CN205528218U - One imitates useless water separator of limbs MVR mixed salt - Google Patents
One imitates useless water separator of limbs MVR mixed salt Download PDFInfo
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- CN205528218U CN205528218U CN201620174278.5U CN201620174278U CN205528218U CN 205528218 U CN205528218 U CN 205528218U CN 201620174278 U CN201620174278 U CN 201620174278U CN 205528218 U CN205528218 U CN 205528218U
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- crystallizing evaporator
- salt
- carnallite
- nitre
- compression machine
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- 239000011780 sodium chloride Substances 0.000 title claims abstract description 111
- 150000003839 salts Chemical class 0.000 title claims abstract description 94
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 210000003414 Extremities Anatomy 0.000 title abstract 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N Potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims abstract description 59
- 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 53
- 239000002351 wastewater Substances 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims description 43
- 238000007906 compression Methods 0.000 claims description 40
- 238000004094 preconcentration Methods 0.000 claims description 30
- 239000006200 vaporizer Substances 0.000 claims description 29
- 239000012528 membrane Substances 0.000 claims description 15
- 238000001704 evaporation Methods 0.000 claims description 14
- 239000012452 mother liquor Substances 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000011552 falling film Substances 0.000 claims description 4
- 238000000703 high-speed centrifugation Methods 0.000 claims description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 35
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 17
- 229910052938 sodium sulfate Inorganic materials 0.000 description 16
- 235000011152 sodium sulphate Nutrition 0.000 description 16
- 238000000034 method Methods 0.000 description 11
- 238000002425 crystallisation Methods 0.000 description 7
- 230000005712 crystallization Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 238000007710 freezing Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000007738 vacuum evaporation Methods 0.000 description 2
- 240000001816 Prunella vulgaris Species 0.000 description 1
- 235000015076 Shorea robusta Nutrition 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000005039 chemical industry 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
- 239000010446 mirabilite Substances 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Abstract
The utility model discloses an one imitates useless water separator of limbs MVR mixed salt, including evaporative concentration ware, salt evaporated crystallizer, nitre evaporated crystallizer, carnallite evaporated crystallizer and vapor compressor in advance, wherein evaporative concentration ware, salt evaporated crystallizer, nitre evaporated crystallizer, carnallite evaporated crystallizer's secondary vapor outlet is connected to same effect vapor compressor's import in advance, and vapor compressor's imported evaporated crystallizer 2 is 80~100 DEG C. The utility model discloses can realize the zero release of mixed salt waste water to therefrom separate, retrieve the salt and the anhydrous nitre of high -purity, investment cost and operating power consumption are low.
Description
Technical field
This utility model belongs to chemical wastewater treatment field, is specifically related to a kind of effect four body MVR mixed salt waste water separators.
Background technology
In some enterprises in the fields such as salt chemical engineering, Coal Chemical Industry, hydrometallurgy, pharmacy, the high concentration mixed salt waste water simultaneously containing sodium chloride, sodium sulfate and other salinity in a large number can be produced.For the desalting processing of this kind of waste water, generally there is following several treatment technology: one is that direct evaporation crystallization obtains mixed salt, and this technical matters is simple, but economic worth is the highest.Two is the multiple-effect vacuum evaporation technology of sal prunella coproduction, and this technology utilizes the dissolubility relation of sodium chloride and sodium sulfate, and high temperature obtains salt (sodium chloride), low temperature obtains nitre (sodium sulfate), higher degree product salt and nitre product can be obtained, but end effect steam is condensed, cause the significant wastage of the energy.Three is the MVR evaporation technology of solventing-out, and this technique is also with the dissolubility relation of sodium chloride and sodium sulfate as above-mentioned multiple-effect vacuum evaporation technology, and high temperature obtains salt, and low temperature obtains nitre, and difference is that indirect steam can be recycled after compressor compresses.But this technique at least needs high temperature and low temperature two nitre vapour compression machine, and the volume flow of Low Temperature Steam compressor is very big, either equipment investment or operation energy consumption is the biggest.Four is frozen saltpeter mention technique, i.e. uses freezing method to make sulfate crystal thus separates with sodium chloride, and this technique cryogenic temperature is low, needs the low temperature mother solution of big cycle volume, and system energy consumption is the highest.Five is embrane method concentrating and separating, utilizes NF membrane to make the sodium chloride in waste water separate with sodium sulfate, can obtain sodium sulfate and the sodium chloride of higher degree then in conjunction with the method for evaporative crystallization or freezing and crystallizing.Wherein, evaporative crystallization or freezing and crystallizing device and the method for operation thereof directly determine the effect of solventing-out and the investment of whole process system and operating cost.
