CN104909503B - A kind of integrated membrane process method for desalting seawater - Google Patents
A kind of integrated membrane process method for desalting seawater Download PDFInfo
- Publication number
- CN104909503B CN104909503B CN201510322192.2A CN201510322192A CN104909503B CN 104909503 B CN104909503 B CN 104909503B CN 201510322192 A CN201510322192 A CN 201510322192A CN 104909503 B CN104909503 B CN 104909503B
- Authority
- CN
- China
- Prior art keywords
- water
- desalination
- membrane
- desalting
- seawater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A kind of integrated membrane process method for desalting seawater, belongs to water desalination technology.With high investment, the defect such as high pressure, high energy consumption existing for existing Membrane seawater desalination technique, with " nanofiltration/pole-reversing electroosmosis " for core desalinating process, wherein nanofiltration reaches the high desalination NF membrane of 90% level using salt rejection rate, and frequently pole-reversing electroosmosis are the multistage multisection type energy-saving electrical electrodialysis apparatus being filled with Ion Exchange Resin In The Mixing Bed in thin electrode room.Sea water raw water priority is after the pretreatment of coagulative precipitation tank, settling pool, sand filter and ultrafilter membrane, successively combined have the nanofiltration desalination device of energy recycle device and energy-saving frequently pole-reversing electroosmosis device to carry out being classified desalination, nanofiltration and energy-saving electrical dialysis are respectively under the low operating pressure less than 3.8MPa and 0.4MPa, product water salinity 80 250mg/L of system, total salt rejection rate can motor-driven adjust in the range of 99 99.75%, and ton water body power consumption is less than 2.15KWh/m3, whole desalting process is invested and energy consumption all significantly reduces, and process operation is safer, more stable.
Description
Technical field
The present invention relates to a kind of method for desalting seawater, especially one kind utilize " nanofiltration/pole-reversing electroosmosis " integrated membrane process
Carry out the method that fresh water is prepared in seawater desalination, belong to water desalination technology.
Background technology
Desalinization, as one of key means solving Present Global water resources problems, worldwide all obtains
Unprecedented attention.The level of development of Chinese desalinization industry and scale, it will to economic, social sustainable development
Produce material impact.For east and Northern Coastal Region water-deficient area, meaning is particularly great.However, in the huge need desalinizing seawater
Sue for peace the limitation aspect of existing desalination technology, also there is conspicuous contradiction.
Existing desalination technology is mainly conventional distillation and sea-water reverse osmose（SWRO）Embrane method, the increasing of latter of which
Quickly, in the newly-built Seawater Desalination Project in global range, SWRO accounts for 70% share to long speed.However, the product water of SWRO becomes
This is generally higher, and, how more than 6 yuan, especially ton water consume is electric for the ton water cost of the SWRO Seawater Desalination Project of domestic at present operation
Amount is under conditions of using concentrated water apparatus for energy recovery typically still above 3.5KWh/m3.Additionally, the operating pressure of SWRO is general all
In more than 5.5MPa it is therefore necessary to adopt the high-pressure-resistant vessel reliably sealing and tubing.Meanwhile, the high salinity that sea water has
The corrosion resistance of pipeline is had high requirements again, the pipe material of high-pressure section requires with sufficiently expensive super duplex steel
Matter, only pipeline investment just account for the 30% about of desalination system.Therefore, SWRO embrane method is desalinated in high energy consumption, high operating pressure, harshness
Corrosion-resistant material require, the congenital technical bottleneck of the aspect such as with high investment, be all unfavorable for the widely available application of this technology.Long-pending
The desalinization new technique of high-efficiency and economic is developed in pole, significantly reduces operating pressure, ton water consumption, more use low costs, corrosion resistant
Erosion tubing, thus reducing system investments and operating cost, the sustainable development for desalinization industry is most important.
In recent years, some new desalination process were persistently reported both at home and abroad.Wherein more is by multiple membrane technologies
Or desalting technology is combined into one, constitute integrated membrane process, using multiple technologies between efficient coupling reducing desalinization
The energy consumption of journey and cost.As Chinese patent CN 1994904 A discloses a kind of " ultrafiltration+nanofiltration+low pressure reverse osmosis " Integrated Films sea
Water desalination process, total operating pressure as little as 3.5MPa, in 42.4%-45%, salt rejection rate is in 95.93%- for device Water Sproading rate
98.16%, energy consumption 2.17KWh/m3-4.48 KWh/m3.This integrated membrane process achieves good effect in terms of realizing low pressure desalination
Really, but total salt rejection rate is not high enough, fail stably more than 98.5%, produce water salinity be generally greater than 800-1000mg/L, can lead
Cause mouthfeel still partially puckery, less suitably as drinking water.In addition, will be mutually integrated with reverse osmosiss for nanofiltration when, both broadly fall into high throwing
Resource system, the equipment investment of whole system is significantly expensive.
