CN107324577A - A kind of epoxy resin production waste-water recycling treatment process - Google Patents
A kind of epoxy resin production waste-water recycling treatment process Download PDFInfo
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- CN107324577A CN107324577A CN201710706831.4A CN201710706831A CN107324577A CN 107324577 A CN107324577 A CN 107324577A CN 201710706831 A CN201710706831 A CN 201710706831A CN 107324577 A CN107324577 A CN 107324577A
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- epoxy resin
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- production waste
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- 239000002351 wastewater Substances 0.000 title claims abstract description 56
- 239000003822 epoxy resin Substances 0.000 title claims abstract description 54
- 229920000647 polyepoxide Polymers 0.000 title claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 42
- 230000008569 process Effects 0.000 title claims abstract description 33
- 238000004064 recycling Methods 0.000 title claims abstract description 17
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 82
- 235000011187 glycerol Nutrition 0.000 claims abstract description 40
- 238000001764 infiltration Methods 0.000 claims abstract description 14
- 238000001704 evaporation Methods 0.000 claims abstract description 13
- 230000008020 evaporation Effects 0.000 claims abstract description 13
- 238000012545 processing Methods 0.000 claims abstract description 13
- 238000002425 crystallisation Methods 0.000 claims abstract description 12
- 230000008025 crystallization Effects 0.000 claims abstract description 12
- 238000001471 micro-filtration Methods 0.000 claims abstract description 11
- 238000011084 recovery Methods 0.000 claims abstract description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 65
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims description 61
- 239000007788 liquid Substances 0.000 claims description 55
- 239000011780 sodium chloride Substances 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 239000002904 solvent Substances 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 14
- 239000012141 concentrate Substances 0.000 claims description 13
- 230000005684 electric field Effects 0.000 claims description 12
- 239000012466 permeate Substances 0.000 claims description 12
- 239000012528 membrane Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 239000007864 aqueous solution Substances 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 239000012267 brine Substances 0.000 claims description 5
- 230000004907 flux Effects 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 5
- 238000010907 mechanical stirring Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 5
- 238000013517 stratification Methods 0.000 claims description 5
- 230000026676 system process Effects 0.000 claims description 3
- 238000000605 extraction Methods 0.000 abstract description 5
- 150000003839 salts Chemical class 0.000 abstract description 5
- 238000010612 desalination reaction Methods 0.000 abstract description 4
- 238000011161 development Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 230000006872 improvement Effects 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 description 6
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 5
- 239000004593 Epoxy Substances 0.000 description 5
- 230000003020 moisturizing effect Effects 0.000 description 4
- 229940106691 bisphenol a Drugs 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- UPBLAVFWWWKVAJ-UHFFFAOYSA-N [Cl].CCC Chemical compound [Cl].CCC UPBLAVFWWWKVAJ-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical group 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 238000005341 cation exchange Methods 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- XKZQKPRCPNGNFR-UHFFFAOYSA-N 2-(3-hydroxyphenyl)phenol Chemical compound OC1=CC=CC(C=2C(=CC=CC=2)O)=C1 XKZQKPRCPNGNFR-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000007259 addition reaction Methods 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 239000003011 anion exchange membrane Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004807 desolvation Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007646 directional migration Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 239000004850 liquid epoxy resins (LERs) Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 235000002639 sodium chloride Nutrition 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- 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
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a kind of epoxy resin production waste-water recycling treatment process, including 1), micro-filtration processing and electric drive membranous system processing；2) extracting system is handled；3) vapo(u)rization system is handled；4), counter-infiltration system is handled；5), evaporation and crystallization system is handled.The present invention is based on the glycerin components reclaimed in waste water, to improve the feature of environmental protection and economy of production, propose the process route of electric drive film+treatment by extraction epoxy resin waste-water, the purpose of desalination can be reached, the glycerine wherein with economic value has been reclaimed again, the qualified discharge of salt in waste water, glycerine recovery and waste water is realized, so as to reach improvement local environment, the sustainable development purpose of the sector and society is promoted.
Description
Technical field
The present invention relates to chemical wastewater treatment field, more particularly, to a kind of epoxy resin production waste-water recycling treatment work
Skill.
