CN107459106A - A kind of electrochemistry membrane-separation water treatment device and its processing method and purposes - Google Patents
A kind of electrochemistry membrane-separation water treatment device and its processing method and purposes Download PDFInfo
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- CN107459106A CN107459106A CN201710864744.1A CN201710864744A CN107459106A CN 107459106 A CN107459106 A CN 107459106A CN 201710864744 A CN201710864744 A CN 201710864744A CN 107459106 A CN107459106 A CN 107459106A
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- C—CHEMISTRY; METALLURGY
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
Abstract
The invention provides a kind of electrochemistry membrane-separation water treatment device and its processing method and purposes, described device includes reaction tank, membrane module is set in the reaction tank, the membrane module side sets induction electrode and positive plate parallel to membrane module from inside to outside, the membrane module opposite side sets minus plate parallel to membrane module, and the anode plate and cathode plate are connected with external power supply；The reaction tank body side is provided with water inlet, and membrane module delivery port is opened up on the reactor body, and the membrane module delivery port is connected with membrane module.Field effect, electrochemical oxidation, electric flocculation and electric floating are carried out integrated combination by the present invention, acted on by electroxidation and electric flocculation, change pollutant structure, regulation desirable particle size size, hydrophilic and porous cake layer is formed on film surface, decelerating membrane pollution, separation of solid and liquid is carried out by membrane filtration, further lifts effluent quality.
Description
Technical field
The invention belongs to drinking water or sewage treatment area, is related to a kind of electrochemistry-membrane-separation water treatment device and its place
Reason method and purposes.
Background technology
Ultra filtration membrane technology has good crown_interception using volume exclusion effect to the pollutant more than membrane pore size,
But simultaneously as retention pollutant in the accumulation on film surface and water body microorganism film surface growth, formed fouling membrane,
The service life of film is reduced, improves the application cost of membrane separation technique.In order to extend the service life of film, before UF membrane
The means pre-processed to water body have been found effective.Conventional preprocessing means have the hands such as pre- flocculation, pre-oxidation, preaeration
Section, wherein flocculation, pre-oxidation are more universal in advance.
Electric flocculation, electroxidation are widely used in electro-chemical water process field, are always the emphasis of scientific research.Wherein electricity wadding
It is solidifying by controlling electrochemical parameter and physical and chemical properties of water, can adjust flocculant dosage in electric flocculation, flocculu shape with
Structure.With the increasingly raising of water standard, electric flocculation technique needs excessively to add flocculant, or combines other advanced treatings
Technology is to reach standard of drainage.In the prior art, UF membrane is proved that electric flocculation effluent quality can be effectively improved.Meanwhile
The abbreviated system of electric flocculation-UF membrane eliminates precipitation link, in actual applications more advantage.
Electroxidation can adjust the response path in electro-oxidation process by controlling electrochemical parameter and physical and chemical properties of water
With reaction rate.Electroxidation is divided into direct oxidation and indirect oxidation.Direct oxidation is that in electrode surface electrochemistry occurs for pollutant
Oxidation reaction.Indirect oxidation is that the chlorion in solution is oxidized to Active Chlorine first, is then aoxidized by Active Chlorine.
The combination of electrochemistry and membrane technology has received significant attention, and an important directions of water treatment technology reform.
At present, the principle for alleviating fouling membrane using electrochemical means mainly has：1) increase desirable particle size, reduce film caused by little particle
Hole plug；2) pre-removal partial contamination thing, film surface contaminant accumulation is reduced；3) flocculu shape is adjusted, is formed more loose porous
Cake layer, reduce Specific Cake；4) change contaminant molecule structure and size, form more hydrophilic cake layer；5) electric field is utilized
The cake layer of inductive formation polarization, improves cake layer hydrophily, reduces Specific Cake；6) micro- gas caused by electrode reaction is utilized
Bubble, washes away film surface, further alleviates fouling membrane.But the problem of energy consumption is higher is still suffered from, and existing electrochemistry and membrane technology
The mode being combined, still have much room for improvement in terms of fouling membrane is sustained.
