CN106076122B - A kind of parallel multiple-effect vacuum distillation device and method - Google Patents
A kind of parallel multiple-effect vacuum distillation device and method Download PDFInfo
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- CN106076122B CN106076122B CN201610665784.9A CN201610665784A CN106076122B CN 106076122 B CN106076122 B CN 106076122B CN 201610665784 A CN201610665784 A CN 201610665784A CN 106076122 B CN106076122 B CN 106076122B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/364—Membrane distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/366—Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
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Abstract
The invention discloses a kind of parallel multiple-effect vacuum distillation device and methods, belong to membrane distillation field.The low energy consumption device includes n grades of membrane distillation units in parallel, first order material liquid tank, booster pump, hollow fiber film assembly tube side constitute the first closed loop；The tube side of hollow fiber film assembly in the second level to n-th grade constitutes the second to the n-th closed loop with the shell side of prime shell-and-tube heat exchanger, this grade of material liquid tank and booster pump.The shell side of n-th grade of shell-and-tube heat exchanger is connected to cooler.Per in level-one, with the tube side inlet communication of shell-and-tube heat exchanger, the connecting pipeline of booster pump and hollow fiber film assembly is equipped with thermometer for the shell-side outlet and finished product collecting tank of empty fiber membrane component.The tube side outlet of shell-and-tube heat exchanger in the first order to the n-th 1 grades is connected with the tube side import of next stage shell-and-tube heat exchanger again after being connected with the shell-side outlet of next stage hollow fiber film assembly, and the tube side of n-th grade of shell-and-tube heat exchanger is exported to be connect with vacuum pump.
Description
Technical field
The present invention relates to membrane distillation field, more particularly to a kind of parallel multiple-effect vacuum distillation device and method.
Background technology
Vacuum membrane distillation technology is a kind of novel membrane separation technique, based on the hot material liquid of substance to be separated is passed through separation
The side (hot side) of film, and (i.e. inlet side) is vacuumized in the other side of seperation film, it is transmitted to be formed in seperation film both sides
Vapour pressure deficit, the water in hot material liquid form steam, driving of the steam in the transmission vapour pressure deficit after the vaporization of the side of seperation film
It is lower the inlet side of seperation film to be transmitted to by the fenestra of seperation film, and pure water is condensed into inlet side, and then realize
The separation of water and other substances in feed liquid.Wherein, above-mentioned seperation film is mostly with board-like, rolling, tubular type or hollow fiber form film
The form of component exists.Since vacuum membrane distillation is using vacuum system as enhancing driving force, not only there are other membrane distillation skills
The advantages of art, and have many advantages, such as separative efficiency height, membrane flux is big, in sea water desalination, water process, solution concentration, ultra-pure water
Prepare etc. has great application prospect.Based on above-mentioned it is found that providing a kind of vacuum diaphragm steaming for vacuum membrane distillation technology
Distillation unit is very necessary.
The prior art provides such a vacuum membrane distillation device comprising material liquid tank, booster pump, heater, metering
Pump, thermometer, hollow fiber film assembly, condenser pipe, vacuum pump, fresh water collecting bottle, Low Constant Temperature Water Baths.Wherein, material liquid tank, increasing
Press pump, heater, metering pump, thermometer, hollow fiber film assembly tube side be sequentially connected to, the shell side of hollow fiber film assembly,
Shell side, the fresh water collecting bottle of condenser pipe are sequentially connected to, meanwhile, the company between vacuum pump and the shell side and fresh water collecting bottle of condenser
Take over line is connected, meanwhile, the tube side of condenser pipe is connected to Low Constant Temperature Water Baths.Wherein, hollow fiber film assembly includes tubular type
Shell, a plurality of hydrophobic hollow fiber film wire being axially arranged on inside tubular outer shell, and hollow fiber film thread passes through tree
Fat is fixed on the both ends of the tubular outer shell, meanwhile, the both ends of tubular outer shell are respectively arranged with end cap.Wherein, it is arranged on end cap
There is the cap bore being connected with the centre bore of hollow fiber film thread, to cooperatively form the tube side of hollow fiber film assembly, tubular outer shell
The pore being connected with its inner cavity is provided on the outer wall of two close end, to cooperatively form the shell side of hollow fiber film assembly.