Background technology
Epoxy resin includes liquid-state epoxy resin (base epoxy resin) and solid epoxy resin.Liquid-state epoxy resin technique
It is divided into one-step technology and two step method production technology.One-step method liquid epoxy resin technology is by bisphenol-A and excessive epoxy chlorine
Propane carries out polycondensation under sodium hydroxide effect, reclaims after excessive epoxychloropropane, then molten through extracting, washing, filter, remove
Agent, is finally made product.At present, the maximum E-44 types epoxy resin of output in domestic uses the technique productions.Two-step process
It is that by bisphenol-A and epoxychloropropane under catalyst action, the first step first passes through addition reaction, generates diphenol propane chloropharin ether
Intermediate, second step carries out ring-closure reaction in the presence of sodium hydroxide again, generates epoxy resin, reclaims excessive epoxychloropropane
Afterwards, then through extraction, washing, filtering, desolvation, product is finally made.At present, domestic E-5l, E-54 type epoxy resin is to adopt
Use the technique productions.Solid epoxy resin production technology is divided into WATER-WASHING METHOD, solvent extraction, three kinds of solvent condensation methods again.Epoxy
Chloropropane is the raw material for preparing epoxy resin, and the advanced method that current various countries are used is using glycerine as main material production epoxy chlorine
Propane, epoxychloropropane will turn into the largest application areas of glycerine.At the same time, production epoxy resin can produce a large amount of high salts
Spend the waste water of high content of organics, main component is NaCl, glycerine, bisphenol-A and a small amount of aged resin, overall pH is into alkalescence.
The characteristics of waste water of epoxy resin production industry has high organic concentration, high salinity, big wastewater discharge, gives up
Shipwreck treatability is to restrict the chief place of Epoxy Industry development.According to incompletely statistics, China's Epoxy Industry
Annual waste discharge millions of tons.The characteristics of its waste water is：Wastewater discharge big (20m3/ tons of products), organic pollution content
High (COD may be up to 50000mg/L sometimes), salt content are high (5~14%), it is impossible to use secondary biochemical treatment technology, belong to compared with
Intractable industrial wastewater.Because epoxy resin production waste-water is difficult to handle so that current most of secondary biochemicals that oneself builds up
Processing unit is idle or handles not up to standard.In addition, epoxy resin industry there is no the reuse for carrying out waste water, water resource is caused
Serious waste, its unit water resources consumption rate is much higher than same kind of products at abroad production target.Epoxy resin production waste-water
It is up to standard to handle the bottleneck that oneself further develops as restriction China Epoxy Industry.And existing technology primarily directed to
This target of hot method concentration desalination, to be applicable the biological effluent treatment with the later stage, have ignored the economy of glycerin components therein
Value.This research topic is based on reclaiming the glycerin components in waste water, to improve the feature of environmental protection and economy of production, proposes electricity
The process route of drive membrane+treatment by extraction epoxy resin waste-water, can reach the purpose of desalination, and having reclaimed again wherein has warp
The glycerine for value of helping, realizes the qualified discharge of salt in waste water, glycerine recovery and waste water, so that improvement local environment is reached,
Promote the sustainable development purpose of the sector and society.
The content of the invention
In view of the above-mentioned problems, the invention provides a kind of epoxy resin production waste-water recycling treatment process, effectively solving
The problem of being pointed out in background technology.
The technical scheme of the use of the present invention is as follows：
A kind of epoxy resin production waste-water recycling treatment process, comprises the following steps：
1), epoxy resin production waste-water first passes around micro-filtration processing and removes graininess impurity, subsequently into electric drive membrane system
The light room of system, dense room is input into the process water of light room equivalent in debugging, then by the logical upper direct current of electric drive membranous system
Electric field makes the NaCl in epoxy resin production waste-water progressively migrate into dense room feed liquid, obtains light room feed liquid and dense room feed liquid, dense
Room feed liquid is the strong brine containing a large amount of NaCl；
2), by step 1) obtained light room feed liquid enters to extracting system, put into the extractor of extracting system certain
The n-butanol solvent of amount, is sufficiently stirred for stratification formation extract and raffinate after mixing, extract be containing glycerine just
Butanol feed liquid, raffinate is the aqueous solution containing a small amount of NaCl and glycerine；
3), by step 2) obtained extract feeding vapo(u)rization system, by evaporation process so that n-butanol volatilization obtains sweet
Oil, step 2 is back to after the n-butanol condensation of volatilization) it is added in extractor；
4), by step 2) obtained raffinate is fed through counter-infiltration system and carries out concentration, obtains concentrate and transmission
Liquid, the composition of concentrate constitutes, concentrate return to step 1 basically identical with epoxy resin production waste-water) re-start at micro-filtration
Reason, permeate is pure water, and permeate is back to step 1) in the dense room of electric drive membranous system process water；
5), by step 1) obtained dense room feed liquid feeding evaporation and crystallization system is evaporated crystallization treatment, obtains technical grade
NaCl products, while condensate liquid be the pure water without volatile materials, Condensate reuse is in step 1) in electric drive membranous system
The process water of dense room.