United States Patent (USP) US 2003/0205526 A1 discloses a kind of twin-stage sea water nanofiltration desalination technique, and process average operates
Pressure reaches 5.17MPa, and wherein one-level nanofiltration is 3.45 MPa, and two grades of nanofiltrations are 1.72 MPa, Water Sproading rate 30%-40% it
Between, salt rejection rate is 97.14%.This complex process degree has declined, but salt rejection rate is still low, and operating pressure does not have compared with SWRO yet
It is decreased obviously, system Water Sproading rate is relatively low, therefore can not meet practical application request.
United States Patent (USP) US 2010/0089756 A1 then discloses a kind of " nanofiltration (NF)+ion friendship of combination nanofiltration
Change (IE)+electrodeionization（CEDI）" integrated membrane process desalination process.This patented technology removes about first by NF membrane
90% salinity, gained fresh water softens through cation exchange resin again, thoroughly removes whole Ga2+、Mg2+Hardness ions, then
Carry out desalination through continuous electrodeionization device again and obtain final desalination water.According to the data of report, using the configuration of artificial sea salt
Simulated seawater, in raw water electrical conductivity 45.5mS/cm, system salt rejection rate more than 98.57%, produce water conductivity 240mg/L, ton
Water consumption as little as 1.85 KWh/m3, the operating pressure of NF membrane is in below 3.8MPa.In this technique, CEDI device is conventional EDI
Desalter, its positive and negative electrode material is different, and diluting compartment is different with the construction of enriched chamber, composition, does not take and frequently switches electrode
Operation；It is filled with Ion Exchange Resin In The Mixing Bed in its diluting compartment, but diluting compartment thickness is very thin, even less than 1.5mm,
This brings great difficulty to effective filling of resin particle, will make the actual production efficiency of the CEDI device of this ultrathin separators
Than relatively low it is difficult to adapt to the needs of large-scale industrial production.In addition, core desalinating process to contain nanofiltration, ion exchange resin soft
Change and tri- units of CEDI, technological process is relatively partially long, and system is more complicated.Compared with SWRO, this integrated desalination process energy consumption is bright
Aobvious reduction, but technological design is more complicated, and ion-exchange unit needs frequent clean regeneration it is impossible to realize continual and steady operation.
Content of the invention
The purpose of the present invention, is the defect for existing desalination technology, provides a kind of new nanofiltration and extremely electricity
The integrated membrane process desalination process that osmotic technique combines, to adapt to low operating pressure, low energy consumption, Low investment, high desalination
The technical requirements of rate etc..
The purpose of the present invention is achieved by the following technical solution：
Design a kind of nanofiltration with high desalination（NF）Membrane technology and Novel low-consumption pole-reversing electroosmosis（SEDR）Technology phase is tied
" NF/SEDR " integrated membrane process closing is core desalinating process, combination coagulated precipitation, sand filtration, dosing sterilization, ultrafiltration（UF）Film mistake
Multiple pretreatment, water purifying process and the energy recycle devices such as filter and the integrated seawater desalination system that constitutes, this desalinization
System contains pretreatment unit, single stage desalting unit and three ingredients of two grades of desalination unit.With seawater and brackish water or bittern
Water is raw water, sequentially passes through above three process step and obtains the lightening products water that content of mineral substances is suitably drunk.
（1）Pretreatment unit
Pretreatment unit includes the techniques such as coagulating sedimentation, dosing sterilization, sand filtration, ultrafiltration membrance filter successively.Sea water raw water is first
First through coagulation-settlement process, in coagulation, help solidifying medicament in the presence of, make fine particle in water, colloid, float and partly micro-
Biological flocculation and precipitation becomes floccule body, passing through further to adsorb microorganism and dissolved matter, volume increases, sinking, thus reducing raw water
Turbidity and colourity；
Sea water through coagulating sedimentation effect carried out agent-feeding treatment before entering downstream sand filter, and medicament used includes adopting
The diluted acids such as dilute HCl are suitably acidified regulation, are carried out sterilization algae removal with strong oxidizers such as hypochlorous acid；
Sea water through chemicals treatment is pressurizeed by booster pump further and enters sand filter.Can adopt depending on raw water quality sand filter
One-level, two grades or multistage sand filtration, filtered with the quartz sand of different-grain diameter size respectively, reduce raw water turbidity, make water quality clear
Clearly；
During sea water through sand filters enters, control fiber ultrafiltration membrane carries out membrane filtration.The pore size filter of ultrafilter membrane is less than
0.1 μm, can effectively remove fine particle in eliminating water, colloid, microorganism and larger molecular organicses, so that the pollution index of sea water is dropped
As little as less than 3.Before ultrafiltration membrance filter, also visually it is actually needed, by the way of the online dosing of dosing pump, more suitably add
Reproducibility medicament such as NaHSO3, for destroying, neutralizing the strong oxidizer of upstream remnants, make organic polymer ultrafilter membrane from oxidation
Destruction.
