CN103755082B - System and method for resource recovery of regenerated wastewater of ion exchange resin - Google Patents
System and method for resource recovery of regenerated wastewater of ion exchange resin Download PDFInfo
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- CN103755082B CN103755082B CN201410026885.2A CN201410026885A CN103755082B CN 103755082 B CN103755082 B CN 103755082B CN 201410026885 A CN201410026885 A CN 201410026885A CN 103755082 B CN103755082 B CN 103755082B
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Abstract
The invention provides a system and a method for resource recovery of regenerated wastewater of ion exchange resin. According to the method and the system, a two-grade reverse osmosis and electrolysis process is used for treating the regenerated wastewater; concentrated water of the first grade of reverse osmosis is used for electrolyzing to prepare sodium hypochlorite; fresh water of the second grade of the reverse osmosis is used for power plant industrial water, denitration water and the like. The system and the method can be used for recycling resources including sodium chloride, ammonia and the like in the regenerated wastewater; meanwhile, the fresh water is recycled; finally, the concentrated water is used for preparing the sodium hypochlorite and the zero emission of the regenerated wastewater can be realized.
Description
Technical field
The invention belongs to Industrial Wastewater Treatment and resource circulation utilization field, be specifically related to a kind of using ion-exchange resin regenerated waste water resource recovering system and method.
Prior art
At present, industrial enterprise's ion exchange resin regenerated acid and alkali waste water normally qualified discharge after neutralizing treatment, or produce all the other acidic and alkaline waste waters with enterprises in regenerative wastewater being used for, seldom there is the useful matter considered in reclaiming waste water.The reported treatment process of ion exchange resin regeneration acidic and alkaline waste water has following several: acid-base neutralisation method, the chemical reaction precipitator method, biochemical process, FENTON reagent method, nanofiltration/reverse osmosis method.
1) acid-base neutralisation method.(Zhang Jiahua. Kweiyang power plant effluent is administered and reuse experimental study [J]. water supply and drainage, 1994,04); (Ren Heshe. the comprehensive utilization [J] of demineralization plant regenerative wastewater. Treatment of Industrial Water, 1995,05); (square Xi, Zhang Gehong, Han Yaoxia, et al. heat power plant ash slag waste water, regenerative wastewater comprehensive utilization technological transformation design [J]. environmental engineering, 2006,02); (analogy army, Zhang Zhanping, Gao Wenfeng. thermal power plant's using ion-exchange resin regenerated waste water process and reduction of discharging [J]. environmental protection for electric power, 2008,06): 7-9.); (Qian Feng, Xiang Jing, Li Wei, et al. boiler soft water station regenerative wastewater is used for the research [J] of flue gas desulfurization. Environmental science and technology, 2009,01); (Fang Jinxiang. certain power plant chemistry wastewater utilization engineering practice [J]. water supply and drainage, 2010,09); (Liu Jingming, Xi Lijuan, Li Bing. the research [J] of acidic and alkaline waste water neutralized system optimization of flocculation conditions and best sludge output. environmental engineering, 2002,05) etc. report ion exchange regenerant acid waste water is used for boiler punching ash, alkaline waste water is used as the technology such as sweetening agent and acid-base neutralisation system optimization.
2) the chemical reaction precipitator method.(Guo Chun plum is old, Zhang Zhongzhi. the analysis of steam-injected boiler brine waste and reuse technology research [J]. and Treatment of Industrial Water, 2003,12); (Guo Chunmei, Chen Jinfu. using ion-exchange resin regenerated waste water Treatment for Reuse simulation test research [J]. environmental engineering journal, 2008,01); (Che Chunbo. the research [J] of precipitator method process using ion-exchange resin regenerated waste water. Harbin University of Commerce's journal (natural science edition), 2010,03): 291-4.); (Wang Xiaohui, Li Yuyin. the simulation test [J] that using ion-exchange resin regenerated waste water reclaims and utilizes. Hebei Metallurgy, 2012,12) hardness ions removed by step chemical reaction precipitation method in regenerative wastewater: 24-7.) etc. is reported, reclaim calcium salt and magnesium salts two kinds of byproducts, utilize the technology such as the sodium-chlor regeneration sodium ion exchange resin produced in water.
3) biochemical process.(Tang Yunlei. the discussion [J] of District of Shanghai power plant resin regeneration wastewater treatment. east china electric power, 2001,12); (Zhang Ping, Chen Xiaoyu. the research [J] of biological contact oxidation pond-membrane bioreactor combined treatment power plant regenerative wastewater. east china electric power, 2006,05) etc. biomembrance process, bio-contact oxidation and membrane bioreactor process using ion-exchange resin regenerated waste water is adopted, remove organism wherein, reach emission standard.