Preferably, the step 1) current density of DC electric field is 0.02A/cm2, the NaCl concentration of light room feed liquid is small
In 1%.
Preferably, the step 2) in charging hole be provided with the top of extractor and add hole, described charging hole is used for
The charging of light room feed liquid, the described hole that adds is used to add n-butanol solvent.
Preferably, the step 2) in be provided with extract delivery outlet in the middle part of extractor, for the output of extract, bottom
Portion is provided with raffinate delivery outlet, for the output of raffinate, and mechanical stirring device is provided with described extractor.
Preferably, the step 2) in by charging hole enter extractor light room feed liquid with by add hole add extraction
The volume ratio for taking the n-butanol solvent of tank is 1:1.0-1.5.
Preferably, the step 3) in extract enter vapo(u)rization system evaporation process after, obtained purity is not less than
99.99% glycerine, the yield of the glycerine is more than 95%.
Preferably, the step 4) in counter-infiltration system membrane flux be 18~25LMH, the rate of recovery be 85~90%.
Present invention also offers a kind of epoxy resin production waste-water recycling treatment system, including：
Micro-filtration processing system, for removing the graininess impurity in epoxy resin production waste-water；
Electric drive membranous system, the water outlet of micro-filtration processing system is connected with the light room of electric drive membranous system, electric drive membranous system
The input of dense room and the process water of light room equivalent, make NaCl in the light room epoxy resin production waste water of electric drive membranous system by
Step is migrated into dense room, and obtained dense room feed liquid is the strong brine containing a large amount of NaCl；
Evaporation and crystallization system, for being evaporated crystallization treatment to dense room feed liquid, obtains the NaCl products of technical grade, simultaneously
Condensate liquid is the pure water without volatile materials, and Condensate reuse is in the dense room moisturizing of electric drive membranous system；
Extracting system, the light room feed liquid feeding extracting system of electric drive membranous system, and n-butanol solvent is added, it is sufficiently stirred for
Stratification formation extract and raffinate after mixing, extract are the n-butanol feed liquid containing glycerine, and raffinate is containing few
Measure the aqueous solution of NaCl and glycerine；
Vapo(u)rization system, extract is evaporated processing into vapo(u)rization system so that n-butanol volatilization obtains glycerine, volatilization
Extracting system is back to after n-butanol condensation；
Counter-infiltration system, raffinate enters counter-infiltration system and carries out concentration, obtains concentrate and permeate, concentrate
Composition composition it is basically identical with epoxy resin production waste-water, permeate is pure water, and permeate is back to electric drive membranous system
Dense room moisturizing.
Preferably, described electric drive membranous system makes NaCl in epoxy resin production waste-water progressively by DC electric field
Migrate into dense room feed liquid, the current density of the DC electric field is 0.02A/cm2, and the NaCl concentration of light room feed liquid is less than 1%.
Preferably, the light room feed liquid of the electric drive membranous system is entered in the extractor of extracting system, tank deck is extracted
Portion is provided with charging hole and n-butanol solvent adds hole.
Preferably, being provided with extract delivery outlet in the middle part of the extractor, bottom is provided with raffinate delivery outlet, extractor
It is interior to be provided with mechanical stirring device.
Preferably, into the extracting system light room feed liquid with add extracting system n-butanol solvent volume ratio
For 1:1.0-1.5.
Preferably, extract enters after vapo(u)rization system evaporation process, obtained purity is not less than 99.99% glycerine,
The yield of the glycerine is more than 95%.
Preferably, the membrane flux of the counter-infiltration system is 18~25LMH, the rate of recovery is 85~90%.
