CN105948364A - Desulfurization wastewater zero discharging treatment system based on bypass flue evaporation - Google Patents
Desulfurization wastewater zero discharging treatment system based on bypass flue evaporation Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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Abstract
The invention provides a desulfurization wastewater zero discharging treatment system based on bypass flue evaporation. The desulfurization wastewater zero discharging treatment system comprises a second-stage precipitation pre-treatment system, a two-membrane concentration and decrement system and a bypass flue evaporation system, wherein desulfurization wastewater enters the two-membrane concentration and decrement system after being treated by the second-stage precipitation pre-treatment system, and concentrated water treated by the two-membrane concentration and decrement system is guided into the bypass flue evaporation system. According to the desulfurization wastewater zero discharging treatment system provided by the invention, suspended solid particles, heavy metal, SO4<2-> and the like can be removed through the second-stage precipitation pre-treatment system, the water quality can be sufficiently softened, and a membrane scaling risk in the two-membrane concentration and decrement system is reduced; water load entering the bypass flue system is effectively reduced by the two-membrane concentration and decrement system, so that the influence on boiler efficiency is reduced; high-temperature flue gas is utilized by a bypass flue, so that energy consumption is reduced, the running cost is effectively reduced, and zero discharge of the desulfurization wastewater is realized.
Description
Technical field
The present invention relates to technical field of waste water processing, particularly relate to desulfurization wastewater zero discharge treatment.
Background technology
Along with China industry develop rapidly, electricity needs rapidly increases, and coal fired power generation is the main generation mode of China's present stage, according to middle Electricity Federation energy-conserving and environment-protective branch issue industry data by August, 2015 China's thermoelectricity generated energy account for the 73.3% of gross generation.Coal combustion produces substantial amounts of pollutant, in order to meet the smoke gas treatment dynamics of country, major part thermal power plant is all configured with desulphurization system, in numerous desulfurization technology, limestone--gypsum wet flue gas desulfurizing technology is high by feat of technology maturation desulfuration efficiency, it is wide to be suitable for coal, by-product cheap to boiler load change strong adaptability, absorbent raw material can the advantage such as reuse, become the first-selection of Desulphurization Process in Thermal Power Plants.
In order to maintain the properly functioning of desulphurization system, prevent desulphurization system material corrosion, chloride ion need to be maintained in serosity in certain concentration by a part of desulfurization wastewater of outer row.Desulfurization wastewater pH is 4.5～6.5, and contains a large amount of SO4 2-, suspended solids, heavy metal ion etc., corrosivity is strong, intractability is big." the water prevention and cure of pollution action plan " promulgated along with in April, 2015 is formally implemented, and electric power enterprise pressure in terms of resource constraint with emission limit suddenly rises, and accelerates to implement degree of depth water saving and wastewater zero discharge has become inevitable choice.And the effectively process of desulfurization wastewater is the key point of restriction coal-burning power plant wastewater zero discharge, it is achieved the demand of desulfurization wastewater zero-emission is the most urgent.
Summary of the invention
The technical problem to be solved in the present invention, is to provide a kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation, concentrates abatement system, bypass flue vapo(u)rization system including two-stage precipitation pretreatment system, bi-membrane method；Described two-stage precipitation pretreatment system includes collecting-tank, one-level flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, the first pond and solid-liquid separator；Described collecting-tank, one-level flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, first ponds are sequentially connected with；Described primary-clarifiers is all connected with described solid-liquid separator with described Secondary clarifier；Added with lime cream, liquid caustic soda, PAC, PAM in described one-level flocculation basin, added with Na in described two grades of flocculation basins2CO3, PAC and PAM, the pH value in described first pond is neutral；Desulfurization wastewater enters described bi-membrane method after described two-stage precipitation pretreatment system processes and concentrates abatement system, concentrates after abatement system processes through described bi-membrane method and introduces described bypass flue vapo(u)rization system, and described bypass flue vapo(u)rization system is provided with gas-solid separating device.
