CN201864630U - Zero-discharge device for treating printing and dyeing wastewater - Google Patents
Zero-discharge device for treating printing and dyeing wastewater Download PDFInfo
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- CN201864630U CN201864630U CN2010205463581U CN201020546358U CN201864630U CN 201864630 U CN201864630 U CN 201864630U CN 2010205463581 U CN2010205463581 U CN 2010205463581U CN 201020546358 U CN201020546358 U CN 201020546358U CN 201864630 U CN201864630 U CN 201864630U
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Abstract
The utility model provides a zero-discharge device for treating printing and dyeing wastewater. The treatment object is high-concentration and high-salt printing and dyeing wastewater discharged in a quality-divided manner; the system comprises three parts, namely a materializing pretreatment part, an RO (reverse osmosis) desalting system and a concentrated water treatment part, wherein the materializing pretreatment part comprises three parts, namely a coagulation-settlement tank, a sedimentation tank and an UF (ultra filtration) membrane; the RO system is divided into two stages, namely a low pressure RO system and a high pressure RO system; tubular UF fresh water enters the first stage of low pressure RO system, and first stage RO concentrated water enters the second stage of high pressure RO system; first stage RO freshwater and second stage RO freshwater are mixed and serve as the final outlet water of the system, which can be reused in parts of work sections; second stage RO concentrated water enters a membrane distillation system; waste heat of low-concentration water discharged in a quality-divided manner is utilized to distill the concentrated water, so as to acquire saturated solution; and finally, distilled water and solid salt are acquired through condensation and crystallization. The system adopts an energy-saving, environmentally-friendly and low-carbon novel printing and dyeing wastewater treatment process, can achieve zero discharge, and provides a new solving way for treating the high-concentration and high-salt printing and dyeing wastewater.
Description
Technical field:
The utility model belongs to environment protection, field of waste water treatment, the device of particularly a kind of high dense high salt treatment of dyeing wastewater zero release.
Background technology:
Dyeing not only water consumption is big but also be draining rich and influential family in the industry, accounts for 35% of industrial total displacement.What saliferous was the highest in the dyeing waste water is dyeing waste-water, and high salt dyeing waste water accounts for about 20% of Total Water, and salinity accounts for 70%～80% of total salt amount.The dyeing waste water quantity discharged is big, complicated component, and the Pollutant levels height, saltiness is higher simultaneously.In 10,000 tons of waste water, common saliferous 40t～50t, and contain monovalence and divalent salts simultaneously.
The treatment process commonly used of dyeing waste water can be divided into physics method, chemical method and biological process three classes.The physics method mainly contains grid and screen cloth, adjusting, precipitation, air supporting, filtration, membrane technique etc., and chemical method has that neutralization, coagulation, electrolysis, oxidation, absorption, sterilization etc., biological process have anaerobic biological process, aerobe method, the oxygen biological process of holding concurrently.At present, domestic treatment of dyeing wastewater means are aided with physics method and chemical method based on biological process.Because the development and the finishing process in printing and dye-ing development of technology of chemical ﹠ blended fabric make bio-refractory organism such as new dye, PVA slurry, New-type adjuvant enter dyeing waste water in a large number in recent years, have increased difficulty to processing.Original biological treatment system COD clearance mostly drops to about 50% by original 70%, even lower.The removal of colourity is a great problem of treatment of dyeing wastewater, and old biochemical process always can not be satisfactory aspect decolouring.In addition, the ratio that the COD that chemical sizwes such as PVA cause accounts for the total COD of dyeing waste water is quite big, but makes its clearance have only 20%～30% owing to they are difficult to be utilized by common micro-organisms.At the problems referred to above, some research work have all been carried out both at home and abroad.
The cotton dyeing waste water has two essential characteristics: promptly contain high chroma, high chemical oxygen demand, low biochemical oxygen demand (BOD), high pH, the 2nd, have supersalinity, show as high conductivity, at These characteristics, handle high chroma, high chemical oxygen demand, low biochemical oxygen demand (BOD) sewage has been got rid of bio-oxidation scheme commonly used.
