CN104230084A - Device for recovering sodium chloride and glycerinum from high-salinity and high-depth organic wastewater containing glycerinum - Google Patents
Device for recovering sodium chloride and glycerinum from high-salinity and high-depth organic wastewater containing glycerinum Download PDFInfo
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- CN104230084A CN104230084A CN201410414140.3A CN201410414140A CN104230084A CN 104230084 A CN104230084 A CN 104230084A CN 201410414140 A CN201410414140 A CN 201410414140A CN 104230084 A CN104230084 A CN 104230084A
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Abstract
The invention discloses a device for recovering sodium chloride and glycerinum from a high-salinity and high-depth organic wastewater containing glycerinum. The device comprises a complexing reaction tank, a multi-stage nanofiltration system, an evaporator, a crystallizer, a decomplexing reaction tank, a centrifuge device, a nanofiltration system, a reverse osmosis device, a distillation tower, a rectifying tower and a glycerinum storage tank. Based on components, properties and existing processing scheme of the high-salinity and high-depth organic wastewater containing glycerinum, the device relates to the processing procedures such as complexing, nanofiltration, decomplexing, centrifuging, reverse osmosis concentration, evaporation concentration, crystallization and distillation. The salinity of the wastewater which is processed by the treatment device is reduced, and a biochemical treatment process is adopted after the wastewater is diluted, so that the effluent quality reaches the standard, meanwhile, sodium chloride and glycerinum are effectively recovered, and the purity of the finished glycerinum product reaches 95%.
Description
Technical field
The present invention relates to the field for the treatment of of water pollution of environmental engineering, particularly relate to the combined treatment devices such as complexing, nanofiltration, decomplexing, centrifugal, absorption, evaporation concentration, crystallization, fractionation and reclaim high salt containing sodium-chlor and glycerine in glycerine high depth organic waste water.
Background technology
Along with industrial expansion, the quantity discharged of organic waste water is increasing, processes organic waste water, make its qualified discharge or recycling utilization significant.In the industrial production such as soapmaking industry, epoxy chloropropane production, production of biodiesel, glycerol production, can produce the organic waste water of a large amount of high salt also containing finite concentration glycerine, its sodium chloride concentration is about 5 ~ 30%, glycerol content about 2 ~ 20%, COD
crbe about 20000 ~ 350000mg/L.The characteristic of high salt makes it be difficult to adopt bioprocess technology to process, and is also difficult to adopt membrane sepn, electrodialysis separation is separated with capacitive adsorption, and may causes heavy corrosion to treatment facility.At present, high salt containing Glycerol Wastewater treated side degree of facing danger or disaster greatly, high in cost of production problem.
Glycerine as important industrial chemicals, in the equal tool of industry utility values widely such as organic chemical industry, Polymer Synthesizing, household chemicals, textiles, coating, leather, tobacco, food and medicines.For many years, China is always at a large amount of import glycerine, and glycerol market remains very fast development.In addition, sodium-chlor, as the important raw materials for production of the industry such as chlor-alkali, also has very high using value.Therefore, how effectively processing containing Glycerol Wastewater high salt, make it reach emission standard to alleviate the pollution to environment, the recycling simultaneously realizing glycerine and sodium chloride has great value.
Chinese invention CN85105641 discloses a kind of method reclaiming glycerine from salt solution.This treatment process comprises evaporation removing moisture, and at least precipitates the salinity of about 85%; Liquid product is separated from deposited salt; Dilution liquid product makes its viscosity lower than 10 centipoises; Electrodialysis obtains dilution water flow further; Fractionation is to reclaim glycerine.This technique can realize sodium-chlor in waste water and sweet oil recovery, but facility investment is large, and complex manufacturing, cost is high, operation energy consumption is large, and equipment corrosion is serious.