The content of the invention
For problems of the prior art, the invention provides a kind of electrochemistry-membrane-separation water treatment device, processing
Method and application thereof.The present invention is led to by the way that field effect, electrochemical oxidation, electric flocculation and electric floating are carried out into integrated combination
Electroxidation and electric flocculation effect are crossed, changes pollutant structure, regulation desirable particle size size, is formed on film surface hydrophilic and porous
Cake layer, decelerating membrane pollution, by membrane filtration carry out separation of solid and liquid, further lift effluent quality.The present invention passes through sensing
Electric flocculation acting regulatory flocculu shape and structure, accumulation of the pollutant on film surface is reduced, while dirt is controlled by electrode reaction
The directly or indirectly oxidation of thing is contaminated, changes the molecular structure and polarity of pollutant, high pore structure and hydrophilic is formed on film surface
The cake layer of property.And the cake layer polarity enhancing, further enhancing cake layer due to the polarization by electric field between pole plate
Water-wet behavior, further slow down fouling membrane.
To use following technical scheme up to this purpose, the present invention：
In a first aspect, the invention provides a kind of electrochemistry-membrane-separation water treatment device, described device includes reaction tank,
Membrane module is set in the reaction tank, and the membrane module side sets induction electrode and anode parallel to membrane module from inside to outside
Plate, the membrane module opposite side set minus plate parallel to membrane module, and the anode plate and cathode plate are connected with external power supply；
The reaction tank body side is provided with water inlet；Membrane module delivery port, the film are opened up on the reactor body
Component delivery port is connected with membrane module.
In the present invention, induction electrode is set in the electrochemistry-membrane-separation water treatment device, effect be electroxidation and
Electric flocculation PROCESS COUPLING is to same electrochemical reaction system.Anode is as oxidizing electrode, partial organic substances of directly degrading, simultaneously
Active Chlorine indirect oxidation pollutant is produced, and is suppressed growth of microorganism；Induction electrode is set between anode and cathode, induction electrode by
The induction of electric field, sensing electric flocculation occurs, forms thick, porous, loose flco, loose porous filter cake is formed on film surface
Layer, prevent pollutant from being contacted with the direct of film surface, suppress fouling membrane.
When anode and induction electrode are applied in electrochemical membrane reactor simultaneously, its electroxidation and electric flocculation mistake for occurring
Regulation and control of the journey to the forming process of cake layer have synergy.There is higher surface pore in the cake layer that film surface is formed
Rate, substantially increase the quantity in cake layer duct.The hydrophily of filter cake layer surface is enhanced simultaneously.Therefore this synergy has
Help decelerating membrane pollution, improve water flux.
When electroxidation is combined with UF membrane, pollutant is degraded by directly or indirectly oxidizing process.Degradation process changes
Pollutant molecular structure and polarity, cause generation cake layer there is higher hydrophily.In addition, caused by indirect oxidation
Active Chlorine can suppress the growth of microorganism in water body, further decelerating membrane pollution.Electroxidation, which has, improves cake layer hydrophily
With sterilization double action, it is thus possible to effectively reduce fouling membrane.That is, electric flocculation, electroxidation and UF membrane are carried out one by the present invention
Bodyization combines, and changes particulate matter size, molecular structure and polarity in water by flocculation and oxidation, adjusts cake layer
Pore structure and hydrophily, and then effectively alleviate fouling membrane, while improve effluent quality.
Currently preferred technical scheme is used as below, but not as the limitation of technical scheme provided by the invention, is passed through
Following technical scheme, it can preferably reach and realize the technical purpose and beneficial effect of the present invention.
As currently preferred technical scheme, the positive plate is titanium ruthenium electrode.
Preferably, number >=1 of the positive plate.
In the present invention, using titanium ruthenium electrode as anode, relative to traditional iron material, aluminium, titanium or zinc material, titanium ruthenium electrode
For dimensionally stable anode, arc is higher, and electrochemical oxidation reactions preferentially occur for the pollutant in the aqueous solution.
As currently preferred technical scheme, the induction electrode is sensing aluminium electrode or sensing iron electrode.
Preferably, number >=1 of the induction electrode.
