CN105692875A - Membrane pollution vibration control device used in process of treating algae containing water through low-pressure spiral membrane and method for controlling membrane pollution through device - Google Patents
Membrane pollution vibration control device used in process of treating algae containing water through low-pressure spiral membrane and method for controlling membrane pollution through device Download PDFInfo
- Publication number
- CN105692875A CN105692875A CN201610150539.4A CN201610150539A CN105692875A CN 105692875 A CN105692875 A CN 105692875A CN 201610150539 A CN201610150539 A CN 201610150539A CN 105692875 A CN105692875 A CN 105692875A
- Authority
- CN
- China
- Prior art keywords
- water
- membrane
- regulating valve
- membrane module
- concentrated solution
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/20—By influencing the flow
- B01D2321/2033—By influencing the flow dynamically
- B01D2321/2058—By influencing the flow dynamically by vibration of the membrane, e.g. with an actuator
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a membrane pollution vibration control device used in the process of treating algae containing water through a low-pressure spiral membrane and a method for controlling membrane pollution through the device. The device and the method aim at solving the problem that at present, no vibration control technology provided for the low-pressure spiral membrane pollution phenomenon is available. A vibration driver is arranged in the device, a spiral membrane reactor is driven by a drive motor to rotate along the axis, rotate back to the original position, reverse and rotate back to the original position, and therefore the vibration effect of a membrane assembly is achieved. According to the vibration method, the time when the spiral membrane maintains high-flux operation is prolonged, and the quality of effluent is guaranteed.
Description
Technical field
The present invention relates to a kind of fouling membrane vibration control apparatus processed in algae-containing water process and the method utilizing this device to control fouling membrane。
Background technology
Large-scale blue-green alga bloom contamination accident at present brings great hidden danger to the mankind and vegeto-animal health, even causes serious political negative effect and society's concussion。Low-pressure membrane isolation technics (micro-filtration membrane, ultrafilter membrane) is as a kind of physical separating process, antibacterial, algae and other aquatiles etc. had very efficient crown_interception, it is to ensure that the most effective means of microorganisms in water safety, therefore applies it in algae removal and there is fairly obvious advantage and significance。But membrane pollution problem is still that the bottleneck that membrane technology further genralrlization is applied。The mode of current lessening membrane fouling mainly includes the adjustment for the treatment of nature water and membrane reactor operational factor and changes the character of former water。In membrane filtration processes, microgranule in former water, colloidal particle or solute transportation can adsorb or be deposited in film surface or fenestra, cause membrane aperture to diminish or block, for delaying the phenomenon that aquifer yield and stalling characteristic are greatly lowered to occur, increasing film surface shear forces is the most frequently used and effective manner, in particular for the solution containing high concentration liquid and solid particle。
As the most common process increasing film surface shear forces, aeration can strengthen the turbulent extent of liquid flowing, hydraulic shear is produced on film surface, suspended impurity and mud is made to be hardly adhered to film surface, thus decreasing resistance of membrane filtration and making membrane module keep relatively Thief zone speed in a long time。But comparing its high energy consumption problem, because Air Bubble Size and the bubble motion direction of actual generation cannot effectively be controlled, the shearing force size that the method produces does not highlight；And the improvement ability of fouling membrane be will appear as well peak value by it when aeration rate reaches certain value。Moreover, at the higher speeds, irregular bubble can destroy the flco produced in sludge structure and coagulation process, especially for frustule, and the broken release meaning more emiocytosis material of cell wall, cause that raw water quality worsens。Increasing former water flow velocity is also another main method alleviating fouling membrane, by directly destroying film surface mass transfer layer, accelerates the mixing rate of its surface solution, eliminates concentration polarization phenomenon。But it also exists inevitable defect when application, namely the raising of film surface velocity must flow through increase transmembrane pressure realization, and this necessarily causes that film surface contamination layer more closely and is difficult to eluting, causes the increase of membrane fouling rate。Except frustule itself in algae-containing water, the secretions that its homergy produces also occupies significant proportion, and wherein carbohydrate is one of important component。This kind of emplastic forms bigger polymer tunicle surface not only by intermolecular force and retains, and by chemical bond, more frustule and other kind secretory substances can be sticked to film surface。For the prevailing water body of this colloid and macromolecular substances, search out suitable method increase film surface shear forces and maintain the integrity of frustule to alleviating fouling membrane by important in inhibiting simultaneously。
The pollution problem that effect of vibration controls in membrane filtration processes is utilized to rise gradually。Such as: succeed in multiple commercial-scale commercial Application for the oscillatory shear reinforced film system of Flat Membrane exploitation and the vertical vibration system proposed for hollow-fibre membrane。But, this research is also limited only to flat and hollow fiber form membrane module at present, is not directed to rolled membrane module。But, compare flat and hollow fiber form membrane module, rolled membrane module, because the many advantages in filling area, cleaning way, transformation and maintenance cost etc. receives the extensive concern of industry, becomes the first-selection of the water supply plant project of upgrading and rebuilding。Therefore, it is necessary to work out a kind of vibration filtering system for low pressure rolled membrane module。
