CN1140325C - Two-way working film separation method and equipment therefor - Google Patents
Two-way working film separation method and equipment therefor Download PDFInfo
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- CN1140325C CN1140325C CNB011040955A CN01104095A CN1140325C CN 1140325 C CN1140325 C CN 1140325C CN B011040955 A CNB011040955 A CN B011040955A CN 01104095 A CN01104095 A CN 01104095A CN 1140325 C CN1140325 C CN 1140325C
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Abstract
The present invention relates to a film separating method and device. The film separating method and device is characterized in that after a film component works for a certain time each time, material liquid in the film component reversely flows through a designed converting system so that films are simultaneously separated and cleaned, and the liquid flow penetrating direction is unchanged. On the basis of the existing film separating device, the converting system correspondingly designed according to film separating method and device comprises a reverse liquid inlet valve, a reverse liquid outlet valve and corresponding connecting pipelines, wherein one end of the reverse liquid inlet valve is in pipe connection to any position of a pipeline between a pump and the liquid inlet valve, and the other end is in pipe connection to any position of a pipeline between the liquid outlet valve and a liquid outlet; one end of the reverse liquid outlet valve is in pipe connection to any position of a pipeline between the liquid inlet valve and a liquid inlet, and the other end is in pipe connection to a material liquid tank.
Description
Technical field
The present invention relates to membrane separating method and device thereof, but be specially the doughnut membrane separating method and the device thereof of two-way operation, it is that B01D 63/02 is or/and B01D 65/02 that international Patent classificating number is intended.
Background technology
The membrane separation technique method and apparatus now has been widely used in the industrial circles such as chemical industry, medicine, food, beverage, water treatment, is important a kind of in the modern technologies.Present general film (inner pressed hollow-fibre membrane, hereinafter to be referred as interior press mold or film) separation method and the device all be an endfeed liquid that makes membrane module, another brings out filtered solution, and the middle opening of membrane module (C mouth) goes out through liquid, feed liquid one-way flow and carry out the film mask work.In practical application in industry, membrane separating method and device thereof are used for some concentrated purpose, when concentrating as the biochemical fermentation liquid system, the capital produces following problem: along with the raising of separation system cycles of concentration, the film pollution level strengthens, the percolate flux of membrane separation device can reduce, and also is decrease in efficiency, even concentration process can't normally be carried out.Present solution is to lengthen working hours, and the poor efficiency running is to reach required cycles of concentration; Perhaps stop, behind cleaning or the replacing membrane module, continue again to produce.And the cleaning method of existing membrane module or film device is to make the work of cleaning fluid one-way flow equally, and promptly an end is squeezed into cleaning fluid, and the other end flows out washed liquid, thereby the flux of film is increased.These methods are time-consuming, feed consumption, poor efficiency, directly influence ordinary production, but people are accustomed to like nothing to be surprised at, do not think that it is the open defect that membrane separating method and device thereof exist.
Summary of the invention
Purpose of the present invention is exactly the above-mentioned defective at press mold separation method in existing and device thereof, a kind of membrane separating method and device thereof that can two-way operation be provided, it has makes film mask work and cleaning online advantage of carrying out simultaneously, also has simple and easy to do, efficient characteristics simultaneously.
The objective of the invention is following realization: the inventive method is behind the every work certain hour of membrane module, utilize the converting system of design, make the material liquid reverse flow in the membrane module, and the flow direction that sees through liquid is constant, it is characterized in that making film separation and cleaning to carry out simultaneously, and the material liquid outlet pressure is 0; Described converting system comprises reverse feed liquor valve, reverse liquid valve and corresponding connecting line; One end pipe of described reverse feed liquor valve is connected on arbitrary position of pipeline between pump and the feed liquor valve, and other end pipe is connected on arbitrary position of pipeline between liquid valve and the liquid outlet; Oppositely an end pipe of liquid valve is connected on the feed liquor valve to arbitrary position of pipeline between the inlet.Other end pipe is connected in the material liquid tank.