4) FENTON reagent method.(king Luo Chun Shen, Ding Huanru, Meng Yi, Yang Gui contain .Fenton agent treated regenerated wastewater of ion-exchanged resin from electric power plant [J]. Environmental Pollution and Control, 2001,05); (Wang Luochun, Li Xiaohua, Jin Long. by Fenton reagent-mineralized waste bio-reactor combination treatment using ion-exchange resin regenerated waste water [J]. Shanghai University Of Electric Power's journal, 2009,05): 461-4.); (golden imperial Zhao .Fenton reagent and mineralized refuse bioreactor combination treatment regenerated wastewater of ion-exchanged resin from electric power plant [J]. water supply and drainage, 2004,12); (Jin Long, Wang Luochun, Chen Mei .Fenton agent treated power plant's difficult degradation using ion-exchange resin regenerated waste water [J]. Suzhou Institute of Science and Technology journal (engineering version), 2008,01): 18-22.); (Yang Guisheng, Meng Yi, Wang Luochun, et al. Treatment of regenerating [J]. energy project, 2007,01): 53-5.); (Che Chunbo, Wang Wei. with the research [J] of Fenton reagent process refinery using ion-exchange resin regenerated waste water. refining and chemical industry, 2009,04): 19-21+58.); (Che Chunbo .Fenton reagent catalytic oxidation process using ion-exchange resin regenerated waste water [J]. environmental science and management, 2010,02) FENTON reagent catalytic oxidation process using ion-exchange resin regenerated waste water: 79-81.) etc. is adopted, remove hardly degraded organic substance wherein, reach emission standard.
5) nanofiltration/reverse osmosis method.(Wang Luochun, Ding Huanru, Wen Renqin. the research [J] of nano filtering process treatment of Power using ion-exchange resin regenerated waste water. Shanghai University Of Electric Power's journal, 2006,04): 338-40.); (Fu Jierong. sugar refinery using ion-exchange resin regenerated waste water recovery technology [J]. Guangxi light industry, 2010,09): 106-7+37.) adopt nanofiltration to reclaim using ion-exchange resin regenerated waste water, remove organism wherein, reach emission standard.(Wei Lian, Liao Chengcheng. reverse osmosis is used for the treatment and reuse [J] of APT ion exchange waste water. Environmental science and technology, 2010,11) etc. adopt reverse osmosis technology to reclaim APT to smelt ion-exchange alkaline waste water, its operating pressure is at 1.7 ~ 1.8MPa.
Using ion-exchange resin regenerated waste water Patents document.
The recycle device of the patent No. 201120177523.5 chelate resin tower regenerative wastewater, by installing storage tank, pump on waste line additional, makes, on its pipeline that tieback is disposed at respective soda acid again, to produce rational chemical reaction, reduce the pressure of ultimate disposal.
Application number: the technology of 97105951.9 producing flocculant using ion-exchange resin regenerated waste waters, hydrochloric acid in regenerative wastewater or sulfuric acid and iron or aluminium are reacted, generate hydrogen, molysite or aluminium salt, hydrogen recovery utilizes, and the regenerative wastewater containing molysite or aluminium salt is applied as flocculation agent.
Patent No. 201010533707.0PVC acidic and alkaline waste water two-stage coagulation and biological synergetic treatment process,
In conjunction with coagulation and biological treatment, realize final qualified discharge.
Application number: 200620094150.4 acid-base waste water treatment systems, by industrial acidic wastewater and industrial alkaline waste water after the techniques such as acidic and alkaline waste water neutralization, coagulation, precipitation, sludge dewatering, reaches emission standard.
Patent No. 201220023152.X resin tower acidic and alkaline waste water recycling system, acid waste water and alkaline waste water are flowed into spent acid groove and salkali waste groove respectively, spent acid is by neutralized wastewater in spent acid pump delivery to PO workshop saponification waste-water groove, and salkali waste is joined alkali by salkali waste pump delivery to clorox operation and to be manufactured a finished product clorox sale.
The patent No. 201220079958.0 thermal power plant acidic and alkaline waste water neutralizing treatment automatic medicine adding apparatus, in conjunction with acid adding, adds the automatic neutralization that alkali and automatic control device realize acidic and alkaline waste water and controls.
