CN110745910B - Honeycomb ceramic membrane filtering method and filtering device - Google Patents
Honeycomb ceramic membrane filtering method and filtering device Download PDFInfo
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- CN110745910B CN110745910B CN201911259458.8A CN201911259458A CN110745910B CN 110745910 B CN110745910 B CN 110745910B CN 201911259458 A CN201911259458 A CN 201911259458A CN 110745910 B CN110745910 B CN 110745910B
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- 239000012528 membrane Substances 0.000 title claims abstract description 199
- 239000000919 ceramic Substances 0.000 title claims abstract description 156
- 238000001914 filtration Methods 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 177
- 238000011010 flushing procedure Methods 0.000 claims abstract description 51
- 230000004907 flux Effects 0.000 claims abstract description 31
- 230000000737 periodic effect Effects 0.000 claims abstract description 23
- 238000005374 membrane filtration Methods 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims abstract description 11
- 230000002457 bidirectional effect Effects 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 6
- 231100000719 pollutant Toxicity 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims description 43
- 239000012141 concentrate Substances 0.000 claims description 31
- 238000010992 reflux Methods 0.000 claims description 31
- 239000006228 supernatant Substances 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000011049 filling Methods 0.000 claims description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 239000010865 sewage Substances 0.000 claims description 11
- 238000004140 cleaning Methods 0.000 claims description 10
- 239000012459 cleaning agent Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- 230000008929 regeneration Effects 0.000 claims description 8
- 238000011069 regeneration method Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 239000008367 deionised water Substances 0.000 claims description 6
- 229910021641 deionized water Inorganic materials 0.000 claims description 6
- 238000001514 detection method Methods 0.000 claims description 6
- 239000003153 chemical reaction reagent Substances 0.000 claims description 5
- 239000011259 mixed solution Substances 0.000 claims description 5
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 4
- 229910017604 nitric acid Inorganic materials 0.000 claims description 4
- 238000009295 crossflow filtration Methods 0.000 claims description 3
- 230000007935 neutral effect Effects 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 238000002791 soaking Methods 0.000 claims description 3
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 13
- 230000008569 process Effects 0.000 abstract description 10
- 230000010349 pulsation Effects 0.000 abstract description 4
- 230000002349 favourable effect Effects 0.000 abstract description 2
- 230000008901 benefit Effects 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 230000000712 assembly Effects 0.000 description 3
- 238000000429 assembly Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 241001391944 Commicarpus scandens Species 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- 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
- B01D2321/02—Forward flushing
-
- 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
- B01D2321/04—Backflushing
-
- 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
- B01D2321/16—Use of chemical agents
- B01D2321/162—Use of acids
-
- 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
- B01D2321/16—Use of chemical agents
- B01D2321/164—Use of bases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- 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
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a honeycomb ceramic membrane filtration method and a filtration device, wherein the liquid to be treated enters a honeycomb ceramic membrane component for filtration in a bidirectional periodical conversion feeding mode; the periodic back flushing is realized during filtering, and the same frequency of periodic forward flushing is matched. The invention adopts bidirectional pulsation feeding, is favorable for fully utilizing turbulence caused by periodical direction conversion to reduce membrane pollution, and fully utilizes the membrane area with lighter pollution at the inlet end part and the outlet end part so as to maintain higher membrane flux operation; the periodic gas-dissolved mixed liquid backflushing is adopted, so that the ceramic membrane aeration head and the gas-dissolved principle are fully exerted, nano-level bubbles and liquid mixed liquid are generated for backflushing, the backflushing effect is enhanced, a backflushing pump is not needed, and energy is saved; the back flushing process is carried out at the same time and with the same frequency, and the liquid is adopted as the forward flushing medium, so that the back flushed pollutant can be brought out of the system in time, and the flux can be recovered instantaneously on line.
Description
Technical Field
The invention relates to a honeycomb ceramic membrane filtering method and a filtering device, and belongs to the field of ceramic membrane application.
Background
The honeycomb ceramic membrane (PCR membrane) is also sintered from inorganic ceramic materials such as alumina, titanium oxide, zirconia, silicon oxide and the like under high temperature conditions, has a similar structure of a tubular multichannel ceramic membrane and also has chemical stability and mechanical strength of the multichannel ceramic membrane, but has the advantage of higher membrane area per unit volume than the multichannel ceramic membrane due to the much denser channel distribution per unit volume than the multichannel ceramic membrane, namely higher packing area per unit volume of the inner membrane. The high filling area not only improves the treatment scale of ceramic membrane equipment and occupies smaller area, but also reduces the treatment cost of the ceramic membrane and has more dominant investment cost.