When the filter efficiency that occurs membrane module because of previous reasons reduces, and then the percolate flux of membrane separation device also reduces, when needing rinsing membrane module (behind the membrane module work certain hour), the inventive method and device do not need the existing needed rinsing membrane module program of membrane separation device, but utilize described converting system, make the flow direction of the operative orientation of membrane module or material liquid (abbreviation feed liquid) opposite, can continue operate as normal.Be (referring to Fig. 2) specifically, open reverse feed liquor valve 6 and reverse liquid valve 8 earlier, close feed liquor valve 7 and liquid valve 5 then, just can make membrane module obtain cleaning, can make the reverse film mask work that oppositely continues in other words of membrane module simultaneously again.When going out (being forward) mode on advancing under the flow direction of filtering stoste is in, the lower semisection hollow-fibre membrane is in the filtration duty in the membrane module, and the upper semisection hollow-fibre membrane is in isobaric cleaning state owing to being bordering on no pressure reduction; Commutation back (being the reverse operation mode), the upper semisection hollow-fibre membrane that has just cleaned has entered duty, and the lower semisection hollow-fibre membrane of just having worked has then entered isobaric cleaning state.So same hollow fiber film assembly is in all the time simultaneously works and the cleaning state efficiently.So positive and negative alternate running makes the described membrane separation device can online long-time continuous ground operate as normal, thereby realizes the two-way membrane module that utilizes of the present invention, and on-line continuous work, and is both simple and easy to do, efficient again goal of the invention.
The inventive method is on the basis of press mold separator in existing, only increased by a cover converting system, be simple two valves (reverse feed liquor valve 6 as shown in Figure 2 and reverse liquid valve 8) and suitable connecting line, under the situation of not stopping, utilize described converting system (as mentioned above by the corresponding valve of switch), rinsing membrane module effectively just, the forward (defining original operative orientation is forward) that can also realize simultaneously membrane module separates and cleaning with the two-way on-line continuous of reverse (operative orientation that definition increases newly is for reverse), thereby obviously has simple in structure, easy to use, efficient improves (referring to specific embodiment described later), consume plurality of advantages such as reduction.
Description of drawings
Be described in further detail the present invention below in conjunction with embodiment and accompanying drawing thereof:
Fig. 1 is the schematic diagram of the inventive method membrane separation device or membrane module operation principle; Among the figure, A, B are that membrane module stoste imports and exports, and C is for seeing through the liquid outlet, and 14 flow to switching mechanism for material liquid.
Fig. 2 is the structural representation of a kind of interior press mold separator embodiment of suitable the inventive method; During the material liquid forward flow, valve 6,8 is closed, and valve 7 is the stoste inlet valve, and valve 5 is the stoste outlet valve; During the stoste reverse flow, open reverse inlet valve 6 of stoste and reverse outlet valve 8, close feed liquor valve 7 and liquid valve 5.
Fig. 3 is the structural representation of a kind of interior press mold separator embodiment with the bubbling air device of being suitable for the inventive method;
Fig. 4 is for being suitable for a kind of structural representation of taking back the interior press mold separator embodiment of stream device of the inventive method;
Fig. 5 is the structural representation of a kind of interior press mold separator embodiment with back purge system of being suitable for the inventive method;
Fig. 6 is for being suitable for a kind of structural representation that has the interior press mold separator embodiment of bubbling air device and reflux simultaneously of the inventive method;
Fig. 7 is for being suitable for a kind of structural representation that has the interior press mold separator embodiment of bubbling air device and back purge system simultaneously of the inventive method;
Fig. 8 is for being suitable for a kind of structural representation that has the interior press mold separator embodiment of reflux and back purge system simultaneously of the inventive method;
Fig. 9 is for being suitable for a kind of structural representation that has the interior press mold separator embodiment of bubbling air device, reflux and back purge system simultaneously of the inventive method.
