CN205603386U - Strong brine zero release membrane concentrator - Google Patents
Strong brine zero release membrane concentrator Download PDFInfo
- Publication number
- CN205603386U CN205603386U CN201620035174.6U CN201620035174U CN205603386U CN 205603386 U CN205603386 U CN 205603386U CN 201620035174 U CN201620035174 U CN 201620035174U CN 205603386 U CN205603386 U CN 205603386U
- Authority
- CN
- China
- Prior art keywords
- strong brine
- micro
- filtration
- membrane
- reverse osmosis
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 85
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 74
- 239000012267 brine Substances 0.000 title claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 48
- 238000001471 micro-filtration Methods 0.000 claims abstract description 41
- 238000010612 desalination reaction Methods 0.000 claims abstract description 38
- 238000000926 separation method Methods 0.000 claims abstract description 35
- 238000002425 crystallisation Methods 0.000 claims abstract description 20
- 230000008025 crystallization Effects 0.000 claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 238000001728 nano-filtration Methods 0.000 claims description 45
- 150000003839 salts Chemical class 0.000 claims description 16
- 239000002562 thickening agent Substances 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 13
- 239000012141 concentrate Substances 0.000 claims description 12
- 239000004902 Softening Agent Substances 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 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 description 3
- 150000001768 cations Chemical class 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000001704 evaporation Methods 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract description 4
- 238000004140 cleaning Methods 0.000 description 16
- 238000000034 method Methods 0.000 description 16
- 230000008569 process Effects 0.000 description 10
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 239000003814 drug Substances 0.000 description 6
- 230000004907 flux Effects 0.000 description 6
- 239000012466 permeate Substances 0.000 description 6
- 230000001105 regulatory effect Effects 0.000 description 6
- 230000004044 response Effects 0.000 description 5
- 239000010802 sludge Substances 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 229910052749 magnesium Inorganic materials 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000002455 scale inhibitor Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009292 forward osmosis Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- ARYKTOJCZLAFIS-UHFFFAOYSA-N hydrogen peroxide;ozone Chemical compound OO.[O-][O+]=O ARYKTOJCZLAFIS-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000004317 sodium nitrate Substances 0.000 description 1
- 235000010344 sodium nitrate Nutrition 0.000 description 1
- XZPVPNZTYPUODG-UHFFFAOYSA-M sodium;chloride;dihydrate Chemical compound O.O.[Na+].[Cl-] XZPVPNZTYPUODG-UHFFFAOYSA-M 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model provides a strong brine zero release membrane concentrator, includes: soften the micro -filtration device, receive and strain membrane separation device, strong brine desalination reverse osmosis membrane device, hyperconcetration device, evaporation crystallization device. Soften the concentrated groove of the reaction delivery port of micro -filtration device and be connected with soft micro -filtration device water inlet, be equipped with pH value adjustment mechanism before the delivery port of soft micro -filtration device, the soft micro -filtration device and water inlet and the delivery port tandem connection of each other of straining membrane separation device, strong brine desalination reverse osmosis membrane device, hyperconcetration device, retrieval and utilization water tank, each equipment of receiving, the super strong brine of hyperconcetration device exports and evaporates the crystallization device to be connected. The utility model discloses technology includes processing step, the concentrated processing step of membrane in advance. The utility model discloses the advantage is the combination through multiple concentrated technology, and effective improve equipment handles the efficiency of strong brine, realizes the minimizing of strong brine, the target of zero release, reduces the running cost of strong brine treatment facility.
Description
Technical field
This utility model relates to a kind of water treatment facilities, particularly to a kind of strong brine zero-emission membrance concentration equipment.
Background technology
Wastewater zero discharge is the target that the industrial trade requirement such as Coal Chemical Industry, papermaking realizes, realize the important step of sustainable stable development, and in whole wastewater zero discharge processing links, cost of investment and operating cost that evaporated crystallization device is high are the big bottlenecks that restriction zero-emission realizes, therefore to the wastewater minimisation reuse before entrance evaporative crystallization, it is key one ring effectively reducing disposed of in its entirety cost.