The inventor finds that the existing technology has at least the following problems：
Since required energy consumption is mainly the consumed feed liquid sensible heat of evaporation that keeps the skin wet during vacuum membrane distillation, and water
Evaporation latent heat is larger, and the steam that the prior art is obtained after being evaporated come condensed moisture using condensed water needs a large amount of condensed water, makes
It is excessive at its energy consumption.
Invention content
Technical problem to be solved of the embodiment of the present invention is, it is latent to provide a kind of evaporation that can recycle water
Heat effectively reduces the parallel multiple-effect vacuum distillation device and method of its energy consumption.Specific technical solution is as follows：
In a first aspect, an embodiment of the present invention provides a kind of parallel multiple-effect vacuum distillation device, including material liquid tank, increasing
Press pump, vacuum pump, hollow fiber film assembly, finished product collecting tank and thermometer, further, described device further include that shell-and-tube changes
Hot device and cooler, and it is provided with heating rod in the material liquid tank；
One hollow fiber film assembly, a shell-and-tube heat exchanger, a material liquid tank, an increasing
Press pump, a finished product collecting tank cooperation constitute level-one membrane distillation unit, and the membrane distillation unit has been arranged in parallel n
Grade, wherein n are more than or equal to 2；
In membrane distillation unit described in the first order, the material liquid tank, the booster pump, the hollow fiber film assembly tube side
It is sequentially connected to, constitutes the first closed loop；The second level is up to the hollow fiber film assembly in n-th grade of membrane distillation unit
Tube side and prime membrane distillation unit in the shell side of the shell-and-tube heat exchanger, the material liquid tank in this grade of membrane distillation unit
It is sequentially connected to the booster pump, constitutes the second to the n-th closed loop；And the institute in n-th grade of membrane distillation unit
The shell side import and shell-side outlet for stating shell-and-tube heat exchanger are connected to the water outlet of the cooler and water inlet respectively, to constitute
Cooling circuit；
The shell-side outlet of the hollow fiber film assembly in membrane distillation unit described in per level-one and the pipe shell type heat exchange
The tube side import of device is connected；In the first order to (n-1)th grade of membrane distillation unit, the tube side outlet of the shell-and-tube heat exchanger is under
The shell-side outlet of the hollow fiber film assembly in membrane distillation unit described in level-one is steamed with film described in next stage again after being connected
The tube side import for evaporating the shell-and-tube heat exchanger in unit is connected, also, the pipe in n-th grade of membrane distillation unit
The tube side outlet of shell heat exchanger is connect with the vacuum pump；
In membrane distillation unit described in per level-one, the tube side import of the shell-and-tube heat exchanger also connects with the finished product collecting tank
It is logical, meanwhile, the booster pump is provided with the thermometer in the connecting pipeline of the hollow fiber film assembly.
Specifically, preferably, described device further includes filter, the charging in the material liquid tank is arranged in the filter
On pipeline.
Specifically, preferably, described device further includes fixed gas heat exchanger, the fixed gas heat exchanger is arranged n-th
In connecting pipeline between the tube side outlet and the vacuum pump of the shell-and-tube heat exchanger in the grade membrane distillation unit.
Specifically, preferably, described device further includes pressure vacuum gauge, the pressure vacuum gauge setting is not coagulated described
In connecting pipeline between gas heat exchanger and the vacuum pump.
Specifically, preferably, being both provided with flowmeter in the tube side inlet line of the hollow fiber film assembly.
Specifically, preferably, the cooler is water cooler or air cooler.
Specifically, preferably, the shell-and-tube heat exchanger is polymer heat exchanger, the polymer heat exchanger includes pipe
Formula shell, a plurality of polymer heat exchanger tube, end cap；
The polymer heat exchanger tube is in doughnut structure, while tube wall dense non-porous, a plurality of polymer heat exchanger tube
It is axially spaced to be arranged inside the tubular outer shell, and it is fixed on by solidified resin the both ends of the tubular outer shell；
The end cap is removably attached to the both ends of the tubular outer shell, and is provided on the end cap and gathers with described
The cap bore that the central through hole of object heat exchanger tube is connected is closed, to cooperatively form the tube side of the polymer heat exchanger；
The tubular outer shell by two close end outer wall on be respectively arranged be connected with the inner cavity of the tubular outer shell into
Liquid pipe and outlet tube, to cooperatively form the shell side of the polymer heat exchanger.