It take glycerine as treatment process and the device of the waste water of raw material production epoxy chloropropane that Chinese invention CN101531442 discloses a kind of.This treatment process, according to the difference of sodium-chlor, water and glycerol molecule diameter, adopts the sorbing material similar to glycerol molecule diameter to adsorb glycerine.The advantage of this treatment process is: using the change salt solution of the sodium chloride-containing waste water after process as chlorine industry, thus realizes recycling, and the rinse water containing lower concentration glycerine can safety dumping after Biochemical method.But this technique the unrealized recycling to byproduct glycerine, cause waste.
It take glycerine as treatment process and the device of the brine waste of raw material production epoxy chloropropane that Chinese invention CN102153230A discloses a kind of.Brine waste and other are polluted lower waste water and mix by this treatment process, make saltiness lower than 5%, add nitrogen, phosphorus nutrition thing; Waste water is introduced moving-bed membrane bioreactor, utilize active sludge to further process; Waste water is introduced ozone reaction unit and carry out ozone Oxidation Treatment; Discharge.The advantage of this treatment process is: treating processes is simple, stable and cost is low, and effluent quality can be ensured.But this technique must utilize the lower waste water of saltiness to be in harmonious proportion, waste is caused to the byproduct such as sodium-chlor and glycerine a large amount of in waste water.
Chinese invention CN103073086A discloses a kind of glycerinated method in borated resin absorption waste water.The principle that this treatment process can react with glycerine based on boric acid is set up.By boric acid process large pore anion resin, form borate type ion exchange resin; Resin is inserted in glycerinated wastewater treatment equipment and adsorbs; When glycerol content reaches set amount in the water outlet of pending device, take out resin and by acid-alkali treatment wash-out boric acid glycerin complex compound, then borate type ion exchange resin recycled.This technique is 30 ~ 50% to the clearance of glycerine in waste water, can realize the recycling to glycerine, but along with the rising of sodium chloride concentration, the adsorptive capacity of resin declines, and this method is inapplicable containing Glycerol Wastewater to high salt.
Above method all provides sweet oil treatment process in brine waste, but not yet has a kind of method to provide the efficient recovery method of high salt containing salinity in Glycerol Wastewater and glycerine.For a long time, China's contour salt of most epoxy resin production waste-waters is in discharge beyond standards state all the time containing Glycerol Wastewater, and high density sodium-chlor wherein and glycerine are not all recycled utilization, not only contaminate environment, and cause significant wastage to resource.
Summary of the invention
The object of the invention is to for the deficiency of existing high salt containing glycerine high depth Technologies for Organic Wastewater Treatment, and high salt is containing the vacancy reclaiming sodium-chlor and glycerine technology in Glycerol Wastewater simultaneously, high salt is provided to contain the efficient recovery device of sodium-chlor and glycerine in glycerine high depth organic waste water.
The present invention adopts following technical scheme:
High salt of the present invention is provided with complex reaction tank, multistage nanofiltration system, vaporizer, crystallizer, decomplexing retort, centrifugal device, nanofiltration system, reverse osmosis unit, distillation tower, rectifying tower, glycerine storage tank containing the retrieving arrangement of sodium-chlor in glycerine high depth organic waste water and glycerine.
The water-in of described complex reaction tank connects with the water outlet of high salt containing glycerine high depth organic waste water, another import of complex reaction tank connects with the solid outlet of centrifugal device, the water outlet of complex reaction tank connects with the water-in of multistage nanofiltration system, the nanofiltration dialyzate water outlet of multistage nanofiltration system connects with vaporizer water-in, the nanofiltration concentrated solution water outlet of multistage nanofiltration system connects with the water-in of decomplexing retort, vaporizer water outlet connects with crystallizer water-in, the water outlet of decomplexing retort connects with the water-in of centrifugal device, the liquid exit of centrifugal device connects with nanofiltration system water-in, the water outlet of nanofiltration system connects with the water-in of reverse osmosis unit, the water outlet of reverse osmosis unit connects with the water-in of distillation tower, the water outlet of distillation tower connects with the water-in of rectifying tower, the water outlet of rectifying tower connects with glycerine storage tank.
