CN108358369A - A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment process method and device - Google Patents
A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment process method and device Download PDFInfo
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- CN108358369A CN108358369A CN201810193920.8A CN201810193920A CN108358369A CN 108358369 A CN108358369 A CN 108358369A CN 201810193920 A CN201810193920 A CN 201810193920A CN 108358369 A CN108358369 A CN 108358369A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 81
- 230000008020 evaporation Effects 0.000 title claims abstract description 76
- 239000012452 mother liquor Substances 0.000 title claims abstract description 73
- 239000012267 brine Substances 0.000 title claims abstract description 52
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 46
- 150000003839 salts Chemical class 0.000 title claims abstract description 34
- 239000002699 waste material Substances 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 93
- 230000000694 effects Effects 0.000 claims abstract description 82
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 claims abstract description 65
- 239000013078 crystal Substances 0.000 claims abstract description 64
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 58
- 238000002425 crystallisation Methods 0.000 claims abstract description 35
- 230000008025 crystallization Effects 0.000 claims abstract description 35
- 238000005352 clarification Methods 0.000 claims abstract description 24
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 21
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 21
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000011575 calcium Substances 0.000 claims abstract description 17
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 17
- 239000003513 alkali Substances 0.000 claims abstract description 15
- 159000000003 magnesium salts Chemical class 0.000 claims abstract description 14
- 239000002002 slurry Substances 0.000 claims abstract description 13
- 238000001914 filtration Methods 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 239000012528 membrane Substances 0.000 claims abstract description 9
- 239000000919 ceramic Substances 0.000 claims abstract description 8
- 238000004062 sedimentation Methods 0.000 claims abstract description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 60
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 37
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 35
- 239000007787 solid Substances 0.000 claims description 26
- 239000002253 acid Substances 0.000 claims description 20
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 20
- 235000017550 sodium carbonate Nutrition 0.000 claims description 17
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 17
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 14
- 150000002500 ions Chemical class 0.000 claims description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 13
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 13
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 12
- 239000006228 supernatant Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000000047 product Substances 0.000 claims description 9
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 8
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 8
- 229910001424 calcium ion Inorganic materials 0.000 claims description 8
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 229910000831 Steel Inorganic materials 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 230000007797 corrosion Effects 0.000 claims description 6
- 238000005260 corrosion Methods 0.000 claims description 6
- 239000011780 sodium chloride Substances 0.000 claims description 6
- 239000010959 steel Substances 0.000 claims description 6
- 239000000725 suspension Substances 0.000 claims description 6
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 230000003139 buffering effect Effects 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000007792 addition Methods 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 3
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 3
- 239000000347 magnesium hydroxide Substances 0.000 claims description 3
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 2
- 239000010413 mother solution Substances 0.000 claims description 2
- 231100000614 poison Toxicity 0.000 claims description 2
- 230000007096 poisonous effect Effects 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 230000007423 decrease Effects 0.000 claims 1
- 229910052573 porcelain Inorganic materials 0.000 claims 1
- 238000001556 precipitation Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 238000007872 degassing Methods 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 230000003373 anti-fouling effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000006194 liquid suspension Substances 0.000 description 1
- 150000001455 metallic ions Chemical class 0.000 description 1
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000000941 radioactive substance Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
Classifications
-
- 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
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- 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
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/08—Corrosion inhibition
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
Landscapes
- 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)
Abstract
A kind of brine waste is concentrated by evaporation mother liquor and divides salt recovery processing technique method and device, it is characterized in that the method includes the following steps：First, brine waste is concentrated by evaporation mother liquor to be sent into except hard pretreatment unit pre-processes, by two alkali dosings, inclined plate sedimentation, ceramic membrane filter and calcium and magnesium salt slurry press filtration, obtains clarification high temperature brine；Secondly, the clarification high temperature brine obtained after except hard pretreatment is sent into an effect sodium sulphate crystal system, entering crystallizer after crystallization heater heats up is concentrated by evaporation, then isolates sodium sulfate salt and primary crystallization mother liquor by centrifugal dehydrator；Third, primary crystallization mother liquor is sent into two effect carnallite crystal systems to be further concentrated by evaporation, feed liquid after evaporation and concentration enters back into centrifugal dehydrator and isolates carnallite and secondary crystallization mother liquor, and secondary crystallization mother liquor, which returns to mix with primary crystallization mother liquor in two effect carnallite crystal systems, carries out circulating and evaporating concentration.Present invention process flow is succinct, low energy consumption, and the pure salt quality of sodium sulphate of separation and recovery is high.
Description
Technical field
The present invention relates to a kind of green technology, especially a kind of wastewater processing technology, specifically a kind of brine waste
It is concentrated by evaporation mother liquor and divides salt recovery processing method and device.