As currently preferred technical scheme, the minus plate is aluminium negative electrode, iron cathode or stainless steel cathode.
Preferably, number >=1 of the minus plate.
As currently preferred technical scheme, the membrane module is curtain Flat Membrane or hollow-fibre membrane；
Preferably, the membrane component in the membrane module is any one in microfiltration membranes, milipore filter or NF membrane or at least two
The combination of kind, the typical but non-limiting example of combination have：The combination of microfiltration membranes and milipore filter, milipore filter and NF membrane
Combination, combination of microfiltration membranes, milipore filter and NF membrane etc..
Second aspect, the invention provides the processing method of above-mentioned electrochemistry-membrane-separation water treatment device, methods described
For：
(a) sewage is passed through, starts electrochemical appliance, adjusts electrochemical parameter and UF membrane parameter, carries out electric flocculation, electrification
Oxidation and electrolytic process are learned, cake layer is formed on membrane module surface；
(b) start power set, carry out membrane filtration processing, the water body after processing is discharged from membrane module delivery port.
In the present invention, carried out using described device in water treatment procedure, pre-oxidation, pollutant are carried out under electric field action
Degrade, molecular structure and polarity change；Meanwhile flocculated using electrochemistry and change the size of particulate matter, regulate and control flco
Characteristic, make flco loose porous；Flco is accumulated in film surface under hydraulic action, forms hydrophilic and loose porous cake layer；
Finally, the cake layer improves water-wet behavior under electric field action.
As currently preferred technical scheme, electric flocculation parameter is adjusted described in step (a) is：Adjusting current density is
5A/m2~50A/m2, such as 5A/m2、10A/m2、15A/m2、20A/m2、25A/m2、30A/m2、35A/m2、40A/m2、45A/m2Or
50A/m2Deng it is not limited to cited numerical value, other interior unrequited numerical value of the number range are equally applicable, preferably
10A/m2。
Preferably, adjusting film separation parameter described in step (a) is：Regulation transmembrane pressure is 20kPa~50kPa, such as
20kPa, 25kPa, 27kPa, 30kPa, 33kPa, 35kPa, 40kPa, 43kPa, 45kPa, 47kPa or 50kPa etc., but simultaneously not only
It is limited to cited numerical value, other unrequited numerical value are equally applicable in the number range, and preferably transmembrane pressure is 30kPa.
In the present invention, by adjusting the parameter of electric flocculation during electric flocculation, the hole of formed cake layer can be controlled
Footpath and the spatial distribution in hole, ensure to retain pollutant while water penetration.Thus, current density and transmembrane pressure during electric flocculation
Difference is both needed to control within the specific limits.
If current density is too high, flocculant concentration can be made excessive, the unnecessary flco of formation causes fouling membrane on the contrary；Electric current is close
Spend low, flocculation can be made incomplete, decelerating membrane pollution effect is deteriorated；
If transmembrane pressure is too high, water outlet water degradation can be made；Transmembrane pressure is too low, can reduce sewage load.
As currently preferred technical scheme, the sewage load described in step (a) is 200Lm-2·h-1~
20000L·m-2·h-1, such as 200Lm-2·h-1、500L·m-2·h-1、1000L·m-2·h-1、3000L·m-2·h-1、
5000L·m-2·h-1、7000L·m-2·h-1、10000L·m-2·h-1、13000L·m-2·h-1、15000L·m-2·h-1、
17000L·m-2·h-1Or 20000Lm-2·h-1Deng it is not limited to cited numerical value, in the number range, other are not
The numerical value enumerated is equally applicable, preferably 3000Lm-2·h-1。
In the present invention, pass through described device and method, under the electrochemical parameter and UF membrane Parameter Conditions, formation
The contact angle of cake layer and membrane module is 60 °~70 °.Herein, the contact angle refers to be made at gas, liquid, solid three-phase intersection point
Liquid-vapor interface angle theta of the tangent line through liquid and solid-liquid boundary line, be measuring for wetness degree.The contact angle
Smaller, wetness degree is bigger, shows that its surface hydrophilic performance is better, the contamination resistance of milipore filter is stronger.