The specific embodiment
The inventive method is based on following research and design (referring to Fig. 2): when existing membrane separation device is worked, feed liquid is to be pressed in the hollow-fibre membrane (hereinafter to be referred as film) in the A end (or a certain end) of membrane module 1 is squeezed into by pump 10, and filtered solution is flowed out by the B end of membrane module 1.Because of the plus-pressure in A end (feed liquid upstream end) zone is bigger, will causes the inside and outside pressure reduction of film both sides or film higher, thereby make the film of A end regions be in the state of working hard.Because the feed liquid pressure loss that flow resistance causes in film, can make away from the pressure reduction of the film both sides of A end (promptly gradually near the B end) gradually or gradient reduce, even be 0, so, in fact film away from A end or close gradually B end is not in running order, but is in minute-pressure or isobaric flushing state.Simple saying is exactly.The film of A end regions is in running order, and the film of B end regions is actual to be to be in the flushing state.Because existing membrane separating method feed liquid is always squeezed in the film from the A end of membrane module 1 by pump 10, filtered solution is flowed out by the B end of membrane module 1, be one-way flow or one-way only operation, so, behind film device work certain hour, the A end regions of in running order film dwindles gradually, and work quality also descends gradually, during down to whole film or membrane module forfeiture film mask work ability, must stop, rinsing membrane module could recover operate as normal.Can expect in view of the above, since now the practical work process of membrane module is that the film of A end regions of membrane module is in running order, the film of B end regions is in the flushing state, so, why not can be behind film device work certain hour, the film of being taken over the A end regions by the film that washed or be in the B end regions of flushing state continues the film mask work, and allow the film of A end regions be converted to the flushing state by duty, recovering its original film separating power, but and then the high-efficiency and continuous that just realizes not stopping produce! Research and experiment show that all answer is sure, promptly adopt membrane separating method and device thereof that can two-way operation of the present invention.
The inventive method is following design (referring to Fig. 1): design one cover membrane module work feed liquid flows to converting system (abbreviation converting system) 14, behind the every work certain hour of membrane module, utilize the converting system 14 of design, make the material liquid reverse flow in the membrane module, even feed liquid (solid arrow among Fig. 1 is represented its flow direction) enters membrane module by the A end, filtered solution (the line of dots arrow among Fig. 1 represents that it flows to) flows out the just flow direction (arrow upwards) duty of membrane module from the B end, be converted to feed liquid and enter membrane module by the B end, filtered solution flows out reverse direction flow (arrow the is downward) duty of membrane module from the A end; And film separation and cleaning are carried out simultaneously, and when promptly just flowing to, the film of A end regions is in running order, and the film of B end regions is in the flushing state; During reverse direction flow, the film of B end regions is in running order, and the film of A end regions is in the flushing state.No matter and just flowing to, or reverse direction flow, the flow direction that sees through liquid (dash-dot arrows among Fig. 1 represents that it flows to) all remains unchanged, and flows out from the C mouth of membrane module.The trade-off work like this of film A, B end just can realize under the not parking situation easily, carries out film efficiently simultaneously and separates and cleaning.
According to the inventive method respective design a kind of membrane separation device (referring to Fig. 2).It is a press mold separator in existing, comprise on the parts bases such as membrane module 1, feed liquor valve 7, liquid valve 5, Pressure gauge 12,13, pump 10 and material liquid tank 11, newly establish described converting system 14, comprised reverse feed liquor valve 6, reverse liquid valve 8 and corresponding connecting line; One end pipe of described reverse feed liquor valve 6 is connected on arbitrary position of pipeline between pump 10 and the feed liquor valve 7 (all valves that does not point the direction and table all make a comment or criticism to, with terse narration), and other end pipe is connected on arbitrary position of pipeline between liquid valve 5 and the liquid outlet 2; One end pipe of described reverse liquid valve 8 is connected on feed liquor valve 7 to arbitrary position of pipeline between the inlet 3, and other end pipe is connected in the material liquid tank 11, thereby constitutes a new membrane separation device.So-called " arbitrary position " is meant that the assembly that is increased maintains and manipulates structural design, the installation of membrane separation device all is scientific and reasonable position; And for the manage situation that exists Pressure gauge (inlet hydraulic table 12 and fluid Pressure gauge 13) in the road of taking over, both then be meant simultaneously and can pipe be connected on before the Pressure gauge (by work feed liquid flow direction, between fluid Pressure gauge 13 and liquid outlet 2) arbitrary position on one section pipeline, also can pipe be connected on the arbitrary position on (between liquid valve 5 and fluid Pressure gauge 13) one section pipeline after the Pressure gauge.
Apparatus of the present invention course of work is (referring to shown in Figure 2): when the forward duty, charging pump 10 pumps feed liquid from batch can 11, by the feed liquor valve 7 opened (at this moment, oppositely feed liquor valve 6 is in closed condition) and inlet hydraulic table 12 to squeeze into inlet 3 interior (at this moment, oppositely liquid valve 8 is in closed condition), and then inject each membrane module 1 and carry out the film separation; Seeing through liquid flows out through filtrate valve 9 from leaching mouthful (C mouth) 4; Filtered solution then flows out from liquid outlet 2, again among fluid Pressure gauge 13 and liquid valve 5 are back to material liquid tank 11.