The utility model content:
The utility model is applicable to the difficult dyeing waste water of handling high COD content, supersalinity, can remedy the defective that conventional biological treatment is difficult to handle high dense high salt dyeing waste water, can be with the salt simmer down to solid salt in the dyeing waste water, realize the dyeing waste water zero release, and effluent quality is good, can not only be back to the part workshop section of dyeing and printing process, reduce water consumption, and solved the problem that the dense shipwreck of conventional film separating system is handled.The utility model device comprises materialization pre-treatment, RO desalting system and dense water treatment three parts, and the materialization pre-treatment comprises coagulant precipitation 11, settling tank 12 and UF13 three parts.Adopting corrosion-resistant vacuum primingpump M1 directly to get former water from the printing and dyeing workshop streamline cools to equalizing tank 1, and by PAM dosing pump M3, PAC dosing pump M4, discoloring agent dosing pump M5, pH regulator agent dosing pump the M6 agent of adding pH regulator, discoloring agent, PAC, PAM before pump M2 successively, the liquid medicine mixture enters coagulant precipitation jar 11, and supernatant liquor enters in the inclined-plate clarifying basin 12 by overflow weir 18.Feed liquid is further separate and subside in inclined-plate clarifying basin 12, and supernatant liquor is collected the back gravity flow by the perforation header and entered ultrafiltration intermediate water tank 6.Ultra-filtration membrane is selected homemade large-flux anti-pollution tubular ultra-filtration membrane assembly 13 for use, adopts the cross flow filter form, and 10% concentrate recirculation is to equalizing tank 1, all the other dense water outer loop, and the water outlet that accounts for processing requirements 50% enters one-level RO circulation barrels 8.
The RO system divides one, two two-stages, former water enters first-stage reverse osmosis device 14 through security personnel's strainer 20 in the one-level RO circulation bucket, the dense water of first-stage reverse osmosis that accounts for treatment capacity 50% enters secondary high pressure reverse osmosis circulatory pool 9, water inlet as secondary RO system 15, one-level, two-pass reverse osmosis mixing of fresh water enter filtered water tank 10 as system's final outflow water, can be back to use part workshop section; The high dense water of two-pass reverse osmosis that accounts for treatment capacity 25% enters membrane distillation system 16.
Membrane distillation system 16 adopts international advanced porous hydrophobic tubular fibre distillation film, utilizes the low dense water used heat of branch matter discharging to make dense water distillation, obtains saturated solution, finally obtains distilled water and solid salt by condensation and crystallization.
The utility model theoretical foundation:
The utility model adopted chemical coagulation process go to solve high chroma, biodegradability difference sewage colourity is fallen, with the CODcr problem, highrank fuel salinity water has adopted the reverse osmosis membrane desalination, has improved the waste water reclamation rate.To the requirement of particle restriction in the water, before entering RO, increased ultra filtration unit when intaking for satisfying the RO film.
Now to the research of RO with use and known by water treatment field day by day, the construction and the long-term practice operation of many successful desalimtors have proved that this is a technology that reaches its maturity, and are first-selected Technologies so be used to handle highrank fuel salinity water.When adopting the RO technology, the high salinity waste water that carries a large amount of colourities, chemical oxygen demand composition is still a thorny difficult problem, show as the pollution of high-enriched organics to film, the cleaning restorability is limited, causes the film water permeable ability comparatively fast to decay, shorten the work-ing life of film, and cost improves.Therefore the native system pre-treatment reduces the Pollutant levels that enter the RO film as far as possible, and the decay of membrane flux is mainly alleviated in back road according to waterpower cleaning, matting and interpolation Scale inhibitors.
Reduce the organic contamination of follow-up RO film, removal COD, colourity, the turbidity that should try one's best in pre-treatment are energetically created rational staging treating processing condition, and assurance equipment can normally move.At dyeing, that generally uses now has reactive dyestuffs and an intellectual circle's dyestuff, exists with colloid and ionic form in a large number after dyestuff is water-soluble, these colloidal solids are little, have negative charge, many printing and dyeing mills all are that decision uses DYE PRODUCTION in batches according to order, and it is very important to the wastewater treatment relation.These organism are relevant with the pH value of water in the removal water, add the kind of flocculation agent and macromolecular decolorizing agent, dosage and combination, proportioning are relevant with removal color removal COD effect, so we have designed a coagulant precipitation reactor and swash plate reactor, have calculated hydraulics and have verified the result.
