CN107162297A - One kind one imitates four body MVR mixed salts waste water separators and separation method - Google Patents
One kind one imitates four body MVR mixed salts waste water separators and separation method Download PDFInfo
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- CN107162297A CN107162297A CN201610129263.1A CN201610129263A CN107162297A CN 107162297 A CN107162297 A CN 107162297A CN 201610129263 A CN201610129263 A CN 201610129263A CN 107162297 A CN107162297 A CN 107162297A
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- evaporator
- crystallizing evaporator
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- crystallizing
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- 150000003839 salts Chemical class 0.000 title claims abstract description 109
- 239000002351 wastewater Substances 0.000 title claims abstract description 43
- 238000000926 separation method Methods 0.000 title claims abstract description 14
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims abstract description 70
- 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 61
- 230000006835 compression Effects 0.000 claims abstract description 49
- 238000007906 compression Methods 0.000 claims abstract description 49
- 238000004094 preconcentration Methods 0.000 claims abstract description 36
- 230000008676 import Effects 0.000 claims abstract description 10
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 43
- 239000000463 material Substances 0.000 claims description 43
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 38
- 230000000694 effects Effects 0.000 claims description 30
- 239000012528 membrane Substances 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000011780 sodium chloride Substances 0.000 claims description 21
- 239000012452 mother liquor Substances 0.000 claims description 19
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 18
- 235000011152 sodium sulphate Nutrition 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 15
- 238000001704 evaporation Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 239000011552 falling film Substances 0.000 claims description 4
- 238000000703 high-speed centrifugation Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000013078 crystal Substances 0.000 description 9
- 238000002425 crystallisation Methods 0.000 description 7
- 230000008025 crystallization Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 230000008014 freezing Effects 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000007738 vacuum evaporation Methods 0.000 description 2
- 241001529739 Prunella <angiosperm> Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Four body MVR mixed salt waste water separators are imitated the invention discloses one kind one, including pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine, wherein pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected to the same import for imitating vapour compression machine, and the inlet steam temperature of vapour compression machine is 80 ~ 100 DEG C.The invention also discloses the mixed salt waste water separation method using said apparatus.The achievable mixed salt wastewater zero discharge of the present invention, and the salt and anhydrous nitre of high-purity are therefrom separated, reclaim, cost of investment and operation energy consumption are low.
Description
Technical field
The invention belongs to chemical wastewater treatment field, and in particular to one kind one imitates four body MVR mixed salts waste water separators and separation method.
Background technology
Some enterprises in fields such as salt chemical engineering, coal chemical industry, hydrometallurgy, pharmacy, can produce a large amount of high concentration mixed salt waste water containing sodium chloride, sodium sulphate and other salinities simultaneously.For the desalting processing of this kind of waste water, generally there are following several treatment technologies：One is that direct evaporative crystallization obtains mixed salt, and this technical matters is simple, but economic value is not high.Two be the multiple-effect vacuum evaporation technology of sal prunella coproduction, and this technology utilizes the solubility relation of sodium chloride and sodium sulphate, and high temperature obtains salt（Sodium chloride）, low temperature obtains nitre（Sodium sulphate）, higher degree product salt and nitre product can be obtained, but end effect steam is condensed, and causes the significant wastage of the energy.Three be the MVR evaporation technologies of solventing-out, this technique as above-mentioned multiple-effect vacuum evaporation technology also with sodium chloride and sodium sulphate solubility relation, high temperature obtains salt, and low temperature obtains nitre, and difference is that indirect steam can be recycled after being compressed through compressor.But this technique at least needs high temperature and the nitre vapour compression machine of low temperature two, and the volume flow of Low Temperature Steam compressor is very big, and either equipment investment or operation energy consumption are all very big.Four be frozen saltpeter mention technique, i.e., make sulfate crystal to separate with sodium chloride using freezing, this technique cryogenic temperature is low, it is necessary to which the low temperature mother liquor of big cycle volume, system energy consumption is very high.Five be embrane method concentrating and separating, separates sodium chloride and sodium sulphate in waste water using NF membrane, the method then in conjunction with evaporative crystallization or freezing and crystallizing can obtain the sodium sulphate and sodium chloride of higher degree.Wherein, evaporative crystallization or freezing and crystallizing device and its method for operation directly determine the effect of solventing-out and investment and the operating cost of whole process system.