Summary of the invention
The purpose of this utility model is to provide a kind of cost-effective, effect four body MVR mixed salt waste water separators of reduction energy consumption, can realize mixed salt wastewater zero discharge by this device, and therefrom separate, reclaims highly purified salt and without liquid glauber salt.
For achieving the above object, this utility model be the technical scheme is that
A kind of effect four body MVR mixed salt waste water separators, including pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine, described pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam of carnallite crystallizing evaporator export the import being connected to same effect vapour compression machine, and the inlet steam temperature of described vapour compression machine is 80 ~ 100 DEG C.
Described effect four body MVR mixed salt waste water separators, wherein, the outlet of vapour compression machine connects pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
Described effect four body MVR mixed salt waste water separators, wherein, the outlet of vapour compression machine connects pre-concentration vaporizer, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the entrance of the second vapour compression machine respectively, and the outlet of the second vapour compression machine connects the heating steam inlet of carnallite crystallizing evaporator.
Described effect four body MVR mixed salt waste water separators, wherein, the material outlet of pre-concentration vaporizer connects the material inlet of salt crystallizing evaporator, the entrance of the material outlet external salt centrifuge of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects salt crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively；The entrance of the material outlet external nitre centrifuge of nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects nitre crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively；The entrance of the material outlet external carnallite centrifuge of carnallite crystallizing evaporator, the mother liquor outlet of carnallite centrifuge connects the material inlet of carnallite crystallizing evaporator.
Described effect four body MVR mixed salt waste water separators, wherein, the product water out of the external NF membrane of material inlet of pre-concentration vaporizer；The dense water out of the external NF membrane of material inlet of nitre crystallizing evaporator；The entrance of NF membrane connects the mixed salt waste water needing to separate.
Described effect four body MVR mixed salt waste water separators, wherein, pre-concentration vaporizer 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.
Described effect four body MVR mixed salt waste water separators, 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 beneficial effects of the utility model are as follows.
1. this utility model uses same effect vapour compression machine that sodium chloride and sodium sulfate are carried out MVR evaporative crystallization, and the inlet temperature of vapour compression machine is 80 ~ 100 DEG C, with used high/low temperature two to imitate or multiple-effect steam compressor carries out MVR evaporative crystallization in the past compared with, greatly reduce the flow to compressor and performance requirement, thus reached to reduce cost and the purpose of operation energy consumption.
2. it is about 2 times of forced-circulation evaporation crystallizer due to the coefficient of heat transfer of falling film evaporator, this utility model produces before water enters salt crystallizing evaporator in NF membrane and first uses pre-concentration vaporizer pre-concentration, and total heat exchange area and the operation energy consumption of system can be greatly lowered.
3., for other salinity in addition to sodium chloride, sodium sulfate contained in mixed salt waste water and high boiling component, this utility model uses carnallite crystallizing evaporator to process.By carnallite crystallizing evaporator, on the one hand can improve sodium chloride and the purity of two kinds of products of anhydrous sodium sulfate, on the other hand can realize wastewater zero discharge, whole device, in addition to solid salt, only can produce with the condensed water of reuse, without other sewage discharge.
4, salt crystallizing evaporator of the present utility model, nitre crystallizing evaporator, carnallite crystallizing evaporator are provided with elutriating cylinder, can produce high-quality Nacl and industrial anhydrous sodium sulfate by elutriating cylinder elutriation, carnallite evaporative crystallization, centrifuge washing.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of this utility model first embodiment；
Fig. 2 is the schematic diagram of this utility model the second embodiment.
Detailed description of the invention
With embodiment, this utility model is described in further detail below in conjunction with the accompanying drawings.
As depicted in figs. 1 and 2, a kind of effect four body MVR mixed salt waste water separators, including pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine.Wherein, pre-concentration vaporizer, 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 vaporizer 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, the crystal separator including heat exchanger, being provided with elutriating cylinder and forced circulation pump.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 that indirect steam outlet is forced-circulation evaporation crystallizer of crystal separator, 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 importing and exporting the temperature difference is 10 ~ 18 DEG C.
