CN106310948A - Reduced-pressure ultrafiltration membrane distillation device and reduced-pressure ultrafiltration membrane distillation method - Google Patents
Reduced-pressure ultrafiltration membrane distillation device and reduced-pressure ultrafiltration membrane distillation method Download PDFInfo
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- CN106310948A CN106310948A CN201510386054.0A CN201510386054A CN106310948A CN 106310948 A CN106310948 A CN 106310948A CN 201510386054 A CN201510386054 A CN 201510386054A CN 106310948 A CN106310948 A CN 106310948A
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Abstract
The invention provides a reduced-pressure ultrafiltration membrane distillation device and a reduced-pressure ultrafiltration membrane distillation method. According to the device, a raw material liquid tank is connected with an ultrafiltration membrane assembly; an un-evaporated clear liquid outlet of the ultrafiltration membrane assembly is connected with a concentrated water collection tank; a distillation steam outlet of the ultrafiltration membrane assembly is connected with an external condenser; the external condenser is connected with a membrane distillation produced water collection tank; and the membrane distillation produced water collection tank is connected with a vacuum pump. The method comprises the following steps: the vacuum pump is started; under the effect of the vacuum pump, raw material liquid enters the ultrafiltration membrane assembly, and is subjected to ultrafiltration membrane filtration; evaporated steam enters the condenser through the membrane distillation steam outlet of the ultrafiltration membrane assembly; condensed membrane distillation produced water flows into the membrane distillation produced water collection tank; un-evaporated clear liquid flows into the concentrated water collection tank; and the concentrated water is discharged when reaches a certain volume. According to the invention, gas-liquid separation is realized with membrane module shell pass or tube pass space and with the effect of natural gravity, such that membrane distillation produced water with ultra-low conductivity is adopted. With the method, a hydrophobic membrane hydrophobic leakage problem can be avoided, and a high-efficiency membrane distillation process can be realized.
Description
Technical field
The present invention relates to high salinity waste water process, chemical industry and the membrane separation technique of medicine concentrating and separating, especially relate to
And a kind of decompression ultrafilter membrane distilling apparatus and method thereof.
Background technology
Film distillation technology is one of focus of technical field of membrane research in recent years, compares with common vaporizer,
One feature the most significant of Membrane Materials is that the disengagement area of unit volume is big, thus device can be made often
Pressure, lower temperature evaporation process in run efficiently, and the vapor phase space needed for distillation procedure is the least.
Compared with reverse osmosis, Membrane Materials is thermal drivers process, and operation pressure is low, therefore wants film mechanical performance
Asking low, cost of equipment is the lowest, and the safety of separation process is improved, and, the desalination of Membrane Materials
Rate is high, and fouling membrane degree is low.
The distillation of existing conventional film is with hydrophobic membrane as separating medium, drives with film both sides vapor pressure differential for mass transfer
Power, the membrane separating process with diabatic process as major control factors.Steam pressure difference in hydrophobic membrane both sides
Driving under, water vapour from heated material liquid side through be condensed into again after hydrophobic membrane liquid point
From process.Owing to the hydrophobicity of film, only water vapour can pass through fenestra, liquid water and be dissolved in raw material
The Nonvolatile solute of liquid cannot pass fenestra, so can be to ion, divide greatly on Membrane Materials procedural theory
Son, colloid, cell and other non-volatile matter realize the removing of 100%.Existing film distillation technology includes decompression
Membrane Materials, air gap membrane distillation, gas sweep Membrane Materials, the distillation of direct contact membranes and absorbing film distillation.Wherein subtract
Press mold distillation has the flux of membrane distillation of maximum and minimum product water conductivity.
Film distillation technology also exists many key issues at present, and the first is existing due to inevitable fouling membrane
As, during Membrane Materials, there is the hydrophiling seepage of unavoidable hydrophobic membrane；The two of key issue are
Owing to hydrophobic membrane prepares the restriction of materials and methods, flux of membrane distillation is the most relatively low with film mechanical strength, therefore,
This is the problem that film distillation technology realizes that industrial applications must solve.
Summary of the invention
Present invention is primarily targeted at the problems referred to above overcoming existing film distillation technology to exist, and provide one
Planting decompression ultrafilter membrane distilling apparatus and method thereof, use ultrafilter membrane as material liquid distribution mechanism, passing through should
The material liquid of ultrafilter membrane, is uniformly distributed on this ultrafilter membrane opposite side surface, and a part is under vacuum pump pressure
The lower evaporation of effect, the steam of evaporation draws membrane module from hyperfiltration membrane assembly upper port, unevaporated material liquid,
Then under natural gravity effect, downwardly flow along ultrafilter membrane, do not evaporate purified liquor outlet stream from membrane module
Go out membrane module, it is achieved gas-liquid separation.