Preferably, the polymer heat exchanger tube is polyfluortetraethylene pipe, outer diameter 0.5-0.9mm, internal diameter 0.3-
0.5mm。
Second aspect, an embodiment of the present invention provides a kind of method carrying out vacuum membrane distillation using above-mentioned device, institutes
The method of stating includes：
In membrane distillation unit described in per level-one, after feed liquid is heated to predetermined temperature in the material liquid tank, pass through the increasing
It is detached in the tube side that press pump enters in the doughnut membrane distillation component, obtains dope and steam；
For membrane distillation unit described in the first order, the dope by this grade of hollow fiber film assembly tube side according to
It is secondary to enter this grade of material liquid tank and this grade of booster pump, and recycled in first closed loop；For described
For the second level to n-th grade of membrane distillation unit, the dope will enter prime by the tube side of this grade of hollow fiber film assembly
The shell side of the shell-and-tube heat exchanger then sequentially enters this grade of material liquid tank and this grade of booster pump, and described
It is recycled in two to the n-th closed loops, while heat exchange condensation is carried out with the steam in pipe for shell-and-tube exchanger journey described in prime；
Shell side of the steam through this grade of hollow fiber film assembly enters the tube side of this grade of shell-and-tube heat exchanger
Heat exchange condensation is carried out with the dope from hollow fiber film assembly described in next stage in shell side, obtains condensation pure water and by certainly
Gravity flows into this grade of finished product collecting tank；Meanwhile into pipe shell type heat exchange described in n-th grade of membrane distillation unit
The cooling water in the cooler in water vapour and shell side in device tube side carries out heat exchange condensation, obtains condensation pure water simultaneously
It is flowed into this grade of finished product collecting tank by self-gravity action；
At the same time, the membrane distillation units at different levels are sucked by vacuum using the vacuum pump, so that from described
Steam in hollow fiber film assembly shell side enters in the tube side of this grade of shell-and-tube heat exchanger.
Further, the method further includes：When the steam carried out in the shell-and-tube heat exchanger it is described heat exchange it is cold
When generating fixed gas after solidifying, using the fixed gas heat exchanger to exporting institute be discharged by the tube side of the shell-and-tube heat exchanger
It states fixed gas and carries out heat exchange condensation.
The advantageous effect that technical solution provided in an embodiment of the present invention is brought is：
Distillation device provided in an embodiment of the present invention is carried out in shell-and-tube heat exchangers at different levels with steam by making feed liquid
Heat exchange condensation, not only realizes the recycling to steam latent heat, while reducing the thermal energy supply to feed liquid and being condensed to steam
Energy supply, so will effectively reduce membrane distillation process energy consumption, and then improve membrane distillation process the thermal efficiency.In addition, will
It obtains being recycled in hollow fiber film assembly of the dope respectively in this grade of membrane distillation unit after feed liquid separation, not only be conducive to
The progress of above-mentioned heat exchange condensation process, additionally it is possible to improve the separating effect of feed liquid, and then improve the water generation ratio of membrane distillation process.
Description of the drawings
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, other are can also be obtained according to these attached drawings
Attached drawing.
Fig. 1 is the structural schematic diagram of parallel multiple-effect vacuum distillation device provided in an embodiment of the present invention.
Reference numeral indicates respectively：
1 material liquid tank,
2 booster pumps,
3 vacuum pumps,
4 hollow fiber film assemblies,
5 finished product collecting tanks,
6 thermometers,
7 shell-and-tube heat exchangers,
8 coolers,
9 heating rods,
10 fixed gas heat exchangers,
11 pressure vacuum gauges.
It should be noted that MD shown in Fig. 1 indicates that hollow fiber film assembly, HE indicate shell-and-tube heat exchanger, accordingly
Ground, MD1, MD2 and MDn indicate first order membrane distillation unit, second level membrane distillation unit and n-th grade of membrane distillation list respectively
Hollow fiber film assembly in member；HE1, HE2 and HEn indicate first order membrane distillation unit, second level membrane distillation unit respectively
And the shell-and-tube heat exchanger in n-th grade of membrane distillation unit.Void between second level membrane distillation unit and n-th grade of membrane distillation unit
Line indicates the 3rd level omitted until (n-1)th grade of membrane distillation unit, their arrangement and so on.
Specific implementation mode
To make the object, technical solutions and advantages of the present invention clearer, below in conjunction with attached drawing to embodiment party of the present invention
Formula is described in further detail.