The targeted strong brine of the industry Zero emission device such as Coal Chemical Industry, papermaking is mainly the institute such as coal chemical engineering equipment, paper technology waste discharge respectively through the strong brine produced after wastewater biochemical process, advanced oxidation, Treated sewage reusing water dual membrane system, there is the features such as higher COD (COD), high salinity, high rigidity, high alkalinity, conventional reverse osmosis cannot be directly used to concentrate reuse further, and owing to the general water yield is bigger, being directly entered evaporative crystallization and carry out full-boiled process condensing crystallizing, investment and operating cost are high.
Process both at home and abroad the decrement reuse method for this type of strong brine now typically to have: efficient oxidation, efficient reverse osmosis, just permeate, electricity desalination, Membrane Materials etc..Although the method processed is a lot, but having certain limitation in application, lack systematicness flow process, it is impossible to complete whole process and process, actual processing effect and economy aspect have significantly shortcoming.
Summary of the invention
Goal of the invention of the present utility model is for defect present in prior art, provides a kind of strong brine zero-emission membrance concentration Processes and apparatus.This utility model combination by kinds of processes, is effectively improved the cycles of concentration of strong brine, it is achieved the minimizing of strong brine, to realize reducing evaporated crystallization device scale, reduces overall operation cost.
This utility model includes: soften micro-filtration, nanofiltration membrane separation device, strong brine desalination reverse osmosis membrane apparatus, ultra concentration device, evaporated crystallization device, reuse water tank, it is characterized in that described softening micro-filtration front end is provided with a reaction thickener, it is provided with in reaction thickener and adds softening agent device, add softening agent device and only add softening agent, be not required to add coagulant and flocculation aid.The outlet of reaction thickener is connected with softening micro-filtration water inlet, the outlet softening micro-filtration is connected with the water inlet of nanofiltration membrane separation device, it is provided with pH value governor motion before softening the outlet of micro-filtration, nanofiltration membrane separation device selects to be applicable to carnallite and separates and the nanofiltration membrane component of tolerance high chemical oxygen demand (COD), and pass through multi-stage series, improve the response rate of nanofiltration membrane separation device, design the response rate >=90%.The outlet of nanofiltration membrane separation device is connected with the water inlet of strong brine desalination reverse osmosis membrane apparatus, the outlet of strong brine desalination reverse osmosis membrane apparatus is connected with the water inlet of ultra concentration device, strong brine desalination reverse osmosis membrane apparatus uses and is applicable to the strong brine desalination membrane module that monovalent salt concentrates, and pass through multi-stage series, improve the response rate of strong brine desalination strong brine desalination reverse osmosis unit, design the response rate >=80%.The outlet of ultra concentration device is connected with reuse water tank, and the super brine outlet of ultra concentration device is connected with evaporated crystallization device.Completed salt and the separation of solvent by evaporated crystallization device or concentrate decrement further.
Ultra concentration device uses the ultra concentration assembly being applicable to high strong brine ultra concentration technique, can meet tolerance high chemical oxygen demand (COD) pollution, high salinity concentrates working condition requirement simultaneously, the design response rate >=45%, ultra concentration device dense water salinity reaches more than 10%, and use energy recovery rate device, effectively reduce operation energy consumption.
The NF membrane of described nanofiltration membrane separation device is to be applicable to the nanofiltration membrane component that carnallite separates and tolerates high chemical oxygen demand (COD), and is multi-stage series structure.
Described strong brine desalination reverse osmosis membrane apparatus is to be applicable to the strong brine desalination membrane module that monovalent salt concentrates, and passes through multi-stage series.
Described softening micro-filtration, for softening micro-filtration membrane device, wherein softens micro-filtration membrane and uses organic tube type filter membrance, filtering accuracy ＜ 0.1 micron.It can also be immersed microfiltration film.
Described nanofiltration membrane separation device can use Weak-acid cation switch to replace.
The utility model has the advantages that the combination by multiple concentration technology, be effectively improved the treatment effect of strong brine, it is achieved the minimizing of strong brine, to realize reducing evaporated crystallization device scale, reduce overall operation cost.
Accompanying drawing explanation
Fig. 1 strong brine zero-emission membrance concentration process flow diagram；
Fig. 2 structural representation of the present utility model.
