CN211169987U - Honeycomb ceramic membrane filter equipment - Google Patents
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- CN211169987U CN211169987U CN201922200617.9U CN201922200617U CN211169987U CN 211169987 U CN211169987 U CN 211169987U CN 201922200617 U CN201922200617 U CN 201922200617U CN 211169987 U CN211169987 U CN 211169987U
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Abstract
The utility model discloses a honeycomb ceramic membrane filter device, which comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid reflux header pipe, a honeycomb ceramic membrane component, a backflushing liquid tank, a dissolved gas tank and a backflushing gas source; the liquid to be treated enters a honeycomb ceramic membrane component for filtration in a bidirectional periodic conversion feeding mode; and the periodic back flushing is realized during the filtering, and the periodic positive flushing with the same frequency is matched. The utility model adopts bidirectional pulsating feeding, which is beneficial to fully utilizing turbulence brought by periodic direction conversion to reduce membrane pollution, and simultaneously fully utilizing the membrane area with light pollution at the inlet end part and the outlet end part to maintain higher membrane flux operation; the mixed liquid of the periodic dissolved air is adopted for backflushing, so that the backflushing effect is enhanced, a backflushing pump is not needed, and the energy is saved; the back flushing process is carried out simultaneously with periodic positive flushing at the same frequency, and liquid is adopted as a positive flushing medium, so that the back-flushed pollutants can be timely taken out of the system, and the flux can be instantly recovered on line.
Description
Technical Field
The utility model relates to a honeycomb ceramic membrane filter equipment belongs to ceramic membrane application.
Background
The honeycomb ceramic membrane (PCR membrane) is the same as a multi-channel ceramic membrane, is also formed by sintering inorganic ceramic materials such as alumina, titanium oxide, zirconia, silicon oxide and the like under a high-temperature condition, has a similar structure of a tubular multi-channel ceramic membrane, and also has the chemical stability and mechanical strength of the multi-channel ceramic membrane, but has the advantage of higher membrane area than the membrane area in a unit volume of the multi-channel ceramic membrane, namely higher filling area of the inner membrane in the unit volume because the multi-channel ceramic membrane has channel distribution which is much denser than the multi-channel ceramic membrane in the unit volume. The high filling area not only improves the processing scale of the ceramic membrane equipment and occupies smaller area, but also reduces the processing cost of the ceramic membrane and has more dominant investment cost.
It is due to the above-mentioned advantages of the honeycomb ceramic membrane that it is possible to apply it to water treatment, especially to water purification. Currently, honeycomb ceramic membranes are also mainly limited to the study of membrane elements and modules, for example: CN102172477A provides a manufacturing method of 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 the preparation process are simple; CN204799114U shows a ceramic honeycomb membrane module for use in clean water manufacture, but this module can only be used for domestic water filtration applications; CN208943852U shows another tubular honeycomb ceramic membrane module which is convenient for installation and maintenance as well as cleaning. All this is still just a research on membrane elements and modules, lacking in-depth research and improvement on specific applications of honeycomb ceramic membranes.
SUMMERY OF THE UTILITY MODEL
The utility model provides a honeycomb ceramic membrane filtration method and filter equipment, according to the pollution mechanism in the honeycomb ceramic membrane filtration process, make full use of ceramic membrane's intensity is high, chemical stability is good, aperture distribution advantage such as narrow, on current terminal or little cross-flow filtration technology basis, creatively use from membrane both ends pulsation feeding, dissolve the frequent recoil of gas mixture and scheme such as the liquid normal impact of in-process companion with the same frequency simultaneously, greatly reduced the membrane pollution that forms in the filtration process, the membrane cleaning cycle has been prolonged, the flux has been improved.
For solving the technical problem, the utility model discloses the technical scheme who adopts as follows:
a honeycomb ceramic membrane filtration method, a liquid to be treated enters a honeycomb ceramic membrane component for filtration through a bidirectional periodic conversion feeding mode; and the periodic back flushing is realized during the filtering, and the periodic positive flushing with the same frequency is matched.