Some achievements in research think that the removal of residual dye is relevant with the PH of water, and the optimization proportioning composition that adds efficiently discolor decontamination polymeric flocculant (coagulant aids) and inorganic polymeric coagulant can be removed most of colourity and COD.
Native system adopts tubular ultra-filtration membrane, though the film price is than hollow-fibre membrane height, but it is high that hollow requires pre-treatment, especially in the pre-treatment of high salt high-concentration waste water, characteristics such as the tubular membrane cross-flow is not stopped up, antipollution are that hollow membrane is incomparable, use tubular membrane can guarantee that whole Waste Water Treatment is long-term, stable, reliability service! Having significantly reduced film replacement cost and cleaning charge uses.Slave unit drops into and working cost comprehensive benefit analysis tubular membrane cost performance valency height in high-concentration waste water is handled.The application of big flux ultra-filtration membrane, can help to remove residual turbidity and colloid again, the leading portion pre-treatment had both been reached meet the SDI index that RO is intake, the follow-up Organic pollutants that RO is carried have been reduced simultaneously again, total system is tending towards rationally, and it is more outstanding with each Elementary Function that the decontamination share of discoloring distribution is more conducive to operation.
The utility model treatment effect:
When the water inlet electricity is led average out to 17581 μ scm-1, CODcr average out to 829mg/L, colourity average out to 1709cu, go out water power through the utility model system and lead average out to 642 μ s.cm-1, water outlet CODcr average out to 44mg/L, delivery turbidity average out to 0.1NTU, effluent color dilution average out to 2.5cu, clearance is respectively 96.35%, 95.3%, 99.7%, 99.5%, has reached the water quality requirement of first country field irrigation, can consider to do industrial water reuse under certain condition.
The utility model system has that input is lower, running cost is very low, floor space is little, safe, stable, reliable, personnel operation expense and the low characteristics of maintenance of equipment expense can also be carried out energy recovery from concentrated solution, further cut operating costs.
The utility model system is applicable to the processing of the high dense high salt dyeing waste water of cotton industry, great to the conserve water resource significance, can self cotton resource is abundant, electric power resource is cheap, introduce the big printing and dyeing enterprise of water requirement have opened up a new outlet for the comparatively nervous plateau saline-alkali area of water resources (as Xinjiang etc.) utilizes.
Description of drawings:
Fig. 1 is the processing synoptic diagram of the utility model treatment system.
Component among the figure, position and numbering: water intaking pump M1, lift pump M2, PAM dosing pump M3, PAC dosing pump M4, discoloring agent dosing pump M5, pH regulator agent dosing pump M6, ultrafiltration recycle pump M7, one-level RO topping-up pump M8, secondary RO topping-up pump M9, equalizing tank 1, PAM medicinal cupping 2, PAC medicinal cupping 3, discoloring agent jar 4, pH regulator agent jar 5, ultrafiltration circulatory pool 6, clean cycle pond 7, one-level RO circulatory pool 7, secondary RO circulatory pool 9, clean water basin 10, coagulant precipitation jar 11, inclined-plate clarifying basin 12, ultrafiltration apparatus 13, one-level RO equipment 14, secondary RO equipment 15, membrane distillation equipment 16, shape zone, coagulant precipitation jar side 17, overflow weir 18, swash plate 19, security personnel's strainer 20
Fig. 2 is the utility model treatment system inner membrance Distallation systm operation synoptic diagram.
Embodiment:
Below by specific embodiment, and in conjunction with the explanation accompanying drawing, system operation is described further to the utility model.
Embodiment: use native system and handle the high dense high salt dyeing waste water of cotton, adopt corrosion-resistant vacuum primingpump M1 directly to get former water from the printing and dyeing workshop streamline, write down used dyestuff kind during water intaking, the on-the-spot simultaneously size that detects specific conductivity and note regulating the water intaking valve, guarantee the former water conductivity of getting, to guarantee cycles of concentration as far as possible.