In a first aspect, an embodiment of the present invention provides a kind of parallel multiple-effect vacuum distillation devices, as shown in Fig. 1,
The device includes material liquid tank 1, booster pump 2, vacuum pump 3, hollow fiber film assembly 4, finished product collecting tank 5 and thermometer 6, further
Ground, which further includes shell-and-tube heat exchanger 7 and cooler 8, and heating rod 9 is provided in material liquid tank 1.
Wherein, 1, booster pump 2, one of material liquid tank of shell-and-tube heat exchanger 7, one of hollow fiber film assembly 4, one
The cooperation of a finished product collecting tank 5 constitutes level-one membrane distillation unit, and membrane distillation unit has been arranged in parallel n grades, wherein n be more than or
Equal to 2.
In first order membrane distillation unit, material liquid tank 1, booster pump 2, hollow fiber film assembly 4 tube side be sequentially connected to, constitute
First closed loop；The second level is until the tube side of the hollow fiber film assembly 4 in n-th grade of membrane distillation unit is steamed with prime film
The material liquid tank 1 evaporated in the shell side of the shell-and-tube heat exchanger 7 in unit, this grade of membrane distillation unit is sequentially connected to booster pump 2, is constituted
The second to the n-th closed loop；And the shell side import of the shell-and-tube heat exchanger 7 in n-th grade of membrane distillation unit and shell side go out
Mouth is connected to the water outlet of cooler 8 and water inlet respectively, to constitute cooling circuit.
Per the pipe of the shell-side outlet and this grade of shell-and-tube heat exchanger 7 of the hollow fiber film assembly 4 in level-one membrane distillation unit
Journey import is connected；In the first order to (n-1)th grade of membrane distillation unit, tube side outlet and the next stage film of shell-and-tube heat exchanger 7 steam
Evaporate the hollow fiber film assembly 4 in unit shell-side outlet be connected after again with the pipe shell type heat exchange in next stage membrane distillation unit
The tube side import of device 7 is connected, also, tube side outlet and the vacuum pump 3 of the shell-and-tube heat exchanger 7 in n-th grade of membrane distillation unit
Connection.
Per in level-one membrane distillation unit, the tube side import of shell-and-tube heat exchanger 7 is also connected to finished product collecting tank 5, meanwhile, increase
Press pump 2 is provided with thermometer 6 in the connecting pipeline of hollow fiber film assembly 4.
It is true to parallel multiple-effect provided in an embodiment of the present invention below with reference to each component in attached drawing 1 and above-mentioned apparatus
The operation principle of empty distillation device is described：
In every level-one membrane distillation unit, due to being provided with heating rod 9 in material liquid tank 1, which will be to the material liquid tank
Feed liquid in 1 is heated, it is made to reach scheduled temperature.It, will after being heated to predetermined temperature in feed liquid is by this grade of material liquid tank 1
It is carried out by hydrophobic hollow fiber film wire in the tube side entered in this grade of doughnut membrane distillation component by this grade of booster pump 2
Separation obtains the dope remained in 4 tube side of hollow fiber film assembly and is evaporated to through the film surface of hollow fiber film thread
Steam in 4 shell side of hollow fiber film assembly.
For dope, due to material liquid tank 1, booster pump 2, the hollow fiber film assembly 4 in first order membrane distillation unit
Tube side be sequentially connected to and constitute the first closed loop, i.e. dope in first order membrane distillation unit will be by this grade of hollow fibre
The tube side outlet of dimension membrane module 4 sequentially enters the tube side of this grade of material liquid tank 1, this grade of booster pump 2 and this grade of hollow fiber film assembly 4
Import recycles in the first closed loop.And the second level is up to the hollow fiber film assembly 4 in n-th grade of membrane distillation unit
Tube side and prime membrane distillation unit in shell-and-tube heat exchanger 7 shell side, the material liquid tank 1 in this grade of membrane distillation unit and supercharging
Pump 2 is sequentially connected to, the second closed loop of composition ... to the n-th closed loop, in these circulation loops, dope
Tube side outlet by this grade of hollow fiber film assembly 4 is entered to the shell side and prime pipe shell type heat exchange of prime shell-and-tube heat exchanger 7
Steam in 7 tube side of device carries out heat exchange condensation, then sequentially enters this grade of material liquid tank 1, this grade of booster pump 2 and this grade of hollow fibre
Tie up the tube side import of membrane module 4, i.e. dope recycles in the second closed loop to the n-th closed loop respectively, and with
Steam in prime shell-and-tube heat exchanger 7 carries out heat exchange condensation.
