CN103910457A - Device and method for treating and recycling salt-containing wastewater in industrial estates - Google Patents
Device and method for treating and recycling salt-containing wastewater in industrial estates Download PDFInfo
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- CN103910457A CN103910457A CN201410148812.0A CN201410148812A CN103910457A CN 103910457 A CN103910457 A CN 103910457A CN 201410148812 A CN201410148812 A CN 201410148812A CN 103910457 A CN103910457 A CN 103910457A
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- reverse osmosis
- osmosis membrane
- high pressure
- membrane system
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Links
- 238000000034 method Methods 0.000 title claims abstract description 17
- 150000003839 salts Chemical class 0.000 title claims abstract description 9
- 239000002351 wastewater Substances 0.000 title abstract description 5
- 238000004064 recycling Methods 0.000 title abstract 3
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 148
- 239000012528 membrane Substances 0.000 claims abstract description 122
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 claims abstract description 35
- 229910052939 potassium sulfate Inorganic materials 0.000 claims abstract description 35
- 235000011151 potassium sulphates Nutrition 0.000 claims abstract description 35
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 17
- 239000003814 drug Substances 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 238000005342 ion exchange Methods 0.000 claims abstract description 4
- 238000001728 nano-filtration Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 131
- 238000005096 rolling process Methods 0.000 claims description 53
- 239000000047 product Substances 0.000 claims description 39
- 239000007788 liquid Substances 0.000 claims description 30
- 239000012267 brine Substances 0.000 claims description 23
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 23
- 239000002699 waste material Substances 0.000 claims description 23
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 18
- 150000002500 ions Chemical class 0.000 claims description 18
- 238000002425 crystallisation Methods 0.000 claims description 15
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 12
- 239000003456 ion exchange resin Substances 0.000 claims description 12
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 12
- 230000008025 crystallization Effects 0.000 claims description 9
- 239000013535 sea water Substances 0.000 claims description 9
- 239000011780 sodium chloride Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 8
- 230000008020 evaporation Effects 0.000 claims description 8
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 claims description 6
- 239000013078 crystal Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 239000002244 precipitate Substances 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- -1 react 10 minutes Substances 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 3
- 235000011152 sodium sulphate Nutrition 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 230000007246 mechanism Effects 0.000 claims 1
- 230000000903 blocking effect Effects 0.000 abstract 1
- 238000007670 refining Methods 0.000 abstract 1
- 238000004062 sedimentation Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 9
- 239000006227 byproduct Substances 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000008521 reorganization Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a device for treating and recycling salt-containing wastewater. The device comprises an adjusting pool, a softening sedimentation tank, a medicament storage box, a multi-medium filter, an ultrafiltration device, a first segment of roll-type reverse osmosis system, a second segment of roll-type reverse osmosis system, an ion exchange device, a roll-type nanofiltration membrane device, a high pressure reverse osmosis membrane system, an efficient evaporator and a potassium sulfate conversion refining groove. The device and the method disclosed by the invention are strong in anti-pollution capacity, capable of solving the blocking problem, high in concentration multiple, high in recycling efficiency, high in treatment efficiency, high in automation degree, capable of saving investment and low in operation cost.
Description
Technical field
The treatment unit and the method that the present invention relates to a kind of industrial park brine waste, belong to the water treatment field in environment protection.
Background technology
Current, the processing of chemical industrial park brine waste, can adopt two schemes: traditional technology, improved technology substantially.
Traditional technology: adopt traditional more medium filter+ultrafiltration+two section rolling reverse osmosis+evaporation pond technique.One section of coiled reverse osmosis membrane system of actual employing in some projects.This traditional technology, system recoveries rate is in 80%, and producing dense water needs big area evaporation pond.
Shortcoming: investment is large, takes up an area greatly, and running cost is large, larger to environment negative impact;
Improved technology: being the advanced technologies of just having risen at home at present, is to have increased high pressure reverse osmosis system in two sections of coiled reverse osmosis membrane system-based, joins afterwards evaporation pond.On the basis of traditional scheme, this programme evaporation pond area reduces to some extent.
Advantage: the advance possessing skills, easy and simple to handle, steam output reduces.
