CN105692998A - Desulfurized waste water zero-emission system and technology adopting redissolution for salt and nitrate supplementation and realizing salt separation for recycling - Google Patents

Desulfurized waste water zero-emission system and technology adopting redissolution for salt and nitrate supplementation and realizing salt separation for recycling Download PDF

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CN105692998A
CN105692998A CN201610130554.2A CN201610130554A CN105692998A CN 105692998 A CN105692998 A CN 105692998A CN 201610130554 A CN201610130554 A CN 201610130554A CN 105692998 A CN105692998 A CN 105692998A
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effect evaporator
salt
evaporator
back dissolving
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CN105692998B (en
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蒋程
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Shanghai Shengfeng Environmental Energy Technology Co ltd
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Shanghai Pushi Environmental Science And Technology Co Ltd
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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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
    • C01D5/16—Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity
    • C01P2006/82—Compositional purity water content
    • 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
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • 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
    • 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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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

The invention provides a desulfurized waste water zero-emission technology adopting redissolution for salt and nitrate supplementation and realizing salt separation for recycling. The technology comprises steps as follows: a membrane concentration liquid after concentrated by a softening membrane is preheated and then enters an MVR (mechanical vapor recompression) system for further concentration, an MVR concentrated solution enters a redissolution tank, salt and nitrate are supplemented to saturation, a mixed solution enters a four-effect evaporation and crystallization system, NaCl and Na2SO4 are crystallized and precipitated out respectively, are separated by a centrifugal salt removing system and a centrifugal denitration system and are dried, and NaCl and Na2SO4 with the purity higher than 98% are obtained. With the technological combination of the membrane, the MVR and the multi-effect evaporation, separation of salt and nitrate is realized, and meanwhile, the operating cost is greatly reduced; with the adoption of the technology of realizing salt and nitrate supplementation through redissolution, the disturbance of water quality fluctuation on operation and control nodes of a salt production system is avoided, so that the system can operate stably for a long term, and the purity of salt and nitrate is guaranteed.

Description

Back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system and technique
Technical field
This technology relates to power plant desulfurization field of wastewater, is specially a kind of back dissolving benefit sal prunella and divides salt to reclaim desulfurization wastewater Zero discharging system and technique。
Background technology
SO in China's firepower electrical plant flue gas2Discharge be strictly controlled, Wet Fgd By Limestone is current domestic and international most popular a kind of fume desulphurization method。The desulfurization wastewater that wet desulphurization produces be mainly characterized in that slant acidity, turbidity big, containing plurality of heavy metal, COD is high, salinity is high；Wherein main salt ion includes Na+、Cl-、SO4 2-Ion, additionally contains a small amount of Ca2+、Mg2+、F-With total silicon plasma。Current domestic power plant adopts method for treating desulfurized wastewater to have coagulation treatment method and pretreatment+evaporative crystallization method。Wherein, coagulation treatment method complex process, medicine system are huge, and effluent quality does not substantially all reach the existing discharge standard of China；Pretreatment+evaporative crystallization technique achieves and desulfurization wastewater is separated into condensed water up to standard and solid carnallite, achieve the zero-emission of desulfurization wastewater, but the solid carnallite amount produced is big, complicated component, its further disposal is also a difficult point problem, and direct evaporation after pretreatment, the water yield is big, and equipment is huge, and investment is big。
Summary of the invention
The purpose of this technology is to provide can constantly produce highly purified NaCl and Na2SO4, simultaneously the salt manufacturing nitre system water yield is little, and equipment investment is relatively low and runs long-acting stable back dissolving and mends sal prunella and divide salt to reclaim desulfurization wastewater technique of zero discharge。
