CN104445786A - Process and device for treating high-concentration salt-containing wastewater - Google Patents
Process and device for treating high-concentration salt-containing wastewater Download PDFInfo
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
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- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
- C02F5/10—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances
- C02F5/105—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances combined with inorganic substances
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- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
- C02F5/10—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances
- C02F5/12—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing nitrogen
- C02F5/125—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing nitrogen combined with inorganic substances
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
- C02F5/10—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances
- C02F5/14—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing phosphorus
- C02F5/145—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances containing phosphorus combined with inorganic substances
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Abstract
The invention relates to a process and a device for treating high-concentration salt-containing wastewater. The process and the device are particularly suitable for treating high-concentration salt-containing wastewater of which the water quality salt content is 0.5-3%, the COD (chemical oxygen demand) content is 1000-10000mg/L and BC ratio is less than 0.15, or containing heavy metal ions including Fe<3+>, Cu<2+>, Zn<2+>, Ni<2+>, Cr<3+>, Cr<6+> and the like. On the basis of core membrane technical products of a butterfly tube reverse osmosis membrane (DT), electrodialysis (ED), membrane distillation (MD) and the like, a process chain for treating the high-concentration wastewater is built, and a particular process and a particular device for treating DEM high-concentration salt-containing wastewater are formed. The process and the device provided by the invention thoroughly defeat other technologies in the aspects of stability, energy conservation, investment cost and the like to ensure that equipment for treating the high-concentration salt-containing wastewater is modularized and simplified, the use cost of an enterprise is greatly reduced, and the reuse rate of the wastewater is guaranteed to be more than 90%, so that a new window for treating the high-concentration salt-containing wastewater is opened.
Description
Technical field
The invention belongs to technical field of waste water processing, specifically relate to a kind for the treatment of process and device of high dense brine waste.
Background technology
Protection of the environment is one of the fundamental interests and elementary object of Chinese long-term stability development, realizes the severe challenge that Sustainable development is still China facing.Under the supervision energetically of country; especially effluent charge raise; under the enforcement of the measures such as environment protection tax legislation; the environmental protection consciousness of enterprise improves relatively, has feasible rational method at present to the process of Normal wastewater, but at some special process chain; the dense brine waste of height produced; because its processing cost is relative higher with outward transport cost, a lot of enterprise still adopts the disorderly method such as row or mixing, severe contamination ecological water body.
High dense brine waste refers to have the waste water that turbidity is high, salinity is high, organic content is high, bio-toxicity is large, biodegradability is poor, environmental hazard is large.The treatment process such as conventional biochemical technology and ultra filtering reverse osmosis membrane technique cannot be suitable for, and cannot reach qualified discharge, the minimizing even object of zero discharge treatment.At present, only have the useless outward transport of flash distillation, multiple-effect evaporation or danger for the treatment process that the dense brine waste of height is conventional, but both energy consumptions are relatively higher above, and the latter is because the outward transport water yield causes greatly transportation cost to increase, general enterprises all cannot bear.
Summary of the invention
In order to overcome the deficiency that prior art exists, the invention provides a kind of good stability, the treatment process of energy saving is excellent, cost of investment the is low dense brine waste of height and device.
A treatment process for high dense brine waste, comprises the steps:
(1) waste water carries out pre-treatment, makes SS content <10mg/L, Ca in water quality
2+, Mg
2+total content <3mg/L;
(2) pretreated waste water is through the first line mixer, regulates pH to be 7 ~ 9, and inflow temperature controls as < 35 DEG C;
(3) waste water after regulating pH is processed by butterfly pipe reverse-osmosis membrane element after high-pressure pump supercharging, and it is 2.5 ~ 8MPa that high-pressure pump controls intake pressure;
(4), after butterfly pipe reverse-osmosis membrane element processes, fresh water enters the first tank and collects reuse, and dense water enters in electrodialysis element and is further processed;
(5) fresh water after the process of electrodialysis element circulates before getting back to high-pressure pump, the second tank transfer of dense water;
After the intersegmental supercharging of dense water impeller pump in (6) second tanks, first through second pipe mixing tank, and add Scale inhibitors, then use interchanger concurrent heating, finally use heater heats, ensure that inflow temperature is at 60 ~ 80 DEG C;
(7) under guarantee inflow temperature condition, dense water enters membrane distillation element and processes, and the fresh water steam of membrane distillation is by vacuum pump condensation reuse after interchanger suction first tank;
(8) the dense water of a part of membrane distillation enters decrease temperature crystalline in crystallizer, and in crystallizer, timing adds pure crystal formation flakes sodium sulfate crystal seed, and the dense water of another part membrane distillation uses recycle pump pump circulation, until membrane distillation solution supersaturation and non-crystallizable; Wherein 75 ~ 90% water yields return second pipe mixing tank, and 10 ~ 25% water yields enter crystallizer; Concrete recycle ratio is determined according to actual waste water concentration and composition;
(9) crystalline mother solution is from the overflow port overflow of crystallizer top, and water-containing crystal salt is discharged from crystalliser feet;
(10) overflow crystalline mother solution and water-containing crystal salt are transported outward after collecting and are carried out useless process of endangering.