（2）Single stage desalting unit
Single stage desalting unit adopts the nanofiltration of high desalination（NF）Film and supporting high-pressure pump, energy recycle device and boost in pressure
Pump group becomes.NF film is equally with pressure as driving force, carries out detached membrane separating process using physics sieving actoion to liquid, its
Pore diameter range is 1-3 nanometer, 2 nanometers of average pore size, its membrane aperture, operating pressure, separating property between reverse osmosiss and ultrafiltration it
Between.Conventional NF film is less than 20% to the rejection of monovalention, to calcium, magnesium hardness ion and other bivalence and high valence ion,
Removal efficiency, up to more than 90%, also can reach more than 90% to the removal efficiency of the various organic impurities of molecular weight more than 200.For
The present invention, the NF film being used has the characteristic of high desalination, and it is to Ga2+、Mg2+And SO4 2-The rejection of ion is typically not less than
97%, highest can exceed 99%, even and if the Na to monovalence+、K+、Cl-Plasma, its removal efficiency also can reach more than 85%, its film
Assembly tolerable highest operating pressure can reach 4.0MPa.Under appropriate conditions, it is permissible to total salt rejection rate of sea water
Reach 90% about.In existing commodity NF film, DOW company produce NF90 series NF membrane possess sea water is carried out 85% with
The ability of upper desalination, its operating pressure is 3.5-3.8MPa.For branched and large-scale NF membranous system, rationally setting by flow process
Meter, its system Water Sproading rate is up to 50% level.
For NF film seawater desalination, its operating pressure is far below the level of the 5.5-6.0MPa of conventional SWRO, therefore to institute
The thickness of putamina, sealing, require all to significantly reduce to materials such as the thickness of pipeline, sealing and antiseptic properties, beneficial to subtracting
Mini system is invested.
Because the operating pressure of NF film is still above 3.5MPa, the concentrated water of its discharge typically also has and is not less than 3.4MPa's
High potential energy, therefore NF film desalination system are also adopted by the energy recycle device in similar SWRO seawater desalination system, using discharge
High pressure concentrated seawater is pressurized to another strand of low pressure seawater, and this pressure exchange process makes high pressure concentrated seawater carry out pressure release heel row
Put, and the low pressure seawater being pressurized then through another boost in pressure pump so as to hydraulic pressure be promoted to identical with NF high pressure pump output pressure
Value, thus collectively as NF membranous system sea water water inlet.
In SWRO desalinization, because operating pressure is more than 5.5MPa, its energy recycle device needs using sufficiently thick
The super duplex steel material of degree；And for the present invention, because the operating pressure of NF film is usually no more than 3.8MPa, therefore it is to energy
The material of amount retracting device requires to be significantly reduced.Under the conditions of this operating pressure, completely can be using glass steel material as energy
The hydraulic cylinder of amount retracting device or pressure vessel, thus equipment investment can be reduced.
The sea water of salinity 35000mg/L carries out desalination through NF membranous system, and, up to 86-90%, water use efficiency can for its salt rejection rate
Reach 50% level, produce water salinity in 3500-4500mg/L level.Because operating pressure is substantially less than SWRO embrane method, this stage
The ton water consume electricity of NF film seawater desalination is in 1.3KWh level.
（3）Two grades of desalination unit
Two grades of desalination unit in the present invention mainly include the multistage multisection type frequently pole-reversing electricity through specific aim Energy-saving reformation
Dialysis（SEDR）Device, and supporting multiple-channel output direct current regulated power supply, booster pump, tubing and corresponding water tank.
Sea water after the effect of the equipment with high desalinization NF film of single stage desalting unit, its salinity will drop to 4500mg/L with
Under, belong to typical bitter water quality, its concentration is also conventional electrodialysis（EDR）The working range of Technical comparing economy.
Traditional EDR technology, with ion exchange membrane as core, belongs to electric drive membrane process.EDR passes through alternately arranged yin, yang
Ion exchange membrane and corresponding water flow partition board, constitute alternately arranged diluting compartment and enriched chamber.The anions and canons of current in diluting compartment
Carry out selective migration under the promotion of DC electric field, enter adjacent enriched chamber and be removed.The positive and negative electrode one of EDR device
As carry out periodically switching, become negative pole in lower half period in the positive pole in upper half period, light in upper half period
Changing room then becomes enriched chamber in lower half period, and vice versa.Thus, diluting compartment and the weak acid and weak base environment concentrating interior
Obtain cycle sex reversal, when switching such that it is able to avoid for a long time not carrying out electrode, weak base occurs after for a long time in certain compartment
Property environment and lead to local scaling, then run down so that process be subject to heavy damage.