Back dissolving described in this technology is mended sal prunella and is divided salt to reclaim desulfurization wastewater technique of zero discharge, including pretreatment concentration systems and salt manufacturing nitre system, wherein pretreatment concentration systems includes one-level softening settling system, dual membrane system, Buffer Pool, secondary softening settling system, preheater, MVR system, back dissolving tank composition；Salt making system includes 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator, primary heater, secondary heater, three grades of heaters, hot-pressing system, centrifugal salt making systems and is centrifuged nitre system processed, comprises the following steps:
(1) desulfurization wastewater enters double; two membrance concentration system after one-level softening precipitation removes carnallite and heavy metal, arranges outside RO film clear liquid, and RO membrance concentration liquid enters Buffer Pool；
(2) in Buffer Pool, feed liquid sends into preheater after secondary softening precipitation removes carnallite and heavy metal further, being concentrated further by entering MVR system after condensed water and raw steam preheating, concentrated solution is directly entered back dissolving tank and mixes NaCl and Na in feed liquid with the sal prunella crystal of backflow2SO4Mend to saturated；
(3) saturated NaCl and Na2SO4Feed liquid is evaporated in transport pump to 2nd effect evaporator, the NaCl crystal precipitated out is delivered to centrifugal salt making system, concentrated solution enters in triple effect evaporator, and a produced indirect steam part is used for the backflow heating in secondary heater, and a part adds vapours as triple effect evaporator；
The NaCl crystal precipitated out in triple effect evaporator is delivered to centrifugal salt making system, and concentrated solution enters four-effect evaporator, and a produced indirect steam part is used for heating primary heater internal reflux liquid, and a part adds vapours as four-effect evaporator；
The NaCl crystal precipitated out in four-effect evaporator is delivered to centrifugal salt making system, and the material after concentration arrange outside disposal except fraction, and all the other sequentially pass through after one-level, two grades and three grades of heaters preheatings in entrance 1st effective evaporator；
The Na that material precipitates out after entering 1st effective evaporator evaporation2SO4Crystal is delivered to centrifugal denitrating system, concentrated solution enters 2nd effect evaporator, and a produced indirect steam part is used for heating three grades of heater internal reflux liquid, a part then enters hot-pressing system and raw steam and adds vapours as add vapours, the remainder of 2nd effect evaporator as this effect。
Above-mentioned back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater technique of zero discharge, and back dissolving tank wall is provided with steam heating shell, and in control back dissolving tank, temperature is at about 108 DEG C。
Above-mentioned back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater technique of zero discharge, and one-level, two grades and three grades of heaters all adopt tubular heat exchanger。
Above-mentioned back dissolving mend sal prunella divide salt reclaim desulfurization wastewater technique of zero discharge, 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator evaporating temperature be gradually lowered；Deliver to saturated NaCl and the Na in 2nd effect evaporator2SO4Feed temperature is 108 DEG C, and the evaporating temperature of four-effect evaporator is 45 DEG C。45 DEG C are adopted to carry out solventing-out with 108 DEG C of sal prunella equilibrium point mutual solubility differences。
This technology additionally provides one simultaneously can constantly produce highly purified NaCl and Na2SO4, simultaneously the salt manufacturing nitre system water yield is little, and equipment investment is relatively low and runs long-acting stable back dissolving and mends sal prunella and divide salt to reclaim desulfurization wastewater Zero discharging system。
This back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system, including pretreatment concentration systems and salt manufacturing nitre system, wherein pretreatment concentration systems includes one-level softening settling system, dual membrane system, Buffer Pool, secondary softening settling system, preheater, MVR system, back dissolving tank；Salt making system includes 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator, primary heater, secondary heater, three grades of heaters, hot-pressing system, centrifugal salt making systems and is centrifuged nitre system processed,
Desulfurization wastewater softens settling system through one-level and enters double; two membrance concentration system, arranges outside RO film clear liquid, and RO membrance concentration liquid enters Buffer Pool；
In Buffer Pool, feed liquid sends into preheater after secondary softening settling system, enters MVR system and concentrate further after preheating, and concentrated solution is directly entered back dissolving tank and mixes NaCl and Na in feed liquid with the sal prunella crystal of backflow2SO4Mend to saturated；