And for steam, it will pass through per steam caused by the hollow fiber film assembly 4 in level-one membrane distillation unit
Shell side of the vacuum suction effect through this grade of hollow fiber film assembly 4 of vacuum pump 3 enters the tube side of this grade of shell-and-tube heat exchanger 7,
And in the tube side of this grade shell-and-tube heat exchanger 7 in its shell side from the dense of prime doughnut membrane distillation component tube side
Liquid carries out heat exchange condensation, and condensation pure water, that is, pure water is then formed in the tube side of the shell-and-tube heat exchanger 7, and condensation pure water will pass through
Self-gravity action flows into this grade of finished product collecting tank 5.Due to the shell-and-tube heat exchanger 7 in n-th grade of membrane distillation unit shell side into
Mouth and shell-side outlet are connected to the water outlet of cooler 8 and water inlet respectively, to constitute cooling circuit, so into n-th
Water vapour in grade membrane distillation unit in 7 tube side of shell-and-tube heat exchanger is carried out with the cooling water from cooler 8 in its shell side
Heat exchange condensation, to obtain condensation pure water and be flowed into this grade of finished product collecting tank 5 by self-gravity action.
Furthermore, it is necessary to further illustrate, first, device provided in an embodiment of the present invention includes that n is respectively arranged in parallel
Membrane distillation unit, such as it may include 2,3,4,5,6,7,8 etc. the membrane distillation units being arranged in parallel, root
Factually water demand is made to determine the numerical value of n in border.
Second, in device provided in an embodiment of the present invention, vacuum pumping is carried out to membrane distillation units at different levels using vacuum pump 3
It inhales, and then realizes and the shell side of the hollow fiber film assembly 4 in every level-one membrane distillation unit is vacuumized, and then be hollow-fibre membrane
Component 4, which provides, transmits vapour pressure deficit, by steam from the shell-and-tube heat exchanger 7 for being drawn into peer in hollow-fibre membrane group.Its
In, for membrane distillation units at different levels, vacuum pump 3 is connected with the outlet of the tube side of shell-and-tube heat exchangers 7 at different levels, specifically,
Following mode may be used to realize the connection between them：As an implementation, the pipe in the n grades of membrane distillation unit
It is connected to a vacuum pump 3 after the tube side outlet serial communication of shell heat exchanger 7, reference can be made to attached drawing 1, i.e., under the embodiment only
Using only a vacuum pump 3.As another embodiment, per the shell-and-tube heat exchanger 7 in level-one membrane distillation unit
Tube side outlet is directly connected to by vacuum pipeline with a vacuum pump 3, and the present invention can be achieved in any of the above connection type.
Third, the feed liquid recycled in first order membrane distillation unit will be supplied by the heating rod 9 being arranged on this grade of material liquid tank 1
To heat, so for first order membrane distillation unit, the heating rod 9 being arranged on material liquid tank 1 is used for this grade of cycle stock
Liquid carries out initial heating and subsequent heat supplement.And the second level until the feed liquid recycled in n-th grade of membrane distillation unit due to
Heat exchange condensation can be carried out with the steam in 7 tube side of prime shell-and-tube heat exchanger, a large amount of steam latent heats for absorbing steam make
Its temperature increases, so, for the second level to n-th grade of membrane distillation unit, the heating rod 9 being arranged on material liquid tank 1 is only
For giving initial heating to the feed liquid in its material liquid tank 1, and follow-up heat supplement need not be carried out, effectively reduce film steaming
Evaporate the energy consumption of process.Heating rod 9 and on material liquid tank 1 be arranged heating rod 9 it is common for this field, the embodiment of the present invention exists
This does not make more specifically to limit to its concrete structure.
4th, since only ideal feeding temperature can not be reached to be heated to feed liquid by steam latent heat, institute
Before hollow fiber film assembly 4 of the feed liquid in entrance first order membrane distillation unit, to utilize the heating rod 9 on material liquid tank 1
Heating is carried out to it until it reaches ideal feeding temperature, and temperature in use meter 6 is monitored.Due to subsequent stages membrane distillation
Heating rod 9 in unit is preferably that feed liquid provides initial heating, thus preferably only in first order membrane distillation unit in
Thermometer 6 is set in the connecting pipeline between empty fiber membrane component 4 and booster pump 2, and need not be configured in subsequent stages.