Meanwhile the apparent porosity of the cake layer formed is 16%~20%, aperture is 8nm~15nm, this demonstrate
The cake layer water penetration that the method for the invention is formed is preferable, and the aperture of the cake layer is less than the aperture of membrane module used,
It is more beneficial for preventing blocking inside fenestra.
The third aspect, the invention provides the purposes of above-mentioned electrochemistry-membrane-separation water treatment device, the electrochemistry-film
Separation water treatment facilities is applied to drinking water and sewage treatment area.
Compared with prior art, the invention has the advantages that：
(1) present invention is by field effect, electrochemical oxidation and induced electricity flocculation, change contaminant molecule structure,
Desirable particle size size is controlled, loose porous and hydrophily enhancing cake layer is formed on film surface, greatly alleviates fouling membrane
And lift effluent quality；
(2) electric flocculation, electroxidation and UF membrane have been carried out integrated combination by the present invention, and the structure of reactor of invention is tight
Gather, compared to the two part arrangement of traditional electric flocculation-UF membrane or electroxidation-UF membrane, effectively alleviating the same of fouling membrane
When be also greatly saved space reactor occupation of land；
(3) present invention can form cake layer loose porous and with high-hydrophilic on the film surface in reactor, can
Decelerating membrane pollution, improve flux (compare ECMR and improve 10%~15%)；Be advantageous to waterpower backwash, membrane flux after backwash simultaneously
Recovery situation more preferably, effectively extends film service life.
Brief description of the drawings
Fig. 1 is the structural representation of electric flocculation-membrane-separation water treatment device of the present invention；
Fig. 2 is that caudacoria flux vs figure is polluted in 1-3 of the embodiment of the present invention and comparative example 1-7；
Wherein, 1- positive plates, 2- induction electrodes, 3- minus plates, 4- membrane modules, 5- reaction tanks, 6- water inlets, 7- backwater
Mouthful, 8- membrane module delivery ports, 9- external power supplys.
Embodiment
For the present invention is better described, technical scheme is readily appreciated, below to the present invention further specifically
It is bright.But following embodiments is only the simple example of the present invention, the scope of the present invention is not represented or limits, this
Invention protection domain is defined by claims.
Specific embodiment of the invention part provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, such as
Shown in Fig. 1, described device includes reaction tank 5, sets membrane module 4 in the reaction tank 5, the side of membrane module 4 is from inside to outside
Induction electrode 2 and positive plate 1 are set parallel to membrane module 4, the opposite side of membrane module 4 sets minus plate parallel to membrane module 4
3, the positive plate 1 and minus plate 3 are connected with external power supply 9；
The body side of reaction tank 5 is provided with water inlet 6, and water return outlet 7 is provided with water inlet opposite side；The reactor
Membrane module delivery port 8 is opened up in 5 main bodys, the membrane module delivery port 8 is connected with membrane module 4.
Its processing method is：
(a) sewage is passed through, starts electrochemical appliance, adjusts electric flocculation parameter, carries out electric flocculation, electrochemical oxidation and electrolysis
Process, cake layer is formed on the surface of membrane module 4；
(b) start power set, carry out membrane filtration processing, the water body after processing is discharged from membrane module delivery port 8.
It is below present invention typical case but non-limiting example：
Embodiment 1：
A kind of electrochemistry-membrane-separation water treatment device and its processing method are present embodiments provided, described device includes anti-
Pond 5 is answered, membrane module 4 is set in the reaction tank 5, the side of membrane module 4 sets induced electricity parallel to membrane module 4 from inside to outside
Pole 2 and positive plate 1, the opposite side of membrane module 4 parallel to membrane module 4 set minus plate 3, the positive plate 1 and minus plate 3 with
External power supply 9 connects；
The body side of reaction tank 5 is provided with water inlet 6, and water return outlet 7 is provided with water inlet opposite side；The reactor
Membrane module delivery port 8 is opened up in 5 main bodys, the membrane module delivery port 8 is connected with membrane module 4.
Wherein, the positive plate 1 is titanium ruthenium electrode；The number of positive plate 1 is 1.
The induction electrode 2 is sensing aluminium electrode；The number of induction electrode 2 is 1.