Saturated NaCl and Na2SO4Feed liquid is evaporated in transport pump to 2nd effect evaporator, the NaCl crystal precipitated out is delivered to centrifugal salt making system, concentrated solution enters in triple effect evaporator, and a produced indirect steam part is used for the backflow heating in secondary heater, and a part adds vapours as triple effect evaporator；
The NaCl crystal precipitated out in triple effect evaporator is delivered to centrifugal salt making system, and concentrated solution enters four-effect evaporator, and a produced indirect steam part is used for heating primary heater internal reflux liquid, and a part adds vapours as four-effect evaporator；
The NaCl crystal precipitated out in four-effect evaporator is delivered to centrifugal salt making system, and the material after concentration arrange outside disposal except fraction, and all the other sequentially pass through after one-level, two grades and three grades of heaters preheatings in entrance 1st effective evaporator；
The Na that material precipitates out after entering 1st effective evaporator evaporation2SO4Crystal is delivered to centrifugal denitrating system, concentrated solution enters 2nd effect evaporator, and a produced indirect steam part is used for heating three grades of heater internal reflux liquid, a part then enters hot-pressing system and raw steam and adds vapours as add vapours, the remainder of 2nd effect evaporator as this effect。
Above-mentioned back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system, and back dissolving tank wall is provided with steam heating shell, and in control back dissolving tank, temperature is at about 108 DEG C。
Above-mentioned back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system, and one-level, two grades and three grades of heaters all adopt tubular heat exchanger。
Above-mentioned back dissolving is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system, 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator evaporating temperature be gradually lowered；Deliver to saturated NaCl and the Na in 2nd effect evaporator2SO4Feed temperature is 108 DEG C, and the evaporating temperature of four-effect evaporator is 45 DEG C。
The beneficial effect of this technology:
This technology is provided with two-stage softening settling system, effectively removes hardness, reduces the scale problems of vapo(u)rization system；This technology pretreatment enriching section adopts double; two film+MVR technique, each process characteristic of Appropriate application, greatly reduces operation energy consumption, reduces follow-up back dissolving and the operating load of salt manufacturing nitre technique simultaneously；This technology arranges back dissolving tank so that the sal prunella in material all reaches unique equilibrium point mutual solubility, ensures the salt manufacturing long-acting operation of nitre system stability；In this technology, salt manufacturing nitre system adopts multistage flash evaporation/evaporation, eliminates the temperature difference adverse effect to flash distillation, and backflow can be heated by a steam part for flash distillation simultaneously, and a part can add vapours, energy efficient as what next effect was evaporated；This technology is provided with hot-pressing system, can the rich indirect steam that an effect produces be recycled, energy efficient。
The back dissolving that this technology provides is mended sal prunella and is divided salt to reclaim desulfurization wastewater technique of zero discharge, and it adopts pretreatment concentration and four-effect evaporation salt manufacturing nitre system, can constantly produce highly purified NaCl and Na2SO4, NaCl and Na2SO4Purity be above 98%, simultaneously the salt manufacturing nitre system water yield is little, and equipment investment is relatively low and runs long-acting stable。It utilizes the different solubility of sal prunella at 45 DEG C and 108 DEG C, and (at 45 DEG C, sal prunella equilbrium solubility is NaCl32.7g/100g water, Na2SO49.5g/100g water；At 108 DEG C, sal prunella equilbrium solubility is NaCl37.8g/100g water, Na2SO46.3g/100g water), from feed liquid, constantly isolate salt and nitre by circulating and evaporating at 45 DEG C and 108 DEG C。
Accompanying drawing explanation
Fig. 1 mends sal prunella for a kind of back dissolving and divides salt to reclaim desulfurization wastewater technique of zero discharge flow process and thermal technology figure。
Fig. 2 is centrifugal desalting system flow chart。
Fig. 3 is centrifugal nitre system flow chart processed。
Detailed description of the invention
Below in conjunction with accompanying drawing, the embodiment of this technology is described further:
One specific embodiment of this technology is as it is shown in figure 1, include one-level softening sedimentation tank, dual membrane system, Buffer Pool, secondary softening sedimentation tank, 1# preheater, 2# preheater, MVR system, back dissolving tank, 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator, mixing condenser, primary heater, secondary heater, three grades of heaters, hot-pressing system, centrifugal desalting systems and be centrifuged nitre system processed composition。