As preferably, in step (6), the intersegmental boost control intake pressure of impeller pump is 0.1 ~ 0.2MPa, concurrent heating thermal source is membrane distillation fresh water steam, heat source can select saturation steam or thermal oil, described Scale inhibitors obtains after being mixed with aqueous sodium hydroxide solution by one or several in Sodium hexametaphosphate 99,1-Hydroxy Ethylidene-1,1-Diphosphonic Acid sodium, mercaptobenzothiazole, sodium polyacrylate, and described Scale inhibitors pH is 8 ~ 9.
As preferably, described Scale inhibitors is made up of the component of following massfraction: Sodium hexametaphosphate 99 1 ~ 10%, 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid sodium 10 ~ 15%, mercaptobenzothiazole 0 ~ 2%, sodium polyacrylate 2 ~ 10%, surplus are aqueous sodium hydroxide solution.
As preferably, described butterfly pipe reverse-osmosis membrane element is butterfly tubular type disc structure, and disk quantity is 40 or its multiple, and the fresh water reclamation rate of butterfly pipe reverse-osmosis membrane element controls 60 ~ 80%.Single membrane element is 1.5 ~ 3 tons/day according to the influent density situation process water yield, and membrane element is according to process water yield modular combination, and maximum operating pressure is 8 MPa, and Water Sproading rate is 60 ~ 80%.
As preferably, described electrodialysis element adopts homogeneous membrane, wide runner design, the operation of falling pole, operation flow velocity is 0.2m/s, and operating pressure is 0.1 ~ 0.2Mpa, running current adjusts according to saltiness, and lower than limiting current, the fresh water reclamation rate of electrodialysis element controls 40 ~ 60%.
As preferably, described interchanger is adverse current plate heat exchanger.
As preferably, the film in membrane distillation element selects polyether-ether-ketone (PEEK) or polytetrafluoroethylene (PTFE) hollow fiber hydrophobic membrane, and its film silk adopts tubulation distribution, operating pressure 0.1 ~ 0.2MPa.Single 14 inches of membrane elements are according to former water temp and the dopant species process water yield 2 ~ 3 tons/day.
As preferably, crystal salt water ratio is 20 ~ 30%.Each unlatching need add suitable crystal seed.
A kind for the treatment of unit of high dense brine waste, described device comprises and arranging in turn and the pretreatment water tank be communicated with, the first line mixer, butterfly pipe reverse-osmosis membrane element, electrodialysis element, second pipe mixing tank, interchanger, well heater, membrane distillation element, crystallizer, described first line mixer is connected with butterfly pipe reverse-osmosis membrane element by high-pressure pump, butterfly pipe reverse-osmosis membrane element is connected with electrodialysis element, described butterfly pipe reverse-osmosis membrane element is also connected with the first tank, and electrodialysis element is connected with the pipeline before high-pressure pump by pipeline; Be provided with the second tank between described electrodialysis element and second pipe mixing tank, described second tank is connected with second pipe mixing tank by impeller pump; Described membrane distillation element side is provided with vapour outlet, and membrane distillation component base is provided with water outlet, and described vapour outlet is connected with interchanger, the first tank successively by vacuum pump, and water outlet is connected with crystallizer, second pipe mixing tank respectively by recycle pump; Described crystallizer top is provided with overflow port, and crystallizer top is provided with crystal seed input port, and crystalliser feet is provided with hydrated crystal relief outlet.