The honeycomb ceramic membrane has the advantages, so that the application to water treatment, especially to water purification treatment, is possible. Honeycomb ceramic membranes are also currently limited to research into membrane elements and components, such as: CN102172477a shows a method for manufacturing a combined honeycomb ceramic membrane filter element, the honeycomb ceramic membrane has higher permeation flux and high packing area in unit volume, and the configuration and preparation process are simple; CN204799114U shows a honeycomb ceramic membrane module for use in the manufacture of purified water, but such module is only applicable to filtration applications for domestic water; CN208943852U shows another tubular honeycomb ceramic membrane module which is convenient to install and maintain and clean. All this is also only a study on membrane elements and components, lacking in-depth research and improvement for specific applications of honeycomb ceramic membranes.
Disclosure of Invention
The invention provides a honeycomb ceramic membrane filtering method and a filtering device, which fully utilize the advantages of high strength, good chemical stability, narrow pore size distribution and the like of ceramic membranes according to a pollution mechanism in the honeycomb ceramic membrane filtering process, creatively use the schemes of pulse feeding from two ends of the membranes, frequent back flushing of dissolved gas mixed liquid, normal flushing of liquid with the same frequency in the process and the like on the basis of the existing terminal or micro cross flow filtering process, greatly reduce membrane pollution formed in the filtering process, prolong the membrane cleaning period and improve the flux.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
in the honeycomb ceramic membrane filtration method, the liquid to be treated enters a honeycomb ceramic membrane component for filtration in a bidirectional periodical conversion feeding mode; the periodic back flushing is realized during filtering, and the same frequency of periodic forward flushing is matched.
The application starts from reducing membrane pollution in the honeycomb ceramic membrane filtration process, and adopts a bidirectional pulsation feeding mode to assist with the back flushing of the mixed solution of dissolved gas, and simultaneously carries out the liquid forward flushing with the same frequency, thereby greatly reducing the membrane pollution and improving the flux.
In order to further reduce membrane pollution, the periodic backflushing takes the mixed solution of dissolved gas as a medium; periodically, liquid is used as medium.
In order to improve the backflushing effect, the mixed solution of dissolved gas for periodic backflushing is a backflushing medium formed by aerating gas with the pressure of 0.3-0.5 MPa through a ceramic membrane with the aperture of 20-100 nm.
In order to further reduce membrane pollution, reduce energy consumption and enhance recycling of materials, the liquid used for periodic backflushing is clear liquid flowing out of the honeycomb ceramic membrane assembly; the periodic liquid is flushing with the liquid to be treated as medium.
When the pollution of the film is heavy and the recoil effect of the dissolved gas mixed liquid is still not ideal, 0.5-5% w/w cleaning agent can be added into the liquid used for periodical recoil. % w/w is the mass percent of the cleaning agent relative to the liquid used for the periodic backflushing. The cleaning agent can be one or more of sodium chlorate, sodium hydroxide, hydrochloric acid, nitric acid and the like.
In order to achieve both filtration efficiency and membrane life, backflushing and forward flushing are performed when the inlet pressure rise of the honeycomb ceramic membrane assembly is greater than 0.5 times or when the membrane flux drop of the honeycomb ceramic membrane assembly is greater than 20%.
In order to further ensure the filtering effect, the time of back flushing and forward flushing is based on that the flux of the honeycomb ceramic membrane is recovered to more than 93% of the original flux.
In order to further reduce membrane pollution, the liquid to be treated is filtered by a coarse filter and pumped into a honeycomb ceramic membrane assembly by a pump, and micro cross flow or dead end filtration is adopted.
In order to achieve both filtration efficiency and membrane life, the filtration accuracy of the coarse filter is 30 mesh or less.
In order to ensure the filtering effect and improve the service life of the membrane, when the inlet pressure rising amount of the honeycomb ceramic membrane component is more than 1-2 times or the membrane flux falling amount of the honeycomb ceramic membrane component is more than 50-1 times, chemical cleaning regeneration is carried out. Chemical cleaning and regeneration: after the concentrated solution side and the clear solution side of the ceramic membrane component are respectively washed clean by deionized water, 0.5-5% w/w of cleaning agent (such as one or more of sodium hypochlorite, sodium hydroxide, hydrochloric acid, nitric acid and the like) is added for cross-flow cleaning and soaking, and the regenerated ceramic membrane component is washed by deionized water again until the pH value is neutral; and then detecting the cleaned and regenerated membrane assembly under the same condition as the initial flux detection before membrane filtration, and comparing the data of the cleaned and regenerated membrane assembly with the initial flux detection to ensure whether the honeycomb ceramic membrane is completely cleaned and regenerated, wherein the regeneration is generally considered to be completed when the membrane flux recovery rate is more than 90%.
