CN105060576A - Combined membrane treatment process applied to high-salinity industrial wastewater - Google Patents
Combined membrane treatment process applied to high-salinity industrial wastewater Download PDFInfo
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- CN105060576A CN105060576A CN201510442045.9A CN201510442045A CN105060576A CN 105060576 A CN105060576 A CN 105060576A CN 201510442045 A CN201510442045 A CN 201510442045A CN 105060576 A CN105060576 A CN 105060576A
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Abstract
The invention belongs to the field of industrial wastewater treatment. The invention discloses a combined membrane treatment process applied to high-salinity industrial wastewater. The combined membrane treatment process comprises: carrying out softening treatment on the high-salinity industrial wastewater, and respectively introducing the high-salinity industrial wastewater, which is subjected to the softening treatment, into a high-pressure reverse osmosis device and an electrodialysis device; introducing a concentrated solution which is treated by the high-pressure reverse osmosis device into the electrodialysis device to concentrate; introducing outlet fresh water which is treated by the electrodialysis device into a low-pressure reverse osmosis device, and feeding an outlet concentrated solution to an evaporation system; converging the concentrated solution which is treated by the low-pressure reverse osmosis device with high-salinity industrial wastewater which is subjected to the softening treatment to obtain a mixture, and then introducing the mixture into the electrodialysis device; and taking outlet fresh water of the low-pressure reverse osmosis device and the high-pressure reverse osmosis device as recycled producing water. According to the combined membrane treatment process, flow of the high-salinity industrial wastewater which enters the high-pressure reverse osmosis device and the electrodialysis device is reasonably distributed, and the high-salinity industrial wastewater is separated and concentrated simultaneously; compared with the previous process, the combined membrane treatment process is low in project cost and low in operation cost; and by virtue of low-pressure reverse osmosis, electrodialysis fresh water is separated and recycled, so that the quality of the recycled producing water is improved, and the recovery rate of the recycled producing water is increased.
Description
Technical field
The invention belongs to Industrial Waste Water Treatments field, especially relate to the high salinity waste water film combined treatment process of less energy-consumption, low cost and zero release.
Background technology
Known evaporation technique is the effective technology realizing wastewater zero discharge, but evaporative process belongs to phase transition process, and greatly, working cost is high for consumption quantity of steam or current consumption.Adopt single membrane separating method, there is concentration should not be too high, and fouling membrane fouling is serious, and adopts disc tube reverse osmosis (dt-ro) film cost high.Simple employing electrodialysis is not only invested greatly, application fee is high, and there is reuse water and cannot meet up-to-date discharging standards.Just permeating and belonging to new technology in wastewater application, but complex process, technology are immature and energy consumption is higher.
At present, to realize zero-discharge technology Application comparison extensive for film combined treatment high salinity waste water.But the inadequate system of integrated artistic, the rate of recovery is not high, and product water quality is low, and energy consumption is high.Such as ZL201110225251.6 introduces a kind of calcium chloride wastewater process and reuse method, pretreated waste water is all entered electrodialysis to concentrate, concentrated solution enters evaporation equipment, and fresh water is by common reverse osmosis produced Water circulation, it is large that the electrodialysis that technological process is simple concentrates energy consumption, changes film cost intensive., there is the problems such as large, that fouling membrane fouling and reuse easily the occur fresh water quality of reverse osmosis membrane operating load is not high in the high salinity zero discharge of industrial waste water technique separately having ZL201310311089.9 to introduce.
Therefore, from cleaner production, watering balance, resource reclaim angle system analysis combination membrane process feature, the comprehensive treating process of high salinity trade effluent is made to have good social and economic effects.
Summary of the invention
The object of the invention is for above-mentioned present situation, aim to provide the high salinity waste water film combined treatment process of less energy-consumption, low cost, zero release, realize the fresh water reuse of high-quality, high-recovery simultaneously.