Summary of the invention
The problem that the invention aims to solve still do not have now a kind of vibration control technology proposed for low pressure rolled film contamination phenomenon, and provide a kind of rolling low-pressure membrane to process the fouling membrane vibration control apparatus in algae-containing water process and the method utilizing this device to control fouling membrane。
A kind of rolling low-pressure membrane of the present invention processes the fouling membrane vibration control apparatus in algae-containing water process by raw water box, peristaltic pump, pressure transducer, rolled membrane module reactor, power transmission shaft, gear, vibratory driver, first conductivity sensor, second conductivity sensor, the first rotor effusion meter, second spinner flowmeter, pH meter, return duct, water inlet pipe, concentrated solution outlet pipe, water outlet pipe after filter, concentrated solution sample tap, water sampling mouth after filter, first goes out water regulating valve, second goes out water regulating valve, discharge outlet, temperature controller, agitator, first inlet regulating valve, second inlet regulating valve, backflow water regulating valve and drive mechanism composition；One end of described power transmission shaft and rolled membrane module reactor are fixedly and coaxially connected, the other end of power transmission shaft and gear are fixedly and coaxially connected, by drive mechanism transmission between described vibratory driver and gear, the outlet of described raw water box is connected with the water inlet of peristaltic pump, it is connected by water inlet pipe between the outlet of peristaltic pump and the water inlet of rolled membrane module reactor, described water inlet pipe is provided with the first inlet regulating valve and the second inlet regulating valve, one end of described return duct is arranged between the first inlet regulating valve and the second inlet regulating valve, the other end of return duct is connected with raw water box, described return duct is provided with backflow water regulating valve, the water inlet of described concentrated solution outlet pipe is connected with rolled membrane module reactor outlet, the outlet of concentrated solution outlet pipe is connected with raw water box, concentrated solution outlet pipe is disposed with first along water (flow) direction and goes out water regulating valve, first conductivity sensor and the first rotor effusion meter, first goes out to be provided with concentrated solution sample tap between water regulating valve and the first conductivity sensor；After described filter, the water inlet of water outlet pipe is connected with rolled membrane module reactor outlet, after described filter, the outlet of water outlet pipe is connected with raw water box, after filter, water outlet pipe is disposed with second along water (flow) direction and goes out water regulating valve, second conductivity sensor and the second spinner flowmeter, second goes out to be provided with between water regulating valve and the second conductivity sensor water sampling mouth after filter, after concentrated solution sample tap and filter, water sampling mouth is provided with valve, described water inlet pipe nearly rolled membrane module reactor place and concentrated solution outlet pipe nearly rolled membrane module reactor place are provided with pressure transducer, it is provided with pH meter in described raw water box, temperature controller and agitator, the bottom of described raw water box sidewall is provided with discharge outlet。
The method that a kind of control membrane fouling device utilized in rolling low-pressure membrane process algae-containing water process of the present invention controls fouling membrane is as follows:
Former water in raw water box enters in rolled membrane module reactor by peristaltic pump through water inlet pipe, rolled membrane module reactor passes through drive mechanism under the driving of vibratory driver, gear and power transmission shaft make rolled membrane module reactor realize the rotation along axial line, revolution playback, rotate backward, turn round the repeating motion of playback again, in running, the concentrated solution in concentrated solution outlet pipe can directly be drained according to demand or be back in raw water box, in running, after filter, the membrane permeation liquid in water outlet pipe can directly be drained according to demand or be back in raw water box, running can pass through return duct and recirculation water thereon regulates pressure and the flow that valve regulation is intake。
Beneficial effects of the present invention:
The present invention is different from flat and hollow fiber form membrane module, vibrate the control that rolled film is polluted and be not only fixed against membrane module own rotation in the direct shearing force of film surface generation, also will utilize the relative motion produced between rolled film feedwater side difference solute and solution simultaneously。Basic law according to fluid flowing, due to two alternate density variations in heterogeneous system, it is possible to making biphase generation relative motion by mechanical means, the research of this project is based on this mechanism。In rolled membrane module horizontal vibration process, due to the density contrast between particulate pollutant and solution, necessarily strengthen the relative motion of this pollutant and bulk solution in water inlet, thus reinforcing membrane surface water body level of disruption, increase film surface shear forces, and finally reduce concentration polarization and fouling membrane phenomenon。Therefore this vibrating effect depends on the relative motion degree between particulate matter and solution, also has with raw water quality, film surface features and oscillation intensity and contacts closely。Present invention utilizes in former water obvious gap between frustule and water density, relative motion will necessarily occur between frustule and solution when rolled membrane module vibrates in the horizontal direction。In membrane filtration processes, this relative motion will necessarily increase film surface or neighbouring frustule and secretions thereof to the diffusion velocity of bulk solution, thus extending film to maintain the time that high flux runs, ensures film effluent quality simultaneously。Concrete advantage is as follows:
(1) as a kind of organism, frustule can break and the gas chromatography matter of water body release towards periphery because of the death that external force causes, thus membrane fouling rate can be increased the weight of。Therefore, the impact on frustule integrity must be reduced when processing eutrophication water as far as possible。The present invention compares conventional aeration, can the size of more effective control film surface shear forces, it is to avoid to the excessive damage of frustule in former water, thus ensure that raw water quality。It is not only does this facilitate enhancing vibrating effect, also ensures effluent quality。
(2) compared with the simple method increasing film surface velocity, method for oscillating is not required to increase transmembrane pressure, namely can produce shearing force when lower pressure on film surface and form water disturbance, thus reducing fouling membrane development speed further。
(3) present invention is making full use of rolled membrane module water inlet current while the vertical direction scouring force that film surface produces, horizontal applied force is produced by effect of vibration, the mixing rate of film surface solution will necessarily be greatly enhanced, the polluter promoting film surface aggregation dissolves in bulk solution again, the mass transfer rate of material in augmenting response device, thus destroying the concentration polarization phenomenon on film surface, extending film and maintaining the time that high flux runs。
(4) present invention can be applied not only to low-pressure membrane filtration technology, also can be widely used to various fouling membrane technology, including high pressure reverse osmosis membrane filtration system。Except algae-containing water, other polluted water bodies are equally applicable, and are particularly suited for the particulate matter solution containing higher concentration。Density contrast between solute and solvent in the control effect of fouling membrane and pending solution is closely connected by the present invention。
(5) method of the present invention is simple to operate, and controllability is strong, and the control method polluted for rolled film provides new thinking。
Accompanying drawing explanation
A kind of rolling low-pressure membrane that Fig. 1 is the present invention processes the fouling membrane vibration control apparatus schematic diagram in algae-containing water process；
Fig. 2 is test two and the conventional crossflow membrane filtration method comparison diagram on the impact that transmembrane pressure (TMP) changes；Wherein 1 is test the influence curve that transmembrane pressure (TMP) is changed by the method for two, and 2 is the influence curve that transmembrane pressure (TMP) is changed by conventional crossflow membrane filtration method；
Fig. 3 is test two and the comparison diagram of irreversible resistance value (RTI) in conventional crossflow membrane filtration method；Wherein 1 be test two method in irreversible resistance value (RTI), 2 be routine crossflow membrane filtration method in irreversible resistance value (RTI)；
Fig. 4 is the SEM photograph on the film surface testing the membrane module in two before physical cleaning；
Fig. 5 is the SEM photograph on the film surface of the membrane module before physical cleaning in matched group one；
Fig. 6 is the SEM photograph on the film surface testing the membrane module in two after physical cleaning；
Fig. 7 is the SEM photograph on the film surface of the membrane module after physical cleaning in matched group one；
Fig. 8 is test two and the aeration method comparison diagram on the impact that transmembrane pressure (TMP) changes；Wherein 1 is test the influence curve that transmembrane pressure (TMP) is changed by the method for two, 2 influence curves transmembrane pressure (TMP) changed for aeration method, 3 is friction and influence curve transmembrane pressure (TMP) changed without aeration；
The comparison diagram that when Fig. 9 processes different pollutant for vibration (test two) from friction, TMP difference (Δ TMP) changes；Wherein 1 is Δ TMP change curve during process algae solution, and 2 is Δ TMP change curve during process silica suspension, and 3 is Δ TMP change curve during process mucilage secretion, and 4 is Δ TMP change curve during process humic acid。
Detailed description of the invention
Detailed description of the invention one: a kind of rolling low-pressure membrane of present embodiment processes the fouling membrane vibration control apparatus in algae-containing water process by raw water box 1, peristaltic pump 2, pressure transducer 3, rolled membrane module reactor 4, power transmission shaft 5, gear 6, vibratory driver 7, first conductivity sensor 8-1, second conductivity sensor 8-2, the first rotor effusion meter 9-1, second spinner flowmeter 9-2, pH meter 10, return duct 11, water inlet pipe 12, concentrated solution outlet pipe 13, water outlet pipe 14 after filter, concentrated solution sample tap 15, water sampling mouth 16 after filter, first goes out water regulating valve 17-1, second goes out water regulating valve 17-2, discharge outlet 18, temperature controller 19, agitator 20, first inlet regulating valve 21, second inlet regulating valve 22, backflow water regulating valve 23 and drive mechanism 24 form；One end of described power transmission shaft 5 and rolled membrane module reactor 4 are fixedly and coaxially connected, the other end of power transmission shaft 5 and gear 6 are fixedly and coaxially connected, by drive mechanism 24 transmission between described vibratory driver 7 and gear 6, the outlet of described raw water box 1 is connected with the water inlet of peristaltic pump 2, it is connected by water inlet pipe 12 between the outlet of peristaltic pump 2 and the water inlet of rolled membrane module reactor 4, described water inlet pipe 12 is provided with the first inlet regulating valve 21 and the second inlet regulating valve 22, one end of described return duct 11 is arranged between the first inlet regulating valve 21 and the second inlet regulating valve 22, the other end of return duct 11 is connected with raw water box 