CN109179540A - Brine waste MVR salt potassium sub-prime crystallization processes - Google Patents
Brine waste MVR salt potassium sub-prime crystallization processes Download PDFInfo
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- CN109179540A CN109179540A CN201811252020.2A CN201811252020A CN109179540A CN 109179540 A CN109179540 A CN 109179540A CN 201811252020 A CN201811252020 A CN 201811252020A CN 109179540 A CN109179540 A CN 109179540A
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- salt
- evaporation tank
- flash evaporation
- temperature
- crystallizer
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Classifications
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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
- C02F1/048—Purification of waste water by evaporation
-
- 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
- C01D3/04—Chlorides
-
- 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
- C02F2103/06—Contaminated groundwater or leachate
-
- 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
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
-
- 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
Abstract
Brine waste MVR salt potassium sub-prime crystallization processes preheat brine waste by pre-heating system；Feed liquid enters evaporator after preheating, and the feed liquid after concentration goes successively to crystallizer, and the clarified mother liquor of crystallizer enters flash evaporation tank 1, and shwoot is simultaneously further concentrated, and is subsequently sent to flash evaporation tank 2, and crystalline potassium chloride is precipitated, and the clarified mother liquor of flash evaporation tank 2 returns to crystallizer.The crystallization sodium chloride salt that crystallizer salt leg is precipitated drains into salt slurry bucket 1 by salt leg, then send to thickener 1, and the slurry after thickening enters the dehydration of centrifuge 1；The wet feed solid come out from centrifuge 1 obtains crystallization sodium chloride salt finished product after entering drying bed drying.The sylvite slurry of flash evaporation tank 2 drains into salt slurry bucket 2, then send to thickener 2, and the slurry after thickening enters the dehydration of centrifuge 2；The solid come out from centrifuge is crystalline potassium chloride salt finished product.The present invention solves the pollution problem of high-concentration salt-containing wastewater, the water evaporation in brine waste obtain can reuse condensed water.
Description
Technical field
The invention belongs to wastewater processing technologies, in particular to garbage leachate wastewater, sintering grey waste water, desulfurization wastewater, smelting
The processing of the high-concentration salt-containing wastewaters such as golden waste water.
Background technique
In the industrial production, the brine waste that can often generate sodium chloride-containing, potassium chloride, such as garbage leachate wastewater, sintering
Grey waste water, desulfurization wastewater, Metallurgical Waste Water etc..As garbage incinerating power plant and refuse landfill can generate in the actual production process
A large amount of percolate waste water, these percolates contain the ingredients such as certain organic matter, ammonia nitrogen, other main components are mostly high concentration
Salt.Percolate waste water passes through pre-treating technology, and remaining saliferous is molten after degrading, eliminating the ingredients such as organic matter therein, ammonia nitrogen
The ingredients such as liquid, including sodium chloride, potassium chloride.The prior art handles these high-concentration salt-containing wastewaters and generally uses multiple-effect evaporation method,
Process flow is after preheating successively by multiple-effect evaporation tank, and the slurry come out through evaporator is dry by centrifugal dehydration, solid
To mixed salt product.The technique occupied area is larger, and control system is relative complex, and operating cost is high, and obtained product is mixed
Salt is closed, it can not resource utilization.
Summary of the invention
The purpose of the present invention is to provide a kind of processing methods of brine waste, are sodium chloride, chlorination for saline solns
The waste water of the ingredients such as potassium is evaporated sub-prime crystallization treatment, and obtaining can be with the condensed water of reuse, while obtaining meeting national standard
Sodium chloride and Potassium Chloride Product, realize zero-emission, and whole system occupied area is small, operating cost is low.
Technical solution of the present invention:
Brine waste MVR salt potassium sub-prime crystallization processes, brine waste are the ingredients such as sodium chloride, potassium chloride, including following technique step
It is rapid:
(a) temperature after the brine waste that salinity is 5%~8% is preheated by preheater is 85~100 DEG C, and heat source is evaporation system
The condensed water that system comes out.
(b) waste water after preheating enters evaporator concentration, and controlling temperature in evaporator is 100~115 DEG C, vapour compression machine
1 inlet steam temperature is 85~105 DEG C, and outlet steam temperature is 100~115 DEG C, and feed liquid is concentrated in evaporator, obtains
15%~20% concentrate.
(c) concentrate is transferred to crystallizer from evaporator, and controlling temperature in crystallizer is 95~110 DEG C, vapour compression machine 2
Inlet steam temperature is 80~90 DEG C, and outlet steam temperature is 100~110 DEG C, feed liquid further condensing crystallizing in crystallizer
Sodium chloride crystal out；Control loop materials in the tube liquid solid-to-liquid ratio is 15%~25%.