It is an object of the invention to be realized by techniques below scheme.
The present invention reduces pressure ultrafilter membrane distilling apparatus, it is characterised in that: pipeline is passed through in the outlet of raw material liquid trough 11
Be connected with shell side or the tube side of hyperfiltration membrane assembly 13, this hyperfiltration membrane assembly 13 do not evaporate purified liquor outlet
15 are connected with dense water collecting groove 16 by pipeline, and hyperfiltration membrane assembly 13 distills steam (vapor) outlet 17 and passes through pipeline
Being connected with the import of external condenser 18, the outlet of this external condenser 18 produces water by pipeline with Membrane Materials
Collecting tank 19 connects, and this Membrane Materials is produced water collecting groove 19 and is connected with vacuum pump 20 by pipeline；This raw material
The pipeline that liquid bath 11 is connected with hyperfiltration membrane assembly 13 shell side or tube side is provided with feed control valve 12,
The pipeline that the outlet of this hyperfiltration membrane assembly 13 second connects is provided with cleaning dump valve 14；This external condenser
18 housings are provided with cooling water inlet 22 and coolant outlet 23；This hyperfiltration membrane assembly 13 distills steam and goes out
Mouthfuls 17 vertical pipeline section height h being connected pipeline with external condenser 18 are 15 to 30cm.
Aforesaid decompression ultrafilter membrane distilling apparatus, wherein the separation aperture of ultrafilter membrane is 0.01 to 2.0 μm,
The version of hyperfiltration membrane assembly is conventional hollow fiber type, tubular type, plate and frame or rolling.
The present invention reduces pressure the using method of ultrafilter membrane distilling apparatus, it is characterised in that: comprise the following steps:
(1) close the cleaning dump valve 14 of hyperfiltration membrane assembly 12, start vacuum pump 20；
(2) the pyrogen feed liquid in raw material liquid trough 11, under the negative pressure-pumping of vacuum pump 20, through charging
Control in tube side or the shell side of the material liquid flow-control entrance hyperfiltration membrane assembly 13 of valve 12, through super
After filter membrane remove impurity is filtered, through the clear liquid NATURAL DISTRIBUTION of ultrafilter membrane at ultrafilter membrane outer surface；
(3) under the swabbing action of vacuum pump 20, part clear liquid evaporates, and water vapour is from hyperfiltration membrane assembly
13 Membrane Materials steam (vapor) outlets 17, after one section of vertical tube completes gas-liquid separation, enter external condenser 18
In, condensed Membrane Materials produces water and flows in Membrane Materials product water collecting groove 19；
(4) unevaporated clear liquid in hyperfiltration membrane assembly 13, under gravity, along ultrafilter membrane appearance
Towards dirty, then do not evaporate purified liquor outlet 15 from hyperfiltration membrane assembly 13 and flow into dense water collecting groove 16；
(5) enter after the dense water in dense water collecting groove (16) reaches certain volume and discharge.
The present invention reduces pressure ultrafilter membrane distilling apparatus, it is characterised in that: pipeline is passed through in the outlet of raw material liquid trough 11
Being connected with circulating water chennel 26 first water inlet 261, the outlet of this circulating water chennel 26 is by pipeline and ultrafiltration
Membrane module 13 shell side or tube side connect, and the material liquid not passing through ultrafilter membrane of this hyperfiltration membrane assembly 13 goes out
Mouth 140 is connected with circulating water chennel 26 second water inlet 262 by pipeline, and hyperfiltration membrane assembly 13 distillation is steamed
Vapor outlet 17 is connected with the import of external condenser 18 by pipeline, hyperfiltration membrane assembly 13 do not evaporate clear liquid
Outlet 15 is connected with circulating water chennel 26 the 3rd water inlet 263 by pipeline, going out of this external condenser 18
Mouth produces water collecting groove 19 by pipeline with Membrane Materials and is connected, and this Membrane Materials produces water collecting groove 19 and passes through pipeline
It is connected with vacuum pump 20；Set on the pipeline that this raw material liquid trough 11 is connected with circulating water chennel 26 first water inlet
Having feed control valve 12, the outlet of this circulating water chennel 26 is connected with hyperfiltration membrane assembly 13 shell side or tube side
Pipeline on be sequentially provided with circular flow control valve 25 and water circulating pump 24；This external condenser 18 housing
It is provided with cooling water inlet 22 and coolant outlet 23；This hyperfiltration membrane assembly distillation steam (vapor) outlet 17 is with outer
Connect condenser 18 connecting the vertical pipeline section height h of pipeline is 15 to 30cm.