For traditional, conventional EDR technology, the indoor operating mode in fact longtime running stability to device of electrode
Have a major impact.One is the effect due to electrode reaction, and negative pole is indoor can be because of the OH generating-Ion and assume alkalescence, be easiest to
Lead to fouling risk；Two is the Cl in cathode chamber endogenous cause of ill water-The Oxidation of ion generates Cl2Harmful gass, its be combined with water and
Generate strong oxidizer HClO, and negative pole interior then can generate O2.Furthermore, electrode chamber is different from diluting compartment and enriched chamber, its compartment
Thickness is typically far above diluting compartment, the thickness of enriched chamber, such as reaches 10mm thickness, and can be using larger, the non-conductive fish scale of thickness
Formula supports mesh sheet, and the therefore resistance of electrode chamber is much larger than the resistance of diluting compartment or enriched chamber.General EDR device is often multistage
Multisection type, has multipair electrode chamber, regards the difference of film logarithm in whole EDR device, and the resistance of electrode chamber accounts for whole EDR membrane stack
The ratio highest of resistance can reach 25% about.Therefore, by corrective measure, manage to significantly reduce the resistance of each electrode chamber
Advantageously reduce the resistance of whole EDR device, reduce process energy consumption.
In the present invention, important improvement has been carried out to the electrode chamber construction of conventional EDR device, that is, cancelled the PVC material of routine
Matter scale type supports mesh sheet, and electrode chamber thickness is thinned to below 3mm, and filling possesses conduction and ion exchange wherein
Ion Exchange Resin In The Mixing Bed.
Using thin electrode compartment and wherein fill Ion Exchange Resin In The Mixing Bed, the conduction of electrode chamber can be greatly improved
Ability, effectively reduces the power consumption of device.Additionally, the filling of resin can also reduce Cl respectively-、OH-The electrode of ion is anti-
Should, reduce harmful substance Cl2、HClO、O2Generation, beneficial to ensure device longtime running stability.
The SEDR device of two grades of desalination unit of the present invention is based on above-mentioned measure and the improvement of conventional EDR device is set
Meter, its operation equally takes the mode periodically switching electrode to run.Hand in the mixed bed ion of whole positive and negative electrode interior fillings
Change resin all using strong acid conductive by force, strong basic ion exchange resin, mix homogeneously before filling.Yin, yang resin used
Volume ratio is 1:1, thus ensureing the concordance of electrode chamber operating mode in the different cycles of the operation of falling pole.
The present invention provide SEDR efficient frequently pole-reversing electroosmosis device salt rejection rate can according to producing water water quality need into
Row mobility adjusts.For multistage multisection type SEDR device, only need to neatly adjust running voltages at different levels, electric current.Right
In the bitter water quality of 1500-5000mg/L, its salt rejection rate can reach 98.5%, and producing water salinity can as little as 50-65mg/L
Level.Due to significantly improving the conductive capability of electrode chamber, decrease the generation of harmful electrode reaction product, its process energy consumption
All it is obviously improved with operation stability.Using the device design of multistage multisection type, disregard the SEDR device of booster water pump power consumption
Body ton water consume electricity can control within 1.0KWh.
In the present invention, the desalination water of SEDR device is the product water of whole seawater desalination system, its condensed water salinity
Generally below 8000mg/L, and through pretreatment and NF membrane, has got rid of float, fine particle, colloid, macromole have
The calcium and magnesium of machine thing, microorganism and bivalence and sulfate ion, water quality is far superior to sea water raw water.Therefore, the concentration of SEDR device
Water is recycled to the water inlet of upstream NF membrance separation completely, that is, enter the product water tank of ultrafilter membrane, such that it is able to improve the water of whole system
Utilization rate.
Additionally, unlike the integrated desalination technology of Multistage Membranes similar from other, two grades of desalination unit in the present invention
Using SEDR technology, as conventional EDR, representative value is in 0.1-0.3MPa, thus adopts UPVC plastics completely for its operating pressure
Pipe-line system, need not be using the expensive pressure material such as the rustless steel of high pressure reverse osmosiss or nanofiltration system, dual phase steel, super duplex steel
Material, and there is not etching problem.