Further, the pH value of described one-level flocculation basin is 9～11.
Further, being equipped with drug feeding pipeline, agitator, overflow pipe in each flocculation basin, described overflow pipe is located at each flocculation basin top, it is ensured that its fully react after overflow to next process, described drug feeding pipeline and described agitator are respectively provided at bottom each flocculation basin.
Further, described defecator includes cantboard clarifier, cyclone clarificator, air float device, and described solid-liquid separator includes filter press device, belt filter press.
Further, according to the difference of water quality, it is determined by experiment described lime cream, liquid caustic soda, CaCO3Addition, described PAC concentration is 80～120ppm, and the concentration of described PAM is 5～15ppm, to reach the most not introduce substantial amounts of calcium ion while sulfate ion, magnesium ion removing, reduces two-stage precipitation reagent cost.
Further, described bi-membrane method concentrates abatement system and includes that multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system, product water tank and dense water tank, described multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system, product water tank are sequentially connected and connect；Described multi-medium filtering machine with described ultrafiltration system respectively collecting-tank with described two-stage precipitation pretreatment system be connected；Described multi-medium filtering machine and described ultrafiltration system, for removing the solid particle impurity in desulfurization wastewater, reduce turbidity of wastewater, and the waste water SDI < 3 after ultrafiltration system processes reaches reverse osmosis membrane influent quality requirement；Desulfurization wastewater after described multi-medium filtering machine and described ultrafiltration system process enters described reverse osmosis membrane system；Described reverse osmosis membrane system uses sea water desalination membrane, and its system reclaims salt rejection rate >=97%, the system response rate >=60%；It is not fresh water and dense water that desulfurization wastewater after sea water desalination membrane processes is divided into two stocks after reclaiming, wherein the fresh water of 60% is used for supplementing sulfur removal technology water, the concentrated stream of 40% enters described bypass flue vapo(u)rization system, reduces the water yield load entering bypass flue, ensures its stable operation；If unit operation load is adjusted, in the case of the dense water of 40% can not evaporate completely, a part of dense water is capable of circulation is again introduced into counter-infiltration system.
Further, described other flue vapo(u)rization system includes flue, cleaner unit between evaporation tube, gas-solid separating device, SCR and air preheater, between described SCR and air preheater, flue contains flue gas, described flue gas is introduced described evaporation tube, described evaporation tube is provided with entrance, the efficient shower nozzle of twin, air compressor machine, electronic isolation baffle plate, motorized adjustment baffle plate, outlet, described entrance is connected with flue between air preheater with described SCR, described outlet is connected with described gas-solid separating device, and described gas-solid separating device is connected with described cleaner unit；Described dense water is delivered to the efficient shower nozzle of described twin through waste pipe, atomization droplets diameter is controlled 40～60um by described air compressor machine regulation gas liquid ratio, in described evaporation tube, flue-gas temperature is high-temperature flue gas when 330～350 DEG C, described atomized drop mixes in evaporation tube with described high-temperature flue gas, realizes high-efficiency evaporating in continuous mass transfer, diabatic process；Described atomized drop contains salts substances, and described salts substances separates out in evaporation process, and the salts substances of precipitation is trapped by described gas-solid separator, and the flue gas after described gas-solid separator separates enters cleaner unit；Described electronic isolation baffle plate can play buffer action when evaporation tube breaks down, and to the stable operation of boiler without negative effect, enters the high-temperature flue gas flow of bypass flue as desired by the regulation of described electric guard board, it is achieved the high-efficiency evaporating of waste water.
Further, described evaporation tube entrance and exit is respectively equipped with thermometer, drimeter, effusion meter and sensor, described sensor connects a computer, on-line monitoring evaporation effect is realized by computer, the high-temperature flue gas flow of bypass flue is entered, it is achieved the high-efficiency evaporating of waste water as desired by electric guard board regulation.
Further, described gas-solid separating device includes sack cleaner, electrostatic precipitator, cyclone dust extractor.