This application starts from reducing honeycomb ceramic membrane filtration in-process membrane pollution, through the mode that adopts two-way pulsation feeding, assists with the mixed liquid of dissolved air and carries out the recoil, carries out the positive impact of liquid with the frequency simultaneously, has greatly reduced membrane pollution, has improved flux.
In order to further reduce membrane pollution, the periodic back flushing takes the mixed solution of dissolved air as a medium; the periodic positive flushing takes liquid as a medium.
In order to improve the backflushing effect, the gas-dissolved mixed liquid used 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, simultaneously reduce energy consumption and enhance the recycling of materials, the liquid used for periodic back flushing is clear liquid flowing out of the honeycomb ceramic membrane component; the periodic liquid positive flushing takes the liquid to be treated as a medium.
When the pollution of the membrane is heavy and the backflushing effect is still not ideal by adopting the dissolved gas mixed solution, 0.5-5% w/w of cleaning agent can be added into the liquid used for periodic backflushing. % w/w is the mass percent of cleaning agent relative to the liquid used for periodic back flushing. The cleaning agent can be one or more of sodium chlorate, sodium hydroxide, hydrochloric acid, nitric acid and the like.
In order to take filtering efficiency and membrane life into consideration, when the inlet pressure rise of the honeycomb ceramic membrane component is more than 0.5 times, or when the membrane flux decline of the honeycomb ceramic membrane component is more than 20%, back flushing and forward flushing are carried out.
In order to further guarantee the filtering effect, the time of back flushing and positive flushing is subject to the condition 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 then pumped into a honeycomb ceramic membrane component by a pump, and micro cross flow or dead-end filtration is adopted.
The filtration precision of the coarse filter is below 30 meshes in order to achieve both filtration efficiency and membrane life.
In order to ensure the filtering effect and prolong the service life of the membrane, when the inlet pressure of the honeycomb ceramic membrane component rises by more than 1-2 times or the membrane flux of the honeycomb ceramic membrane component drops by more than 50-1 times, chemical cleaning regeneration is carried out. Chemical cleaning and regeneration: respectively washing the concentrated solution side and the clear solution side of the ceramic membrane component with deionized water, adding 0.5-5% w/w of a cleaning agent (such as one or more than two of sodium hypochlorite, sodium hydroxide, hydrochloric acid, nitric acid and the like) for cross-flow cleaning and soaking, and washing the regenerated ceramic membrane component with deionized water again until the pH value is neutral; and then detecting the cleaned and regenerated membrane module under the same condition as the initial flux detection before membrane filtration, and comparing the data of the cleaned and regenerated membrane module and the initial flux detection to ensure whether the honeycomb ceramic membrane is completely cleaned and regenerated, wherein generally, the regeneration is considered to be completed when the recovery rate of the membrane flux is more than 90%.