For ensureing that multistage nanofiltration system is not contaminated, before multistage nanofiltration system, a micro-filtration or ultra-filtration equipment can also be increased.
Described multistage nanofiltration system adopt to magnesium sulfate rejection rate be 97%, the sodium-chlor transmitance nanofiltration membrane that is greater than 50%, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.
Described multistage nanofiltration system is 3 ~ 8 grades of nanofiltration system.
Described vaporizer is the one in thin-film evaporator, multiple-effect evaporator, circular form vaporizer, low-flash.
Described nanofiltration system adopt to sodium sulfate rejection be 98%, nanofiltration membrane, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.
Technical scheme of the present invention is:
From the above-mentioned description to structure of the present invention, compared to the prior art, tool of the present invention has the following advantages:
(1) by complexing, nanofiltration and centrifugal treating, realize sodium-chlor and sweet oil separating, make not containing inorganic salt in glycerinated organic phase, the feasibility of guarantee subsequent evaporation concentration and fractionation process.
(2) by adding acid solution adjust ph to 6 ~ 12 to containing in the concentrated solution of glycerine complex compound, make copper glycerolate or other glycerine metal complex decomplexing, form glycerine and copper hydroxide or other metal hydroxides, again through centrifugal, realize being separated of glycerine and copper hydroxide or other metal hydroxides, and by copper hydroxide or other metal hydroxides reuse in complexing, for the preparation of glycerine complex compound, thus realize the recycle of copper hydroxide or other metal hydroxides.
(3) the nanofiltration dialyzate of sodium chloride-containing is after evaporation concentration and crystallization treatment, obtains sodium chloride crystal and crystalline mother solution, because salinity in mother liquor reduces, takes biochemical processing process, make water outlet water quality reaching standard after can diluting.
(4) glycerinated centrifugate is through nanofiltration, reverse osmosis concentration, distillation and fractionation process, and can obtain finished product glycerine, purity reaches 95%.
Accompanying drawing explanation
Fig. 1 is the structured flowchart that height salt of the present invention contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water.
Embodiment
1 the specific embodiment of the present invention is described with reference to the accompanying drawings.
With reference to Fig. 1, high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water, and it comprises: complex reaction tank 1, multistage nanofiltration system 2, vaporizer 3, crystallizer 4, decomplexing retort 5, centrifugal device 6, nanofiltration system 7, reverse osmosis unit 8, distillation tower 9, rectifying tower 10, glycerine storage tank 11.
The water-in of complex reaction tank 1 connects with the water outlet of high salt containing glycerine high depth organic waste water, another import of complex reaction tank 1 connects with the solid outlet of centrifugal device 6, the water outlet of complex reaction tank 1 connects with the water-in of multistage nanofiltration system 2, the nanofiltration dialyzate water outlet of multistage nanofiltration system 2 connects with vaporizer 3 water-in, the nanofiltration concentrated solution water outlet of multistage nanofiltration system 2 connects with the water-in of decomplexing retort 5, vaporizer 3 water outlet connects with crystallizer 4 water-in, the water outlet of decomplexing retort 5 connects with the water-in of centrifugal device 6, the liquid exit of centrifugal device 6 connects with nanofiltration system 7 water-in, the water outlet of nanofiltration system 7 connects with the water-in of reverse osmosis unit 8, the water outlet of reverse osmosis unit 8 connects with the water-in of distillation tower 9, the water outlet of distillation tower 9 connects with the water-in of rectifying tower 10, the water outlet of rectifying tower 10 connects with glycerine storage tank 11, not contaminated in order to ensure multistage nanofiltration system 2, before multistage nanofiltration system 2, a micro-filtration or ultra-filtration equipment 12 can also be increased.