The content of the invention
It is an object of the invention to provide a kind of cost-effective, reduction energy consumption a four body MVR mixed salts waste water separators of effect and separation method, mixed salt wastewater zero discharge can be realized by the apparatus and method, and therefrom separate, reclaim the salt and anhydrous nitre of high-purity.
To achieve the above object, the technical solution adopted in the present invention is：
One kind one imitates four body MVR mixed salt waste water separators, including pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine, the pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected to the same import for imitating vapour compression machine, and the inlet steam temperature of the vapour compression machine is 80 ~ 100 DEG C.
A described four body MVR mixed salt waste water separators of effect, wherein, the outlet of vapour compression machine connects pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
A described four body MVR mixed salt waste water separators of effect, wherein, the outlet of vapour compression machine connects the entrance of pre-concentration evaporator, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the second vapour compression machine, the heating steam inlet of the outlet connection carnallite crystallizing evaporator of the second vapour compression machine respectively.
A described four body MVR mixed salt waste water separators of effect, wherein, the material outlet of pre-concentration evaporator connects the material inlet of salt crystallizing evaporator, the entrance of the external salt centrifuge of material outlet of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects the material inlet of salt crystallizing evaporator and carnallite crystallizing evaporator respectively；The entrance of the external nitre centrifuge of material outlet of nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects the material inlet of nitre crystallizing evaporator and carnallite crystallizing evaporator respectively；The entrance of the external carnallite centrifuge of material outlet of carnallite crystallizing evaporator, the mother liquor outlet of carnallite centrifuge connects the material inlet of carnallite crystallizing evaporator.
A described four body MVR mixed salt waste water separators of effect, wherein, the production water out of the external NF membrane of material inlet of pre-concentration evaporator；The concentrated water outlet of the external NF membrane of material inlet of nitre crystallizing evaporator；The entrance connection of NF membrane needs the mixed salt waste water separated.
A described four body MVR mixed salt waste water separators of effect, wherein, pre-concentration evaporator is falling film evaporator；Salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are forced-circulation evaporation crystallizer；Salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are provided with elutriating cylinder.
A described four body MVR mixed salt waste water separators of effect, wherein, vapour compression machine, the second vapour compression machine are lobed rotor compressor, centrifugal blower or high speed centrifugation compressor；Vapour compression machine, the import and export temperature difference of the second vapour compression machine are 10 ~ 18 DEG C.
The invention also discloses a kind of four body MVR mixed salt waste water separation methods of effect using above-mentioned separator, its technical scheme used is：
One kind one imitates four body MVR mixed salt waste water separation methods, pass through MVR techniques, NF membrane production water is first by pre-concentration evaporator, salt crystallizing evaporator condensing crystallizing, isolated product salt is washed by salt centrifuge afterwards, NF membrane concentrated water is first by nitre crystallizing evaporator condensing crystallizing, isolated nitre product is washed by nitre centrifuge afterwards, salt centrifuge mother liquor and nitre centrifuge mother liquor first by carnallite crystallizing evaporator condensing crystallizing, after by the isolated carnallite of carnallite centrifuge；The indirect steam circulated in pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator enters same effect vapour compression machine, and reuse is shunted after same effect vapour compression machine compression heating.
A described four body MVR mixed salt waste water separation methods of effect, wherein, the ratio between the mass concentration of the sodium chloride in NF membrane production water and the mass concentration of sodium sulphate are more than 5.5；The ratio between the mass concentration of sodium chloride in NF membrane concentrated water and the mass concentration of sodium sulphate are less than 5.5.
Beneficial effects of the present invention are as follows.
