CN109925886A - A kind of application method and its device of inner pressed hollow fiber film assembly - Google Patents
A kind of application method and its device of inner pressed hollow fiber film assembly Download PDFInfo
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- CN109925886A CN109925886A CN201910280042.8A CN201910280042A CN109925886A CN 109925886 A CN109925886 A CN 109925886A CN 201910280042 A CN201910280042 A CN 201910280042A CN 109925886 A CN109925886 A CN 109925886A
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Abstract
The present invention relates to the application methods and its device of a kind of inner pressed hollow fiber film assembly, flow direction periodically reversed of the feed liquid in membrane module tube side, newly establish filtered solution outlet pressure regulating valve, in membrane filtration processes, the filtered solution side outlet pressure value of membrane module is higher than the pressure value at membrane module concentrated solution outlet, difference is set as 0.02-0.08MPa, preferably 0.03-0.05.To make the film close to concentrated solution outlet end be in back flush state.In turn, feed liquid concentrated solution outlet pressure-regulating valve and switch valve are newly established.Adjusting feed liquid concentrated solution outlet pressure value 0.03-0.05MPa, intermediate period of the switch valve in each reversal of direction of flow period, standard-sized sheet 1-5 minutes.The drawbacks of needing stopper film filtering, offline cleaning the present invention overcomes conventional membrane separation device, has many advantages, such as structure is simple, easy to use, film filter efficacy improves.
Description
Technical field
The invention belongs to UF membrane fields, are related to inner pressed hollow fiber film assembly, especially a kind of hollow fibre of inner pressed
Tie up the application method and its device of membrane module.
Background technique
Inner pressed Hollow Fiber Membrane Separation Technology has been widely used in the works such as chemical industry, medicine, food, beverage, water process
Isolation and purification in industry field.
In inner pressed hollow fiber film assembly structure general at present, hollow fiber film thread is parallel arrangement, and both ends are used
The sealing end sealant such as epoxy resin is fixed in the shell of membrane module.When film filters, feed liquid enters film from one end of film wire tube side
Silk is internal, and concentrate flows out membrane module from the other end of film wire tube side, and filtered solution then penetrates doughnut membranous wall, from membrane module
Shell side flow out membrane module, feed liquid one-way flow and complete membrane filtration operation.During full tube side flow, feed liquid lateral pressure is all big
In filtered solution lateral pressure, hollow fiber internal pressure film is whole all in filtration condition.
During actual membrane filtration operation, all it can lead to being remarkably decreased for membrane flux because of the generation of fouling membrane.Especially
When being that membrane filtration technique is used for the dense viscous high pollution material systems such as biochemical fermentation liquid, the pollution of hollow fiber film close to inlet is asked
Topic is serious, the filter efficiency decline of membrane separation device, or even can make membrane filtration processes that can not be normally carried out.Current solution
It is to extend film filtration time, inefficient operation；Or shut down, after cleaning or replacement membrane module, it is further continued for membrane filtration operation.
Summary of the invention
The purpose of the present invention is to the defect of existing inner pressed hollow-fibre membrane application method, provide a kind of new interior
The application method of pressure type hollow fiber membrane module has the advantages that membrane filtration processes and membrane cleaning process are online simultaneously and carries out, together
When also have the characteristics that simple and easy to do, efficient low-consume.
Realize that the technical solution of the object of the invention is as follows:
A kind of application method of inner pressed hollow fiber film assembly is arranged filtered solution on the outlet line of filtered solution and exports
Pressure-regulating valve, in membrane filtration processes, the filtered solution side outlet pressure value of membrane module is higher than at membrane module concentrated solution outlet
Pressure value, difference are set as 0.02-0.08MPa, so that the film close to concentrated solution outlet end be made to be in back flush state.
Moreover, flow direction periodically reversed of the feed liquid in membrane module tube side.
Moreover, concentrated solution outlet pressure-regulating valve and switch valve are arranged on the pipeline of concentrated solution outlet.
Moreover, adjusting pressure-regulating valve on concentrated solution outlet pipeline makes concentrated solution outlet lateral pressure 0.03-0.05MPa.
Moreover, switch valve is made to open 1~5min in the intermediate period of each film filter cycle, pulse cleaning is realized.
