CN105948364B - A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation - Google Patents
A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation Download PDFInfo
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- CN105948364B CN105948364B CN201610528018.8A CN201610528018A CN105948364B CN 105948364 B CN105948364 B CN 105948364B CN 201610528018 A CN201610528018 A CN 201610528018A CN 105948364 B CN105948364 B CN 105948364B
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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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- 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
- C02F1/001—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
Abstract
The present invention provides a kind of desulfurization wastewater zero-discharge treatment systems based on bypass flue evaporation, abatement system, bypass flue vapo(u)rization system is concentrated including two-stage precipitation pretreatment system, bi-membrane method, desulfurization wastewater enters the bi-membrane method after two-stage precipitation pretreatment system processing and abatement system is concentrated, and bi-membrane method concentration abatement system treated concentrated water is introduced the bypass flue vapo(u)rization system.Two-stage precipitation pretreatment system of the invention can remove suspended solid particles, heavy metal, SO4 2‑Deng, and water quality is sufficiently softened, reduce the risk of film fouling in concentration abatement system；Bi-membrane method concentration abatement system effectively reduces the water load into bypass flue system, reduces the influence to boiler efficiency；Bypass flue utilizes high-temperature flue gas, saves energy consumption, operating cost is effectively reduced and realizes desulfurization wastewater zero-emission.
Description
Technical field
The present invention relates to technical field of waste water processing more particularly to desulfurization wastewater zero discharge treatments.
Background technique
With the rapid development of China's industry, electricity needs rapidly increases, and coal fired power generation is China's at this stage main
Generation mode accounts for about always according to the industry data that middle Electricity Federation energy conservation and environmental protection branch issues by 2015 China Nian8Yue thermoelectricity generated energy
The 73.3% of generated energy.Coal combustion generates a large amount of pollutant, in order to meet the smoke gas treatment dynamics of country, most of thermal power plant
It is all configured with desulphurization system, in numerous desulfurization technologies, lime stone -- gypsum wet flue gas desulfurizing technology is by feat of technology maturation
Desulfuration efficiency is high, it is wide to be applicable in coal, to boiler load change adaptable, absorbent raw material are cheap, by-product can reuse etc.
Advantage becomes the first choice of Desulphurization Process in Thermal Power Plants.
In order to maintain the normal operation of desulphurization system, desulphurization system material corrosion is prevented, a part of desulfurization of outlet need to be passed through
Waste water maintains in slurries the chloride ion in certain concentration.Desulfurization wastewater pH contains a large amount of SO 4.5~6.54 2-, suspend it is solid
Body particle, heavy metal ion etc., corrosivity is strong, processing difficulty is big." the water prevention and cure of pollution action meter promulgated in April, 2015
Draw " it is formal implement, pressure of the electric power enterprise in terms of resource constraint with emission limit suddenly rises, quickening implement depth it is water-saving with
Wastewater zero discharge has become inevitable choice.And being effectively treated for desulfurization wastewater is the key that restrict coal-burning power plant's wastewater zero discharge institute
Realizing that the demand of desulfurization wastewater zero-emission is especially urgent.
Summary of the invention
The technical problem to be solved in the present invention is to provide at a kind of desulfurization wastewater zero-emission based on bypass flue evaporation
Abatement system, bypass flue vapo(u)rization system is concentrated in reason system, including two-stage precipitation pretreatment system, bi-membrane method；The second level is heavy
Shallow lake pretreatment system include collecting-tank, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, the first pond and
Solid-liquid separator；The collecting-tank, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, the first pond according to
Secondary connection；The primary-clarifiers and the Secondary clarifier are connected with the solid-liquid separator；The level-one flocculation basin
In added with milk of lime, liquid alkaline, PAC, PAM, added with Na in the second level flocculation basin2CO3, PAC and PAM, the PH in first pond
Value is neutrality；Desulfurization wastewater enters the bi-membrane method after two-stage precipitation pretreatment system processing and abatement system, warp is concentrated
The bypass flue vapo(u)rization system is introduced after the bi-membrane method concentration abatement system processing, the bypass flue vapo(u)rization system is equipped with
Gas-solid separating device.
Further, the pH value of the level-one flocculation basin is 9~11.
Further, drug feeding pipeline, blender, overflow pipe are equipped in each flocculation basin, the overflow pipe is located at each flocculation
At the top of pond, guarantee that overflow to next process, the drug feeding pipeline and the blender is respectively provided at each wadding after it is sufficiently reacted
Solidifying bottom of pond portion.