Further, the high salt particle evaporated is collected separately as highway structure material by described gas-solid separating device, it is to avoid the impact on quality of fly ash.
The present invention, by two-stage precipitation pretreatment system, bi-membrane method are concentrated abatement system, these utilizations of rationally arranging of bypass flue vapo(u)rization system, has reached technology process flow process and has been simple and convenient to operate, and floor space is little, capital construction low cost, saves sulfur removal technology water；Wherein, two-stage precipitation pretreatment system can efficiently remove suspended solids, heavy metal, SO4 2-Deng, and water quality is fully softened, reduce and concentrate the risk of film fouling in abatement system；Bi-membrane method concentrates abatement system and effectively reduces the water yield load entering bypass flue system, reduces the impact on boiler efficiency；Bypass flue utilizes high-temperature flue gas, saves energy consumption, effectively reduces operating cost and realizes desulfurization wastewater zero-emission truly；Realized the isolation of itself and boiler body simultaneously by isolation baffle plate, entered the high-temperature flue gas flow of bypass flue by controllable register regulation, while realizing waste water high-efficiency evaporation, ensure the operation stability of boiler；By gas-solid separating device, the high salt particle evaporated is collected separately utilization, it is to avoid impact on quality of fly ash.
Accompanying drawing explanation
The present invention is further illustrated the most in conjunction with the embodiments.
Fig. 1 be invention the overall structure schematic diagram of desulfurization wastewater zero-discharge treatment system.
Detailed description of the invention
Refer to Fig. 1, be a kind of based on bypass flue evaporation the desulfurization wastewater zero-discharge treatment system as highly preferred embodiment of the present invention, concentrate abatement system, bypass flue vapo(u)rization system including two-stage precipitation pretreatment system, bi-membrane method；Described two-stage precipitation pretreatment system includes collecting-tank, one-level flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, the first pond and solid-liquid separator；Described collecting-tank, one-level flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, first ponds are sequentially connected with；Described primary-clarifiers is all connected with described solid-liquid separator with described Secondary clarifier, and described one-level flocculation basin includes that lime cream, liquid caustic soda, PAC, PAM, described two grades of flocculation basins include Na2CO3, PAC and PAM；Desulfurization wastewater enters described bi-membrane method after described two-stage precipitation pretreatment system processes and concentrates abatement system, concentrates after abatement system processes through described bi-membrane method and introduces described bypass flue vapo(u)rization system, and described bypass flue vapo(u)rization system is provided with gas-solid separating device.
Being equipped with drug feeding pipeline, agitator, overflow pipe in each flocculation basin, described overflow pipe is located at each flocculation basin top, it is ensured that its fully react after overflow to next process, described drug feeding pipeline and described agitator are respectively provided at bottom each flocculation basin；Described defecator includes cantboard clarifier, cyclone clarificator, air float device, and described solid-liquid separator includes filter press device, belt filter press.
Bi-membrane method concentrates abatement system and includes multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system, product water tank and dense water tank；Described multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system, product water tank are sequentially connected and connect；Described multi-medium filtering machine with described ultrafiltration system respectively collecting-tank with described two-stage precipitation pretreatment system be connected；Described multi-medium filtering machine and described ultrafiltration system, for removing the solid particle impurity in desulfurization wastewater, reduce turbidity of wastewater, and the waste water SDI < 3 after ultrafiltration system processes reaches reverse osmosis membrane influent quality requirement.