Behind membrane separation device forward work certain hour, along with the raising of separation system concentration multiple, when the operating efficiency of membrane separation device and percolate flux greatly reduced, the staff just can implement simple reverse operation operation.The using method of the embodiment of the invention is specifically: the staff only needs open earlier according to the order of sequence reverse feed liquor valve 6 and reverse liquid valve 8, close feed liquor valve 7 and liquid valve 5 again, make temporary transient interruption of work feed liquid forward loop and carry out reverse flow, also can make the membrane module reverse operation simultaneously.When the reverse operation state (referring to shown in Figure 2), charging pump 10 pumps feed liquid from batch can 11, by the reverse feed liquor valve 6 opened (at this moment, feed liquor valve 7 has cut out) and fluid Pressure gauge 13 is (at this moment, liquid valve 5 is also closed) squeeze in the liquid outlet 2, and then inject each membrane module 1 and carry out the film separation; Seeing through liquid still flows out through filtrate valve 9 from leaching mouth 4; Filtered solution then flows out from inlet 3, again (at this moment through reverse liquid valve 8, feed liquor valve 7 has cut out) be back among the material liquid tank 11. under the reverse operation state, fluid Pressure gauge 13, liquid outlet 2 and inlet 3 during forward work commutate respectively---changing role, (this only is clear and convenient for what narrate to actual inlet hydraulic table 13, inlet 2 and liquid outlet 3 when becoming reverse operation, can adopt the neutral component Name of not being with directionality fully,, table several as valve is several etc.).Behind reverse operation state work certain hour, when the operating efficiency of membrane separation device and percolate flux greatly reduce, just need to clean once more, also promptly recover forward duty (also being simultaneously the cleaning of membrane module during to reverse operation).The staff can implement simple reverse operation operation equally.Specifically: open feed liquor valve 7 and liquid valve 5 according to the order of sequence earlier, close reverse feed liquor valve 6 and reverse liquid valve 8 again, make the temporary transient interruption in work feed liquid return circuit and recover forward flow, make the work of membrane module recovery forward simultaneously again.So positive and negative alternate running, membrane module or film device can obtain cleaning under the situation of not stopping efficiently, can guarantee that the film mask work normally carries out for a long time continuously simultaneously.
The principle of efficient operation of the present invention is to make the duty and the flushing state of membrane separation device and deposit, and carries out simultaneously in other words.When forward is worked, feed liquid is pressed in the hollow-fibre membrane in the A end of membrane module 1 is squeezed into by pump 10, because of the plus-pressure in A end (feed liquid upstream end) zone is bigger, will causes the inside and outside pressure reduction of film both sides or film higher, thereby make the film of A end regions be in the state of working hard.Because the feed liquid pressure loss that flow resistance causes in film, can make away from the pressure reduction of the film both sides of A end (promptly gradually near the B end) gradually or gradient reduce, even be 0, so, in fact film away from A end or close gradually B end is not in running order, but is in minute-pressure or isobaric flushing state.Simple saying is exactly.The film of A end regions is in running order, and the film of B end regions is in the flushing state.When reverse operation, feed liquid is pressed in the hollow-fibre membrane in the B end of membrane module 1 is squeezed into by pump 10, plus-pressure increase because of B end (feed liquid upstream end) zone, will cause the inside and outside pressure reduction of film both sides or film higher, thus minute-pressure the when film of B end regions work by forward or isobaric the work hard state of state-transition when being reverse operation that wash.Meanwhile, the A end stops (closing feed liquor valve 7) feed in advance, it no longer is the feed liquid inlet, this regional film also no longer includes source pressure, thereby the same because feed liquid pressure loss that flow resistance causes in film, can make away from the pressure reduction of the film both sides of B end (promptly gradually near the A end) gradually or gradient reduce, even be 0, so, minute-pressure or isobaric flushing state when the state-transition of working hard when also being worked by forward away from the film of B end or close gradually A end is reverse operation.Simple saying is exactly.The film of B end regions is in running order, and the film of A end regions is in the flushing state.This means, no matter be the forward duty, or the reverse operation state, the two-way membrane separation device of the present invention all is that the part of film is in the mask work state, its another part is in the flushing state simultaneously, and constant through the unidirectional outflow of liquid.