Former water adds pH regulator agent, discoloring agent, PAC, PAM by PAM dosing pump M3, PAC dosing pump M4, discoloring agent dosing pump M5, pH regulator agent dosing pump M6 before the lift pump M2 successively before pump M2 in lift pump M2 enters into coagulant precipitation jar 11.Massfraction is 33% technical hydrochloric acid and water preparation in 1: 2 by volume, and different according to water inlet pH value, adding dose is 6-23L/h, and then adding dose is 1.98～7.59kg/t; PAC is made into the amount adding of the solution of 20% concentration according to 3.75L/h, and adding dose is 650g/t; PAM is made into the amount adding of the solution of 5 ‰ concentration according to 10L/h, and adding dose is 0.5g/t, and it is unsuitable excessive to add dose, otherwise can cause film to pollute, and influences the work-ing life of film.Supernatant liquor entered in the inclined-plate clarifying basin 12 by overflow weir 18 after the liquid medicine mixture entered coagulant precipitation jar 11 stop 1.5h.Feed liquid further separate and subside in inclined-plate clarifying basin 12 stops behind the 2.4h supernatant liquor and collects the laggard ultrafiltration intermediate water tank 6 of going into by the perforation header.
Ultrafiltration membrane system 13 is selected the organic tubular membrane of certain homemade 19 passage hydrophilic PVDF for use, and supporting layer is ultrathin, can not form generally speaking to block in supporting layer, can handle high solid content material, high density liquid stream; Concentration polarization and dirt can be controlled effectively, the flow velocity of feed liquid can be regulated on a large scale; Feed liquid produces cross-flow with high flow rate by the tube chamber lining endothelium, and material is not easy to pile up the formation fouling at face, has prolonged the cycle that film cleans.Adopt the cross flow filter form, 10% concentrate recirculation is to equalizing tank 1, all the other dense water outer loop, and working pressure is 0.045～0.18Mpa, treat effluent enters one-level RO circulatory pool 8, and the strainer 20 of ensuring public security is set before the one-level RO system.
It is the aromatic polyamide matrix material that one-level RO system 14 adopts membrane material, and working pressure is 1.4～1.8Mpa, and the rate of recovery is 50%, can hold back 96% salts substances, and the dense water that accounts for total treatment capacity 50% enters into two-pass reverse osmosis 15 and carries out further desalination and concentration; Two-pass reverse osmosis system 15 membrane materials are the aromatic polyamide matrix material, working pressure is 2.2～4.4Mpa, the rate of recovery is 50%, can hold back the salts substances more than 98%, accounts for high dense water total treatment capacity 25%, that concentrate more than 3 times and enters into vapo(u)rization system 16.
High dense water through pre-treatment+reverse osmosis enters evaporating film 1 through after the heat exchanger heats, and the steam that sees through film is blown to condenser condenses and becomes pure water.Remain dense water and enter next stage evaporating film 2 continuation evaporation concentration after heat exchanger heats, the steam that sees through film is blown to condenser condenses and becomes pure water.Obtain 35% (crystallization concentration) concentrated solution after the dense water process of the RO n level evaporating film evaporation concentration and enter crystallizer, finally obtain solid salt and handle as solid waste, or fully utilize, the steam that sees through evaporating films at different levels obtains pure water after condenser condenses.
When the distillation film can make full use of low-temperature waste heat, its running cost can obviously descend.Xinjiang dyeing waste water Total Water is 20000 tons/day, and wherein 18000 tons/day are low pollutant effluents, average water temperature 45 degree.After being cooled to 25 degree, adopt biological treatment to reach the reuse of agricultural filling standard.Need cooling tower refrigerative used heat to be used in biochemical waste water if can being handled, not only greatly reduce the expense of 18000 tons of cooling waste waters, also can utilize these used heat to distill and handle 600 tons concentrated waste water, (the boiling hot utilization ratio of low temperature reaches about 70%) reclaims 531 tons of pure water and 69 tons of composite salt.
And membrane distillation is when utilizing used heat handle to concentrate waste water fully, and equipment such as reverse osmosis membrane just need not to reach maximum running status in the pretreatment technology, only needs to reclaim 70% fresh water and can reach the system handles target.70% the rate of recovery will be the running status that whole pretreatment system is in moderate duty, can make that system is stable more, safety, long-time running.Prolong service life of equipment, further reduce engineering cost.
