CN204185326U - A kind of power plant desulfurization Wastewater zero-discharge treatment system - Google Patents
A kind of power plant desulfurization Wastewater zero-discharge treatment system Download PDFInfo
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- CN204185326U CN204185326U CN201420551370.XU CN201420551370U CN204185326U CN 204185326 U CN204185326 U CN 204185326U CN 201420551370 U CN201420551370 U CN 201420551370U CN 204185326 U CN204185326 U CN 204185326U
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Abstract
The utility model discloses a kind of power plant desulfurization Wastewater zero-discharge treatment system, comprise the pre-processing device, evaporation concentration equipment and the evaporation crystallization equipment that are communicated with in turn, described pre-processing device comprises precipitation concentration pond, and reactor, secondary softening reactor and softening settling tank are softened in sludge dewatering equipment and the former water precipitation pond connected in turn, one-level; Described evaporation concentration equipment comprises the automatic anti-filter rinsed, plate type preheater, degasifier and the falling-film evaporator that are communicated with in turn; Described evaporation crystallization equipment comprises the dope tank, crystallization well heater and the crystallizer that are communicated with in turn.Desulfurization water treatment system of the present utility model is rational in infrastructure, design closely, by the pre-treatment to desulfurization wastewater, evaporation concentration and evaporative crystallization process, final product is only distilled water and crystal salt, thus decrease the discharge of nuisance, reduce energy consumption, achieve the zero release target of desulfurization wastewater.
Description
Technical field
The utility model relates to environmental protection industry (epi), is specifically related to a kind of zero-discharge treatment system for power plant desulfurization waste water and other high salinity, high rigidity trade effluent.
Background technology
" zero release " is defined as industrial and mining enterprises and does not discharge any waste water to bad border, trade effluent fully recovering.Along with industrialization degree is more and more higher, the quantity discharged of industrial water and waste water is also increasing, and the harm caused ecotope is also more serious.Meanwhile, some regional serious water shortage, becomes the restriction to social economy's sustainable development.In the face of situation severe like this, the country that some industry are flourishing, to the industrial and mining enterprises of certain areas, implements waste water zero emission.
Treatment process at present for power plant desulfurization waste water mainly contains chemical tendering+ultrafiltration+reverse osmosis, chemical tendering+multiple-effect evaporation, by facts have proved that these technology mainly exist following shortcoming:
The index such as hardness, suspended substance, salinity, turbidity of chemical tendering+ultrafiltration+reverse osmosis to influent quality all has higher requirements, and pre-treatment requires high, complex process; Product is short for work-ing life, and replacement cost is high; Reverse osmosis can only reclaim the waste water of about 60%, and the dense water of generation still needs additive method process, can not reach the requirement of zero release.
The subject matter that chemical tendering+multiple effective evaporation method exists is: the waste water hardness after chemical tendering generally at 20 ~ 300mg/L(in CaCO3), along with the carrying out of evaporation, the meeting such as carbonate, vitriol, the phosphoric acid salt crystallization gradually of calcium, magnesium ion, and be attached on evaporation wall, serious fouling will be formed in vaporizer and piping system.According to practice, under this condition, vaporizer runs 2 ~ 4 months, just needs to shut down snaking, causes production continuity not carry out; Multiple-effect evaporation compares single-effect evaporation, and steam consumption decreases, but goes up along with domestic steam price, and system cloud gray model expense is still very high; Operational process needs constantly to add live steam, some is not had to the enterprise of residue steam, also needs additionally to increase steam supply, increases project construction cost.
Adopt the power plant desulfurization waste water total salt quantity (TDS) of lime stone-gypsum method desulfurization general at 20000 ~ 50000mg/L, wherein chlorion is about 15000mg/L, sulfate radical is about 2000mg/L, sodium ion 1500 ~ 6000mg/L, total hardness about 10000 ~ 20000 mg/L(is in CaCO3), suspended substance 20000 ~ 60000 mg/L, also containing a small amount of heavy metal ion such as mercury, cadmium, lead in waste water, if in flue gas desulphurization system upstream, be equipped with SCR (SCR) system, then also likely there is unreacted ammonia in waste water.Desulfurization wastewater has the feature of high saliferous, high rigidity, and zero discharge treatment is very difficult, and power plant desulfurization process without drainage of waste water needs the critical problem solved to comprise:
1. be separated the suspended substance in waste water and salinity, form solid waste, produce pure, can the water of reuse;
2. reduce steam, electric power equal energy source consumes, reduce running cost;
3. reduce the scaling tendency of evaporation, crystal system, increase the continuous cycle of operation.