It can be seen from the above, distillation device provided in an embodiment of the present invention, by making feed liquid in shell-and-tube heat exchangers 7 at different levels
In with steam carry out heat exchange condensation, not only realize the recycling to steam latent heat, while reducing to the thermal energy of feed liquid for giving
And the energy supply to steam condensation, so by effective energy consumption for reducing membrane distillation process, and then improve the heat of membrane distillation process
Efficiency.In addition, obtaining carrying out again in hollow fiber film assembly 4 of the dope respectively in this grade of membrane distillation unit after feed liquid is detached
Cycle is not only conducive to the progress of above-mentioned heat exchange condensation process, additionally it is possible to improve the separating effect of feed liquid, and then improve membrane distillation mistake
The water generation ratio of journey.Good treatment effect can be reached under low energy consumption state by carrying out water process using the device, for tap water
For, the conductivity that it condenses pure water can be made to reach 2 μ s/cm, its water generation ratio is made to reach at least 1.7；For seawater, it can make
It condenses the conductivity of pure water and reaches 12 μ s/cm, its water generation ratio is made to reach at least 1.6.
It will be appreciated by persons skilled in the art that the above-mentioned thermal efficiency refers to the heat needed for water evaporation and itself and film
Heat transfer needed for the sum of heat ratio, above-mentioned water generation ratio refers to that the distillation device pure water total output adds with feed liquid
The ratio between the quantity of steam that hot device is consumed.
In device provided in an embodiment of the present invention, hollow fiber film assembly 4 and shell-and-tube heat exchanger 7 are vertically arranged,
And its tube side import is located at lower end, and tube side outlet is located at upper end.The hollow fiber film assembly 4 is common for this field, this
Field technology personnel can be obtained by purchased in market.For example comprising tubular outer shell, axially spaced setting are in tubular outer shell
Internal a plurality of hydrophobic hollow fiber film wire, a plurality of hollow fiber film thread are fixed on the two of the tubular outer shell by resin
End, meanwhile, the both ends of tubular outer shell are respectively arranged with end cap.Wherein, it is provided on end cap logical with the center of hollow fiber film thread
The cap bore that hole is connected, to cooperatively form the tube side of hollow fiber film assembly 4, tubular outer shell is provided on the outer wall of close end
The pore being connected with its inner cavity, to cooperatively form the shell side of the hollow fiber film assembly 4.The center fiber film wire is hydrophobic
Film, film surface are hydrophobic porous structure, are only capable of that steam is made to pass through, and feed liquid can not be made to pass through, and so can guarantee its tool
There is higher separating effect, obtains the higher condensation pure water of purity.
Preferably, device provided in an embodiment of the present invention further includes filter, the filter be arranged material liquid tank 1 into
On expects pipe line.Coarse filtration pretreatment can be carried out to the feed liquid for entering material liquid tank 1, by the way that above-mentioned filter is arranged to remove mud therein
The bulky grains component such as sand, iron rust, suspended matter, to prevent them from being polluted to the film wire of hollow-fibre membrane.For example, the mistake
Quartz filter, disc filter or the bag filter that filter can select this field common.
Further, preferably, as shown in Fig. 1, device provided in an embodiment of the present invention further includes fixed gas heat exchange
Tube side outlet and the vacuum pump of the shell-and-tube heat exchanger 7 in n-th grade of membrane distillation unit is arranged in device 10, the fixed gas heat exchanger 10
In connecting pipeline between 3.Since steam carries out being possible to a residual part after heat exchange condensation in shell-and-tube heat exchanger 7 not coagulating
Gas, in order to prevent its be lost in, the outlet of the tube side of shell-and-tube heat exchanger 7 in n-th grade of membrane distillation unit of the embodiment of the present invention with it is true
Setting fixed gas heat exchanger 10 in connecting pipeline between sky pump 3, to be exchanged heat again to fixed gas, to make its total condensation
At pure water, the water generation ratio of pure water is improved.Wherein, the structure of fixed gas heat exchanger 10 can be with above-mentioned shell-and-tube heat exchanger 7
Structure is identical, realizes heat exchange condensation effect.