For achieving the above object, the invention provides following technical scheme:
Be applied to a film combined treatment process for high salinity trade effluent, described film combined treatment process comprises the following steps:
(1) softening process process is carried out to high salinity trade effluent;
(2) the high salinity trade effluent after softening one enter high pressure reverse osmosis unit, another stock enters electrodialysis unit; Enter the high salinity trade effluent of high pressure reverse osmosis unit after reverse-osmosis treated, fresh water produces water as reuse, and concentrated solution enters electrodialysis unit; Enter the high salinity trade effluent of electrodialysis unit after concentration, outlet fresh water enters low pressure reverse osmosis device, and outlet concentrated solution is delivered to vapo(u)rization system and carried out salinity recovery; Enter the fresh water of low pressure reverse osmosis device after reverse-osmosis treated, outlet fresh water produces water as reuse, enters electrodialysis unit after the high salinity trade effluent exported after concentrated solution and sofening treatment converges.
Further, the flow entering the high salinity trade effluent of high pressure reverse osmosis unit is the 35-45% of high salinity trade effluent total flux.
Further, the described high salinity trade effluent entering high pressure reverse osmosis unit is divided into two strands, one passes into in high pressure reverse osmosis unit, another stock-traders' know-how crosses the dump energy that energy recycle device reclaims the concentrated solution of output from high pressure reverse osmosis unit, then converge with one high salinity trade effluent before and enter high pressure reverse osmosis unit, described energy recycle device is one-level one section or one-level multistage.
Further, two strands arrange the first high-pressure pump and the second high-pressure pump respectively without energy recycle device with on the high salinity trade effluent process pipe entering high pressure reverse osmosis unit of energy recycle device, and described second high-pressure pump is arranged on the downstream direction of energy recycle device.
Further, the saltiness of the high salinity trade effluent before softening process process is 1.5%wt ~ 3.5%wt, COD
crbe less than 200mg/L.
Further, described softening process is that adding medicine method or resin soften bed process or duct type microfiltration method.
Further, the concentrated solution saltiness after high pressure reverse osmosis unit reverse-osmosis treated reaches 5%wt ~ 7%wt and enters electrodialysis concentration compartments.
Further, described electrodialysis unit is electron ion membrane concentrator matrix, and described electron ion membrane concentrator matrix comprises M × N number of electron ion membrane concentrator, and wherein M and N is respectively the integer being more than or equal to 1.
Further, the electrodialytic membranes of described electrodialysis unit is homogeneous ion-exchange membrane, membrane resistance 0.1 ~ 0.8 Ω/cm
2, degree of crosslinking is 70 ~ 90%.
Further, the high salinity trade effluent after softening is through electrodialysis unit concentration, and the outlet fresh water that saltiness is reduced to 0.3%wt ~ 0.5%wt enters low pressure reverse osmosis device.
Further, the high salinity trade effluent after softening is through electrodialysis unit concentration, and vapo(u)rization system recovery salinity delivered to by the outlet concentrated solution that saltiness rises to 15%wt ~ 20%wt.
Further, the TDS that water is produced in the reuse exported from high pressure reverse osmosis unit and low pressure reverse osmosis device is less than 1000mg/L.
According to technical scheme of the present invention, the high salinity waste water combined films treatment process of this less energy-consumption zero release, comprehensively analyzed by Technological Economy, reasonably distribute the flow that high salinity trade effluent enters high pressure reverse osmosis unit and electrodialysis unit, and it is concentrated to carry out separation simultaneously, before comparing, the energy consumption of technique is low, and construction costs and running cost low; Further, electrodialysis fresh water is separated recirculation by low pressure reverse osmosis, improves quality and the rate of recovery that water is produced in reuse.
Accompanying drawing explanation
Fig. 1 is a kind of schematic diagram being applied to the film combined treatment process of high salinity waste water provided by the invention;
In figure: 101-one-level dosing flocculation basin; 102-one-level settling pond; 103-secondary dosing flocculation basin; 104-secondary settling pond; 105-clean water basin; 106-pressure filter; 201-ensures public security filter; 202-first high-pressure pump; 203-first vacuum breaker; 204-high pressure reverse osmosis unit; 205-energy recycle device; 206-second high-pressure pump; 207-electrodialysis unit; 208-concentrates water tank; 209-third high press pump; 210-second vacuum breaker; 211-low pressure reverse osmosis device.
Embodiment
Below in conjunction with accompanying drawing, one exemplary embodiment of the present invention is made an explanation, comprising the various details of the embodiment of the present invention to help understanding, they should be thought it is only exemplary.Therefore, those of ordinary skill in the art will be appreciated that, can make various change and amendment, and can not deviate from scope and spirit of the present invention to the embodiments described herein.Equally, for clarity and conciseness, the description to known function and structure is eliminated in following description.
