CN219637050U - High-flux ceramic ultrafiltration water treatment system - Google Patents
High-flux ceramic ultrafiltration water treatment system Download PDFInfo
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- CN219637050U CN219637050U CN202320851833.3U CN202320851833U CN219637050U CN 219637050 U CN219637050 U CN 219637050U CN 202320851833 U CN202320851833 U CN 202320851833U CN 219637050 U CN219637050 U CN 219637050U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 314
- 239000000919 ceramic Substances 0.000 title claims abstract description 121
- 238000000108 ultra-filtration Methods 0.000 title claims abstract description 83
- 239000012528 membrane Substances 0.000 claims abstract description 72
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 230000004907 flux Effects 0.000 claims abstract description 25
- 239000003513 alkali Substances 0.000 claims abstract description 17
- 239000008394 flocculating agent Substances 0.000 claims abstract description 17
- 238000004062 sedimentation Methods 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims description 38
- 238000001223 reverse osmosis Methods 0.000 claims description 26
- 244000005700 microbiome Species 0.000 abstract description 4
- 230000000903 blocking effect Effects 0.000 abstract description 3
- 238000011001 backwashing Methods 0.000 description 26
- 238000004140 cleaning Methods 0.000 description 12
- 238000002156 mixing Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 238000011010 flushing procedure Methods 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 238000009295 crossflow filtration Methods 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000002131 composite material Substances 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 238000005352 clarification Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000012466 permeate Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 238000002791 soaking Methods 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- DNXNYEBMOSARMM-UHFFFAOYSA-N alumane;zirconium Chemical compound [AlH3].[Zr] DNXNYEBMOSARMM-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 241001391944 Commicarpus scandens Species 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- GELKBWJHTRAYNV-UHFFFAOYSA-K lithium iron phosphate Chemical compound [Li+].[Fe+2].[O-]P([O-])([O-])=O GELKBWJHTRAYNV-UHFFFAOYSA-K 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Classifications
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a high-flux ceramic ultrafiltration water treatment system, which belongs to the technical field of water treatment and comprises the following components: the device comprises an alkali adding device, a flocculating agent adding device, a raw water pipe, a reaction tank, a sedimentation tank, a raw water tank, a first booster pump, a ceramic ultrafiltration device and a water producing tank which are sequentially connected in series, wherein the discharge outlets of the alkali adding device and the flocculating agent adding device are communicated with the water inlet of the raw water pipe. The utility model utilizes the alkali adding device to improve the pH value of the raw water in the raw water pipe, and as the pH value of the raw water is higher, the electric potential of the surface of the ceramic membrane in the ceramic ultrafiltration device is higher, the flux is larger, and when the raw water flows through the ceramic membrane, the operation flux of the ceramic ultrafiltration device can be improved, and the operation cost is reduced; meanwhile, the high pH value can inhibit the growth of microorganisms in raw water, so that the microorganisms are prevented from blocking membrane holes of the ceramic membrane, and the operation flux of the ceramic ultrafiltration device is maintained.
Description
Technical Field
The utility model relates to the technical field of water treatment, in particular to a high-flux ceramic ultrafiltration water treatment system.
Background
In the field of water treatment, a large amount of wastewater has higher hardness, such as mine water, reverse osmosis concentrated water, circulating sewage, desulfurization wastewater, lithium iron phosphate wastewater, wastewater in the polycrystalline silicon industry and a large amount of chemical wastewater, the common treatment process of the water adopts a filtering mode of a hollow fiber column type membrane or an immersed ultrafiltration membrane after alkaline precipitation filtration, and the residual calcium-magnesium suspended matters float on the surface of the hollow fiber membrane due to the high hardness of the wastewater and the incomplete precipitation filtration after the alkaline removal, so that membrane wires become fragile, are extremely easy to break, are frequently maintained and replaced, have a service life of usually within 2 years, and meanwhile, the water quality of the discharged water is poor due to wire breakage, so that a following security filter element is frequently replaced, reverse osmosis membrane is frequently cleaned, the reverse osmosis cleaning frequency is within 1 month, and the security filter element replacement period is about 1 week, so that a large amount of built equipment cannot normally run. Another treatment process is to adopt a tubular ultrafiltration or microfiltration membrane after alkaline precipitation, and the process adopts a large-flow circulation mode to prevent scaling, so that the operation cost is high due to high energy consumption required by large-flow circulation, and meanwhile, the occupied area and investment are large due to small filling area of the tubular membrane, so that the process is difficult to accept by owners.