A honeycomb ceramic membrane filter device comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid return manifold, a honeycomb ceramic membrane component, a backflushing liquid tank, a dissolved air tank and a backflushing air source;
The top of the ceramic membrane component is provided with an upper feed and discharge port and a supernatant port, and the bottom of the ceramic membrane component is provided with a lower feed and discharge port and a backflushing inlet;
The raw liquid tank, the feed pump and the inlet of the coarse filter are sequentially communicated through a pipeline; the outlet of the coarse filter is connected with a feeding pipe, the feeding pipe is branched into an upper feeding pipe and a lower feeding pipe (namely, one end of the feeding pipe is communicated with the outlet of the coarse filter, the other end of the feeding pipe is branched into an upper feeding pipe and a lower feeding pipe), the upper feeding pipe is communicated with an upper feeding hole and a lower feeding hole of the ceramic membrane assembly, a first feeding valve is arranged on the upper feeding pipe, the lower feeding pipe is communicated with a lower feeding hole of the ceramic membrane assembly, and a second feeding valve is arranged on the lower feeding pipe;
One end of a concentrate return manifold extends into the concentrate tank from the top of the concentrate tank, the other end of the concentrate return pipe is branched into a first concentrate return pipe, a second concentrate return pipe and a concentrate blow-off pipe, the first concentrate return pipe is communicated with an upper feed inlet and a lower feed outlet of the ceramic membrane assembly, and a first concentrate return valve is arranged on the first concentrate return pipe: the second thick liquid return pipe is communicated with the lower feed and discharge port of the ceramic membrane component, and a second thick liquid return valve is arranged on the second thick liquid return pipe: the concentrated solution blow-down pipe can be led to a sewage tank and the like for further treatment, and a blow-down valve is arranged on the concentrated solution blow-down pipe; a concentrated solution reflux main pipe before branching is provided with a concentrated solution reflux main valve;
The device comprises a supernatant port of a ceramic membrane assembly, a backflushing liquid tank, a dissolved air tank and a backflushing inlet of the ceramic membrane assembly, wherein the supernatant port of the ceramic membrane assembly, the backflushing liquid tank, the dissolved air tank and the backflushing inlet of the ceramic membrane assembly are sequentially communicated through pipelines, a supernatant control valve is arranged on the pipeline between the supernatant port of the ceramic membrane assembly and the backflushing liquid tank, a liquid filling valve is arranged on the pipeline between the backflushing liquid tank and the backflushing inlet of the ceramic membrane assembly, a backflushing air source is connected with an inlet of a ceramic membrane aeration device in the dissolved air tank through the pipeline, small bubbles with the diameter of 20-100 nm are uniformly distributed in the dissolved air tank after the ceramic membrane aeration device is aerated, an outlet of the dissolved air tank is communicated with the backflushing inlet of the ceramic membrane assembly, a backflushing air inlet valve is arranged between the backflushing air source and the ceramic membrane aeration device in the dissolved air tank, and an exhaust valve is also arranged on the dissolved air tank;
the clear liquid output pipe is arranged on the back flushing liquid tank, and the clear liquid output pipe is provided with a clear liquid discharge valve. The clear liquid output pipe can be connected to a clear liquid tank or other pipe networks for direct utilization.
In order to improve the recoil effect, the honeycomb ceramic membrane filtering device further comprises a dosing tank and a dosing pump, wherein the dosing tank, the dosing pump and the dissolved air tank are sequentially connected through pipelines, and a dosing control valve is arranged on the pipeline between the dosing pump and the dissolved air tank. When the pollution of the film is heavy and the backflushing effect of the dissolved gas mixed liquid is still not ideal, the chemical reagent is added into the backflushing liquid to backflush when the film is backflushed, and the chemical reagent are sequentially opened at the inlet of the backflushing pump. For example, 0.5 to 5% w/w cleaning agent may be added to the liquid used for periodic backflushing. % w/w is the mass percent of the cleaning agent relative to the liquid used for the periodic backflushing. The cleaning agent can be one or more of sodium chlorate, sodium hydroxide, hydrochloric acid, nitric acid and the like.
The application can add meters, valves and the like on each part and each pipeline according to the needs.
The membrane component is tubular and is provided with two inlet (outlet) ports and two clear liquid outlet ports; the honeycomb ceramic membrane assemblies are vertically arranged.
The honeycomb ceramic membrane assembly is provided with one or more than two honeycomb ceramic membrane assemblies which are connected in parallel, and the honeycomb ceramic membrane assembly can be specifically selected according to the treatment capacity of water and the like. When the honeycomb ceramic membrane assembly has more than two parallel connection, all the upper feed and discharge ports are converged to form a total upper feed and discharge port, all the supernatant fluid ports are converged to form a total supernatant fluid port, all the lower feed and discharge ports are converged to form a total lower feed and discharge port, and all the backflushing inlets are converged to form a total backflushing inlet.