The connection of one effect four body MVR mixed salt waste water separator material pipes is as follows:
The product water out of the external NF membrane of material inlet of pre-concentration vaporizer, the material outlet of pre-concentration vaporizer connects the material inlet of salt crystallizing evaporator, the entrance of the material outlet external salt centrifuge of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects material inlet and the material inlet of carnallite crystallizing evaporator of salt crystallizing evaporator respectively.
The dense water out of the external NF membrane of material inlet of nitre crystallizing evaporator, the entrance of the material outlet external nitre centrifuge of nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects material inlet and the material inlet of carnallite crystallizing evaporator of nitre crystallizing evaporator respectively.
Material inlet external salt centrifuge, nitre centrifuge and the mother liquor outlet of carnallite centrifuge of carnallite crystallizing evaporator, the entrance of the material outlet external carnallite centrifuge of carnallite crystallizing evaporator.
The connection son with the following Examples of one effect four body MVR mixed salt waste water separator jet chimneys illustrates.
Embodiment 1:
As shown in Figure 1, pre-concentration vaporizer, 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 vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
Embodiment 2:
As shown in Figure 2, pre-concentration vaporizer, 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 pre-concentration vaporizer, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the entrance of the second vapour compression machine respectively, and the outlet of the second vapour compression machine connects the heating steam inlet of carnallite crystallizing evaporator.
Using above-mentioned effect four body MVR mixed salt waste water separators, detailed description of the invention is as follows.
1. mixed salt waste water passes through NF membrane, obtain rich in the product water of sodium chloride and the dense water rich in sodium sulfate, wherein, NF membrane produces the mass concentration of the sodium chloride in water with the ratio of the mass concentration of sodium sulfate more than 5.5, and the mass concentration of the sodium chloride in the dense water of NF membrane is less than 5.5 with the ratio of the mass concentration of sodium sulfate.
2. NF membrane is produced water and is entered the pre-concentration vaporizer of effect four body MVR mixed salt waste water separators after heat exchange, first it is evaporated concentrating by pre-concentration vaporizer, evaporating temperature is 80 ~ 100 DEG C, when the sodium chloride in pre-concentration vaporizer is close to time saturated, deliver to the salt further condensing crystallizing of crystallizing evaporator that evaporating temperature is 80 ~ 100 DEG C.When in salt crystallizing evaporator, sodium sulfate is close to time saturated, and magma discharging is delivered to salt centrifuge and carried out solid-liquid separation, can obtain product salt after scrubbed dried.Magma first can also improve granularity and the solid content of magma of crystal through salt thickener before delivering to salt centrifuge.A centrifuge mother liquor part for salt centrifuge is back to salt crystallizing evaporator, and another part then pump to carnallite crystallizing evaporator processes.
3. the dense water of NF membrane enter after heat exchange one effect four body MVR mixed salt waste water separators nitre crystallizing evaporator carry 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 time saturated, and magma discharging is delivered to nitre centrifuge and carried out solid-liquid separation, can obtain nitre product after scrubbed dried.Magma first can also improve granularity and the solid content of magma of crystal through nitre thickener before delivering to nitre centrifuge.A centrifuge mother liquor part for nitre centrifuge is back to nitre crystallizing evaporator, and another part then pump to carnallite crystallizing evaporator processes.
4. owing to mixed salt waste water would generally contain other high boiling component such as salinity and Organic substance in addition to sodium chloride, sodium sulfate; if the constantly circulation accumulation in salt evaporative crystallization and nitre evaporation and crystal process of these salinities and Organic substance; on the one hand product salt and the purity of nitre product will be affected; on the other hand the boiling point temperature rise of material can be caused seriously to raise, affect the precipitation of sodium chloride and sodium sulfate.In order to avoid above-mentioned situation, prior art is it is generally required to periodically discharge part centrifugal mother solution, it is impossible to realize wastewater zero discharge.This utility model uses carnallite crystallizing evaporator to process salt centrifuge mother liquor and nitre centrifuge mother liquor, obtains carnallite, without other sewage discharge after being evaporated process.