Further, the clarifier includes cantboard clarifier, cyclone clarificator, air float device, the separation of solid and liquid
Device includes plate compression device, belt pressure filter.
Further, according to the difference of water quality, the milk of lime, liquid alkaline, CaCO are determined by experiment3Additional amount, institute
Stating PAC concentration is 80~120ppm, the concentration of the PAM is 5~15ppm, to reach in removal sulfate ion, magnesium ion
It does not introduce a large amount of calcium ion again simultaneously, reduces two-stage precipitation reagent cost.
Further, bi-membrane method concentration abatement system includes multi-medium filtering machine, the second pond, ultrafiltration system, the
Three ponds, counter-infiltration system, water producing tank and concentrated water case, the multi-medium filtering machine, the second pond, ultrafiltration system, third pond,
Counter-infiltration system, water producing tank, which are sequentially connected, to be connect；The multi-medium filtering machine and the ultrafiltration system respectively with the two-stage precipitation
The collecting-tank of pretreatment system is connected；The multi-medium filtering machine and the ultrafiltration system are for removing consolidating in desulfurization wastewater
Body granulometric impurity reduces turbidity of wastewater, through ultrafiltration system treated waste water SDI < 3, reaches reverse osmosis membrane influent quality requirement；
The multi-medium filtering machine and the ultrafiltration system treated desulfurization wastewater enter the reverse osmosis membrane system；It is described reverse osmosis
Membranous system uses sea water desalination membrane, and system recycles salt rejection rate >=97%, the system rate of recovery >=60%；Through sea water desalination film process
Being divided into two stocks after desulfurization wastewater recycling afterwards is not fresh water and concentrated water, wherein 60% fresh water is for supplementing sulfur removal technology use
Water, 40% concentrated water flow into the bypass flue vapo(u)rization system, reduce the water load for entering bypass flue, ensure that it stablizes fortune
Row；If unit operating load is adjusted, in the case that 40% concentrated water is unable to evaporating completely, a part of concentrated water is recyclable again
Into counter-infiltration system.
Further, the other flue vapo(u)rization system include flue between evaporation tube, gas-solid separating device, SCR and air preheater,
Deduster, flue contains flue gas between the SCR and air preheater, the flue gas is introduced the evaporation tube, the evaporation tube is equipped with
The efficient spray head of entrance, twin, air compressor machine, electronic isolation baffle plate, motorized adjustment baffle, outlet, the entrance with it is described
Flue connects between SCR and air preheater, and the outlet is connect with the gas-solid separating device, and the gas-solid separating device is removed with described
The connection of dirt device；The concentrated water is delivered to the efficient spray head of the twin through waste pipe, adjusts gas by the air compressor machine
It is high-temperature flue gas at 330~350 DEG C that liquor ratio, which controls atomization droplets diameter flue-gas temperature in 40~60um, the evaporation tube,
The atomized drop mixes in evaporation tube with the high-temperature flue gas, realizes high-efficiency evaporating in continuous mass transfer, diabatic process；Institute
It states atomized drop and contains salts substances, the salts substances are precipitated in evaporation process, and the salts substances of precipitation are by the gas-solid
Separator trapping, the flue gas after gas-solid separator separation enter deduster；The electronic isolation baffle plate is sent out in evaporation tube
Buffer action can be played when raw failure, and to the stable operation of boiler without negative effect, as desired by the electric guard board
The high-temperature flue gas flow for entering bypass flue is adjusted, realizes the high-efficiency evaporating of waste water.
Further, the evaporation tube entrance and exit is respectively equipped with thermometer, hygrometer, flowmeter and sensor, institute
It states sensor and connects a computer, on-line monitoring evaporation effect is realized by computer, is adjusted as desired by electric guard board
Into the high-temperature flue gas flow of bypass flue, the high-efficiency evaporating of waste water is realized.
Further, the gas-solid separating device includes bag filter, electrostatic precipitator, cyclone dust collectors.
Further, the high salt particle evaporated is collected separately as highway structure material the gas-solid separating device,
Avoid the influence to quality of fly ash.
