CN109052534A - A method of desulfurization wastewater zero-emission is evaporated using fume afterheat - Google Patents
A method of desulfurization wastewater zero-emission is evaporated using fume afterheat Download PDFInfo
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- CN109052534A CN109052534A CN201810795713.XA CN201810795713A CN109052534A CN 109052534 A CN109052534 A CN 109052534A CN 201810795713 A CN201810795713 A CN 201810795713A CN 109052534 A CN109052534 A CN 109052534A
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- flue gas
- desulfurization wastewater
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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
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
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Abstract
The invention discloses a kind of methods using fume afterheat evaporation desulfurization wastewater zero-emission, desulfurization wastewater passes through circulating pump after mixing, enter concentration tower by recycling water spray system, enter concentration tower using flue gas blower and concentration desulfurization wastewater heat exchange is evaporated, concentration tower is discharged through demister in the flue gas of the moisture content containing evaporation, return to flue, into desulfurizing tower, complete concentration desulfurization wastewater is not evaporated, fall into concentration tower bottom liquid storage area with newly mixed into desulfurization wastewater, a certain amount of concentration desulfurization wastewater is extracted to enter in clarifying basin, body refuse is precipitated in clarifying basin, and sludge dewatering equipment is delivered to by slush pump, mud cake is formed individually to handle, separation waste water returns to clarifying basin, desulfurization wastewater after clarifying in clarifying basin enters circular treatment in concentration tower, the invention utilizes the heat of vaporization desulfurization wastewater of residual heat from boiler fume, reach the treatment of wastes with processes of wastes against one another and desulfurization The purpose of wastewater zero discharge, with saving, investment, operating cost is low, is not required to add the advantages such as any chemicals.
Description
Technical field
The present invention relates to desulfurization wastewater zero-discharge technology fields, specially a kind of to evaporate desulfurization wastewater zero using fume afterheat
The method of discharge.
Background technique
Domestic thermal power plant at present usually contains a certain amount of SO2, SO3, mesh due to coal-fired in boiler smoke
The sulfur method that the preceding country mainly uses for lime stone-gypsum wet flue gas desulfurizing technique, the technique in the process of running, cigarette
HCL, particulate matter, heavy metal in gas etc. are constantly enriched in desulfurization slurry, and enrichment can cause desulfuration efficiency to drop to a certain extent
The various problems such as low, equipment corrosion acceleration, it is therefore necessary to a certain amount of waste water be discharged to control various impurity in desulfurization slurry
Concentration, this effluent part are that desulfurization is useless.
Most domestic desulfurization wastewater zero-discharge technology is also in starting conceptual phase, mainstream both direction difference at present
Are as follows: one, utilize electric heating evaporative crystallization；Two, it is evaporated using high-temperature flue gas.
Using the method for electric heating evaporative crystallization, due under this process route, desulfurization wastewater soften pre- early period
Processing and film filtering and concentrating decrement treatment, equipment early investment is big, and occupation area of equipment is big.And utilize " softening+film is concentrated "
Process route technological operation is more complex, and is determined according to the characteristics of film itself, and desulfurization wastewater is unable to arbitrary proportion concentration decrement,
There are certain upper physical limits, and referring to general desulfurization wastewater concentration, 50% or so, and the throwing of medicament can only be concentrated in usual film concentration
With can generate additional operating cost, and crystallization is evaporated using electrically heated method, needs additional power supply, increase hair
The cost of electricity, operating cost are high.
The process route evaporated using high-temperature flue gas, the route can not need to carry out softening pre- place to waste water lower early period
Reason and film filtering and concentrating decrement link, after denitration, into deduster before flue gas be evaporated, and consumption compared with
Greatly, the flue gas itself under this stage gives up partial fume herein to desulfurization there are also to the utility value preheated into boiler air
Water is evaporated drying, it will the quality for directly affecting air preheat, from by thermally equilibrated conversion, in operational process recessiveness at
This is higher, and crystal salt can be mixed among flyash after furthermore desulfurization wastewater is dry, reduces the quality of flyash.
Using electric heating evaporative crystallization, additional power supply is needed, direct operating cost is high, evaporates using high-temperature flue gas, drops
The low quality of flyash, recessive operating cost is high, it would therefore be highly desirable to which a kind of improved technology is come in the presence of solving the prior art
This problem.