In figure: 1 reaction thickener, 2 softening micro-filtration, 3 nanofiltration membrane separation devices, 4 strong brines desalination reverse osmosis membrane apparatus, 5 ultra concentration devices, 6 evaporated crystallization devices, 7 reuse water tanks；In Fig. 2: pretreatment workshop section: 101 storage regulating reservoirs, 102 advanced oxidation devices, 103 reaction thickeners, 104 softening micro-filtration, 105 intermediate pool, 106 sludge dewatering units, 107 regulating reservoir elevator pumps, 108 micro-filtration membrane suction pumps, 110 strong oxidizer throwing devices, 111 softening medicament addition devices；
Membrance concentration workshop section: 201 cartridge filters, 202 nanofiltration membrane separation devices, 203 nanofiltration effluent troughs, 204 cartridge filters, 205 strong brine desalination reverse osmosis units, 206 reverse osmosis concentrated tanks, 207 film softening plants, 208 ultra concentration intake chambers, 209 ultra concentration devices, 210 reuse tanks, 211 ultrafiltration intake pumps, 212 feed water by reverse osmosis pumps, 213 reverse osmosis high-pressure pumps, 214 films soften feed pump, 215 ultra concentration feed pumps, 216 ultra concentration high-pressure pumps, 217 ultrafiltration apparatus clean pump, 219 air compressor machines, 220 chemically-cleaning devices, 221 sodium hypochlorite throwing devices, 222 softening agent throwing devices, 223 scale inhibitor feeding devices, 224 citric acid throwing devices；230 evaporated crystallization devices.
Detailed description of the invention
Further illustrate embodiment of the present utility model below in conjunction with the accompanying drawings.
Embodiment one:
Strong brine enters the reaction thickener 1 of the softening micro-filtration membrane device 2 of pretreatment workshop section, (seeing Fig. 1) enters softening micro-filtration membrane device 2 and carried out filtering hard turbidity removal after fully softening reaction after the softening agents such as feeding lime in reacting thickener 1, remove most calcium and magnesium, hardness, basicity and suspended contamination in strong brine；The inorganic mud of softening micro-filtration membrane device 2 cycle emissions is after filter-press dehydration, and filtrate returns reaction thickener 1, and dehydrated sludge cake forms the outward transport disposal of common sludge solid waste；Nanofiltration membrane separation device 3 is entered after softening micro-filtration membrane device 2 water outlet pH readjustment；Strong brine separates through nanofiltration membrane separation device 3 and concentrates, and the dense water of nanofiltration forming main sulfur acid sodium and overwhelming majority COD produces water with main containing sodium nitrate, sodium chloride, the nanofiltration of trace amounts of CO D；Nanofiltration is produced water and is entered the strong brine desalination further desalination and concentration of reverse osmosis unit 4, reverse osmosis produced water after desalination meets entrance recycle-water case 7 after reuse requires further, the high strong brine that reverse osmosis concentration is formed and the dense water of nanofiltration are mixed into the further desalination and concentration of ultra concentration device 5, the water that ultra concentration after desalination produces further meets entrance recycle-water case 7 after reuse requires, for plant area's circulating cooling make-up water, the super strong brine that ultra concentration is formed enters follow-up evaporated crystallization device 6.Solid-liquid separation is completed by evaporated crystallization device 6.
Microfiltration in device, nanofiltration, reverse osmosis, super ultra concentration, the cycle of crystallization apparatus make up a prescription, cleaning etc. all uses the self-produced water of device with water, cleans discharge water and returns the reaction thickener 1 softening micro-filtration membrane device 2.
The technique of the present embodiment comprises the following steps:
(1) high strong brine is delivered to pretreatment and softens micro-filtration membrane device 2, for high strong brine being carried out softening turbidity removal pretreatment；
(2) the high strong brine after step (1) softens turbidity removal is delivered to nanofiltration membrane separation device 3, utilize the stalling characteristic of NF membrane, COD in high strong brine, divalent salts are separated with monovalent salt, formed respectively based on COD, divalent salts concentrated solution with based on monovalent salt, the permeate of trace amounts of CO D；
(3) permeate after step (2) nanofiltration separation is delivered to strong brine desalination reverse osmosis membrane apparatus 4, salts substances in removing nanofiltration permeate further, forms the reverse osmosis produced water meeting reuse water quality requirement and the reverse osmosis concentrated water concentrating monovalent salt；
(4) the high strong brine of higher COD, high salinity will be formed after the dense water water dense with nanofiltration of step (3) strong brine desalination reverse osmosis concentration mixes, it is delivered to the further decrement of ultra concentration device 5 concentrate, high strong brine forms super strong brine after ultra concentration device 5 concentrates decrement and goes successively to evaporative crystallization technique section, ultra concentration after desalination is produced water and is mixed with the reverse osmosis produced water through step (3) desalination, and water quality meets reuse water quality requirement；
(5) pretreatment formed through step (1) softening mud is delivered to sludge dewatering unit, after filter-press dehydration, filtrate returns step (1) and softens micro-filtration membrane device 2, improves overall Water Sproading rate, and the filter cake that filter pressing is formed is disposed as common solid waste；
Rinse in step (1) (2) (3) (4), Chemical cleaning water all uses the self-produced water of device, and the Chemical cleaning discharge water periodically produced all is recycled to pretreatment unit, improves overall water use efficiency.