Further, as shown in Fig. 1, device provided in an embodiment of the present invention further includes pressure vacuum gauge 11, vacuum pressure
Power table 11 is arranged in the connecting pipeline between fixed gas heat exchanger 10 and vacuum pump 3.It will be appreciated by those skilled in the art that
It is that, when being not provided with fixed gas heat exchanger 10, can also pressure vacuum gauge be set in the connecting pipeline of the upstream of vacuum pump 3
11, the vacuum suction pressure of hollow fiber film assembly 4 can be monitored in real time by the way that pressure vacuum gauge 11 is arranged, and then basis
Actual demand controls vacuum pump 3, to make membrane distillation process be smoothed out under in low energy consumption state.
Further, in device provided in an embodiment of the present invention, the hollow fiber film assembly 4 in membrane distillation units at different levels
Tube side inlet line on be both provided with flowmeter.By the way that flowmeter is arranged in above-mentioned connecting pipeline, with to entering per level-one
The feed liquid flow of hollow fiber film assembly 4 in membrane distillation unit is measured in real time, to detect the UF membrane efficiency of the device.
Further, an electronic balance can also be set below each finished product collecting tank 5, pass through pure water in cooling water of units of measurement time
Weight detect the separative efficiency of the distillation device.Furthermore, it is desirable to explanation, it, can according to the progress of membrane distillation process
To supplement feed liquid to material liquid tank 1.
Further, in embodiments of the present invention, come to the shell in n-th grade of membrane distillation unit by using cooler 8
Steam in formula heat exchanger 7 is condensed, wherein and the cooler 8 can be selected from water cooler or air cooler commonly used in the art,
It is recycled, and then ensured before each with stationary temperature in itself and n-th grade of shell-and-tube heat exchanger 7 from extraneous cooling water
Fixed gas in all shell-and-tube heat exchangers 7 of grade is condensed into condensation pure water, improves water generation ratio.
Above-mentioned heat exchange condensation process is carried out using shell-and-tube heat exchanger 7 in embodiments of the present invention, preferably, for this
Shell-and-tube heat exchanger 7 is preferably polymer heat exchanger, and polymer heat exchanger includes tubular outer shell, a plurality of polymer heat exchanger tube, end
Lid.Polymer heat exchanger tube is in doughnut structure, while tube wall dense non-porous, a plurality of axially spaced setting of polymer heat exchanger tube
Inside tubular outer shell, and it is fixed on by solidified resin the both ends of tubular outer shell；End cap is removably attached to tubular outer shell
Both ends, and the cap bore being connected with the central through hole of polymer heat exchanger tube is provided on end cap, to cooperatively form polymerization
The tube side of object heat exchanger；Tubular outer shell is respectively arranged with the feed liquor being connected with the inner cavity of tubular outer shell on the outer wall of two close end
Pipe and outlet tube, to cooperatively form the shell side of polymer heat exchanger.It can be seen from the above, above-mentioned polymer heat exchanger and structure
Similar to the structure of hollow fiber film assembly 4, the difference is that the tube wall of the polymer heat exchanger tube is dense non-porous, to
Steam is set to carry out abundant heat exchange processing with the feed liquid outside pipe.Since the polymer heat exchanger has used polymer heat exchanger tube, tool
There are good chemical stability and excellent corrosion resistance, and the polymer heat exchanger volume is small, it is compact-sized, have larger
Effective heat exchange area, the economic serviceability of the device so can be improved.
Specifically, the polymer heat exchanger tube be polyfluortetraethylene pipe, outer diameter 0.5-0.9mm, for example, 0.55mm,
0.6mm, 0.7mm, 0.8mm etc., internal diameter 0.3-0.5mm, such as 0.35mm, 0.4mm, 0.45mm etc..Poly- the four of above structure
Fluoride tubes can bear positive pressure 1.6Mpa, negative pressure：77Kpa, can in -60 DEG C~+260 DEG C normal use, have reliable excellent
Corrosion resistance.The strong corrosive air-liquid body etc. under high temperature is conveyed, there is high adaptability.
In addition, for hollow fiber film assembly 4 and shell-and-tube heat exchanger 7, it is preferable to use transparent for tubular outer shell
Hard high strength plastics be prepared, and used solidified resin passes through it is preferable to use the common epoxy resin in this field
The both ends of tubular outer shell are blocked using epoxy resin, while ensureing the connection of itself and hollow fiber film thread and polymer heat exchanger tube
Property.In addition, the connection type between end cap and tubular outer shell is preferably threadedly coupled, i.e., interior spiral shell is set on the inner wall of end cap
Line is arranged on the both ends outer wall of tubular outer shell compatible external screw thread therewith and realizes.