Each ingredient in the present invention integrates, and can produce following effect：
Conventional coagulating sedimentation, acidifying regulation, dosing, sand filtration and ultrafilter membrane pretreatment, can go various trickle in eliminating water
The impurity such as granule, float, colloid, larger molecular organicses, microorganism, reduce turbidity and the colourity of sea water raw water, protect downstream
NF film；The NF film containing energy recycle device of single stage desalting unit can continuously and stably remove nearly 90% salt ion, and institute
The ion obtaining in permeate is mainly monovalence salt ion.The operating pressure of NF desalination system as little as 3.8MPa, its energy regenerating fills
Put and adopt glass steel material, effectively reduce equipment investment；The water yield of NF system reaches 50% level, produces water salinity and is less than
4500mg/L.The SEDR enhanced type frequently pole-reversing electroosmosis device of two grades of desalination unit, in the low pressing operation of 0.1-0.3MPa,
Using cheap, corrosion resistant UPVC plastic pipe；The electrode chamber of SEDR is slim compartment, and is filled with mixed bed ion friendship wherein
Change resin, more conventional EDR device significantly reduces electrode chamber resistance；SEDR device can optionally adopt the Water flow-path of multistage multisection type
Design, highest salt rejection rate can reach 98.5%, and ton water body power consumption is less than 1.0KWh；The condensed water of SEDR is recycled to completely
Water tank is produced in upstream ultrafiltration, as the water inlet of NF film, to improve NF film influent quality and system water use efficiency.With salinity
The sea water of 35000mg/L is raw water, will be mutually integrated with energy-saving SEDR device for equipment with high desalinization NF film, whole seawater desalination system
Ton water body power consumption be less than 2.2KWh, water yield nearly 40%；NF stages operating pressure as little as 3.8MPa, SEDR are then complete
Using conventional UPVC material tubing, it is achieved thereby that the sea water of low power consuming, Low investment, low operating pressure and low corrosion-resistant requirement is light
Change.
Brief description
Fig. 1 is the process chart of integrated membrane process desalinization provided by the present invention.
In figure：
1- sea water raw water；2- coagulative precipitation tank；3- settling pool；4- sand filter；5- ultrafilter membrane；6- high-pressure pump；7- energy returns
Receiving apparatus；8- boost in pressure pump；9- NF membrane；10- nanofiltration condensed water；11- reinforced electric electrodialysis apparatus；12- voltage stabilization and current stabilization is straight
Stream power supply；13- lightening products water；14- electrodialysis condensed water.
Specific embodiment
Below in conjunction with the accompanying drawings and embodiment the invention will be further described.Embodiment is to be illustrative rather than definitive thereof this
Bright described integrated membrane process method for desalting seawater.
Embodiment 1：
For pretreatment unit, sea water raw water 1 enters coagulative precipitation tank 2 by the effect of elevator pump first, poly- through adding
The routine coagulation such as acrylamide, flocculation medicament carry out precipitating, enter settling pool 3 after turbidity removal, carry out acidifying and adjust in settling pool,
Its pH is made to be reduced between 6.5-7.0.Sea water clear water enters sand filter 4 by booster pump further and is filtered, and sand filter 4 is by two
Level sand filtration is in series, and filter medium used is quartz sand, and its particle diameter is respectively 1.0-2.0mm and 0.5-1.0mm.First order sand
Before filter, carry out pipeline and add strong oxidizer sodium hypochlorite sterilizing and algae-removing online, between second level sand filter and ultrafilter membrane 5
Line adds reducing agent NaHSO3, eliminate remaining oxidant, the ultrafilter membrane in protection downstream.
Sea water clear water in settling pool 3 successively enters sand filter 4 and hyperfiltration membrane assembly 5 through ultrafiltration booster pump.Using 2 groups altogether
4 8040 specification Kynoar（PVDF）The polysulfone hollow fiber ultrafiltration membrane system of material, every group each 2 to realize mutual backwash
Function.
Nanofiltration desalination device in single stage desalting unit adopts the NF90-4040 NF membrane 9 of DOW chemical company, using 5
3 core glaze steel pressure vessels, with the arrangement of " 3-2 " combined method one-level two-part, series connection in each pressure vessel loads 3
NF90-4040 model NF film, 15 altogether.The condensed water of 3 pressure vessels of first paragraph is as 2 pressure vessels of second segment
Water inlet.NF high-pressure pump 6 water flow is 20.0L/m, and another strand of low pressure seawater is through energy recycle device 7 and boost in pressure pump 8
Jointly enter 3 NF membrane pressure vessels of first paragraph afterwards with the water outlet of high-pressure pump 6, low pressure seawater flow is 26.0L/m, i.e. NF system
Total flow of inlet water of uniting is 46.0L/m（I.e. 2.76m3/h）.
NF high-pressure pump 6 adopts plunger displacement pump, export pressure, and that is, the inlet pressure of first paragraph NF film is 3.8MPa.Firstth,
The intermembranous concentrated water pressure of two-stage nitration NF is 3.75MPa, and the condensed water outlet pressure of second segment NF film is 3.7MPa, and this is energy regenerating
The intake pressure of the high pressure concentrated seawater of device 7.The low pressure seawater of energy recycle device 7 is intake by the pressure with high pressure concentrated seawater
Exchange interaction reclaims the high pressure kinetic energy of the latter, and its water outlet equally rises to 3.8MPa through boost in pressure pump 8, with high-pressure plunger pump 6
Water outlet is combined into NF membrane pressure vessel.Under conditions of embodiment 1, the desalination water yield of NF device is 19.3L/m, with high pressure
The flow of inlet water of pump 6 is roughly the same, and the flow of high pressure concentrated seawater is 26.7L/m, the flow of inlet water substantially phase with low pressure seawater
When.The water use efficiency of NF device is 19.3/46, that is, 42%.