Strong brine after step (2) solid-liquid centrifugation separates is transported to nanofiltration membrane separation device 3, utilize nanofiltration membrane component that far above the characteristic of common reverse osmosis and to monovalent salt, the selection of divalent salts in water body, the tolerance of COD is passed through characteristic, use nanofiltration that the strong brine through pretreatment carries out pre-concentration separation, formed based on COD, divalent salts concentrated solution with based on monovalent salt, the permeate of trace amounts of CO D.
The permeate produced through step (3) nanofiltration separation mainly contains monovalent salt and trace amounts of CO D, therefore strong brine desalination film device can be used to carry out reconcentration reuse, desalination is produced water water quality and is reached to supplement as open type recirculated cooling water about recycled water in country " urban sewage reutilization industry water standard " (GB/T 19923-2005) water standard of water, and concentration side forms salinity and reaches the high strong brine of about 5%.
After the high strong brine mixing that step (3) (4) is formed, COD reaches about 1000mg/L, salinity reaches about 6%, use conventional reverse osmosis membrane module cannot continue to concentrate, therefore the ultra concentration assembly that can simultaneously meet the high COD of tolerance and high salinity operating mode is used to carry out ultra concentration, the high strong brine that step (3) (4) is formed being concentrated decrement further, makes strong brine salinity reach more than 10%, COD reaches more than 2000mg/L.Owing in order to overcome high osmotic pressure, needing the operating pressure higher than conventional strong brine desalination reverse osmosis, operation energy consumption is higher, uses energy recycle device effectively to reduce the operation energy consumption of this ultra concentration device.Ultra concentration device product water produces water quality after water mixes with leading portion strong brine desalination strong brine desalination reverse osmosis unit and reaches to supplement as open type recirculated cooling water about recycled water in country " urban sewage reutilization industry water standard " (GB/T 19923-2005) water standard of water.
As a example by typical case's pending strong brine of Coal Chemical Industry Zero emission device, amount of inlet water 60m3/ h, salinity 1.7%, COD300mg/L, total hardness 1000mg/L, total alkalinity 2000mg/L, after the technique decrement reuse of this membrance concentration, ultimately form super strong brine water yield ＜ 10m3/ h, overall operation 7 yuan/m of cost ＜3。
Seeing Fig. 2, in pretreatment section, strong brine is stored in storage regulating reservoir 101 and carries out water quality and quantity regulation, and storage regulating reservoir outlet is connected with the water inlet of advanced oxidation device 102 by pipeline and regulating reservoir elevator pump 107；Advanced oxidation device 102 is provided with strong oxidizer throwing device 110, adds strong oxidizer and aoxidizes；Advanced oxidation device 102 outlet is connected to react thickener 103 by pipeline, and reaction thickener 103 is provided with softening medicament addition device 111, adds softening agent, makes the calcium and magnesium plasma in water produce precipitate and removes in subsequent handling；Reaction thickener 103 outlet is connected with softening micro-filtration 104 by pipeline；The metal flco such as calcium carbonate, magnesium hydroxide is removed through micro-filtrate membrane filtration in softening micro-filtration 104；Softening micro-filtration 104 water outlet and enter intermediate pool 105 by pipeline and micro-filtration membrane suction pump 108, intermediate pool 105 outlet is connected to membrance concentration workshop section by pipeline.The precipitate softened in micro-filtration 104 is processed to sludge treating block 106 through pumping by mud mouth.