(d) clarified mother liquor is sent to flash evaporation tank 1 in crystallizer, and controlling temperature in flash evaporation tank 1 is 80~90 DEG C, flash steam temperature
Degree is 65~80 DEG C, and further a small amount of crystallization sodium chloride and potassium chloride mixture is precipitated in concentration to feed liquid in flash evaporation tank 1.
(e) salt slurry that flash evaporation tank 1 comes out by pump to the further shwoot of flash evaporation tank 2, control temperature in flash evaporation tank 2 be 45~
60 DEG C, flash steam temperature is 35~55 DEG C, and feed liquid crystallizes sodium chloride on a small quantity in flash evaporation tank 2 and re-dissolves, crystalline potassium chloride
It is precipitated, the clarified mother liquor of flash evaporation tank 2 is back to crystallizer.
(f) the sodium chloride salt slurry that crystallizer salt leg comes out is sent again by pump to salt slurry bucket 1 to thickener 1, controls thickener 1
Solid-to-liquid ratio be 40%~60%.
(g) salt slurry that thickener 1 comes out enters centrifuge 1, the wet feed moisture content 2.5%~4% that centrifuge 1 comes out.
(h) wet feed after centrifugal dehydration enters drying bed, and crystallization sodium chloride salt product is obtained after dry.
The potassium chloride salt slurry that (i) flash evaporation tank 2 comes out is sent again by pump to salt slurry bucket 2 to thickener 2, and thickener 2 is controlled
Solid-to-liquid ratio is 40%~60%.
(j) salt slurry that thickener 2 comes out enters centrifuge 2, the wet feed moisture content 2.5%~4% that centrifuge 2 comes out.
(k) crystalline potassium chloride product salt is obtained after centrifugal dehydration.
Temperature in the step (a) after the preheating of control preheater is preferably 90~95 DEG C.
Temperature is preferably 100~110 DEG C in control evaporator in the step (b).
Temperature is preferably 100~105 DEG C in control crystallizer in the step (c).
Temperature is preferably 80~85 DEG C in control flash evaporation tank 1 in the step (d).
Temperature is preferably 45~50 DEG C in control flash evaporation tank 2 in the step (e).
Beneficial effects of the present invention: mechanical hot pressing contracting falling film concentration technology, mechanical hot pressing contracting external-heating forced circulation are used
Evaporator analyses the combined process of sodium salt+second level shwoot cooling analysis sylvite, by vapour compression machine by the secondary steam of evaporation again
The heating room of evaporator or crystallizer is pushed back, is so recycled, makes that whole system occupied area is small, operating cost is low.One side
Face realizes the salt potassium separation in brine waste, obtains the sodium chloride for meeting national standard and Potassium Chloride Product；An other side
Face, the condensed water of evaporation process meet reuse or outlet requirement, realize the double goal of zero-emission and recycling.
Detailed description of the invention
Fig. 1 is brine waste MVR salt potassium sub-prime crystallization processes flow diagram.
Specific embodiment
Embodiment 1
Brine waste MVR salt potassium sub-prime crystallization processes.25 DEG C, concentration be 5.5%(sodium chloride 3.7%, potassium chloride 1.8%) saliferous
Temperature after waste water is preheated by preheater is 94 DEG C, and heat source is the condensed water that vapo(u)rization system comes out；Waste water after preheating enters
Evaporator, controlling temperature in evaporator is 102.5 DEG C, and the inlet steam temperature of vapour compression machine 1 is 97.5 DEG C, outlet vapor temperature
Degree be 106.5 DEG C, feed liquid is concentrated in evaporator, obtains 18%(sodium chloride 12.1%, potassium chloride 5.9%) concentrate；Concentrate
It is transferred to crystallizer, controlling temperature in crystallizer is 100 DEG C, and the inlet steam temperature of vapour compression machine 2 is 87.5 DEG C, outlet vapor
Temperature is 106.5 DEG C, and further crystallization sodium chloride salt is precipitated in concentration to feed liquid in crystallizer；Control loop materials in the tube liquid solid-to-liquid ratio is
20%；Clarified mother liquor is sent to flash evaporation tank 1 in crystallizer, and controlling temperature in flash evaporation tank 1 is 83 DEG C, and flash steam temperature is 74 DEG C, material
Further a small amount of crystallization sodium chloride and potassium chloride mixture is precipitated in concentration to liquid in flash evaporation tank 1；The salt slurry that flash evaporation tank 1 comes out passes through
Pump is to the further shwoot of flash evaporation tank 2, and controlling temperature in flash evaporation tank 2 is 50 DEG C, and flash steam temperature is 42 DEG C, and feed liquid is in flash evaporation tank
Sodium chloride is crystallized in 2 on a small quantity to re-dissolve, crystalline potassium chloride is precipitated；Sodium chloride salt slurry in crystallizer is expelled to salt by salt leg
Slurry bucket, pump to thickener 1, the solid-to-liquid ratio for controlling thickener is 50%；The salt slurry that thickener 1 comes out enters centrifuge 1, centrifuge 1
Wet feed moisture content 3% out；Dewatered wet feed enters drying bed, obtains sodium chloride product after dry, product quality reaches
The dry salt secondary standard quality index requirement of industry in GB/T5462-2015 refining industrial salt.2 potassium chloride salt slurry of flash evaporation tank passes through
Salt leg is expelled to sylvite slurry bucket, and pump to thickener 2, the solid-to-liquid ratio for controlling thickener 2 is 50%；The salt slurry that thickener 2 comes out enters
Centrifuge 2, the wet feed moisture content 3% that centrifuge 2 comes out, obtains Potassium Chloride Product, product quality reaches GB/T7118-2008 bis-
Grade product standard quality index request.