The ceramic membrane is also called an inorganic ceramic membrane, and is an asymmetric membrane formed by sintering inorganic ceramic materials at high temperature. The ceramic membrane separation process is a fluid separation process in the form of "cross-flow filtration": the raw material liquid flows in the membrane tube, the clarified permeate containing small molecular components is driven by pressure to permeate the membrane outwards along the direction perpendicular to the clarified permeate, and the turbid concentrate containing large molecular components is intercepted by the membrane, so that the purposes of separating, concentrating and purifying fluid are achieved. The ceramic membrane has the advantages of good chemical stability, acid and alkali resistance, pollution resistance, high mechanical strength, good regeneration performance, long service life, good and stable effluent quality and the like. The ceramic membrane cross-flow filtration mode is divided into 'large cross-flow' and 'micro cross-flow', the traditional ceramic membrane filtration is mainly based on 'large cross-flow', the membrane surface flow rate is usually more than 2 m/s, the operation mode has the advantages of large water production flux per unit membrane area, membrane holes are not easy to block, but the operation cost is higher, the operation mode has the advantages of small investment and low operation cost, but the membrane holes are easy to block, the surface flow rate of the 'micro cross-flow' operation membrane is usually less than 0.1 m/s, the operation mode has the advantages of small investment and low operation cost, but the water production flux per unit membrane area is small, generally less than 150 LMH.
Therefore, how to design a ceramic ultrafiltration water treatment system with small investment, low operation cost, large water production flux per unit membrane area and difficult membrane hole blockage is a technical problem to be solved by the technicians in the field.
Disclosure of Invention
The utility model aims to provide a large-flux ceramic ultrafiltration water treatment device, which utilizes the advantages of large ceramic membrane operation flux, small equipment investment, low operation power consumption, difficult blockage of membrane holes, difficult scaling of the membrane surface and good quality of produced water, ensures higher recovery rate of a subsequent reverse osmosis device, and prolongs the cleaning period and the service life of a reverse osmosis membrane.
The technical scheme for solving the technical problems is as follows, a high-flux ceramic ultrafiltration water treatment system comprises: a raw water pipe, a reaction tank, a sedimentation tank, a raw water tank, a first booster pump, an internal ceramic ultrafiltration device, a water producing tank, an alkali adding device and a flocculating agent adding device,
the raw water pipe, the reaction tank, the sedimentation tank, the raw water tank, the first booster pump, the ceramic ultrafiltration device and the water outlet and water inlet of the water producing tank are sequentially connected in series through water pipes; and the discharge ports of the alkali adding device and the flocculating agent adding device are communicated with the water inlet of the raw water pipe.
The beneficial effects of the utility model are as follows: the pH value of raw water in a raw water pipe is improved by using an alkali adding device, and as the pH value of the raw water is higher, the electric potential of the surface of a ceramic membrane in the ceramic ultrafiltration device is higher, the flux is higher, and when the raw water flows through the ceramic membrane, the operation flux of the ceramic ultrafiltration device can be improved, and the operation cost is reduced; meanwhile, the high pH value can inhibit the growth of microorganisms in raw water, so that the microorganisms are prevented from blocking membrane holes of the ceramic membrane, and the operation flux of the ceramic ultrafiltration device is maintained; in addition, the ceramic ultrafiltration device operates in a high pH value environment, so that the surface of the ceramic membrane has negative charges (the pH value of the isoelectric point of the membrane layer of the ceramic membrane is between 5 and 6, and when the pH value of the filtered liquid is higher than the isoelectric point, the surface of the ceramic membrane has negative charges), and as most of pollutants in raw water have negative charges, the effect of homopolar repulsion can be generated, and the pollutants are prevented from being adsorbed on the surface of the ceramic membrane and blocking the ceramic membrane holes.