Specific implementation process comprises the following steps:
(1) 25 DEG C of desulfurization wastewater enters double; two membrance concentration system after one-level softening precipitation removes the pollutant such as carnallite and heavy metal, arrange outside RO film clear liquid, RO membrance concentration liquid enters Buffer Pool, and in Buffer Pool, feed liquid removes the pollutant such as carnallite and heavy metal further then through secondary softening precipitation；
(2) after the condensed water of material (in 1# preheater) of secondary softening precipitation and raw steam (in 2# preheater) are preheated to 108 DEG C, enter MVR system to concentrate further, outer row after condensed water preheating stock solution, concentrated solution enters back dissolving tank, by NaCl and the Na in material2SO4Mending to saturated, the sal prunella failing to dissolve in back dissolving tank is back to Buffer Pool, and controlling temperature in back dissolving tank is 108 DEG C；
(3) saturated NaCl and Na2SO4Material evaporates in transport pump to 2nd effect evaporator, controlling flash temperature is 88 DEG C, the NaCl crystal precipitated out is delivered to centrifugal desalting system through base of evaporator salt lower limb, concentrated solution enters in triple effect evaporator, and the indirect steam producing 80 DEG C heats mother solution in secondary heater internal reflux liquid and triple effect evaporator respectively；
Controlling triple effect evaporator flash temperature is 68 DEG C, the NaCl crystal precipitated out is delivered to centrifugal desalting system through base of evaporator salt lower limb, concentrated solution enters four-effect evaporator, and the indirect steam producing 60 DEG C heats mother solution in primary heater internal reflux liquid and four-effect evaporator respectively；
Controlling four-effect evaporator flash temperature is that the NaCl crystal precipitated out in 45 DEG C is delivered to centrifugal desalting system through base of evaporator salt lower limb, concentrated solution enters after a part of one-level, two grades and the preheating of three grades of heaters that a part in 1st effective evaporator is directly outer arranges disposal, produces the indirect steam of 38 DEG C and enters outside after mixing condenser mixes with condensed water and arrange；
The Na precipitated out in 1st effective evaporator2SO4Crystal is delivered to centrifugal denitrating system through base of evaporator salt lower limb, concentrated solution enters 2nd effect evaporator, and an indirect steam part heats mother solution in three grades of heater internal reflux liquid, part heating 2nd effect evaporator, is partly into hot-pressing system and raw steam post-heating this effect mother solution；
(4) 1# preheater preheating stock solution is entered after giving birth to steam and the mixing of indirect steam condensed water。
Certain power plant is according to the 50m of this technique3/ h desulfurization wastewater zero discharge treatment project, water inlet leading indicator is in Table 1, and effluent quality is in Table 3。
Table 1 influent quality table
Sequence number Project Unit Index
1 TDS mg/L 39989
2 Ca2+ mg/L 276
3 Mg2+ mg/L 276
4 Na+ mg/L 10182
5 Cl— mg/L 22466
6 SO4 2- mg/L 6750
7 Total silicon mg/L 39.08
8 CODCr mg/L 600
9 Cd mg/L 0.89
10 Hg mg/L 0.06
11 PH 4-6
Table 2 is intake main salt amount
Effluent quality is in Table 3。
Table 3 effluent quality table
Project Unit Value
Qd t/d 1150
CODCr mg/L 50
PH 6-9
System simultaneously also produce 31.07t/d purity be 99% sodium chloride, 11.98t/d purity be 98% sodium sulfate and 6.18t/d moisture content be 20% carnallite。
System is run and is consumed raw steam 48kg/ ton water, power consumption 35KWH/ ton water, consumes 17 yuan/ton of water of medicament expense。
The monitoring in every 1 day of 1 Buffer Pool water quality once, mends salt amount in the evaporation capacity of adjustment MVR system and back dissolving tank, control MVR system has a small amount of crystal to precipitate out and in back dissolving tank, in material, sal prunella dissolving is saturated, provides stable flow condition for follow-up salt making system。Additionally, back dissolving tank wall is provided with heating shell, accurately controls temperature in back dissolving tank, it is ensured that 2nd effect evaporator feed liquor is maintained at about 108 DEG C, maintain the operating condition of salt making system。
2 stock solutions enter back into salt making system after adopting double; two film+MVR concentration, reduce the operating load of follow-up workshop section, reduce cost of investment。
3 materials are before entering salt making system, by NaCl and Na in back dissolving tank2SO4It is supplemented to saturated, ensure that the stability of salt making system operating condition, when avoiding leading portion pretreatment concentration systems fluctuation of service, two kinds of salt change of component cause salt making system to run node uncontrollability, if system without back dissolving, have at least the delay of 6-8 hour from monitoring water analysis to Operating condition adjustment, very easily cause salt making system not go out salt or salt separates unsuccessfully。