The present invention is based on high salt containing the composition of glycerine high depth organic waste water, character and existing processing scheme, devise a kind of high salt containing Glycerol Wastewater treatment process, it relates to the treatment process such as complexing, nanofiltration, decomplexing, centrifugal, reverse osmosis concentration, evaporation concentration, crystallization, fractionation, thus is formed and a kind ofly effectively can realize the device of high salt containing sodium-chlor in glycerine high depth organic waste water and glycerine recycling.
The specific embodiment of high salt containing the retrieving arrangement workflow of sodium-chlor in glycerine high depth organic waste water and glycerine is provided below in conjunction with Fig. 1.
Embodiment 1
(1) complexing
High salt enters complex reaction tank 1 containing Glycerol Wastewater after pipeline is collected, and adds alkaline solution and copper sulfate in complex reaction tank 1, to make in waste water contained glycerine in the basic conditions with cupric ion generation complex reaction, generate copper glycerolate.
Described high salt is 30% containing the concentration of sodium-chlor in Glycerol Wastewater, and the concentration of glycerine is 2%, and alkaline solution is sodium hydroxide solution.
(2) nanofiltration desalination (glycerine is separated with salt)
Make the water outlet of step (1) complex reaction tank 1 enter multistage nanofiltration system 2 and carry out classified filtering desalination, obtain containing the nanofiltration concentrated solution of copper glycerolate and the nanofiltration dialyzate of sodium chloride-containing.Not contaminated in order to ensure multistage nanofiltration system 2, before nanofiltration desalination, increase ultra-filtration equipment 12 to remove large granular impurity, be purified glycerine organic waste water.
Multistage nanofiltration system 2 adopt to magnesium sulfate rejection rate be 97%, the sodium-chlor transmitance nanofiltration membrane that is greater than 50%, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.Multistage nanofiltration system 2 for classified filtering desalination is 5 grades of nanofiltration system.
(3) evaporation concentration
Make to flow into vaporizer 3 by the nanofiltration dialyzate of nanofiltration system 2 gained sodium chloride-containing multistage in step (2) by pipeline, evaporation concentration is carried out to nanofiltration dialyzate, obtains sodium-chlor concentrated solution.
Described vaporizer 3 is thin-film evaporator, and the nanofiltration dialyzate flowing into vaporizer is the supersaturated solution of sodium-chlor.
(4) crystallization
Make to evaporate gained sodium-chlor concentrated solution by vaporizer 3 to enter crystallizer 4 and carry out crystallization treatment, obtain solid sodium chloride and crystallization filter after mother liquor.
(5) decomplexing
Make to enter decomplexing retort 5 by the nanofiltration concentrated solution containing copper glycerolate of nanofiltration system 2 gained multistage in step (2), in decomplexing retort 5, add acid solution adjust pH to 10, make copper glycerolate decomplexing.
Described acid solution is sulphuric acid soln.
(6) being separated of glycerine and copper hydroxide
Make the waste water containing glycerine and copper hydroxide of decomplexing gained in decomplexing retort 5 enter centrifugal device 6, through centrifugation, obtain copper hydroxide precipitation and glycerinated centrifugate, copper hydroxide precipitation enters in complex reaction tank 1 and recycles.
(7) nanofiltration separation glycerine
The glycerine centrifugate that contains through centrifugal device 6 gained is carried out nanofiltration by nanofiltration system 7, is separated and obtains nanofiltration concentrated solution and glycerinated nanofiltration dialyzate.
Described nanofiltration system 7 adopt to sodium sulfate rejection be 98%, nanofiltration membrane, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.
(8) reverse osmosis concentration glycerine
Glycerinated nanofiltration dialyzate through nanofiltration system 7 gained is concentrated through reverse osmosis system 8, obtains glycerinated reverse osmosis concentrated liquid.
(9) distillation and concentration glycerine
Distillation tower 9 will be entered through the glycerinated reverse osmosis concentrated liquid of reverse osmosis system 8 gained to distill, obtain glycerinated organic liquid waste.