On the basis of the technical scheme, the utility model can be improved as follows.
The ceramic ultrafiltration device is provided with a water inlet, a concentrated water inlet and a water producing port, wherein the water inlet is communicated with the water outlet of the first booster pump through a water pipe, and the water producing port is communicated with the water inlet of the water producing tank through a water pipe; the water concentration port is communicated with a water inlet of the reaction tank; the air outlet of the blower is correspondingly communicated with a water pipe between the water outlet of the first booster pump and the water inlet; the water inlet of the backwash pump is communicated with the interior of the water producing tank, and the water outlet of the backwash pump is communicated with the water producing port.
The water in the water producing pool is introduced into the ceramic ultrafiltration device through the water producing port by utilizing the backwash pump, and the ceramic membrane can be reversely flushed due to the water flow direction opposite to the water producing direction of the ceramic ultrafiltration device, so that the scaling on the surface of the ceramic membrane is avoided (the ceramic ultrafiltration device operates in a high pH value environment, and the surface of the ceramic membrane is easy to scale); meanwhile, the blower is utilized to charge air into the water inlet of the ceramic ultrafiltration device, so that flushing water in the ceramic ultrafiltration device can enter the reaction tank through the concentrated water inlet, and capacity is provided for continuously flushing the ceramic membrane.
Further, the water pump further comprises a first acid adding device, the backwash pump is a variable-frequency water pump, and a discharge port of the first acid adding device is correspondingly communicated with a water pipe between a water outlet of the backwash pump and the water producing port.
The ceramic ultrafiltration device has the further beneficial effects that the output power of the backwash pump is adjusted downwards, the water yield of the backwash pump is reduced, acid is added into a water pipe between the water outlet and the water producing port of the backwash pump, and after the acid water enters the ceramic ultrafiltration device, the surface of the ceramic membrane is prevented from scaling easily, so that the operation flux of the ceramic ultrafiltration device is maintained.
Further, the ceramic ultrafiltration device is also provided with a water outlet, and an exhaust valve is arranged at the water outlet.
Further, the device also comprises a second booster pump, a filter, a reverse osmosis device and a water purifying pipe, wherein the second booster pump, the filter, the reverse osmosis device and a water outlet and a water inlet of the water purifying pipe are sequentially connected in series through the water pipe, and a water inlet of the second booster pump is communicated with a water outlet of the water producing pool.
The water treatment device has the further beneficial effects that water in the water producing pool can be purified again through the filter and the reverse osmosis device, so that the water treatment efficiency is improved.
Further, the device also comprises a second acid adding device, wherein a discharge hole of the second acid adding device is correspondingly communicated with a water pipe between the water outlet of the second booster pump and the water inlet of the filter.
The water purifying device has the further beneficial effects that acidic substances are added into the water pipe between the water outlet of the second booster pump and the water inlet of the filter, so that the pH value of water flowing out of the water purifying pipe can be prevented from being too high.
Further, the filter is a cartridge filter.
Further, the operation flux of the ceramic ultrafiltration device is 200-500 LMH, the hardness of the effluent is 50 mg/L-100 mg/L, and the error flow is 30% -40%.
Further, the backwashing period of the ceramic membrane in the ceramic ultrafiltration device is 10min-60min.