Background technology
Brine waste acquires process essentially from chemical plant and coal, oil, natural gas, contains many kinds of substance, packet
Include inorganic salts, oil, organic matter heavy metal and radioactive substance etc..Brine waste the way of production is extensive, and water also increases year by year.It should
The directly outer row of class waste water, can cause river water quality salinity to increase, further serious dirt is brought to soil, surface water, underground water
Dye destroys ecological environment.The increasingly strict environmental protection policy of country forces the dirty Business Enterprise Adopting New Technology of each production, new process, realizes dirty
Water harnessing and reuse.In recent years, with the rise of the proposition and the relevant technologies of waste water near-zero release theory, brine waste is controlled
Reason has formd a series of effective treatment measures.Brine waste is by pretreatment, film concentration, then arrives and be concentrated by evaporation,
Evaporation pond is arranged outside the highly concentrated mother liquor formed continues natural evaporation, it is final to realize waste liquid near-zero release.That realizes water effectively repeats profit
With protecting water ecological environment, save water resource, reduce operation cost of enterprises.
To being concentrated by evaporation mother liquid disposal, technology is generally achieved the nearly zero-emission of waste liquid by evaporation pond natural evaporation earlier
It puts.But since the evaporation efficiency of most of built evaporation pond is difficult to reach design requirement, and evaporation pond occupies a large amount of soil
Resource cannot be satisfied following discharge needs.On the other hand, the solid carnallite that evaporation pond natural evaporation generates, it is qualitative at present
Difficulty usually carries out security landfill processing as dangerous solid waste.The expense handled as hazardous waste per ton 2000 ~
3000 yuan or so, high processing cost increases enterprise's production cost.In view of the above-mentioned problems, being badly in need of developing a kind of high efficiency, low cost
It will be concentrated by evaporation the further sub-prime crystallization technique of mother liquor, realize solid carnallite recycling.Solve the same of dangerous waste disposal difficulties
When, recycling has the inorganic salts of economic value to sell outside, to reduce zero-emission operating cost.
In general, being concentrated by evaporation before mother liquor generation, feed liquid is handled by conventional sewage treatment technology means：
Such as bioanalysis（A/O, A2/O, SBR, BAF）Or advanced oxidation processes（Iron-carbon micro-electrolysis, Fenton process, ozone oxidation, WAO）It reduces former
Water content of organics；Calcium and magnesium hardness ions and heavy metal ion content in raw water are reduced by the way that water treatment agent is added, is suspended
Object and colloidal ion content are also greatly reduced.Therefore, evaporator discharge concentrated mother liquor water quality situation is stablized and is easy to control relatively
System.Mother liquor will be concentrated by evaporation and directly carry out sub-prime crystallization treatment, the high temperature heat of outer row's mother liquor on the one hand can be utilized, reduce crystallization
System thermal energy consumption.On the other hand, reduce crystal system adding of agent so that brine waste near-zero release technique obtain upgrading and
Closed loop, is finally reached waste liquid near-zero release and crystal salt recycling efficiently uses dual purpose.
Invention content
It is of high cost the purpose of the present invention is being directed to existing evaporation and concentration mother liquor harmless treatment, it can not achieve resource reclaim
The problem of utilization, invents a kind of recycling brine waste and is concentrated by evaporation mother liquor and divide salt recovery processing method, while providing phase
The device answered.
One of technical scheme of the present invention is：
A kind of brine waste is concentrated by evaporation mother liquor and divides salt recovery processing technique method, it is characterized in that it includes the following steps：
First, brine waste mother liquor is concentrated by evaporation to be sent into except hard pretreatment unit pre-processes, by two alkali dosings, inclined plate
Sedimentation, ceramic membrane filter and calcium and magnesium salt slurry press filtration obtain clarification high temperature brine；
Secondly, the clarification high temperature brine that will be obtained after removing pretreatment firmly is sent into an effect sodium sulphate crystal system, adds by crystallizing
Enter crystallizer after hot device heating to be concentrated by evaporation, then sodium sulfate salt and primary crystallization mother liquor are isolated by centrifugal dehydrator；
Primary crystallization mother liquor is sent into two effect carnallite crystal systems and is further concentrated by evaporation by third, the feed liquid after evaporation and concentration
It enters back into centrifugal dehydrator and isolates carnallite and secondary crystallization mother liquor, secondary crystallization mother liquor returns in two effect carnallite crystal systems
It is mixed with primary crystallization mother liquor and carries out circulating and evaporating concentration.
The secondary steam part that crystallization heater in the one effect sodium sulphate crystal system generates is as two effect carnallites
The heat source of crystallizing evaporator in crystal system.