The minus plate 3 is aluminium negative electrode；The number of minus plate 3 is 1.
The membrane module 4 is curtain Flat Membrane；Membrane component in membrane module 4 is microfiltration membranes.
Drinking water is handled using described device, TOC contents are 5ppm, turbidity 38NTU in the drinking water, its
Treating capacity is 2500Lm-2·h-1。
The processing method is：
(a) pending reference water is passed through from the water inlet 6 of reaction tank 5, starts electrochemical appliance, regulation current density is
5A/m2, transmembrane pressure 30kPa, electric flocculation, electrochemical oxidation and electrolytic process are carried out, filter cake are formed on the surface of membrane module 4
Layer；
(b) start power set, carry out membrane filtration processing, the water body after processing is discharged from membrane module delivery port 8.
In the present embodiment, membrane flux is 1965Lm after being polluted in step (a)-2·h-1, contact angle is 67.75 °, filter cake
The apparent porosity of layer is 16.73%, and the aperture of cake layer is 10nm.
TOC contents are 0~0.5ppm in the drinking water obtained after processing, and turbidity is down to 0NTU, separated from contaminants efficiency
For 98%.
Embodiment 2：
Present embodiments provide a kind of electrochemistry-membrane-separation water treatment device and its processing method, the structure of described device
With reference to embodiment 1, difference is：The number of positive plate 1 is 2, and the number of minus plate 3 is 2, and the membrane module 4 is hollow
Tunica fibrosa；Membrane component in membrane module 4 is milipore filter.
Trade effluent is handled using described device, wherein TOC contents are 450ppm, turbidity 60NTU, and its treating capacity is
3000L·m-2·h-1。
With reference to embodiment 1, difference is the processing method：Regulation current density is 10A/m in step (1)2, transmembrane pressure
Difference is 35kPa.
In the present embodiment, membrane flux is 2463Lm after being polluted in step (a)-2·h-1, contact angle is 64.22 °, filter cake
The apparent porosity of layer is 14.77%, and the aperture of cake layer is 13nm.
TOC contents are 1ppm in the drinking water obtained after processing, and turbidity is down to 0NTU, and separated from contaminants efficiency is
97%.
Embodiment 3：
Present embodiments provide a kind of electrochemistry-membrane-separation water treatment device and its processing method, the structure of described device
With reference to embodiment 1.
Trade effluent is handled using described device, wherein TOC contents are 450ppm, turbidity 60NTU, and its treating capacity is
3500L·m-2·h-1。
With reference to embodiment 1, difference is the processing method：Regulation current density is 15A/m in step (1)2, transmembrane pressure
Difference is 25kPa.
In the present embodiment, membrane flux is 2990.75Lm after being polluted in step (a)-2·h-1, 61.34 ° of contact angle, filter cake
The apparent porosity of layer is 15.87%, and the aperture of cake layer is 16nm.
TOC contents are 0.5ppm in the drinking water obtained after processing, and turbidity is down to 0NTU, and separated from contaminants efficiency is
97%.
Comparative example 1：
This comparative example provides the pending drinking water in a kind of sewage water treatment method Processing Example 1, the processing side
Method is：The membrane module of device described in embodiment 1 in CN 104787940A is directly used to be handled.
In this comparative example, membrane flux is 1777.5Lm after the membrane module pollution-2·h-1, contact angle is 73.04 °, filter
The apparent porosity of cake layer is 15.30%, and the aperture of cake layer is 25nm.
TOC contents are 0.5ppm in the drinking water obtained after processing, turbidity 0.5NTU, and separated from contaminants efficiency is
95%.
It can be seen that membrane flux is significantly lower than embodiment 1 after membrane module pollution in CN 104787940A, its hydrophily is inferior to reality
Example 1 is applied, cake layer aperture is larger, is unfavorable for retaining pollutant, can cause to block inside fenestra.The present invention utilizes electro-oxidation process
Partial digestion organic matter, hydrophobic larger molecular organicses are oxidized to the small molecule of relative hydropathic, thus the cake layer formed is more
Add hydrophilic, contribute to decelerating membrane pollution, improve water flux.Meanwhile its cake layer is easier to be removed by sluicing, extending film makes
Use the life-span.