Shortcoming: save than traditional technology investment, but still larger, take up an area minimizing but still larger, running cost is larger, and to environment, negative impact reduces a little, but there is no essential distinction.
Zero discharge of industrial waste water is the policy that meets strict environmental requirement, in brine waste process field, be badly in need of a kind of contamination resistance strong, solve blockage problem, cycles of concentration is high, reuse efficiency is high, processing efficiency is high, reduced investment, the treatment process that running cost is low and equipment.
Summary of the invention
The problem existing for prior art, the invention provides a kind for the treatment of unit of brine waste, comprise equalizing tank, softening settling tank, medicament torage tank, more medium filter, ultra-filtration equipment, first paragraph rolling reverse osmosis system, second segment rolling reverse osmosis system, ion exchange unit, rolling nano filter membrance device, high pressure reverse osmosis membrane system, high-efficiency evaporator, brine waste outfall pipeline connects equalizing tank entrance, equalizing tank outlet connects softening settling tank entrance by pipeline, the dosing mouth of medicament torage tank passes into softening settling tank, softening settling tank supernatant liquor outlet connects the entrance of more medium filter by pipeline, the outlet of more medium filter is connected ultra-filtration equipment by pipeline with high-pressure pump, the outlet of ultra-filtration equipment is connected first paragraph rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of first paragraph rolling reverse osmosis system is connected the entrance of second segment rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of second segment rolling reverse osmosis system connects the entrance of ion exchange resin by pipeline, the product water out of first and second section of rolling reverse osmosis system is connected and produced water reclaiming system by pipeline, the outlet of ion exchange resin is connected the entrance of leading portion high pressure reverse osmosis membrane system with high-pressure pump by pipeline, the dense water out of leading portion high pressure reverse osmosis membrane system is connected the entrance of rolling nano filter membrance device with high-pressure pump by pipeline, the product water out of leading portion high pressure reverse osmosis membrane system is connected and produced water reclaiming system by pipeline, the monovalent ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 2 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 2 connects the entrance of second segment high pressure reverse osmosis membrane system 2 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 2 connects high-efficiency evaporator by pipeline, evaporative crystallization goes out monovalence Industrial Salt, and the product water out of first paragraph high pressure reverse osmosis membrane system 2, the product water out of second segment high pressure reverse osmosis membrane system 2 are connected and produced water reclaiming system by pipeline, the high valence ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 1 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 1 connects the entrance of second segment high pressure reverse osmosis membrane system 1 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 1 connects first paragraph potassium sulfate by pipeline and transforms refinery pit, the 3K wherein separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate and is transformed in refinery pit, crystallization goes out agricultural potassium sulfate, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outlet access second segment high pressure reverse osmosis membrane system 2 of refinery pit, and the product water out of first paragraph high pressure reverse osmosis membrane system 1, second segment high pressure reverse osmosis membrane system 1 is connected and produced water reclaiming system by pipeline.
In softening settling tank, agitator being set makes medicament fully mix with water.
The present invention also provides a kind of method that uses the treatment unit of above-mentioned brine waste to process brine waste, comprises the steps:
(1) brine waste enters equalizing tank by pipeline and carries out entering after simple modulation softening settling tank, first add liming reaction 10 minutes to softening settling tank, precipitate 30 minutes, add again sodium carbonate, react 10 minutes, precipitate 30 minutes, then acid adding regulates below PH to 6.5, and supernatant liquor flows into more medium filter;
(2) enter ultra-filtration equipment through the preliminary liquid stream filtering of more medium filter by high-pressure pump, the liquid stream filtering through ultra-filtration membrane device enters first paragraph rolling reverse osmosis system by high-pressure pump;
(3) concentrated stream of first paragraph rolling reverse osmosis system enters by high-pressure pump to enter second segment rolling reverse osmosis system, produces water and enters product water reclaiming system;
(4) concentrated stream of second segment rolling reverse osmosis system enters into ion exchange resin, produces water and enters product water reclaiming system;
(5) ion exchange resin is set, useless water hardness is further removed, liquid stream enters leading portion high pressure reverse osmosis membrane system by high-pressure pump afterwards;
(6) concentrated stream of leading portion high pressure reverse osmosis membrane system enters into rolling nanofiltration membrane, produces water and enters product water reclaiming system;
(7) liquid stream is divided into monovalent ion liquid stream and high valence ion liquid stream in rolling nano filter membrance device; Monovalent ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 2 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 2, produces water and enters product water reclaiming system; High valence ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 1 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 1, produces water and enters product water reclaiming system;
(8) in the dense water that second segment high pressure reverse osmosis membrane system 1 produces, contain a large amount of sodium sulfate, enter first paragraph potassium sulfate and transform in refinery pit, add wherein Repone K, generate 3K
2sO
4na
2sO
4and sodium-chlor, filter the 3K separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate conversion refinery pit and is reacted with the Repone K that continues to add, generate potassium sulfate and sodium-chlor, crystallization potassium sulfate crystal, potassium sulfate crystal is after washing, obtain meeting the potassium sulfate of agricultural first grade, and recycle, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outflow remittance second segment high pressure reverse osmosis membrane system 2 in refinery pit; The product water that second segment high pressure reverse osmosis membrane system 1 produces enters and produces water reclaiming system;
(9) the dense water that second segment high pressure reverse osmosis membrane system 2 produces and the sodium chloride solution of remittance enter high-efficiency evaporator, produce monovalence Industrial Salt through concentration and evaporation, and recycle, and produce water and enter product water reclaiming system.