According to literature search interpretation of result, current ion exchange resin regeneration acidic and alkaline waste water is mainly regarded as a kind of waste, can qualified discharge through acid-base neutralisation method, the chemical reaction precipitator method, biochemical process, FENTON reagent method, nanofiltration/reverse osmosis method etc., or for low-quality occasion as boiler punching ash etc., a small amount of technology considers the regenerator of reuse sodium chloride solution after the removals such as the hardness in regenerative wastewater as sodium ion exchange resin to use, and when not having Na-ion exchanger, sodium chloride solution cannot effectively utilize.(Wei Lian, Liao Chengcheng. reverse osmosis is used for the treatment and reuse [J] of APT ion exchange waste water. Environmental science and technology, 2010,11) mention with reverse osmosis technology recovery APT smelting ion-exchange alkaline waste water, but its working pressure is low, only have 1.7 ~ 1.8MPa, and do not reclaim the chemical resource in waste water.
At present, industrial enterprise's desalted water processing system generally adopts reverse osmosis technology, after reverse osmosis unit, connect positive and negative again, hybrid ionic exchange column carries out desalting treatment, during ion exchange resin regeneration with de-mineralized water dilution Hhigh purit salt acid and ionic membrane caustic soda as regenerated liquid, wherein concentration impurity ion is very low.Because the fouling composition such as hardness, sulfate radical, barium, strontium, silicon in ion exchange tower water inlet is removed to very low degree by reverse osmosis unit, therefore the salinity in ion exchange regenerant waste water is the sodium ion brought into of regenerator and chlorion mainly, fouling components and concentration is very low, possesses the technical qualification that reverse osmosis is reclaimed.
Containing a large amount of chlorion, ammonia and a small amount of hardness ionses and corrosion product in thermal power plant's condensed water precision processing system cation exchange tower regenerative wastewater, containing a large amount of sodium ions and a small amount of hardness ions, sulfate ion in anion exchange tower regenerative wastewater, become the regenerative wastewater of main sodium chloride-containing and ammonia after the two mixing, also possess the technical qualification that reverse osmosis is reclaimed.
Summary of the invention
The object of the present invention is to provide one can reclaim the useful resources such as sodium-chlor, ammonia in ion exchange resin regeneration acidic and alkaline waste water, reclaim fresh water simultaneously, the dense water that process system produces can prepare clorox, finally realizes using ion-exchange resin regenerated waste water resource recovering system and the method for regenerative wastewater zero release.
For achieving the above object, system of the present invention comprises: comprise and sun, the waste water tank with blower fan that anionresin regenerative wastewater is connected, the outlet of waste water tank by the road successively with strainer/ultrafiltration, one-level booster pump and one-level cartridge filter are connected, and the pipeline be connected with one-level cartridge filter in one-level booster pump is also provided with Scale inhibitors chemicals dosing plant, the water outlet of one-level cartridge filter by the road respectively with one-level high-pressure pump, the entrance of energy recycle device is connected, the entrance of one-level high pressure pump outlet and one-level one section of reverse osmosis unit is connected, the water outlet of one-level one section of reverse osmosis unit is connected with fresh-water tank by the road, fresh-water tank water outlet delivers to reuse water spot after fresh water pump supercharging, the entrance of dense water out and one-level two sections of reverse osmosis units of one-level one section of reverse osmosis unit is connected, the water outlet of one-level two sections of reverse osmosis units is connected with second level reverse osmosis apparatus by the road, the water outlet of second level reverse osmosis apparatus is connected with fresh-water tank, the dense water out of second level reverse osmosis apparatus is connected with the export pipeline of strainer by the road, the dense water out of one-level two sections of reverse osmosis units is connected with another entrance of energy recycle device, energy recycle device one outlet is connected with one-level high pressure pump outlet by the road, another outlet is connected with electrolyzer, the clorox of electrolyzer output delivers to chemical feeding points by clorox dosing pump.
Pipeline between described waste water tank and strainer/ultrafiltration is also provided with lift pump.
Described strainer/be also provided with filtered water tank between ultrafiltration and one-level booster pump.
Described Scale inhibitors chemicals dosing plant comprise Scale inhibitors case and with the anti-sealant dosing pump be connected with the entrance pipe of Scale inhibitors case, one-level cartridge filter respectively.
Described second level reverse osmosis apparatus comprises secondary one section of reverse osmosis unit, secondary inter-section booster and two-stage two-segment reverse osmosis unit, the entrance of water outlet and secondary one section of reverse osmosis unit of one-level two sections of reverse osmosis units is communicated with, the dense water out of secondary one section of reverse osmosis unit is connected through the entrance of secondary inter-section booster with two-stage two-segment reverse osmosis unit, the dense water out of two-stage two-segment reverse osmosis unit is connected with the export pipeline of strainer, and the water outlet of secondary one section of reverse osmosis unit and two-stage two-segment reverse osmosis unit is connected with fresh-water tank respectively.