As preferably, described membrane distillation element side is provided with two vapour outlets, and one of them vapour outlet is arranged on the top of membrane distillation element, and another vapour outlet is arranged on the bottom of membrane distillation element.
The present invention is particularly useful for water quality treatment saltiness 0.5 ~ 3%, COD content 1000 ~ 10000mg/L, BC than <0.15, or containing Fe
3+, Cu
2+, Zn
2+, Ni
2+, Cr
3+, Cr
6+etc. the dense brine waste of the height of heavy metal ion.The present invention can not only reduce the processing cost of high dense brine waste, and can also ensure that wastewater recycle rate is more than 90%.
The present invention creates more economical resource circulation utilization for guiding theory with modern technique, based on core membrane technique products such as butterfly pipe reverse osmosis membrane (DT), electrodialysis (ED) and membrane distillations (MD), get through high load wastewater treatment technology chain, form the high dense brine waste treatment process of exclusive DEM and device.This treatment process is in stability, and energy saving, the aspects such as cost of investment defeat other technologies completely, and make high dense brine waste treatment facility modularization, summary, greatly reduces the use cost of enterprise, and the window that also a fan is new is opened in the process for the dense brine waste of height.
Accompanying drawing explanation
Fig. 1 is the structural representation of the high dense salt-containing waste water treating device of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the invention will be further described, but protection scope of the present invention is not limited to this.
Embodiment 1
With reference to Fig. 1, a kind for the treatment of process of high dense brine waste, comprises the steps:
(1) the former water of hc effluent is after sand filtration, secondary filter, tubular type ultrafiltration, the pretreatment technology such as softening, makes SS content <10mg/L in water quality, Ca
2+, Mg
2+total content <3mg/L, qualified pretreated waste water is deposited in pretreatment water tank 1;
(2) pretreated waste water is through the first line mixer 2, regulates pH to be 8, and inflow temperature controls as < 35 DEG C;
(3) waste water after regulating pH carries out the first step process by butterfly pipe reverse-osmosis membrane element (DT) 4 after high-pressure pump 3 supercharging, and it is 5MPa that high-pressure pump controls intake pressure;
(4) after butterfly pipe reverse-osmosis membrane element 4 processes, gained fresh water enters the first tank 13 and collects reuse, and dense water enters in electrodialysis element (ED) 5 and is further processed; Control the fresh water reclamation rate of butterfly pipe reverse osmosis membrane (DT) element 4 70%;
(5) there is ion migration in the dense water of DT in electrodialysis (ED) element 5, because electrodialysis (ED) can only desalination, and can not remove COD, and therefore ED fresh water need get back to circulation before high-pressure pump 3, removes the COD in ED fresh water; Fresh water after the process of electrodialysis element circulates before getting back to high-pressure pump 3, the second tank 6 transfer of the dense water of ED; Control the fresh water reclamation rate of electrodialysis (ED) element 4 50%;
The intersegmental supercharging of dense water impeller pump 7 in (6) second tanks 6, controls intake pressure at the dense water of 0.2MPa, ED first through second pipe 8 mixing tank, and timing adds specific Scale inhibitors, then use interchanger 9 concurrent heating, finally heat with well heater 10, ensure that inflow temperature is at 70 DEG C; Wherein, described specific Scale inhibitors is made up of the component of following massfraction: Sodium hexametaphosphate 99 5%, 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid sodium 13%, mercaptobenzothiazole 1%, sodium polyacrylate 6%, surplus are aqueous sodium hydroxide solution, and Scale inhibitors pH is 9; Described concurrent heating thermal source is membrane distillation (MD) fresh water steam, and heat source can select saturation steam or heat conduction wet goods, and described interchanger is adverse current plate heat exchanger;
(7) under guarantee inflow temperature condition, the dense water of ED enters membrane distillation (MD) element 11 and processes, and the fresh water steam of membrane distillation is pumped by vacuum pump 12, and steam is first by interchanger 9, as the thermal source of the dense water of ED, then enter the first tank 13 condensation and collect reuse;
(8) the dense water of MD uses recycle pump 14 pump circulation, until membrane distillation (MD) solution supersaturation and non-crystallizable; After wherein 80% water yield returns second pipe mixing tank 8,20% water yield enters crystallizer 15; The dense water of MD decrease temperature crystalline in crystallizer 15, in crystallizer, timing adds pure crystal formation flakes sodium sulfate crystal seed, and ensure that crystal is even, crystalline mother solution becomes ladder to lower the temperature in crystallizer, and crystallizer discharge is smooth and easy, not easily blocks up;
(9) crystalline mother solution timing is from overflow port 19 overflow on crystallizer top, and water-containing crystal salt is discharged from hydrated crystal relief outlet 20 timing of crystalliser feet, and water-containing crystal salt water ratio is 25%;
(10) overflow crystalline mother solution and water-containing crystal salt are transported outward after collecting and are carried out useless process of endangering.