The operating parameter of NF device, power consumption, influent quality and producing water water quality are as shown in table 1：
The operating parameter of table 1 NF seawater desalination and water-in and water-out water quality
In this embodiment 1, total salt rejection rate of the sea water clear water to salinity 32749.0mg/L for the NF film reaches 89.2%, with electricity
The salt rejection rate that conductance calculates is 90.3%, to Na+、Cl-The removal efficiency of ion all reaches 89%, and the Ca to bivalence2+、Mg2+、SO4 2-
The removal efficiency of ion then reaches 99.5-99.6%.System water yield 42%, closely conventional high pressure reverse osmosiss SWRO sea water is light
The level of change technology, and will height compared with the level of low temperature multiple-effect distillation MED technology 33% about.
The desalination water of NF enters intermediate water tank, enters SEDR device 11 by the supercharging pumping action of two grades of desalination unit.This reality
Apply in example, SEDR device 11 adopts three-level six segmentation Water flow-path, and each section is one-level two-part flow process, all include a pair independently
Electrode, its voltage/current all can independent regulation.In 6 electrode chambers of whole 3 pairs of electrodes, electrode chamber thickness is 3mm,
All packing volume ratios are for 1:1 mixed bed strong acid and strong base ion exchange resin.Dividing plate specification used by SEDR device 11 is 400*
800mm standard specificationss, total film logarithm is 250.The electrode water of SEDR device, using the fresh water being pre-configured with, is excluding electrode reaction
The gas Posterior circle generating uses.The desalination water of SEDR device 11 and condensed water raw water are the desalination water of NF film, and total Water is
25L/m.Because the desalination discharge of upstream NF device only has 19.3L/m it is impossible to continuously meet the water demand of SEDR device, because
During this practical operation, NF desalter is continuous operation, and SEDR device then shut down when not enough by water level in intermediate water tank.Due to
SEDR device operating pressure is very low, therefore regularly shuts down, start can't produce other adverse effects to system.SEDR's is light
Change the lightening products water that water 13 is whole system, the condensed water 14 of SEDR is then recycled to upstream sea water settling pool.SEDR device
Operating parameter, power consumption, water quality parameter as shown in table 2：
The operating parameter of table 2 SEDR seawater desalination and water-in and water-out water quality
In this embodiment, SEDR device aquifer yield reaches 17L/m, i.e. 1.02m3/ h, it produces water conductivity as little as 144.0 μ
S/cm, produces the total salinity TDS as little as 83.0mg/L of water, the relatively salinity of sea water clear water 32749mg/L, whole system de-
Salt rate reaches 99.75%.Condensed water 14 salinity of SEDR device is only 15405mg/L, the substantially less than saliferous of sea water clear water
The condensed water 14 of SEDR device is recycled to sea water clear water reserviors when therefore continuously running, can improve entering of NF device by amount completely
Water water quality, and improve system water use efficiency.In the case of not considering that SEDR concentrates Water Sproading, the continuous aquifer yield of NF device reaches
19.3L/m, i.e. 1158L/h, power consumption is 1.3KWh/m3；Continuous water consumption 25L/m of SEDR device, i.e. 1500L/h, power consumption
For 0.77KWh/ (m3Product water).It can be seen that, if for large scale system, when the water consumption phase of aquifer yield and the SEDR device of NF device
Deng when, whole NF and SEDR device then can continuously run, and its maximum power consumption should be 1.3*1.5/1.158+0.77, that is,
2.45KWh/(m3Product water).In practice because the concentration Water Sproading of SEDR can improve influent quality to a certain extent, because
This ton of water consume electricity will be less than 2.4 degree, and this is less than the power consumption of conventional SWRO method desalination process.