The method for treating sewage by using the honeycomb ceramic membrane filtering device comprises the following steps of: after the liquid to be treated enters the raw liquid tank, the liquid is conveyed to a coarse filter through a feed pump, and after prefiltering is carried out, the liquid is periodically switched through a first feed valve and a second feed valve to carry out bidirectional periodic conversion feeding on the honeycomb ceramic membrane assembly; when dead-end filtration is performed, clear liquid flows out from a clear liquid port of the honeycomb ceramic membrane assembly, firstly enters a backflushing liquid tank, is discharged to the clear liquid tank through a clear liquid discharge valve or is directly used for a pipe network and the like, clear liquid entering the backflushing tank is filled into a solution tank through a solution filling valve, and the solution filling valve is closed after the solution tank reaches a specified liquid level; when micro cross-flow filtration is adopted, the trend of the clear liquid is the same as that of dead-end filtration, and the trend of the concentrated liquid is as follows: when the pre-filtered material enters from the upper feed inlet and outlet, the first thick liquid reflux valve is closed, the second thick liquid reflux valve is opened, and thick liquid flows out from the lower feed inlet and outlet of the honeycomb ceramic membrane assembly and flows back to the raw water tank through the thick liquid reflux main valve; when the pre-filtered material enters from the lower feed inlet and outlet, the second concentrated solution reflux valve is closed, the first concentrated solution reflux valve is opened, and concentrated solution flows out from the upper feed inlet and outlet of the honeycomb ceramic membrane assembly and flows back to the raw water tank through the concentrated solution reflux main valve;
When the liquid to be treated is filtered, periodic recoil and periodic forward flushing with the same frequency are realized: when the inlet pressure rise of the honeycomb ceramic membrane assembly is more than 0.5 times or when the membrane flux drop of the honeycomb ceramic membrane assembly is more than 20%, the backflushing and the forward flushing are simultaneously carried out. Recoil: the feed pump is not stopped, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are firstly closed, the backflushing air inlet valve is opened, the pressure is kept at 0.3-0.5 MPa for 10-15 seconds, then the backflushing liquid inlet valve is opened after 10-15 seconds, after the backflushing is finished, the backflushing air inlet valve and the backflushing liquid inlet valve are closed, and the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are opened to recover normal filtration; forward flushing: and when the back flushing is finished, the feed pump is continuously stopped, the concentrated solution reflux main valve is closed, the blow-off valve is opened, membrane pollutants which are back flushed are discharged to the sewage tank through the blow-off valve, and after the normal flushing is finished, the concentrated solution reflux main valve is opened, and meanwhile, the blow-off valve is closed, so that normal filtration is recovered.
In order to improve the filtration efficiency, the back flushing and forward flushing time is based on that the flux of the honeycomb ceramic membrane is recovered to more than 93% of the original flux.
After the dissolved air tank reaches the designated liquid level, the liquid filling valve is closed, and the liquid in the dissolved air tank is not smaller than the amount required by one back flushing.
The terms of up and down, left and right, top, bottom, horizontal, vertical and other directions refer to the relative positions of the device in normal use.
The control of the opening, closing, starting and stopping of each valve and each device can realize automatic control according to the existing automatic control technology.
The technology not mentioned in the present invention refers to the prior art, for example, refer to Xu Naping et al, inorganic membrane separation technology and application (chemical industry Press, 2003), and the like.
The honeycomb ceramic membrane filtration method starts from reducing membrane pollution in the honeycomb ceramic membrane filtration process, and adopts a bidirectional pulsation feeding mode to assist in backflushing by dissolved gas mixed liquid, and simultaneously carries out liquid forward flushing at the same frequency, thereby greatly reducing membrane pollution and improving flux; has obvious advancement, and has the following advantages compared with the multi-channel tubular ceramic membrane and hollow fiber organic membrane filtration process:
1. The application provides a ceramic membrane filtering method with high filling area, the high filling area means that the treatment capacity in unit volume is large, compared with a multi-channel ceramic membrane, the investment cost is greatly reduced, and the energy consumption and the treatment cost are also greatly reduced by adding a micro cross flow or dead end filtering mode, so that the competitiveness of the ceramic membrane for water purification treatment is improved and becomes possible;
2. The application adopts bidirectional pulsation feeding, is favorable for fully utilizing turbulence caused by periodical direction conversion to reduce membrane pollution, and fully utilizes the membrane area with lighter pollution at the inlet end part and the outlet end part so as to maintain higher membrane flux operation;
3. the application adopts periodic gas-dissolved mixed liquid backflushing, skillfully applies the gas-dissolved principle to the honeycomb ceramic membrane backflushing process, utilizes the nano-scale ceramic membrane as an aeration head, ensures that the gas in the backflushing medium-gas-dissolved mixed liquid is uniformly distributed, removes impurities such as dust and the like, has bubbles smaller than or equal to the membrane aperture, strengthens the effective backflushing removal effect on pollution caused by membrane hole blockage and membrane surface deposition, and utilizes the pressure in a gas dissolving tank as backflushing power; compared with the method that only liquid is used for backflushing the hollow fiber organic membrane, the method has the advantages that the backflushing effect is good, the defects that the organic membrane is easy to break and is not corrosion-resistant are overcome, a backflushing pump is not needed as power, and energy is saved;
4. The application carries out periodic forward flushing with the same frequency at the same time of the back flushing process, adopts liquid as a forward flushing medium, not only timely brings the back flushed pollutant out of the system, but also can flush the pollutant on the membrane surface more effectively than gas by using the liquid, can recover flux instantaneously on line, and also has promotion effect on the high flux operation of the honeycomb ceramic membrane.
