Suntar Membrane Technology (Xiamen) Co., Ltd. Patentee before: Suntar Membrane Environment Technology Co., Ltd. |