1, described return duct 11 is provided with backflow water regulating valve 23, the water inlet of described concentrated solution outlet pipe 13 is connected with rolled membrane module reactor 4 outlet, the outlet of concentrated solution outlet pipe 13 is connected with raw water box 1, concentrated solution outlet pipe 13 is disposed with first along water (flow) direction and goes out water regulating valve 17-1, first conductivity sensor 8-1 and the first rotor effusion meter 9-1, first goes out and is provided with concentrated solution sample tap 15 between water regulating valve 17-1 and the first conductivity sensor 8-1；After described filter, the water inlet of water outlet pipe 14 is connected with rolled membrane module reactor 4 outlet, after described filter, the outlet of water outlet pipe 14 is connected with raw water box 1, after filter, water outlet pipe 14 is disposed with second along water (flow) direction and goes out water regulating valve 17-2, second conductivity sensor 8-2 and the second spinner flowmeter 9-2, second goes out to be provided with between water regulating valve 17-2 and the second conductivity sensor 8-2 water sampling mouth 16 after filter, after concentrated solution sample tap 15 and filter, water sampling mouth 16 is provided with valve, described nearly rolled membrane module reactor 4 place of water inlet pipe 12 and nearly rolled membrane module reactor 4 place of concentrated solution outlet pipe 13 are provided with pressure transducer 3, it is provided with pH meter 10 in described raw water box 1, temperature controller 19 and agitator 20, the bottom of described raw water box 1 sidewall is provided with discharge outlet 18。
The device of present embodiment in vibration processes, membrane module and membrane reactor synchronous axial system。
The device of present embodiment is mounted on effusion meter real time record film running status at membrane permeation liquid and concentrated solution water outlet side。
In the device of present embodiment, after concentrated solution outlet pipe 13 and filter, water outlet pipe 14 adopts flexible pipe so that concentrated solution and membrane permeation liquid in running can directly be drained according to demand or be back in raw water box 1。
In the device of present embodiment can after concentrated solution sample tap 15 and filter water sampling mouth 16 place water sampling。
In the device of present embodiment, the effect of discharge outlet 18 is when needing cleaning raw water box 1 after plant running a period of time, is emptied by the water of raw water box 1 by discharge outlet 18, then disassembles the water pipe between peristaltic pump 2 and raw water box 1, then clear up。
All electronic instrument video datas in the device of present embodiment are each through the incoming computer of data acquisition unit。
The vibratory driver 7 of present embodiment can regulate the frequency of vibration of needs at any time。
Detailed description of the invention two: the method that a kind of fouling membrane vibration control apparatus utilized in rolling low-pressure membrane process algae-containing water process of present embodiment controls fouling membrane is as follows:
Former water in raw water box 1 enters in rolled membrane module reactor 4 by peristaltic pump 2 through water inlet pipe 12, rolled membrane module reactor 4 passes through drive mechanism 24 under the driving of vibratory driver 7, gear 6 and power transmission shaft 5 make rolled membrane module reactor 4 realize the rotation along axial line, revolution playback, rotate backward, turn round the repeating motion of playback again, in running, the concentrated solution in concentrated solution outlet pipe 13 can directly be drained according to demand or be back in raw water box 1, in running, after filter, the membrane permeation liquid in water outlet pipe 14 can directly be drained according to demand or be back in raw water box 1, running can pass through return duct 11 and backflow water regulating valve 23 thereon regulates the pressure and flow intake。
In present embodiment, after concentrated solution outlet pipe 13 and filter, water outlet pipe 14 adopts flexible pipe so that concentrated solution and membrane permeation liquid in running can directly be drained according to demand or be back in raw water box 1。
Detailed description of the invention three: present embodiment and detailed description of the invention two the difference is that: rolled membrane module reactor 4 along the rotational angle of axial line with to rotate backward angle identical。Other steps and parameter and detailed description of the invention two are identical。
Detailed description of the invention four: present embodiment and detailed description of the invention two or three the difference is that: rolled membrane module reactor 4 is 8 °～16 ° along the rotational angle of axial line。Other steps and parameter and detailed description of the invention two or three are identical。
Detailed description of the invention five: one of present embodiment and detailed description of the invention two to four the difference is that: rolled membrane module reactor 4 is 9 ° along the rotational angle of axial line。Other steps and one of parameter and detailed description of the invention two to four are identical。
Test one, a kind of rolling low-pressure membrane of this test processes the fouling membrane vibration control apparatus in algae-containing water process by raw water box 1, peristaltic pump 2, pressure transducer 3, rolled membrane module reactor 4, power transmission shaft 5, gear 6, vibratory driver 7, first conductivity sensor 8-1, second conductivity sensor 8-2, the first rotor effusion meter 9-1, second spinner flowmeter 9-2, pH meter 10, return duct 11, water inlet pipe 12, concentrated solution outlet pipe 13, water outlet pipe 14 after filter, concentrated solution sample tap 15, water sampling mouth 16 after filter, first goes out water regulating valve 17-1, second goes out water regulating valve 17-2, discharge outlet 18, temperature controller 19, agitator 20, first inlet regulating valve 21, second inlet regulating valve 22, backflow water regulating valve 23 and drive mechanism 24 form；One end of described power transmission shaft 5 and rolled membrane module reactor 4 are fixedly and coaxially connected, the other end of power transmission shaft 5 and gear 6 are fixedly and coaxially