Other flue vapo(u)rization system includes flue, cleaner unit between evaporation tube, gas-solid separating device, SCR and air preheater, between described SCR and air preheater, flue contains flue gas, described flue gas is introduced described evaporation tube, described evaporation tube is provided with entrance, the efficient shower nozzle of twin, air compressor machine, electronic isolation baffle plate, motorized adjustment baffle plate, outlet, described entrance is connected with flue between air preheater with described SCR, outlet is connected with described gas-solid separating device, and described gas-solid separating device is connected with described cleaner unit；Described dense water is delivered to the efficient shower nozzle of described twin through waste pipe, atomization droplets diameter is controlled 40～60um by described air compressor machine regulation gas liquid ratio, in described evaporation tube, flue-gas temperature is high-temperature flue gas when 330～350 DEG C, described atomized drop mixes in evaporation tube with described high-temperature flue gas, realizes high-efficiency evaporating in continuous mass transfer, diabatic process；Described atomized drop contains salts substances, and described salts substances separates out in evaporation process, and the salts substances of precipitation is trapped by described gas-solid separator, and the flue gas after described gas-solid separator separates enters cleaner unit；Described electronic isolation baffle plate can play buffer action when evaporation tube breaks down, and to the stable operation of boiler without negative effect, enters the high-temperature flue gas flow of bypass flue as desired by the regulation of described electric guard board, it is achieved the high-efficiency evaporating of waste water.Described gas-solid separating device includes that high salt particle is collected separately by sack cleaner, electrostatic precipitator, cyclone dust extractor, described gas-solid separating device, as highway structure material, it is to avoid the impact on quality of fly ash.
Entrance and exit at evaporation tube is respectively equipped with thermometer, drimeter, effusion meter and sensor, described sensor connects a computer, on-line monitoring evaporation effect is realized by computer, the high-temperature flue gas flow of bypass flue is entered, it is achieved the high-efficiency evaporating of waste water as desired by electric guard board regulation.
As a example by certain power plant desulfurization waste water quality (table 1) processes, the present invention is described in further detail below.
Certain power plant desulfurization waste water quality of table 1
Desulfurization wastewater enters two-stage precipitation pretreatment system after collecting, in one-level flocculation basin, lime cream, liquid caustic soda and PAC is added by medicine system, pH value controls between 9～11, to remove oil removal, heavy metal, sulfate ion, magnesium ion etc., adds Na in two grades of flocculation basins2CO3, PAC and PAM, with the calcium in removal water, magnesium ion, realize the abundant softening of waste water, water outlet after the large particulate matter clarified device clarification that complex, precipitate and SS after flocculation is formed, bottom of clarifier mud is separated by solid-liquid separator after collecting, reflowable to the described collecting-tank of mud percolate.
Lime cream and the addition of liquid caustic soda in one-level flocculation basin are determined by beaker experiments, for operating mode one water quality, Calx chemical feeding quantity is 12g/L, sodium hydroxide chemical feeding quantity is 10g/L, sodium carbonate chemical feeding quantity is 8g/L, the chemical feeding quantity of PAC be the chemical feeding quantity of 80mg/L, PAM be 5mg/L, reagent cost is 42 yuan/ton；For operating mode two water quality, Calx chemical feeding quantity is 3g/L, and sodium hydroxide chemical feeding quantity is 12g/L, sodium carbonate chemical feeding quantity be the chemical feeding quantity that chemical feeding quantity is 100mg/L, PAM of 2.7g/L, PAC be 10mg/L, reagent cost is 39 yuan/ton；For operating mode three water quality, Calx chemical feeding quantity is 10g/L, and sodium hydroxide chemical feeding quantity is 14g/L, sodium carbonate chemical feeding quantity be the chemical feeding quantity that chemical feeding quantity is 120mg/L, PAM of 4.8g/L, PAC be 15mg/L, reagent cost is 55 yuan/ton；Satisfied through the effluent quality of two-stage precipitation pretreatment, Ca2+Content is less than 250mg/L, Mg2+Content is less than 50mg/L, SO42-Content is about 5000mg/L～6000mg/L.
The two-stage precipitation pretreatment water outlet hydrochloric acid of operating mode three water quality is pulled back to PH to after neutrality, introduce bi-membrane method and concentrate abatement system, ultrafiltration influent quality such as table 2.