A honeycomb ceramic membrane filtering device comprises a raw liquid tank, a feeding pump, a coarse filter, a concentrated liquid reflux main pipe, a honeycomb ceramic membrane component, a back flushing liquid tank, a dissolved air tank and a back flushing air source;
the top of the ceramic membrane component is provided with an upper feeding and discharging port and a supernatant fluid port, and the bottom of the ceramic membrane component is provided with a lower feeding and discharging port and a backflushing inlet;
the raw liquid tank, the feeding pump and the inlet of the coarse filter are communicated in sequence through pipelines; 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, and the other end of the feeding pipe is branched into the upper feeding pipe and the lower feeding pipe), the upper feeding pipe is communicated with an upper feeding hole and a lower discharging hole of the ceramic membrane assembly, the upper feeding pipe is provided with a first feeding valve, the lower feeding pipe is communicated with a lower feeding hole and a lower discharging hole of the ceramic membrane assembly;
in concentrate backward flow house steward one end stretched into the concentrate groove from the concentrate groove top, concentrate back flow other end branch was first concentrate back flow, second concentrate back flow and concentrate blow off pipe, and first concentrate back flow communicates with ceramic membrane module's last feeding hole, is equipped with first concentrate return valve on the first concentrate back flow: the second thick liquid back flow is equipped with the second thick liquid back flow valve with ceramic membrane subassembly feed inlet and outlet feed opening intercommunication in the lower of the second thick liquid back flow: the concentrated solution blow-off pipe can be communicated to a sewage tank and the like for further treatment, and a blow-off valve is arranged on the concentrated solution blow-off pipe; a concentrated solution reflux main valve is arranged on the concentrated solution reflux main pipe before branching;
the device comprises a ceramic membrane component, a backflushing liquid tank, a gas dissolving tank, a backflushing inlet of the ceramic membrane component, a liquid control valve, a liquid filling valve, a backflushing liquid inlet valve, a backflushing gas source, a backflushing gas inlet valve and an emptying valve, wherein the backflushing inlet of the ceramic membrane component is communicated with the backflushing liquid tank through pipelines;
a clear liquid output pipe is arranged on the backflushing liquid tank, and a clear liquid discharge valve is arranged on the clear liquid output pipe. The clear liquid output pipe can be connected to a clear liquid tank or connected to other pipe networks for direct utilization.
In order to improve the backflushing effect, the honeycomb ceramic membrane filtering device further comprises a dosing tank and a dosing pump, 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 membrane is heavy and the backflushing effect is still not ideal by adopting the dissolved air mixed solution, the dosing pump and the dosing valve are sequentially opened at the inlet of the backflushing pump during backflushing, and chemical reagents are added into the backflushing solution for backflushing. For example, 0.5-5% w/w of a cleaning agent may be added to the liquid used for periodic back flushing. % w/w is the mass percent of cleaning agent relative to the liquid used for periodic back flushing. The cleaning agent can be one or more of sodium chlorate, sodium hydroxide, hydrochloric acid, nitric acid and the like.
Instruments, valves and the like can be additionally arranged on all parts and all pipelines as required.
The membrane component is tubular and is provided with two inlet (outlet) ports and two clear liquid outlets; the honeycomb ceramic membrane components are vertically arranged.
The number of the honeycomb ceramic membrane modules is one, or the number of the honeycomb ceramic membrane modules is more than two, and the honeycomb ceramic membrane modules can be selected according to the water treatment capacity and the like. When more than two honeycomb ceramic membrane assemblies are connected in parallel, all the upper feed and discharge ports are converged to form a total upper feed and discharge port, all the upper clear liquid ports are converged to form a total upper clear liquid 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 a stock solution tank, the liquid is conveyed to a coarse filter through a feeding pump, after the liquid is pre-filtered, the liquid is periodically switched through a first feeding valve and a second feeding valve, and feeding of bidirectional periodic conversion is carried out on the honeycomb ceramic membrane component; when the filtration is dead-end, clear liquid flows out from a clear liquid port of the honeycomb ceramic membrane component, firstly enters a backflushing liquid tank, then is discharged to the clear liquid tank through a control clear liquid discharge valve or is directly used for a pipe network and the like, clear liquid entering the backflushing liquid tank is filled into a dissolved air tank through a liquid filling valve, and the liquid filling valve is closed when the dissolved air tank reaches a specified liquid level; when the filtration is micro cross flow filtration, the direction of the clear solution is the same as that of the dead end filtration, and the direction of the concentrated solution is as follows: when the pre-filtered material enters from the upper inlet and outlet, the first concentrated solution reflux valve is closed, the second concentrated solution reflux valve is opened, and concentrated solution flows out from the lower inlet and outlet of the honeycomb ceramic membrane component and flows back to the raw water tank through the concentrated solution 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 outlet and the upper feed outlet of the honeycomb ceramic membrane component and flows back to the raw water tank through the concentrated solution reflux main valve;
when the liquid to be treated is filtered, periodic back flushing is realized, and periodic positive flushing with the same frequency is matched: when the inlet pressure rise of the honeycomb ceramic membrane component is more than 0.5 time or the membrane flux decline of the honeycomb ceramic membrane component is more than 20%, back flushing and forward flushing are simultaneously carried out. Back flushing: the feeding pump is stopped, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are closed firstly, the recoil air inlet valve is opened, the pressure is kept at 0.3-0.5 MPa for 10-15 seconds, then the recoil liquid inlet valve is opened after 10-15 seconds of delay, after the recoil is finished, the recoil air inlet valve and the recoil liquid inlet valve are closed, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are opened, and normal filtration is recovered; positive punching: and (3) closing the concentrated solution reflux main valve and opening the blow-down valve when the feeding pump is stopped during backflushing, discharging the backflushed membrane pollutants to a sewage tank through the blow-down valve, opening the concentrated solution reflux main valve after the positive flushing is finished, closing the blow-down valve at the same time, and recovering normal filtration.