1. the present invention carries out MVR evaporative crystallizations using same effect vapour compression machine to sodium chloride and sodium sulphate, and the inlet temperature of vapour compression machine is 80 ~ 100 DEG C, compared with imitated using high/low temperature two or multiple-effect steam compressor carries out MVR evaporative crystallizations in the past, the flow and performance requirement to compressor are greatly reduced, so that having reached reduces the purpose of cost and operation energy consumption.
2. because the coefficient of heat transfer of falling film evaporator is about 2 times of forced-circulation evaporation crystallizer, the present invention first uses pre-concentration evaporator pre-concentration before NF membrane production water enters salt crystallizing evaporator, and the total heat exchange area and operation energy consumption of system can be greatly lowered.
3. for containing other salinities and high boiling component in addition to sodium chloride, sodium sulphate in mixed salt waste water, the present invention is handled using carnallite crystallizing evaporator.By carnallite crystallizing evaporator, the purity of two kinds of products of sodium chloride and anhydrous sodium sulfate on the one hand can be improved, wastewater zero discharge on the other hand can be realized, whole device can only be produced, without other sewage discharges in addition to solid salt with the condensed water of reuse.
4th, salt crystallizing evaporator of the invention, nitre crystallizing evaporator, carnallite crystallizing evaporator are provided with elutriating cylinder, and high-quality Nacl and industrial anhydrous sodium sulfate can be produced by elutriating cylinder elutriation, carnallite evaporative crystallization, centrifuge washing.
Brief description of the drawings
Fig. 1 is the schematic diagram of first embodiment of the invention；
Fig. 2 is the schematic diagram of second embodiment of the invention.
Embodiment
The present invention is described in further detail with reference to the accompanying drawings and examples.
As depicted in figs. 1 and 2, one kind one imitates four body MVR mixed salt waste water separators, including pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine.Wherein, pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected with the import of same effect vapour compression machine.
Pre-concentration evaporator is falling film evaporator, including evaporator body, the gas-liquid separation chamber that is connected with evaporator body.
Salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are forced-circulation evaporation crystallizer, including heat exchanger, crystal separator and forced circulation pump provided with elutriating cylinder.Wherein, the heating steam inlet of heat exchanger is the heating steam inlet of forced-circulation evaporation crystallizer, and the material inlet of heat exchanger is the material inlet of forced-circulation evaporation crystallizer, and the material outlet of heat exchanger is connected with the material inlet of crystal separator.The indirect steam outlet of crystal separator exports for the indirect steam of forced-circulation evaporation crystallizer, and the material outlet of crystal separator is the material outlet of forced-circulation evaporation crystallizer.The entrance and exit of forced circulation pump is connected with the material outlet of crystal separator and the material inlet of heat exchanger respectively.
Vapour compression machine is lobed rotor compressor, centrifugal blower or high speed centrifugation compressor, and the inlet steam temperature of vapour compression machine is 80 ~ 100 DEG C, and it is 10 ~ 18 DEG C to import and export the temperature difference.
The connection of one four body MVR mixed salt waste water separator material pipes of effect is as follows：
The production water out of the external NF membrane of material inlet of pre-concentration evaporator, the material outlet of pre-concentration evaporator connects the material inlet of salt crystallizing evaporator, the entrance of the external salt centrifuge of material outlet of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects the material inlet of salt crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively.
The concentrated water outlet of the external NF membrane of material inlet of nitre crystallizing evaporator, the entrance of the external nitre centrifuge of material outlet of nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects the material inlet of nitre crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively.
The mother liquor outlet of the external salt centrifuge of material inlet of carnallite crystallizing evaporator, nitre centrifuge and carnallite centrifuge, the entrance of the external carnallite centrifuge of material outlet of carnallite crystallizing evaporator.
Son is illustrated with the following Examples for the connection of one four body MVR mixed salt waste water separator jet chimneys of effect.
Embodiment 1：
As shown in Figure 1, pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected with the import of same effect vapour compression machine, and the outlet of vapour compression machine connects pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
Embodiment 2：
As shown in Figure 2, pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected with the import of same effect vapour compression machine, the outlet of vapour compression machine connects the entrance of pre-concentration evaporator, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the second vapour compression machine, the heating steam inlet of the outlet connection carnallite crystallizing evaporator of the second vapour compression machine respectively.