Table 2 ultrafiltration influent quality
Ultrafilter membrane is 15L/m at flux2H, pressure is 6.1kPa～6.5kPa, runs 8h, equipment normal operation continuously, and ultra-filtration water turbidity is between 0.09NTU～0.18NTU, and raw water turbidity is 0.83NTU, the ultrafilter membrane clearance ＞ 78% to turbidity.Ultrafiltration is produced water SDI be measured, SDI=2.33, reach reverse osmosis membrane influent quality requirement.Ultrafiltration membrane elements is run infiltration coefficient after 8h and is dropped to 0.00205m/Pa s from initial value 0.00212m/Pa s, and fall is only 3.28%, shows that ultrafilter membrane is not blocked up by dirt, can long-play and without cleaning or only need to use clear water backwash simply.
Further, ultra-filtration water is introduced counter-infiltration system, by parameters such as adjusting high-pressure pump frequency, concentrated water discharge flow, dense water circular flows, control the counter-infiltration system response rate 56%, membrane flux 17.1L/m2H, after counter-infiltration system is stable, run 96h continuously, system running pressure is maintained between 6.58～6.61Mpa, transmembrane pressure is between 12.1～12.4kPa, and the fluctuating margin of pressure reduction is less, and counter-infiltration system salt rejection rate is 97.1%, the salt rejection rate of single film is 99.8%, and desalting effect is preferable.Produce in water and do not detect Ca2+, and dense water side Ca2+Content fluctuating margin is less, illustrates do not have obvious CaSO4Scale formation produces.Producing TOC content in water the lowest, between 0.14mg/L～0.52mg/L, dense water side TOC content fluctuating margin is less, between 35mg/L～37mg/L, illustrates that reverse osmosis membrane does not occur obvious organic fouling.
With generating set for 2 × 350MW, as a example by evaporation tube diameter 900mm, flue gas flow rate controls in 3～5m/s scopes, and the desulfurization wastewater of evaporation 2t/h needs to draw the high-temperature flue gas 19000Nm of 340 DEG C3/ h, after extracting the flue gas of this size, air preheater outlet exhaust gas temperature reduces by 4 DEG C, and air preheater outlet heat primary air temperature reduces by 3 DEG C, and air preheater exports hot secondary wind temperature and reduces by 2 DEG C, only makes boiler thermal effect reduce by 0.1%.
In sum, the present invention by by two-stage precipitation pretreatment system, bi-membrane method concentrate abatement system, bypass flue vapo(u)rization system, these utilizations of rationally arranging of cleaner, reach technology process flow process to be simple and convenient to operate, floor space is little, capital construction low cost, saves sulfur removal technology water；Wherein, two-stage precipitation pretreatment system can efficiently remove suspended solids, heavy metal, SO4 2-Deng, and water quality is fully softened, reduce and concentrate the risk of film fouling in abatement system；Bi-membrane method concentrates abatement system and effectively reduces the water yield load entering bypass flue system, reduces the impact on boiler efficiency；Bypass flue utilizes high-temperature flue gas, saves energy consumption, effectively reduces operating cost and realizes desulfurization wastewater zero-emission truly；Realized the isolation of itself and boiler body simultaneously by isolation baffle plate, entered the high-temperature flue gas flow of bypass flue by controllable register regulation, while realizing waste water high-efficiency evaporation, ensure the operation stability of boiler；High salt particle is collected separately by gas-solid separating device, as highway structure material, ensures the quality of flyash.
Above in conjunction with accompanying drawing, the present invention is exemplarily described; obviously the present invention implements and is not subject to the restrictions described above; if the improvement of the various unsubstantialities that the method design that have employed invention is carried out with technical scheme; or the most improved design by the present invention and technical scheme directly apply to other occasion, all within the protection domain of invention.