Summary of the invention
Boiler smoke is called low-temperature flue gas after air preheater and deduster, this section of flue gas will not usually remake
Any utilization belongs to theoretic flue gas, and flue gas still has the temperature spent 100 more at this time, and moisture content is lower, is suitble to
For heat drying desulfurization wastewater.
Since the temperature difference is lower between low-temperature flue gas and desulfurization wastewater, heat exchange rate is more gentle, and single evaporation efficiency is lower,
So the method that we use circulating and evaporating in the art inventions, is evaporated desulfurization wastewater, is finally reached waste water zero-emission
The effect put.
Based on this point, the purpose of the present invention is to provide a kind of sides using fume afterheat evaporation desulfurization wastewater zero-emission
Method achievees the purpose that the treatment of wastes with processes of wastes against one another and desulfurization wastewater zero-emission, with low investment out, operating cost is low, is not required to add anyization
The advantages such as drug are learned, to solve the problems mentioned in the above background technology.
To achieve the above object, the invention provides the following technical scheme: it is a kind of useless using the desulfurization of fume afterheat circulating and evaporating
The method of water zero discharge；
Step 1: the desulfurization wastewater after desulfurization wastewater is concentrated before entering concentration tower lower part mixes；
Step 2: desulfurization wastewater enters concentration tower by circulating pump, circulation water spray system after mixing；
Step 3: extract air preheater after and desulfurizing tower before low-temperature flue gas, using flue gas blower enter concentration tower with
Desulfurization wastewater heat exchange evaporation is concentrated；
Step 4: concentration tower is discharged through demister in the flue gas of the moisture content containing evaporation, flue is returned to, into desulfurizing tower；
Step 5: not evaporating complete concentration desulfurization wastewater, fall into concentration tower bottom liquid storage area with newly mixed into desulfurization wastewater；
Step 6: concentration tower lower end liquid storage area extracts a certain amount of concentration desulfurization wastewater and enters in clarifying basin；
Step 7: body refuse is precipitated in clarifying basin by slush pump and is delivered to sludge dewatering equipment, mud cake is formed and individually handles, separation is useless
Water returns to clarifying basin；
Step 8: the desulfurization wastewater after clarifying in clarifying basin enters circular treatment in concentration tower.
Preferably, smoke outlet is equipped with demister at the top of concentration tower in step 1, and concentration tower top to middle part opens up
Several layers of circulation water spray system.
Preferably, bottom of pond portion is clarified in step 2 and is provided with mud discharging mouth, and mud discharging mouth passes through slush pump phase with sludge dewatering equipment
Precipitating slurry content in clarifying basin is sent into sludge dewatering equipment by slush pump and is carried out dehydrating by connection, is formed aqueous
Lower mud cake is measured, the high-salt wastewater generated in sludge dewatering equipment dehydration then returns in value clarifying basin, clarifying basin
Middle and upper part is equipped with circulating water outlet, and circulating water outlet is docked with the circulation water spray system of concentration tower by waste water circulating pump,
Concentration waste water is squeezed into concentration tower again after waste water circulation is pumped into recirculated water spray equipment after clarifying in clarifying basin, from upper
It is lower to be concentrated by evaporation again with by low-temperature flue gas.
Preferably, water spray system is recycled in step 3 to be preferably but not limited to using eccentric nozzle or spiral nozzle and in tower
2 ~ 10 layers of spraying layer of interior setting, the place 1m below single layer spray spout, design spray coverage rate are as follows: 140% ~ 280%；The dress of water spray
It sets, the supply pressure of every nozzle of design is 2 ~ 10bar, and every layer of circulation water spray system is evenly distributed with several nozzles.
Preferably, flue-gas temperature are as follows: the low-temperature flue gas between 100 DEG C ~ 130 DEG C；Evaporate flue gas dosage and waste water evaporation capacity
Ratio design be scheduled on: between 35:1 ~ 60:1 in step 3 evaporate flue gas in gas inlet localized design flow velocity be lower than 40m/
S, mean flow rate of the flue gas in concentration tower are as follows: between 1.5 ~ 8m/s.
Preferably, low-temperature flue gas designs included water content are as follows: between 3% ~ 10%；Low-temperature flue gas after evaporation designs aqueous
Amount are as follows: between 8% ~ 20%.