The maximum 120bar of first paragraph high pressure reverse osmosis membrane system 1 working pressure, the maximum 75bar of first paragraph high pressure reverse osmosis membrane system 2 working pressures, the maximum 160bar of second segment high pressure reverse osmosis membrane system 1 working pressure, the maximum 120bar of second segment high pressure reverse osmosis membrane system 2 working pressures.
In the time of SDI≤5 that enter liquid stream of first paragraph high pressure reverse osmosis membrane system 2, first paragraph high pressure reverse osmosis membrane system 2 is substituted by sea water desaltination film system, SDI≤5 o'clock that enter liquid stream of present segment high pressure reverse osmosis membrane system, leading portion high pressure reverse osmosis membrane system is substituted by sea water desaltination film system, the highest 80bar of working pressure of sea water desaltination film system.
The TDS < 500mg/L of the product water of final reuse, reuse water production rate accounts for 97% of brine waste inlet.
The present invention has following advantage compared with prior art:
(1) contamination resistance is strong, solves blockage problem
Design for processing high density high pollution waste water specially, allow influent quality fluctuation range large, high voltage type reverse osmosis membrane water inlet SDI can, up to 6.5, simplify pre-treatment, reduces investment, even the in the situation that of high turbidity water inlet, flux decline is still less.Unique structure, has solved the dirty stifled and scale problems of diaphragm; Cleaning interval is long, and membrane flux is restorative good.
(2) cycles of concentration is high, and reuse efficiency is high
High pressure reverse osmosis membrane (high-pressure membrane) technology is on traditional rolled film element, carry out bold innovation, it is the membrane element form of a kind of uniqueness in current membrane sepn field, its unique design makes operating pressure be up to 200bar, can tolerate the brine waste of greater concn, this is the working pressure that existing rolled film all can not be promised to undertake; Rolling reverse osmosis and high-pressure membrane are used in conjunction with, and Waste water concentrating multiple is very high, can be up to arriving 40-50 doubly.
(3) high rejection, stable and reliable operation
High precision film all has high clearance to every pollutent, and one-level just can be held back COD and be greater than 96%, and ammonia nitrogen is greater than 93%, and salt is greater than 97-99%; Secondary is all greater than 99.5-99.99%, and system effluent quality is highly stable.
(4) running cost is low, and byproduct output is worth high
Waste water reclamation rate is high, reaches 97%, and evaporation pond investment reduces greatly; When running cost reduces, processing water outlet can reuse, realizes closed cycle, reaches real zero release.Whole system can be produced the agricultural one-level potassium sulfate of byproduct one simultaneously, and output is high, and added value is high, has further reduced running cost
(5) modular design, flexible operation
As physical sepn equipment, and through modular design, the system operation of high voltage type film is flexible, can be continuously or intermittent operation, and the series-parallel system of capable of regulating system, adapts to water quality and quantity requirement.Follow-up reorganization and expansion is easy.