Comparative example 2：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Device in example 1 is applied, difference is：The positive plate 1 uses aluminium electrode.
The processing method is with reference to embodiment 1.
In this comparative example, membrane flux is 1875Lm after being polluted in step (a)-2·h-1, contact angle is 70.63 °, filter cake
The apparent porosity of layer is 15.65%, and the aperture of cake layer is 18nm.As can be seen that the porosity of the cake layer formed is bright
The aobvious porosity less than cake layer of the present invention, the semi permeability of cake layer is poor, and contact angle is larger, cake layer hydrophilicity compared with
Difference, and then its strainability is influenceed, and the performance of decelerating membrane pollution is also poor.
TOC contents are 0.5ppm in the drinking water obtained after processing, and turbidity is down to 0NTU, and separated from contaminants efficiency is
91%.
Comparative example 3：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Device in example 1 is applied, difference is：Induction electrode 2 is not provided with described device.
The processing method is with reference to embodiment 1.
In this comparative example, membrane flux is 1802.75Lm after pollution-2·h-1, contact angle be 105 °, cake layer it is apparent
Porosity is 12.67%, and the aperture of cake layer is 20nm.As can be seen that because the electric flocculation for lacking induction electrode acts on, anode
Pollutant is oxidized to small molecule, causes apparent porosity to decline；Due to the accumulation of small molecule, the aperture of cake layer reduces；Together
When, the hydrophilicity of cake layer is also poor.
TOC contents are 0.5~0.8ppm in the drinking water obtained after processing, and turbidity is down to 0NTU, separated from contaminants effect
Rate is 87%.
Comparative example 4：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Apply device in example 1.
With reference to embodiment 1, difference is the processing method：Regulation current density is 3A/m in step (1)2(i.e. electric current
Density is too small)；
In this comparative example, membrane flux is 1887Lm after pollution-2·h-1, contact angle is 69.75 °, the apparent holes of cake layer
Gap rate is 13.67%, and the aperture of cake layer is 15nm.As can be seen that because current density is too low, cause under apparent porosity
Drop, decelerating membrane pollution effect are deteriorated.
TOC contents are 1.2ppm in the drinking water obtained after processing, and separated from contaminants efficiency is 84%.
Comparative example 5：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Apply device in example 1.
With reference to embodiment 1, difference is the processing method：Regulation current density is 60A/m in step (1)2(i.e. electric current
Density is excessive)；
In this comparative example, flux is 1825Lm after pollution-2·h-1, contact angle is 65.63 °, the apparent hole of cake layer
Rate is 15.54%, and the aperture of cake layer is 18nm.As can be seen that because current density is too high, excessive flco can be generated, is formed
Unnecessary flco cause fouling membrane on the contrary.
TOC contents are 1.1ppm in the drinking water obtained after processing, and separated from contaminants efficiency is 86%.
Comparative example 6：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Apply device in example 1.
With reference to embodiment 1, difference is the processing method：Regulation transmembrane pressure is 15kPa (i.e. cross-films in step (1)
Pressure difference is too small)；
In this comparative example, flux is 1700Lm after pollution-2·h-1, contact angle is 71.11 °, the apparent hole of cake layer
Rate is 13.27%, and the aperture of cake layer is 16nm,.
TOC contents are 1.0ppm in the drinking water obtained after processing, and separated from contaminants efficiency is 85%.
Comparative example 7：
This comparative example provides a kind of electrochemistry-membrane-separation water treatment device and its processing method, and described device is with reference to real
Apply device in example 1.
With reference to embodiment 1, difference is the processing method：Regulation transmembrane pressure is 60kPa (i.e. cross-films in step (1)
Pressure difference is excessive)；
In this comparative example, membrane flux is 1696Lm after pollution-2·h-1, contact angle is 82.64 °, the apparent holes of cake layer
Gap rate is 8.42%, and the aperture of cake layer is 6nm.
TOC contents are 1.7ppm in the drinking water obtained after processing, and separated from contaminants efficiency is 82%.