Preferably, the concentration waste water displacement of clarifying basin, design is between processing water 5% ~ 30%；Enter in step 6 clear
The concentration waste water in clear pond designs settling time between 4h ~ 6h.
Preferably, flue gas blower draws low-temperature flue gas from flue in step 5, concentration tower lower part set low-temperature flue gas into
Mouthful, low-temperature flue gas is entered concentration tower by flue gas blower by low-temperature flue gas from bottom to top, and flue gas fan frequency conversion is controllable, Ke Yigen
Flue gas input and initial velocity are adjusted according to the fluctuation of desulfurated circulating water input difference and low-temperature flue gas actual temperature.
Compared with prior art, the beneficial effects of the present invention are:
(1) desulfurization wastewater is not required to be directly entered concentration tower through any pretreatment.
(2) desulfurization wastewater is introduced into concentration tower bottom heating, makes full use of fume afterheat, improves subsequent evaporation efficiency.
(3) demister is placed in concentration tower, reduces the additional occupied space of equipment.
(4) treatment process is simple, and processing equipment type is few, reduces input cost and occupation area of equipment.
(5) device structure is simple, and daily maintenance is simple and convenient.
(6) evaporation curable output is individually handled, and does not influence the quality of other products of the power plant such as flyash.
(7) humidifying low-temperature flue gas reduces the subsequent absorption to desulfurizing tower moisture content, reduces the rate of water make-up of desulfurizing tower.
(8) by physical method to desulfurization wastewater processing, technology environmental protection, no chemical agent addition.
(9) evaporation curable output is individually handled, and does not influence the quality of other products of the power plant such as flyash.
(10) processing equipment involved by is normal pressure operation, safety and stability.
(11) flue gas and the concentration mutual adverse current of wastewater room, are sufficiently exchanged heat, can take away moisture content more as far as possible.
(12) water spray system is recycled, is preferably but not limited to split several layers in tower using eccentric nozzle or spiral nozzle,
Every layer several uniformly distributed, is sprayed, and the area with smoke contacts is increased, and realizes contact sufficiently, is concentrated by evaporation rapid.
(13) flue gas fan frequency conversion is controllable, can it is different according to desulfurated circulating water input and and the practical temperature of low-temperature flue gas
The fluctuation of degree, and flue gas input, initial velocity are adjusted, guarantee evaporation effect.
Detailed description of the invention
Fig. 1 is each components connection schematic diagram of the present invention.
In figure: 1 flue gas blower, 2 concentration towers, 3 demisters, 4 circulation water spray systems, 5 waste water circulating pumps, 6 thickened wastes
Water pump, 7 clarifying basins, 8 slush pumps, 9 sludge dewatering equipments.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
The present invention provides a kind of technical solution: a method of desulfurization wastewater zero-emission being evaporated using fume afterheat, including
Following steps:
Step 1: the desulfurization wastewater after desulfurization wastewater is concentrated before entering concentration tower lower part mixes；
Step 2: desulfurization wastewater enters concentration tower by circulating pump, circulation water spray system after mixing；
Step 3: extract air preheater after and desulfurizing tower before low-temperature flue gas, using flue gas blower enter concentration tower with
Desulfurization wastewater heat exchange evaporation is concentrated；
Step 4: concentration tower is discharged through demister in the flue gas of the moisture content containing evaporation, flue is returned to, into desulfurizing tower；
Step 5: not evaporating complete concentration desulfurization wastewater, fall into concentration tower bottom liquid storage area with newly mixed into desulfurization wastewater；
Step 6: concentration tower lower end liquid storage area extracts a certain amount of concentration desulfurization wastewater and enters in clarifying basin；
Step 7: body refuse is precipitated in clarifying basin by slush pump and is delivered to sludge dewatering equipment, mud cake is formed and individually handles, separation is useless
Water returns to clarifying basin；
Step 8: the desulfurization wastewater after clarifying in clarifying basin enters circular treatment in concentration tower.
2 top smoke outlet of concentration tower is equipped with demister 3 in step 4, and demister 3 is for by desulfurization wastewater
The water mist generated after contacting with high-temperature flue gas is separated, due to not only containing moisture in water mist, also have sulfuric acid, sulfosalt acid,
Sulfur dioxide etc. will cause the stained heavy corrosion of blower, heat exchanger and flue, therefore design the object that demister is passed through flue
Matter is separated, and guarantees the service life of flue, and demister 3 is placed in concentration tower 2, reduces the additional occupied space of equipment, dense
2 top of contracting tower to middle part opens up several layers of circulation water spray system 4, and the desulfurization wastewater of concentration enters the spray of concentration tower 2 from top to bottom.