In order to improve the filtration efficiency, the back flushing time and the positive flushing time are subject to the condition that the flux of the honeycomb ceramic membrane is recovered to more than 93 percent of the original flux.
And after the dissolved air tank reaches the specified liquid level, the liquid filling valve is closed, and at the moment, the liquid in the dissolved air tank is not less than the amount required by one-time back flushing.
The control of opening and closing, starting and stopping and the like of each valve and each device can be realized according to the existing automatic control technology.
The terms of orientation such as up-down, left-right, top, bottom, horizontal, vertical and the like in the application all refer to the relative positions of the device in normal use.
The techniques not mentioned in the present invention are all referred to the prior art, for example, inorganic membrane separation technique and application (chemical industry Press, 2003) by Xunan Ping et al.
The utility model discloses honeycomb ceramic membrane filtration method starts with reducing the membrane pollution in honeycomb ceramic membrane filtration process, through adopting the mode of two-way pulsation feeding, assists with the gas-dissolved mixed liquid and recoils, carries out the positive impact of liquid with the same frequency simultaneously, has greatly reduced membrane pollution, has improved the flux; compared with the multi-channel tubular ceramic membrane and hollow fiber organic membrane filtration process, the method has the following advantages:
1. the application provides a ceramic membrane filtration method with a high filling area, wherein 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 a micro cross flow or dead-end filtration mode, so that the competitiveness of the ceramic membrane in the aspect of water purification treatment is improved and is possible;
2. the method adopts bidirectional pulse feeding, is favorable for fully utilizing turbulence caused by periodic direction conversion to reduce membrane pollution, and simultaneously fully utilizes the membrane area with light pollution at the inlet end and the outlet end to maintain high membrane flux operation;
3. the method adopts the periodic back flushing of the gas-dissolved mixed liquid, skillfully applies the gas-dissolved principle to the back flushing process of the honeycomb ceramic membrane, and utilizes the nano-grade ceramic membrane as an aeration head, so that the gas in the back flushing medium-gas-dissolved mixed liquid is uniformly distributed, impurities such as dust and the like are removed, bubbles are smaller than or equal to the pore diameter of the membrane, the back flushing effect on pollution caused by membrane pore blockage and membrane surface deposition is effectively removed, and the pressure in the gas-dissolved tank is utilized as back flushing power; compared with the hollow fiber organic membrane which is back-flushed only by liquid, the back-flushing effect is good, the defects that the organic membrane is easy to break and is not corrosion-resistant are overcome, a back-flushing pump is not needed as power, and energy is saved;
4. the periodic positive flushing with the same frequency is carried out while the back flushing process is carried out, and liquid is used as a positive flushing medium, so that the back-flushed pollutants are timely taken out of the system, the pollutants on the membrane surface can be flushed away more effectively by the liquid than gas, the flux can be instantly recovered on line, and the high-flux operation of the honeycomb ceramic membrane is promoted.