(10) fractionation
Make the glycerinated organic liquid waste of gained after distillation tower 9 distillation and concentration enter rectifying tower 10, in rectifying tower 10, carry out fractionation, obtain finished product glycerine and organic rectificated remaining liquid, make finished product glycerine enter glycerine storage tank 11.
Embodiment 2
(1) complexing
High salt enters complex reaction tank 1 containing Glycerol Wastewater after pipeline is collected, and adds alkaline solution and other metal-salt in complex reaction tank 1, to make in waste water contained glycerine in the basic conditions with other metal ion generation complex reaction, generate other glycerine metal complex.
Described high salt is 18% containing the concentration of sodium-chlor in Glycerol Wastewater, and the concentration of glycerine is 20%, and alkaline solution is sodium carbonate solution, and other metal-salt is zinc oxide, and other metal ion is zine ion, and other glycerine metal complex is glycerin zinc.
(2) nanofiltration desalination (glycerine is separated with salt)
Make the water outlet of step (1) complex reaction tank 1 enter multistage nanofiltration system 2 and carry out classified filtering desalination, obtain containing the nanofiltration concentrated solution of glycerin zinc and the nanofiltration dialyzate of sodium chloride-containing.Not contaminated in order to ensure multistage nanofiltration system 2, before nanofiltration desalination, increase micro-filtration 12 to remove large granular impurity, be purified glycerine organic waste water.
Multistage nanofiltration system 2 adopt to magnesium sulfate rejection rate be 97%, the sodium-chlor transmitance nanofiltration membrane that is greater than 50%, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.Multistage nanofiltration system 2 for classified filtering desalination is 3 grades of nanofiltration system.
(3) evaporation concentration
Make to flow into vaporizer 3 by the nanofiltration dialyzate of nanofiltration system 2 gained sodium chloride-containing multistage in step (2) by pipeline, evaporation concentration is carried out to nanofiltration dialyzate, obtains sodium-chlor concentrated solution.
Described vaporizer 3 is multiple-effect evaporator, and the nanofiltration dialyzate flowing into vaporizer is the supersaturated solution of sodium-chlor.
(4) crystallization
Make to evaporate gained sodium-chlor concentrated solution by vaporizer 3 to enter crystallizer 4 and carry out crystallization treatment, obtain solid sodium chloride and crystallization filter after mother liquor.
(5) decomplexing
Make to enter decomplexing retort 5 by the nanofiltration concentrated solution containing glycerin zinc of nanofiltration system 2 gained multistage in step (2), in decomplexing retort 5, add acid solution adjust pH to 12, make glycerin zinc decomplexing.
Described acid solution is hydrochloric acid soln.
(6) being separated of glycerine and zinc hydroxide
Make the waste water containing glycerine and zinc hydroxide of decomplexing gained in decomplexing retort 5 enter centrifugal device 6, through centrifugation, obtain zinc hydroxide precipitation and glycerinated centrifugate, zinc hydroxide precipitation enters in complex reaction tank 1 and recycles.
(7) nanofiltration separation glycerine
By being filtered by nanofiltration system 7 containing glycerine centrifugate through centrifugal device 6 gained, be separated and obtain nanofiltration concentrated solution and glycerinated nanofiltration dialyzate.
Described nanofiltration system 7 adopt to sodium sulfate rejection be 98%, nanofiltration membrane, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.
(8) reverse osmosis concentration glycerine
Glycerinated nanofiltration dialyzate through nanofiltration system 7 gained is concentrated through reverse osmosis system 8, obtains glycerinated reverse osmosis concentrated liquid.
(9) distillation and concentration glycerine
Distillation tower 9 will be entered through the glycerinated reverse osmosis concentrated liquid of reverse osmosis system 8 gained to distill, obtain glycerinated organic liquid waste.