Aforesaid decompression ultrafilter membrane distilling apparatus, wherein the separation aperture of ultrafilter membrane is 0.01 to 2.0 μm,
The version of hyperfiltration membrane assembly is conventional hollow fiber type, tubular type, plate and frame or rolling.
The present invention reduces pressure the using method of ultrafilter membrane distilling apparatus, it is characterised in that comprise the following steps:
(1) starting vacuum pump 20, the pyrogen feed liquid in raw material liquid trough 11, in the negative pressure of vacuum pump 20
Under suction, control material liquid flow through feed control valve 12, enter circulating water chennel 26；
(2) starting water circulating pump 24, the material liquid entering circulating water chennel 26 drives at water circulating pump 24
Under, by circular flow control valve 25, enter in tube side or the shell side of hyperfiltration membrane assembly 13, through ultrafiltration
After film remove impurity is filtered, through the clear liquid NATURAL DISTRIBUTION of ultrafilter membrane at the outer surface of ultrafilter membrane；
(3) under the swabbing action of vacuum pump 20, part clear liquid evaporates, and water vapour is from hyperfiltration membrane assembly
The Membrane Materials steam (vapor) outlet 17 of 13, is that the vertical pipeline section of 15 to 30cm completes gas-liquid through one section of height h
After separation, enter in condenser 18；
(4) during in condenser 18, condensed Membrane Materials produces water inflow Membrane Materials product water collecting groove 19；
(5) unevaporated clear liquid, under gravity, downwardly flows along ultrafilter membrane, then from
Hyperfiltration membrane assembly 13 do not evaporate purified liquor outlet 15, flow back in circulating water chennel 26；
(6) not through the material liquid of ultrafilter membrane from this hyperfiltration membrane assembly 13 not through ultrafilter membrane material liquid
Outlet 140 is in pipeline is back to circulating water chennel 26.
The present invention reduces pressure ultrafilter membrane distilling apparatus and method is noteworthy characterized by: do not use hydrophobic membrane conduct
Gas-liquid separation medium, changes into using water penetration ultrafilter membrane as material liquid distribution mechanism.This ultrafilter membrane has
Water permeability, because the disengagement area that water penetration ultrafilter membrane is provided is more than the actual gas-to-liquid contact in fenestra road
Interfacial area, compared with hydrophobic membrane, has the advantages that disengagement area in unit volume is bigger；Utilize film
Assembly shell side space and natural gravity effect, it is achieved gas-liquid separation, can obtain the Membrane Materials of low conductivity
Produce water；Evaporation process is to be not dependent on fenestra passage on the surface separating film, thus can prepare low hole
Gap rate and the film of small-bore, can obtain the film of more high mechanical properties accordingly；Owing to the machine of film can be improved
Tool intensity, thus thinner film can be prepared, improve carrying of the heat conductivility of film, beneficially evaporating temperature
High；Carry out mass transfer without vapour transmission fenestra, thus reduce resistance of gas mass transfer；Hydrophobic because not using
Film, avoids the hydrophiling leakage problems of hydrophobic membrane accordingly.So can realize efficient film distillation mistake
Journey.
The method is by membrane technology and the film distillation technology that Conventional espresso technology is combined equally, make use of separation
The advantage that film gas-liquid contact area is big, sweeps film steam compared to existing pressure reducing film distillation, air gap membrane distillation, gas
Evaporate, direct contact membranes distills and absorbing film distillation, and the decompression ultrafilter membrane distillation that the present invention proposes is the highest
The film distillation technology of effect.
Different according to the mode being embodied as, can there be decompression ultrafilter membrane distillation, i.e. passing through at ultrafilter membrane
Side applies negative pressure, is retracted to enter in the condenser outside membrane module by the water vapour evaporated at ultrafiltration membrane surface
Row condensation liquefaction；Can have gas sweep formula ultrafilter membrane distillation, i.e. ultrafilter membrane through side apply purge gas,
The water vapour evaporated at ultrafiltration membrane surface is blown out in the condenser outside membrane module carry out condensation liquefaction,
Etc..
Accompanying drawing explanation
Fig. 1 is that existing hydrophobic membrane distillation gas-liquid contact surface implements view.In figure 1 be pyrogen feed liquid,
2 it is hydrophobic membrane material, 3 is the gas-to-liquid contact face of hydrophobic fenestra.