Notice the problem of the rate of recovery in the native system design.Coagulant precipitation jar 11, settling tank 12 spoil disposal water enter in the factory in the biochemistry pool and reclaim, and UF and RO waterpower rinse water are returned to handle into equalizing tank 1 again and do not missed, in the matting water and after enter equalizing tank 1 and utilizing, make the high level of utilization ratio maintenance of water.
Claims (8)
1. treatment of dyeing wastewater Zero emission device is characterized in that: this device comprises that materialization pre-treatment, RO desalting system and dense water treatment three parts form; The materialization pre-treatment partly comprises equalizing tank (1), coagulant precipitation jar (11), settling tank (12), tubular ultra-filtration membrane (13) four parts composition; The RO desalting system comprises one-level RO system (14), secondary RO system (15), and the dense water of one-level RO is intake as secondary RO; Dense water treatment portion is meant membrane distillation system (16).
2. treatment of dyeing wastewater Zero emission device according to claim 1, it is characterized in that: equalizing tank (1) is directly fetched water from shop production line by vacuum primingpump (M1), be connected with lift pump (M2) between equalizing tank (1) and the coagulant precipitation jar (11), and by PAM dosing pump (M3), PAC dosing pump (M4), discoloring agent dosing pump (M5), pH regulator agent dosing pump (M6) successively at the agent of the preceding adding pH regulator of lift pump (M2), discoloring agent, PAC, PAM.
3. treatment of dyeing wastewater Zero emission device according to claim 1 is characterized in that: the design of coagulant precipitation jar (11) side has a square region (17), and in order to carry out the thorough mixing of liquid medicine behind pump, overflow weir (18) is arranged at top.
4. treatment of dyeing wastewater Zero emission device according to claim 1, it is characterized in that: place swash plate (19) in the settling tank (12), coagulant precipitation jar (11) supernatant liquor enters settling tank (12) by overflow weir (18) through pipeline self, the perforation header is established in the settling tank top, and supernatant liquor enters ultrafiltration circulatory pool (6) through pipeline self.
5. treatment of dyeing wastewater Zero emission device according to claim 1 is characterized in that: ultrafiltration system membrane module (13) is selected certain homemade antipollution tubular ultra-filtration membrane for use, adopts the cross flow filter form, and treat effluent enters the RO system and carries out desalting treatment.
6. treatment of dyeing wastewater Zero emission device according to claim 1 is characterized in that: one-level RO fresh water is discharged into the part of filtered water tank (10) as system's water outlet, and secondary RO fresh water is discharged into filtered water tank (10) also as the part of system's water outlet.
7. treatment of dyeing wastewater Zero emission device according to claim 1 is characterized in that: this technology of installing dense water treatment portion employing is a film distillation technology.
8. treatment of dyeing wastewater Zero emission device according to claim 1 is characterized in that: the membrane distillation equipment (16) of dense water treatment portion is made up of heat exchanger, evaporating film, crystallizer, condenser.