The clarification high temperature brine makes basicity ion in feed liquid be reacted with acid by adding acid for adjusting pH in 5 ~ 6 ranges
Generate carbon dioxide discharge；Feed liquid is after deaerator is handled, and dissolubility on-condensible gas is discharged in feed liquid, to reduce equipment fortune
The possibility of fouling and corrosion occurs during row, the clarification high temperature brine after adjusting acid degassing is then sent into an effect sulfuric acid again
Receive crystal system,
The brine waste is concentrated by evaporation mother liquor and is mainly made of sodium chloride and sodium sulphate, and salinity accounting is more than 80%, sodium sulphate
It is more than 3.5 with sodium chloride mass ratio：1；；Total dissolved solid content in the mg/L of 80000 mg/L ~ 130000, temperature 80 DEG C ~
90 DEG C, containing a small amount of foreign ion, poisonous and harmful heavy metallic ion, COD are not containedcrContent is less than 1500mg/L.
The two alkali dosings refer to that successively addition caustic soda and soda ash, caustic soda and soda ash are configured to solution and are thrown by pipeline
Add；Dosing reaction device is furnished with blender so that medicament is added and is uniformly mixed rapidly, reacts abundant with feed liquid；Material after dosing
For liquid pH in 11 ~ 12 ranges, the sum of calcium ions and magnesium ions concentration is less than 50mg/L.
It includes carbonic acid that feed liquid forms suspended particulate and flocculent substance, main component after two alkali dosings reaction, in solution
Calcium, magnesium hydroxide, silica；Mix suspending object settling property is good, after inclined plate settler, supernatant liquor suspension content
It is greatly reduced；Supernatant liquor is successively into obtained clarification feed liquid after coarse filter and purpose ceramic-film filter excessively；The highly concentrated turbid of lower layer
By filtering equipment, calcium and magnesium salt slurry, outward transport disposition are obtained.
Total suspended matter solid content after coarse filtration equipment and the filtering of ceramic membrane filter equipment in feed liquid further drops
Low, TSS is less than 1mg/L.
The one effect sulfate crystal system is using pressure outer circulation crystallizer（FC types）, feeding manner be it is axial into
Material can eliminate liquid level vortex, reduce cycle feed liquid short circuit temperature loss；Vaporization chamber section evaporation intensity improves, and salt crystal grain is precipitated
Diameter is larger, is conducive to the raising of the pure salt quality of follow-up workshop section's sodium sulphate；After evaporating the indirect steam part generated by condensation
As product water reuse, another part is as two effect carnallite crystallizer heat sources；Effectively reduce raw steam consumption.
Feed liquid is concentrated by evaporation to 30% or so during the sulfate crystal, starts that crystal salt is precipitated, and is suspended admittedly when total
Body reaches 10% ~ 15%, and feed liquid enters centrifugal dehydrator and isolates sodium sulfate salt, and crystalline mother solution enters carnallite crystallizer, further
After evaporation and concentration, carnallite is isolated by centrifuge dewatering machine.
The sodium sulfate salt and carnallite that the centrifugal dehydrator is isolated, sodium sulfate salt moisture content are 10% or so, and carnallite is aqueous
Rate is 50% ~ 60%；Carnallite moisture content height is conducive to the highly concentrated mother liquor of entrainment portions and goes out system, plays and periodically arranges dense purpose, realizes useless
Liquid near-zero release；Sodium sulphate centrifugal dehydrator uses double push-material formula or horizontal helical type, carnallite centrifuge to use horizontal helical type.
Technical scheme of the present invention second is that：
A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment device, it is characterized in that it includes：
One removes hard pretreatment unit, which obtains for that will carry out pretreatment into evaporation and concentration mother liquor therein
High temperature brine must be clarified, while obtaining the outward transport of calcium and magnesium salt slurry；
One adjusts sour degasser；The tune acid degasser is used for will be through the pH except the pretreated clarification high temperature brine of hard pretreatment unit
Adjustment makes basicity ion in feed liquid react generation carbon dioxide discharge with acid, to reduce in equipment running process in 5 ~ 6 ranges
The possibility of fouling and corrosion occurs；
Sulfuric acid steel crystal system is imitated one by one, and the effect sulfuric acid steel crystal system is mainly de- by an effect heating crystalline device and an effect centrifugation
Water dispenser forms, and crystal salt is precipitated in the clarification high temperature brine heating concentration after adjusting sour degasser tune acid to deaerate by heating crystalline device,
And it is discharged into when suspended solid reaches 10%-15% in centrifugal dehydrator and isolates the sodium sulfate salt that moisture content is no more than 10%；Heating
Crystallizer adds a thermogenetic steam part as the heat source of two effect carnallite crystal systems, and another is made after condenser condenses
For product water reuse；
One or two effect carnallite crystal systems, the two effect carnallites crystal system is mainly by two effect heating crystalline devices and two effect centrifugal dehydrators
The feed liquid of composition, an effect centrifugal dehydrator discharge generates carnallite after pipeline is sent into two effect heating crystalline device heating, is sent into two effects
Centrifugal dehydrator dehydration obtains the carnallite that moisture content is 50-60%, and the feed liquid for deviating from carnallite enters two effect carnallites again by pipeline
Enter in two effect heating crystalline devices after being mixed with the feed liquid of an effect centrifugal dehydrator discharge in crystal system；Two effect heating crystalline devices
It is used as product water reuse after the condensed device condensation of steam of generation.