The present invention by by two-stage precipitation pretreatment system, bi-membrane method be concentrated abatement system, bypass flue vapo(u)rization system this
Several reasonable arrangements utilize, and have reached technology process process and have been simple and convenient to operate, and occupied area is small, capital construction is at low cost, save de-
Sulphur process water；Wherein, two-stage precipitation pretreatment system can efficiently remove suspended solid particles, heavy metal, SO4 2-Deng, and to water
Matter is sufficiently softened, and the risk of film fouling in concentration abatement system is reduced；Bi-membrane method concentration abatement system effectively reduces
Into the water load of bypass flue system, reduce the influence to boiler efficiency；Bypass flue utilizes high-temperature flue gas, saves energy
Operating cost and the desulfurization wastewater zero-emission of realization truly is effectively reduced in consumption；Simultaneously by isolation baffle plate realize its with
The isolation of boiler body adjusts the high-temperature flue gas flow for entering bypass flue by controllable register, is realizing waste water high-efficiency evaporation
While, ensure the operation stability of boiler；Utilization is collected separately in the high salt particle evaporated by gas-solid separating device,
Avoid the influence to quality of fly ash.
Detailed description of the invention
The present invention is further illustrated in conjunction with the embodiments with reference to the accompanying drawings.
Fig. 1 is the overall structure diagram of the desulfurization wastewater zero-discharge treatment system of invention.
Specific embodiment
Referring to Fig. 1, being a kind of desulfurization wastewater zero based on bypass flue evaporation as highly preferred embodiment of the present invention
Abatement system, bypass flue vapo(u)rization system is concentrated in discharge treating system, including two-stage precipitation pretreatment system, bi-membrane method；It is described
Two-stage precipitation pretreatment system includes collecting-tank, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, first
Pond and solid-liquid separator；The collecting-tank, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, first
Pond is sequentially connected；The primary-clarifiers and the Secondary clarifier are connected with the solid-liquid separator, the level-one
Flocculation basin includes milk of lime, liquid alkaline, PAC, PAM, and the second level flocculation basin includes Na2CO3, PAC and PAM；Described in desulfurization wastewater warp
Enter the bi-membrane method after the processing of two-stage precipitation pretreatment system and abatement system is concentrated, at bi-membrane method concentration abatement system
The bypass flue vapo(u)rization system is introduced after reason, the bypass flue vapo(u)rization system is equipped with gas-solid separating device.
Drug feeding pipeline, blender, overflow pipe are equipped in each flocculation basin, the overflow pipe is located at the top of each flocculation basin, is protected
It demonstrate,proves overflow to next process, the drug feeding pipeline and the blender after it is sufficiently reacted and is respectively provided at each flocculation bottom of pond portion；
The clarifier includes cantboard clarifier, cyclone clarificator, air float device, the solid-liquid separator include plate compression device,
Belt pressure filter.
Bi-membrane method concentration abatement system includes multi-medium filtering machine, the second pond, ultrafiltration system, third pond, reverse osmosis
System, water producing tank and concentrated water case；The multi-medium filtering machine, the second pond, ultrafiltration system, third pond, counter-infiltration system, production
Water tank, which is sequentially connected, to be connect；The multi-medium filtering machine and the ultrafiltration system collection with the two-stage precipitation pretreatment system respectively
Pond is connected；The multi-medium filtering machine and the ultrafiltration system are used to remove the solia particle impurity in desulfurization wastewater, drop
Low turbidity of wastewater reaches reverse osmosis membrane influent quality requirement through ultrafiltration system treated waste water SDI < 3.
Other flue vapo(u)rization system includes flue, deduster between evaporation tube, gas-solid separating device, SCR and air preheater, described
Flue contains flue gas between SCR and air preheater, the flue gas is introduced the evaporation tube, the evaporation tube is equipped with entrance, two-fluid
Atomization high-efficiency spray head, air compressor machine, electronic isolation baffle plate, motorized adjustment baffle, outlet, the entrance and the SCR and air preheater
Between flue connect, outlet connect with the gas-solid separating device, the gas-solid separating device is connect with the deduster；It is described
Concentrated water is delivered to the efficient spray head of the twin through waste pipe, adjusts gas liquid ratio by the air compressor machine and controls atomized liquid
Drip partial size in 40~60um, the evaporation tube flue-gas temperature at 330~350 DEG C be high-temperature flue gas, the atomized drop with
The high-temperature flue gas mixes in evaporation tube, realizes high-efficiency evaporating in continuous mass transfer, diabatic process；The atomized drop contains
Salts substances, the salts substances are precipitated in evaporation process, and the salts substances of precipitation are trapped by the gas-solid separator, through institute
Flue gas after stating gas-solid separator separation enters deduster；The electronic isolation baffle plate can be played when evaporation tube breaks down every
It is adjusted as desired by the electric guard board without negative effect from effect, and to the stable operation of boiler and enters bypass flue
High-temperature flue gas flow, realize the high-efficiency evaporating of waste water.The gas-solid separating device include bag filter, electrostatic precipitator,
High salt particle is collected separately for cyclone dust collectors, the gas-solid separating device, is used as highway structure material, avoids to flyash product
The influence of matter.