In addition, a method for treating high-flux ceramic ultrafiltration water is provided, which comprises the following steps:
s1, raw water enters a raw water pipe, alkali is quantitatively added through an alkali adding device, flocculating agent is quantitatively added through a flocculating agent adding device, the raw water enters a reaction tank for mixing reaction, water after mixing reaction in the reaction tank enters a sedimentation tank for sedimentation and clarification, and clarified supernatant enters a raw water tank;
s2, enabling water in the raw water tank to enter a ceramic ultrafiltration device through a first booster pump for micro cross flow filtration, enabling produced water to enter a produced water tank, and enabling concentrated water to enter a reaction tank;
s3, water in the water producing pool enters a security filter through a second booster pump to be filtered and then enters a reverse osmosis device, and finally is output and recycled through a water purifying pipe;
s4, after the S1-S3 is operated for a period of time, washing and descaling or acid adding and descaling are carried out, wherein the washing and descaling are as follows: the backwash pump adopts variable frequency control, the output power of the backwash pump is adjusted upwards, the water yield of the backwash pump is improved, water in the water producing pool enters the ceramic ultrafiltration device through the water producing port, and the ceramic membrane can be reversely flushed due to the reverse water flow direction and the water producing direction of the ceramic ultrafiltration device, so that the scaling on the surface of the ceramic membrane is avoided (the ceramic ultrafiltration device operates in a high pH value environment, and the surface of the ceramic membrane is easy to scale); meanwhile, the blower is utilized to charge air into the water inlet of the ceramic ultrafiltration device, so that flushing water in the ceramic ultrafiltration device can enter the reaction tank through the concentrated water inlet, and capacity is provided for continuously flushing the ceramic membrane; adding acid to remove scale: the output power of the backwash pump is regulated downwards, the water yield of the backwash pump is reduced, acid is added into a water pipe between a water outlet and a water producing port of the backwash pump, after soaking for a certain time, a first booster pump is started, and mixed solution of the acid and the water enters a water producing tank from the water producing port of the ceramic ultrafiltration device;
s5, adopting a shutdown emptying method for preventing scaling on the surface of the membrane, and opening an emptying valve to empty water in the ceramic ultrafiltration device when the ceramic ultrafiltration device is shut down.
Drawings
FIG. 1 is a schematic diagram of a high-throughput ceramic ultrafiltration water treatment system according to the present utility model;
FIG. 2 is a schematic diagram of a ceramic ultrafiltration device in a high-throughput ceramic ultrafiltration water treatment system according to the present utility model.
In the drawings, the list of components represented by the various numbers is as follows:
1. raw water pipe, 2, water purifying pipe, 3, reaction tank, 4, sedimentation tank, 5, raw water tank, 6, first booster pump, 7, ceramic ultrafiltration device, 71, water inlet, 72, water producing port, 73, concentrated water port, 8, water producing tank, 9, alkali adding device, 10, flocculating agent adding device, 11, blower, 12, backwash pump, 13, first acid adding device, 14, second booster pump, 15, filter, 16, reverse osmosis device, 17, second acid adding device, 18, and emptying valve.
Detailed Description
The principles and features of the present utility model are described below with reference to the drawings, the examples are illustrated for the purpose of illustrating the utility model and are not to be construed as limiting the scope of the utility model.
As shown in fig. 1, a high flux ceramic ultrafiltration water treatment system comprising: a raw water pipe 1, a reaction tank 3, a sedimentation tank 4, a raw water tank 5, a first booster pump 6, a ceramic ultrafiltration device 7, a water producing tank 8, an alkali adding device 9 and a flocculating agent adding device 10,
the raw water pipe 1, the reaction tank 3, the sedimentation tank 4, the raw water tank 5, the first booster pump 6, the ceramic ultrafiltration device 7 and the water outlet and the water inlet of the water producing tank 8 are sequentially connected in series through water pipes; the discharge ports of the alkali adding device 9 and the flocculating agent adding device 10 are communicated with the water inlet of the raw water pipe 1.