Four body MVR mixed salt waste water separation methods are imitated using the one of above-mentioned separator, embodiment is as follows.
1. mixed salt waste water passes through NF membrane, obtain the production water rich in sodium chloride and the concentrated water rich in sodium sulphate, wherein, the ratio between the mass concentration of sodium chloride in NF membrane production water and the mass concentration of sodium sulphate are more than the ratio between the mass concentration of the sodium chloride in 5.5, NF membrane concentrated water and the mass concentration of sodium sulphate and are less than 5.5.
2. NF membrane produces the pre-concentration evaporator that water enters a four body MVR mixed salt waste water separators of effect after heat exchange, concentration is first evaporated by pre-concentration evaporator, evaporating temperature is 80 ~ 100 DEG C, when the sodium chloride in pre-concentration evaporator is close to saturation, the further condensing crystallizing of salt crystallizing evaporator that evaporating temperature is 80 ~ 100 DEG C is delivered to.When sodium sulphate is close to saturation in salt crystallizing evaporator, magma discharging delivers to salt centrifuge and carries out separation of solid and liquid, and product salt can be obtained after scrubbed drying process.Magma delivers to before salt centrifuge the solid content of the granularity that crystal can also be first improved through salt thickener and magma.A centrifuge mother liquor part for salt centrifuge is back to salt crystallizing evaporator, and then pump to carnallite crystallizing evaporator is handled another part.
3. the nitre crystallizing evaporator that NF membrane concentrated water enters a four body MVR mixed salt waste water separators of effect after heat exchange carries out condensing crystallizing, the evaporating temperature of nitre crystallizing evaporator is 80 ~ 100 DEG C.When the sodium chloride in nitre crystallizing evaporator is close to saturation, magma discharging delivers to nitre centrifuge and carries out separation of solid and liquid, and nitre product can be obtained after scrubbed drying process.Magma delivers to before nitre centrifuge the solid content of the granularity that crystal can also be first improved through nitre thickener and magma.A centrifuge mother liquor part for nitre centrifuge is back to nitre crystallizing evaporator, and then pump to carnallite crystallizing evaporator is handled another part.
4. due to the high boiling components such as the other salinities and organic matter in addition to sodium chloride, sodium sulphate would generally be contained in mixed salt waste water; if these salinities and organic matter constantly circulate accumulation in salt evaporative crystallization and nitre evaporation and crystal process; by the purity of one side influence product salt and nitre product; on the other hand the boiling point temperature rise of material can be caused seriously to raise, the precipitation of influence sodium chloride and sodium sulphate.In order to avoid above-mentioned situation, prior art generally requires regular discharge part centrifuge mother liquor, it is impossible to realize wastewater zero discharge.The present invention obtains carnallite, without other sewage discharges using carnallite crystallizing evaporator processing salt centrifuge mother liquor and nitre centrifuge mother liquor after being evaporated processing.
5. 80 ~ 100 DEG C of the indirect steam that pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator and carnallite crystallizing evaporator are produced enters same vapour compression machine jointly, shunting returns to pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator and carnallite crystallizing evaporator and used as heating steam circulation after improving 10 ~ 18 DEG C through vapour compression machine compression temperature.When causing the boiling point temperature rise of material seriously to raise containing higher boiling carnallite and component in mixed salt waste water, the heating steam that above-mentioned shunting returns to carnallite crystallizing evaporator is also needed to enter the second vapour compression machine before carnallite crystallizing evaporator is entered, and carnallite crystallizing evaporator is delivered to again after compressing through the second vapour compression machine, improve 10 ~ 18 DEG C again.
Claims (9)
1. one kind one imitates four body MVR mixed salt waste water separators, it is characterised in that：Including pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine, the pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam outlet of carnallite crystallizing evaporator are connected to the same import for imitating vapour compression machine, and the inlet steam temperature of the vapour compression machine is 80 ~ 100 DEG C.