Embodiment 2
Brine waste MVR salt potassium sub-prime crystallization processes.25 DEG C, concentration be 5.0%(sodium chloride 3.1%, potassium chloride 1.9%) saliferous
Temperature after waste water is preheated by preheater is 92 DEG C, and heat source is the condensed water that vapo(u)rization system comes out；Waste water after preheating enters
Evaporator, controlling temperature in evaporator is 107.5 DEG C, and the inlet steam temperature of vapour compression machine 1 is 103.5 DEG C, outlet vapor
Temperature be 111.5 DEG C, feed liquid is concentrated in evaporator, obtains 17.9%(sodium chloride 11.2%, potassium chloride 6.7%) concentrate；It is dense
Contracting liquid is transferred to crystallizer, and controlling temperature in crystallizer is 105 DEG C, and the inlet steam temperature of vapour compression machine 2 is 93.5 DEG C, outlet
Vapor (steam) temperature is 111.5 DEG C, and further crystallization sodium chloride salt is precipitated in concentration to feed liquid in crystallizer；Control loop materials in the tube liquid solid-liquid
Than being 20%；Clarified mother liquor is sent to flash evaporation tank 1 in crystallizer, and controlling temperature in flash evaporation tank 1 is 83 DEG C, and flash steam temperature is 74
DEG C, further a small amount of crystallization sodium chloride and potassium chloride mixture is precipitated in concentration to feed liquid in flash evaporation tank 1；The salt that flash evaporation tank 1 comes out
For slurry by pump to the further shwoot of flash evaporation tank 2, controlling temperature in flash evaporation tank 2 is 50 DEG C, and flash steam temperature is 42 DEG C, and feed liquid exists
Sodium chloride is crystallized in flash evaporation tank 2 on a small quantity to re-dissolve, crystalline potassium chloride is precipitated；Sodium chloride salt slurry in crystallizer is arranged by salt leg
Out to salt slurry bucket, pump to thickener 1, the solid-to-liquid ratio for controlling thickener is 50%；The salt slurry that thickener 1 comes out enters centrifuge 1,
The wet feed moisture content 3% that centrifuge 1 comes out；Dewatered wet feed enters drying bed, obtains sodium chloride product, product matter after dry
Amount reaches the dry salt secondary standard quality index requirement of the industry in GB/T5462-2015 refining industrial salt.2 potassium chloride salt of flash evaporation tank
Slurry is expelled to sylvite slurry bucket by salt leg, and pump to thickener 2, the solid-to-liquid ratio for controlling thickener 2 is 50%；The salt that thickener 2 comes out
Slurry enters centrifuge 2, and the wet feed moisture content 3% that centrifuge 2 comes out obtains Potassium Chloride Product, product quality reaches GB/T7118-
2008 seconds standard quality index requests.