Drawings
FIG. 1 is a schematic diagram of a honeycomb ceramic membrane filtration device of the present invention;
in the figure, 1, a raw liquid tank; 2. a feed pump; 3. a coarse filter; 4. a honeycomb ceramic membrane assembly; 4-1, a lower feed inlet and a lower feed outlet; 4-2, upper feed and discharge ports; 4-3, recoil inlet; 4-4, a supernatant port; 5. a backflushing liquid tank; 6. a dissolved air tank; 7. a dosing pump; 8. a dosing box; 9. a first concentrate return valve; a second concentrate return valve; 10. a first feed valve; 11 a second feed valve; 13. a clear liquid control valve; 14. a back flushing liquid inlet valve; 15. recoil air inlet valve; 16. a clear liquid discharge valve; 17. a dosing control valve; 18. a concentrate reflux main valve; 19. a blow-down valve; 20. a charging valve; 21. an emptying valve of the dissolved air tank; a. stock solution (to-be-treated solution); b. a backflushing air source; c. clear liquid; d. a medicament; e. and (3) sewage.
Detailed Description
For a better understanding of the present invention, the following examples are further illustrated, but are not limited to the following examples.
As shown in FIG. 1, the honeycomb ceramic membrane filtering device comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid return main pipe, a honeycomb ceramic membrane assembly, a backflushing liquid tank, a dissolved air tank and a backflushing air source;
The top of the ceramic membrane component is provided with an upper feed and discharge port and a supernatant port, and the bottom of the ceramic membrane component is provided with a lower feed and discharge port and a backflushing inlet;
The raw liquid tank, the feed pump and the inlet of the coarse filter are sequentially communicated through a pipeline; the outlet of the coarse filter is connected with a feeding pipe, the feeding pipe is branched into an upper feeding pipe and a lower feeding pipe, the upper feeding pipe is communicated with an upper feeding hole and a lower feeding hole of the ceramic membrane assembly, a first feeding valve is arranged on the upper feeding pipe, the lower feeding pipe is communicated with a lower feeding hole and a lower feeding hole of the ceramic membrane assembly, and a second feeding valve is arranged on the lower feeding pipe;
One end of a concentrate return manifold extends into the concentrate tank from the top of the concentrate tank, the other end of the concentrate return pipe is branched into a first concentrate return pipe, a second concentrate return pipe and a concentrate blow-off pipe, the first concentrate return pipe is communicated with an upper feed inlet and a lower feed outlet of the ceramic membrane assembly, and a first concentrate return valve is arranged on the first concentrate return pipe: the second thick liquid return pipe is communicated with the lower feed and discharge port of the ceramic membrane component, and a second thick liquid return valve is arranged on the second thick liquid return pipe: a drain valve is arranged on the concentrated liquid drain pipe; a concentrated solution reflux main pipe before branching is provided with a concentrated solution reflux main valve;
The device comprises a supernatant port of a ceramic membrane assembly, a backflushing liquid tank, a dissolved air tank and a backflushing inlet of the ceramic membrane assembly, wherein the supernatant port of the ceramic membrane assembly, the backflushing liquid tank, the dissolved air tank and the backflushing inlet of the ceramic membrane assembly are sequentially communicated through pipelines, a supernatant control valve is arranged on the pipeline between the supernatant port of the ceramic membrane assembly and the backflushing liquid tank, a liquid filling valve is arranged on the pipeline between the backflushing liquid tank and the backflushing inlet of the ceramic membrane assembly, a backflushing air source is connected with an inlet of a ceramic membrane aeration device in the dissolved air tank through the pipeline, small bubbles with the diameter of 20-100 nm are uniformly distributed in the dissolved air tank after the ceramic membrane aeration device is aerated, an outlet of the dissolved air tank is communicated with the backflushing inlet of the ceramic membrane assembly, a backflushing air inlet valve is arranged between the backflushing air source and the ceramic membrane aeration device in the dissolved air tank, and an exhaust valve is also arranged on the dissolved air tank;
The clear liquid output pipe is arranged on the back flushing liquid tank, and the clear liquid output pipe is provided with a clear liquid discharge valve.
In order to improve the recoil effect, the honeycomb ceramic membrane filtering device further comprises a dosing tank and a dosing pump, wherein the dosing tank, the dosing pump and the dissolved air tank are sequentially connected through pipelines, and a dosing control valve is arranged on the pipeline between the dosing pump and the dissolved air tank. When the pollution of the film is heavy and the backflushing effect of the dissolved gas mixed liquid is still not ideal, the chemical reagent is added into the backflushing liquid to backflush when the film is backflushed, and the chemical reagent are sequentially opened at the inlet of the backflushing pump.