Utility model content
Utility model object: the purpose of this utility model is to solve deficiency of the prior art, a kind of compact construction is provided, reasonable in design, can reduce waste water to equipment corrosion and improve heat exchange efficiency, reduce energy consumption, decreasing pollution, the consumption of reduction system energy, finally realize the power plant desulfurization Wastewater zero-discharge treatment system of desulfurization wastewater zero release target.
Technical scheme: a kind of power plant desulfurization Wastewater zero-discharge treatment system described in the utility model, comprise the pre-processing device be communicated with in turn, evaporation concentration equipment and evaporation crystallization equipment, described pre-processing device comprises precipitation concentration pond, sludge dewatering equipment and the former water precipitation pond connected in turn, one-level softens reactor, secondary softening reactor and softening settling tank, described one-level is softened reactor and is communicated with calcium hydroxide stirred pot and calcium hydroxide storage tank successively, described secondary softening reactor is connected with the flocculation agent stirred pot be interconnected, flocculant storage tank and sodium carbonate stirred pot, sodium carbonate storage tank, described evaporation concentration equipment comprises the automatic anti-filter rinsed, plate type preheater, degasifier and the falling-film evaporator that are communicated with in turn, and described falling-film evaporator is also connected with evaporator condensation water pot, volume tank and vapour compressor, described evaporation crystallization equipment comprises the dope tank, crystallization well heater and the crystallizer that are communicated with in turn, and described dope tank is also connected with crystal salt water extracter, and described crystallization well heater is also connected with well heater cooling tank, and described crystallizer is also connected with barometric condenser.
Further optimization, described former water precipitation pond is communicated with precipitation concentration pond respectively with softening settling tank, and described precipitation concentration pond is communicated with sludge dewatering equipment, and described sludge dewatering equipment is communicated with former water precipitation pond equally.
Further optimization, is also provided with Scale inhibitors stirred pot and hydrochloric acid tank between described automatic anti-filter rinsed and plate type preheater.
Further optimization, the steam that described falling-film evaporator and the outer steam heat-exchanging of pipe produce flow into the shell-side of falling-film evaporator successively after volume tank and vapour compressor.
Further optimization, described evaporator condensation water pot is communicated with volume tank by pump, and described volume tank is communicated with plate type preheater by pump.
Further optimization, described crystallizer is connected with described crystallization well heater by steam ejector.
Further optimization, the output terminal of described softening settling tank is connected with the input terminus of automatic anti-filter rinsed.
Further optimization, the output terminal of described falling-film evaporator is connected with dope tank through pump; Described well heater condensate water pot is communicated with evaporator condensation water pot.