In membrance concentration workshop section, by pipeline and nanofiltration intake pump 211, intermediate pool 106 outlet of pretreatment section is connected to cartridge filter 201, before cartridge filter 201, is provided with scale inhibitor feeding device 223, is used for adding antisludging agent；The outlet of cartridge filter 201 is connected to the water inlet of nanofiltration membrane separation device 202 by pipeline, and waste water is after nanofiltration membrane separation, and float in waste water, divalent ion etc. are removed, and outlet is connected to nanofiltration effluent trough 203 by pipeline；Nanofiltration membrane separation device 202 is provided with chemically-cleaning device 220, when film contaminated serious time, be used for cleaning ultrafilter membrane, cleaning medicinal liquid, to be back to chemically-cleaning device 220 reusable, arranges outside the cleanout fluid of inefficacy；One outlet of nanofiltration effluent trough 203 is connected with the water inlet of feed water by reverse osmosis pump 212 with cartridge filter 204 by pipeline, another outlet cleans pump 217 by pipeline with nanofiltration membrane separation device and is connected with the Butterworth Hatch of nanofiltration membrane separation device 202, its pipeline is provided with sodium hypochlorite throwing device 221 and citric acid throwing device 224, NF membrane can carry out daily cleaning, and the dense water that nanofiltration membrane separation device 202 produces enters reverse osmosis concentrated tank 206；The outlet of cartridge filter 204 is connected with the water inlet of strong brine desalination reverse osmosis unit 205 by pipeline and reverse osmosis high-pressure pump 213, water is after reverse osmosis membrane separation, salt in waste water can be concentrated in dense water, strong brine desalination reverse osmosis unit is provided with scale inhibitor feeding device 223, can add antisludging agent and slow down film fouling；Reverse osmosis produced water is demineralized water, is connected to reuse tank 210 by the clean water outlet of strong brine desalination reverse osmosis unit 205 by pipeline, and dense water is then connected to reverse osmosis concentrated tank 206 by pipeline；The cleaning of strong brine desalination reverse osmosis unit 205 is imported and exported by pipeline export and import with chemically-cleaning device 220 respectively and is connected, and after reverse osmosis membrane is contaminated, can carry out Chemical cleaning.Reverse osmosis concentrated tank 206 is provided with softening agent throwing device 222, can add softening medicament, and the calcium and magnesium plasma in dense water is formed precipitate；The water outlet of reverse osmosis concentrated tank 206 softens feed pump 214 by pipeline and film and enters film softening plant 207, and in film softening plant, the precipitate such as calcium and magnesium is separated removal.The outlet of film softening plant 207 enters ultra concentration intake chamber 208 by pipeline, the outlet of ultra concentration intake chamber 208 is connected with cartridge filter 204 with ultra concentration feed pump 215 by pipeline, cartridge filter 204 outlet is connected with the water inlet of ultra concentration device 209 by pipeline and ultra concentration high-pressure pump 216, ultra concentration device 209 is high pressure reverse osmosis rolled film, in ultra concentration device, by membrance separation, the salinity in dense water concentrates further；The fresh water that ultra concentration device 209 produces is entered reuse tank 210 by the clean water outlet of ultra concentration device by pipeline, and the dope that ultra concentration device 209 produces is connected to evaporated crystallization device 230 by pipeline.The cleaning of ultra concentration device 209 is provided with chemically-cleaning device 220, can carry out Chemical cleaning after film is contaminated.
During aforesaid operations, should be noted and control following parameter:
Pretreatment workshop section: the time of staying of storage regulating tank 101, the chemical feeding quantity of Strong oxdiative throwing device 110 and pH, reaction thickener 103 softens dosage and pH, the concentration of suspension of medicament, softens the membrane flux of micro-filtration 104, membrane area and the turbidity of water outlet, SDI and hardness.
Membrance concentration workshop section: the membrane flux of nanofiltration membrane separation device 202, the membrane flux of strong brine desalination reverse osmosis unit 205, the membrane flux of film softening plant 207, the dosage softening medicament in reverse osmosis concentrated tank 206, the membrane flux of ultra concentration device 209, the membrane flux of above-mentioned various films will have different values with different raw water qualities.Also to control each section of film and go out electrical conductivity of water, kind and consumption, the cleaning frequency etc. of the most various membranization cleaning agents also change with the change of former water.The evaporation capacity of evaporated crystallization device 230, operating temperature and pressure.