A kind of inner pressed hollow yarn membrane module unit, including membrane module, material fluid bath, pump, pressure-regulating valve, multiple switch
Valve, material fluid bath connect one end of feed pipe, and pump is equipped on feed pipe, and the other end of feed pressure regulating valve, feed pipe connects
Leading to one end of Jie Liang branch feed pipe, the other end of two branch's feed pipes is separately connected the upper port and lower port of membrane module,
Connection upper port branch's feed pipe on install upper feeding switch valve, connection lower port branch's feed pipe on install under into
Expect switch valve, upper port connects one end of top set's concentration liquid pipe, and lower port connects one end of inferior division concentration liquid pipe, at upper point
Concentrate switch valve is installed in branch concentration liquid pipe, concentrate switch valve, top set are dense under installation in inferior division concentration liquid pipe
Contracting liquid pipe connect concentrate general pipeline with the other end of inferior division concentration liquid pipe jointly, and concentrate general pipeline connection material fluid bath is filtering
Filtered solution outlet pressure regulating valve and pressure gauge are installed on the outlet line of liquid.
Moreover, installing concentrated solution outlet pressure-regulating valve and pressure gauge on concentrate general pipeline.
Moreover, film wire is in addition to conventional straight arrangement in the membrane module, using three bursts of plait shape braidings or helical form
The form of distortion is more preferable.It in addition to 1 meter of conventional length, can also lengthen to 2 meters, reduce film device land occupation.
Furthermore, it is possible to improve the inlet pressure of membrane module tube side, film filter efficacy is improved.
The advantages of the present invention:
1, the drawbacks of needing stopper film filtering, offline cleaning the present invention overcomes conventional membrane separation device, has structure letter
Many advantages, such as single, easy to use, film filter efficacy improves.
2, the present invention makes the film mistake that elevated pressures are near the film of entrance end regions by adjusting filtered solution lateral pressure
Filter state, the film near outlet end regions are in back flush state.Exist simultaneously with membrane filtration processes and membrane cleaning process
The advantages of line carries out.Moreover, the effect that backwash restores membrane flux is better than isobaric cleaning, it is possible to improve the filtering of film device
Efficiency.
Detailed description of the invention
Fig. 1 is the first inner pressed hollow yarn membrane module unit schematic diagram of the invention；
Fig. 2 is second of inner pressed hollow yarn membrane module unit schematic diagram of the invention；
Fig. 3 is three strands of woven hollow fiber membrane component diagrams of plait shape；
Fig. 4 is that helical form distorts hollow fiber film assembly schematic diagram；
Fig. 5 is conventional straight arrangement hollow fiber film assembly schematic diagram.
Specific embodiment
The invention will be further described with reference to the accompanying drawing and by specific embodiment, and following embodiment is descriptive
, it is not restrictive, this does not limit the scope of protection of the present invention.
A kind of inner pressed hollow yarn membrane module unit, as shown in Figure 1, including membrane module 18, material fluid bath 1, pump 2, pressure
Regulating valve 3 and 14, multiple switch valve 5,6,7,8 are equipped with pump 2 and charging on the feed pipe of connection material fluid bath and membrane module 18
The other end of pressure-regulating valve 3, feed pipe bifurcates, and is separately connected the upper port and lower port of membrane module 18, in connection upper end
Upper feeding switch valve 5 is installed on branch's feed pipe of mouth, feeds switch valve under installation on branch's feed pipe of connection lower port
6.18 upper port of membrane module connects one end of top set's concentration liquid pipe, and 18 lower port of membrane module connects the one of inferior division concentration liquid pipe
Concentrate switch valve 7 is installed in top set's concentration liquid pipe in end, concentrate switch valve under installing in inferior division concentration liquid pipe
8, top set is concentrated liquid pipe and connect concentrate general pipeline, concentrate general pipeline connection feed liquid jointly with the other end of inferior division concentration liquid pipe
Slot 1 installs filtered solution outlet pressure regulating valve 14 and pressure gauge 13 on the outlet line of 18 filtered solution of membrane module.
Valve 5,6,7,8 is switch valve in figure, can be Hand-operated butterfly valve or ball valve, preferably automatic valve, as pneumatically or electrically
Dynamic ball valve, butterfly valve etc..