Claims (10)
1. a desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation, it is characterised in that include two-stage precipitation pretreatment system
System, bi-membrane method concentrate abatement system, bypass flue vapo(u)rization system；Described two-stage precipitation pretreatment system includes collecting-tank, one-level
Flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, the first pond and solid-liquid separator；Described collecting-tank, one
Level flocculation basin, primary-clarifiers, two grades of flocculation basins, Secondary clarifier, first ponds are sequentially connected with；Described primary-clarifiers and
Described Secondary clarifier is all connected with described solid-liquid separator；In described one-level flocculation basin added with lime cream, liquid caustic soda, PAC,
PAM, added with Na in described two grades of flocculation basins2CO3, PAC and PAM, the pH value in described first pond is neutral；Desulfurization
Waste water enters described bi-membrane method after described two-stage precipitation pretreatment system processes and concentrates abatement system, concentrates through described bi-membrane method and subtracts
Amount system introduces described bypass flue vapo(u)rization system after processing, and described bypass flue vapo(u)rization system is provided with gas-solid separating device.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
The pH value of described one-level flocculation basin is 9～11.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
Being equipped with drug feeding pipeline, agitator, overflow pipe in each flocculation basin, described overflow pipe is located at each flocculation basin top, described chemical feed pipe
Road and described agitator are respectively provided at bottom each flocculation basin.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
Described defecator includes cantboard clarifier, cyclone clarificator, air float device, described solid-liquid separator include filter press device,
Belt filter press.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
Described PAC concentration is 80～120ppm, and the concentration of described PAM is 5～15ppm.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
Described bi-membrane method concentrate abatement system include multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system,
Produce water tank and dense water tank；Described multi-medium filtering machine, the second pond, ultrafiltration system, the 3rd pond, counter-infiltration system, product water
Case is sequentially connected and connects；Described multi-medium filtering machine and described ultrafiltration system respectively with the collecting-tank of described two-stage precipitation pretreatment system
It is connected；Desulfurization wastewater after described multi-medium filtering machine and described ultrafiltration system process enters described reverse osmosis membrane system；Described
Reverse osmosis membrane system uses sea water desalination membrane, and it is not fresh water and dense water that the desulfurization wastewater after sea water desalination membrane processes is divided into two stocks,
Described fresh water is used for supplementing sulfur removal technology water, and described dense water introduces described bypass flue vapo(u)rization system.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 1, it is characterised in that
Described other flue vapo(u)rization system includes flue, cleaner unit between evaporation tube, gas-solid separating device, SCR and air preheater, described SCR
And flue contains flue gas between air preheater, described flue gas being introduced described evaporation tube, described evaporation tube is provided with entrance, twin
Efficiently shower nozzle, air compressor machine, electronic isolation baffle plate, motorized adjustment baffle plate, outlet, between described entrance and described SCR and air preheater
Flue connects, and described outlet is connected with described gas-solid separating device, and described gas-solid separating device is connected with described cleaner unit；Described
Dense water is delivered to the efficient shower nozzle of described twin through waste pipe, controls atomized drop by described air compressor machine regulation gas liquid ratio
Particle diameter is 40～60um, and in described evaporation tube, flue-gas temperature is high-temperature flue gas when 330～350 DEG C, and described atomized drop is with described
High-temperature flue gas mixes evaporation in evaporation tube, and described atomized drop contains salts substances, and described salts substances is analysed in evaporation process
Going out, the salts substances of precipitation is trapped by described gas-solid separator, and the flue gas after described gas-solid separator separates enters cleaner unit.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 7, it is characterised in that
Described evaporation tube entrance and exit is respectively equipped with thermometer, drimeter, effusion meter and sensor, and described sensor connects a calculating
Machine, realizes on-line monitoring evaporation effect by computer.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 7, it is characterised in that
Described gas-solid separating device includes sack cleaner, electrostatic precipitator, cyclone dust extractor.
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation the most according to claim 9, it is characterised in that
The high salt particle evaporated is collected separately as highway structure material by described gas-solid separating device.