It is described except hard pretreatment unit is mainly by homogeneous tank, caustic soda retort, soda ash retort, inclined plate settler, clear
Flow container, coarse filter, purpose ceramic-film filter, NaOH solution tank NaOH and filter press composition are concentrated by evaporation mother liquor and enter homogeneous tank progress water quality
Buffering is adjusted, and avoids influence of the water quality larger fluctuation to process system, and the evaporation and concentration mother liquor after the adjusting of homogeneous tank is advanced
Enter to be added in caustic soda retort after caustic soda is stirred to react to be re-fed into soda ash retort and soda ash support is added mixes, reaction generates a large amount of outstanding
Floating particles and flocculent substance, enter back into inclined plate settler, are divided into the dense liquid of supernatant liquor and lower layer, and dense liquid enters dope tank again
It is sent into filter press and is press-filtered out the outward transport of calcium and magnesium salt slurry；Supernatant clear liquid enters in Clear liquid tank flows into coarse filter filtering again, eventually enters into
It is filtered in purpose ceramic-film filter and obtains calcium ions and magnesium ions concentration to reduce total suspended solid content in feed liquid and be less than 50mg/L, it is total outstanding
Floating solid content is less than the clarification high temperature brine of 1mg/L.
Beneficial effects of the present invention：
Evaporation and concentration mother liquor passes through removes hard pretreatment unit above, at sulfate crystal recovery unit and other carnallite crystalline elements
After reason, most water and sodium sulphate salinity in evaporation and concentration mother liquor have finally been recycled.Realize the complete zero-emission of waste liquid and resource
Change efficiently uses purpose, and heat exchanger heat-exchanging tube using efficient special type pipe (such as interior wave male-pipe, bellows, it is inner or outer or
Inside and outside conduit pipe), greatly reduce heat transmission equipment size, energy-saving effect is clearly.
The present invention's divides the feature that salt technique fully considers row dense mother liquor of the brine waste after evaporation and concentration, and it is suitable to select
Pretreating process device, pass through two effect crystal systems realize salinities recycle.The whole series divide that salt technological process is succinct, energy consumption
Low, the pure salt quality of sodium sulphate of separation and recovery is high.
Description of the drawings
Fig. 1 is that the evaporation and concentration mother liquor of the present invention divides salt process unit composed structure schematic diagram.
Fig. 2 be the present invention except hard pretreatment unit composition and flow diagram.
Specific implementation mode
The present invention is further illustrated with reference to the accompanying drawings and examples.
Embodiment one.
A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment process method, it includes the following steps：
First, brine waste mother liquor is concentrated by evaporation to be sent into except hard pretreatment unit pre-processes, by two alkali dosings, inclined plate
Sedimentation, ceramic membrane filter and calcium and magnesium salt slurry press filtration obtain clarification high temperature brine；
Secondly, clarification high temperature brine is carried out adjusting acid degassing reaction, the dissolvings such as the dissolved oxygen eliminated in feed liquid is reacted by acid adding
Property on-condensible gas；
Third, the clarification high temperature brine that will be obtained after removing pretreatment firmly are sent into an effect sodium sulphate crystal system, are added by crystallizing
Enter crystallizer after hot device heating to be concentrated by evaporation, then sodium sulfate salt and primary crystallization mother liquor are isolated by centrifugal dehydrator；
4th, primary crystallization mother liquor is sent into two effect carnallite crystal systems and is further concentrated by evaporation, the feed liquid after evaporation and concentration
It enters back into centrifugal dehydrator and isolates carnallite and secondary crystallization mother liquor, secondary crystallization mother liquor returns in two effect carnallite crystal systems
It is mixed with primary crystallization mother liquor and carries out circulating and evaporating concentration.