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| CN2010205463581U CN201864630U (en) | 2010-09-28 | 2010-09-28 | Zero-discharge device for treating printing and dyeing wastewater |
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| CN102583862A (en) * | 2012-02-22 | 2012-07-18 | 北京纬纶华业环保科技股份有限公司 | Method and system for treating saline wastewater to zero discharge and recycling |
| CN103304069A (en) * | 2013-07-03 | 2013-09-18 | 北京赛诺水务科技有限公司 | Novel sewage sub-zero discharge treatment method and novel sewage sub-zero discharge treatment device |
| CN103319042A (en) * | 2013-07-16 | 2013-09-25 | 北京倍杰特国际环境技术有限公司 | High-salt complex wastewater reuse and zero discharge integrated equipment and technology |
| CN103896437A (en) * | 2014-01-02 | 2014-07-02 | 杭州深瑞水务有限公司 | Zero emission treatment process of high-salinity wastewater |
| CN104129882A (en) * | 2014-08-25 | 2014-11-05 | 成都美富特膜科技有限公司 | Novel treatment technology of high-concentration industrial wastewater |
| CN104445774A (en) * | 2014-11-24 | 2015-03-25 | 神华集团有限责任公司 | Wastewater treating device and method |
| CN104529035A (en) * | 2014-12-24 | 2015-04-22 | 北京桑德环境工程有限公司 | High-concentration organic wastewater zero-discharge treatment system and method |
| CN106630360A (en) * | 2017-03-01 | 2017-05-10 | 苏州澄江环境科技有限公司 | Treatment system of surface treatment wastewater and use method thereof |
| CN108178360A (en) * | 2018-03-05 | 2018-06-19 | 山东联恒环境科技有限公司 | A kind of waste emulsified mixture purifying processing device of waste emulsified mixture purifying treatment method and adopting said method |
| CN108766610A (en) * | 2018-05-31 | 2018-11-06 | 同济大学 | The concentration method and Spent Radioactive water treatment system of radioactive wastewater |
| CN109336270A (en) * | 2018-10-10 | 2019-02-15 | 浙江津膜环境科技有限公司 | A kind of dye vat Liquid Residue resource utilization method and its system |
| CN110526520A (en) * | 2019-09-24 | 2019-12-03 | 福建省晋蓝环保科技有限公司 | A kind of dyeing waste water dual treatment multistage reuse method and device |
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| CN102583862B (en) * | 2012-02-22 | 2015-07-01 | 北京纬纶华业环保科技股份有限公司 | Method and system for treating saline wastewater to zero discharge and recycling |
| CN102583862A (en) * | 2012-02-22 | 2012-07-18 | 北京纬纶华业环保科技股份有限公司 | Method and system for treating saline wastewater to zero discharge and recycling |
| CN103304069A (en) * | 2013-07-03 | 2013-09-18 | 北京赛诺水务科技有限公司 | Novel sewage sub-zero discharge treatment method and novel sewage sub-zero discharge treatment device |
| CN103319042A (en) * | 2013-07-16 | 2013-09-25 | 北京倍杰特国际环境技术有限公司 | High-salt complex wastewater reuse and zero discharge integrated equipment and technology |
| CN103319042B (en) * | 2013-07-16 | 2014-11-05 | 北京倍杰特国际环境技术有限公司 | High-salt complex wastewater reuse and zero discharge integrated equipment and technology |
| CN103896437A (en) * | 2014-01-02 | 2014-07-02 | 杭州深瑞水务有限公司 | Zero emission treatment process of high-salinity wastewater |
| CN104129882A (en) * | 2014-08-25 | 2014-11-05 | 成都美富特膜科技有限公司 | Novel treatment technology of high-concentration industrial wastewater |
| CN104445774A (en) * | 2014-11-24 | 2015-03-25 | 神华集团有限责任公司 | Wastewater treating device and method |
| CN104529035A (en) * | 2014-12-24 | 2015-04-22 | 北京桑德环境工程有限公司 | High-concentration organic wastewater zero-discharge treatment system and method |
| CN106630360A (en) * | 2017-03-01 | 2017-05-10 | 苏州澄江环境科技有限公司 | Treatment system of surface treatment wastewater and use method thereof |
| CN108178360A (en) * | 2018-03-05 | 2018-06-19 | 山东联恒环境科技有限公司 | A kind of waste emulsified mixture purifying processing device of waste emulsified mixture purifying treatment method and adopting said method |
| CN108766610A (en) * | 2018-05-31 | 2018-11-06 | 同济大学 | The concentration method and Spent Radioactive water treatment system of radioactive wastewater |
| CN108766610B (en) * | 2018-05-31 | 2022-02-08 | 同济大学 | Concentration treatment method of radioactive wastewater and radioactive wastewater treatment system |
| CN109336270A (en) * | 2018-10-10 | 2019-02-15 | 浙江津膜环境科技有限公司 | A kind of dye vat Liquid Residue resource utilization method and its system |
| CN110526520A (en) * | 2019-09-24 | 2019-12-03 | 福建省晋蓝环保科技有限公司 | A kind of dyeing waste water dual treatment multistage reuse method and device |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110615 Termination date: 20190928 |
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| CF01 | Termination of patent right due to non-payment of annual fee |