In some specific embodiments, the ceramic ultrafiltration device (7) is provided with a water inlet (71), a water producing port (72) and a concentrated water port (73), wherein the water inlet (71) is communicated with the water outlet of the first booster pump (6) through a water pipe, and the water producing port (72) is communicated with the water inlet of the water producing tank (8) through a water pipe; the water concentration port 73 is communicated with the water inlet of the reaction tank 3; the air outlet of the blower 11 is correspondingly communicated with a water pipe between the water outlet of the first booster pump 6 and the water inlet 71; the water inlet of the backwash pump 12 is connected to the interior of the water producing reservoir 8 and the water outlet thereof is connected to the water producing port 72.
In some specific embodiments, the acid adding device may further comprise a first acid adding device 13, and the backwash pump 12 is a variable-frequency water pump; the discharge port of the first acid adding device 13 is correspondingly communicated with a water pipe between the water outlet of the backwash pump 12 and the water producing port 72.
In some embodiments, the ceramic ultrafiltration device 7 may also be provided with a drain opening and a drain valve 18 is mounted in correspondence of the water pipe at the drain opening.
In some specific embodiments, the water treatment device further comprises a second booster pump 14, a filter 15, a reverse osmosis device 16 and a water purifying pipe 2, wherein the water outlets and water inlets of the second booster pump 14, the filter 15, the reverse osmosis device 16 and the water purifying pipe 2 are sequentially connected in series through the water pipes, and the water inlet of the second booster pump 14 is communicated with the water outlet of the water producing tank 8.
In some specific embodiments, the device further comprises a second acid adding device 17, wherein a discharge port of the second acid adding device 17 is correspondingly communicated with a water pipe between a water outlet of the second booster pump 14 and a water inlet of the filter 15.
In some embodiments, filter 15 may be a cartridge filter.
Specifically, the operation flux of the ceramic ultrafiltration device 7 is 200LMH-500LMH, the hardness of the effluent is 50 mg/L-100 mg/L, and the error flow is 30% -40%.
Specifically, the backwashing period of the ceramic membrane inside the ceramic ultrafiltration device 7 is 10min-60min.
Example 1
Sampling raw water: the chemical industry circulation sewage of Shandong Min, turbidity 36NTU, COD26.7, calcium ion 38 mg/L, magnesium ion 69.8 mg/L, total hardness 161 mg/L (calculated by calcium carbonate) petroleum 0.11 mg/L;
the ceramic membrane is selected from: the model of the composite material is CM-122, the aperture is 30nm, the area is 27 square meters, and the composite material is zirconium-aluminum composite material
Cartridge filter with aperture 5 μm for market purchase;
reverse osmosis membrane, dow company BW30FR-400/34
The water treatment method comprises the following steps: the circulating sewage enters a raw water pipe 1, the pH value is adjusted to 12 by quantitatively adding sodium hydroxide and sodium carbonate through an alkali adding device 9, the flocculating agent ferric sulfate is quantitatively added through a flocculating agent adding device 10, the mixed sewage enters a reaction tank 3 for mixing reaction, the water after mixing reaction in the reaction tank 3 enters a sedimentation tank 4 for sedimentation and clarification, and the clarified supernatant enters a raw water tank 5; starting a first booster pump 6 to pump water in a raw water tank 5 into a ceramic ultrafiltration device 7 for micro cross-flow filtration, enabling produced water to enter a water producing tank 8, and enabling concentrated water to enter a reaction tank 3; the water in the water producing pool 8 enters a security filter through a second booster pump 14 to be filtered and then enters a reverse osmosis device 16, and finally is output through a water purifying pipe 2 to be reused for supplementing water to circulating water;
the ceramic ultrafiltration device 7 adopts micro cross-flow filtration, the cross-flow rate is 30%, the transmembrane pressure difference is 0.7MPa, the operation flux is 420LMH, and the ceramic membrane is used after 40 minutes of operationSurface pollution, rising the transmembrane pressure difference to 0.8MPa, adopting air-water backwashing at the moment, stopping the first booster pump 6, starting the backwashing pump 12, adopting variable frequency control for the backwashing pump 12, and starting the blower 11, pumping water in the water producing tank 8 along the water producing port 72 through the backwashing pump 12, carrying out back flushing on the ceramic membrane, and controlling the backwashing flow to be 15m 3 And/h flushing plugs in the ceramic membrane pores while gas is blown in along the water inlet 71 at a flow rate of 5m 3 And (h) mixing air and water to form dissolved air and water, flushing a mixture formed by calcium and magnesium suspended matters on the surface of the ceramic membrane and a flocculating agent by the dissolved air and water, discharging the mixture into a reaction tank 3 from a concentrated water port 73, backwashing for 90 seconds, and recovering a transmembrane pressure difference to an initial state after backwashing is finished;
in order to prevent the scaling of the membrane surface, a shutdown draining method is adopted, when the ceramic ultrafiltration device 7 is shut down, a draining valve 18 is opened, and water in the ceramic ultrafiltration device 7 is drained.