Drawings
FIG. 1 is a schematic structural view of the honeycomb ceramic membrane filter device of the present invention;
in the figure, 1, a stock solution tank; 2. a feed pump; 3. a coarse filter; 4. a honeycomb ceramic membrane module; 4-1, feeding and discharging; 4-2, an upper feeding port and a discharge port; 4-3, a backflushing inlet; 4-4, a supernatant liquid 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; 12 a second concentrate return valve; 10. a first feed valve; 11 a second feed valve; 13. a clear liquid control valve; 14. back flushing a liquid inlet valve; 15. a recoil air intake valve; 16. a clear liquid discharge valve; 17. a dosing control valve; 18. a concentrated solution reflux main valve; 19. a blowoff valve; 20. a liquid charging valve; 21. an exhaust valve of the dissolved air tank; a. stock solution (solution to be treated); b. a back flushing gas source; c. clear liquid; d. a medicament; e. and (4) sewage.
Detailed Description
For a better understanding of the present invention, the following examples are provided to further illustrate the present invention, but the present invention is not limited to the following examples.
As shown in fig. 1, a honeycomb ceramic membrane filtration device comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid reflux main pipe, 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 feeding and discharging port and a supernatant fluid port, and the bottom of the ceramic membrane component is provided with a lower feeding and discharging port and a backflushing inlet;
the raw liquid tank, the feeding pump and the inlet of the coarse filter are communicated in sequence through pipelines; the outlet of the coarse filter is connected with a feed pipe, the feed pipe is branched into an upper feed pipe and a lower feed pipe, the upper feed pipe is communicated with an upper feed outlet of the ceramic membrane component, the upper feed pipe is provided with a first feed valve, the lower feed pipe is communicated with a lower feed inlet and a lower feed outlet of the ceramic membrane component, and the lower feed pipe is provided with a second feed valve;
in concentrate backward flow house steward one end stretched into the concentrate groove from the concentrate groove top, concentrate back flow other end branch was first concentrate back flow, second concentrate back flow and concentrate blow off pipe, and first concentrate back flow communicates with ceramic membrane module's last feeding hole, is equipped with first concentrate return valve on the first concentrate back flow: the second thick liquid back flow is equipped with the second thick liquid back flow valve with ceramic membrane subassembly feed inlet and outlet feed opening intercommunication in the lower of the second thick liquid back flow: a drain valve is arranged on the concentrated solution drain pipe; a concentrated solution reflux main valve is arranged on the concentrated solution reflux main pipe before branching;
the device comprises a ceramic membrane assembly, a backflushing liquid tank, a gas dissolving tank and a backflushing inlet of the ceramic membrane assembly, wherein a supernatant liquid port of the ceramic membrane assembly, a backflushing liquid tank, a gas charging valve and a backflushing inlet of the ceramic membrane assembly are sequentially communicated through pipelines, a clear liquid control valve is arranged on a pipeline between the supernatant liquid port of the ceramic membrane assembly and the backflushing liquid tank, a liquid charging valve is arranged on a pipeline between the backflushing liquid tank and the gas dissolving tank, a backflushing liquid charging valve is arranged on a pipeline between the gas dissolving tank and the backflushing inlet of the ceramic membrane assembly, a backflushing gas source is connected with an inlet of a ceramic membrane aeration device in the gas dissolving tank through a pipeline, gas with the pressure of 0.3-0.5 MPa is aerated through a ceramic membrane with the aperture of 20-100 nm, and is uniformly distributed in the gas dissolving tank through;
a clear liquid output pipe is arranged on the backflushing liquid tank, and a clear liquid discharge valve is arranged on the clear liquid output pipe.
In order to improve the backflushing effect, the honeycomb ceramic membrane filtering device further comprises a dosing tank and a dosing pump, 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 membrane is heavy and the backflushing effect is still not ideal by adopting the dissolved air mixed solution, the dosing pump and the dosing valve are sequentially opened at the inlet of the backflushing pump during backflushing, and chemical reagents are added into the backflushing solution for backflushing.