Electric drive membrane technology refers in the case where electric field force is acted on ion by the membrane separating process of selective ion exchange membrane, its
Core is anion and cation exchange membrane, i.e., only allow cation to pass through using cation-exchange membrane, anion-exchange membrane is only permitted
Perhaps the characteristic that anion passes through carries out the technology of Selective Separation to effects of ion.Under electric field force effect, the moon in solution
Directional migration occurs for cation, and another part water body is moved to from a part of water body, so as to reach solution separation, purification and concentrate
Purpose.
The present invention, to improve the feature of environmental protection and economy of production, proposes electric drive based on the glycerin components reclaimed in waste water
The process route of film+treatment by extraction epoxy resin waste-water, can reach the purpose of desalination, and having reclaimed again wherein has economic valency
The glycerine of value, realizes the qualified discharge of salt in waste water, glycerine recovery and waste water, so as to reach improvement local environment, promotes
The sector and the sustainable development purpose of society.
Its advantage is as follows：
1) NaCl in epoxy resin production waste-water, is migrated by the electric drive membranous system of the present invention, can be effectively realized
The separation of glycerine and NaCl, glycerine leak rate is less than 5%, and light room NaCl remains below 10000mg/L；
2) glycerine in the light room feed liquid of electric drive film can effectively, be reclaimed by the extracting system of the present invention, and can be reclaimed
Extractant (n-butanol)；
3) concentration of glycerine and NaCl in extracting system raffinate, can be improved by the counter-infiltration system of the present invention, can be followed
Ring can reclaim most water to the dense room of electric drive membranous system to raw water tank, reduce water increment；
4), epoxy resin production waste-water is handled by electric drive membranous system+extracting system of the present invention, obtained
Glycerol product high purity 99.99%, product yield more than 95%, quality be higher than national standard；
5), epoxy resin production waste-water is handled by electric drive membranous system+evaporation and crystallization system of the present invention, institute
The NaCl product purities of acquisition are up to 98%, and product yield is more than 97%, and quality is higher than national two grades of Nacl standards；
6), the handling process provided by the present invention carries out full dose recycling treatment to epoxy resin production waste-water has extensively
General application prospect, not only carries out comprehensive utilization of resources, while also developing the product of high value.
Brief description of the drawings
Fig. 1 is flowage structure schematic diagram of the invention.
Embodiment
The present invention is described in further detail below by specific embodiment and with reference to accompanying drawing.
Embodiment 1
A kind of epoxy resin production waste-water recycling treatment process, comprises the following steps：
1), epoxy resin production waste-water first passes around micro-filtration processing and removes graininess impurity, subsequently into electric drive membrane system
The light room of system, dense room is input into the process water of light room equivalent in debugging, then by the logical upper direct current of electric drive membranous system
Electric field makes the NaCl in epoxy resin production waste-water progressively migrate into dense room feed liquid, obtains light room feed liquid and dense room feed liquid, dense
Room feed liquid is the strong brine containing a large amount of NaCl, and the current density of DC electric field is 0.02A/cm2, the NaCl concentration of light room feed liquid
Less than 1%；
2), by step 1) obtained light room feed liquid enters to extracting system, put into the extractor of extracting system certain
The n-butanol solvent of amount, is sufficiently stirred for stratification formation extract and raffinate after mixing, extract be containing glycerine just
Butanol feed liquid, raffinate is that charging hole is provided with the top of the aqueous solution containing a small amount of NaCl and glycerine, extractor and hole is added, institute
The charging hole stated is used for the charging of light room feed liquid, and the described hole that adds is used to add n-butanol solvent, is entered by charging hole and extracted
The light room feed liquid of tank is taken with being 1 by adding the volume ratio for the n-butanol solvent that hole adds extractor:1.0-1.5, extractor
Middle part is provided with extract delivery outlet, for the output of extract, and bottom is provided with raffinate delivery outlet, for the output of raffinate,
Mechanical stirring device is provided with described extractor；
3), by step 2) obtained extract feeding vapo(u)rization system, by evaporation process so that n-butanol volatilization obtains sweet
Oil, the purity of glycerine is not less than 99.99%, and yield is back to step 2 more than 95% after the n-butanol condensation of volatilization) it is added to
In extractor；
4), by step 2) obtained raffinate is fed through counter-infiltration system and carries out concentration, obtains concentrate and transmission
Liquid, the composition of concentrate constitutes, concentrate return to step 1 basically identical with epoxy resin production waste-water) re-start at micro-filtration
Reason, permeate is pure water, and permeate is back to step 1) in the dense room of electric drive membranous system process water, the film of counter-infiltration system
Flux is 18~25LMH, and the rate of recovery is 85~90%；
5), by step 1) obtained dense room feed liquid feeding evaporation and crystallization system is evaporated crystallization treatment, obtains technical grade
NaCl products, while condensate liquid be the pure water without volatile materials, Condensate reuse is in step 1) in electric drive membranous system
The process water of dense room.