After 3 days of operation, the transmembrane pressure difference is increased to 0.10MPa, the transmembrane pressure difference cannot be reduced by gas-water mixed backwashing, at the moment, the acid adding mode is adopted, the first booster pump 6 is stopped, the backwashing pump 12 is started, the backwashing pump 12 adopts variable frequency control, and the backwashing flow is 5m 3 And (3) simultaneously starting the first acid adding device 13, mixing acid with water, pumping the mixed acid into the ceramic ultrafiltration device 7 along the water outlet 72, adding hydrochloric acid with the acid type, mixing the mixed acid with water, stopping the backwash pump 12 after soaking for 15 minutes, closing the blower 11, starting the first booster pump 6, starting the ceramic ultrafiltration device 7 to normally operate, recovering the transmembrane pressure difference to 0.7MPa, and operating the flux 420LMH.
After stable operation for one month, detecting the water quality: turbidity was not detected, COD11.9, calcium ions 4.33 mg/L, magnesium ions 1.63 mg/L, total hardness 17.6 mg/L (calculated as calcium carbonate) of petroleum was not detected, SDI value was 1.3;
the chemical cleaning period of the ceramic ultrafiltration device 7 is 2 months, the replacement period of the cartridge filter element of the cartridge filter is 4 months, the recovery rate of the reverse osmosis device is 90.6%, the cleaning period of the reverse osmosis membrane in the first and second sections is 9 months, and the cleaning period in the third section is 6 months.
Example 2
The difference is pH8.5 as in example 1;
long-term operating flux 180LMH
Example 3
The same as in example 1, except that the shutdown evacuation device was not installed:
the backwashing acid adding period is 4 times per day, and the chemical cleaning period is 7 days and 1 time
Example 4
The same as in example 1 was distinguished in that no flocculant and gas-water mixed backwash was used, the backwash acid addition period was 4 times per day, and the chemical cleaning period was 1 time per 3 days.