Beneficial effect: the utility model has following beneficial effect:
(1) adopt lime-soda process to soften desulfurization wastewater, after softening, flocculation, precipitation, waste water hardness is reduced to 15 ~ 30mg/L;
(2) the desulfurization wastewater basicity adopting lime-soda process softening is higher, carbonate fouling is easily produced when evaporation or crystallization, so, add hydrochloric acid before evaporation concentration, adjust waste water ph between 5 ~ 6, after plate type preheater heating, the carbonic acid gas be dissolved in waste water, dissolved oxygen and other non-condensable gasess can be removed in degasifier, reduce the formation of evaporation, crystallisation process carbonate fouling, meanwhile, reduce waste water and heat exchange efficiency is improved to the corrodibility of equipment;
(3) when system starts, the addition of C aSO4 crystal seed is added in vaporizer, utilize crystal seed structure identical with dirty thing, the principle that plane of crystal is large compared with pipeline material wall to the avidity of dirty thing, the calcium sulfate molecule of separating out in evaporative process is preferentially attached on the calcium sulphate crystal of suspension, the degree of supersaturation of calcium sulfate in timely elimination solution, thus avoid the nucleation of calcium sulfate on heat exchange tube wall and growth, reduce evaporation, crystallisation process calcium sulfate scaling is formed.The existence of calcium sulfate crystal seed, can strengthen the souring to tube wall when waste water flows through tube wall, reduce the attachment of dirty class at tube wall;
(4) evaporating concentration process, when desulfurization wastewater seethes with excitement and forms a large amount of bubbles on hot face, after water flashes to vapour, the whole crystalline deposit of salinity in waste water, so the hot face at bubble place has an annular salt-pepper noise, the crystallization of steam bubble larger then annular is more large thicker.After bubble departure hot face, water can only dissolve a part again holding in annular salt-pepper noise diffluent salinity, so often generates a steam bubble and just produces salt crust, hot face constantly produces steam bubble, just piles up and defines one deck incrustation scale.By controlling evaporative process heat transfer temperature difference, make them between 2.5 ~ 5 DEG C, evaporative process is gentleer, avoids waste water acutely to seethe with excitement, thus effectively reduces salt crust formation;
(5) evaporating concentration process, the secondary steam of generation compresses through vapour compressor, and pressure, temperature raise, and heat content increases, and heating steam use is used as by the heating chamber then delivering to vaporizer, and heating desulfurization wastewater, heating steam itself is then condensed into water.Like this, the steam originally will discarded just is fully utilized, and reclaims latent heat, improves thermo-efficiency, meanwhile, decreases the demand to indirect heating and cooling resource, reduces energy consumption, decreasing pollution;
(6) evaporation and crystal process, adopts pump circulation crystallizer, and waste water by heat temperature raising, but evaporation and crystallization does not occur in crystallization well heater, meanwhile, because waste water keeps higher flow velocity in the heater, reduces the possibility of in-tube fouling.
(7) evaporation and crystal process, in the secondary steam of generation about 30 ~ 45% ratio by after steam ejector supercharging as the thermal source of crystallization well heater, decrease the usage quantity of raw steam, reduce system energy consumption;
(8) in whole system, the distilled water that required water coolant all can use system self to produce, do not need extraneous supply water coolant, system operation does not need to consume Freshwater resources completely;
(9) by the beneficial effect of above-mentioned 1,2,3,4,6 clauses, effectively reduce the formation of fouling in system, improve running efficiency of system, the cleaning interval can reach 2 years even for more time;
(10) after desulfurization wastewater enters system, through a series for the treatment of scheme, final product is distilled water and crystal salt, achieves the target of desulfurization wastewater zero release, completely avoid the pollution of desulfurization wastewater to environment; The high quality distilled water produced, can supply enterprise's reuse, reduces enterprise to the consumption of Freshwater resources;
(11) when carrying out evaporation concentration, waste water saltiness is lower, and boiling point temperature rise is relatively little, and the energy consumption that evaporation concentration is carried out in use mechanical steam recompression technique (MVR) is relatively little.During evaporative crystallization, solution is in state of saturation, and boiling point temperature rise reaches maximum value, is not suitable for continuing to use MVR technique, use thermal type vapor recompression technique (TVR) evaporative crystallization to be equivalent to the energy-saving effect of 2 ~ 3 effect multiple-effect evaporations, and system is simpler, cost is lower.In conjunction with MVR and TVR two kinds of techniques, segmentation realizes evaporation concentration and evaporative crystallization, effectively controls system cloud gray model energy consumption, and the energy consumption that processing 1 ton of desulfurization wastewater needs is 15 ~ 35kWh electricity and 0.085 ~ 0.14 ton of steam.
Accompanying drawing explanation
Fig. 1 is pre-processing device structural representation of the present utility model.
Fig. 2 is evaporation concentration equipment structural representation of the present utility model.
Fig. 3 is evaporation crystallization equipment structural representation of the present utility model.