Details are as follows：
Soluble solid content is in the mg/L of 80000 mg/L ~ 130000, salinity in the brine waste evaporation and concentration mother liquor
It is mainly made of sodium chloride and sodium sulphate, two kinds of salt quality accountings are more than 80%, and sodium sulphate is more than 3.5 with sodium chloride mass ratio:1,
Separately contain a small amount of foreign ion, CODcrContent is less than 1500mg/L, and feed temperature is at 80 ~ 90 DEG C.Mother liquor is concentrated by evaporation to pass through successively
It crosses and removes hard pretreatment unit, sulfate crystal recovery unit and other carnallite crystalline elements.Using two effect crystallization processes, an effect is
Sulfate crystal device is heated by outer for steam；Two effects are carnallite crystallizer, and the indirect steam generated by an effect is as heating warm
Source.Dosing pretreatment stage, high temperature concentrated mother liquor pass through caustic soda dosing retort, soda ash dosing retort, inclined plate sedimentation successively
Device, coarse filter, purpose ceramic-film filter finally obtain clarified brine, and highly concentrated turbid obtains calcium and magnesium salt mud cake by filter press, female
Liquid is back to pretreatment front end.Two alkali retort medicament additions are with according to calcium and magnesium hardness number timely adjustment in actual water sample, to burn
PH controls are advisable 11 ~ 12 in alkali and soda ash retort.Calcium ions and magnesium ions and a small amount of heavy metal ion are reacted with two alkali in feed liquid, raw
At magnesium hydroxide flco and calcium carbonate solid, while small amounts silicon and organic matter are adsorbed, ultimately forms cotton-shaped suspension.Through one
After road inclined plate settler, supernatant liquor suspension content substantially reduces；Through two coarse filters, feed liquid suspension content is further
It reduces；Through three purpose ceramic-film filters, clarified brine is obtained, total suspended solid content is less than 1mg/L.Due to feed liquid salinity compared with
It is high and contain organic components, it is equipped with a set of ceramic membrane on-line cleaning system, hot water rinsing, pickling and alkali cleaning is realized, reaches anti-caking
Dirty, antifouling stifled purpose.
By removing hard pretreatment unit, it is concentrated by evaporation the sum of calcium ions and magnesium ions concentration in mother liquor and is less than 50mg/L, total suspension is solid
Body content is less than 1mg/L, and pH is 11 or so.After adjusting sour degasification, feed liquid enters sulfate crystal recovery unit.Acid adding tune
PH is saved in 5 ~ 6 ranges, basicity ion is reacted with acid in feed liquid generates carbon dioxide discharge.Feed liquid will be in feed liquid by deaerator
Except the dissolubilities on-condensible gas such as dissolved oxygen is exhausted from system, the possibility that fouling and corrosion occur in equipment running process is reduced
Property.After crystallization heater, the further temperature raising of feed liquid, crystallization heater outlet temperature is controlled at 105 ~ 110 DEG C, into crystallization
It is concentrated by evaporation in device, the indirect steam of generation is used as two effect carnallite crystalline element heat sources by demister rear portion, remains
Remaining part lease making is used as recycle-water after crossing condensation, recycles.Crystallizer using forcing outer circulation FC types, feeding manner be it is axial into
Material can eliminate liquid level vortex, reduce cycle feed liquid short circuit temperature loss.Vaporization chamber section evaporation intensity improves, and salt crystal grain is precipitated
Diameter is larger, is conducive to the raising of the pure salt quality of follow-up workshop section's sodium sulphate.Mother liquid concentration control is arranged outside sulfate crystal device bottom to exist
30% or so, total suspended solid(s) (TSS) is controlled 10% ~ 15%.Outer row's mother liquor obtains solid sulphuric acid sodium salt after centrifugal dehydrator,
Moisture content is 10% or so.The mother liquor of abjection, to two effect carnallite crystalline elements, continues carnallite crystallization operation by Pipeline transport.
Two effect carnallite crystalline element feeding liquids, are directly over the heating of carnallite crystallization heater, and it is laggard further to increase temperature
Enter carnallite crystallizer.Carnallite crystallizer is in negative pressure after being handled by vacuum pump, realizes that multiple-effect evaporation crystallizes purpose, reduces energy damage
Consumption.Using tangential admission mode, it can effectively prevent crystallizer wall surface and generate serious scale phenomenon.Mother is arranged outside carnallite crystalliser feet
The control of liquid concentration is controlled in 40%-45%, total suspended solid(s) (TSS) in 10%-15%.Outer row's mother liquor obtains after centrifuge dewatering machine
Carnallite, abjection mother liquor, which is back in carnallite crystal system, beats cycle, and carnallite moisture content is 50% ~ 60%.High-moisture percentage is conducive to press from both sides
The highly concentrated mother liquor of band part goes out system, plays and periodically arranges dense purpose.Due to arranging content of organics in mother liquor outside two effect carnallite crystallizers
Higher, much larger than content of organics in row's mother liquor outside first effect sulfate crystal device, therefore double push away can be used in sodium sulphate centrifugal dehydrator
Material formula or horizontal helical type, carnallite centrifuge use horizontal helical type.
Embodiment two.