connected, by drive mechanism 24 transmission between described vibratory driver 7 and gear 6, the outlet of described raw water box 1 is connected with the water inlet of peristaltic pump 2, it is connected by water inlet pipe 12 between the outlet of peristaltic pump 2 and the water inlet of rolled membrane module reactor 4, described water inlet pipe 12 is provided with the first inlet regulating valve 21 and the second inlet regulating valve 22, one end of described return duct 11 is arranged between the first inlet regulating valve 21 and the second inlet regulating valve 22, the other end of return duct 11 is connected with raw water box 1, described return duct 11 is provided with backflow water regulating valve 23, the water inlet of described concentrated solution outlet pipe 13 is connected with rolled membrane module reactor 4 outlet, the outlet of concentrated solution outlet pipe 13 is connected with raw water box 1, concentrated solution outlet pipe 13 is disposed with first along water (flow) direction and goes out water regulating valve 17-1, first conductivity sensor 8-1 and the first rotor effusion meter 9-1, first goes out and is provided with concentrated solution sample tap 15 between water regulating valve 17-1 and the first conductivity sensor 8-1；After described filter, the water inlet of water outlet pipe 14 is connected with rolled membrane module reactor 4 outlet, after described filter, the outlet of water outlet pipe 14 is connected with raw water box 1, after filter, water outlet pipe 14 is disposed with second along water (flow) direction and goes out water regulating valve 17-2, second conductivity sensor 8-2 and the second spinner flowmeter 9-2, second goes out to be provided with between water regulating valve 17-2 and the second conductivity sensor 8-2 water sampling mouth 16 after filter, after concentrated solution sample tap 15 and filter, water sampling mouth 16 is provided with valve, described nearly rolled membrane module reactor 4 place of water inlet pipe 12 and nearly rolled membrane module reactor 4 place of concentrated solution outlet pipe 13 are provided with pressure transducer 3, it is provided with pH meter 10 in described raw water box 1, temperature controller 19 and agitator 20, the bottom of described raw water box 1 sidewall is provided with discharge outlet 18。
In the device of this test, after concentrated solution outlet pipe 13 and filter, water outlet pipe 14 adopts flexible pipe so that concentrated solution and membrane permeation liquid in running can directly be drained according to demand or be back in raw water box 1。
In the device of this test, the effect of discharge outlet 18 is when needing cleaning raw water box 1 after plant running a period of time, is emptied by the water of raw water box 1 by discharge outlet 18, then disassembles the water pipe between peristaltic pump 2 and raw water box 1, then clear up。
Test two: utilize the method tested the fouling membrane vibration control apparatus control fouling membrane in a kind of rolling low-pressure membrane process algae-containing water process as described in as follows:
Former water in raw water box 1 enters in rolled membrane module reactor 4 by peristaltic pump 2 through water inlet pipe 12, rolled membrane module reactor 4 passes through drive mechanism 24 under the driving of vibratory driver 7, gear 6 and power transmission shaft 5 make rolled membrane module reactor 4 realize the rotation along axial line, revolution playback, rotate backward, turn round the repeating motion of playback again, in running, the concentrated solution in concentrated solution outlet pipe 13 can directly be drained according to demand or be back in raw water box 1, in running, after filter, the membrane permeation liquid in water outlet pipe 14 can directly be drained according to demand or be back in raw water box 1, running can pass through return duct 11 and backflow water regulating valve 23 thereon regulates the pressure and flow intake。
In this test, rolled membrane module reactor 4 is along the rotational angle of axial line with to rotate backward angle identical, and rolled membrane module reactor 4 is 9 ° along the rotational angle of axial line。
Contrast test (one): the impact of fouling membrane is tested by test two with conventional crossflow membrane filtration method:
Former water is the microcystic aeruginosa solution of laboratory cultures, and detailed water quality index is in Table 1。
The water quality index of the former water of table 1
The method adopting test two, namely utilizes vibration to slow down mode as fouling membrane in reactor。
Matched group one: reactor adopts conventional crossflow membrane filtration mode。
To adopt all the time in the process of test and flow the method for operation continuously, ultrafilter membrane flux constant is 40L/ (m2H), reactor temperature is 23～25 DEG C, and duration of experiment is 6 hours, rotational angle 9 °, and in reactor, membrane module frequency of vibration is 10Hz, film surface cross-flow flow velocity 2～3cm/s。
Obtain test two as shown in Figure 2 and the conventional crossflow membrane filtration method comparison diagram on the impact that transmembrane pressure (TMP) changes；Wherein 1 is test the influence curve that transmembrane pressure (TMP) is changed by the method for two, and 2 is the influence curve that transmembrane pressure (TMP) is changed by conventional crossflow membrane filtration method。
Obtain test two as shown in Figure 3 and the comparison diagram of irreversible resistance value (RTI) in conventional crossflow membrane filtration method；Wherein 1 be test two method in irreversible resistance value (RTI), 2 be routine crossflow membrane filtration method in irreversible resistance value (RTI)。
By Fig. 2 and Fig. 3 it can be seen that fouling membrane is had fairly obvious remission effect by the rotary action of membrane module, and relative irreversible resistance value can be reduced。
The membrane module taken off after off-test in test two and matched group one carries out physical cleaning, and before and after physical cleaning, the film surface of membrane module is carried out SEM detection carrying out respectively:
The SEM photograph on the film surface of the membrane module obtained before physical cleaning as shown in Figure 4 in test two, the SEM photograph on the film surface of the membrane module in matched group one before physical cleaning as shown in Figure 5, the SEM photograph on the film surface of the membrane module in test two, the SEM photograph on the film surface of the membrane module in matched group one after physical cleaning as shown in Figure 7 after physical cleaning as shown in Figure 6。
From Fig. 4～7 it can be seen that the vibrational energy tested two effectively scrubs the pollutant on film surface, especially oarse-grained frustule。After physical cleaning, diaphragm face pollutant are substantially removed, but still it is covered with one layer of rough polluter on friction film surface, the pollution development speed that the effect of vibration of test two can not only effectively be alleviated in membrane filtration processes is described, physical cleaning effect can be strengthened simultaneously。
Contrast test (two): the impact of fouling membrane is tested by contrast test two and aeration method:
Former water takes from water factory's coagulative precipitation tank water outlet, and its main water quality index is as shown in table 2。
The water quality index of the former water of table 2
The method adopting test two, namely utilizes vibration to slow down mode as fouling membrane in reactor。
Matched group two: adopting aeration mode, in aeration reactor, aeration rate/flux ratio is 1:1。
To adopt all the time in the process of test and flow the method for operation continuously, ultrafilter membrane flux constant is 40L/ (m2H), reactor temperature is 23～25 DEG C, and duration of experiment is 6 hours, rotational angle 9 °, and in reactor, membrane module frequency of vibration is 10Hz, film surface cross-flow flow velocity 2～3cm/s。
Obtain test two as shown in Figure 8 and the aeration method comparison diagram on the impact that transmembrane pressure (TMP) changes；Wherein 1 is test the influence curve that transmembrane pressure (TMP) is changed by the method for two, 2 influence curves transmembrane pressure (TMP) changed for aeration method, 3 is friction and influence curve transmembrane pressure (TMP) changed without aeration。
From figure 8, it is seen that compare aeration effect, membrane module effect of vibration can more effective control fouling membrane development speed。
Thinking: compare aeration method, method for oscillating is owing to can clearly control the important factor in order such as rotational frequency and rotational angle, so can effectively shearing force size required in actual application be regulated and controled。On the contrary, although many-sided active force that aeration method can be produced in uphill process by bubble strengthens the shearing force suffered by particulate matter, but this process is difficult to concrete some important factor of influence of manipulation (such as Air Bubble Size, the rate of climb and the direction of motion etc.), thus causing that cleaning performance occurs lower than phenomenons such as expection and energy wastes, and the even more serious problems such as the reduction of film aquifer yield and operating cost raising that ultimately cause occur。
Contrast test (three): heterogeneity is carried out membrane filtration test by the membrane filtering method (vibration) and the conventional crossflow membrane filtration mode (friction) that are respectively adopted test two, carry out the contrast test of the control effect of the fouling membrane that heterogeneity is caused by vibration with friction control membrane fouling method, specific as follows:
In the former water of algae solution, frustule concentration is about 2 × 108Individual/L；Using algae-containing water filtrate after 0.45 μm of membrane filtration as the former water of mucilage secretion。Meanwhile, have employed the natural organic matter in humic acid simulation eutrophication water (humic acid storing solution being added distilled water as the former water of humic acid)。For simulation water body in silt and minerals material, test have employed silicon dioxide configuration aaerosol solution, the concentration of aaerosol solution is 5g/L, and wherein the mean diameter of silicon dioxide is about 10 μm。Concrete test raw water quality is in Table 3。
The water quality index of the former water of table 3
To adopt all the time in the process of test and flow the method for operation continuously, ultrafilter membrane flux constant is 40L/ (m2H), reactor temperature is 23～25 DEG C, and duration of experiment is 3 hours, rotational angle 9 °, and in reactor, membrane module frequency of vibration is 10Hz, film surface cross-flow flow velocity 2～3cm/s。
Conclusion: utilize the TMP difference (Δ TMP) vibrating the ultrafilter membrane after two kinds of methods of (test two) and friction process under the same time to characterize the vibration (test two) control ability to the fouling membrane that different polluters (algae-containing water, mucilage secretion, silicon dioxide and humic acid) cause, namely obtains the comparison diagram that when vibration (test two) as shown in Figure 9 processes different pollutant from friction, TMP difference (Δ TMP) changes；Wherein 1 is TMP difference (Δ TMP) change curve during process algae solution, 2 for processing TMP difference (Δ TMP) change curve during silica suspension, 3 for processing TMP difference (Δ TMP) change curve during mucilage secretion, and 4 is TMP difference (Δ TMP) change curve during process humic acid。
As seen from Figure 9, vibrating effect be ordered as algae solution > silicon dioxide > mucilage secretion > humic acid。Vibrate and accelerate the solution diffusion rate within membrane module mainly by raising membrane module with the relative motion of solution in reactor, thus the concentration polarization phenomenon alleviated in reactor；Rely on the shearing force that this relative motion generates that film surface is constantly scrubbed simultaneously, reach to suppress the effect of cake layer generating rate。It is entirely through the particulate matter that crown_interception is removed for silicon dioxide is this, interaction force between they and film surface is more weak, gathering on film surface is substantially dependence film area suction power effect, can very effective reduction membrane fouling rate hence with effect of vibration。Although frustule surface generally all can adhere to one layer of carbohydrate, but speculating according to experimental result, under weak basic condition, carbohydrate and film surface are all in elecrtonegativity, electrostatic repulsion to each other is relatively strong, so the active force between carbohydrate and film is not fairly obvious。Conversely, for this Organic substance containing multiple hydrophilic and hydrophobic group of humic acid, intramolecular action can be passed through and occur to produce very close chemical reaction with ultrafiltration membrane surface functional group, vibrate this control ability is relatively weak。