Unevaporated concentration desulfurization wastewater in step 1, sink down into 2 bottom of concentration tower and with newly mixed into desulfurization wastewater, it is dense
2 bottom of contracting tower is connect with clarifying basin 7 by the way that waste water pump 6 is concentrated, and the concentration concentrated waste water pump 6 of desulfurization wastewater is delivered to clarifying basin 7
It is staticly settled, staticly settles mode by the way that desulfurization wastewater will be concentrated, reduce the suspended matter of recycling waste water, recirculated water is avoided to spray
The spray nozzle clogging of shower device 4.
7 bottom of clarifying basin is provided with mud discharging mouth in step 2, and mud discharging mouth is connected with sludge dewatering equipment 9 by slush pump 8,
Precipitating slurry content in clarifying basin 7 is sent into sludge dewatering equipment 9 by slush pump 8 and is carried out dehydrating, water content is formed
Lower mud cake, the high-salt wastewater generated in 9 dehydration of sludge dewatering equipment then return in value clarifying basin 7, evaporation curable
Output is individually handled, and does not influence the quality of other products of the power plant such as flyash, and the middle and upper part of clarifying basin 7 is equipped with circulating water outlet,
Circulating water outlet is docked with the circulation water spray system 4 of concentration tower 2 by waste water circulating pump 5, is concentrated after clarifying in clarifying basin 7
Waste water through waste water circulating pump 5 be sent into circulation water spray system 4 after squeezed into concentration tower 2 again, from top to bottom with pass through low temperature cigarette
Gas is concentrated by evaporation again.
Water spray system 4 is recycled in step 2 to be preferably but not limited to using eccentric nozzle or spiral nozzle and split in tower
Several layers, every layer of circulation water spray system 4 is evenly distributed with several nozzles, increases the area with smoke contacts, realizes contact sufficiently, evaporation
Concentration is rapid.
Flue gas blower 1 draws low-temperature flue gas from flue in step 3, and 2 lower part of concentration tower sets low-temperature flue gas import, low
Low-temperature flue gas is entered concentration tower 2 by flue gas blower 1 by warm flue gas from bottom to top, and 1 frequency conversion of flue gas blower is controllable, can basis
Desulfurated circulating water input is different and the fluctuation of low-temperature flue gas actual temperature and adjusts flue gas input and initial velocity, guarantees evaporation
Effect has a large amount of moisture content in the low-temperature flue gas after evaporating, and can reduce when desulfurization to desulfurization in entering desulfurizing tower later
The loss of tower moisture content point, reduces the moisturizing of desulfurizing tower, since low-temperature flue gas temperature is lower, cannot make desulfurization wastewater in a short time
Evaporating completely, using the cured method of continuous circulating and evaporating, low-temperature flue gas is useless to evaporate with this as the exhaust gas in traditional handicraft
Water does not need additional energy, belongs to waste heat recycling, greatly reduces the operation cost of wastewater treatment.
In step 2 enter circulated sprinkling desulfurization wastewater, design cycle amount be increase newly desulfurization wastewater (step 1) 20 ~
Between 60 times.When design cycle amount is lower than the 20 of waste water incrementss, the offer disengagement area in concentration tower is very little, it is difficult to produce
Raw enough evaporation capacity；When design cycle amount is higher than 60 times of waste water increment, the equipment volume needed, circulation line volume, pump
Send power too many, beyond economic and practical scope.
Clear desulfurization wastewater in step 2, the device of the circulation water spray of the mistake entered, is arranged 2 ~ 10 layers of spraying layer.
Single layer spraying layer cannot provide enough heat exchange areas, influence heat exchange efficiency.When the spray number of plies is more than 10 layers, spray region is accounted for
It is too many with space, extruding and practical heat transfer space, equally influence heat transfer effect.
The device that water spray is recycled in step 2 is preferably but not limited to using eccentric nozzle or spiral nozzle.Such nozzle
With effective anti-clogging, flow adjustable extent is big, the features such as specially determining misting of pressure uniform in effect in range.