The honeycomb ceramic membrane assembly is provided with one or more than two honeycomb ceramic membrane assemblies which are connected in parallel, and the honeycomb ceramic membrane assembly can be specifically selected according to the treatment capacity of water and the like. When the honeycomb ceramic membrane assembly has more than two parallel connection, all the upper feed and discharge ports are converged to form a total upper feed and discharge port, all the supernatant fluid ports are converged to form a total supernatant fluid port, all the lower feed and discharge ports are converged to form a total lower feed and discharge port, and all the backflushing inlets are converged to form a total backflushing inlet.
The method for treating coal mine water by using the honeycomb ceramic membrane filtering device comprises the following steps of: after entering a raw liquid tank, mine water is conveyed to a coarse filter through a feed pump, and is subjected to prefiltering, and then is subjected to bidirectional periodic conversion feeding through a first feed valve and a second feed valve, wherein the filtering precision of the coarse filter is 30 meshes; when dead-end filtration is performed, the clear liquid flows out from a clear liquid port of the honeycomb ceramic membrane assembly, firstly enters a backflushing liquid tank, then is discharged to the clear liquid tank through a control clear liquid discharge valve, and the clear liquid entering the backflushing tank is filled into a dissolved air tank through a liquid filling valve, and the liquid filling valve is automatically closed after reaching a certain liquid level; when micro cross-flow filtration is adopted, the trend of the clear liquid is the same as that of dead-end filtration, and the trend of the concentrated liquid is as follows: when the pre-filtered material enters from the upper feed inlet and outlet, the first thick liquid reflux valve is closed, the second thick liquid reflux valve is opened, and thick liquid flows out from the lower feed inlet and outlet of the honeycomb ceramic membrane assembly and flows back to the raw water tank through the thick liquid reflux main valve; when the pre-filtered material enters from the lower feed inlet and outlet, the second concentrated solution reflux valve is closed, the first concentrated solution reflux valve is opened, and concentrated solution flows out from the upper feed inlet and outlet of the honeycomb ceramic membrane assembly and flows back to the raw water tank through the concentrated solution reflux main valve;
When mine water is filtered, periodic recoil and periodic forward flushing with the same frequency are realized: when the inlet pressure rise of the honeycomb ceramic membrane assembly is more than 1 time or when the membrane flux drop of the honeycomb ceramic membrane assembly is more than 20 percent, the backflushing and the forward flushing are simultaneously carried out: recoil: the feed pump is not stopped, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are firstly closed, the backflushing air inlet valve is opened, the pressure is kept at 0.3-0.5 MPa for 10-15 seconds, the backflushing liquid inlet valve is opened after 10-15 seconds of time delay, the backflushing is carried out for 10 seconds, after the backflushing is finished, the backflushing air inlet valve and the backflushing liquid inlet valve are closed, and the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are opened, so that normal filtering is recovered; forward flushing: and when the back flushing is finished, the feed pump is continuously stopped, the concentrated solution reflux main valve is closed, the blow-off valve is opened, membrane pollutants which are back flushed are discharged to the sewage tank through the blow-off valve, and after the normal flushing is finished, the concentrated solution reflux main valve is opened, and meanwhile, the blow-off valve is closed, so that normal filtration is recovered. The back flushing and forward flushing time is based on that the flux of the honeycomb ceramic membrane is recovered to more than 93% of the original flux.
When the inlet pressure of the honeycomb ceramic membrane assembly is increased from 0.1MPa to 0.2MP, or the membrane flux of the honeycomb ceramic membrane assembly is reduced from 200L/m 2. H to 100L/m 2. H, chemical cleaning and regeneration are carried out. Chemical cleaning and regeneration: respectively flushing the concentrated solution side and the clear solution side of the ceramic membrane component with deionized water, adding a cleaning agent (1% NaOH and 0.5% HNO 3) to carry out cross-flow cleaning for 0.5h and soaking for 0.5h, and flushing the regenerated ceramic membrane component with deionized water again until the pH value is neutral; and then detecting the cleaned and regenerated membrane assembly under the same condition as the initial flux detection before membrane filtration, and comparing the data of the cleaned and regenerated membrane assembly with the initial flux detection to ensure whether the honeycomb ceramic membrane is completely cleaned and regenerated or not, and finishing regeneration when the membrane flux recovery rate reaches more than 90%.
The performance of the above honeycomb ceramic membrane filtration apparatus is shown in Table 1 in comparison with the conventional organic ultrafiltration membrane (comparative example 1) and tubular ceramic membrane apparatus (comparative example 2).
