CN101185847A - Ceramic film backwash method - Google Patents
Ceramic film backwash method Download PDFInfo
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- CN101185847A CN101185847A CNA2007100560179A CN200710056017A CN101185847A CN 101185847 A CN101185847 A CN 101185847A CN A2007100560179 A CNA2007100560179 A CN A2007100560179A CN 200710056017 A CN200710056017 A CN 200710056017A CN 101185847 A CN101185847 A CN 101185847A
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- ceramic film
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Abstract
A ceramic membrane backwashing method belongs to the field of mechanical equipment cleaning. The aim of the invention is the ceramic membrane backwashing method which employs a backwashing way to clean a ceramic membrane cleaning device. The invention is provided with a tee at the liquid outlet of a ceramic membrane component; the tee is communicated with a cleaning solution tank through a pipeline; a backwashing pump, a backwashing control valve, a backwashing pressure gauge are arranged on the pipeline; and the backwashing is conducted by the added equipments. Based on the general traditional cleaning method, the invention also adds a plurality of advantages that the equipment needs not to be stopped; the restoration and regeneration of the ceramic membrane flux can be conducted online faster and more thoroughly than the original cleaning method; and the cleaning agent amount can also be saved.
Description
Technical field:
The invention belongs to plant equipment and clean the field.
Background technology:
At present, the ceramic membrane production equipment is in order to recover membrane flux, generally all adopt traditional cleaning method, also cry and just washing method, (both added acid or added alkali or other cleaning agent in pure water, device systems is during as ordinary production, and the ON cycle pump carries out wash cycles, different is to close the penetrating fluid outlet valve; Every about 20 minutes, open the penetrating fluid outlet valve, observe the permeate flow meter, detect membrane flux, recover) until membrane flux.There is following problem in traditional cleaning method:
1, the flux resume speed is slow, the energy consumption height;
2, flux recovers not thorough;
3, can not onlinely carry out the recovery regeneration of ceramic membrane flux.
Summary of the invention:
The objective of the invention is to adopt a kind of backwash mode that the membrane flux of ceramic membrane equipment is cleaned the ceramic film backwash method that recovers regeneration.
Concrete steps of the present invention are:
A, at first threeway is installed at the purified liquor outlet place of ceramic film component feed end, in threeway, communicates with the counter-flushing liquid storage tank, backwashing pump, backwash control valve, backwashing pressure table are installed on pipeline by pipeline;
B, when ceramic membrane filter equipment cleans, in the recoil cleaning of evaporator, inject cleaning fluid in advance;
C, close ceramic film component earlier and see through the liquid outlet valve up and down; Close the system that connects this ceramic film component again and see through the liquid outlet valve, make it stop through liquid; Other ceramic film component continues operation;
D, open recoil cleaning of evaporator outlet valve, in backwashing pump, inject pure water;
E, open backwashing pump outlet pressure compensation flap, start backwashing pump, pure water is back in the recoil cleaning of evaporator, circulation in forming;
F, utilize the backwashing pressure compensation flap to regulate the backwash outlet pressure, when pressure reaches greater than this ceramic membrane spare inlet pressure, open the ceramic film component back flush valves;
G, open ceramic film component and see through the liquid outlet valve; Regulate the backwashing pressure compensation flap once more, when making backwashing system pressure, utilize pressure differential method that ceramic film component is carried out backwash greater than ceramic film component internal operation pressure;
After 3min～10min is carried out in h, backwash, observe the recoil cleaning performance, close the ceramic film component back flush valves after washing, open the pressure balance valve simultaneously, make the backwash pure water be back to the recoil cleaning of evaporator by concentrate return flow meter;
I, the system that opens ceramic film component see through the liquid outlet valve; Make ceramic film component recover normal operation.
The present invention increases many advantages again on conventional clean method basis:
1, equipment need not shut down, and can onlinely carry out the recovery regeneration of ceramic membrane flux.
2, faster, more thorough than conventional clean method to membrane flux recovery regeneration, can also save the energy and cleaning agent consumption.
Not only can select single component to carry out backwash recovery regeneration when 3, equipment moves, can also carry out in batches, divide into groups to carry out backwash to membrane module and recover regeneration (but necessary parallel connection divides group selection).
4, sustainablely provide the enough backwashing pressure and backwash water yields.
5, in system, when material is concentrated to a certain degree when certain multiple (or), need add the water dialysis, open backwashing pump this moment, so both reached the purpose that adds the water dialysis, and the while has been realized the regeneration that is restored of ceramic membrane flux again in the shortest time.