A kind of brine waste is concentrated by evaporation mother liquor and divides salt treatment device, as shown in Figure 1, it includes：
One removes hard pretreatment unit, which obtains for that will carry out pretreatment into evaporation and concentration mother liquor therein
High temperature brine must be clarified, while obtaining the outward transport of calcium and magnesium salt slurry；
One adjusts sour degasser；The tune acid degasser is used for will be through the pH except the pretreated clarification high temperature brine of hard pretreatment unit
Adjustment makes basicity ion in feed liquid react generation carbon dioxide discharge with acid, to reduce in equipment running process in 5 ~ 6 ranges
The possibility of fouling and corrosion occurs；
Sulfuric acid steel crystal system is imitated one by one, and the effect sulfuric acid steel crystal system is mainly de- by an effect heating crystalline device and an effect centrifugation
Water dispenser forms, and crystal salt is precipitated in the clarification high temperature brine heating concentration after adjusting sour degasser tune acid to deaerate by heating crystalline device,
And it is discharged into when suspended solid reaches 10%-15% in centrifugal dehydrator and isolates the sodium sulfate salt that moisture content is no more than 10%；Heating
Crystallizer adds a thermogenetic steam part as the heat source of two effect carnallite crystal systems, and another is made after condenser condenses
For product water reuse；
One or two effect carnallite crystal systems, the two effect carnallites crystal system is mainly by two effect heating crystalline devices and two effect centrifugal dehydrators
The feed liquid of composition, an effect centrifugal dehydrator discharge generates carnallite after pipeline is sent into two effect heating crystalline device heating, is sent into two effects
Centrifugal dehydrator dehydration obtains the carnallite that moisture content is 50-60%, and the feed liquid for deviating from carnallite enters two effect carnallites again by pipeline
Enter in two effect heating crystalline devices after being mixed with the feed liquid of an effect centrifugal dehydrator discharge in crystal system；Two effect heating crystalline devices
It is used as product water reuse after the condensed device condensation of steam of generation.
It is described to remove hard pretreatment unit as shown in Fig. 2, it is mainly by homogeneous tank, caustic soda retort, soda ash retort, tiltedly
Plate settler, Clear liquid tank, coarse filter, purpose ceramic-film filter, NaOH solution tank NaOH and filter press composition, are concentrated by evaporation mother liquor and enter homogeneous
Tank carries out water quality buffering and adjusts, and avoids influence of the water quality larger fluctuation to process system, and the evaporation after the adjusting of homogeneous tank is dense
Contracting mother liquor be introduced into caustic soda retort be added caustic soda be stirred to react after be re-fed into soda ash retort be added soda ash support mix, react
Generate a large amount of suspended particulates and flocculent substance, enter back into inclined plate settler, be divided into the dense liquid of supernatant liquor and lower layer, dense liquid into
Enter dope tank be re-fed into filter press be press-filtered out calcium and magnesium salt slurry outward transport；Supernatant clear liquid enters flows into coarse filter mistake again in Clear liquid tank
Filter, eventually enters into filter in purpose ceramic-film filter and obtains calcium ions and magnesium ions concentration to reduce total suspended solid content in feed liquid and be less than
50mg/L, total suspended solid content are less than the clarification high temperature brine of 1mg/L.
The course of work of whole device is：
High temperature evaporation concentrated mother liquor enters homogeneous tank, plays water quality buffering adjustment effect, avoids water quality larger fluctuation to technique system
The influence of system.Feed water is pumped into caustic soda retort, and soda bath, turn on agitator is added so that feed liquid reaction is uniform.It pumps again
Enter in soda ash retort, soda ash solution is added, turn on agitator is conducive to chemical reaction and carries out.It is specific in two alkali retort
Dosage is depending on practical water quality, and pH controls are in 11 ~ 12 ranges in retort.It is generated after two alkali are added, in feed liquid a large amount of
Suspended particulate and flocculent substance, total suspended solid content increases sharply, and after inclined plate settler, is divided into supernatant liquor and lower layer
Dense liquid.Dense liquid enters dope tank, then through filter press, finally obtains calcium and magnesium salt slurry, outward transport disposition.Clear liquid enters Clear liquid tank,
Again respectively through coarse filter and purpose ceramic-film filter, total suspended solid content in feed liquid is further decreased.By removing hard pretreatment
After unit, obtained feed liquid calcium ions and magnesium ions concentration and it is less than 50mg/L, total suspended solid content is less than 1mg/L.
After the pretreated feed liquid of dosing is by adjusting acid and degasser, basicity and dissolubility fixed gas in feed liquid are removed
Body is advantageously implemented crystallization apparatus scale inhibition anticorrosion purpose.Feed liquid is after the heating of sulfate crystal heater, into sulfate crystal
Device is concentrated by evaporation, until after a certain concentration, is precipitated crystal, sodium sulfate salt is made through centrifugal dehydrator in feed liquid, and the mother liquor of abjection is through miscellaneous
After salt crystallization heater continues heating, it is concentrated by evaporation into carnallite crystallizer, continues to precipitate crystal, feed liquid is through centrifugal dehydration mechanism
Carnallite is obtained, the mother liquor of abjection is returned into carnallite crystal system.Carnallite crystallizer is in subnormal ambient by vacuum pumping action.