It should be appreciated that, the principle of efficient operation of the present invention is not only duty and the flushing state that makes membrane separation device and is deposited, and be to make that two states is active and effective to carry out simultaneously: in running order film end, passing with the working time, the closer to its end face, pollution is just serious more, and the ability of continuous firing is just poor more; And after the task at film two ends was exchanged, this end just was converted to the flushing state, and at this moment, the closer to its end face, the pressure reduction inside and outside the film is just more little, or even 0, therefore the effect of isobaric flushing is just good more.After the role replaced once more, then the closer to its end face, film just cleaned more, and inside and outside pressure reduction is just big more, and the effect of separation is just good more.So ingenious design of the present invention has met effective working mechanism of film well, film is separated and the flushing maximum effect can be desirable and bring into play fully.In a word, behind certain or reasonable time interval, the exchange of film A, B two ends task or role replace, not only finished the design of the inventive method and membrane separation device two-way operation, prolonged the time of membrane separation device continuous firing greatly, but also realized on-line cleaning, separated, clean and carry out simultaneously, simple and easy to do, the purpose of double or many times of effects.
So-called " certain or reasonable time at interval " is meant that definite commutation working time is at interval or the cycle according to the viscosity of filtration system with owing to pollute the permeation flux pad value situation that causes.General commutation or counter-rotating working time are 10～180 minutes, and the working time is 20～60 minutes preferably.
In order to make the inventive method and device thereof better and more effectively bring into play usefulness, can also carry out improvement as described below, improve or improve body membrane separator of the present invention:
1. pipe inserts bubbling air device (referring to Fig. 3) on described membrane separation device, is included on arbitrary position of pipeline between pump 10 and the feed liquor valve 7, and pipe is connected to control valve 16; On arbitrary position of pipeline between control valve 16 and the feed liquor valve 7, the order pipe is connected to intake valve 15 and compressed air gas source 17.Its action principle is when the needs bubbling air cleans, can open valve 15, feeding compressed air.Utilize the souring of gas-vapor mix to clean the pollutant on hollow-fibre membrane surface, to recover the permeation flux of film.
2. pipe inserts reflux (referring to Fig. 4) on described membrane separation device, is included in the return valve 18 that pipe connects on arbitrary position of pipeline between pump 10 and the feed liquor valve 7, its other end pipe access material liquid tank 11.Its action principle is, when the output of water pump 10 is big, can appropriateness open valve 18, to regulate the inlet pressure of film.Prevent owing to the membrane filtration hypertonia is damaged diffusion barrier.
3. pipe inserts back purge system (referring to Fig. 5) on described membrane separation device, is included in the order pipe connects in the following outlet of membrane module 1 Pressure gauge 24, valve 20, pump 23, valve 19 and can,douche 22; Also pipe is connected to valve 21 between can,douche 22 and valve 19.Its effect is that by opening valve 20, the water pressure of utilizing water pump to squeeze into is carried out backwash to membrane module.This operation both can be carried out in filter process simultaneously, also can finish to carry out separately when the back is cleaned filtration system in filtration.
4. be any two kinds in described bubbling air device, reflux or the back purge system of pipe access simultaneously on described membrane separation device, comprise that promptly pipe inserts described bubbling air device and reflux (referring to Fig. 6) simultaneously; Pipe inserts described bubbling air device and back purge system (referring to Fig. 7) simultaneously; Pipe inserts described reflux and back purge system (referring to Fig. 8) simultaneously.The effect of each device that inserts as hereinbefore.They both can use separately, also can be used.When being used, can improve the filter efficacy of film well.
5. on described membrane separation device, manage simultaneously and insert described bubbling air device, reflux and back purge system (referring to Fig. 9).This is the most perfect design.Equally, the effect of each device that inserts as hereinbefore.They both can use separately, also can be used.When being used, can further improve the filter efficacy of film.
The purpose of the bubbling air device of above-mentioned increase design is, the bubble oscillation effect that the compressed air that utilization is squeezed into produces in liquid, quickening pollutant comes off from film, improve the effect of on-line cleaning, and then the filter efficacy of increase membrane separation device, its concrete running parameter is (referring to Fig. 3): charge into compressed-air actuated pressure than the high 0.01～0.10MPa of film inlet pressure.The frequency that adds air is the every work 10-180 of film device minute, charges into compressed air 2-240 second.Concrete time parameter relies on concrete filtered fluid to determine.Principle is, makes permeation flux descend when very fast because film pollutes, and can shorten bubbling air (promptly improving frequency) at interval, also can prolong each feeding compressed air time, also can both improve frequency, increases each the feeding the compressed-air actuated time simultaneously again.