(6) level of automation is high, and operation operation is easy
Whole system is full rotation type, and whole system is provided with perfect monitoring, Controlling System, and PLC can regulate automatically according to sensor parameters, sends guard signal in good time, and system is formed to protection.
Brief description of the drawings
Fig. 1 is the treatment unit of the embodiment of the present invention and the schematic diagram of method.
Embodiment
Be introduced taking industry park brine waste processing project as embodiment below.
Comprise equalizing tank, softening settling tank, medicament torage tank, more medium filter, ultra-filtration equipment, first paragraph rolling reverse osmosis system, second segment rolling reverse osmosis system, ion exchange unit, rolling nano filter membrance device, high pressure reverse osmosis membrane system, high-efficiency evaporator, brine waste outfall pipeline connects equalizing tank entrance, equalizing tank outlet connects softening settling tank entrance by pipeline, the dosing mouth of medicament torage tank passes into softening settling tank, softening settling tank supernatant liquor outlet connects the entrance of more medium filter by pipeline, the outlet of more medium filter is connected ultra-filtration equipment by pipeline with high-pressure pump, the outlet of ultra-filtration equipment is connected first paragraph rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of first paragraph rolling reverse osmosis system is connected the entrance of second segment rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of second segment rolling reverse osmosis system connects the entrance of ion exchange resin by pipeline, the product water out of first and second section of rolling reverse osmosis system is connected and produced water reclaiming system by pipeline, the outlet of ion exchange resin is connected the entrance of leading portion high pressure reverse osmosis membrane system with high-pressure pump by pipeline, the dense water out of leading portion high pressure reverse osmosis membrane system is connected the entrance of rolling nano filter membrance device with high-pressure pump by pipeline, the product water out of leading portion high pressure reverse osmosis membrane system is connected and produced water reclaiming system by pipeline, the monovalent ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 2 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 2 connects the entrance of second segment high pressure reverse osmosis membrane system 2 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 2 connects high-efficiency evaporator by pipeline, evaporative crystallization goes out monovalence Industrial Salt, and the product water out of first paragraph high pressure reverse osmosis membrane system 2, the product water out of second segment high pressure reverse osmosis membrane system 2 are connected and produced water reclaiming system by pipeline, the high valence ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 1 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 1 connects the entrance of second segment high pressure reverse osmosis membrane system 1 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 1 connects first paragraph potassium sulfate by pipeline and transforms refinery pit, the 3K wherein separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate and is transformed in refinery pit, crystallization goes out agricultural potassium sulfate, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outlet access second segment high pressure reverse osmosis membrane system 2 of refinery pit, and the product water out of first paragraph high pressure reverse osmosis membrane system 1, second segment high pressure reverse osmosis membrane system 1 is connected and produced water reclaiming system by pipeline.
Garden uses above-mentioned treatment unit to process the method for brine waste, comprises the steps:
(1) brine waste enters equalizing tank by pipeline and carries out entering after simple modulation softening settling tank, first add liming reaction 10 minutes to softening settling tank, precipitate 30 minutes, add again sodium carbonate, react 10 minutes, precipitate 30 minutes, then acid adding regulates below PH to 6.5, and supernatant liquor flows into more medium filter;
(2) enter ultra-filtration equipment through the preliminary liquid stream filtering of more medium filter by high-pressure pump, the liquid stream filtering through ultra-filtration membrane device enters first paragraph rolling reverse osmosis system by high-pressure pump;
(3) concentrated stream of first paragraph rolling reverse osmosis system enters by high-pressure pump to enter second segment rolling reverse osmosis system, produces water and enters product water reclaiming system;
(4) concentrated stream of second segment rolling reverse osmosis system enters into ion exchange resin, produces water and enters product water reclaiming system;
(5) ion exchange resin is set, useless water hardness is further removed, liquid stream enters leading portion high pressure reverse osmosis membrane system by high-pressure pump afterwards;
(6) concentrated stream of leading portion high pressure reverse osmosis membrane system enters into rolling nanofiltration membrane, produces water and enters product water reclaiming system;
(7) liquid stream is divided into monovalent ion liquid stream and high valence ion liquid stream in rolling nano filter membrance device; Monovalent ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 2 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 2, produces water and enters product water reclaiming system; High valence ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 1 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 1, produces water and enters product water reclaiming system;
(8) in the dense water that second segment high pressure reverse osmosis membrane system 1 produces, contain a large amount of sodium sulfate, enter first paragraph potassium sulfate and transform in refinery pit, add wherein Repone K, generate 3K
2sO
4na
2sO
4and sodium-chlor, filter the 3K separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate conversion refinery pit and is reacted with the Repone K that continues to add, generate potassium sulfate and sodium-chlor, crystallization potassium sulfate crystal, potassium sulfate crystal is after washing, obtain meeting the potassium sulfate of agricultural first grade, and recycle, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outflow remittance second segment high pressure reverse osmosis membrane system 2 in refinery pit; The product water that second segment high pressure reverse osmosis membrane system 1 produces enters and produces water reclaiming system;
(9) the dense water that second segment high pressure reverse osmosis membrane system 2 produces and the sodium chloride solution of remittance enter high-efficiency evaporator, produce monovalence Industrial Salt through concentration and evaporation, and recycle, and produce water and enter product water reclaiming system.