One effect sulfate crystal device is heated by outer for steam, the indirect steam that two effect carnallite crystallizers are generated by first effect crystallizer as plus
Heat source.The indirect steam that two effect crystallizers generate, is used as product water reuse after being condensed by demister.The final waste water, miscellaneous realized
Salt efficiently uses, and reaches near-zero release target.
Part that the present invention does not relate to is the same as those in the prior art or can be realized by using the prior art.
Claims (12)
1. a kind of brine waste, which is concentrated by evaporation mother liquor, divides salt recovery processing technique method, it is characterized in that it includes the following steps：
First, brine waste mother liquor is concentrated by evaporation to be sent into except hard pretreatment unit pre-processes, by two alkali dosings, inclined plate
Sedimentation, ceramic membrane filter and calcium and magnesium salt slurry press filtration obtain clarification high temperature brine；
Second, the clarification high temperature brine that will be obtained after removing pretreatment firmly is sent into an effect sodium sulphate crystal system, adds by crystallizing
Enter crystallizer after hot device heating to be concentrated by evaporation, then sodium sulfate salt and primary crystallization mother liquor are isolated by centrifugal dehydrator；
Primary crystallization mother liquor is sent into two effect carnallite crystal systems and is further concentrated by evaporation by third, the feed liquid after evaporation and concentration
It enters back into centrifugal dehydrator and isolates carnallite and secondary crystallization mother liquor, secondary crystallization mother liquor returns in two effect carnallite crystal systems
It is mixed with primary crystallization mother liquor and carries out circulating and evaporating concentration.
2. evaporation, crystallization heater heat exchanger tube are (such as interior wave male-pipe, bellows, inner or outer or inside and outside using efficient special type pipe
Conduit pipe), greatly reduce heat transmission equipment size.
3. according to the method described in claim 1, it is characterized in that described one imitates the crystallization heater in sodium sulphate crystal system
Heat source of the secondary steam part of generation as the crystallizing evaporator in two effect carnallite crystal systems.
4. according to the method described in claim 1, it is characterized in that the clarification high temperature brine is by adding acid for adjusting pH in 5 ~ 6 models
In enclosing, basicity ion in feed liquid is made to react generation carbon dioxide discharge with acid；Feed liquid dissolves after deaerator is handled in feed liquid
Property on-condensible gas be discharged, then again will be through adjusting acid de- to reduce the possibility that fouling and corrosion occur in equipment running process
Clarification high temperature brine after gas is sent into an effect sodium sulphate crystal system,
According to the method described in claim 1, it is characterized in that the brine waste be concentrated by evaporation mother liquor mainly by sodium chloride and
Sodium sulphate forms, and salinity accounting is more than 80%, and sodium sulphate is more than 3.5 with sodium chloride mass ratio：1；Total dissolved solid content exists
The mg/L of 80000 mg/L ~ 130000, temperature, containing a small amount of foreign ion, do not contain poisonous and harmful heavy metallic at 80 DEG C ~ 90 DEG C
Ion, CODcrContent is less than 1500mg/L.
5. according to the method described in claim 1, it is characterized in that the two alkali dosings, which refer to priority, is added caustic soda and soda ash, burning
Alkali and soda ash are configured to solution and are added by pipeline；Dosing reaction device is furnished with blender so that medicament is added and mixes rapidly
Uniformly, react abundant with feed liquid；For material liquid pH after dosing in 11 ~ 12 ranges, the sum of calcium ions and magnesium ions concentration is less than 50mg/L.
6. according to the method described in claim 5, it is characterized in that feed liquid forms suspension after two alkali dosings reaction in solution
Grain and flocculent substance, main component include calcium carbonate, magnesium hydroxide, silica；Mix suspending object settling property is good, passes through inclined plate
After settler, supernatant liquor suspension content is greatly reduced；Supernatant liquor is successively into coarse filter and ceramic membrane filter excessively
Clarification feed liquid is made after device；The highly concentrated turbid of lower layer passes through filtering equipment, obtains calcium and magnesium salt slurry, outward transport disposition.
7. according to the method described in claim 6, it is characterized in that expecting after coarse filtration equipment and the filtering of ceramic membrane filter equipment
Total suspended matter solid content in liquid further decreases, and TSS is less than 1mg/L.