Fig. 2 be the present invention reduce pressure ultrafilter membrane distilling apparatus implement view.In figure, 1 is pyrogen feed liquid,
4 is ultrafilter membrane, and 5 is the surface liquid film of ultrafilter membrane.
Fig. 3 is that the present invention ultrafilter membrane distilling apparatus structure one that reduces pressure implements illustration.In figure 11 be raw material liquid trough,
12 be feed control valve, 13 be hyperfiltration membrane assembly, 14 for cleaning dump valve, 15 not steaming for membrane module
Send out purified liquor outlet, 16 be dense water collecting groove, 17 for membrane module Membrane Materials steam (vapor) outlet, 18 be external condensation
Device, 19 be Membrane Materials produce water collecting groove, 20 be the vacuum pump of negative pressure is provided, 22 be the cooling water of condenser
Import, 23 be the coolant outlet of condenser, h be hanging down of membrane module shell side upper end Membrane Materials steam (vapor) outlet
Straight tube height.
Fig. 4 be the present invention reduce pressure ultrafilter membrane distilling apparatus structure another implement illustration.In figure, 11 is material liquid
Groove, 12 be inlet control valve, 13 for hyperfiltration membrane assembly, 140 for hyperfiltration membrane assembly through ultrafilter membrane not former
Material liquid outlet, 15 for membrane module do not evaporate purified liquor outlet, 17 be membrane module Membrane Materials steam (vapor) outlet, 18 be
External condenser, 19 be Membrane Materials produce water collecting groove, 20 be the vacuum pump of negative pressure is provided, 22 be condenser
Cooling water inlet, 23 be the coolant outlet of condenser, 24 be water circulating pump, 25 for circular flow control
Valve processed, 26 it is circulating water chennel, 261 first water inlets, 262 second water inlets, 263 the 3rd water inlets.
Detailed description of the invention
As it is shown in figure 1, use the Membrane Materials process of conventional hydrophobic membrane, its disengagement area and hydrophobic membrane surface
Perforate situation closely related, owing to film-forming method is limited with membrane material strength problem, constrain in Fig. 1
The raising of the gas liquid interfacial area in the gas-to-liquid contact face 3 of hydrophobic fenestra.
As in figure 2 it is shown, use the ultrafilter membrane distillating method of the present invention, material liquid 1 will pass through ultrafilter membrane
4, the opposite side at ultrafilter membrane flows down naturally due to action of gravity, forms one on the surface of ultrafilter membrane simultaneously
The liquid film 5 that layer thickness is controlled.This has the ultrafilter membrane 4 distribution mechanism as material liquid 1 of water permeability,
The boil-off gas liquid interface of material liquid 1 is provided, utilizes membrane module shell side space and natural gravity effect, water
Steam rises, and unevaporated material liquid flows downward as dense water, it is achieved gas-liquid separation.
Due to percent opening and the restriction of strength problem of masking, in Fig. 1, the surface area in gas-to-liquid contact face 3 is remote
Surface area less than liquid film in Fig. 25；Evaporation process is to be not dependent on fenestra lead on the surface separating film
Road, thus the film of low porosity and small-bore can be prepared, the film of more high mechanical properties can be obtained accordingly；
Owing to the mechanical strength of film can be improved, thus thinner film can be prepared, improve the heat conductivility of film,
Be conducive to the raising of evaporating temperature；Existing film distillation technology, is all that steam permeable membrane hole carries out mass transfer,
Flux of membrane distillation is inversely proportional to the thickness of film, and ultrafilter membrane still-process carries out mass transfer without vapour transmission fenestra,
Thus reduce resistance of gas mass transfer；Due to not against ultrafilter membrane as gas-liquid spacer medium, thus do not deposit
Fenestra moistening leakage problems in hydrophobic membrane.So can realize efficient film distillation process.Ultrafilter membrane
Function as material liquid distribution mechanism, for material liquid provide greater area of gas-liquid evaporation boundary.