With the treatment capacity of 30 tons per hour to each treatment unit design of whole technique and installation and debugging, finally carry out spot testing, pilot plant test carried out to certain desulfurization wastewater:
The pH of certain factory's desulfurization wastewater is 6-9, saltiness 3%wt, COD
crbe less than 200mg/L, suspended substance is less than 70mg/L, water temperature 30 DEG C;
Dosing sofening treatment method is adopted to remove calcium ions and magnesium ions to the desulfurization wastewater of 30m3/h, respectively through one-level dosing flocculation basin 101, one-level settling pond 102, secondary dosing flocculation basin 103, security personnel's filter 201 is delivered to after secondary settling pond 104 and clean water basin 105, waste water after softening enters high pressure reverse osmosis unit 204 with the flow of 12m3/h, electrodialysis unit 207 is entered with 18m3/h, pressure filter 106 press filtration is delivered to from the precipitation of one-level settling pond 102 and secondary settling pond 104, the mud outward transport of press filtration, filtrate recycle is extremely without in the high salinity trade effluent of sofening treatment,
The described high salinity trade effluent entering high pressure reverse osmosis unit 204 is divided into two strands, one passes into in high pressure reverse osmosis unit 204 after the first high-pressure pump 202, first vacuum breaker 203, another stock-traders' know-how crosses the dump energy that energy recycle device 205 reclaims the concentrated solution of output from high pressure reverse osmosis unit 204, then carry out boost in pressure through the second high-pressure pump 206, then converge with one high salinity trade effluent before and enter high pressure reverse osmosis unit 204; The flow of the reuse product water of high pressure reverse osmosis unit 204 is that 6m3/h, TDS are less than 500mg/L, and the concentrated solution saltiness after high pressure reverse osmosis unit 204 processes reaches the concentration compartments that 6%wt enters electrodialysis unit 207;
High salinity trade effluent after softening enters the desalting chamber of electrodialysis unit 207 with the flow of 18m3/h, through electrodialysis unit 207 concentration, outlet fresh-water flow 18m3/h saltiness is reduced to 1%wt and enters low pressure reverse osmosis device 211, outlet concentrated solution saltiness rises to 15% and delivers to concentrated water tank 208, in concentrated water tank 208, dense water section reuse is to the high pressure reverse osmosis unit concentrated solution after energy recovery, and part is delivered to vapo(u)rization system and carried out salinity recovery;
The electrodialysis entering low pressure reverse osmosis device 211 exported after fresh water entered third high press pump 208, second vacuum breaker 209 and enters low pressure reverse osmosis device 211; The flow of the reuse product water of low pressure reverse osmosis device 211 is that 18m3/h, TDS are less than 500mg/L, and the flow of the concentrated solution after low pressure reverse osmosis device 211 processes is 6m3/h, and saltiness is 3%wt, and enters the desalting chamber of electrodialysis unit 207.
Overall energy consumption of the present invention is as follows, and the energy consumption of high pressure reverse osmosis system is 1kWh, and the electrodialytic energy consumption of homogeneous membrane is 180kWh, and the energy consumption of low pressure reverse osmosis system is 27kWh, and energy consumption is altogether 225kWh; Same process 30 tons of water, it is a kind of calcium chloride wastewater process and reuse method introduced in 15wt%, ZL201110225251.6 that dope is concentrated into saltiness, needs energy consumption to be 260kWh; For the high salinity zero discharge of industrial waste water technique that ZL201310311089.9 introduces, reverse osmosis after first electrodialysis, test finds very uneconomical, and when saltiness is at 6%wt, utilize high pressure reverse osmosis, working pressure more than 80 kilograms, equipment fluctuation of service, there is potential safety hazard, be more difficult to be concentrated into 15%wt.
According to technical scheme of the present invention, the high salinity waste water combined films treatment technology of this less energy-consumption zero release, reasonably distributes high salinity waste water and enter high pressure reverse osmosis unit and electrodialysis unit, and to carry out separation concentrated simultaneously, before comparing, the energy consumption of processing method is low, and construction costs and running cost low; Electrodialysis fresh water is separated recirculation by low pressure reverse osmosis device, and the quality and the rate of recovery that improve reuse product water meet power plant water requirement.