The device of water spray is recycled in step 2, below single layer spray spout at 1m, design spray coverage rate are as follows: 140% ~
280%。
The device of water spray is recycled in step 2, the supply pressure of every nozzle of design is 2 ~ 10bar.
In step 3 the flue-gas temperature scope of application of evaporation and heat-exchange from: between 100 DEG C ~ 500 DEG C.It is steamed by using fume waste heat
Hair, the thinking of the treatment of wastes with processes of wastes against one another design preferred flue-gas temperature are as follows: the low-temperature flue gas between 100 DEG C ~ 130 DEG C.
The ratio design that flue gas dosage and waste water evaporation capacity are evaporated in step 3 is scheduled on: between 35:1 ~ 55:1.
It evaporates flue gas in step 3 to be input into concentration tower using extension set, by actual evaporation demand, flue gas conveying capacity is adjustable.
It is lower than 40m/s that flue gas is evaporated in step 3 in gas inlet localized design flow velocity, and flue gas is flat in concentration tower
Equal flow velocity are as follows: between 1.5 ~ 8m/s.
Low-temperature flue gas and circulation desulfurization waste water in step 3, design heat-exchange time are as follows: between 0.5 ~ 5s.
Low-temperature flue gas in step 3 flows from bottom to top in concentration tower, and circulation desulfurization waste water flows from above to below, and two
It drives in the wrong direction and exchanges heat between person, sufficiently exchange heat, moisture content more as far as possible can be taken away.
Low-temperature flue gas in step 3 designs included water content are as follows: between 3% ~ 10%.
The low-temperature flue gas after evaporation in step 4 designs water content are as follows: between 8% ~ 20%.
The water mist that demister is used to generate after contacting desulfurization wastewater with high-temperature flue gas in step 4 separates, due to
Not only contain moisture in water mist, also has sulfuric acid, sulfosalt acid, sulfur dioxide etc., will cause the flaw of blower, heat exchanger and flue
Dirty heavy corrosion, therefore design demister and be passed through the substance of flue and separated, guarantee the service life of flue.
Enter the concentration waste water displacement of clarifying basin in step 6, design is between processing water 5% ~ 30%.
The concentration waste water for entering clarifying basin in step 6 designs settling time between 4h ~ 6h.
It although an embodiment of the present invention has been shown and described, for the ordinary skill in the art, can be with
A variety of variations, modification, replacement can be carried out to these embodiments without departing from the principles and spirit of the present invention by understanding
And modification, the scope of the present invention is defined by the appended.
Claims (8)
1. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission, it is characterised in that: the following steps are included:
Step 1: the desulfurization wastewater after desulfurization wastewater is concentrated before entering concentration tower lower part mixes；
Step 2: desulfurization wastewater enters concentration tower by circulating pump, circulation water spray system after mixing；
Step 3: extract air preheater after and desulfurizing tower before low-temperature flue gas, using flue gas blower enter concentration tower with
Desulfurization wastewater heat exchange evaporation is concentrated；
Step 4: concentration tower is discharged through demister in the flue gas of the moisture content containing evaporation, flue is returned to, into desulfurizing tower；
Step 5: not evaporating complete concentration desulfurization wastewater, fall into concentration tower bottom liquid storage area with newly mixed into desulfurization wastewater；
Step 6: concentration tower lower end liquid storage area extracts a certain amount of concentration desulfurization wastewater and enters in clarifying basin；
Step 7: body refuse is precipitated in clarifying basin by slush pump and is delivered to sludge dewatering equipment, mud cake is formed and individually handles, separation is useless
Water returns to clarifying basin；
Step 8: the desulfurization wastewater after clarifying in clarifying basin enters circular treatment in concentration tower.
2. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Smoke outlet is equipped with demister at the top of concentration tower in the step 1, and concentration tower top to middle part opens up several layers of recirculated water spray
Shower device.
3. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Bottom of pond portion is clarified in the step 2 and is provided with mud discharging mouth, and mud discharging mouth is connected with sludge dewatering equipment by slush pump, will be clarified
Precipitating slurry content in pond is sent into sludge dewatering equipment by slush pump to be carried out dehydrating, and the lower mud of water content is formed
Cake, the high-salt wastewater generated in sludge dewatering equipment dehydration then return in value clarifying basin, and the middle and upper part of clarifying basin is equipped with
Circulating water outlet, the circulating water outlet is docked with the circulation water spray system of concentration tower by waste water circulating pump, described clear
Concentration waste water is squeezed into concentration tower again after waste water circulation is pumped into recirculated water spray equipment after clarifying in clear pond, from top to bottom
It is concentrated by evaporation again with by low-temperature flue gas.
4. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Water spray system is recycled in the step 3 to be preferably but not limited to that 2 ~ 10 are arranged using eccentric nozzle or spiral nozzle and in tower
Layer spraying layer, the place 1m below single layer spray spout, design spray coverage rate are as follows: 140% ~ 280%；The device of water spray, design are every
The supply pressure of nozzle is 2 ~ 10bar, and every layer of circulation water spray system is evenly distributed with several nozzles.
5. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Flue-gas temperature are as follows: the low-temperature flue gas between 100 DEG C ~ 130 DEG C；Evaporation flue gas dosage and the ratio design of waste water evaporation capacity are scheduled on:
Evaporating flue gas between 35:1 ~ 60:1 in step 3 in gas inlet localized design flow velocity is lower than 40m/s, and flue gas is in concentration tower
Mean flow rate are as follows: between 1.5 ~ 8m/s.
6. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Low-temperature flue gas designs included water content are as follows: between 3% ~ 10%；Low-temperature flue gas after evaporation, design water content are as follows: 8% ~ 20% it
Between.
7. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
The concentration waste water displacement of clarifying basin, design is between processing water 5% ~ 30%；Enter the concentration waste water of clarifying basin in step 6,
Settling time is designed between 4h ~ 6h.
8. a kind of method using fume afterheat evaporation desulfurization wastewater zero-emission according to claim 1, it is characterised in that:
Flue gas blower draws low-temperature flue gas from flue in the step 5, and concentration tower lower part sets low-temperature flue gas import, low-temperature flue gas
Low-temperature flue gas is entered into concentration tower from bottom to top by flue gas blower, flue gas fan frequency conversion is controllable, can be according to desulfurated circulating water
Input is different and the fluctuation of low-temperature flue gas actual temperature and adjusts flue gas input and initial velocity.
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| CN110054243A (en) * | 2019-04-17 | 2019-07-26 | 无锡雪浪环境科技股份有限公司 | A kind of high slat-containing wastewater flue gas drying method and device |
| CN110436549A (en) * | 2019-09-10 | 2019-11-12 | 合众思(北京)环境工程有限公司 | A kind of desulfurization wastewater high concentration strong brine evaporation technology |
| CN110812870A (en) * | 2019-12-23 | 2020-02-21 | 无锡市蓝天水处理设备有限公司 | Integrated evaporator |
| CN111138016A (en) * | 2019-12-31 | 2020-05-12 | 江苏利保科技股份有限公司 | Zero-emission low-energy-consumption concentration tower |
| CN111252993A (en) * | 2020-03-25 | 2020-06-09 | 成都锐思环保技术股份有限公司 | System and method for evaporating and concentrating desulfurization wastewater by using flue gas waste heat |
| CN111777119A (en) * | 2020-07-09 | 2020-10-16 | 南京万德斯环保科技股份有限公司 | Waste water evaporation treatment equipment and process |
| CN111825144A (en) * | 2020-07-23 | 2020-10-27 | 盛发环保科技（厦门）有限公司 | Anti-scaling high-salinity wastewater concentrator and high-salinity wastewater concentrating method |
| CN111892218A (en) * | 2020-06-29 | 2020-11-06 | 张建东 | High-efficient low-cost desulfurization waste water treatment's of coal fired power plant zero discharge system |
| CN112194318A (en) * | 2020-09-28 | 2021-01-08 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Flue gas waste heat concentration method and device for desulfurization wastewater |
| CN112604496A (en) * | 2020-12-30 | 2021-04-06 | 广东电网有限责任公司电力科学研究院 | System for removing hydrogen chloride and sulfur trioxide in flue gas in coordination with desulfurization wastewater |
| CN114477335A (en) * | 2022-01-25 | 2022-05-13 | 山东国舜建设集团有限公司 | Desulfurization wastewater evaporation and concentration zero-emission system and process based on double circulation loops |
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| CN114477335A (en) * | 2022-01-25 | 2022-05-13 | 山东国舜建设集团有限公司 | Desulfurization wastewater evaporation and concentration zero-emission system and process based on double circulation loops |
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Application publication date: 20181221 |