Feed liquid passes through 2 adherence pressure of delivery pump from material fluid bath 1, adjusts entering for membrane module 18 by feed pressure regulating valve 3
The value of mouth pressure gauge 4 is 0.05-0.30MPa, passes through the valve 6 of standard-sized sheet first, enters membrane module 18 from the lower mouth 9 of membrane module 18
In, the feed liquid after concentration returns to material fluid bath 1, the filtration of film filtering by the valve 7 of standard-sized sheet from 10 outflow membrane module 18 suitable for reading
Liquid flows out film device from 18 side outlet 11 of membrane module, film filter is discharged using regulating valve 14, valve 5 and 8 is complete at this time
Closed state.
If being not provided with valve 14 and pressure gauge 13.The filtered solution of film filtering is filled from 18 side outlet 11 of membrane module outflow film
It sets, 18 side outlet 11 of membrane module may slightly have without pressure because of the reasons such as film filtered solution export pipeline length, thickness in film device
Low pressure, if test, the reading of general purpose pressure gauge 13 is 0-0.02MPa.In membrane filtration processes, since film concentrate goes out
Mouth valve 7 or 8 is that full-gear is made at 18 concentrated solution outlet of membrane module due to concentrated solution outlet length of pipe, thickness etc.
9 or 10 pressure are 0-0.02MPa.The reading value of pressure gauge 13 is concentrated than membrane module 18 in the aperture of control valve 14 of the present invention
The pressure value of liquid delivery gauge 17 high 0.02-0.08MPa, preferably 0.03-0.05.
When membrane separation device filtering is run after a certain period of time, as fouling membrane aggravates, the filtered solution flux of membrane separation device
When being substantially reduced, flow direction of the feed liquid in membrane tube journey is reversed, that is, standard-sized sheet valve 5 and 8, fully closed valve 6 and 7.This
When, feed liquid passes through the valve 5 of standard-sized sheet, enters in membrane module 18 from membrane module 18 suitable for reading 10, the feed liquid after concentration is flowed out from lower mouth 9
Membrane module 18 returns to material fluid bath 1 by the valve 8 of standard-sized sheet, and the filtered solution of film filtering is still flowed from 18 side outlet 11 of membrane module
Out, film filter is discharged using regulating valve 14, valve 6 and 7 is full-shut position at this time.It maintains operation after a certain period of time, leads to
The switching of opening and closing again for crossing valve 5,6,7,8, reverses feed liquid again in membrane tube journey flow direction.From there through valve 5,6,7,
8 periodical opening and closing switching, is finally completed the membrane filtration operation of feed liquid.When according to film filtering, the decline of practical filtered solution flux
Speed, come determine feed liquid flow direction turn-around period, turn-around period of the invention is generally 10-60 minutes.Valve 5,6,
7,8 periodical opening and closing switching, can be automatically brought into operation by process controls such as PLC, can also be manually operated.Valve in figure
Door 12 is the low level exhaust-valve of film device, and film is in close state when filtering.
The present invention is newly-increased provided with pressure gauge 13 and regulating valve 14 in film device filtered solution export pipeline, filtered in film
Cheng Zhong makes 13 reading value 0.02-0.08MPa of filtered solution pressure gauge, preferably 0.03-0.05 by regulating valve 14.In this way, working as
Feed liquid enters from 18 lower port 9 of membrane module, when upper port 10 flows out, because the transmembrane pressure that feed liquid enters end regions is larger, makes to lean on
The film wire of nearly entrance end regions is in the film filtration condition of elevated pressures.The damage of the pressure as caused by feed liquid flow resistance in film
It loses, the transmembrane pressure of the film wire far from arrival end (i.e. close to outlet end) can be made to be gradually reduced；It is used at 18 side port 11 of membrane module
After valve 14 adjusts the pressure that the reading of pressure gauge 13 is 0.02-0.08MPa, since filtered solution lateral pressure can be greater than in membrane module 18
Outlet pressure is concentrated in 18 feed liquid of membrane module, and the film wire transmembrane pressure close to hollow-fibre membrane outlet end in this way is negative value, so,
Film near outlet end is actually not to be in film filtration condition, but be successively in backwash, isobaric flushing and minute-pressure state.
That is, being in the film filtration condition of elevated pressures near the film of entrance end regions, it is in reversed near the film of outlet end regions
Flushing state.After the flow direction of feed liquid is reversed, the input end of hollow-fibre membrane and outlet end are exchanged, also due to membrane module
Filtered solution lateral pressure can be greater than feed liquid outlet pressure is concentrated in 18, then, the top film wire of the membrane module 18 of rigid backwash into
Enter film filtration condition, the lower part film wire of fouling membrane most serious then enters backwash state.It is former by the periodical reversal of direction of flow of feed liquid
The film wire of film filtration condition in elevated pressures is placed in back flush state, and original place is set in the film wire of back flush state
In the film filtration condition of elevated pressures.That is, the entrance area of fouling membrane weight is in the best backwash state of cleaning effect, fouling membrane
Secondary critical regions are in isobaric cleaning state.