(10) fractionation
Make the glycerinated organic liquid waste of gained after distillation tower 9 distillation and concentration enter rectifying tower 10, in rectifying tower 10, carry out fractionation, obtain finished product glycerine and organic rectificated remaining liquid, make finished product glycerine enter glycerine storage tank 11.
Embodiment 3
(1) complexing
High salt enters complex reaction tank 1 containing Glycerol Wastewater after pipeline is collected, and adds alkaline solution and other metal-salt in complex reaction tank 1, to make in waste water contained glycerine in the basic conditions with other metal ion generation complex reaction, generate other glycerine metal complex.
Described high salt is 30% containing the concentration of sodium-chlor in Glycerol Wastewater, and the concentration of glycerine is 12%, and alkaline solution is sodium carbonate solution, and other metal-salt is iron(ic) chloride, and other metal ion is iron ion, and other glycerine metal complex is glycerine iron.
(2) nanofiltration desalination (glycerine is separated with salt)
Make the water outlet of step (1) complex reaction tank 1 enter multistage nanofiltration system 2 and carry out classified filtering desalination, obtain containing the nanofiltration concentrated solution of glycerine iron and the nanofiltration dialyzate of sodium chloride-containing.
Multistage nanofiltration system 2 adopt to magnesium sulfate rejection rate be 97%, the sodium-chlor transmitance nanofiltration membrane that is greater than 50%, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.Multistage nanofiltration system 2 for classified filtering desalination is 8 grades of nanofiltration system.
(3) evaporation concentration
Make to flow into vaporizer 3 by the nanofiltration dialyzate of nanofiltration system 2 gained sodium chloride-containing multistage in step (2) by pipeline, evaporation concentration is carried out to nanofiltration dialyzate, obtains sodium-chlor concentrated solution.
Described vaporizer 3 is circular form vaporizer, and the nanofiltration dialyzate flowing into vaporizer is the supersaturated solution of sodium-chlor.
(4) crystallization
Make to evaporate gained sodium-chlor concentrated solution by vaporizer 3 to enter crystallizer 4 and carry out crystallization treatment, obtain solid sodium chloride and crystallization filter after mother liquor.
(5) decomplexing
Make to enter decomplexing retort 5 by the nanofiltration concentrated solution containing glycerine iron of nanofiltration system 2 gained multistage in step (2), in decomplexing retort 5, add acid solution adjust pH to 6, make glycerine iron decomplexing.
Described acid solution is hydrochloric acid soln.
(6) being separated of glycerine and ironic hydroxide
Make the waste water containing glycerine and ironic hydroxide of decomplexing gained in decomplexing retort 5 enter centrifugal device 6, through centrifugation, obtain ferric hydroxide precipitate and glycerinated centrifugate, ferric hydroxide precipitate enters in complex reaction tank 1 and recycles.
(7) nanofiltration separation glycerine
By being filtered by nanofiltration system 7 containing glycerine centrifugate through centrifugal device 6 gained, be separated and obtain nanofiltration concentrated solution and glycerinated nanofiltration dialyzate.
Described nanofiltration system 7 adopt to sodium sulfate rejection be 98%, nanofiltration membrane, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C, and optimum temps is 35 ~ 40 DEG C.
(8) reverse osmosis concentration glycerine
Glycerinated nanofiltration dialyzate through nanofiltration system 7 gained is concentrated through reverse osmosis system 8, obtains glycerinated reverse osmosis concentrated liquid.
(9) distillation and concentration glycerine
Distillation tower 9 will be entered through the glycerinated reverse osmosis concentrated liquid of reverse osmosis system 8 gained to distill, obtain glycerinated organic liquid waste.
(10) fractionation
Make the glycerinated organic liquid waste of gained after distillation tower 9 distillation and concentration enter rectifying tower 10, in rectifying tower 10, carry out fractionation, obtain finished product glycerine and organic rectificated remaining liquid, make finished product glycerine enter glycerine storage tank 11.