Embodiment 2
As shown in figure 1, a kind of epoxy resin production waste-water recycling treatment system, it is characterised in that including：
Micro-filtration processing system, for removing the graininess impurity in epoxy resin production waste-water；
Electric drive membranous system, the water outlet of micro-filtration processing system is connected with the light room of electric drive membranous system, electric drive membranous system
The input of dense room and the process water of light room equivalent, the NaCl in epoxy resin production waste-water is progressively migrated by DC electric field
Into dense room feed liquid, the current density of the DC electric field is 0.02A/cm2, and the NaCl concentration of obtained light room feed liquid is less than
1%, obtained dense room feed liquid is the strong brine containing a large amount of NaCl；
Evaporation and crystallization system, for being evaporated crystallization treatment to dense room feed liquid, obtains the NaCl products of technical grade, simultaneously
Condensate liquid is the pure water without volatile materials, and Condensate reuse is in the dense room moisturizing of electric drive membranous system；
Charging hole is provided with the top of extracting system, extractor and n-butanol solvent adds hole, the light room material of electric drive membranous system
In the extractor of liquid feeding extracting system, and add n-butanol solvent, the volume ratio of light room feed liquid and n-butanol solvent is 1:
Extract delivery outlet is provided with the middle part of 1.0-1.5, extractor, bottom is provided with raffinate delivery outlet, extractor and stirred provided with machinery
Mix device, stratification formation extract and raffinate after mixing be sufficiently stirred for by mechanical stirring device, extract be containing
The n-butanol feed liquid of glycerine, raffinate is the aqueous solution containing a small amount of NaCl and glycerine, and extract is exported from extract delivery outlet,
Raffinate is exported from raffinate delivery outlet；
Vapo(u)rization system, extract is evaporated processing into vapo(u)rization system so that n-butanol volatilization obtains purity and is not less than
99.99% glycerine, the yield of glycerine is back to extracting system more than 95% glycerine after the n-butanol condensation of volatilization；
Counter-infiltration system, the membrane flux of counter-infiltration system is 18~25LMH, and the rate of recovery is 85~90%, and raffinate enters
Counter-infiltration system carries out concentration, obtains concentrate and permeate, the composition composition and epoxy resin production waste-water of concentrate
Basically identical, permeate is pure water, and permeate is back to the dense room moisturizing of electric drive membranous system.
Claims (7)
1. a kind of epoxy resin production waste-water recycling treatment process, it is characterised in that comprise the following steps：
1), epoxy resin production waste-water first passes around micro-filtration processing and removes graininess impurity, subsequently into electric drive membranous system
Light room, dense room is input into the process water of light room equivalent in debugging, then by the logical upper DC electric field of electric drive membranous system
The NaCl in epoxy resin production waste-water is progressively migrated into dense room feed liquid, obtain light room feed liquid and dense room feed liquid, dense room material
Liquid is the strong brine containing a large amount of NaCl；
2), by step 1) obtained light room feed liquid enters to extracting system, put into the extractor of extracting system a certain amount of
N-butanol solvent, is sufficiently stirred for stratification formation extract and raffinate after mixing, and extract is the n-butanol containing glycerine
Feed liquid, raffinate is the aqueous solution containing a small amount of NaCl and glycerine；
3), by step 2) obtained extract feeding vapo(u)rization system, by evaporation process so that n-butanol volatilization obtains glycerine, wave
Step 2 is back to after the n-butanol condensation of hair) it is added in extractor；
4), by step 2) obtained raffinate is fed through counter-infiltration system and carries out concentration, obtains concentrate and permeate, dense
The composition of contracting liquid constitutes, concentrate return to step 1 basically identical with epoxy resin production waste-water) micro-filtration processing is re-started, thoroughly
Liquid is crossed for pure water, permeate is back to step 1) in the dense room of electric drive membranous system process water；
5), by step 1) obtained dense room feed liquid feeding evaporation and crystallization system is evaporated crystallization treatment, obtains technical grade
NaCl products, at the same condensate liquid be the pure water without volatile materials, Condensate reuse is in step 1) in electric drive membranous system it is dense
The process water of room.