5. the indirect steam of 80 ~ 100 DEG C of pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator and the generation of carnallite crystallizing evaporator enters same vapour compression machine jointly, and after vapour compression machine compression temperature improves 10 ~ 18 DEG C, shunting returns to pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator and carnallite crystallizing evaporator as adding vapours recycling.When mixed salt waste water causes the boiling point temperature rise of material seriously to raise containing high boiling point carnallite and component, above-mentioned shunting returns to the vapours that adds of carnallite crystallizing evaporator and also needs to enter the second vapour compression machine before entering carnallite crystallizing evaporator, delivers to carnallite crystallizing evaporator again after the second vapour compression machine compresses, improves 10 ~ 18 DEG C again.
Claims (7)
1. effect four body MVR mixed salt waste water separators, it is characterized in that: include pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator and vapour compression machine, described pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, the indirect steam of carnallite crystallizing evaporator export the import being connected to same effect vapour compression machine, and the inlet steam temperature of described vapour compression machine is 80 ~ 100 DEG C.
Effect four body MVR mixed salt waste water separators the most as claimed in claim 1, it is characterised in that: the outlet of described vapour compression machine connects pre-concentration vaporizer, salt crystallizing evaporator, nitre crystallizing evaporator, the heating steam inlet of carnallite crystallizing evaporator respectively.
Effect four body MVR mixed salt waste water separators the most as claimed in claim 1, it is characterized in that: the outlet of described vapour compression machine connects pre-concentration vaporizer, salt crystallizing evaporator, the heating steam inlet of nitre crystallizing evaporator and the import of the second vapour compression machine respectively, the outlet of the second vapour compression machine connects the heating steam inlet of carnallite crystallizing evaporator.
4. the effect four body MVR mixed salt waste water separators as described in claim 1 or 2 or 3, it is characterized in that: the material outlet of described pre-concentration vaporizer connects the material inlet of salt crystallizing evaporator, the entrance of the material outlet external salt centrifuge of salt crystallizing evaporator, the mother liquor outlet of salt centrifuge connects salt crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively；The entrance of the material outlet external nitre centrifuge of described nitre crystallizing evaporator, the mother liquor outlet of nitre centrifuge connects nitre crystallizing evaporator and the material inlet of carnallite crystallizing evaporator respectively；The entrance of the material outlet external carnallite centrifuge of described carnallite crystallizing evaporator, the mother liquor outlet of carnallite centrifuge connects the material inlet of carnallite crystallizing evaporator.
5. the effect four body MVR mixed salt waste water separators as described in claim 1 or 2 or 3, it is characterised in that: the product water out of the external NF membrane of material inlet of described pre-concentration vaporizer；The dense water out of the external NF membrane of material inlet of described nitre crystallizing evaporator；The entrance of NF membrane connects the mixed salt waste water needing to separate.
6. the effect four body MVR mixed salt waste water separators as described in claim 1 or 2 or 3, it is characterised in that: described pre-concentration vaporizer is falling film evaporator；Described salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are forced-circulation evaporation crystallizer；Described salt crystallizing evaporator, nitre crystallizing evaporator, carnallite crystallizing evaporator are provided with elutriating cylinder.
7. the effect four body MVR mixed salt waste water separators as described in claim 1 or 2 or 3, it is characterised in that: described vapour compression machine, the second vapour compression machine are lobed rotor compressor, centrifugal blower or high speed centrifugation compressor；Described vapour compression machine, the import and export temperature difference of the second vapour compression machine are 10 ~ 18 DEG C.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620174278.5U CN205528218U (en) | 2016-03-08 | 2016-03-08 | One imitates useless water separator of limbs MVR mixed salt |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620174278.5U CN205528218U (en) | 2016-03-08 | 2016-03-08 | One imitates useless water separator of limbs MVR mixed salt |
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| CN205528218U true CN205528218U (en) | 2016-08-31 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107162297A (en) * | 2016-03-08 | 2017-09-15 | 广州市心德实业有限公司 | One kind one imitates four body MVR mixed salts waste water separators and separation method |
| WO2018126651A1 (en) * | 2017-01-05 | 2018-07-12 | 广州市心德实业有限公司 | Evaporation, crystallization and drying integrated device and evaporation crystallization drying method |
-
2016
- 2016-03-08 CN CN201620174278.5U patent/CN205528218U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107162297A (en) * | 2016-03-08 | 2017-09-15 | 广州市心德实业有限公司 | One kind one imitates four body MVR mixed salts waste water separators and separation method |
| WO2018126651A1 (en) * | 2017-01-05 | 2018-07-12 | 广州市心德实业有限公司 | Evaporation, crystallization and drying integrated device and evaporation crystallization drying method |
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