The purpose of the reflux of above-mentioned increase design is, utilizes bypass return valve 18 to regulate the operating pressure of membrane filtration, prevents owing to the filtration system hypertonia is damaged diffusion barrier.
The purpose of the back purge system of above-mentioned increase design is, the film that utilizes back purge system further to improve membrane separation device separates effect and cooperates the membrane separating method of two-way operation of the present invention to realize the on-line cleaning of film device better: also can wash or improve yield to the filtered solution product concentrate simultaneously.
Obviously, described bubbling air device, reflux and back purge system both can use separately, also can be used in combination arbitrarily, and for example, pipe inserts described bubbling air device and reflux (referring to Fig. 6) simultaneously; Or pipe inserts described bubbling air device and back purge system (referring to Fig. 7) simultaneously; Or pipe inserts described reflux and back purge system (referring to Fig. 8) simultaneously.And the best selection of implementing is to manage simultaneously to insert bubbling air device, reflux and back purge system (referring to Fig. 9).Like this, according to actual needs, both can use a certain device wherein separately, and also can be used certain two kinds of device wherein simultaneously, perhaps three kinds of devices are used together.When three kinds of devices used simultaneously, the course of work that it is concrete and the course of work of aforesaid a certain device did not have essential distinction.
Should be pointed out that converting system 14 of the present invention is not limited to above-mentioned simple embodiment, it can also adopt other modes to realize, as timing controlled converting system 14, autocontrol valve converting system 14, computer control converting system 14 etc.Pump 10 of the present invention and 23 both can be common constant speed water pump 10 and 23, also can be novel frequency conversion speed adjusting pump 10 and 23, with the pressure stability of guaranteeing piece-rate system and the quality requirement that satisfies real work.
Provide specific embodiment and comparative example below:
Embodiment 1: adopt method of the present invention and membrane separation device shown in Figure 2 to be used for concentrating of certain amino acid fermentation liquid.The heavy 42g/L of the wet bacterium of fermented liquid handles zymotic fluid 1.3m
3(specification is the membrane separation device of the present invention of 89 * 1000mm) 8 formations of φ to the inner pressed Kynoar hollow fiber microporous membrane membrane module that adopts Tianjin MoTian Membrane Engineering Technology Co., Ltd to produce; The major parameter design is: the pressure of inlet is 0.1MPa, and liquid valve is opened (being that outlet pressure is 0); Setting commutating period is 20 minutes, concentrates.Only after 55 minutes, the zymotic fluid cycles of concentration has promptly reached 12 times; The concentrated requirement that weighed of wet bacterium.
Embodiment 2: adopt membrane separation device of the present invention as shown in Figure 3 to concentrate.Adopt frequency conversion speed adjusting pump, inlet pressure is set at 0.10MPa, and outlet pressure is 0, feeds the compressed air of a 0.12Mpa in per 10 minutes, and in each 10 seconds, all the other conditions concentrate after 60 minutes with embodiment 1, and the zymotic fluid cycles of concentration has promptly reached 12 times; Reached concentrated requirement.Owing to adopt VFC, thereby inlet pressure is steady in concentration process, keep constant pressure value, effectively prevented because the membrane module that superpressure causes damages.
Embodiment 3: adopt membrane separation device of the present invention as shown in Figure 6 to concentrate.Inlet pressure was set at 0.10MPa, and outlet pressure is 0, charged into the compressed air of a 0.15MPa every 10 minutes, and in each 30 seconds, all the other conditions concentrate after 45 minutes with embodiment 1, and the zymotic fluid cycles of concentration has promptly reached described concentrated requirement.
Embodiment 4: adopt membrane separation device of the present invention as shown in Figure 9 to concentrate.The heavy 40g/L of the wet bacterium of fermented liquid handles zymotic fluid 2.5m
3, inlet pressure is set at 0.10MPa, and outlet pressure is 0, and setting commutating period is 30 minutes; After the commutation, the employing backwash pressure is 0.11Mpa, and in 60 seconds of backwash, backwash liquor is a deionized water, by adding water thalline is washed simultaneously; All the other conditions concentrate after 120 minutes with embodiment 1, and the zymotic fluid cycles of concentration has promptly reached desired 11 times.