The number of the honeycomb ceramic membrane modules is one, or the number of the honeycomb ceramic membrane modules is more than two, and the honeycomb ceramic membrane modules can be selected according to the water treatment capacity and the like. When more than two honeycomb ceramic membrane assemblies are connected in parallel, all the upper feed and discharge ports are converged to form a total upper feed and discharge port, all the upper clear liquid ports are converged to form a total upper clear liquid 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 the coal mine water by using the honeycomb ceramic membrane filtering device comprises the following steps: after entering a raw liquid tank, mine water is conveyed to a coarse filter through a feeding pump, after pre-filtration is carried out, feeding of bidirectional periodic conversion is carried out on a honeycomb ceramic membrane component through periodic switching of a first feeding valve and a second feeding valve, wherein the filtering precision of the coarse filter is 30 meshes; when the filtration is dead-end, the clear liquid flows out from a clear liquid port of the honeycomb ceramic membrane component, firstly enters a backflushing liquid tank, then is discharged to the clear liquid tank through a control clear liquid discharge valve, 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 when the dissolved air tank reaches a specified liquid level; when the filtration is micro cross flow filtration, the direction of the clear solution is the same as that of the dead end filtration, and the direction of the concentrated solution is as follows: when the pre-filtered material enters from the upper inlet and outlet, the first concentrated solution reflux valve is closed, the second concentrated solution reflux valve is opened, and concentrated solution flows out from the lower inlet and outlet of the honeycomb ceramic membrane component and flows back to the raw water tank through the concentrated solution 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 outlet and the upper feed outlet of the honeycomb ceramic membrane component and flows back to the raw water tank through the concentrated solution reflux main valve;
when mine water is filtered, periodic back flushing is realized, and periodic positive flushing with the same frequency is matched: when the inlet pressure rise of the honeycomb ceramic membrane component is more than 1 time, or when the membrane flux decline of the honeycomb ceramic membrane component is more than 20%, performing back flushing and positive flushing simultaneously: back flushing: the feeding pump is stopped, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are closed firstly, 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 delay, 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, the clear liquid control valve, the clear liquid discharge valve, the dissolved air tank emptying valve and the liquid filling valve are opened, and normal filtration is recovered; positive punching: and (3) closing the concentrated solution reflux main valve and opening the blow-down valve when the feeding pump is stopped during backflushing, discharging the backflushed membrane pollutants to a sewage tank through the blow-down valve, opening the concentrated solution reflux main valve after the positive flushing is finished, closing the blow-down valve at the same time, and recovering normal filtration. The back flushing time and the positive flushing time are based on that the flux of the honeycomb ceramic membrane is recovered to more than 93% of the original flux.
When the honeycomb ceramicsThe inlet pressure of the membrane component is increased from 0.1MPa to 0.2MP, or the membrane flux of the honeycomb ceramic membrane component is 200L/m2H down to 100L/m2And h, carrying out chemical cleaning regeneration. Chemical cleaning and regeneration: respectively washing the concentrated solution side and the clear solution side of the ceramic membrane component with deionized water, adding cleaning agents (1% NaOH and 0.5% HNO3) to perform cross-flow cleaning for 0.5h and soaking for 0.5h, and washing the regenerated ceramic membrane component with deionized water again until the pH value is neutral; and then detecting the cleaned and regenerated membrane module under the same condition as the initial flux detection before membrane filtration, comparing the data of the cleaned and regenerated membrane module and the initial flux detection before membrane filtration to ensure whether the honeycomb ceramic membrane is completely cleaned and regenerated, and completing regeneration when the recovery rate of the membrane flux reaches more than 90%.