Description of drawings:
Fig. 1 is an overall structure schematic diagram of the present invention; Solid line partly is existing ceramic membrane cleaning structure schematic diagram, the back-flushing structure schematic diagram that dotted portion increases for the present invention among the figure.
Fig. 2 is an integral structure manufacturing process flow chart of the present invention;
Fig. 3 is that counter-flushing liquid of the present invention flows to schematic diagram in ceramic film component.
The specific embodiment:
Concrete steps of the present invention are:
A, at first threeway is installed at the purified liquor outlet place of ceramic film component feed end, in threeway, communicates with the counter-flushing liquid storage tank, backwashing pump, backwash control valve, backwashing pressure table are installed on pipeline by pipeline;
B, when ceramic membrane filter equipment cleans, in the recoil cleaning of evaporator, inject cleaning fluid in advance; , the temperature of cleaning fluid identical with circulation fluid temperature in the ceramic membrane equipment (20 ℃-95 ℃ of general ranges).Cleaning process is can be in the ceramic membrane filter device fabrication in service or all can clean when stopping production, and cleaning fluid can be a pure water or through ultrafiltration and have certain density soda acid water, for example 1% nitric acid or NaOH of 1% or the like;
C, close ceramic film component earlier and see through liquid outlet valve (being a valve and the b valve among Fig. 1) up and down; Close the system that connects this ceramic film component again and see through liquid outlet valve (being the c valve among Fig. 1), make it stop through liquid.Other ceramic film component continues operation.
D, open recoil cleaning of evaporator outlet valve, in backwashing pump, inject pure water;
E, open backwashing pump outlet pressure compensation flap, start backwashing pump, pure water is back in the recoil cleaning of evaporator, circulation in forming;
F, utilize the backwashing pressure compensation flap to regulate the backwash outlet pressure, when pressure reaches greater than this ceramic membrane spare inlet pressure 0.1～0.2MPa (pressure 〉=ceramic film component inlet pressure), open ceramic film component back flush valves (being the d valve among Fig. 1);
G, open ceramic film component and see through liquid outlet valve (being the b valve among Fig. 1); Regulate the backwashing pressure compensation flap once more, when making backwashing system pressure, utilize pressure differential method that ceramic film component is carried out backwash greater than ceramic film component import operating pressure 0.1～0.2MPa (pressure＞ceramic film component inlet pressure); The so-called backwash pressure that promptly to be flushing liquor produce by backwashing pump washes in the film tube passage from the outer surface of ceramic-film tube, with existing by the outwards flushing just in time opposite (as shown in Figure 3) of film pipe internal channel.
After 3min～10min is carried out in h, backwash, observe the recoil cleaning performance, close ceramic film component back flush valves (being the d valve among Fig. 1) after washing, open the pressure balance valve simultaneously, make the backwash pure water be back to the recoil cleaning of evaporator by concentrate return flow meter;
I, the system that opens ceramic film component see through liquid outlet valve (being the c valve among Fig. 1); Make ceramic film component recover normal operation.
More than be the back-flushing method of the present invention to a ceramic film component.
There are two kinds of situations basically in two or more ceramic film component back-flushing methods, and this connecting mode with ceramic film component is relevant.
One, when two or more ceramic film component parallel connections, can adopt a backwashing pump to carry out backwash simultaneously.
Two, when two or more ceramic film component coupled in series, can not carry out backwash simultaneously with a backwashing pump, and answer the classification section to carry out backwash respectively, or adopt a plurality of backwashing pumps simultaneously at different levels sections ceramic film components to be carried out backwash.
With two ceramic film component series connection purging methods is example, and its method is as follows:
1, repeats aforesaid purging method, finish the flushing of first ceramic film component (being the 1# ceramic film component among Fig. 1), proceed second ceramic film component and carry out backwash; At first threeway is installed, in threeway, communicates with the counter-flushing liquid storage tank, backwashing pump, backwash control valve, backwashing pressure table are installed on pipeline by pipeline at the purified liquor outlet place of 2# ceramic film component feed end;
2, close the 2# ceramic film component and see through liquid outlet valve (being e valve and the f valve among Fig. 1) up and down, close the system that connects this ceramic film component again and see through liquid outlet valve (being the g valve among Fig. 1), make it stop through liquid.Other ceramic film component continues operation.