Claims (5)
1. a rolling low-pressure membrane processes the fouling membrane vibration control apparatus in algae-containing water process, it is characterised in that this device is by raw water box (1), peristaltic pump (2), pressure transducer (3), rolled membrane module reactor (4), power transmission shaft (5), gear (6), vibratory driver (7), first conductivity sensor (8-1), second conductivity sensor (8-2), the first rotor effusion meter (9-1), second spinner flowmeter (9-2), pH meter (10), return duct (11), water inlet pipe (12), concentrated solution outlet pipe (13), water outlet pipe (14) after filter, concentrated solution sample tap (15), water sampling mouth (16) after filter, first goes out water regulating valve (17-1), second goes out water regulating valve (17-2), discharge outlet (18), temperature controller (19), agitator (20), first inlet regulating valve (21), second inlet regulating valve (22), backflow water regulating valve (23) and drive mechanism (24) composition；One end of described power transmission shaft (5) and rolled membrane module reactor (4) are fixedly and coaxially connected, the other end of power transmission shaft (5) and gear (6) are fixedly and coaxially connected, by drive mechanism (24) transmission between described vibratory driver (7) and gear (6), the outlet of described raw water box (1) is connected with the water inlet of peristaltic pump (2), it is connected by water inlet pipe (12) between outlet and the water inlet of rolled membrane module reactor (4) of peristaltic pump (2), described water inlet pipe (12) is provided with the first inlet regulating valve (21) and the second inlet regulating valve (22), one end of described return duct (11) is arranged between the first inlet regulating valve (21) and the second inlet regulating valve (22), the other end of return duct (11) is connected with raw water box (1), described return duct (11) is provided with backflow water regulating valve (23), the water inlet of described concentrated solution outlet pipe (13) is connected with rolled membrane module reactor (4) outlet, the outlet of concentrated solution outlet pipe (13) is connected with raw water box (1), concentrated solution outlet pipe (13) is disposed with first along water (flow) direction and goes out water regulating valve (17-1), first conductivity sensor (8-1) and the first rotor effusion meter (9-1), first goes out to be provided with concentrated solution sample tap (15) between water regulating valve (17-1) and the first conductivity sensor (8-1)；After described filter, the water inlet of water outlet pipe (14) is connected with rolled membrane module reactor (4) outlet, after described filter, the outlet of water outlet pipe (14) is connected with raw water box (1), after filter, water outlet pipe (14) is disposed with second along water (flow) direction and goes out water regulating valve (17-2), second conductivity sensor (8-2) and the second spinner flowmeter (9-2), second goes out to be provided with between water regulating valve (17-2) and the second conductivity sensor (8-2) water sampling mouth (16) after filter, after concentrated solution sample tap (15) and filter, water sampling mouth (16) is provided with valve, nearly rolled membrane module reactor (4) place of described water inlet pipe (12) is provided with pressure transducer (3) with nearly rolled membrane module reactor (4) place of concentrated solution outlet pipe (13), it is provided with pH meter (10) in described raw water box (1), temperature controller (19) and agitator (20), the bottom of described raw water box (1) sidewall is provided with discharge outlet (18)。
2. utilizing a kind of rolling low-pressure membrane as claimed in claim 1 to process the fouling membrane vibration control apparatus in algae-containing water process, to control the method for fouling membrane as follows:
Former water in raw water box (1) enters in rolled membrane module reactor (4) by peristaltic pump (2) through water inlet pipe (12), rolled membrane module reactor (4) under the driving of vibratory driver (7) by drive mechanism (24), gear (6) and power transmission shaft (5) make rolled membrane module reactor (4) realize the rotation along axial line, revolution playback, rotate backward, turn round the repeating motion of playback again, in running, the concentrated solution in concentrated solution outlet pipe (13) can directly drain or be back in raw water box (1) according to demand, in running, after filter, the membrane permeation liquid in water outlet pipe (14) can directly drain or be back in raw water box (1) according to demand, running can pass through return duct (11) and backflow water regulating valve thereon (23) regulates the pressure and flow intake。
3. according to claim 3 a kind of utilize rolling low-pressure membrane to process the method that the fouling membrane vibration control apparatus in algae-containing water process controls fouling membrane, it is characterised in that rolled membrane module reactor (4) along the rotational angle of axial line with to rotate backward angle identical。
4. a kind of method utilizing rolling low-pressure membrane to process the fouling membrane vibration control apparatus control fouling membrane in algae-containing water process according to claim 3, it is characterised in that the rotational angle along axial line of rolled membrane module reactor (4) is 8 °～16 °。
5. a kind of method utilizing rolling low-pressure membrane to process the fouling membrane vibration control apparatus control fouling membrane in algae-containing water process according to claim 3, it is characterised in that the rotational angle along axial line of rolled membrane module reactor (4) is 9 °。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610150539.4A CN105692875B (en) | 2016-03-16 | 2016-03-16 | A kind of fouling membrane vibration control apparatus during rolling low pressure film process algae-containing water and the method using device control fouling membrane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610150539.4A CN105692875B (en) | 2016-03-16 | 2016-03-16 | A kind of fouling membrane vibration control apparatus during rolling low pressure film process algae-containing water and the method using device control fouling membrane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105692875A true CN105692875A (en) | 2016-06-22 |