The pipeline of described one-level two sections between reverse osmosis unit and second level reverse osmosis apparatus is provided with intermediate water tank, two stage supercharging pump, secondary cartridge filter and secondary high-pressure pump successively.
Described blower fan adopts roots blower.
Using ion-exchange resin regenerated waste water its recovery method as resource of the present invention is that the condensate refining treatment ion exchange resin regeneration waste water containing ammonia is sent into waste water tank, controls mixed regeneration waste water ph and reaches more than 10, in waste water tank, blast air with roots blower fully mix, oxygen supply is simultaneously to be oxidized the Fe that may exist
2+, by lift pump, mixed regeneration waste water is sent into strainer/ultrafiltration to remove particle suspensions and iron, water outlet enters filtered water tank, by one-level booster pump, one-level cartridge filter is sent in filtered water tank water outlet to filter, added the Scale inhibitors be stored in Scale inhibitors case by anti-sealant dosing pump according to operational conditions before one-level cartridge filter, an one-level cartridge filter water outlet part enters the pressurization of one-level high-pressure pump, one-level one section of reverse osmosis unit is together entered with the water outlet of one-level high-pressure pump after the dense water that another part enters energy recycle device and one-level two sections of reverse osmosis units carries out energy exchange, the fresh water of one-level one section of reverse osmosis unit output directly enters fresh-water tank reuse, the fresh water of one-level two sections of reverse osmosis unit outputs enters intermediate water tank, the dense water of one-level two sections of reverse osmosis units is delivered to electrolyzer and is carried out preparing chlorine by electrolysis after energy recycle device exchange energy, when reclaiming the condensate refining treatment ion exchange resin regeneration waste water containing ammonia, in electrolyzer, also carry out the oxidation removal reaction of ammonia, by two stage supercharging pump, secondary cartridge filter is sent in intermediate water tank water outlet to filter, the water outlet of secondary cartridge filter sends into secondary one section of reverse osmosis unit after the pressurization of secondary high-pressure pump, the fresh water of secondary one section of reverse osmosis unit output enters fresh-water tank, the dense water of secondary one section of reverse osmosis unit enters two-stage two-segment reverse osmosis unit after the supercharging of secondary inter-section booster, the fresh water of two-stage two-segment reverse osmosis unit output enters fresh-water tank, and the dense water of two-stage two-segment reverse osmosis unit returns filtered water tank and continues process, fresh-water tank water outlet delivers to reuse water spot after fresh water pump supercharging, the clorox of electrolyzer output delivers to chemical feeding points by clorox dosing pump.
Effect of the present invention is as follows:
1) the using ion-exchange resin regenerated waste water water quality characteristics that the present invention is directed to is that the fouling components and concentrations such as hardness, sulfate radical, silicon-dioxide are very low, reverse osmosis can be adopted to reclaim sodium-chlor a large amount of in waste water, the reverse osmosis rate of recovery is provided, operating pressure is made to reach 8MPa or higher, reverse osmosis concentrated water saltiness after concentrated reaches 8% or higher, thus maximum reclaimed fresh water, sodium-chlor is retained in a small amount of dense water;
2) because the iron in regenerative wastewater pollutes reverse osmosis membrane, before reverse osmosis, aeration-filtration/ultrafiltration technology is provided with, the Fe that may be able to exist in oxidized waste water
2+, filtration medium selects quartz sand or manganese sand, forms active catalytic layer, the iron of solubilised state is converted into insoluble Fe (OH) in filtration procedure at filter material surface
3remove after filtration, particulate iron oxide compound is also filtered removal simultaneously, connects ultra-filtration equipment more thereafter, removes the particulate matter in regenerative wastewater, thus protection reverse osmosis unit;
3) for the condensate polishing treatment regenerative wastewater containing ammonia, reverse osmosis operate in pH value be 10 or higher condition under, utilize the feature that reverse osmosis membrane is lower to molecular state material clearance, make ammonia in regenerative wastewater mainly with amino molecule form through reverse osmosis membrane, be retained in fresh water, thus the ammonia resource in reclaiming waste water, run pH value higher, the ammonia of recovery is more;
4) first step reverse osmosis adopts two-part arrangement, reverse osmosis membrane adopts the sea water desalination membrane of the companies such as DOW, HYDRANAUTICS, TORAY, KOCH, GE, when reclaiming ammonia, reverse osmosis operate in pH value be 10 or higher condition under, operating pressure reaches the ultimate pressure (8MPa or higher) of film, when regenerative wastewater saltiness is about 2% time, system recoveries rate is more than 75%, and dense water saltiness is more than 8%;