Claims (10)
1. be applied to a film combined treatment process for high salinity trade effluent, it is characterized in that, described film combined treatment process comprises the following steps:
(1) softening process process is carried out to high salinity trade effluent;
(2) the high salinity trade effluent after softening one enter high pressure reverse osmosis unit, another stock enters electrodialysis unit; Enter the high salinity trade effluent of high pressure reverse osmosis unit after reverse-osmosis treated, fresh water produces water as reuse, and concentrated solution enters electrodialysis unit; Enter the high salinity trade effluent of electrodialysis unit after concentration, outlet fresh water enters low pressure reverse osmosis device, and outlet concentrated solution is delivered to vapo(u)rization system and carried out salt recovery; Enter the fresh water of low pressure reverse osmosis device after reverse-osmosis treated, outlet fresh water produces water as reuse, enters electrodialysis unit after the high salinity trade effluent exported after concentrated solution and sofening treatment converges.
2. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, is characterized in that, the flow entering the high salinity trade effluent of high pressure reverse osmosis unit is the 35-45% of high salinity trade effluent total flux.
3. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, it is characterized in that, the described high salinity trade effluent entering high pressure reverse osmosis unit is divided into two strands, one passes into in high pressure reverse osmosis unit, another stock-traders' know-how is crossed energy recycle device and is reclaimed the dump energy of the concentrated solution of output from high pressure reverse osmosis unit, then converges with one high salinity trade effluent before and enters high pressure reverse osmosis unit.
4. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, is characterized in that, the saltiness of the high salinity trade effluent before softening process process is 1.5%wt ~ 3.5%wt, COD
crbe less than 200mg/L.
5. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, is characterized in that, the concentrated solution saltiness after high pressure reverse osmosis unit reverse-osmosis treated reaches 5%wt ~ 7%wt and enters electrodialysis concentration compartments.
6. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, it is characterized in that, described electrodialysis unit is electron ion membrane concentrator matrix, described electron ion membrane concentrator matrix comprises M × N number of electron ion membrane concentrator, and wherein M and N is respectively the integer being more than or equal to 1.
7. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, is characterized in that, the electrodialytic membranes of described electrodialysis unit is homogeneous ion-exchange membrane, membrane resistance 0.1 ~ 0.8 Ω/cm
2, degree of crosslinking is 70 ~ 90%.
8. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, it is characterized in that, high salinity trade effluent after softening is through electrodialysis unit concentration, and the outlet fresh water that saltiness is reduced to 0.3%wt ~ 0.5%wt enters low pressure reverse osmosis device.
9. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, it is characterized in that, high salinity trade effluent after softening is through electrodialysis unit concentration, and vapo(u)rization system recovery salinity delivered to by the outlet concentrated solution that saltiness rises to 15%wt ~ 20%wt.
10. a kind of film combined treatment process being applied to high salinity trade effluent according to claim 1, is characterized in that, produces the TDS of water be less than or equal to 1000mg/L from the reuse of high pressure reverse osmosis unit and the outlet of low pressure reverse osmosis device.
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| CN105347594A (en) * | 2015-12-01 | 2016-02-24 | 杭州水处理技术研究开发中心有限公司 | High-salinity wastewater zero emission and high-purity sodium chloride recovering system |
| CN105417795A (en) * | 2015-12-15 | 2016-03-23 | 江苏肯创环境科技股份有限公司 | Desulfurization waste water zero discharging treatment process for coal-fired power plant |
| CN107098526A (en) * | 2016-02-22 | 2017-08-29 | 麦王环境技术股份有限公司 | The film concentrator and handling process of strong brine zero-emission sub-prime crystallization |
| CN107954528A (en) * | 2017-12-01 | 2018-04-24 | 山东省盐业集团有限公司 | A kind of method of Salt production concentrated brine |
| CN109264675A (en) * | 2018-11-02 | 2019-01-25 | 厦门亿赛膜技术有限公司 | A kind of technique and system preparing ammonium hydroxide and sulfuric acid using ammonia nitrogen washing water |
| CN113292194A (en) * | 2021-06-08 | 2021-08-24 | 苏州融和福天宝环保科技有限责任公司 | Method for treating electroplating comprehensive wastewater |
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| CN113292194A (en) * | 2021-06-08 | 2021-08-24 | 苏州融和福天宝环保科技有限责任公司 | Method for treating electroplating comprehensive wastewater |
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