3, regulate backwashing pump outlet pressure compensation flap, when making backwashing system pressure, open 2# ceramic film component back flush valves (being the h valve among Fig. 1) more than or equal to this ceramic film component internal pressure;
4, open the 2# ceramic film component and see through liquid outlet valve (being the f valve among Fig. 1).Regulate the backwashing pressure compensation flap once more, when making backwashing system pressure, utilize pressure differential method that the 2# ceramic film component is carried out backwash greater than 2# ceramic film component internal operation pressure 0.1-0.2MPa (pressure＞ceramic film component inlet pressure).
5, after 3min～10min is carried out in backwash, close 2# ceramic film component back flush valves (being the h valve among Fig. 1), open the pressure balance valve simultaneously, make the backwash pure water be back to purge tank;
6, open and see through liquid outlet valve (being the g valve among Fig. 1) in the 2# ceramic film component system, the 2# ceramic film component is normally moved
7, no matter what assemblies equipment has, and all can carry out backwash respectively by above narration program, or divides into groups to carry out backwash, makes membrane flux recover regeneration;
8, backwashing water requires to use pure water, needs often to change, in case microbiological contamination or other impurity enter in the system.
By that analogy, can wash more ceramic film component.
Concrete experimentation:
Experiment 1:
A equipment: new film, membrane area 0.1m
2, molecular cut off 100,000, non-recoil is washed
B equipment: new film, membrane area 0.1m
2, molecular cut off 100,000, backwash is arranged
Experiment place: Jilin Ji Hua company
The experiment feed liquid: 1, the ammediol zymotic fluid
A device processes 30L feed liquid ruuning situation sees Table 1
(0.3MPa/0.2MPa/25 ℃/800L/m of pure water test
2.h)
| Time | Inlet pressure | Outlet pressure | Temperature ℃ | Average flux | Remarks |
| 16:15 | ?0.3MPa | ?0.2MPa | ?28 | ?800ml/min | Start |
| 16:20 | ?0.3MPa | ?0.2MPa | ?34 | ?780ml/min | |
| 16:30 | ?0.3MPa | ?0.2MPa | ?40 | ?690ml/min | |
| 16:35 | ?0.3MPa | ?0.2MPa | ?48 | ?630ml/min | |
| 17:00 | ?0.3MPa | ?0.2MPa | ?52 | ?400ml/min | Add water 2.5L dialysis |
| 17:20 | ?0.3MPa | ?0.2MPa | ?62 | ?450ml/min | |
| 17:35 | ?0.3MPa | ?0.2MPa | ?78 | ?400ml/min | |
| 17:55 | ?0.3MPa | ?0.2MPa | ?70 | ?320ml/min | Add water 2.5L dialysis |
| 18:25 | ?0.3MPa | ?0.2MPa | ?72 | ?340ml/min | |
| 18:45 | ?0.3MPa | ?0.2MPa | ?72 | ?300ml/min | Shutdown |
| Average flux | ?150L/m 2.h |
Experimental result: total 2 hours 30 minutes time spent; Go out clear liquid 40L; Concentrate 4L adds water 5L; 50 liters of feed liquid ruuning situations of B equipment see Table 2
(0.3MPa/0.2MPa/25 ℃/800L/m of pure water test
2.h)
| Time | Inlet pressure | Outlet pressure | Temperature ℃ | Average flux | Remarks |
| ?16:15 | ?0.3MPa | ?0.2MPa | ?28 | ?800ml/min | Start |
| ?16:20 | ?0.3MPa | ?0.2MPa | ?31 | ?780ml/min | |
| ?16:30 | ?0.3MPa | ?0.2MPa | ?37 | ?690ml/min | |
| ?16:35 | ?0.3MPa | ?0.2MPa | ?40 | ?630ml/min | |
| ?17:00 | ?0.3MPa | ?0.2MPa | ?52 | ?400ml/min | Recoil dialysis 2.5L |
| ?17:20 | ?0.3MPa | ?0.2MPa | ?62 | ?470ml/min | |
| ?17:35 | ?0.3MPa | ?0.2MPa | ?78 | ?430ml/min | |
| ?17:55 | ?0.3MPa | ?0.2MPa | ?72 | ?320ml/min | Recoil dialysis 2.5L |
| ?18:25 | ?0.3MPa | ?0.2MPa | ?72 | ?360ml/min | |
| ?18:45 | ?0.3MPa | ?0.2MPa | ?74 | ?310ml/min | Shutdown |
| Average flux | ?170L/m 2.h |
Experimental result: total 3 hours times spent; Go out clear liquid 50L; Concentrate 5L adds water 5L;
The cleaning and regeneration of film:
With 60 ℃ of concentration is that 1% buck cleans A equipment, cleans 1 hour 30 minutes, and flux recovers as before; Same is that 1% buck cleans B equipment with 60 ℃ of concentration, and discontinuity opens backwashing system, cleans 45 minutes membrane fluxs with regard to recovery as before.