First paragraph high pressure reverse osmosis membrane system 1 working pressure is 120bar, first paragraph high pressure reverse osmosis membrane system 2 working pressures are 75bar, second segment high pressure reverse osmosis membrane system 1 working pressure is 160bar, and second segment high pressure reverse osmosis membrane system 2 working pressures are 120bar.
In the time of SDI≤5 that enter liquid stream of first paragraph high pressure reverse osmosis membrane system 2, first paragraph high pressure reverse osmosis membrane system 2 is substituted by sea water desaltination film system, SDI≤5 o'clock that enter liquid stream of present segment high pressure reverse osmosis membrane system, leading portion high pressure reverse osmosis membrane system is substituted by sea water desaltination film system, and the working pressure of sea water desaltination film system is 80bar.
The TDS < 500mg/L of the product water of final reuse, reuse water production rate accounts for 97% of brine waste inlet.
Claims (6)
1. the processing reclamation set of a brine waste, comprise equalizing tank, softening settling tank, medicament torage tank, more medium filter, ultra-filtration equipment, first paragraph rolling reverse osmosis system, second segment rolling reverse osmosis system, ion exchange unit, rolling nano filter membrance device, high pressure reverse osmosis membrane system, high-efficiency evaporator, it is characterized in that: brine waste outfall pipeline connects equalizing tank entrance, equalizing tank outlet connects softening settling tank entrance by pipeline, the dosing mouth of medicament torage tank passes into softening settling tank, softening settling tank supernatant liquor outlet connects the entrance of more medium filter by pipeline, the outlet of more medium filter is connected ultra-filtration equipment by pipeline with high-pressure pump, the outlet of ultra-filtration equipment is connected first paragraph rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of first paragraph rolling reverse osmosis system is connected the entrance of second segment rolling reverse osmosis system with high-pressure pump by pipeline, the dense water out of second segment rolling reverse osmosis system connects the entrance of ion exchange resin by pipeline, the product water out of first and second section of rolling reverse osmosis system is connected and produced water reclaiming system by pipeline, the outlet of ion exchange resin is connected the entrance of leading portion high pressure reverse osmosis membrane system with high-pressure pump by pipeline, the dense water out of leading portion high pressure reverse osmosis membrane system is connected the entrance of rolling nano filter membrance device with high-pressure pump by pipeline, the product water out of leading portion high pressure reverse osmosis membrane system is connected and produced water reclaiming system by pipeline, the monovalent ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 2 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 2 connects the entrance of second segment high pressure reverse osmosis membrane system 2 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 2 connects high-efficiency evaporator by pipeline, evaporative crystallization goes out monovalence Industrial Salt, and the product water out of first paragraph high pressure reverse osmosis membrane system 2, the product water out of second segment high pressure reverse osmosis membrane system 2 are connected and produced water reclaiming system by pipeline, the high valence ion water export of rolling nano filter membrance device is connected the entrance of first paragraph high pressure reverse osmosis membrane system 1 with high-pressure pump by pipeline, the dense water out of first paragraph high pressure reverse osmosis membrane system 1 connects the entrance of second segment high pressure reverse osmosis membrane system 1 by pipeline, the dense water out of second segment high pressure reverse osmosis membrane system 1 connects first paragraph potassium sulfate by pipeline and transforms refinery pit, the 3K wherein separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate and is transformed in refinery pit, crystallization goes out agricultural potassium sulfate, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outlet access second segment high pressure reverse osmosis membrane system 2 of refinery pit, and the product water out of first paragraph high pressure reverse osmosis membrane system 1, second segment high pressure reverse osmosis membrane system 1 is connected and produced water reclaiming system by pipeline.