Table 1 2400m 3/d mine Water treatment Effect comparison Table
Claims (4)
1. A method for treating sewage by a honeycomb ceramic membrane filter device is characterized by comprising the following steps:
The honeycomb ceramic membrane filtering device comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid return manifold, a honeycomb ceramic membrane component, a backflushing liquid tank, a dissolved air tank and a backflushing air source;
The top of the ceramic membrane component is provided with an upper feed and discharge port and a supernatant port, and the bottom of the ceramic membrane component is provided with a lower feed and discharge port and a backflushing inlet;
The raw liquid tank, the feed pump and the inlet of the coarse filter are sequentially communicated through a pipeline; the outlet of the coarse filter is connected with a feeding pipe, the feeding pipe is branched into an upper feeding pipe and a lower feeding pipe, the upper feeding pipe is communicated with an upper feeding hole and a lower feeding hole of the ceramic membrane assembly, a first feeding valve is arranged on the upper feeding pipe, the lower feeding pipe is communicated with a lower feeding hole and a lower feeding hole of the ceramic membrane assembly, and a second feeding valve is arranged on the lower feeding pipe;
One end of a concentrate return manifold extends into the raw liquid tank from the top of the raw liquid tank, the other end of the concentrate return manifold is branched into a first concentrate return pipe, a second concentrate return pipe and a concentrate blow-off pipe, the first concentrate return pipe is communicated with an upper feed inlet and a lower feed outlet of the ceramic membrane assembly, and a first concentrate return valve is arranged on the first concentrate return pipe: the second thick liquid return pipe is communicated with the lower feed and discharge port of the ceramic membrane component, and a second thick liquid return valve is arranged on the second thick liquid return pipe: a drain valve is arranged on the concentrated liquid drain pipe; a concentrated solution reflux main valve is arranged on the concentrated solution reflux main pipe;
The device comprises a supernatant port of a ceramic membrane component, a backflushing liquid tank, a dissolved air tank and a backflushing inlet of the ceramic membrane component, wherein the supernatant port of the ceramic membrane component, the backflushing liquid tank, the dissolved air tank and the backflushing inlet of the ceramic membrane component are sequentially communicated through pipelines, a supernatant control valve is arranged on the pipeline between the supernatant port of the ceramic membrane component and the backflushing liquid tank, a liquid filling valve is arranged on the pipeline between the backflushing liquid tank and the backflushing inlet of the ceramic membrane component, a backflushing air source is connected with an inlet of a ceramic membrane aeration device in the dissolved air tank through the pipeline, small bubbles with the diameter of 20-100 nm are uniformly distributed in the dissolved air tank after the ceramic membrane aeration device is aerated, an outlet of the dissolved air tank is communicated with the backflushing inlet of the ceramic membrane component, a backflushing air inlet valve is arranged between the backflushing air source and the ceramic membrane aeration device in the dissolved air tank, and an exhaust valve is also arranged on the dissolved air tank;
The clear liquid output pipe is arranged on the back flushing liquid tank, and the clear liquid output pipe is provided with a clear liquid discharge valve;
the method for treating sewage by the honeycomb ceramic membrane filter device comprises the following steps:
Filtering the liquid to be treated: after the liquid to be treated enters the raw liquid tank, the liquid is conveyed to a coarse filter through a feed pump, and after prefiltering is carried out, the liquid is periodically switched through a first feed valve and a second feed valve to carry out bidirectional periodic conversion feeding on the honeycomb ceramic membrane assembly; when dead-end filtration is performed, the clear liquid flows out from a clear liquid port of the honeycomb ceramic membrane assembly, firstly enters a backflushing liquid tank, is discharged through a clear liquid discharge valve, and the clear liquid entering the backflushing tank is filled into a solution tank through a solution filling valve, and when the solution tank reaches a specified liquid level, the solution filling valve is closed; when micro cross-flow filtration is adopted, the trend of the clear liquid is the same as that of dead-end filtration, and the trend of the concentrated liquid is as follows: when the pre-filtered material enters from the upper feed inlet and the lower feed outlet, the first thick liquid reflux valve is closed, the second thick liquid reflux valve is opened, and thick liquid flows out from the lower feed inlet and the lower feed outlet of the honeycomb ceramic membrane assembly and flows back into the raw liquid tank through the thick liquid reflux main valve; when the pre-filtered material enters from the lower feed inlet and outlet, the second concentrated solution reflux valve is closed, the first concentrated solution reflux valve is opened, and concentrated solution flows out from the upper feed inlet and outlet of the honeycomb ceramic membrane assembly and flows back into the raw liquid tank through the concentrated solution reflux main valve;