Existing knowledge, the effect that backwash restores membrane flux are better than isobaric cleaning, it is possible to improve the filtering of film device
Efficiency.If 14 aperture of regulating valve is too small, filtered solution pressure gauge 13 reads excessive, then can make the film wire in film filtration condition
Transmembrane pressure reduces, while backwash can reduce the practical filtrable volume of filtered solution, then can reduce the filter efficacy of film device entirety, because
This, will adjust the pressure value of suitable filtered solution pressure gauge 13 according to the practical pollution condition of feed liquid.Can be manual, it can also be with
Preset pressure value is automatically adjusted by pneumatically or electrically flowing mode.
Membrane module application method of the invention, be the every work of membrane module after a certain period of time, utilize design feed liquid flow direction
Reverse system makes the feed liquid reverse flow in membrane module, keeps membrane filtration processes and Membrane cleaning (backwash is cleaned with equipressure) process same
Shi Jinhang, that is, a part of membrane module is in film filtration condition, while another part of membrane module is in backwash and equipressure is clear
Wash state.More serious, lasting work is polluted closer to its end face with the passage of working time in running order film end
The ability of work is poorer；And after the exchange of the material liquid entrance at membrane module both ends, that is, the entrance area of fouling membrane weight is in cleaning
The best backwash state of effect, fouling membrane time critical regions are in isobaric cleaning state, make UF membrane and Membrane cleaning maximum effect
It can be ideal and fully brings into play.The drawbacks of overcoming conventional membrane separation device to need stopper film filtering, offline cleaning, it is bright
It is aobvious that there is many advantages, such as structure is simple, easy to use, film filter efficacy improves.
Since there is certain pressure in filtration side, under the membrane module filter condition for maintaining former transmembrane pressure, film can be improved
The inlet pressure level of component, the i.e. reading of pressure gauge 4, the specific difference of raising can be close to the number of even more than pressure gauge 13
Value, in this way, feed liquid can be improved in the flow velocity of film wire tube side, can be improved feed liquid in the shear velocity of film surface, further decreases
Fouling membrane, simultaneously as feed pressure entrance improves, the inner pressed hollow-fibre membrane group that can be accordingly 1 meter by normal length
Part increases to 1.2-2.0 meters, can reduce the occupied area of per membrane area in this way, improves film device unit occupied area
Processing capacity.
Such as Fig. 1, in all membrane filtration process figures of the invention, it is only schematically drawn 1 membrane module, is filtered according to actual membrane
The demand for the treatment of capacity, in a conventional manner, more membrane modules of laid out in parallel constitute film device.
Valve converting system of the invention can use the loop control of time relay sequence, can be using PLC programming control
System, can also adopt and computerized control.Pump 2 of the present invention, either common centrifugal water pump, is also possible to frequency conversion tune
Fast water pump, the pressure to ensure film separation system is stable and meets the quality requirement of real work.
The present invention devises another membrane filtration process and its membrane separation device (referring to fig. 2) in turn.It is dense to add feed liquid
Contracting liquid index combustion fan 15, switch valve 16 and pressure gauge 17.Switch valve 16 can be Hand-operated butterfly valve or ball valve, preferably automatically
Valve, such as ball valve, butterfly valve pneumatically or electrically.Can be manual, preset pressure can also be automatically adjusted by pneumatically or electrically flowing mode
Value.
Made in membrane filtration processes by newly establishing feed liquid concentrated solution outlet regulating valve 15, switch valve 16 and pressure gauge 17
Membrane module concentrated solution outlet side also keeps certain pressure.Valve 16 is set in the intermediate period in each reversal of direction of flow period, entirely
It opens 1-5 minutes, forms the pulse of feed liquid, with flux depression caused by decelerating membrane pollution.Such as when turn-around period be 14 minutes,
16 standard-sized sheet of valve 1 minute, just refers to, when feed liquid runs to the 7th minute in a manner of bottom in and top out, 16 standard-sized sheet of valve 1 minute, so
After close, etc. feed liquids reverse be upper entering and lower leaving mode, when running to the 7th minute, 16 standard-sized sheet of valve 1 minute is then shut off.