| CN105692875B CN105692875B (en) | 2018-05-18 |
Family
ID=56221758
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610150539.4A Active CN105692875B (en) | 2016-03-16 | 2016-03-16 | A kind of fouling membrane vibration control apparatus during rolling low pressure film process algae-containing water and the method using device control fouling membrane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105692875B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362592A (en) * | 2016-08-31 | 2017-02-01 | 广东工业大学 | Benzenes solution desulfurization method |
| CN108816050A (en) * | 2018-06-08 | 2018-11-16 | 南京大学 | A kind of filter device being made of transmission cross-current type plate membrane component and method |
| CN113069928A (en) * | 2021-03-12 | 2021-07-06 | 东北农业大学 | Torsional vibration type hollow fiber membrane filtering device |
| CN113149132A (en) * | 2021-03-25 | 2021-07-23 | 东北农业大学 | High-pressure reverse osmosis membrane filtration system capable of backwashing |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4333832A (en) * | 1977-08-29 | 1982-06-08 | Thomas L. Siwecki | Rotating solution separation system |
| JP2001259384A (en) * | 2000-03-17 | 2001-09-25 | Kurita Water Ind Ltd | Method for washing spiral membrane module |
| CN101545797A (en) * | 2009-04-30 | 2009-09-30 | 上海交通大学 | Method for detecting compaction degree of screen in flat plate reverse osmosis or nano-filtration membrane equipment |
| CN103007759A (en) * | 2012-12-03 | 2013-04-03 | 北京清大国华环保科技有限公司 | Ultrasound vibration type rolling type ultrafiltration membrane group device and ultrafiltration device thereof |
| CN204684958U (en) * | 2015-03-24 | 2015-10-07 | 谢洁萍 | A kind of modified rotates film sewage filter device |
| CN204910969U (en) * | 2015-09-14 | 2015-12-30 | 山东杨帆环保工程有限公司 | Cylinder microstrainer |
-
2016
- 2016-03-16 CN CN201610150539.4A patent/CN105692875B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4333832A (en) * | 1977-08-29 | 1982-06-08 | Thomas L. Siwecki | Rotating solution separation system |
| JP2001259384A (en) * | 2000-03-17 | 2001-09-25 | Kurita Water Ind Ltd | Method for washing spiral membrane module |
| CN101545797A (en) * | 2009-04-30 | 2009-09-30 | 上海交通大学 | Method for detecting compaction degree of screen in flat plate reverse osmosis or nano-filtration membrane equipment |
| CN103007759A (en) * | 2012-12-03 | 2013-04-03 | 北京清大国华环保科技有限公司 | Ultrasound vibration type rolling type ultrafiltration membrane group device and ultrafiltration device thereof |
| CN204684958U (en) * | 2015-03-24 | 2015-10-07 | 谢洁萍 | A kind of modified rotates film sewage filter device |
| CN204910969U (en) * | 2015-09-14 | 2015-12-30 | 山东杨帆环保工程有限公司 | Cylinder microstrainer |
Non-Patent Citations (1)
| Title |
|---|
| 李红海等: "卷式膜分离技术的应用研究进展", 《山东化工》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362592A (en) * | 2016-08-31 | 2017-02-01 | 广东工业大学 | Benzenes solution desulfurization method |
| CN108816050A (en) * | 2018-06-08 | 2018-11-16 | 南京大学 | A kind of filter device being made of transmission cross-current type plate membrane component and method |
| CN113069928A (en) * | 2021-03-12 | 2021-07-06 | 东北农业大学 | Torsional vibration type hollow fiber membrane filtering device |
| CN113149132A (en) * | 2021-03-25 | 2021-07-23 | 东北农业大学 | High-pressure reverse osmosis membrane filtration system capable of backwashing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105692875B (en) | 2018-05-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Tarleton | Progress in filtration and separation | |
| Li et al. | Fouling control of submerged hollow fibre membranes by vibrations | |
| CN105692875A (en) | Membrane pollution vibration control device used in process of treating algae containing water through low-pressure spiral membrane and method for controlling membrane pollution through device | |
| Zhao et al. | The comparison between vibration and aeration on the membrane performance in algae harvesting | |
| CN203507822U (en) | High-frequency vibration enhanced membrane filtration device | |
| SA110320023B1 (en) | Osmotic Separation Systems and Methods | |
| CN204544009U (en) | A kind of oscillatory shear membrane separation plant | |
| Chatzikonstantinou et al. | Membrane fouling control using high-frequency power vibration, in an SMBR pilot system—preliminary studies | |
| CN105540939B (en) | The device and method of calcium, magnesium, fluorine and element silicon in a kind of removal waste water | |
| CN106336070A (en) | Method for improving recovery rate of membrane separation system and device thereof | |
| CN206526685U (en) | Purpose ceramic-film filter and separation of fermentative broth processing system | |
| Klyuchnikov et al. | Hydrodynamic methods for reducing concentration polarization during beer processing by membranes | |
| CN207591634U (en) | Interface moves dock cellulosic ultrafiltration putamina | |
| Xue et al. | Fouling control of a pilot scale self-forming dynamic membrane bioreactor for municipal wastewater treatment | |
| CN201825825U (en) | Textile sewage treatment system | |
| CN208223932U (en) | A kind of water quality monitoring pretreatment unit | |
| CN113069928B (en) | Torsional vibration type hollow fiber membrane filtering device | |
| CN108706809A (en) | A kind of sewage membrane separation equipment | |
| KR100785815B1 (en) | Tubular membrane module and system equipped reciprocated and rotated suction tubing for continuous cleaning | |
| CN215209035U (en) | Anti-fouling durable hollow fiber membrane separation device | |
| JP2009082029A (en) | Membrane bioreactor for continuously producing valuable resources through fermentation | |
| CN105565551B (en) | The processing system of organic phosphate in a kind of removal electroplating wastewater | |
| CN214973103U (en) | Hollow fiber membrane torsional vibration subassembly | |
| CN107487913A (en) | A kind of counter-infiltration system | |
| CN1272090C (en) | Air bubble circulation flow type hollow fibrous membrane separating device |
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 |