The embodiment 1-4 shows that the pH value of the added alkali is 10-12, the ceramic ultrafiltration device 7 is provided with a shutdown emptying device, the flocculant and the air-water are adopted for mixed backwashing, the flux of the ceramic membrane can reach more than 400LMH, and the SDI value is less than 2;
example 5
Sampling raw water: concentrated water after reverse osmosis treatment of yellow river water in Taihe company factory, with conductivity 3236 mu S/cm and total hardness 912mg/L (calculated by calcium carbonate)
The ceramic membrane is selected from: the model of the composite material is CM-122, the aperture is 30nm, the area is 27 square meters, and the composite material is zirconium-aluminum composite material
Cartridge filter with aperture 5 μm for market purchase;
reverse osmosis membrane, dow company BW30FR-400/34
The water treatment method comprises the following steps: the reverse osmosis concentrated water enters a raw water pipe 1, sodium hydroxide and sodium carbonate are quantitatively added through an alkali adding device 9 to adjust the pH value to 10.5, flocculating agent ferric sulfate is quantitatively added through a flocculating agent adding device 10, the mixed water enters a reaction tank 3 to carry out a mixing reaction, the water after the mixing reaction in the reaction tank 3 enters a sedimentation tank 4 to carry out sedimentation and clarification, and clarified supernatant enters a raw water tank 5; starting a first booster pump 6 to pump water in a raw water tank 5 into a ceramic ultrafiltration device 7 for micro cross-flow filtration, enabling produced water to enter a water producing tank 8, and enabling concentrated water to enter a reaction tank 3; the water in the water producing pool 8 enters a security filter through a second booster pump 14 to be filtered and then enters a reverse osmosis device 16, and finally is output through a water purifying pipe 2;
the ceramic ultrafiltration device 7 adopts micro cross-flow filtration, the cross-flow rate is 15%, the transmembrane pressure difference is 0.9MPa, the operation flux is 360LMH, and the membrane is transmembrane after 20 minutes of operation due to the surface pollution of the membraneThe pressure difference is increased to 0.10MPa, at this time, air-water backwashing is adopted, the first booster pump 6 is stopped, the backwashing pump 12 is started, the backwashing pump 12 is controlled by variable frequency, the blower 11 is started, water in the water producing tank 8 is pumped into the water producing port 72 through the backwashing pump 12, the ceramic membrane is reversely washed, and the backwashing flow is 10m 3 And/h flushing plugs in the ceramic membrane pores while gas is blown in along the water inlet 71 at a flow rate of 8m 3 And (h) mixing air and water to form dissolved air and water, flushing a mixture formed by calcium and magnesium suspended matters on the surface of the ceramic membrane and a flocculating agent by the dissolved air and water, discharging the mixture into a reaction tank 3 from a concentrated water port 73, backwashing for 60 seconds, and recovering a transmembrane pressure difference to an initial state after backwashing is finished;
in order to prevent the scaling of the membrane surface, a shutdown draining method is adopted, when the ceramic ultrafiltration device 7 is shut down, a draining valve 18 is opened, and water in the ceramic ultrafiltration device 7 is drained.
After 5 days of operation, the transmembrane pressure difference is increased to 0.12MPa, the transmembrane pressure difference cannot be reduced by gas-water mixed backwashing, at the moment, the acid adding mode is adopted, the first booster pump 6 is stopped, the backwashing pump 12 is started, the backwashing pump 12 adopts variable frequency control, and the backwashing flow is 3m 3 And (3) simultaneously starting the first acid adding device 13, mixing acid with water, pumping the mixed acid into the ceramic ultrafiltration device 7 along the water outlet 72, adding hydrochloric acid with the acid type, mixing the mixed acid with water, stopping the backwash pump 12 after soaking for 15 minutes, closing the blower 11, starting the first booster pump 6, starting the ceramic ultrafiltration device 7 to normally operate, recovering the transmembrane pressure difference to 0.9MPa, and operating the flux of 360LMH.
After stable operation for 20 days, water quality is detected: turbidity was not detected, COD was 11.9, total hardness was 80.8 mg/L (calculated as calcium carbonate), SDI value was 1.1;
the recovery rate of the reverse osmosis device is 90.6 percent.
Example 6
The same as in example 1 was repeated, except that the backwash pump 12 and the first acid adding device 13 were not added, and the chemical cleaning cycle was 1 time for 4 days.
Example 7
The same as in example 1, except that flocculant was changed to polyaluminum chloride
The recovery rate of the reverse osmosis device is reduced to 75 percent, and the chemical cleaning period is shortened to 2 months.