4 one-levels, two grades and three grades of heaters employing Secondary-steam heatings, and heater employing tubular heat exchanger, to ensure that heat exchanger tube washes away under the big flow velocity of mother solution, it is prevented that Na2SO4Precipitation blocking heat exchanger tube。
The indirect steam produced in 5 1st effective evaporators, after being supplied to three grades of heaters and 2nd effect evaporator, still has more than needed, therefore is provided with hot-pressing system, made full use of by indirect steam。
6 1st effective evaporator concentrated solutions enter four-effect evaporator after two effects and triple effect double flash evaporation, can make full use of the secondary steam for preheating backflow mother solution that flash distillation produces, can effectively control foam volume with time stage flash distillation, it is ensured that system stable operation。
7 back dissolvings mend sal prunella evaporation technology systems evaporated water do not increase, more traditional without back dissolving benefit sal prunella evaporation technology operation energy consumption will not raise。
This technology having the beneficial effects that compared with conventional art process:
(1) native system efficiently achieves and is realizing desulfurization wastewater zero-emission simultaneously by wherein important salinity NaCl and Na2SO4Separate, and NaCl and Na2SO4Purity reaches more than 98%, has recovery value, decreases carnallite and disposes。
(2) material advances into back dissolving tank by NaCl and Na at entrance salt making system2SO4It is supplemented to saturated, it is to avoid two kinds of salt change of component cause salt making system operation node uncontrollable。
(3) native system adopts double; two film+MVR+ hot pressing multi-effect evaporation system, wherein double; two membrane process operational energy efficiencies are relatively low, MVR secondly, hot pressing multiple-effect steam energy consumption is the highest, three kinds of techniques effectively combine and can reduce operation energy consumption, reduce that technique is the most complicated simultaneously, control to require the highest salt manufacturing nitre system operating load, reduce equipment investment, easy and simple to handle。
(4) indirect steam that process system produces is fully used dramatically, and system operation cost is relatively low。

Claims (8)

1. back dissolving benefit sal prunella divides salt to reclaim desulfurization wastewater technique of zero discharge, including pretreatment concentration systems and salt manufacturing nitre system, wherein pretreatment concentration systems includes one-level softening settling system, dual membrane system, Buffer Pool, secondary softening settling system, preheater, MVR system, back dissolving tank；Salt making system includes 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator, primary heater, secondary heater, three grades of heaters, hot-pressing system, centrifugal salt making systems and is centrifuged nitre system processed, it is characterised in that comprise the following steps:
(1) desulfurization wastewater enters double; two membrance concentration system after one-level softening precipitation removes carnallite and heavy metal, arranges outside RO film clear liquid, and RO membrance concentration liquid enters Buffer Pool；
(2) in Buffer Pool, feed liquid sends into preheater after secondary softening precipitation removes carnallite and heavy metal further, being concentrated further by entering MVR system after condensed water and raw steam preheating, concentrated solution is directly entered back dissolving tank and mixes NaCl and Na in feed liquid with the sal prunella crystal of backflow2SO4Mend to saturated；
(3) saturated NaCl and Na2SO4Feed liquid is evaporated in transport pump to 2nd effect evaporator, the NaCl crystal precipitated out is delivered to centrifugal salt making system, concentrated solution enters in triple effect evaporator, and a produced indirect steam part is used for the backflow heating in secondary heater, and a part adds vapours as triple effect evaporator；
The NaCl crystal precipitated out in triple effect evaporator is delivered to centrifugal salt making system, and concentrated solution enters four-effect evaporator, and a produced indirect steam part is used for heating primary heater internal reflux liquid, and a part adds vapours as four-effect evaporator；
The NaCl crystal precipitated out in four-effect evaporator is delivered to centrifugal salt making system, and the material after concentration arrange outside disposal except fraction, and all the other sequentially pass through after one-level, two grades and three grades of heaters preheatings in entrance 1st effective evaporator；
The Na that material precipitates out after entering 1st effective evaporator evaporation2SO4Crystal is delivered to centrifugal denitrating system, concentrated solution enters 2nd effect evaporator, and a produced indirect steam part is used for heating three grades of heater internal reflux liquid, a part then enters hot-pressing system and raw steam and adds vapours as add vapours, the remainder of 2nd effect evaporator as this effect。