As it is shown on figure 3, the decompression ultrafilter membrane distillating method of the present invention is, close the clear of hyperfiltration membrane assembly 12
Wash dump valve 14, startup vacuum pump 20: the pyrogen feed liquid in raw material liquid trough 11, bearing at vacuum pump 20
Under pressure suction, through the material liquid flow-control of feed control valve 12, enter ultrafilter membrane by certain flow
In the tube side of assembly 13, after ultrafilter membrane remove impurity is filtered, through the clear liquid NATURAL DISTRIBUTION of ultrafilter membrane in ultrafiltration
The outer surface of film；Under the swabbing action of vacuum pump 20, part clear liquid evaporates, and water vapour is from ultrafilter membrane group
Part 13 shell side upper end Membrane Materials steam (vapor) outlet 17, has the vertical pipeline section h of enough height through one section, complete
After becoming gas-liquid separation, entering in external condenser 18, condensed Membrane Materials produces water and flows into Membrane Materials product water
In collecting tank 19, the height of vertical pipeline section is 20cm；Unevaporated clear liquid, under gravity, along super
Filter membrane downwardly flows, and then flows into dense water collect from hyperfiltration membrane assembly 13 shell side lower end outlet 15
In groove 16, enter after the dense water in dense water collecting groove 16 reaches certain volume and discharge.Cooling water is from cooling
Water inlet 22 enters condenser 18, then discharges from the coolant outlet 23 of condenser 18.
Material liquid can control to be upwardly into ultrafiltration from hyperfiltration membrane assembly 13 bottom through feed control valve 12
In the tube side of membrane module 13, it is also possible to be upwardly into hyperfiltration membrane assembly 13 from hyperfiltration membrane assembly 13 bottom
In shell side, it is also possible to be downwardly into the tube side of hyperfiltration membrane assembly 13 from hyperfiltration membrane assembly 13 top, also
Can be downwardly into the shell side of hyperfiltration membrane assembly 13 from hyperfiltration membrane assembly 13 top, concrete stream sets
Put the version according to membrane module such as hollow fiber type, tubular type, plate and frame or rolling, and raw material
Depending on liquid characteristic.
During Membrane Materials, circulated by material liquid, fouling membrane process can be controlled, be conducive to carrying simultaneously
The temperature of high evaporation clear liquid, thus improve flux of membrane distillation.As shown in Figure 4, the decompression ultrafiltration of the present invention
Membrane distillation method is, startup vacuum pump 20: the pyrogen feed liquid in raw material liquid trough 11, at vacuum pump 20
Under negative pressure-pumping, control material liquid flow through feed control valve 12, enter recirculated water by certain flow
Groove 26；Start water circulating pump 24, the first water inlet 261 material liquid entering circulating water chennel 26 is following
Under ring water pump 24 drives, by circular flow control valve 25, hyperfiltration membrane assembly 13 bottom enter ultrafiltration
In the tube side of membrane module 13, after ultrafilter membrane remove impurity is filtered, the clear liquid NATURAL DISTRIBUTION through ultrafilter membrane is surpassing
The outer surface of filter membrane；Under the swabbing action of vacuum pump 20, part clear liquid evaporates, and water vapour is super from being positioned at
The Membrane Materials steam (vapor) outlet 17 of filter membrane component 13 shell side upper end, is the vertical of 15cm through one section of height h
After pipeline section completes gas-liquid separation, entering in condenser 18, condensed Membrane Materials produces water and flows into Membrane Materials product
In water collecting groove 19；Unevaporated clear liquid, under gravity, downwardly flows along ultrafilter membrane, so
After do not evaporate purified liquor outlet 15 from hyperfiltration membrane assembly 13 shell side lower end, the 3rd water inlet 263 flow back to follow
In ring tank 26.Through ultrafilter membrane material liquid from this hyperfiltration membrane assembly 13 not through ultrafilter membrane former
Material liquid outlet 140, through pipeline, is back in circulating water chennel 26 by the second water inlet 262.
Cooling water enters condenser 18 from cooling water inlet 22, then from the coolant outlet of condenser 18
23 discharge.
Equally, the material liquid controlled through controlling valve 12 can enter hyperfiltration membrane assembly 13 from bottom to top
In tube side, it is also possible to enter from bottom to top in the shell side of hyperfiltration membrane assembly 13, it is also possible to enter from the top down
In the tube side of hyperfiltration membrane assembly 13, it is also possible to enter in the shell side of hyperfiltration membrane assembly 13 from the top down, tool
The stream of body arranges version such as hollow fiber type, tubular type, plate and frame or rolling according to membrane module,
And depending on material liquid characteristic.