Embodiment
Desulfurization wastewater zero-discharge treatment system of the present utility model mainly comprises three process, that is: pretreatment process, evaporation concentration operation and evaporative crystallization operation, is described in detail successively below to above-mentioned three operations (equipment):
(1) pretreatment process
The equipment of this operation comprises precipitation concentration pond 11, sludge dewatering equipment 12 and the former water precipitation pond 7 connected in turn, one-level softens reactor 8, secondary softening reactor 9 and softening settling tank 10, one-level is softened reactor 8 and is communicated with calcium hydroxide stirred pot 4 and calcium hydroxide storage tank 1 successively, secondary softening reactor 9 is connected with the flocculation agent stirred pot 5 be interconnected, flocculant storage tank 2 and sodium carbonate stirred pot 6, sodium carbonate storage tank 3, former water precipitation pond 7 is communicated with precipitation concentration pond 11 respectively with softening settling tank 10, precipitation concentration pond 11 is communicated with sludge dewatering equipment 12, sludge dewatering equipment 12 is communicated with former water precipitation pond 7 equally.
First desulfurization wastewater enters former water precipitation pond, after suspended substance preliminary sedimentation in waste water, throw out enters precipitation concentration pond, supernatant liquor enters one-level and softens reactor and Ca(OH) 2 to react, Mg2+ in waste water generates Mg(OH) 2 precipitations, then waste water enters secondary softening reactor, Ca2+ and Na2CO3 reaction in waste water generates CaCO3 precipitation, further reduction original water hardness, and flocculation agent is added in secondary softening reactor, after sedimentary size and quality are constantly increased, flow into softening settling tank, throw out and heavy metal ion precipitate gradually and enter in precipitation concentration pond, waste water is after precipitate and separate, supernatant liquor supplies follow-up flow process advanced treatment, throw out precipitates further in precipitation concentration pond, isolated supernatant liquor is back to former water precipitation pond, mud slurries are after sludge dewatering equipment dehydration is separated, mud is discharged outside the venue, slurry reflux is to former water precipitation pond.
High rigidity waste water is easy to form fouling in heating, evaporation and crystallisation process, causes heat transfer coefficient to decline, and time serious, meeting blocking pipeline and equipment, cause disorderly closedown.So need the hardness reduced by pre-treatment in waste water.The mechanism that employing lime-soda process softens desulfurization wastewater is as follows:
Mg
2++ Ca（OH）
2= Mg（OH）
2↓ + Ca
2+
Ca
2++ Na
2CO
3= CaCO
3 ↓ + 2Na
+
Softening process is actual is the calcium ions and magnesium ions replaced with sodium ion in waste water, and calcium ions and magnesium ions reaction is generated throw out removal, so the desulfurization wastewater after softening is based on sodium salt, and negatively charged ion mainly chlorion, sulfate radical, bicarbonate radical etc. in water.
Most suspended substances, calcium, magnesium ion and heavy metal ion after softening, flocculation, precipitation in waste water all precipitate removal, and waste water hardness is reduced to 15 ~ 30mg/L, turbidity 50 ~ 100NTU, pH9 ~ 10.
(2) evaporation concentration operation
This processing apparatus comprises the automatic anti-filter rinsed 13, plate type preheater 16, degasifier 18 and the falling-film evaporator 19 that are communicated with in turn, falling-film evaporator 19 is also connected with evaporator condensation water pot 17, volume tank 20 and vapour compressor 21, Scale inhibitors stirred pot 14 and hydrochloric acid tank 15 is also provided with between automatic anti-filter rinsed 13 and plate type preheater 16.
After pretreatment, softening desulfurization wastewater enters automatic anti-filter rinsed, suspended substance in filtering waste water, then Scale inhibitors and HCl is added, adjusted to ph is between 5 ~ 6, be heated to after boiling point through plate type preheater, enter degasifier, the gases such as the carbon dioxide and oxygen be dissolved in the water are separated and enter air, desulfurization wastewater after degasification enters falling-film evaporator, constantly circulate in falling film evaporation organ pipe through recycle pump, and with pipe outer steam heat-exchanging, waste water is evaporated and is concentrated, the steam that evaporation produces enters scrubber tower after silk screen demist, liquid water droplets in steam is caught further, pure steam enters vapour compressor, water vapor will be compressed, thus the pressure and temperature of raising steam is to superheated vapour state, spray appropriate distilled water to mix with superheated vapour, after becoming saturation steam, flow into the shell-side of falling-film evaporator, steam is by tube wall and wastewater heat exchange in pipe, and generate distilled water, distilled water flows into vaporizer distillation water pot, then be pumped to volume tank to use as gas washing water, from distilled water thermoplastic desulfurization wastewater plate type preheater that volume tank flows out, distilled water after cooling can electric power supply plant reuse.