Conclusion:
1, the B equipment of backwash is arranged as can be seen than A equipment average flux height from table 1 and table 2
2, under similarity condition, there is the B equipment of backwash to recover to regenerate faster, more thorough than A equipment membrane flux.
Experiment 2:
A equipment: new film, membrane area 0.1m
2, molecular cut off 100,000, non-recoil is washed
B equipment: new film, membrane area 0.1m
2, molecular cut off 100,000, backwash is arranged
Experiment place: Changchun University of Traditional Chinese Medicine
Experiment feed liquid: Chinese traditional medicine water extract (compound GANMAO QINGRE KELI electuary)
A device processes 30L feed liquid ruuning situation sees Table 3
(0.3MPa/0.2MPa/25 ℃/800L/m of pure water test
2.h)
| Time | Inlet pressure | Outlet pressure | Temperature ℃ | Flux | Remarks |
| ?8:30 | ?0.3MPa | ?0.2MPa | ?65 | ?120L/m 2.h | Start |
| ?9:00 | ?0.3MPa | ?0.2MPa | ?68 | ?95L/m 2.h | |
| ?9:30 | ?0.3MPa | ?0.2MPa | ?70 | ?80L/m 2.h | |
| ?10:00 | ?0.3MPa | ?0.2MPa | ?72 | ?75L/m 2.h | |
| ?11:00 | ?0.3MPa | ?0.2MPa | ?75 | ?60L/m 2.h | |
| ?11:30 | ?0.3MPa | ?0.2MPa | ?78 | ?70L/m 2.h | Add water 2.5L dialysis |
| ?12:00 | ?0.3MPa | ?0.2MPa | ?80 | ?65L ?/m2.h | |
| ?12:30 | ?0.3MPa | ?0.2MPa | ?83 | ?50L ?/m2.h | Add water 2.5L dialysis |
| ?13:00 | ?0.3MPa | ?0.2MPa | ?85 | ?40L ?/m2.h | |
| ?13:30 | ?0.3MPa | ?0.2MPa | ?87 | ?35L ?/m2.h | Shut down |
| Average flux | ?54L ?/m2.h |
Experimental result: total 5 hours times spent; Go out clear liquid 27L; Concentrate 8L adds water 5L; Average flux 54L/m
2.h
30 liters of feed liquid ruuning situations of B equipment see Table 4
(0.3MPa/0.2MPa/25 ℃/800L/m of pure water test
2.h)
| Time | Inlet pressure | Outlet pressure | Temperature ℃ | Flux | Remarks |
| 8:30 | ?0.3MPa | ?0.2MPa | ?65 | ?120L/m 2.h | Start |
| 9:00 | ?0.3MPa | ?0.2MPa | ?65 | ?95L/m 2.h | |
| 9:30 | ?0.3MPa | ?0.2MPa | ?68 | ?80L/m 2.h | |
| 10:00 | ?0.3MPa | ?0.2MPa | ?70 | ?75L/m 2.h |
| ?10:30 | ?0.3MPa | ?0.2MPa | ?72 | ?80L/m 2.h | Recoil dialysis 2.5L |
| ?11:00 | ?0.3MPa | ?0.2MPa | ?75 | ?65L/m 2.h | |
| ?11:30 | ?0.3MPa | ?0.2MPa | ?80 | ?75L/m 2.h | Recoil dialysis 2.5L |
| ?12:00 | ?0.3MPa | ?0.2MPa | ?83 | ?60L/m 2.h | |
| ?12:30 | ?0.3MPa | ?0.2MPa | ?85 | ?45L/m 2.h | Shut down |
| Average flux | ?68L/m 2.h |
Experimental result: total 4 hours times spent; Go out clear liquid 27L; Concentrate 8L adds water 5L; Average flux 68L/m
2.h
The cleaning and regeneration of film:
With 60 ℃ of concentration is that 1% buck cleans A equipment, cleans 1 hour 30 minutes, and flux recovers as before; Same is that 1% buck cleans B equipment with 60 ℃ of concentration, and discontinuity opens backwashing system, cleans 45 minutes membrane fluxs with regard to recovery as before.