2. the processing reclamation set of brine waste as claimed in claim 1, is characterized in that, in softening settling tank, the mechanisms such as agitator is set medicament is fully mixed with water.
3. right to use requires the processing reclamation set of the arbitrary described brine waste of 1-2 to process a method for brine waste, it is characterized in that comprising the steps:
(1) brine waste enters equalizing tank by pipeline and carries out entering after simple modulation softening settling tank, first add liming reaction 10 minutes to softening settling tank, precipitate 30 minutes, add again sodium carbonate, react 10 minutes, precipitate 30 minutes, then acid adding regulates below PH to 6.5, and supernatant liquor flows into more medium filter;
(2) enter ultra-filtration equipment through the preliminary liquid stream filtering of more medium filter by high-pressure pump, the liquid stream filtering through ultra-filtration membrane device enters first paragraph rolling reverse osmosis system by high-pressure pump;
(3) concentrated stream of first paragraph rolling reverse osmosis system enters by high-pressure pump to enter second segment rolling reverse osmosis system, produces water and enters product water reclaiming system;
(4) concentrated stream of second segment rolling reverse osmosis system enters into ion exchange resin, produces water and enters product water reclaiming system;
(5) ion exchange resin is set, useless water hardness is further removed, liquid stream enters leading portion high pressure reverse osmosis membrane system by high-pressure pump afterwards;
(6) concentrated stream of leading portion high pressure reverse osmosis membrane system enters into rolling nanofiltration membrane, produces water and enters product water reclaiming system;
(7) liquid stream is divided into monovalent ion liquid stream and high valence ion liquid stream in rolling nano filter membrance device; Monovalent ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 2 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 2, produces water and enters product water reclaiming system; High valence ion liquid stream enters first paragraph high pressure reverse osmosis membrane system 1 by high-pressure pump, and the dense water of generation enters second segment high pressure reverse osmosis membrane system 1, produces water and enters product water reclaiming system;
(8) in the dense water that second segment high pressure reverse osmosis membrane system 1 produces, contain a large amount of sodium sulfate, enter first paragraph potassium sulfate and transform in refinery pit, add wherein Repone K, generate 3K
2sO
4na
2sO
4and sodium-chlor, filter the 3K separating out
2sO
4na
2sO
4crystallization is thrown in second segment potassium sulfate conversion refinery pit and is reacted with the Repone K that continues to add, generate potassium sulfate and sodium-chlor, crystallization potassium sulfate crystal, potassium sulfate crystal is after washing, obtain meeting the potassium sulfate of agricultural first grade, and recycle, two sections of potassium sulfate transform the dense water out of the sodium chloride solution outflow remittance second segment high pressure reverse osmosis membrane system 2 in refinery pit; The product water that second segment high pressure reverse osmosis membrane system 1 produces enters and produces water reclaiming system;
(9) the dense water that second segment high pressure reverse osmosis membrane system 2 produces and the sodium chloride solution of remittance enter high-efficiency evaporator, produce monovalence Industrial Salt through concentration and evaporation, and recycle, and produce water and enter product water reclaiming system.
4. a method as claimed in claim 3, it is characterized in that, the maximum 120bar of first paragraph high pressure reverse osmosis membrane system 1 working pressure, the maximum 75bar of first paragraph high pressure reverse osmosis membrane system 2 working pressures, the maximum 160bar of second segment high pressure reverse osmosis membrane system 1 working pressure, the maximum 120bar of second segment high pressure reverse osmosis membrane system 2 working pressures.