The aperture for adjusting return valve 15, making the reading of pressure gauge 17 is 0.03-0.05MPa, adjusts the aperture of valve 14, makes to press
The reading of power table 13 is higher than the reading value 0.01-0.05MPa of pressure gauge 17, and when ensureing 16 contract fully of valve, membrane module has one
End is still in backwash state.When 16 standard-sized sheet of valve, the effect of pulse cleaning is realized in feed liquid concentration outlet pressure release.
Embodiment 1
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 3 (specification for),
Using 10 film wires as 1 strand, 3 strands of film wire plait shapes are woven into small film wire beam, multiple film wire Shu Pingzhi arrange,
Constitute whole film wires in membrane module.The internal diameter of press mold is 0.80mm in polyvinylidene fluoride hollow fiber.14 membrane modules arranged side by side,
Constitute film device.The concentration of amino acid fermentation liquid is used for using membrane separation device shown in FIG. 1.The wet bacterium weight of fermented liquid
43g/L handles fermentation liquid 5.3m3.The pressure value for adjusting inlet pressure gauge 4 is 0.10 MPa, and control valve 14 makes pressure gauge 13
Pressure be 0.030MPa.It is 20 minutes that feed liquid, which is arranged, to flow to turn-around period by PLC, is concentrated.After 42 minutes, fermentation liquid
Cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
Embodiment 2
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 4 (specification for), it will
The distortion of film wire one-piece auger shape, is fitted into membrane module shell, is prepared into membrane module, and wherein h is 10 centimetres.14 film groups arranged side by side
Part constitutes film device.The concentration of amino acid fermentation liquid is used for using membrane separation device shown in FIG. 1.The wet bacterium of fermented liquid
Weight 43g/L, handles fermentation liquid 5.3m3.The pressure value for adjusting inlet pressure gauge 4 is 0.10 MPa, and control valve 14 makes pressure gauge
13 pressure is 0.030MPa.It is 20 minutes that feed liquid, which is arranged, to flow to turn-around period by PLC, is concentrated.After 51 minutes, fermentation
Liquid cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
Comparative example 1,
Use conventional structure shown in fig. 5 inner pressed Pvdf Microporous Hollow Fiber Membrane component (specification for), 14 membrane modules arranged side by side constitute film device.Amino acid fermentation is used for using membrane separation device shown in FIG. 1
The concentration of liquid.The wet bacterium weight 43g/L of fermented liquid, handles fermentation liquid 5.3m3.Adjustment inlet pressure gauge 4 pressure value be
0.10 MPa cancels setting valve 14.It is 20 minutes that feed liquid, which is arranged, to flow to turn-around period by PLC, is concentrated.86 minutes
Afterwards, fermentation liquid cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
Embodiment 3
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 3 (specification for), side by side
14 membrane modules constitute film device.The concentration of amino acid fermentation liquid is used for using membrane separation device shown in FIG. 1.Fermentation liquid
The wet bacterium weight 43g/L of body, handles fermentation liquid 5.3m3.The pressure value for adjusting inlet pressure gauge 4 is 0.3 MPa, and control valve 14 makes
The pressure of pressure gauge 13 is 0.030MPa.It is 14 minutes that feed liquid, which is arranged, to flow to turn-around period by PLC, is concentrated.35 minutes
Afterwards, fermentation liquid cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
Embodiment 4
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 3 (membrane module diameter still for), length is normal
Rule are 1 meter long, and can increase is 1.5 meters, 14 membrane modules arranged side by side, constitute film device.Using membrane separation device shown in FIG. 1
Concentration for amino acid fermentation liquid.The wet bacterium weight 43g/L of fermented liquid, handles fermentation liquid 5.3m3.Adjust inlet pressure gauge
4 pressure value is 0.25 MPa, and control valve 14 makes the pressure 0.030MPa of pressure gauge 13.Feed liquid is arranged by PLC to flow to
Turn-around period is 14 minutes, is concentrated.After 16 minutes, fermentation liquid cycles of concentration has reached 12 times；Wet bacterium has weighed dense
Contracting requires.