Embodiment 5: adopt membrane separation device of the present invention as shown in Figure 7 to concentrate.The heavy 47g/L of the wet bacterium of fermented liquid handles zymotic fluid 2.3m
3Adopt frequency conversion speed adjusting pump, inlet pressure is set at 0.10MPa, and outlet pressure is 0, and setting commutating period is 30 minutes; After the commutation, adopt backwash pressure 0.11MPa backwash 60 seconds, backwash liquor was a deionized water, by adding water thalline is washed simultaneously, charged into the compressed air 30 seconds of 0.15MPa every 10 minutes.All the other conditions concentrate after 130 minutes with embodiment 1, and the zymotic fluid cycles of concentration has promptly reached desired 10 times.
Embodiment 6: the inventive method is used for the clear and bright refining of certain amino acid fermentation liquid.The volume of fermented liquid is 1.0m
3(specification is that 89 * 1000mm) 8 of φ constitute membrane separation device of the present invention shown in Figure 5 to adopt the inner pressed Kynoar hollow fiber microporous membrane membrane module that Tianjin MoTian Membrane Engineering Technology Co., Ltd produces; Adopt frequency conversion speed adjusting pump, the pressure of inlet is 0.1MPa, and outlet pressure is 0; Setting commutating period is 20 minutes, filters.After the commutation, adopt backwash pressure 0.11Mpa, in 60 seconds of backwash, backwash liquor is a deionized water.Filter after 58 minutes, amino acid whose yield reaches 98% in the zymotic fluid.
Comparative example 1: adopt general membrane separation device, all the other conditions are with embodiment 1.The every work of membrane separation device 20 minutes just needs isobaric flushing 5 minutes; When zymotic fluid is concentrated into 8 times, consuming time 2 hours 50 minutes.
Comparative example 2: except that the outlet pressure of membrane separation device is adjusted into the 0.05Mpa, all the other conditions are with comparative example 1.When zymotic fluid is concentrated into 7 times, consuming time 3 hours 25 minutes.
Claims (1)
1. press mold separation method in a kind, behind the every work certain hour of membrane module (1), utilize converting system (14) to make material liquid reverse flow in the membrane module (1), and the flow direction that sees through liquid is constant, it is characterized in that the interior film of described membrane module (1) separates and cleaning is carried out simultaneously, and the material liquid outlet pressure is 0; Described converting system (14) comprises reverse feed liquor valve (6), reverse liquid valve (8) and corresponding connecting line; One end pipe of described reverse feed liquor valve (6) is connected on arbitrary position of pipeline between pump (10) and the feed liquor valve (7), and other end pipe is connected on arbitrary position of pipeline between liquid valve (5) and the liquid outlet (2); Oppositely an end pipe of liquid valve (8) is connected on feed liquor valve (7) to arbitrary position of pipeline between the inlet (3), and other end pipe is connected in the material liquid tank (11).
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| Application Number | Priority Date | Filing Date | Title |
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| CNB011040955A CN1140325C (en) | 2001-02-23 | 2001-02-23 | Two-way working film separation method and equipment therefor |
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| CNB011040955A CN1140325C (en) | 2001-02-23 | 2001-02-23 | Two-way working film separation method and equipment therefor |
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| CN1311055A CN1311055A (en) | 2001-09-05 |
| CN1140325C true CN1140325C (en) | 2004-03-03 |
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| CN101785972B (en) * | 2009-01-23 | 2011-10-26 | 天津膜天膜科技股份有限公司 | Water treatment system with bidirectional cleaning function |
| JP6287860B2 (en) * | 2013-06-21 | 2018-03-07 | 東レ株式会社 | Filtration device, chemical production device, and operation method of filtration device |
| CN109381998A (en) * | 2017-08-09 | 2019-02-26 | 上海澄沥环保科技有限公司 | A kind of reverse osmosis nanofiltration processing technique |
| CN109647216B (en) * | 2019-01-18 | 2021-07-06 | 清华大学深圳研究生院 | System and method for on-line chemical cleaning of ceramic membrane |
| CN109925886B (en) * | 2019-04-09 | 2021-10-01 | 吕剑阳 | Application method and device of internal pressure type hollow fiber membrane component |
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