Embodiment two:
The present embodiment is identical with embodiment one, except that advanced oxidation can be ozone oxidation (or catalytic ozonation, ozone hydrogen peroxide oxidation).Ultra concentration device 209 can be vibrating diaphragm, high-pressure membrane or forward osmosis membrane.Soften micro-filtration membrane device 104 can be precipitation+submergence decline (surpass) filter, or precipitation+tubular type micro-(surpassing) filter membrane, it is also possible to be traditional medicament softening process, i.e. dosing reaction+precipitation+filtration+ultrafiltration.Crystallizing evaporator 230 can be that multiple-effect evaporation concentrates or mechanical compress evaporation and concentration.Nanofiltration membrane separation device 202 can make Weak-acid cation exchange into, and the supporting auxiliary equipment of nanofiltration system makes the corollary system of ion exchange together into, and film softening plant 207 and the corollary equipment thereof of film processing section saves simultaneously.
Embodiment three:
The present embodiment is identical with embodiment one, except that when in former water, hardness is relatively low, the film softening plant 207 in film treatment process can save.
Claims (5)
- null1. a strong brine zero-emission membrance concentration equipment，Including: soften micro-filtration、Nanofiltration membrane separation device、Strong brine desalination reverse osmosis membrane apparatus、Ultra concentration device、Evaporated crystallization device、Reuse water tank，It is characterized in that described softening micro-filtration front end is provided with a reaction thickener，It is provided with in reaction thickener and adds softening agent device，The outlet of reaction thickener is connected with softening micro-filtration water inlet，The outlet softening micro-filtration is connected with the water inlet of nanofiltration membrane separation device，It is provided with pH value governor motion before softening the outlet of micro-filtration，The outlet of nanofiltration membrane separation device is connected with the water inlet of strong brine desalination reverse osmosis membrane apparatus，The outlet of strong brine desalination reverse osmosis membrane apparatus is connected with the water inlet of ultra concentration device，The outlet of ultra concentration device is connected with reuse water tank，The super brine outlet of ultra concentration device is connected with evaporated crystallization device.
- Strong brine zero-emission membrance concentration equipment the most according to claim 1, it is characterized in that described softening micro-filtration is for softening micro-filtration membrane device, wherein soften micro-filtration membrane and use organic tube type filter membrance, filtering accuracy ＜ 0.1 micron, or use immersed microfiltration film.
- Strong brine zero-emission membrance concentration equipment the most according to claim 1, it is characterised in that the NF membrane of described nanofiltration membrane separation device is to be applicable to the nanofiltration membrane component that carnallite separates and tolerates high chemical oxygen demand, and is multi-stage series structure.
- Strong brine zero-emission membrance concentration equipment the most according to claim 1, it is characterised in that described strong brine desalination reverse osmosis membrane apparatus is to be applicable to the strong brine desalination membrane module that monovalent salt concentrates, and passes through multi-stage series.
- Strong brine zero-emission membrance concentration equipment the most according to claim 1, it is characterised in that described nanofiltration membrane separation device uses Weak-acid cation switch to replace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620035174.6U CN205603386U (en) | 2016-01-14 | 2016-01-14 | Strong brine zero release membrane concentrator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620035174.6U CN205603386U (en) | 2016-01-14 | 2016-01-14 | Strong brine zero release membrane concentrator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205603386U true CN205603386U (en) | 2016-09-28 |
Family
ID=56960991
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620035174.6U Active CN205603386U (en) | 2016-01-14 | 2016-01-14 | Strong brine zero release membrane concentrator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205603386U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106966536A (en) * | 2016-01-14 | 2017-07-21 | 麦王环境技术股份有限公司 | Strong brine zero-emission film concentration technology and equipment |
| CN108249668A (en) * | 2016-12-28 | 2018-07-06 | 麦王环境技术股份有限公司 | Slurrying yellow liquor concentrate and dry Processes and apparatus |
| CN108689540A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Incineration of refuse flyash wastewater zero discharge and recycling unit and treatment process |