5) first step reverse osmosis adopts fresh water segmentation reuse design, first paragraph due to cycles of concentration lower, fresh water saltiness is lower can direct reuse, and second segment cycles of concentration is higher, and fresh water saltiness, more than 1000mg/L, continues to enter two-pass reverse osmosis and carries out desalting treatment;
6) first step reverse osmosis uses energy recycle device to reclaim the energy of dense water, runs power consumption only 3 ~ 4kWh/m
3fresh water;
7) second stage reverse osmosis adopts two-part arrangement, intersegmentally establish topping-up pump, reverse osmosis membrane adopts the brackish water film of the companies such as DOW, HYDRANAUTICS, TORAY, KOCH, GE, when reclaiming ammonia, reverse osmosis operate in pH value be 10 or higher condition under, the fresh water of output mixes rear reuse with first step first paragraph reverse osmosis freshwater, dense water continues process before returning first step reverse osmosis;
8) main sodium chloride-containing in the dense water of first step reverse osmosis, when processing the condensate polishing treatment regenerative wastewater containing ammonia, higher ammonia is also had in dense water, dense water is delivered to electrolyzer and carries out electrolysis, ammonia complete oxidation is removed by the clorox utilizing electrolysis to produce, chlorine bleach liquor is made in further electrolysis, can be used for sterilization and disinfection;
9) electrolyzer uses titanium-based metal oxide coating DSA anode, adopts RuO
2, IrO
2, Ta
2o
5, SnO
2, PbO
2, TiO
2combine catalytically active coatings Deng metal oxide, there is lower chlorine evolution potential and higher oxygen evolution potential, be conducive to the direct of ammonia and indirect oxidation, be applicable to electrolytic chlorination sodium solution clorox simultaneously.
Accompanying drawing explanation
Fig. 1 is one-piece construction schematic diagram of the present invention.
In figure, 1-waste water tank, 2-lift pump, 3-strainer/ultrafiltration, 4-filtered water tank, 5-one-level booster pump, 6-one-level cartridge filter, 7-one-level high-pressure pump, 8-one-level one section of reverse osmosis unit, 9-one-level two sections of reverse osmosis units, 10-energy recycle device, 11-electrolyzer, 12-intermediate water tank, 13-two stage supercharging pump, 14-secondary cartridge filter, 15-secondary high-pressure pump, 16-secondary one section of reverse osmosis unit, 17-two-stage two-segment reverse osmosis unit, 18-secondary inter-section booster, 19-fresh-water tank, 20-fresh water pump, 21-Scale inhibitors case, 22-anti-sealant dosing pump, 23-roots blower, 24-clorox dosing pump.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
See Fig. 1, system of the present invention comprises: comprise and sun, the waste water tank 1 with roots blower 23 that anionresin regenerative wastewater is connected, the outlet of waste water tank 1 by the road successively with lift pump 2, strainer/ultrafiltration 3, filtered water tank 4, one-level booster pump 5 and one-level cartridge filter 6 are connected, and the pipeline be connected with one-level cartridge filter 6 in one-level booster pump 5 is also provided with Scale inhibitors chemicals dosing plant, Scale inhibitors chemicals dosing plant comprise Scale inhibitors case 21 and with respectively with Scale inhibitors case 21, the anti-sealant dosing pump 22 that the entrance pipe of one-level cartridge filter 6 is connected, the water outlet of one-level cartridge filter 6 by the road respectively with one-level high-pressure pump 7, the entrance of energy recycle device 10 is connected, the entrance of outlet and one-level one section of reverse osmosis unit 8 of one-level high-pressure pump 7 is connected, the water outlet of one-level one section of reverse osmosis unit 8 is connected with fresh-water tank 19 by the road, fresh-water tank 19 water outlet delivers to reuse water spot after fresh water pump 20 supercharging, the entrance of dense water out and one-level two sections of reverse osmosis units 9 of one-level one section of reverse osmosis unit 8 is connected, the dense water out of one-level two sections of reverse osmosis units 9 is connected with another entrance of energy recycle device 10, energy recycle device 10 1 outlet is connected with the outlet of one-level high-pressure pump 7 by the road, another outlet is connected with electrolyzer 11, the clorox of electrolyzer 11 output delivers to chemical feeding points by clorox dosing pump 24, the water outlet of one-level two sections of reverse osmosis units 9 by the road successively with intermediate water tank 12, two stage supercharging pump 13, secondary cartridge filter 14, secondary high-pressure pump 15 and second level reverse osmosis apparatus are connected, second level reverse osmosis apparatus comprises secondary one section of reverse osmosis unit 16, secondary inter-section booster 18 and two-stage two-segment reverse osmosis unit 17, the entrance of water outlet and secondary one section of reverse osmosis unit 16 of one-level two sections of reverse osmosis units 9 is communicated with, the dense water out of secondary one section of reverse osmosis unit 16 is connected through the entrance of secondary inter-section booster 18 with two-stage two-segment reverse osmosis unit 17, the dense water out of two-stage two-segment reverse osmosis unit 17 is connected with the export pipeline of strainer/ultrafiltration 3, the water outlet of secondary one section of reverse osmosis unit 16 and two-stage two-segment reverse osmosis unit 17 is connected with fresh-water tank 19 respectively.