Owing to needing the outer surface of ultrafilter membrane to provide the disengagement area of material liquid, therefore, making ultrafiltration
During membrane module, need uniformly to arrange ultrafilter membrane, to reduce film outer surface directly connecing each other as far as possible
Touch, in order to avoid loss disengagement area.The pipeline that the Membrane Materials steam (vapor) outlet of membrane module connects must assure that and makes steaming
Vapour vertical ascent has the vertical pipeline section h of enough height, the height of this vertical pipeline section h could be arranged to 10 to
100cm, depends on concrete distillation device structure and membrane module structure configuration, to prevent aerosol from carrying shadow secretly
Ring Membrane Materials and produce the water quality of water, complete gas-liquid separation, of a sufficiently low to ensure Membrane Materials product water conductivity value,
Meet process requirement.It is preferable that the height of this vertical pipeline section h is generally located on 15 to 30cm.
Embodiment 1, uses such as Fig. 3 to reduce pressure ultrafilter membrane distilling apparatus, using tap water as material liquid, from
Under be upwardly in the tube side of hyperfiltration membrane assembly, tap water electrical conductivity is 360 μ S/cm, and tap water temperature is
60 DEG C, by hydrophobic membrane assembly (self-control, code name M-1) conduct after ethanol wet that area is 0.05
Ultrafilter membrane, carries out the ultrafilter membrane still-process that reduces pressure, and the height h arranging vertical pipeline section is 15cm, and vacuum is born
Pressure is 0.089MPa, and the flux of membrane distillation obtained is 15L/ .h, and Membrane Materials produces water conductivity and is
4.2μS/cm。
Comparative example 1, uses conventional vacuum distillation device, equally using tap water as material liquid, from the beginning
Water conductivity is 360 μ S/cm, and tap water temperature is 60 DEG C, and usable floor area is the hydrophobic membrane group of 0.05
Part (self-control, code name M-1) carries out conventional vacuum Membrane Materials process, and negative pressure of vacuum is 0.089MPa,
To flux of membrane distillation be 11L/ .h, Membrane Materials produce water conductivity be 3.2 μ S/cm.
By from the point of view of embodiment 1 and comparative example 1, using a same membrane module, Membrane Materials process is different,
Flux of membrane distillation difference is bigger.
Embodiment 2, uses polysulfone hollow fiber ultrafiltration membrane system (self-control, code name M-2), and remaining condition is with real
Execute example 1.The flux of membrane distillation obtained is 15L/ .h, and it is 4.1 μ S/cm that Membrane Materials produces water conductivity.
The pure water ultrafilter membrane flux of M-1 membrane module is 280L/ [email protected], M-2 membrane module and M-1
The hollow-fibre membrane external surface area of membrane module is identical, and the pure water ultrafilter membrane flux of M-2 membrane module is 1080L/
[email protected], far above M-1 membrane module.Being compared with embodiment 2 by embodiment 1, Membrane Materials leads to
Measure unrelated with the aperture of ultrafilter membrane used and ultra-filtration flux.
Embodiment 3, uses such as Fig. 4 to reduce pressure ultrafilter membrane distilling apparatus, using tap water as material liquid, under
Being upwardly in the tube side of hyperfiltration membrane assembly, tap water electrical conductivity is 360 μ S/cm, and tap water temperature is
60 DEG C, material liquid rate of circulating flow is 0.40m/S.By hydrophobic membrane assembly that area is 0.05 (self-control,
Code name M-1) carry out, as ultrafilter membrane, the ultrafilter membrane still-process that reduces pressure with after ethanol wet, vertical pipeline section is set
Highly h is 15cm, and negative pressure of vacuum is 0.089MPa, and the flux of membrane distillation obtained is 22L/ .h, and film steams
Evaporating product water conductivity is 4.2 μ S/cm.Circulated by material liquid, be conducive to improving the temperature of evaporation clear liquid,
Thus improve flux of membrane distillation.
The content not illustrated in the embodiment of the present invention is prior art, therefore, no longer repeat.
The present invention is to utilize membrane module shell side or tube side space and natural gravity effect, it is achieved gas-liquid is divided
From, the Membrane Materials that can obtain low conductivity produces water.Advantages of the present invention: do not use hydrophobic membrane as gas
Liquid separating medium, is improved to use water penetration ultrafilter membrane as material liquid distribution mechanism, thus avoids thin
The hydrophiling leakage problems of moisture film；Compared with the fenestra road gas-liquid interface of hydrophobic membrane, ultrafilter membrane has bigger
Material liquid disengagement area, thus have bigger flux of membrane distillation；Evaporation process is on the surface separating film
And it is not dependent on fenestra passage, thus the film of low porosity and small-bore can be prepared, can obtain accordingly
The film of more high mechanical properties；Owing to the mechanical strength of film can be improved, thus thinner film can be prepared,
Improve the heat conductivility of film, the beneficially raising of evaporating temperature；Mass transfer is carried out without vapour transmission fenestra,
Thus reduce resistance of gas mass transfer, such that it is able to realize efficient film distillation process.