Claims (6)
1. brine waste MVR salt potassium sub-prime crystallization processes, brine waste includes sodium chloride, chlorination potassium composition, it is characterised in that packet
Include following steps:
(a) temperature after the brine waste that salinity is 5%~8% is preheated by preheater is 85~100 DEG C, and heat source is evaporation system
The condensed water that system comes out；
(b) waste water after preheating enters evaporator concentration, and controlling temperature in evaporator is 100~115 DEG C, vapour compression machine 1
Inlet steam temperature is 85~105 DEG C, and outlet steam temperature is 100~115 DEG C, and feed liquid is concentrated in evaporator, obtain 15%~
20% concentrate；
(c) concentrate is transferred to crystallizer from evaporator, and controlling temperature in crystallizer is 95~110 DEG C, the entrance of vapour compression machine 2
Vapor (steam) temperature is 80~90 DEG C, and outlet steam temperature is 100~110 DEG C, and feed liquid further condensing crystallizing in crystallizer goes out chlorine
Change sodium crystal；Control loop materials in the tube liquid solid-to-liquid ratio is 15%~25%；
(d) clarified mother liquor is sent to flash evaporation tank 1 in crystallizer, and controlling temperature in flash evaporation tank 1 is 80~90 DEG C, and flash steam temperature is
65~80 DEG C, further a small amount of crystallization sodium chloride and potassium chloride mixture is precipitated in concentration to feed liquid in flash evaporation tank 1；
(e) for the salt slurry that flash evaporation tank 1 comes out by pump to the further shwoot of flash evaporation tank 2, controlling temperature in flash evaporation tank 2 is 45~60
DEG C, flash steam temperature is 35~55 DEG C, and feed liquid crystallizes sodium chloride on a small quantity in flash evaporation tank 2 and re-dissolves, crystalline potassium chloride analysis
Out, the clarified mother liquor of flash evaporation tank 2 is back to crystallizer；
(f) the sodium chloride salt slurry that crystallizer salt leg comes out is sent again by pump to salt slurry bucket 1 to thickener 1, controls consolidating for thickener 1
Liquor ratio is 40%~60%；
(g) salt slurry that thickener 1 comes out enters centrifuge 1, the wet feed moisture content 2.5%~4% that centrifuge 1 comes out；
(h) wet feed after centrifugal dehydration enters drying bed, and crystallization sodium chloride salt product is obtained after dry；
The potassium chloride salt slurry that (i) flash evaporation tank 2 comes out is sent again by pump to salt slurry bucket 2 to thickener 2, and the solid-liquid of thickener 2 is controlled
Than being 40%~60%；
(j) salt slurry that thickener 2 comes out enters centrifuge 2, the wet feed moisture content 2.5%~4% that centrifuge 2 comes out；
(k) crystalline potassium chloride product salt is obtained after centrifugal dehydration.
2. brine waste MVR salt potassium sub-prime crystallization processes according to claim 1, it is characterised in that: control in step (a)
Temperature after preheater preheating is 90~95 DEG C.
3. brine waste MVR salt potassium sub-prime crystallization processes according to claim 1, it is characterised in that: control in step (b)
Temperature is 100~110 DEG C in evaporator.
4. brine waste MVR salt potassium sub-prime crystallization processes according to claim 1, it is characterised in that: control in step (c)
Temperature is 100~105 DEG C in crystallizer.
5. brine waste MVR salt potassium sub-prime crystallization processes according to claim 1, it is characterised in that: control in step (d)
Temperature is 80~85 DEG C in flash evaporation tank 1.
6. brine waste MVR salt potassium sub-prime crystallization processes according to claim 1, it is characterised in that: control in step (e)
Temperature is 45~50 DEG C in flash evaporation tank 2.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811252020.2A CN109179540A (en) | 2018-10-25 | 2018-10-25 | Brine waste MVR salt potassium sub-prime crystallization processes |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110183022A (en) * | 2019-06-18 | 2019-08-30 | 上海晶宇环境工程股份有限公司 | A kind of evaporative crystallization technique and special equipment reducing carnallite rate |
| CN111056682A (en) * | 2020-01-08 | 2020-04-24 | 福州大学 | Evaporative concentration and sectional crystallization method for RO concentrated solution of landfill leachate |
| CN111302309A (en) * | 2020-01-20 | 2020-06-19 | 泰安渤洋化工科技有限公司 | Process device and method for continuous crystal form passivation and modification of hydrotalcite product |
| CN111908533A (en) * | 2020-06-26 | 2020-11-10 | 中国轻工业长沙工程有限公司 | Treatment process of high-concentration high-salt mother liquor in zero discharge of wastewater |
| CN112110517A (en) * | 2020-09-21 | 2020-12-22 | 北京今大禹环境技术股份有限公司 | Method for separating crystalline salt from high organic matter crystalline salt solution |
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| CN112110517A (en) * | 2020-09-21 | 2020-12-22 | 北京今大禹环境技术股份有限公司 | Method for separating crystalline salt from high organic matter crystalline salt solution |
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