Wherein, described butterfly pipe reverse-osmosis membrane element is butterfly tubular type disc structure, and disk quantity is 40.Single membrane element is 2.5 tons/day according to the influent density situation process water yield, and membrane element is according to process water yield modular combination, and maximum operating pressure is 8 MPa, and Water Sproading rate is 70%.
Described electrodialysis element adopts homogeneous membrane, wide runner design, the operation of falling pole, and run flow velocity 0.2m/s, operating pressure 0.2MPa, running current adjusts according to saltiness, and lower than limiting current, Water Sproading rate is 50%.
Film in described membrane distillation element selects polyether-ether-ketone (PEEK) or polytetrafluoroethylene (PTFE) hollow fiber hydrophobic membrane, its film silk adopts tubulation distribution, operating pressure 0.2MPa, single 14 inches of membrane elements are according to former water temp and the dopant species process water yield 2 ~ 3 tons/day.
Owing to have employed exclusive DEM high load wastewater treatment technology, improve the treatment capacity of high dense brine waste greatly, single device reclamation rate can reach more than 90%; Simultaneously owing to have employed energy-saving technique, energy consumption is well below flash distillation or multiple-effect evaporation technology.
For butterfly pipe reverse osmosis membrane (DT), 1 ton of water treatment energy consumption is 7 ~ 8 ° of electricity;
For electrodialysis (ED), 1 ton of water treatment energy consumption is 5 ~ 10 ° of electricity;
For membrane distillation (MD), 1 ton of water treatment energy consumption is 20 ~ 30 ° of electricity;
For exclusive DEM high load wastewater treatment technical finesse one ton of water, each process section presses minimum process capacity calculation, maximum energy consumption=(1*8+0.4*10+0.24*30)=19.2 °; Be evaporated to example with five effects in multiple-effect evaporation, process one ton of water, need power consumption 168 degree.Therefore, DEM high load wastewater treatment technology there is very excellent falling can advantage.
Embodiment 2
With reference to Fig. 1, a kind for the treatment of unit of high dense brine waste, described device comprises and arranging in turn and the pretreatment water tank 1 be communicated with, first line mixer 2, butterfly pipe reverse-osmosis membrane element 4, electrodialysis element 5, second pipe mixing tank 8, interchanger 9, well heater 10, membrane distillation element 11, crystallizer 15, described first line mixer 2 is connected with butterfly pipe reverse-osmosis membrane element 4 by high-pressure pump 3, butterfly pipe reverse-osmosis membrane element 4 is connected with electrodialysis element 5, described butterfly pipe reverse-osmosis membrane element 4 is also connected with the first tank 13, electrodialysis element 5 is connected with the pipeline before high-pressure pump 3 by pipeline, be provided with the second tank 6 between described electrodialysis element 5 and second pipe mixing tank 8, described second tank 6 is connected with second pipe mixing tank 8 by impeller pump 7, described membrane distillation element 11 side is provided with vapour outlet 17, water outlet 18 is provided with bottom membrane distillation element 11, described vapour outlet 17 is connected with interchanger 9, first tank 13 successively by vacuum pump 12, and water outlet 18 is connected with crystallizer 15, second pipe mixing tank 8 respectively by recycle pump 14, described crystallizer 15 top is provided with overflow port 19, and crystallizer top is provided with crystal seed input port 16, and crystalliser feet is provided with hydrated crystal relief outlet 20.
Described membrane distillation element 11 side is provided with two vapour outlets 17, and one of them vapour outlet is arranged on the top of membrane distillation element, and another vapour outlet is arranged on the bottom of membrane distillation element.