8. according to the method described in claim 1, it is characterized in that an effect sulfate crystal system is using pressure outer circulation
Crystallizer（FC types）, feeding manner is axial admission, can eliminate liquid level vortex, reduces cycle feed liquid short circuit temperature loss；Evaporation
Room section evaporation intensity improves, and precipitation salt crystal size is larger, is conducive to the raising of the pure salt quality of follow-up workshop section's sodium sulphate；Evaporation production
A raw indirect steam part is by becoming product water reuse after condensation, another part is as two effect carnallite crystallizer heating warm
Source；Effectively reduce raw steam consumption.
9. according to the method described in claim 8, it is characterized in that feed liquid is concentrated by evaporation to 30% during the sulfate crystal
Left and right starts that crystal salt is precipitated, and when total suspended solid reaches 10% ~ 15%, feed liquid enters centrifugal dehydrator and isolates sodium sulfate salt,
Crystalline mother solution enters carnallite crystallizer, and after being further concentrated by evaporation, carnallite is isolated by centrifuge dewatering machine.
10. according to the method described in claim 9, it is characterized in that sodium sulfate salt and carnallite that the centrifugal dehydrator is isolated,
Sodium sulfate salt moisture content is 10% or so, and carnallite moisture content is 50% ~ 60%；Carnallite moisture content height is conducive to the highly concentrated mother of entrainment portions
Liquid goes out system, plays and periodically arranges dense purpose, realizes waste liquid near-zero release；Sodium sulphate centrifugal dehydrator uses double push-material formula or sleeping spiral shell
Formula, carnallite centrifuge use horizontal helical type.
11. a kind of brine waste, which is concentrated by evaporation mother liquor, divides salt treatment device, it is characterized in that it includes：
One removes hard pretreatment unit, which obtains for that will carry out pretreatment into evaporation and concentration mother liquor therein
High temperature brine must be clarified, while obtaining the outward transport of calcium and magnesium salt slurry；
One adjusts sour degasser；The tune acid degasser is used for will be through the pH except the pretreated clarification high temperature brine of hard pretreatment unit
Adjustment makes basicity ion in feed liquid react generation carbon dioxide discharge with acid, to reduce in equipment running process in 5 ~ 6 ranges
The possibility of fouling and corrosion occurs；
Sulfuric acid steel crystal system is imitated one by one, and the effect sulfuric acid steel crystal system is mainly de- by an effect heating crystalline device and an effect centrifugation
Water dispenser forms, and crystal salt is precipitated in the clarification high temperature brine heating concentration after adjusting sour degasser tune acid to deaerate by heating crystalline device,
And it is discharged into when suspended solid reaches 10%-15% in centrifugal dehydrator and isolates the sodium sulfate salt that moisture content is no more than 10%；Heating
Crystallizer adds a thermogenetic steam part as the heat source of two effect carnallite crystal systems, and another is made after condenser condenses
For product water reuse；
One or two effect carnallite crystal systems, the two effect carnallites crystal system is mainly by two effect heating crystalline devices and two effect centrifugal dehydrators
The feed liquid of composition, an effect centrifugal dehydrator discharge generates carnallite after pipeline is sent into two effect heating crystalline device heating, is sent into two effects
Centrifugal dehydrator dehydration obtains the carnallite that moisture content is 50-60%, and the feed liquid for deviating from carnallite enters two effect carnallites again by pipeline
Enter in two effect heating crystalline devices after being mixed with the feed liquid of an effect centrifugal dehydrator discharge in crystal system；Two effect heating crystalline devices
It is used as product water reuse after the condensed device condensation of steam of generation.
12. brine waste according to claim 11, which is concentrated by evaporation mother liquor, divides salt treatment device, it is characterized in that described removes
Hard pretreatment unit is mainly by homogeneous tank, caustic soda retort, soda ash retort, inclined plate settler, Clear liquid tank, coarse filter, pottery
Porcelain membrane filter, NaOH solution tank NaOH and filter press composition are concentrated by evaporation mother liquor and enter the progress water quality buffering adjusting of homogeneous tank, avoid water quality
Influence of the larger fluctuation to process system, the evaporation and concentration mother liquor after the adjusting of homogeneous tank, which is introduced into caustic soda retort, to be added
Caustic soda is re-fed into addition soda ash support in soda ash retort and mixes after being stirred to react, reaction generates a large amount of suspended particulates and flocculent substance,
Inclined plate settler is entered back into, is divided into the dense liquid of supernatant liquor and lower layer, dense liquid, which enters dope tank and is re-fed into filter press, to be press-filtered out
Calcium and magnesium salt slurry is transported outward；Supernatant clear liquid enters in Clear liquid tank flows into coarse filter filtering again, eventually enters into mistake in purpose ceramic-film filter
Filter obtains calcium ions and magnesium ions concentration to reduce total suspended solid content in feed liquid and is less than 50mg/L, and total suspended solid content is less than
The clarification high temperature brine of 1mg/L.
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