It is respectively equipped with thermometer, hygrometer, flowmeter and sensor in the entrance and exit of evaporation tube, the sensor connects
A computer is connect, on-line monitoring evaporation effect is realized by computer, is adjusted as desired by electric guard board and enters bypass cigarette
The high-temperature flue gas flow in road, realizes the high-efficiency evaporating of waste water.
The present invention is described in further detail by taking the processing of certain power plant desulfurization wastewater water quality (table 1) as an example below.
Certain the power plant desulfurization wastewater water quality of table 1
Desulfurization wastewater enters two-stage after collecting and precipitates pretreatment system, is added in level-one flocculation basin by medicine system
Milk of lime, liquid alkaline and PAC, pH value controls between 9~11, to remove oil removal, heavy metal, sulfate ion, magnesium ion
Deng Na is added in second level flocculation basin2CO3, PAC and PAM the abundant softening of waste water realized with the calcium and magnesium ion gone in water removal,
It is discharged after the clarified device clarification of the large particulate matter that complex compound, sediment and SS after flocculation are formed, bottom of clarifier sludge
It is separated after collecting by solid-liquid separator, the sludge percolate collecting-tank.
The additional amount of milk of lime and liquid alkaline in level-one flocculation basin is determined by beaker experiments, for one water quality of operating condition, stone
Grey dosage is 12g/L, and sodium hydroxide dosage is 10g/L, and sodium carbonate dosage is 8g/L, and the dosage of PAC is 80mg/L,
The dosage of PAM is 5mg/L, and reagent cost is 42 yuan/ton；For two water quality of operating condition, lime dosage is 3g/L, sodium hydroxide
Dosage is 12g/L, and sodium carbonate dosage is 2.7g/L, and the dosage of PAC is 100mg/L, and the dosage of PAM is 10mg/L,
Reagent cost is 39 yuan/ton；For three water quality of operating condition, lime dosage is 10g/L, and sodium hydroxide dosage is 14g/L, carbonic acid
Sodium dosage is 4.8g/L, and the dosage of PAC is 120mg/L, and the dosage of PAM is 15mg/L, and reagent cost is 55 yuan/ton；
Meet through the pretreated effluent quality of two-stage precipitation, Ca2+Content is lower than 250mg/L, Mg2+Content is lower than 50mg/L, SO42-Content
About 5000mg/L~6000mg/L.
After the two-stage precipitation pretreatment water outlet of three water quality of operating condition is pulled back to PH to neutrality with hydrochloric acid, bi-membrane method concentration is introduced
Abatement system, ultrafiltration influent quality such as table 2.
2 ultrafiltration influent quality of table
Ultrafiltration membrane is 15L/m in flux2H, pressure be 6.1kPa~6.5kPa, continuous operation 8h, equipment normal operation,
Ultra-filtration water turbidity is between 0.09NTU~0.18NTU, raw water turbidity 0.83NTU, removal rate > of the ultrafiltration membrane to turbidity
78%.It produces water SDI to ultrafiltration to be measured, SDI=2.33 reaches reverse osmosis membrane influent quality requirement.Ultrafiltration membrane elements operation
Infiltration coefficient drops to 0.00205m/Pas from initial value 0.00212m/Pas after 8h, and fall is only 3.28%, table
Bright ultrafiltration membrane is not stifled by dirt, can long-play clear water backwash need to be simply used without cleaning or only.
Further, ultra-filtration water is introduced into counter-infiltration system, by adjusting high-pressure pump frequency, concentrated water discharge flow, dense
The parameters such as water circular flow control the counter-infiltration system rate of recovery 56%, membrane flux 17.1L/m2H is run to counter-infiltration system
After stabilization, continuous operation 96h, system running pressure is maintained between 6.58~6.61Mpa, transmembrane pressure 12.1~
Between 12.4kPa, the fluctuating range of pressure difference is smaller, and counter-infiltration system salt rejection rate is 97.1%, and the salt rejection rate of single branch film is
99.8%, desalting effect is preferable.It produces in water and Ca is not detected2+, and concentrated water side Ca2+Content fluctuating range is smaller, illustrates unobvious
CaSO4Scale formation generates.It is very low to produce TOC content in water, between 0.14mg/L~0.52mg/L, concentrated water side TOC content
Fluctuating range is smaller, and between 35mg/L~37mg/L, illustrating reverse osmosis membrane, there is no apparent organic foulings.