The above, be only presently preferred embodiments of the present invention, not the present invention is made any in form
Restriction, any simple modification that above example is made by every technical spirit according to the present invention, etc.
With change and modification, all still fall within the range of technical solution of the present invention.
Claims (6)
1. a decompression ultrafilter membrane distilling apparatus, it is characterised in that: the outlet of raw material liquid trough (11) is passed through
Pipeline is connected with shell side or the tube side of hyperfiltration membrane assembly (13), not steaming of this hyperfiltration membrane assembly (13)
Sending out purified liquor outlet (15) to be connected with dense water collecting groove (16) by pipeline, hyperfiltration membrane assembly (13) steams
Evaporate steam (vapor) outlet (17) to be connected with external condenser (18) import by pipeline, this external condenser (18)
Outlet produce water collecting groove (19) by pipeline and Membrane Materials and be connected, this Membrane Materials product water collecting groove (19)
It is connected with vacuum pump (20) by pipeline；This raw material liquid trough (11) and hyperfiltration membrane assembly (13) shell side
Or the pipeline that tube side connects is provided with feed control valve (12), and this hyperfiltration membrane assembly (13) second goes out
The pipeline that mouth connects is provided with cleaning dump valve (14)；This external condenser (18) housing is provided with cooling
Water inlet (22) and coolant outlet (23)；This hyperfiltration membrane assembly (13) distillation steam (vapor) outlet (17)
Vertical pipeline section height (h) being connected pipeline with external condenser (18) is 15 to 30cm.
Decompression ultrafilter membrane distilling apparatus the most according to claim 1, it is characterised in that: described ultrafiltration
The separation aperture of film is 0.01 to 2.0 μm, the version of hyperfiltration membrane assembly be conventional hollow fiber type,
Tubular type, plate and frame or rolling.
3. a using method for decompression ultrafilter membrane distilling apparatus as claimed in claim 1, its feature exists
In: comprise the following steps:
(1) close the cleaning dump valve (14) of hyperfiltration membrane assembly (12), start vacuum pump (20)；
(2) the pyrogen feed liquid in raw material liquid trough (11), under the negative pressure-pumping of vacuum pump (20),
Through feed control valve (12) material liquid flow-control enter hyperfiltration membrane assembly (13) tube side or
In shell side, after ultrafilter membrane remove impurity is filtered, through the clear liquid NATURAL DISTRIBUTION of ultrafilter membrane at ultrafilter membrane outer surface；
(3) under the swabbing action of vacuum pump (20), part clear liquid evaporates, and water vapour is from ultrafilter membrane
Assembly (13) Membrane Materials steam (vapor) outlet (17), after one section of vertical tube completes gas-liquid separation, enters external
In condenser (18), condensed Membrane Materials produces water and flows in Membrane Materials product water collecting groove (19)；
(4) unevaporated clear liquid in hyperfiltration membrane assembly (13), under gravity, along ultrafilter membrane
Downwardly flow, then do not evaporate purified liquor outlet (15) from hyperfiltration membrane assembly (13) and flow into dense water
In collecting tank (16)；
(5) enter after the dense water in dense water collecting groove (16) reaches certain volume and discharge.
4. a decompression ultrafilter membrane distilling apparatus, it is characterised in that: the outlet of raw material liquid trough (11) is passed through
Pipeline is connected with circulating water chennel (26) first water inlet (261), and the outlet of this circulating water chennel (26) is led to
Cross pipeline to be connected with hyperfiltration membrane assembly (13) shell side or tube side, not passing through of this hyperfiltration membrane assembly (13)
Material liquid outlet (140) of ultrafilter membrane is by pipeline with circulating water chennel (26) second water inlet (262) even
Connecing, hyperfiltration membrane assembly (13) distillation steam (vapor) outlet (17) is entered with external condenser (18) by pipeline
Mouth connects, and the purified liquor outlet (15) that do not evaporates of hyperfiltration membrane assembly (13) passes through pipeline and circulating water chennel (26)
3rd water inlet (263) connects, and the outlet of this external condenser (18) produces water by pipeline with Membrane Materials
Collecting tank (19) connects, and this Membrane Materials produces water collecting groove (19) by pipeline with vacuum pump (20) even
Connect；The pipeline that this raw material liquid trough (11) is connected with circulating water chennel (26) first water inlet is provided with charging
Controlling valve (12), this circulating water chennel (26) outlet connects with hyperfiltration membrane assembly (13) shell side or tube side
Circular flow control valve (25) and water circulating pump (24) it is sequentially provided with on the pipeline connect；This external condenser
(18) housing is provided with cooling water inlet (22) and coolant outlet (23)；This hyperfiltration membrane assembly distills
Steam (vapor) outlet (17) be connected with external condenser (18) vertical pipeline section height (h) of pipeline be 15 to
30cm。
Decompression ultrafilter membrane distilling apparatus the most according to claim 4, it is characterised in that: described ultrafiltration
The separation aperture of film is 0.01 to 2.0 μm, the version of hyperfiltration membrane assembly be conventional hollow fiber type,
Tubular type, plate and frame or rolling.