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106587231A (en) * | 2017-01-23 | 2017-04-26 | 麦克罗特技术无锡有限公司 | FGD wastewater zero discharge system |
| CN106843295A (en) * | 2017-03-06 | 2017-06-13 | 浙江浙能技术研究院有限公司 | A kind of gas bypass evaporates desulfurization wastewater system control method and control system |
| CN107089755A (en) * | 2017-06-12 | 2017-08-25 | 杭州云众电力科技有限公司 | A kind of desulfurization wastewater Zero discharging system device evaporated after concentration with drying tower |
| CN107129094A (en) * | 2017-06-08 | 2017-09-05 | 上海电力学院 | The Zero discharging system of desulfurization wastewater is evaporated based on multi-heat source |
| CN109292866A (en) * | 2018-11-26 | 2019-02-01 | 伍育毅 | A kind of desulfurizing waste water processing device and processing method |
| CN109336202A (en) * | 2018-11-20 | 2019-02-15 | 国电龙源节能技术有限公司 | Desulfurization wastewater vaporising device and control method |
| CN109453642A (en) * | 2018-10-24 | 2019-03-12 | 东莞理工学院 | Chemical laboratory rubbish processing to be harmless system |
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| CN109650476A (en) * | 2019-01-11 | 2019-04-19 | 东南大学 | A kind of desulfurization wastewater zero-emission system and method |
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| CN106587231A (en) * | 2017-01-23 | 2017-04-26 | 麦克罗特技术无锡有限公司 | FGD wastewater zero discharge system |
| CN106843295B (en) * | 2017-03-06 | 2023-05-12 | 浙江浙能长兴发电有限公司 | Control method and control system for flue gas bypass evaporation desulfurization wastewater system |
| CN106843295A (en) * | 2017-03-06 | 2017-06-13 | 浙江浙能技术研究院有限公司 | A kind of gas bypass evaporates desulfurization wastewater system control method and control system |
| CN107129094A (en) * | 2017-06-08 | 2017-09-05 | 上海电力学院 | The Zero discharging system of desulfurization wastewater is evaporated based on multi-heat source |
| CN107129094B (en) * | 2017-06-08 | 2020-07-17 | 上海电力学院 | Zero discharge system based on multi-heat-source evaporation desulfurization waste water |
| CN107089755A (en) * | 2017-06-12 | 2017-08-25 | 杭州云众电力科技有限公司 | A kind of desulfurization wastewater Zero discharging system device evaporated after concentration with drying tower |
| CN109534567A (en) * | 2017-09-22 | 2019-03-29 | 上海江柘环境工程技术有限公司 | A kind of desulfurization wastewater treatment system |
| CN109453642A (en) * | 2018-10-24 | 2019-03-12 | 东莞理工学院 | Chemical laboratory rubbish processing to be harmless system |
| CN109336202A (en) * | 2018-11-20 | 2019-02-15 | 国电龙源节能技术有限公司 | Desulfurization wastewater vaporising device and control method |
| CN109292866A (en) * | 2018-11-26 | 2019-02-01 | 伍育毅 | A kind of desulfurizing waste water processing device and processing method |
| CN109650476A (en) * | 2019-01-11 | 2019-04-19 | 东南大学 | A kind of desulfurization wastewater zero-emission system and method |
| CN111807543A (en) * | 2020-06-30 | 2020-10-23 | 武汉钢铁有限公司 | Zero-discharge treatment method and system for acid-making wastewater of low-cost sintering activated carbon desulfurization process |
| CN112939287A (en) * | 2021-03-25 | 2021-06-11 | 四川恩特普环保科技有限公司 | Sulfuric acid production wastewater treatment method |
| CN113943072A (en) * | 2021-10-18 | 2022-01-18 | 华电水务工程有限公司 | Zero-discharge system and process for tail-end wastewater of direct-current cooling power plant |
| CN113943072B (en) * | 2021-10-18 | 2024-03-08 | 华电水务工程有限公司 | Zero discharge system and process for tail end wastewater of direct-current cooling power plant |
| CN114735869A (en) * | 2021-12-27 | 2022-07-12 | 国能铜陵发电有限公司 | Method for removing ions from desulfurized slurry and solidifying high-temperature flue gas bypass of concentrated solution |
| CN114477595A (en) * | 2022-02-23 | 2022-05-13 | 杰瑞环境工程技术有限公司 | Wastewater treatment system |
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