With generating set for 2 × 350MW, for evaporating pipe diameter 900mm, flue gas flow rate control is steamed in 3~5m/s range
The desulfurization wastewater of hair 2t/h needs to draw 340 DEG C of high-temperature flue gas 19000Nm3/ h, after the flue gas for extracting the size, air preheater goes out
Mouth exhaust gas temperature reduces by 4 DEG C, and air preheater, which exports heat primary air temperature, reduces by 3 DEG C, and air preheater exports hot Secondary Air temperature reduction by 2
DEG C, so that boiler thermal effect is reduced by 0.1%.
In conclusion of the invention by the way that abatement system, bypass flue is concentrated in two-stage precipitation pretreatment system, bi-membrane method
These the rationally arrangement utilizations of vapo(u)rization system, cleaner, have reached technology process process and have been simple and convenient to operate, occupied area
It is small, capital construction is at low cost, save sulfur removal technology water；Wherein, two-stage precipitation pretreatment system can efficiently remove suspended solid particles,
Heavy metal, SO4 2-Deng, and water quality is sufficiently softened, reduce the risk of film fouling in concentration abatement system；Bi-membrane method is dense
Reduction system effectively reduces the water load into bypass flue system, reduces the influence to boiler efficiency；Bypass flue
Using high-temperature flue gas, energy consumption is saved, operating cost and the desulfurization wastewater zero-emission of realization truly is effectively reduced；Lead to simultaneously
It crosses isolation baffle plate and realizes its being isolated with boiler body, the high-temperature flue gas flow for entering bypass flue is adjusted by controllable register,
While realizing waste water high-efficiency evaporation, the operation stability of boiler has been ensured；Gas-solid separating device individually receives high salt particle
Collection is used as highway structure material, ensures the quality of flyash.
The present invention is exemplarily described above in conjunction with attached drawing, it is clear that the present invention implements not by aforesaid way
Limitation, it is or not improved as long as using the method concept of invention and the improvement of various unsubstantialities that technical solution carries out
The conception and technical scheme of the invention are directly applied to other occasions, within the protection scope of invention.
Claims (4)
1. a kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation, which is characterized in that pre- including two-stage precipitation
Abatement system, bypass flue vapo(u)rization system is concentrated in processing system, bi-membrane method；The two-stage precipitation pretreatment system includes catchmenting
Pond, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, the first pond and solid-liquid separator；It is described to catchment
Pond, level-one flocculation basin, primary-clarifiers, second level flocculation basin, Secondary clarifier, the first pond are sequentially connected；The level-one clarification
Device and the Secondary clarifier are connected with the solid-liquid separator, and primary-clarifiers and Secondary clarifier base sludge are through receiving
It is separated after collection by solid-liquid separator, the sludge percolate collecting-tank；Added with lime in the level-one flocculation basin
Cream, liquid alkaline, PAC, PAM, added with Na in the second level flocculation basin2CO3, PAC and PAM, the pH value in first pond is neutrality；
Desulfurization wastewater enters the bi-membrane method after two-stage precipitation pretreatment system processing and abatement system is concentrated, through the bi-membrane method
The bypass flue vapo(u)rization system is introduced after concentration abatement system processing, the bypass flue vapo(u)rization system is filled equipped with gas solid separation
It sets, the pH value of the level-one flocculation basin is equipped with drug feeding pipeline, blender and overflow pipe in 9~11, each flocculation basin, described to overflow
Flow tube is located at the top of each flocculation basin, and the drug feeding pipeline and the blender are respectively provided at each flocculation bottom of pond portion, the clarifier
Including cantboard clarifier, cyclone clarificator or air float device, the solid-liquid separator includes plate compression device or belt filters pressing
Device, the PAC concentration are 80~120ppm, and the concentration of the PAM is 5~15ppm, and the bi-membrane method concentration abatement system includes
Multi-medium filtering machine, the second pond, ultrafiltration system, third pond, counter-infiltration system, water producing tank and concentrated water case；The multimedium
Filter, the second pond, ultrafiltration system, third pond, counter-infiltration system, water producing tank are sequentially connected and connect；The multi-medium filtering