2. a kind of epoxy resin production waste-water recycling treatment process according to claim 1, it is characterised in that the step
The current density of rapid 1) DC electric field is 0.02A/cm2, and the NaCl concentration of light room feed liquid is less than 1%.
3. a kind of epoxy resin production waste-water recycling treatment process according to claim 1 or 2, it is characterised in that institute
State step 2) in charging hole be provided with the top of extractor and add hole, described charging hole is used for the charging of light room feed liquid, described
Add hole be used for add n-butanol solvent.
4. a kind of epoxy resin production waste-water recycling treatment process according to claim 3, it is characterised in that the step
It is rapid 2) in be provided with extract delivery outlet in the middle part of extractor, for the output of extract, bottom is provided with raffinate delivery outlet, is used for
Mechanical stirring device is provided with the output of raffinate, described extractor.
5. a kind of epoxy resin production waste-water recycling treatment process according to claim 4, it is characterised in that the step
It is rapid 2) in by charging hole enter extractor light room feed liquid with pass through add hole add extractor n-butanol solvent volume
Than for 1:1.0-1.5.
6. a kind of epoxy resin production waste-water recycling treatment process according to claim 5, it is characterised in that the step
It is rapid 3) in extract enter after vapo(u)rization system evaporation process, obtained purity is not less than 99.99% glycerine, the glycerine
Rate is more than 95%.
7. a kind of epoxy resin production waste-water recycling treatment process according to claim 6, it is characterised in that the step
It is rapid 4) in counter-infiltration system membrane flux be 18~25LMH, the rate of recovery be 85~90%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113373463A (en) * | 2021-06-24 | 2021-09-10 | 宁波环洋新材料股份有限公司 | Method for preparing caustic soda from sodium chloride wastewater generated in epoxy resin production process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85105641A (en) * | 1984-12-10 | 1987-01-28 | 国际壳牌研究有限公司 | From salt solution, reclaim the method for glycerine |
| CN102503014A (en) * | 2011-11-22 | 2012-06-20 | 浙江大学 | Treatment method of glycerin wastewater containing salt |
| CN105692989A (en) * | 2014-11-27 | 2016-06-22 | 上海凯鑫分离技术股份有限公司 | A comprehensive utilization process for viscose fiber acidic waste water |
| US20160200652A1 (en) * | 2013-08-19 | 2016-07-14 | REG Life Sciences, LLC | Production of partially refined waste glycerol |
| CN206051730U (en) * | 2016-08-30 | 2017-03-29 | 杭州上拓环境科技股份有限公司 | A kind of system using various membrane technology recycling treatment kelp processing waste water |
-
2017
- 2017-08-17 CN CN201710706831.4A patent/CN107324577A/en not_active Withdrawn
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85105641A (en) * | 1984-12-10 | 1987-01-28 | 国际壳牌研究有限公司 | From salt solution, reclaim the method for glycerine |
| CN102503014A (en) * | 2011-11-22 | 2012-06-20 | 浙江大学 | Treatment method of glycerin wastewater containing salt |
| US20160200652A1 (en) * | 2013-08-19 | 2016-07-14 | REG Life Sciences, LLC | Production of partially refined waste glycerol |
| CN105692989A (en) * | 2014-11-27 | 2016-06-22 | 上海凯鑫分离技术股份有限公司 | A comprehensive utilization process for viscose fiber acidic waste water |
| CN206051730U (en) * | 2016-08-30 | 2017-03-29 | 杭州上拓环境科技股份有限公司 | A kind of system using various membrane technology recycling treatment kelp processing waste water |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113373463A (en) * | 2021-06-24 | 2021-09-10 | 宁波环洋新材料股份有限公司 | Method for preparing caustic soda from sodium chloride wastewater generated in epoxy resin production process |
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Application publication date: 20171107 |