The performance of the honeycomb ceramic membrane filtration apparatus is compared with that of the conventional organic ultrafiltration membrane (comparative example 1) and tubular ceramic membrane apparatus (comparative example 2) as shown in table 1.
Watch 12400 m3Comparison table for treatment effect of mine water
Claims (7)
1. A honeycomb ceramic membrane filter device, characterized in that: comprises a raw liquid tank, a feed pump, a coarse filter, a concentrated liquid reflux main pipe, 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 feeding and discharging port and a supernatant fluid port, and the bottom of the ceramic membrane component is provided with a lower feeding and discharging port and a backflushing inlet;
the raw liquid tank, the feeding pump and the inlet of the coarse filter are communicated in sequence through pipelines; the outlet of the coarse filter is connected with a feed pipe, the feed pipe is branched into an upper feed pipe and a lower feed pipe, the upper feed pipe is communicated with an upper feed outlet of the ceramic membrane component, the upper feed pipe is provided with a first feed valve, the lower feed pipe is communicated with a lower feed inlet and a lower feed outlet of the ceramic membrane component, and the lower feed pipe is provided with a second feed valve;
in concentrate backward flow house steward one end stretched into the concentrate groove from the concentrate groove top, concentrate back flow other end branch was first concentrate back flow, second concentrate back flow and concentrate blow off pipe, and first concentrate back flow communicates with ceramic membrane module's last feeding hole, is equipped with first concentrate return valve on the first concentrate back flow: the second thick liquid back flow is equipped with the second thick liquid back flow valve with ceramic membrane subassembly feed inlet and outlet feed opening intercommunication in the lower of the second thick liquid back flow: a drain valve is arranged on the concentrated solution drain pipe; a concentrated solution reflux main valve is arranged on the concentrated solution reflux main pipe before branching;
the device comprises a ceramic membrane component, a backflushing liquid tank, a gas dissolving tank, a backflushing inlet of the ceramic membrane component, a liquid control valve, a liquid filling valve, a backflushing liquid inlet valve, a backflushing gas source, a backflushing gas inlet valve and an emptying valve, wherein the backflushing inlet of the ceramic membrane component is communicated with the backflushing liquid tank through pipelines;
a clear liquid output pipe is arranged on the backflushing liquid tank, and a clear liquid discharge valve is arranged on the clear liquid output pipe.
2. A honeycomb ceramic membrane filter device according to claim 1, wherein: the device also 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.
3. A honeycomb ceramic membrane filter device according to claim 1 or 2, wherein: the aperture of the ceramic membrane aeration device in the dissolved air tank is 20-100 nm.
4. A honeycomb ceramic membrane filter device according to claim 1 or 2, wherein: the filtration precision of the coarse filter is below 30 meshes.
5. A honeycomb ceramic membrane filter device according to claim 1 or 2, wherein: there is one honeycomb ceramic membrane module.
6. A honeycomb ceramic membrane filter device according to claim 1 or 2, wherein: the honeycomb ceramic membrane component is provided with more than two parallel-connected upper feed ports and discharge ports, all the upper feed ports and the lower feed ports are converged to form a total upper feed port and discharge port, all the upper clear liquid ports are converged to form a total upper clear liquid port, all the lower feed ports and discharge ports are converged to form a total lower feed port and discharge port, and all the backflushing inlets are converged to form a total backflushing inlet.
7. A honeycomb ceramic membrane filter device according to claim 1 or 2, wherein: the honeycomb ceramic membrane component consists of a tubular membrane component.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110745910A (en) * | 2019-12-10 | 2020-02-04 | 南京钛净流体技术有限公司 | Honeycomb ceramic membrane filtering method and filtering device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110745910A (en) * | 2019-12-10 | 2020-02-04 | 南京钛净流体技术有限公司 | Honeycomb ceramic membrane filtering method and filtering device |
| CN110745910B (en) * | 2019-12-10 | 2024-09-20 | 南京钛净流体技术有限公司 | Honeycomb ceramic membrane filtering method and filtering device |
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