2. back dissolving according to claim 1 benefit sal prunella divides salt to reclaim desulfurization wastewater technique of zero discharge, it is characterised in that: back dissolving tank wall is provided with steam heating shell, and in control back dissolving tank, temperature is at about 108 DEG C。
3. back dissolving according to claim 1 is mended sal prunella and is divided salt to reclaim desulfurization wastewater technique of zero discharge, it is characterised in that: one-level, two grades and three grades of heaters all adopt tubular heat exchanger。
4. back dissolving according to claim 1 mend sal prunella divide salt reclaim desulfurization wastewater technique of zero discharge, it is characterised in that: 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator evaporating temperature be gradually lowered；Deliver to saturated NaCl and the Na in 2nd effect evaporator2SO4Feed temperature is 108 DEG C, and the evaporating temperature of four-effect evaporator is 45 DEG C。
5. back dissolving benefit sal prunella divides salt to reclaim desulfurization wastewater Zero discharging system, including pretreatment concentration systems and salt manufacturing nitre system, wherein pretreatment concentration systems includes one-level softening settling system, dual membrane system, Buffer Pool, secondary softening settling system, preheater, MVR system, back dissolving tank；Salt making system includes 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator, primary heater, secondary heater, three grades of heaters, hot-pressing system, centrifugal salt making systems and is centrifuged nitre system processed, it is characterised in that
(1) desulfurization wastewater softens the double; two membrance concentration system of settling system entrance through one-level, arranges outside RO film clear liquid, and RO membrance concentration liquid enters Buffer Pool；
(2) in Buffer Pool, feed liquid sends into preheater after secondary softening settling system, enters MVR system and concentrate further after preheating, and concentrated solution is directly entered back dissolving tank and mixes NaCl and Na in feed liquid with the sal prunella crystal of backflow2SO4Mend to saturated；
(3) saturated NaCl and Na2SO4Feed liquid is evaporated in transport pump to 2nd effect evaporator, the NaCl crystal precipitated out is delivered to centrifugal salt making system, concentrated solution enters in triple effect evaporator, and a produced indirect steam part is used for the backflow heating in secondary heater, and a part adds vapours as triple effect evaporator；
The NaCl crystal precipitated out in triple effect evaporator is delivered to centrifugal salt making system, and concentrated solution enters four-effect evaporator, and a produced indirect steam part is used for heating primary heater internal reflux liquid, and a part adds vapours as four-effect evaporator；
The NaCl crystal precipitated out in four-effect evaporator is delivered to centrifugal salt making system, and the material after concentration arrange outside disposal except fraction, and all the other sequentially pass through after one-level, two grades and three grades of heaters preheatings in entrance 1st effective evaporator；
The Na that material precipitates out after entering 1st effective evaporator evaporation2SO4Crystal is delivered to centrifugal denitrating system, concentrated solution enters 2nd effect evaporator, and a produced indirect steam part is used for heating three grades of heater internal reflux liquid, a part then enters hot-pressing system and raw steam and adds vapours as add vapours, the remainder of 2nd effect evaporator as this effect。
6. back dissolving according to claim 5 benefit sal prunella divides salt to reclaim desulfurization wastewater Zero discharging system, it is characterised in that: back dissolving tank wall is provided with steam heating shell, and in control back dissolving tank, temperature is at about 108 DEG C。
7. back dissolving according to claim 5 is mended sal prunella and is divided salt to reclaim desulfurization wastewater Zero discharging system, it is characterised in that: one-level, two grades and three grades of heaters all adopt tubular heat exchanger。
8. back dissolving according to claim 5 mend sal prunella divide salt reclaim desulfurization wastewater Zero discharging system, it is characterised in that: 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, four-effect evaporator evaporating temperature be gradually lowered；Deliver to saturated NaCl and the Na in 2nd effect evaporator2SO4Feed temperature is 108 DEG C, and the evaporating temperature of four-effect evaporator is 45 DEG C。
CN201610130554.2A 2016-03-08 2016-03-08 Back dissolving mends sal prunella and divides salt recovery desulfurization wastewater Zero discharging system and technique Active CN105692998B (en)

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CN110217934A (en) * 2019-07-22 2019-09-10 四川省川南酿造有限公司 A kind of preparation method of pickled vegetable brine MVR evaporative crystallization

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