Embodiment 2
In the present embodiment, the NF device operating parameter of pretreatment and single stage desalting unit all keeps constant, SEDR device
Flow, pressure condition also in the same manner as in Example 1, only change SEDR device voltage at different levels, electric current, suitably reduce SEDR dress
The salt rejection rate put, but still keep it to produce water salinity and belong in the range of preferable drinking water quality.SEDR device in embodiment 2
Operating parameter, power consumption, water quality parameter are as shown in table 3：
The operating parameter of table 3 SEDR seawater desalination and water-in and water-out water quality
Compared with Example 1, suitable reduction SEDR device running voltage at different levels, electric current, its fresh water are passed through in embodiment 2
Electrical conductivity 410 μ S/cm, TDS are 241mg/L, salt rejection rate 99.26%, and ton water consume electricity is reduced to 0.52KWh/m3, compared with embodiment 1
The power consumption of middle SEDR saves 0.25KWh/m3.Obviously, when desalination water being prepared with the scheme of embodiment 2, whole desalinization
The body power consumption of system will be less than 2.15 KWh/m3.Compared with document US 2010/0089756 A1 report, it adopts
Simulated seawater raw water electrical conductivity 45500 μ S/cm, less than the level of the present embodiment 48000 μ S/cm, salt rejection rate about 98.6%, produces water
TDS240mg/L, the two is substantially suitable, power consumption 1.85KWh/m3.Both power consumption differ less than 0.2-0.3KWh, this and two
The difference of person's sea water raw water salinity essentially in proportion, but the former adopt for simulated seawater, and the present embodiment uses
Actual sea water, in addition to having various inorganic ionss in raw water, also including certain organic impurities.This explanation, is carried with the present invention
For based on " NF/SEDR " integrated membrane process be core desalination process, its body power consumption, water yield all with above-mentioned literary composition
" NF/IE/CEDI " in offering quite, and salt rejection rate also slightly advantage.Both compare, and " NF/SEDR " technological process is more simple,
Cost is lower, and the slim dividing plate of relative usage 1.5mm left and right thickness leads to resin filling difficult, and be difficult to extensive, convenient
For the CEDI of ground industrialized production, SEDR device that the present invention provides only need in electrode chamber potting resin, and electrode chamber is thick
Degree 3mm, filling difficulty is little, and whole machine assembling is convenient and swift to produce it is easier to beat technical scale metaplasia.With existing conventional seawater reverse osmosis
SWRO membrane technology is compared thoroughly, the desalination process based on " NF/SEDR " integrated membrane process that the present invention provides, and operating pressure shows
Write and reduce, and SEDR more only need to adopt plastic pipe, anti-corrosion, seal aspect the requirement of whole system all significantly reduces, operation
Safety improves, and the producing water water quality of SEDR also can motor-driven adjust, and overall salt rejection rate is all adjustable between 99-99.75%, ton water body
Power consumption is minimum to be less than 2.15 degree, the substantially less than energy consumption of SWRO desalinization, the investment of therefore whole desalting process
All effectively reduce with operating cost, and operate more simple and convenient, longtime running stability is higher.
Finally it should be noted that：Above example is for described integrated membrane process method for desalting seawater is described, rather than limit
The integrated membrane process method for desalting seawater that the present invention processed provides.Those skilled in the art should be understood：It still can be to front
State the technical scheme described in embodiment and carry out various changes and deformation, or wherein some or all of technical characteristic is carried out
Equivalent, and these change and deform, and without departing from the spirit of the present invention, all should belong to claims institute of the present invention
The scope of definition.
Claims (4)
1. a kind of integrated membrane process method for desalting seawater, with sea water as raw water, sequentially passes through pretreatment, single stage desalting unit and two
Level three ingredients of desalination unit and be obtained desalination water it is characterised in that taking following integrated membrane process technique：
(1) pretreatment unit is formed using " coagulating sedimentation-sand filtration-ultrafilter membrane " integrating process, and first laggard before ultrafilter membrane
Row acidifying is adjusted and strong oxidizer, the adding of reducing agent, and wherein acidifying is adjusted and adding of strong oxidizer is being made through coagulating sedimentation
With sea water enter downstream sand filter before carry out, reducing agent adds before the sea water through sand filters enters ultrafilter membrane；
(2) single stage desalting unit is become with boost in pressure pump group using NF membrane, high-pressure pump, energy recycle device, to sea water clear water
Carry out single stage desalting；
(3) adopt frequently pole-reversing electroosmosis system to be two grades of desalination unit, two are carried out to the nanofiltration desalination water of single stage desalting unit
Secondary desalination, frequently pole-reversing electroosmosis device used is multistage multisection type flow process, and at different levels all containing can independent regulation voltage x current
1 pair of electrode, and be filled with strong acid and strong base Ion Exchange Resin In The Mixing Bed in electrode interior.
2. a kind of integrated membrane process method for desalting seawater according to claim 1 is it is characterised in that NF membrane used is tool
Standby seawater desalination rate reaches the high desalination NF membrane of 85% level above.
3. a kind of integrated membrane process method for desalting seawater according to claim 1 is it is characterised in that the behaviour of NF membrane used
Make pressure and be less than 4.0MPa.