See Fig. 1, using ion-exchange resin regenerated waste water its recovery method as resource of the present invention is that the condensate refining treatment ion exchange resin regeneration waste water containing ammonia is sent into waste water tank 1, controls mixed regeneration waste water ph and reaches more than 10, in waste water tank 1, blast air with roots blower 23 fully mix, oxygen supply is simultaneously to be oxidized the Fe that may exist
2+, by lift pump 2, mixed regeneration waste water is sent into strainer/ultrafiltration 3 to remove particle suspensions and iron, water outlet enters filtered water tank 4, by one-level booster pump 5, one-level cartridge filter 6 is sent in filtered water tank 4 water outlet to filter, added the Scale inhibitors be stored in Scale inhibitors case 21 by anti-sealant dosing pump 22 according to operational conditions before one-level cartridge filter 6, an one-level cartridge filter 6 water outlet part enters one-level high-pressure pump 7 and pressurizes, another part enters after energy recycle device 10 carries out energy exchange with the dense water of one-level two sections of reverse osmosis units 9 and together enters one-level one section of reverse osmosis unit 8 with one-level high-pressure pump 7 water outlet, the fresh water of one-level one section of reverse osmosis unit 8 output directly enters fresh-water tank 19 reuse, the fresh water of one-level two sections of reverse osmosis unit 9 outputs enters intermediate water tank 12, the dense water of one-level two sections of reverse osmosis units 9 is delivered to electrolyzer 11 and is carried out preparing chlorine by electrolysis after energy recycle device 10 exchange energy, when reclaiming the condensate refining treatment ion exchange resin regeneration waste water containing ammonia, in electrolyzer 11, also carry out the oxidation removal reaction of ammonia, by two stage supercharging pump 13, secondary cartridge filter 14 is sent in intermediate water tank 12 water outlet to filter, secondary cartridge filter 14 water outlet sends into secondary one section of reverse osmosis unit 16 after secondary high-pressure pump 15 is pressurizeed, the fresh water of secondary one section of reverse osmosis unit 16 output enters fresh-water tank 19, the dense water of secondary one section of reverse osmosis unit 16 enters two-stage two-segment reverse osmosis unit 17 after secondary inter-section booster 18 supercharging, the fresh water of two-stage two-segment reverse osmosis unit 17 output enters fresh-water tank 19, and the dense water of two-stage two-segment reverse osmosis unit 17 returns filtered water tank 4 and continues process, fresh-water tank 19 water outlet delivers to reuse water spot after fresh water pump 20 supercharging, the clorox of electrolyzer 11 output delivers to chemical feeding points by clorox dosing pump 24.
The present invention can the resource such as sodium-chlor, ammonia in reclaiming waste water, and reclaim fresh water, the dense water that technique produces is for clorox sterilant processed, and entirety achieves the zero release of resource circulation utilization and regenerative wastewater, has good economic and environmental benefit simultaneously;
Technology of the present invention is adopted to reclaim using ion-exchange resin regenerated waste water, when regenerative wastewater saltiness about 2%, callable fresh water saltiness about 400 ~ 600mg/L, fresh-water recovery rate is greater than 75%, and dense water saltiness is greater than 8%; When reclaiming containing the condensate polishing treatment regenerative wastewater of ammonia, the rate of recovery about 50% ~ 60% of ammonia, is retained in fresh water, in dense water remaining ammonia in a cell oxidized degraded realize innoxious, the clorox of electrolysis output is used for sterilization and disinfection;
Technology of the present invention is adopted to reclaim the using ion-exchange resin regenerated waste water containing ammonia, the ammonia fresh water that contains of output can be used for service water moisturizing or denitration system of power plant moisturizing, and because power plant's denitration need use outsourcing ammoniacal liquor, reuse is containing after ammonia fresh water, can reduce outsourcing ammonia amount, economic benefit is obvious;
Technology of the present invention is adopted to reclaim using ion-exchange resin regenerated waste water, dense hydromining electrolysis process clorox, can realize innoxious by remaining ammonia in the dense water of oxidative degradation, the clorox simultaneously made be for sterilization and disinfection, can reduce the expense of power plant's outsourcing sodium-chlor, economic benefit is obvious.