6. the using method of a decompression ultrafilter membrane distilling apparatus as claimed in claim 4, it is characterised in that
Comprise the following steps:
(1) starting vacuum pump (20), the pyrogen feed liquid in raw material liquid trough (11), in vacuum pump (20)
Negative pressure-pumping under, through feed control valve (12) control material liquid flow, enter circulating water chennel (26)；
(2) start water circulating pump (24), enter the material liquid of circulating water chennel (26) in water circulating pump (24)
Under driving, by circular flow control valve (25), enter tube side or the shell side of hyperfiltration membrane assembly (13)
In, after ultrafilter membrane remove impurity is filtered, through the clear liquid NATURAL DISTRIBUTION of ultrafilter membrane at the outer surface of ultrafilter membrane；
(3) under the swabbing action of vacuum pump (20), part clear liquid evaporates, and water vapour is from ultrafilter membrane
The Membrane Materials steam (vapor) outlet (17) of assembly (13), is the vertical tube of 15 to 30cm through one section of height h
After section completes gas-liquid separation, enter in condenser (18)；
(4) in condenser (18), condensed Membrane Materials produces water and flows into Membrane Materials product water collecting groove (19)
In；
(5) unevaporated clear liquid, under gravity, downwardly flows along ultrafilter membrane, then from
Hyperfiltration membrane assembly (13) do not evaporate purified liquor outlet (15), flow back in circulating water chennel (26)；
(6) not through the material liquid of ultrafilter membrane from this hyperfiltration membrane assembly (13) not through ultrafilter membrane raw material
Liquid outlet (140) is in pipeline is back to circulating water chennel (26).
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| CN108636121A (en) * | 2018-06-19 | 2018-10-12 | 南京航空航天大学 | A kind of membrane distillation coupling MVR concentration strong corrosive solution systems and method |
| CN113069926A (en) * | 2021-03-24 | 2021-07-06 | 江苏新宜中澳环境技术有限公司 | System and method for extracting polysaccharide substances in traditional Chinese medicine wastewater |
| CN114101308A (en) * | 2021-11-16 | 2022-03-01 | 安徽省通源环境节能股份有限公司 | System and method for restoring petroleum hydrocarbon polluted soil |
| CN114502259A (en) * | 2019-10-11 | 2022-05-13 | 旭化成株式会社 | Raw material liquid concentration system and concentration device |
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| CN203736968U (en) * | 2014-02-24 | 2014-07-30 | 上海远舰石油技术服务有限公司 | Treatment equipment of inorganic membrane distillation applied to waste oil product |
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| JP2006272135A (en) * | 2005-03-29 | 2006-10-12 | Toray Ind Inc | Membrane separation method and membrane separation device |
| CN203736968U (en) * | 2014-02-24 | 2014-07-30 | 上海远舰石油技术服务有限公司 | Treatment equipment of inorganic membrane distillation applied to waste oil product |
| CN204097225U (en) * | 2014-09-28 | 2015-01-14 | 广东梅雁吉祥水电股份有限公司 | Electronic industry wastewater treatment equipment |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108636121A (en) * | 2018-06-19 | 2018-10-12 | 南京航空航天大学 | A kind of membrane distillation coupling MVR concentration strong corrosive solution systems and method |
| CN114502259A (en) * | 2019-10-11 | 2022-05-13 | 旭化成株式会社 | Raw material liquid concentration system and concentration device |
| CN113069926A (en) * | 2021-03-24 | 2021-07-06 | 江苏新宜中澳环境技术有限公司 | System and method for extracting polysaccharide substances in traditional Chinese medicine wastewater |
| CN114101308A (en) * | 2021-11-16 | 2022-03-01 | 安徽省通源环境节能股份有限公司 | System and method for restoring petroleum hydrocarbon polluted soil |
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Application publication date: 20170111 |