Machine and the ultrafiltration system are connected with the collecting-tank of the two-stage precipitation pretreatment system respectively；The multi-medium filtering machine and
The ultrafiltration system treated desulfurization wastewater enters the reverse osmosis membrane system；The reverse osmosis membrane system uses sea water desalination
Film, through sea water desalination membrane, treated that desulfurization wastewater is divided into that two stocks are not fresh water and concentrated water, and the fresh water is for supplementing desulfurization
Process water, the concentrated water introduce the bypass flue vapo(u)rization system, and the bypass flue vapo(u)rization system includes evaporation tube, gas-solid
Flue, the first deduster between separator, SCR and air preheater, flue contains flue gas between the SCR and air preheater, by the cigarette
Gas introduces the evaporation tube, and the evaporation tube is equipped with entrance, the efficient spray head of twin, air compressor machine, electronic isolation baffle plate, electricity
Dynamic controllable register, outlet, flue connects between the entrance and the SCR and air preheater, and the outlet is filled with the gas solid separation
Connection is set, the gas-solid separating device is connect with first deduster；The concentrated water is delivered to the double fluid through waste pipe
Body atomization high-efficiency spray head adjusts gas liquid ratio by the air compressor machine and controls atomization droplets diameter in 40~60um, the evaporation tube
Interior flue-gas temperature is high-temperature flue gas at 330~350 DEG C, and the atomized drop mixes steaming with the high-temperature flue gas in evaporation tube
Hair, the atomized drop contain salts substances, and the salts substances are precipitated in evaporation process, and the salts substances of precipitation are described
Gas-solid separating device trapping, the flue gas after gas-solid separating device separation enter the first deduster.
2. a kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation according to claim 1, feature
It is, the evaporation tube entrance and exit is respectively equipped with thermometer, hygrometer, flowmeter and sensor, the sensor connection
One computer realizes on-line monitoring evaporation effect by computer.
3. a kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation according to claim 1, feature
It is, the gas-solid separating device includes bag filter, electrostatic precipitator or cyclone dust collectors.
4. a kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation according to claim 1, feature
It is, the high salt particle evaporated is collected separately as highway structure material the gas-solid separating device.
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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 |
| 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 |
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| CN111807543B (en) * | 2020-06-30 | 2022-09-27 | 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 |
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| 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 |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001179047A (en) * | 1999-12-24 | 2001-07-03 | Toshiba Corp | Wastewater treatment facility |
| CN204474356U (en) * | 2014-12-05 | 2015-07-15 | 浙江浙能技术研究院有限公司 | A kind of heat-engine plant wet desulfurization wastewater flue atomization evaporate to dryness treatment unit |
| CN104926008A (en) * | 2014-03-18 | 2015-09-23 | 王辛平 | Wet desulfurization wastewater zero emission process and device thereof |
| CN105481157A (en) * | 2015-12-18 | 2016-04-13 | 王辛平 | Method for zero emission treatment of desulfurization waste water based on flue gas waste heat evaporation |
| CN205856232U (en) * | 2016-07-05 | 2017-01-04 | 盛发环保科技（厦门）有限公司 | A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation |
-
2016
- 2016-07-05 CN CN201610528018.8A patent/CN105948364B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001179047A (en) * | 1999-12-24 | 2001-07-03 | Toshiba Corp | Wastewater treatment facility |
| CN104926008A (en) * | 2014-03-18 | 2015-09-23 | 王辛平 | Wet desulfurization wastewater zero emission process and device thereof |
| CN204474356U (en) * | 2014-12-05 | 2015-07-15 | 浙江浙能技术研究院有限公司 | A kind of heat-engine plant wet desulfurization wastewater flue atomization evaporate to dryness treatment unit |
| CN105481157A (en) * | 2015-12-18 | 2016-04-13 | 王辛平 | Method for zero emission treatment of desulfurization waste water based on flue gas waste heat evaporation |
| CN205856232U (en) * | 2016-07-05 | 2017-01-04 | 盛发环保科技（厦门）有限公司 | A kind of desulfurization wastewater zero-discharge treatment system based on bypass flue evaporation |
Non-Patent Citations (1)
| Title |
|---|
| 燃煤电厂脱硫废水烟气余热蒸发零排放工程的设计与应用;张净瑞等;《电力科技与环保》;20160615;第32卷(第03期);第17-20页第1-2节 |
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