Described interchanger is adverse current plate heat exchanger, described butterfly pipe reverse-osmosis membrane element is butterfly tubular type disc structure, disk quantity is 40 or its multiple, and the film in described membrane distillation element selects polyether-ether-ketone or polytetrafluoroethylhollow hollow fiber hydrophobic membrane, and its film silk adopts tubulation distribution.
Embodiment 3
DEM high load wastewater treatment technology is for the treatment of certain wastewater from chemical industry, and its result is as shown in table 1:
Table 1
Can find out according to table 1 result, certain wastewater from chemical industry, by DEM high load wastewater treatment technology, DT fresh water reclamation rate can reach 56%, MD fresh water reclamation rate can reach 46%, and total fresh water reuse can reach 90.5%, and outer discharge capacity is 9.5% when not processing.Total reuse fresh water saltiness <1500mg/L, COD≤22, meet two class Water circulation standards completely.
Embodiment 4
DEM high load wastewater treatment technology is for the treatment of certain pharmacy mother liquor, and its result is as shown in table 2:
Table 2
Can find out according to table 2 result, certain pharmacy mother liquor, by DEM high load wastewater treatment technology, DT fresh water reclamation rate can reach 80%, MD fresh water reclamation rate can reach 50%, and total fresh water reuse can reach 97%, and outer discharge capacity is 3% when not processing.Total reuse fresh water saltiness <300mg/L, COD≤25, meet a class Water circulation standard completely.
Embodiment 5
DEM high load wastewater treatment technology is for the treatment of certain percolate, and its result is as shown in table 3:
Table 3
Can find out according to table 3 result, certain percolate, by DEM high load wastewater treatment technology, DT fresh water reclamation rate can reach 70%, MD fresh water reclamation rate can reach 50%, and total fresh water reuse can reach 95%, and outer discharge capacity is 5% when not processing.Total reuse fresh water saltiness <300mg/L, COD≤25, meet a class Water circulation standard completely.
Embodiment 6
Energy consumption and the expense of DEM high load wastewater treatment technology are as shown in table 4:
Table 4
| Embodiment 3 | Embodiment 4 | Embodiment 5 | |
| DT energy consumption kwh/ ton | 7.5 | 7 | 7 |
| ED energy consumption kwh/ ton | 10 | 9 | 8 |
| MD energy consumption kwh/ ton | 25 | 21 | 20 |
| Total energy consumption kwh/ ton | 18.28 | 11.88 | 13.87 |
| Equipment amortization yuan/ton | 13.4 | 15.3 | 13.4 |
| Total expenses yuan/ton | 28.02 | 24.81 | 24.49 |
Be 1 ton of water for steam output, single-action or multiple-effect evaporation art breading energy consumption and expense as shown in table 5:
Table 5
| Effect number | Single-action | Economic benefits and social benefits | Triple effect | Quadruple effect | Five effects |
| Steam consumption t | 1.1 | 0.57 | 0.4 | 0.3 | 0.27 |
| Energy expenditure kwh | 686 | 355 | 244 | 187 | 168 |
| Equipment amortization yuan/ton | 0.3 | 0.6 | 0.9 | 1.2 | 1.5 |
| Total expenses yuan/ton | 549.1 | 213 | 196.1 | 150.8 | 135.9 |
Contrast table 4 and table 5, wherein ability consumption is finally converted to the electricity charge, calculate with general industry electricity consumption 0.8 yuan/kwh, be 1 ton of water for steam output, single-action or the expense needed for multiple-effect evaporation technique evaporate to dryness 1 ton of water are also far longer than DEM high load wastewater treatment technique, therefore, DEM high load wastewater treatment technology there is very excellent falling can advantage.
The direct outward transport cost of untreated effluent is as shown in table 6:
Table 6
| Certain wastewater from chemical industry | Certain pharmacy mother liquor | Certain percolate | |
| COD | 200 | 1500 | 3000 |
| Saltiness mg/L | 25000-27000 | 6000-8000 | 6000 |
| Outward transport cost yuan/ton | 1500 | 3000 | 1300 |
Contrast table 4 and table 6, for Hangzhou, wherein transport outward processing cost greatly about 1500 yuan/ton containing higher salinity in certain wastewater from chemical industry, in certain pharmacy waste water, because containing unknown non-degradable thing, outward transport cost is greatly about 3000 yuan/ton, certain percolate, relative outward transport cost is lower at about 1300 yuan/ton, but, the direct external application cost of untreated effluent is still far away higher than processing cost, simultaneously, after the technical finesse of DEM high load wastewater treatment, most of water still can reuse, again need not take target water, not only reach the effect of energy-saving and emission-reduction, also for enterprise provides cost savings.