Above are only the specific embodiment of the present invention, but design concept of the present invention is not limited thereto, all changes utilizing this design the present invention to be carried out to unsubstantiality, all should belong to the behavior of invading scope.
Claims (8)
1. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water, it is characterized in that: comprise complex reaction tank, multistage nanofiltration system, vaporizer, crystallizer, decomplexing retort, centrifugal device, nanofiltration system, reverse osmosis unit, distillation tower, rectifying tower, glycerine storage tank;
The water-in of described complex reaction tank connects with the water outlet of high salt containing glycerine high depth organic waste water, another import of complex reaction tank connects with the solid outlet of centrifugal device, the water outlet of complex reaction tank connects with the water-in of multistage nanofiltration system, the nanofiltration dialyzate water outlet of multistage nanofiltration system connects with vaporizer water-in, the nanofiltration concentrated solution water outlet of multistage nanofiltration system connects with the water-in of decomplexing retort, vaporizer water outlet connects with crystallizer water-in, the water outlet of decomplexing retort connects with the water-in of centrifugal device, the liquid exit of centrifugal device connects with nanofiltration system water-in, the water outlet of nanofiltration system connects with the water-in of reverse osmosis unit, the water outlet of reverse osmosis unit connects with the water-in of distillation tower, the water outlet of distillation tower connects with the water-in of rectifying tower, the water outlet of rectifying tower connects with glycerine storage tank.
2. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 1, it is characterized in that: set up a micro-filtration or ultra-filtration equipment before described multistage nanofiltration system.
3. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 1, it is characterized in that: described multistage nanofiltration system adopt to magnesium sulfate rejection rate be 97%, the sodium-chlor transmitance nanofiltration membrane that is greater than 50%, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C.
4. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 3, it is characterized in that: the working temperature of described membrane module is 35 ~ 40 DEG C.
5. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 1, it is characterized in that: described multistage nanofiltration system is 3 ~ 8 grades of nanofiltration system.
6. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 1, it is characterized in that: described vaporizer is the one in thin-film evaporator, multiple-effect evaporator, circular form vaporizer, low-flash.
7. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 1, it is characterized in that: it is the nanofiltration membrane of 98% that described nanofiltration system adopts sodium sulfate rejection, membrane module is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 3 ~ 45bar, and working temperature is 20 ~ 45 DEG C.
8. high salt contains the retrieving arrangement of sodium-chlor and glycerine in glycerine high depth organic waste water as claimed in claim 7, it is characterized in that: the working temperature of described membrane module is 35 ~ 40 DEG C.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107473484A (en) * | 2017-09-20 | 2017-12-15 | 大连理工大学 | NF RO MD divide salt desalination system |
| TWI636967B (en) * | 2017-06-30 | 2018-10-01 | 國立清華大學 | System and method for treating salt-containing glycerin wastewater |
| CN113461246A (en) * | 2021-08-13 | 2021-10-01 | 江苏扬农化工集团有限公司 | Method for recovering glycerol monomethyl ether and glycerol from epichlorohydrin wastewater |
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| CN102689936A (en) * | 2012-05-24 | 2012-09-26 | 西安汉术化学工程股份有限公司 | Method for processing wastewater from production of epoxy chloropropane by using glycerol as material |
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| TWI636967B (en) * | 2017-06-30 | 2018-10-01 | 國立清華大學 | System and method for treating salt-containing glycerin wastewater |
| US10364162B2 (en) | 2017-06-30 | 2019-07-30 | National Tsing Hua University | System and method for treating salt-containing glycerin wastewater |
| CN107473484A (en) * | 2017-09-20 | 2017-12-15 | 大连理工大学 | NF RO MD divide salt desalination system |
| CN113461246A (en) * | 2021-08-13 | 2021-10-01 | 江苏扬农化工集团有限公司 | Method for recovering glycerol monomethyl ether and glycerol from epichlorohydrin wastewater |
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