It can be obtained from examples 5-7 that the ceramic ultrafiltration device 7 is added with a backwash pump 12 and a first acid adding device 13, and an iron flocculant is adopted, the chemical cleaning period of the ceramic ultrafiltration device 7 can reach 2 months, the replacement period of the cartridge of the security filter can reach 4 months, the recovery rate of the reverse osmosis device can reach 90.6%, the cleaning period of the reverse osmosis membrane in the first and second sections can reach 9 months, and the cleaning period in the third section can reach 6 months.
The foregoing is only illustrative of the present utility model and is not to be construed as limiting thereof, but rather as various modifications, equivalent arrangements, improvements, etc., within the spirit and principles of the present utility model.
Claims (9)
1. A high flux ceramic ultrafiltration water treatment system comprising: raw water pipe (1), reaction tank (3), sedimentation tank (4), raw water tank (5), first booster pump (6), ceramic ultrafiltration device (7), water producing tank (8), alkali adding device (9) and flocculating agent adding device (10),
the raw water pipe (1), the reaction tank (3), the sedimentation tank (4), the raw water tank (5), the first booster pump (6), the ceramic ultrafiltration device (7) and the water outlet and the water inlet of the water producing tank (8) are sequentially connected in series through water pipes; the discharge ports of the alkali adding device (9) and the flocculating agent adding device (10) are communicated with the water inlet of the raw water pipe (1).
2. The high-flux ceramic ultrafiltration water treatment system according to claim 1, further comprising a blower (11) and a backwash pump (12), wherein the ceramic ultrafiltration device (7) is provided with a water inlet (71), a water producing port (72) and a concentrated water port (73), the water inlet (71) is communicated with the water outlet of the first booster pump (6) through a water pipe, and the water producing port (72) is communicated with the water inlet of the water producing tank (8) through a water pipe; the water concentration port (73) is communicated with a water inlet of the reaction tank (3); the air outlet of the blower (11) is correspondingly communicated with a water pipe between the water outlet of the first booster pump (6) and the water inlet (71); the water inlet of the backwash pump (12) is communicated with the interior of the water producing tank (8) and the water outlet of the backwash pump is communicated with the water producing port (72).
3. A high flux ceramic ultrafiltration water treatment system according to claim 2, further comprising a first acid adding device (13), said backwash pump (12) being a variable frequency water pump; the discharge port of the first acid adding device (13) is correspondingly communicated with a water pipe between the water outlet of the backwash pump (12) and the water producing port (72).
4. A high throughput ceramic ultrafiltration water treatment system according to claim 2, wherein said ceramic ultrafiltration device (7) is further provided with a drain port and a drain valve (18) is mounted in correspondence of a water pipe at said drain port.
5. The high-flux ceramic ultrafiltration water treatment system according to claim 1, further comprising a second booster pump (14), a filter (15), a reverse osmosis device (16) and a water purifying pipe (2), wherein the water outlets and water inlets of the second booster pump (14), the filter (15), the reverse osmosis device (16) and the water purifying pipe (2) are sequentially connected in series through the water pipe, and the water inlet of the second booster pump (14) is connected with the water outlet of the water producing tank (8).
6. The high-flux ceramic ultrafiltration water treatment system according to claim 5, further comprising a second acid adding device (17), wherein a discharge port of the second acid adding device (17) is correspondingly communicated with a water pipe between a water outlet of the second booster pump (14) and a water inlet of the filter (15).
7. A high flux ceramic ultrafiltration water treatment system according to claim 5, wherein said filter (15) is a cartridge filter.
8. The high-flux ceramic ultrafiltration water treatment system according to claim 1, wherein the operation flux of the ceramic ultrafiltration device (7) is 200-500 LMH, the hardness of the outlet water is 50 mg/L-100 mg/L, and the error flow is 30% -40%.
9. A high flux ceramic ultrafiltration water treatment system according to claim 1, wherein the backwash cycle of the ceramic membranes inside the ceramic ultrafiltration device (7) is 10min-60min.
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