| CN108689539A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Dense salt wastewater zero discharge and resources apparatus and treatment process |
| CN108996791A (en) * | 2018-08-03 | 2018-12-14 | 山东和生海洋科技有限公司 | A kind of sea water desalination and comprehensive utilization new process |
| EP3517508A1 (en) * | 2018-09-21 | 2019-07-31 | SUEZ Groupe | Zero liquid discharge treatment process for recovering water from a contaminated liquid effluent for its subsequent reuse |
-
2016
- 2016-01-14 CN CN201620035174.6U patent/CN205603386U/en active Active
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106966536A (en) * | 2016-01-14 | 2017-07-21 | 麦王环境技术股份有限公司 | Strong brine zero-emission film concentration technology and equipment |
| CN108249668A (en) * | 2016-12-28 | 2018-07-06 | 麦王环境技术股份有限公司 | Slurrying yellow liquor concentrate and dry Processes and apparatus |
| CN108689540A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Incineration of refuse flyash wastewater zero discharge and recycling unit and treatment process |
| CN108689539A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Dense salt wastewater zero discharge and resources apparatus and treatment process |
| CN108996791A (en) * | 2018-08-03 | 2018-12-14 | 山东和生海洋科技有限公司 | A kind of sea water desalination and comprehensive utilization new process |
| CN108996791B (en) * | 2018-08-03 | 2021-02-12 | 山东和生海洋科技有限公司 | Novel process for seawater desalination and comprehensive utilization |
| EP3517508A1 (en) * | 2018-09-21 | 2019-07-31 | SUEZ Groupe | Zero liquid discharge treatment process for recovering water from a contaminated liquid effluent for its subsequent reuse |
| ES2754898R1 (en) * | 2018-09-21 | 2020-04-27 | Suez Groupe | Zero liquid discharge treatment process to recover water from a contaminated liquid effluent for later reuse |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN205603386U (en) | Strong brine zero release membrane concentrator | |
| CN105000737B (en) | A kind of Industrial sewage treatment system and sewage water treatment method | |
| CN108249646A (en) | Can resource recycling power plant desulfurization wastewater Zero-discharge treating process and device | |
| CN108218087B (en) | System for treating high-salt-content wastewater based on multistage electrically-driven ionic membrane | |
| CN106966536A (en) | Strong brine zero-emission film concentration technology and equipment | |
| CN106966535A (en) | Strong brine zero-emission film is concentrated and sub-prime crystallization processes and equipment | |
| CN103979729A (en) | Desulfurization waste water recycling and zero discharge system and method | |
| CN205603387U (en) | Strong brine zero release divides membrane concentrator of matter crystallization | |
| CN105236659A (en) | Nanofiltration treatment method of desulfurization waste water | |
| CN104176857B (en) | The treatment process of Mn-bearing waste water in wet method electrolysis manganese production process | |
| CN107915360A (en) | Zero-emission crystallization divides salt device and technique | |
| CN105084587A (en) | Treatment method and equipment of high-salt waste water | |
| CN205011545U (en) | Desulfurization waste water resourceful treatment device | |
| CN208120896U (en) | Can resource recycling power plant desulfurization wastewater zero discharge treatment device | |
| CN110526512A (en) | A kind of high-COD waste water with high salt recycling Zero discharging system and technique | |
| CN105439341A (en) | Salt-containing wastewater treatment system and treatment method | |
| CN107840511A (en) | Coal chemical industry method for treating strong brine and system | |
| CN108658345A (en) | A kind of method and system of high-salt wastewater purified salt | |
| CN205603385U (en) | Concentrated and branch matter crystallization equipment of strong brine zero release membrane | |
| CN108793517A (en) | A kind for the treatment of process of high COD leather-making waste waters with high salt | |
| CN111170524A (en) | Reverse osmosis concentrated water recycling method | |
| CN110937728A (en) | Desulfurization wastewater treatment method and system | |
| CN105198141A (en) | High-temperature high-salinity wastewater zero-discharging method | |
| CN205575837U (en) | Processing system of lime stone / lime - gypsum method flue gas desulfurization waste water | |
| CN111170519A (en) | Treatment process and treatment system for desulfurization wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 200000, 4th floor, Block A, Oriental Fisherman's Wharf, 1088 Yangshupu Road, Yangpu District, Shanghai Patentee after: Mai Wang Environmental Technology Co.,Ltd. Country or region after: China Address before: 200135, room 1001, golden peach mansion, 1900 Shangcheng Road, Shanghai, Pudong New Area Patentee before: MCWONG ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Country or region before: China |
|
| CP03 | Change of name, title or address |