The treatment for reuse of certain system of refined treating congeals water processing in power plant ion exchange tower regenerative wastewater, mixed cationic, anionic exchange resin regenerative wastewater water quality is in table 1, and the water yield is 5m
3/ h.
Certain power plant's ion exchange regenerant waste water mixing water quality of table 1
Adopt treatment process of the present invention, the pH value that the regenerative wastewater of positive and negative resin regeneration tower records according to the pH meter be arranged in waste water tank 1 adjusts proportional quantity, makes pH value about 10.Send into manganese sand filter by lift pump 2, carry out deironing filtration, then filter through ultra-filtration equipment, produce water and enter filtered water tank 4.
First-stage reverse osmosis device adopts two sections of layouts, and reverse osmosis operating pressure 8.5MPa, the rate of recovery 75%, membrane flux is about 17L/m
2* h; First paragraph fresh water saltiness is about 450mg/L, and ammonia content is about 1700mg/L, directly enters fresh-water tank 19; Second segment fresh water saltiness is about 2000mg/L, and ammonia content is about 2500mg/L, enters intermediate water tank 12; Dense water saltiness is about 80900mg/L, and ammonia content is about 5000mg/L, sends into electrolyzer 11.
Second level reverse osmosis apparatus adopts two sections of layouts, intersegmental supercharging, and reverse osmosis operating pressure is about 2.0MPa, and the rate of recovery 90%, membrane flux is about 30L/m
2* h; Fresh water saltiness is about 470mg/L, and ammonia content is about 2100mg/L, enters fresh-water tank 19; Dense water saltiness is about 15000mg/L, and ammonia content is about 3000mg/L, returns filtered water tank 4 and continues process.
Dense water electrolysis in electrolyzer 11 of first-stage reverse osmosis device, electrolyzer DSA anode is Ti/RuO
2-IrO
2material, electrolysis time 90 ~ 120min, current density 100 ~ 200mA/m
2, the 5000mg/L ammonia nitrogen after electrolysis completes in dense water is completely degraded, the chlorine bleach liquor of output concentration about 7 ‰, as plant condenser cooling system biocide.
Implementation result: adopt technique of the present invention to reclaim system of refined treating congeals water processing in power plant using ion-exchange resin regenerated waste water, 75% is greater than containing ammonia fresh-water recovery rate, the rate of recovery of ammonia is greater than 52%(and is retained in fresh water), fresh water is back to denitration system of power plant water, dense water is for clorox processed, as plant condenser cooling system biocide, wherein remaining ammonia nitrogen is fully oxidized removal, and entirety achieves recycle and the wastewater zero discharge of resource.
Claims (6)
1. a using ion-exchange resin regenerated waste water resource recovering system, it is characterized in that: comprise and sun, the waste water tank with blower fan (23) (1) that anionresin regenerative wastewater is connected, the outlet of waste water tank (1) by the road successively with strainer/ultrafiltration (3), one-level booster pump (5) and one-level cartridge filter (6) are connected, and the pipeline be connected with one-level cartridge filter (6) in one-level booster pump (5) is also provided with Scale inhibitors chemicals dosing plant, the water outlet of one-level cartridge filter (6) by the road respectively with one-level high-pressure pump (7), the entrance of energy recycle device (10) is connected, the entrance of outlet and one-level one section of reverse osmosis unit (8) of one-level high-pressure pump (7) is connected, the water outlet of one-level one section of reverse osmosis unit (8) is connected with fresh-water tank (19) by the road, fresh-water tank (19) water outlet delivers to reuse water spot after fresh water pump (20) supercharging, the entrance of dense water out and one-level two sections of reverse osmosis units (9) of one-level one section of reverse osmosis unit (8) is connected, the water outlet of one-level two sections of reverse osmosis units (9) is connected with second level reverse osmosis apparatus by the road, the water outlet of second level reverse osmosis apparatus is connected with fresh-water tank (19), the dense water out of second level reverse osmosis apparatus is connected with the export pipeline of strainer/ultrafiltration (3) by the road, the dense water out of one-level two sections of reverse osmosis units (9) is connected with another entrance of energy recycle device (10), energy recycle device (10) one outlet is connected with the outlet of one-level high-pressure pump (7) by the road, another outlet is connected with electrolyzer (11), the clorox of electrolyzer (11) output delivers to chemical feeding points by clorox dosing pump (24),
Pipeline between described waste water tank (1) and strainer/ultrafiltration (3) is also provided with lift pump (2);
Described second level reverse osmosis apparatus comprises secondary one section of reverse osmosis unit (16), secondary inter-section booster (18) and two-stage two-segment reverse osmosis unit (17), the entrance of water outlet and secondary one section of reverse osmosis unit (16) of one-level two sections of reverse osmosis units (9) is communicated with, the dense water out of secondary one section of reverse osmosis unit (16) is connected through the entrance of secondary inter-section booster (18) with two-stage two-segment reverse osmosis unit (17), the dense water out of two-stage two-segment reverse osmosis unit (17) is connected with the export pipeline of strainer/ultrafiltration (3), the water outlet of secondary one section of reverse osmosis unit (16) and two-stage two-segment reverse osmosis unit (17) is connected with fresh-water tank (19) respectively.