What finally illustrate is, above embodiment is only in order to illustrate technical scheme of the present invention and unrestricted, although with reference to preferred embodiment to invention has been detailed description, those of ordinary skill in the art is to be understood that, can modify to technical scheme of the present invention or equivalent replacement, and not departing from aim and the scope of technical solution of the present invention, it all should be encompassed in the middle of right of the present invention.
Claims (10)
1. a treatment process for high dense brine waste, is characterized in that comprising the steps:
(1) waste water carries out pre-treatment, makes SS content <10 mg/L in water quality, Ca
2+, Mg
2+total content <3mg/L;
(2) pretreated waste water is through the first line mixer, regulates pH to be 7 ~ 9, and inflow temperature controls as < 35 DEG C;
(3) waste water after regulating pH is processed by butterfly pipe reverse-osmosis membrane element after high-pressure pump supercharging, and it is 2.5 ~ 8MPa that high-pressure pump controls intake pressure;
(4), after butterfly pipe reverse-osmosis membrane element processes, fresh water enters the first tank and collects reuse, and dense water enters in electrodialysis element and is further processed;
(5) fresh water after the process of electrodialysis element circulates before getting back to high-pressure pump, the second tank transfer of dense water;
After the intersegmental supercharging of dense water impeller pump in (6) second tanks, first through second pipe mixing tank, and add Scale inhibitors, then use interchanger concurrent heating, finally use heater heats, ensure that inflow temperature is at 60 ~ 80 DEG C;
(7) under guarantee inflow temperature condition, dense water enters membrane distillation element and processes, and the fresh water steam of membrane distillation is by vacuum pump condensation reuse after interchanger suction second tank;
(8) the dense water of a part of membrane distillation enters decrease temperature crystalline in crystallizer, and in crystallizer, timing adds pure crystal formation flakes sodium sulfate crystal seed, and the dense water of another part membrane distillation uses recycle pump pump circulation, until membrane distillation solution supersaturation and non-crystallizable; Wherein 75 ~ 90% water yields return second pipe mixing tank, and 10 ~ 25% water yields enter crystallizer;
(9) crystalline mother solution is from the overflow port overflow of crystallizer top, and water-containing crystal salt is discharged from crystalliser feet;
(10) overflow crystalline mother solution and water-containing crystal salt are transported outward after collecting and are carried out useless process of endangering.
2. the treatment process of the dense brine waste of height according to claim 1, it is characterized in that: in step (6), the intersegmental boost control intake pressure of impeller pump is 0.1 ~ 0.2MPa, concurrent heating thermal source is membrane distillation fresh water steam, heat source can select saturation steam or thermal oil, described Scale inhibitors obtains after being mixed with aqueous sodium hydroxide solution by one or several in Sodium hexametaphosphate 99,1-Hydroxy Ethylidene-1,1-Diphosphonic Acid sodium, mercaptobenzothiazole, sodium polyacrylate, and described Scale inhibitors pH is 8 ~ 9.
3. the treatment process of the dense brine waste of height according to claim 2, is characterized in that: described Scale inhibitors is made up of the component of following massfraction: Sodium hexametaphosphate 99 1 ~ 10%, 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid sodium 10 ~ 15%, mercaptobenzothiazole 0 ~ 2%, sodium polyacrylate 2 ~ 10%, surplus are aqueous sodium hydroxide solution.
4. the treatment process of the dense brine waste of height according to claim 1, is characterized in that: described butterfly pipe reverse-osmosis membrane element is butterfly tubular type disc structure, and disk quantity is 40 or its multiple, and the fresh water reclamation rate of butterfly pipe reverse-osmosis membrane element controls 60 ~ 80%.
5. the treatment process of the dense brine waste of height according to claim 1, is characterized in that: described electrodialysis element adopts homogeneous membrane, wide runner design, the operation of falling pole, operation flow velocity is 0.2m/s, and operating pressure is 0.1 ~ 0.2Mpa, and the fresh water reclamation rate of electrodialysis element controls 40 ~ 60%.