4. a kind of integrated membrane process method for desalting seawater according to claim 1 is it is characterised in that frequently pole-reversing used is electric
The thickness of each electrode chamber of electrodialysis apparatus is less than 5mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510322192.2A CN104909503B (en) | 2015-06-12 | 2015-06-12 | A kind of integrated membrane process method for desalting seawater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510322192.2A CN104909503B (en) | 2015-06-12 | 2015-06-12 | A kind of integrated membrane process method for desalting seawater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104909503A CN104909503A (en) | 2015-09-16 |
| CN104909503B true CN104909503B (en) | 2017-03-01 |
Family
ID=54079015
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510322192.2A Active CN104909503B (en) | 2015-06-12 | 2015-06-12 | A kind of integrated membrane process method for desalting seawater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104909503B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106865807A (en) * | 2015-12-10 | 2017-06-20 | 金達行有限公司 | A kind of multisection type reverse osmosis of by-product high concentration strong brine |
| CN107902800A (en) * | 2017-12-01 | 2018-04-13 | 山东省盐业集团有限公司 | Salt production embrane method sea brine concentration method |
| CN110937728A (en) * | 2018-09-25 | 2020-03-31 | 国家能源投资集团有限责任公司 | Desulfurization wastewater treatment method and system |
| CN109502709B (en) * | 2019-01-16 | 2022-04-15 | 天津碧水源膜材料有限公司 | Water purifier capable of producing alkalescent electrodialysis water and method for manufacturing alkalescent water |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101723491A (en) * | 2009-11-12 | 2010-06-09 | 南开大学 | Electrodeionization method and device for basic working unit containing three compartments |
| CN101967026A (en) * | 2010-09-03 | 2011-02-09 | 葛文宇 | Energy-saving emission-reduction seawater comprehensive utilizing method |
| US8999171B2 (en) * | 2011-07-18 | 2015-04-07 | Hl Seawater Holdings, Llc | Membrane and electrodialysis based seawater desalination with salt, boron and gypsum recovery |
| CN103304078A (en) * | 2013-07-09 | 2013-09-18 | 南开大学 | Laboratory wastewater treatment process equipment and wastewater treatment method using same |
| CN104016530B (en) * | 2014-06-05 | 2016-08-24 | 中国科学院过程工程研究所 | A kind of high saliferous advanced treatment of industrial waste water and the method for desalination reuse |
-
2015
- 2015-06-12 CN CN201510322192.2A patent/CN104909503B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN104909503A (en) | 2015-09-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Ye et al. | Loose nanofiltration-based electrodialysis for highly efficient textile wastewater treatment | |
| CA2663906C (en) | Method and apparatus for desalination | |
| Honarparvar et al. | Frontiers of membrane desalination processes for brackish water treatment: A review | |
| CN105502756B (en) | A kind of water-soluble liquid treating system and its processing method of the easy scale-forming ion containing concentration | |
| CN103936202B (en) | A kind of method for desalting brackish water and device thereof | |
| CN107055713A (en) | One kind is based on the selectively electrodialytic high rigidity brackish water method for concentration of univalent cation | |
| KR100874269B1 (en) | High efficiency seawater electrolysis apparatus and electrolysis method including pretreatment process | |
| CN104909503B (en) | A kind of integrated membrane process method for desalting seawater | |
| CN106315935B (en) | Water quality desalting plant and the method for desalinating water quality using the device | |
| CN105254083A (en) | Process and system for treating high salinity wastewater in coal chemical industry | |
| CN105198133A (en) | Ultra-pure water preparation system and method capable of preventing electrodeionization device from scaling | |
| EP2429678A1 (en) | Brine treatment scaling control system and method | |
| CN108793517A (en) | A kind for the treatment of process of high COD leather-making waste waters with high salt | |
| CN106966536A (en) | Strong brine zero-emission film concentration technology and equipment | |
| CN109250846A (en) | A kind of brine waste processing system inhibiting fouling | |
| Liu et al. | Energy-saving “NF/EDR” integrated membrane process for seawater desalination. Part II. The optimization of ED process | |
| CN101935111A (en) | Wastewater recycling preparation system with low energy consumption | |
| CN211972026U (en) | Ultrapure water preparation system for laboratory | |
| CN210915600U (en) | Recycling device of RO strong brine | |
| Xia et al. | An innovative beneficial reclamation of flue gas desulfurization brine using bipolar membrane electrodialysis technique | |
| Khoiruddin et al. | Polymeric membranes in electrodialysis, electrodialysis reversal, and capacitive deionization technologies | |
| CN114873816A (en) | Phosphate waste water zero release processing system | |
| CN204174021U (en) | High purity water treatment unit | |
| CN204174025U (en) | Multi-functional pure water treatment unit | |
| CN105236658A (en) | Method and system for preparing salt from seawater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200714 Address after: No.3 building-1-907, No.1, Huake Third Road, Haitai, Huayuan Industrial Zone, Binhai New Area, Tianjin Patentee after: TIANJIN ZHONGLING WATER SYSTEM TECHNOLOGY Co.,Ltd. Address before: 300071 Tianjin City, Nankai District Wei Jin Road No. 94 Patentee before: NANKAI University |
|
| TR01 | Transfer of patent right |