2. using ion-exchange resin regenerated waste water resource recovering system according to claim 1, is characterized in that: be also provided with filtered water tank (4) between described strainer/ultrafiltration (3) and one-level booster pump (5).
3. using ion-exchange resin regenerated waste water resource recovering system according to claim 1, is characterized in that: described Scale inhibitors chemicals dosing plant comprise Scale inhibitors case (21) and with the anti-sealant dosing pump (22) be connected with the entrance pipe of Scale inhibitors case (21), one-level cartridge filter (6) respectively.
4. using ion-exchange resin regenerated waste water resource recovering system according to claim 1, is characterized in that: the pipeline between described one-level two sections of reverse osmosis units (9) and second level reverse osmosis apparatus is provided with intermediate water tank (12), two stage supercharging pump (13), secondary cartridge filter (14) and secondary high-pressure pump (15) successively.
5. using ion-exchange resin regenerated waste water resource recovering system according to claim 1, is characterized in that: described blower fan (23) adopts roots blower.
6. the using ion-exchange resin regenerated waste water its recovery method as resource as the system in claim 1-5 as described in any one: it is characterized in that: the condensate refining treatment ion exchange resin regeneration waste water containing ammonia is sent into waste water tank (1), controls mixed regeneration waste water ph and reaches more than 10, blast air at waste water tank (1) middle roots blower (23) fully to mix, oxygen supply is simultaneously to be oxidized the Fe that may exist
2+, by lift pump (2), mixed regeneration waste water is sent into strainer/ultrafiltration (3) to remove particle suspensions and iron, water outlet enters filtered water tank (4), by one-level booster pump (5), one-level cartridge filter (6) is sent in filtered water tank (4) water outlet to filter, the Scale inhibitors be stored in Scale inhibitors case (21) is added by anti-sealant dosing pump (22) one-level cartridge filter (6) is front according to operational conditions, one-level cartridge filter (6) water outlet part enters one-level high-pressure pump (7) pressurization, another part enters after energy recycle device (10) carries out energy exchange with the dense water of one-level two sections of reverse osmosis units (9) and together enters one-level one section of reverse osmosis unit (8) with one-level high-pressure pump (7) water outlet, the fresh water of one-level one section of reverse osmosis unit (8) output directly enters fresh-water tank (19) reuse, the fresh water of one-level two sections of reverse osmosis unit (9) outputs enters intermediate water tank (12), the dense water of one-level two sections of reverse osmosis units (9) is delivered to electrolyzer (11) and is carried out preparing chlorine by electrolysis after energy recycle device (10) exchange energy, when reclaiming the condensate refining treatment ion exchange resin regeneration waste water containing ammonia, in electrolyzer (11), also carry out the oxidation removal reaction of ammonia, by two stage supercharging pump (13), secondary cartridge filter (14) is sent in intermediate water tank (12) water outlet to filter, secondary cartridge filter (14) water outlet sends into secondary one section of reverse osmosis unit (16) after secondary high-pressure pump (15) pressurization, the fresh water of secondary one section of reverse osmosis unit (16) output enters fresh-water tank (19), the dense water of secondary one section of reverse osmosis unit (16) enters two-stage two-segment reverse osmosis unit (17) after secondary inter-section booster (18) supercharging, the fresh water of two-stage two-segment reverse osmosis unit (17) output enters fresh-water tank (19), the dense water of two-stage two-segment reverse osmosis unit (17) returns filtered water tank (4) and continues process, fresh-water tank (19) water outlet delivers to reuse water spot after fresh water pump (20) supercharging, the clorox of electrolyzer (11) output delivers to chemical feeding points by clorox dosing pump (24).
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