2. four body MVR mixed salt waste water separators of an effect as claimed in claim 1, it is characterised in that：The outlet of the vapour compression machine connects pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
3. four body MVR mixed salt waste water separators of an effect as claimed in claim 1, it is characterised in that：The outlet of the vapour compression machine connects the import of pre-concentration evaporator, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the second vapour compression machine, the heating steam inlet of the outlet connection carnallite crystallizing evaporator of the second vapour compression machine respectively.
4. the four body MVR mixed salt waste water separators of effect as described in claim 1 or 2 or 3, it is characterised in that：The material outlet of the pre-concentration evaporator connects the material inlet of salt crystallizing evaporator, the entrance of the external salt centrifuge of material outlet of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects the material inlet of salt crystallizing evaporator and carnallite crystallizing evaporator respectively；The entrance of the external nitre centrifuge of material outlet of the nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects the material inlet of nitre crystallizing evaporator and carnallite crystallizing evaporator respectively；The entrance of the external carnallite centrifuge of material outlet of the carnallite crystallizing evaporator, the mother liquor outlet of carnallite centrifuge connects the material inlet of carnallite crystallizing evaporator.
5. a four body MVR mixed salt waste water separators of effect as claimed in claim 1 or 2 or 3 or 4, it is characterised in that：The production water out of the external NF membrane of material inlet of the pre-concentration evaporator；The concentrated water outlet of the external NF membrane of material inlet of the nitre crystallizing evaporator；The entrance connection of NF membrane needs the mixed salt waste water separated.
6. the four body MVR mixed salt waste water separators of effect as described in claim 1 or 2 or 3, it is characterised in that：The pre-concentration evaporator is falling film evaporator；The salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are forced-circulation evaporation crystallizer；The salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are provided with elutriating cylinder.
7. the four body MVR mixed salt waste water separators of effect as described in claim 1 or 2 or 3, it is characterised in that：The vapour compression machine, the second vapour compression machine are lobed rotor compressor, centrifugal blower or high speed centrifugation compressor；The vapour compression machine, the import and export temperature difference of the second vapour compression machine are 10 ~ 18 DEG C.
8. a kind of separation method of the four body MVR mixed salt waste water separators of effect in usage right requirement 1 to 7 described in any claim, it is characterised in that：Pass through MVR techniques, NF membrane production water is first by pre-concentration evaporator, salt crystallizing evaporator condensing crystallizing, isolated product salt is washed by salt centrifuge afterwards, NF membrane concentrated water is first by nitre crystallizing evaporator condensing crystallizing, isolated nitre product is washed by nitre centrifuge afterwards, salt centrifuge mother liquor and nitre centrifuge mother liquor first by carnallite crystallizing evaporator condensing crystallizing, after by the isolated carnallite of carnallite centrifuge；The indirect steam circulated in pre-concentration evaporator, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator enters same effect vapour compression machine, and reuse is shunted after same effect vapour compression machine compression heating.
9. separation method as claimed in claim 8, it is characterised in that：The ratio between the mass concentration of sodium chloride in the NF membrane production water and the mass concentration of sodium sulphate are more than 5.5；The ratio between the mass concentration of sodium chloride in the NF membrane concentrated water and the mass concentration of sodium sulphate are less than 5.5.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107522339A (en) * | 2017-10-11 | 2017-12-29 | 新乡市锦源化工有限公司 | The processing method of caused condensation waste water in a kind of contraposition ester production process |
| CN110436548A (en) * | 2019-09-05 | 2019-11-12 | 广州市心德实业有限公司 | A complete set of high-salt wastewater evaporative zero-discharge treatment equipment |
| CN111661886A (en) * | 2019-03-07 | 2020-09-15 | 广州市迈源科技有限公司 | MVR evaporation salt separation system |
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| CN102743890A (en) * | 2012-08-03 | 2012-10-24 | 赵建安 | Improved heating power vapor recompression process and special heating power vapor recompression system for same |
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