When the liquid to be treated is filtered, periodic recoil and periodic forward flushing with the same frequency are realized: when the inlet pressure rising amount of the honeycomb ceramic membrane component is more than 0.5 times or when the membrane flux falling amount of the honeycomb ceramic membrane component is more than 20%, backflushing and forward flushing are simultaneously carried out; the back flushing takes the mixed solution of dissolved gas as a medium, the mixed solution of dissolved gas used for back flushing is a back flushing medium formed by aerating gas with the pressure of 0.3-0.5 MPa through a ceramic membrane with the aperture of 20-100 nm, and the liquid used for back flushing is clear liquid flowing out of a honeycomb ceramic membrane component; the liquid to be treated is used as a medium; the backflushing step comprises the following steps: the feed pump is not stopped, the clear liquid control valve, the clear liquid discharge valve, the emptying valve of the dissolved air tank and the liquid filling valve are closed firstly, the backflushing air inlet valve is opened, the air inlet pressure is kept to be 0.3-0.5 MPa, the air inlet time is kept to be 10-15 seconds, then the backflushing liquid inlet valve is opened after the backflushing is finished, the backflushing air inlet valve and the backflushing liquid inlet valve are closed, and the clear liquid control valve, the clear liquid discharge valve, the emptying valve of the dissolved air tank and the liquid filling valve are opened, so that normal filtration is recovered; the forward flushing step comprises the following steps: at the same time of back flushing, the feed pump is kept, the concentrated solution reflux main valve is closed, the blow-off valve is opened, membrane pollutants after back flushing are discharged to the sewage tank through the blow-off valve, after the back flushing is finished, the concentrated solution reflux main valve is opened, and meanwhile, the blow-off valve is closed, and normal filtration is recovered;
When the rising amount of the inlet pressure of the honeycomb ceramic membrane component is 1-2 times of the inlet pressure or the falling amount of the membrane flux of the honeycomb ceramic membrane component is 50-1 times of a set value, chemical cleaning and regeneration are carried out;
The chemical cleaning and regenerating method comprises the following steps: respectively flushing the concentrated solution side and the clear solution side of the ceramic membrane component with deionized water, adding 0.5-5% w/w of cleaning agent for cross-flow cleaning and soaking, and flushing the regenerated ceramic membrane component with deionized water again until the pH value is neutral; then detecting the cleaned and regenerated membrane component under the same condition as the initial flux detection before membrane filtration, and comparing the data of the cleaned and regenerated membrane component with the initial flux detection to ensure whether the honeycomb ceramic membrane is completely cleaned and regenerated, and considering that regeneration is completed when the membrane flux recovery rate is more than 90%; wherein the cleaning agent is one or more of sodium hypochlorite solution, sodium hydroxide solution, hydrochloric acid and nitric acid.
2. The method for treating sewage by using the honeycomb ceramic membrane filter apparatus of claim 1, wherein: the honeycomb ceramic membrane filter device further comprises a dosing tank and a dosing pump, wherein the dosing tank, the dosing pump and the dissolved air tank are sequentially connected through pipelines, a dosing control valve is arranged on the pipeline between the dosing pump and the dissolved air tank, the dosing pump and the dosing valve are sequentially opened during backflushing, and chemical reagents are added into backflushing liquid to carry out backflushing.
3. A method of treating sewage by a honeycomb ceramic membrane filtration apparatus according to claim 1 or 2, wherein: when the honeycomb ceramic membrane assembly is provided with more than two parallel connection, all upper feed and discharge ports are converged to form a total upper feed and discharge port, all supernatant ports are converged to form a total supernatant port, all lower feed and discharge ports are converged to form a total lower feed and discharge port, and all backflushing inlets are converged to form a total backflushing inlet.
4. A method of treating sewage by a honeycomb ceramic membrane filtration apparatus according to claim 1 or 2, wherein: the filtering precision of the coarse filter is below 30 meshes.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580545A (en) * | 2012-03-22 | 2012-07-18 | 华南理工大学 | Combined ultra-filtration device with membrane pollution control and ultrasonic cleaning functions |
| CN103055543A (en) * | 2012-12-29 | 2013-04-24 | 上海安赐机械设备有限公司 | Large-channel vertical-flow membrane device for recycling superfine solid catalyst and process |
| CN105217733A (en) * | 2015-10-12 | 2016-01-06 | 北京碧水源膜科技有限公司 | A kind of nanometer filtering film water treatment system of two-way flow and method |
| CN106629958A (en) * | 2017-01-20 | 2017-05-10 | 南京工业大学 | Closed continuous high-pressure gas dissolving device and method |
| CN211169987U (en) * | 2019-12-10 | 2020-08-04 | 南京钛净流体技术有限公司 | Honeycomb ceramic membrane filter equipment |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108012533A (en) * | 2015-06-19 | 2018-05-08 | 纳诺斯通水务公司 | For removing the ceramic membranous system and correlation technique of silica |
| CN105251367A (en) * | 2015-11-12 | 2016-01-20 | 郑州银科尔科技有限公司 | Technology and device for efficiently purifying film through dissolved air flotation method |
-
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580545A (en) * | 2012-03-22 | 2012-07-18 | 华南理工大学 | Combined ultra-filtration device with membrane pollution control and ultrasonic cleaning functions |
| CN103055543A (en) * | 2012-12-29 | 2013-04-24 | 上海安赐机械设备有限公司 | Large-channel vertical-flow membrane device for recycling superfine solid catalyst and process |
| CN105217733A (en) * | 2015-10-12 | 2016-01-06 | 北京碧水源膜科技有限公司 | A kind of nanometer filtering film water treatment system of two-way flow and method |
| CN106629958A (en) * | 2017-01-20 | 2017-05-10 | 南京工业大学 | Closed continuous high-pressure gas dissolving device and method |
| CN211169987U (en) * | 2019-12-10 | 2020-08-04 | 南京钛净流体技术有限公司 | Honeycomb ceramic membrane filter equipment |
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