5. a method as claimed in claim 3, it is characterized in that, in the time of SDI≤5 that enter liquid stream of first paragraph high pressure reverse osmosis membrane system 2, first paragraph high pressure reverse osmosis membrane system 2 is substituted by sea water desaltination film system, SDI≤5 o'clock that enter liquid stream of present segment high pressure reverse osmosis membrane system, leading portion high pressure reverse osmosis membrane system is substituted by sea water desaltination film system, the highest 80bar of working pressure of sea water desaltination film system.
6. a method as claimed in claim 3, is characterized in that, the TDS < 500mg/L of the product water of final reuse, and reuse water production rate accounts for 97% of brine waste inlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410148812.0A CN103910457B (en) | 2014-04-15 | 2014-04-15 | The treatment for reuse apparatus and method of a kind of industrial park brine waste |
Applications Claiming Priority (1)
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| CN104787951A (en) * | 2014-12-22 | 2015-07-22 | 内蒙古久科康瑞环保科技有限公司 | A treatment system for high-salt waste water |
| CN105502782A (en) * | 2015-12-07 | 2016-04-20 | 湖南湘牛环保实业有限公司 | Technology for recovering water resources and salt from coking wastewater in coal chemical industry |
| CN105906129A (en) * | 2016-06-12 | 2016-08-31 | 鲁西化工集团股份有限公司 | Method for reutilization of water resources and transformation and utilization of salt in waste water |
| CN106006681A (en) * | 2016-05-18 | 2016-10-12 | 化工部长沙设计研究院 | Method for resourceful treatment of high-salt wastewater |
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| CN109437445A (en) * | 2019-01-02 | 2019-03-08 | 利尔化学股份有限公司 | The method that high-salt wastewater recycling recycles |
| CN109650601A (en) * | 2019-01-31 | 2019-04-19 | 湖北金润德环保技术有限公司 | A kind of Copper making sulfuric acid acid water Zero discharge treatment method |
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| CN104787951A (en) * | 2014-12-22 | 2015-07-22 | 内蒙古久科康瑞环保科技有限公司 | A treatment system for high-salt waste water |
| CN105502782A (en) * | 2015-12-07 | 2016-04-20 | 湖南湘牛环保实业有限公司 | Technology for recovering water resources and salt from coking wastewater in coal chemical industry |
| CN105502782B (en) * | 2015-12-07 | 2019-09-27 | 湖南湘牛环保实业有限公司 | A kind of coal chemical industry coking wastewater water resource and salt recovery process |
| CN106006681A (en) * | 2016-05-18 | 2016-10-12 | 化工部长沙设计研究院 | Method for resourceful treatment of high-salt wastewater |
| CN105906129A (en) * | 2016-06-12 | 2016-08-31 | 鲁西化工集团股份有限公司 | Method for reutilization of water resources and transformation and utilization of salt in waste water |
| CN106082516A (en) * | 2016-07-12 | 2016-11-09 | 中国石油集团东北炼化工程有限公司吉林设计院 | A kind of point of salt-pepper noise technique and device |
| CN106082516B (en) * | 2016-07-12 | 2020-02-11 | 中国石油集团东北炼化工程有限公司吉林设计院 | Salt separation crystallization process and device |
| CN106277534A (en) * | 2016-09-23 | 2017-01-04 | 江苏瑞达环保科技有限公司 | The processing means of a kind of low concentration brine waste and technique |
| CN108117213A (en) * | 2017-12-18 | 2018-06-05 | 天津膜天膜科技股份有限公司 | A kind of metal Copper making waste discharge recovery process |
| CN109437445A (en) * | 2019-01-02 | 2019-03-08 | 利尔化学股份有限公司 | The method that high-salt wastewater recycling recycles |
| CN109437445B (en) * | 2019-01-02 | 2022-03-15 | 利尔化学股份有限公司 | Method for recycling high-salinity wastewater |
| CN109650601A (en) * | 2019-01-31 | 2019-04-19 | 湖北金润德环保技术有限公司 | A kind of Copper making sulfuric acid acid water Zero discharge treatment method |
| CN109650601B (en) * | 2019-01-31 | 2021-11-12 | 湖北金润德环保技术有限公司 | Copper smelting sulfuric acid waste acid wastewater zero-discharge treatment method |
| CN114075008A (en) * | 2021-11-19 | 2022-02-22 | 苏州金渠环保科技有限公司 | Chemical wastewater recycling treatment method |
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