Membrane flux is contrasted after being polluted in embodiment 1-3 and comparative example 1-7, as shown in Figure 2, it can be seen that the present invention
Film after being polluted in described device has higher membrane flux, and the cake layer of formation is more hydrophilic, contributes to decelerating membrane pollution.
Summary embodiment and comparative example can be seen that the present invention by field effect, electrochemical oxidation and electric floating
Effect, using the film in membrane module as basement membrane, be formed on one layer it is new have semipermeable cake layer as new membrane structure,
Pollutant is modified as membrane material, and then decelerating membrane pollution improves the water treatmenting performance of device simultaneously.
Applicant states that the present invention illustrates the detailed process equipment of the present invention and technological process by above-described embodiment,
But the invention is not limited in above-mentioned detailed process equipment and technological process, that is, it is above-mentioned detailed not mean that the present invention has to rely on
Process equipment and technological process could be implemented.Person of ordinary skill in the field it will be clearly understood that any improvement in the present invention,
The addition of equivalence replacement and auxiliary element to each raw material of product of the present invention, selection of concrete mode etc., all fall within the present invention's
Within the scope of protection domain and disclosure.
Claims (9)
1. a kind of electrochemistry-membrane-separation water treatment device, it is characterised in that described device includes reaction tank (5), the reaction tank
(5) membrane module (4) is set in, and membrane module (4) side sets gradually induction electrode parallel to membrane module (4) from inside to outside
(2) and positive plate (1), membrane module (4) opposite side set minus plate (3), the positive plate (1) parallel to membrane module (4)
It is connected with minus plate (3) with external power supply (9)；
Reaction tank (5) body side is provided with water inlet (6)；Membrane module delivery port is opened up in reactor (5) main body
(8), the membrane module delivery port (8) is connected with membrane module (4).
2. electrochemistry-membrane-separation water treatment device according to claim 1, it is characterised in that the positive plate (1) is titanium
Ruthenium electrode；
Preferably, number >=1 of the positive plate (1).
3. electrochemistry-membrane-separation water treatment device according to claim 1 or 2, it is characterised in that the induction electrode
(2) it is sensing aluminium electrode or sensing iron electrode；
Preferably, number >=1 of the induction electrode (2).
4. according to electrochemistry-membrane-separation water treatment device described in claim any one of 1-3, it is characterised in that the negative electrode
Plate (3) is aluminium negative electrode, iron cathode or stainless steel cathode；
Preferably, number >=1 of the minus plate (3).
5. according to electrochemistry-membrane-separation water treatment device described in claim any one of 1-4, it is characterised in that the film group
Part (4) is curtain Flat Membrane or hollow-fibre membrane；
Preferably, the membrane component in the membrane module (4) is any one in microfiltration membranes, milipore filter or NF membrane or at least two
Combination；
Preferably, reaction tank (5) body side is provided with water return outlet (7) with water inlet opposite side.
6. the processing method of electrochemistry-membrane-separation water treatment device according to claim any one of 1-5, its feature exist
In methods described is：
(a) sewage is passed through, starts electrochemical appliance, adjusts electrochemical parameter and UF membrane parameter, carries out electric flocculation, electrochemistry oxygen
Change and electrolytic process, cake layer is formed on membrane module (4) surface；
(b) start power set, carry out membrane filtration processing, the water body after processing is discharged from membrane module delivery port (8).
7. processing method according to claim 6, it is characterised in that electrochemical parameter is adjusted described in step (a) is：Adjust
Economize on electricity current density is 5A/m2~50A/m2, preferably 10A/m2；
Preferably, adjusting film separation parameter described in step (a) is：Regulation transmembrane pressure is 20kPa~50kPa, preferably across
Mould difference is 30kPa.
8. according to the processing method described in claim any one of 6-7, it is characterised in that the sewage load described in step (a)
For 200Lm-2·h-1~20000Lm-2·h-1, preferably 3000Lm-2·h-1。
9. the purposes of electrochemistry-membrane-separation water treatment device according to claim any one of 1-5, it is characterised in that institute
State electrochemistry-membrane-separation water treatment device and be applied to drinking water and sewage treatment area.
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