Conclusion:
1, the B equipment of backwash is arranged as can be seen than A equipment average flux height from table 1 and table 2
2, under similarity condition, there is the B equipment of backwash to recover to regenerate faster, more thorough than A equipment membrane flux.
Claims (1)
1. ceramic film backwash method is characterized in that:
A, at first threeway is installed at the purified liquor outlet place of ceramic film component feed end, in threeway, communicates with the counter-flushing liquid storage tank, backwashing pump, backwash control valve, backwashing pressure table are installed on pipeline by pipeline;
B, when ceramic membrane filter equipment cleans, in the recoil cleaning of evaporator, inject cleaning fluid in advance;
C, close ceramic film component earlier and see through the liquid outlet valve up and down; Close the system that connects this ceramic film component again and see through the liquid outlet valve, make it stop through liquid; Other ceramic film component continues operation;
D, open recoil cleaning of evaporator outlet valve, in backwashing pump, inject pure water;
E, open backwashing pump outlet pressure compensation flap, start backwashing pump, pure water is back in the recoil cleaning of evaporator, circulation in forming;
F, utilize the backwashing pressure compensation flap to regulate the backwash outlet pressure, when pressure reaches greater than this ceramic membrane spare inlet pressure, open the ceramic film component back flush valves;
G, open ceramic film component and see through the liquid outlet valve; Regulate the backwashing pressure compensation flap once more, when making backwashing system pressure, utilize pressure differential method that ceramic film component is carried out backwash greater than ceramic film component internal operation pressure;
After 3min～10min is carried out in h, backwash, observe backwash effect, close the ceramic film component back flush valves after washing, open the pressure balance valve simultaneously, make the backwash pure water be back to the recoil cleaning of evaporator by concentrate return flow meter;
I, the system that opens ceramic film component see through the liquid outlet valve; Make ceramic film component recover normal operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007100560179A CN101185847A (en) | 2007-08-31 | 2007-08-31 | Ceramic film backwash method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007100560179A CN101185847A (en) | 2007-08-31 | 2007-08-31 | Ceramic film backwash method |
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| Publication Number | Publication Date |
|---|---|
| CN101185847A true CN101185847A (en) | 2008-05-28 |
Family
ID=39478594
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007100560179A Pending CN101185847A (en) | 2007-08-31 | 2007-08-31 | Ceramic film backwash method |
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| Country | Link |
|---|---|
| CN (1) | CN101185847A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102234162A (en) * | 2010-04-28 | 2011-11-09 | 冯军 | Double-flow single-pump fluid process equipment |
| CN104645835A (en) * | 2015-02-02 | 2015-05-27 | 杭州利群环保纸业有限公司 | Cleaning method and device for deeply removing impurities of tobacco extract liquid with silicon carbide film method |
| CN106045816A (en) * | 2016-06-22 | 2016-10-26 | 苏州苏震生物工程有限公司 | Membrane filtration and separating method using PDO (1,3-propylene glycol) fermenting liquid |
| CN106861440A (en) * | 2017-03-22 | 2017-06-20 | 科林普尔环保科技有限公司 | A kind of new reverse osmosis membrane is on-line Full positive and negative to wash cleaning equipment |
-
2007
- 2007-08-31 CN CNA2007100560179A patent/CN101185847A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102234162A (en) * | 2010-04-28 | 2011-11-09 | 冯军 | Double-flow single-pump fluid process equipment |
| CN104645835A (en) * | 2015-02-02 | 2015-05-27 | 杭州利群环保纸业有限公司 | Cleaning method and device for deeply removing impurities of tobacco extract liquid with silicon carbide film method |
| CN106045816A (en) * | 2016-06-22 | 2016-10-26 | 苏州苏震生物工程有限公司 | Membrane filtration and separating method using PDO (1,3-propylene glycol) fermenting liquid |
| CN106045816B (en) * | 2016-06-22 | 2018-08-07 | 苏州苏震生物工程有限公司 | A kind of 1,3- propanediol fermentation liquors membrane filtration separation method |
| CN106861440A (en) * | 2017-03-22 | 2017-06-20 | 科林普尔环保科技有限公司 | A kind of new reverse osmosis membrane is on-line Full positive and negative to wash cleaning equipment |
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Open date: 20080528 |