6. the treatment process of the dense brine waste of height according to claim 1, is characterized in that: described interchanger is adverse current plate heat exchanger.
7. the treatment process of the dense brine waste of height according to claim 1, is characterized in that: the film in membrane distillation element selects polyether-ether-ketone or polytetrafluoroethylhollow hollow fiber hydrophobic membrane, and its film silk adopts tubulation distribution, operating pressure 0.1 ~ 0.2MPa.
8. the treatment process of the dense brine waste of height according to claim 1, is characterized in that: crystal salt water ratio is 20 ~ 30%.
9. the treatment unit of one kind high dense brine waste, it is characterized in that: described device comprises and arranging in turn and the pretreatment water tank be communicated with, first line mixer, butterfly pipe reverse-osmosis membrane element, electrodialysis element, second pipe mixing tank, interchanger, well heater, membrane distillation element, crystallizer, described first line mixer is connected with butterfly pipe reverse-osmosis membrane element by high-pressure pump, butterfly pipe reverse-osmosis membrane element is connected with electrodialysis element, described butterfly pipe reverse-osmosis membrane element is also connected with the first tank, electrodialysis element is connected with the pipeline before high-pressure pump by pipeline, be provided with the second tank between described electrodialysis element and second pipe mixing tank, described second tank is connected with second pipe mixing tank by impeller pump, described membrane distillation element side is provided with vapour outlet, and membrane distillation component base is provided with water outlet, and described vapour outlet is connected with interchanger, the first tank successively by vacuum pump, and water outlet is connected with crystallizer, second pipe mixing tank respectively by recycle pump, described crystallizer top is provided with overflow port, and crystallizer top is provided with crystal seed input port, and crystalliser feet is provided with hydrated crystal relief outlet.
10. the treatment unit of the dense brine waste of height according to claim 9, it is characterized in that: described membrane distillation element side is provided with two vapour outlets, one of them vapour outlet is arranged on the top of membrane distillation element, and another vapour outlet is arranged on the bottom of membrane distillation element.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776702A (en) * | 2016-04-06 | 2016-07-20 | 吴桂香 | Method for disposing waste liquid generated during garbage pyrolysis |
| CN108164065A (en) * | 2016-12-07 | 2018-06-15 | 北京有色金属研究总院 | A kind of sulfuric acid system acid heavy metal wastewater treatment process |
| CN110723857A (en) * | 2019-11-21 | 2020-01-24 | 东莞市三人行环境科技有限公司 | High-salinity water concentration and crystallization treatment system and process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102260006A (en) * | 2011-07-04 | 2011-11-30 | 昆明理工大学 | Method for treating heavy-metal-containing wastewater membrane filtration concentrated liquid |
| CN204325059U (en) * | 2014-12-15 | 2015-05-13 | 宁波摩尔森膜环保科技有限公司 | A kind for the treatment of unit of high dense brine waste |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102260006A (en) * | 2011-07-04 | 2011-11-30 | 昆明理工大学 | Method for treating heavy-metal-containing wastewater membrane filtration concentrated liquid |
| CN204325059U (en) * | 2014-12-15 | 2015-05-13 | 宁波摩尔森膜环保科技有限公司 | A kind for the treatment of unit of high dense brine waste |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776702A (en) * | 2016-04-06 | 2016-07-20 | 吴桂香 | Method for disposing waste liquid generated during garbage pyrolysis |
| CN108164065A (en) * | 2016-12-07 | 2018-06-15 | 北京有色金属研究总院 | A kind of sulfuric acid system acid heavy metal wastewater treatment process |
| CN110723857A (en) * | 2019-11-21 | 2020-01-24 | 东莞市三人行环境科技有限公司 | High-salinity water concentration and crystallization treatment system and process |
| CN110723857B (en) * | 2019-11-21 | 2022-04-12 | 东莞市三人行环境科技有限公司 | High-salinity water concentration and crystallization treatment system and process |
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Effective date of registration: 20170329 Address after: Hangzhou City, Zhejiang province 311404 Fuyang Xindeng Town Industrial Park Patentee after: Hangzhou Anow Microfiltration Co., Ltd. Address before: 315194 Yinzhou District, Ningbo, South Street, the first emerging industrial park Patentee before: NINGBO MOER SENMO ENVIRONMENTAL PROTECTION TECHNOLOGY CO., LTD. |