Evaporating concentration process adopts mechanical steam recompression (MVR) technology, MVR technology is combined with vapour pump by vaporizer, to consume a part of high potential (mechanical energy, electric energy etc.) for cost, by thermodynamic cycle compression process, pressure, the temperature of secondary steam raise, and heat content increases, then heating steam use is used as by the heating chamber delivering to vaporizer, make feed liquid maintain boiling state, heating steam itself is then condensed into water.Heat energy like this when processing waste water needed for evaporation, when being cooled by vapor condensation and water of condensation, the heat energy of release provided.In operation, there is no the loss of latent heat; Consuming in operation, is only the electric energy driving the water pump of waste water, steam and condensate water circulatory and flowing in vaporizer, vapour pump and Controlling System to consume.
After evaporation concentration, in wastewater flow, the moisture content of 80 ~ 90% is evaporated and is generated distilled water, because the desulfurization wastewater saltiness after concentrated raises, boiling point temperature rise also can increase, the energy consumption of vapour compressor also can increase, so control the desulfurization wastewater saltiness about 20% after concentrating, boiling point temperature rise 4 ~ 5 DEG C (changing because salt component is different).
(3) evaporative crystallization operation
This processing apparatus comprises the dope tank 27, crystallization well heater 22 and the crystallizer 24 that are communicated with in turn, dope tank 27 is also connected with crystal salt water extracter 28, crystallization well heater 22 is also connected with well heater cooling tank 23, crystallizer 24 is also connected with barometric condenser 26, and crystallizer 24 is connected with crystallization well heater 22 by steam ejector 25.
First desulfurization wastewater after concentrated enters dope tank, then crystallization well heater is pumped to, desulfurization wastewater after heat temperature raising flows into crystallizer, at this flash crystallization, the a part of steam generated is sucked by steam ejector, momentum exchange is there is with ejection gas (raw steam), the increasing temperature and pressure steam exported enters the shell-side of crystallization well heater, with the desulfurization wastewater heat exchange of pipe side, and generate distilled water, distilled water flows into well heater condensate water pot, then vaporizer distillation water pot is pumped to, in crystallizer, rest part steam enters barometric condenser, the reuse of distilled water electric power supply plant is generated with the direct condensation by contact of distilled water, the crystal salt of crystallizer obtains final product crystal salt through pump delivery to crystal salt water extracter.
Evaporation and crystal process adopts thermal type vapor recompression (TVR) technology.Under the drive of the raw steam (pressure 6 ~ 8Bar) of high pressure, enter steam ejector from vaporizer out a secondary steam part, after mixing increasing temperature and pressure, steam can be utilized again, enters heating chamber and is used as heating steam and uses, heat feed liquid.Another part enters condenser, discharges after condensation.Heating steam condenses into water and discharges in heating chamber.According to its performance characteristics, the energy that the energy using a steam ejector to save is saved with increase 1st effective evaporator is suitable, can save energy 50%.
The working load of evaporation and crystallization system is generally 10 ~ 20% raw wastewater water yields, and by heating-evaporate-crystallization-sepn process, the salinity in desulfurization wastewater is thoroughly separated with water, forms crystal salt and distilled water.
Claims (8)
1. a power plant desulfurization Wastewater zero-discharge treatment system, it is characterized in that: comprise the pre-processing device be communicated with in turn, evaporation concentration equipment and evaporation crystallization equipment, described pre-processing device comprises precipitation concentration pond, sludge dewatering equipment and the former water precipitation pond connected in turn, one-level softens reactor, secondary softening reactor and softening settling tank, described one-level is softened reactor and is communicated with calcium hydroxide stirred pot and calcium hydroxide storage tank successively, described secondary softening reactor is connected with the flocculation agent stirred pot be interconnected, flocculant storage tank and sodium carbonate stirred pot, sodium carbonate storage tank, described evaporation concentration equipment comprises the automatic anti-filter rinsed, plate type preheater, degasifier and the falling-film evaporator that are communicated with in turn, and described falling-film evaporator is also connected with evaporator condensation water pot, volume tank and vapour compressor, described evaporation crystallization equipment comprises the dope tank, crystallization well heater and the crystallizer that are communicated with in turn, and described dope tank is also connected with crystal salt water extracter, and described crystallization well heater is also connected with well heater cooling tank, and described crystallizer is also connected with barometric condenser.
2. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, it is characterized in that: described former water precipitation pond is communicated with precipitation concentration pond respectively with softening settling tank, described precipitation concentration pond is communicated with sludge dewatering equipment, and described sludge dewatering equipment is communicated with former water precipitation pond equally.
3. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: be also provided with Scale inhibitors stirred pot and hydrochloric acid tank between described automatic anti-filter rinsed and plate type preheater.
4. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: the steam that described falling-film evaporator and the outer steam heat-exchanging of pipe produce flow into the shell-side of falling-film evaporator successively after volume tank and vapour compressor.
5. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: described evaporator condensation water pot is communicated with volume tank by pump, and described volume tank is communicated with plate type preheater by pump.
6. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: described crystallizer is connected with described crystallization well heater by steam ejector.
7. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: the output terminal of described softening settling tank is connected with the input terminus of automatic anti-filter rinsed.
8. a kind of power plant desulfurization Wastewater zero-discharge treatment system according to claim 1, is characterized in that: the output terminal of described falling-film evaporator is connected with dope tank through pump; Described well heater condensate water pot is communicated with evaporator condensation water pot.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104843927A (en) * | 2015-05-26 | 2015-08-19 | 中国华电工程(集团)有限公司 | Desulfurization waste water zero discharging process and system |
| CN105217702A (en) * | 2015-11-03 | 2016-01-06 | 神华集团有限责任公司 | A kind of desulfurization wastewater treatment system |
| CN105254100A (en) * | 2015-10-22 | 2016-01-20 | 得利满水处理***(北京)有限公司 | System and method for treating sewage containing salt |
| CN106396231A (en) * | 2016-10-28 | 2017-02-15 | 浙江蓝天求是环保股份有限公司 | Treatment system and treatment method for evaporating and crystallizing desulfurization waste water by using cooling tower |
| CN106517606A (en) * | 2016-11-27 | 2017-03-22 | 杭州水处理技术研究开发中心有限公司 | Treating apparatus capable of realizing zero discharge of desulphurization wastewater from power plant |
| CN109422376A (en) * | 2017-08-30 | 2019-03-05 | 韦勇 | A kind of drinking water pumping station system of the adjustable water hardness |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104843927A (en) * | 2015-05-26 | 2015-08-19 | 中国华电工程(集团)有限公司 | Desulfurization waste water zero discharging process and system |
| CN105254100A (en) * | 2015-10-22 | 2016-01-20 | 得利满水处理***(北京)有限公司 | System and method for treating sewage containing salt |
| CN105217702A (en) * | 2015-11-03 | 2016-01-06 | 神华集团有限责任公司 | A kind of desulfurization wastewater treatment system |
| CN105217702B (en) * | 2015-11-03 | 2019-03-05 | 神华集团有限责任公司 | A kind of desulfurization wastewater treatment system |
| CN106396231A (en) * | 2016-10-28 | 2017-02-15 | 浙江蓝天求是环保股份有限公司 | Treatment system and treatment method for evaporating and crystallizing desulfurization waste water by using cooling tower |
| CN106396231B (en) * | 2016-10-28 | 2019-08-02 | 浙江蓝天求是环保股份有限公司 | It is a kind of to utilize cooling tower evaporative crystallization desulfurization wastewater treatment system and processing method |
| CN106517606A (en) * | 2016-11-27 | 2017-03-22 | 杭州水处理技术研究开发中心有限公司 | Treating apparatus capable of realizing zero discharge of desulphurization wastewater from power plant |
| CN109422376A (en) * | 2017-08-30 | 2019-03-05 | 韦勇 | A kind of drinking water pumping station system of the adjustable water hardness |
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