Embodiment 5
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 3 (specification for), side by side
14 membrane modules constitute film device.The concentration of amino acid fermentation liquid is used for using membrane separation device shown in Fig. 2.Fermentation liquid
The wet bacterium weight 43g/L of body, handles fermentation liquid 5.3m3.The pressure value for adjusting inlet pressure gauge 4 is 0.18 MPa, control valve 15
Make the pressure 0.030MPa of pressure gauge 17, control valve 14 makes the pressure 0.050MPa of pressure gauge 13.It is arranged by PLC and is expected
Liquid stream is 30 minutes to turn-around period, and setting valve 16 is standard-sized sheet 2 minutes the 14th minute started in each period, is concentrated.
After 31 minutes, fermentation liquid cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
Embodiment 6
Use inner pressed Pvdf Microporous Hollow Fiber Membrane component shown in Fig. 3 (specification for), side by side
14 membrane modules constitute film device.The concentration of amino acid fermentation liquid is used for using membrane separation device shown in Fig. 2.Fermentation liquid
The wet bacterium weight 43g/L of body, handles fermentation liquid 5.3m3.The pressure value for adjusting inlet pressure gauge 4 is 0.20 MPa, control valve 15
Make the pressure 0.030MPa of pressure gauge 17,13 setting value of pressure gauge is 0.05MPa.By PLC, feed liquid reversal of direction of flow week is set
Phase is 60 minutes, and setting valve 16 is standard-sized sheet 5 minutes the 28th minute started in each period, is concentrated.After 33 minutes, fermentation
Liquid cycles of concentration has reached 12 times；Wet bacterium has weighed to be concentrated and require.
What has been described above is only a preferred embodiment of the present invention, it is noted that for those of ordinary skill in the art
For, under the premise of not departing from inventive concept, various modifications and improvements can be made, these belong to protection of the invention
Range.
Claims (9)
1. a kind of application method of inner pressed hollow fiber film assembly, it is characterised in that: be arranged on the outlet line of filtered solution
Filtered solution outlet pressure regulating valve, in membrane filtration processes, adjusting pressure-regulating valve makes filtered solution lateral pressure be greater than concentrated solution outlet
Locate pressure, so that the film close to concentrated solution outlet end be made to be in back flush state.
2. application method according to claim 1, it is characterised in that: flow direction of the feed liquid in membrane tube journey is periodically inverse
Turn.
3. application method according to claim 1, it is characterised in that: it is dense that the filtered solution lateral pressure of membrane module is higher than membrane module
Contracting liquid exit pressure levels 0.02-0.08MPa.
4. application method according to claim 1 or 2 or 3, it is characterised in that: be arranged on the pipeline of concentrated solution outlet dense
Contracting liquid outlet pressure regulating valve and switch valve.
5. application method according to claim 4, it is characterised in that: adjusting pressure-regulating valve on concentrated solution outlet pipeline makes
Concentrated solution outlet lateral pressure is 0.03-0.05MPa.
6. application method according to claim 4, it is characterised in that: make switch valve when film filters the centre in each period
1~5min of Duan Kaiqi realizes pulse cleaning.
7. a kind of device for the application method for realizing inner pressed hollow fiber film assembly described in claim 1, it is characterised in that:
Including membrane module, material fluid bath, pump, pressure-regulating valve, multiple switch valve, material fluid bath connects one end of feed pipe, on feed pipe
Pump, feed pressure regulating valve, one end of other end connection two branch's feed pipes of connection of feed pipe, two branch's feed pipes are installed
The other end be separately connected the upper port and lower port of membrane module, installation upper feeding is opened on branch's feed pipe of connection upper port
It closes valve, feed switch valve under installation on branch's feed pipe of connection lower port, upper port connects the one of top set's concentration liquid pipe
End, lower port connect one end of inferior division concentration liquid pipe, concentrate switch valve are installed in top set's concentration liquid pipe, at lower point
Branch, which is concentrated in liquid pipe, installs lower concentrate switch valve, and top set is concentrated liquid pipe and connect jointly with the other end of inferior division concentration liquid pipe
Concentrate general pipeline, concentrate general pipeline connection material fluid bath install filtered solution outlet pressure regulating valve on the outlet line of filtered solution
And pressure gauge.
8. device according to claim 7, it is characterised in that: install concentrated solution outlet pressure on concentrate general pipeline and adjust
Valve and pressure gauge.
9. device according to claim 7 or 8, it is characterised in that: film wire uses three strands of plait shape in the membrane module
Braiding or torsive form.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111111451A (en) * | 2020-01-17 | 2020-05-08 | 吕剑阳 | Reduced pressure multi-effect membrane distillation method and device thereof |
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