Second aspect, an embodiment of the present invention provides the method for carrying out vacuum membrane distillation using above-mentioned distillation device,
This method includes：
Per in level-one membrane distillation unit, after feed liquid is heated to such as 60-95 DEG C of predetermined temperature in material liquid tank 1, pass through increasing
It is detached in the tube side that press pump 2 enters in doughnut membrane distillation component, obtains dope and steam.
For first order membrane distillation unit, dope sequentially enters this grade by the tube side of this grade of hollow fiber film assembly 4
Material liquid tank 1 and this grade of booster pump 2, and recycled in the first closed loop；The second level to n-th grade of membrane distillation unit is come
It says, dope will be entered the shell side of prime shell-and-tube heat exchanger 7 by the tube side of this grade of hollow fiber film assembly 4, then be sequentially entered
This grade of material liquid tank 1 and this grade of booster pump 2, and recycled in the second to the n-th closed loop, at the same with shell-and-tube described in prime
Steam in 7 tube side of heat exchanger carries out heat exchange condensation.
Shell side of the steam through this grade of hollow fiber film assembly 4 enters in the tube side and shell side of this grade of shell-and-tube heat exchanger 7
Feed liquid from next stage hollow fiber film assembly 4 carries out heat exchange condensation, obtains condensation pure water and is flowed by self-gravity action
In this grade of finished product collecting tank 5；Meanwhile into the water vapour and shell side in 7 tube side of shell-and-tube heat exchanger in n-th grade of membrane distillation unit
In the cooling water in cooler 8 carry out heat exchange condensation, obtain condensation pure water and by self-gravity action flow into this grade at
In product collecting tank 5.
At the same time, membrane distillation units at different levels are sucked by vacuum using vacuum pump 3, so as to come from hollow-fibre membrane group
Steam in 4 shell side of part enters in the tube side of this grade of shell-and-tube heat exchanger 7.
The membrane distillation method carried out using device provided in an embodiment of the present invention, is equally realized and is returned to steam latent heat
It receives, reduces and the thermal energy of feed liquid is supplied and to the energy supply that steam condenses, effectively reduces the energy consumption of membrane distillation process, into
And improve the thermal efficiency of membrane distillation process.In addition, passing through the hollow-fibre membrane group in this grade of membrane distillation unit respectively by dope
It is recycled in part 4, is not only conducive to the progress of above-mentioned heat exchange condensation process, additionally it is possible to improve the separating effect of feed liquid, in turn
Improve the water generation ratio of membrane distillation process.For tap water, the conductivity that it condenses pure water can be made to reach 2 μ s/cm, it is made to make
Water ratio reaches at least 1.7；For seawater, the conductivity that it condenses pure water can be made to reach 12 μ s/cm, its water generation ratio is made to reach
At least 1.6.
Further, method provided in an embodiment of the present invention further includes：When steam exchanges heat in shell-and-tube heat exchanger 7
When generating fixed gas after condensation, do not coagulated to what the tube side outlet by shell-and-tube heat exchanger 7 was discharged using fixed gas heat exchanger 10
Gas carries out heat exchange condensation, and to be exchanged heat again to fixed gas, to make its total condensation at pure water, that improves pure water makes water
Than.
The foregoing is merely presently preferred embodiments of the present invention, the protection domain being not intended to limit the invention, all in this hair
Within bright spirit and principle, any modification, equivalent replacement, improvement and so on should be included in protection scope of the present invention
Within.
Claims (10)
1. a kind of parallel multiple-effect vacuum distillation device, including material liquid tank (1), booster pump (2), vacuum pump (3), doughnut
Membrane module (4), finished product collecting tank (5) and thermometer (6), which is characterized in that described device further include shell-and-tube heat exchanger (7) and
Cooler (8), and heating rod (9) is provided in the material liquid tank (1)；
One hollow fiber film assembly (4), a shell-and-tube heat exchanger (7), a material liquid tank (1), one
The booster pump (2), finished product collecting tank (5) cooperation constitute level-one membrane distillation unit, and the membrane distillation unit
N grades have been arranged in parallel it, wherein n is more than or equal to 2；
In membrane distillation unit described in the first order, the material liquid tank (1), the booster pump (2), the hollow fiber film assembly (4)
Tube side be sequentially connected to, constitute the first closed loop；The second level is up to the doughnut in n-th grade of membrane distillation unit
In the tube side of membrane module (4) and the shell side of the shell-and-tube heat exchanger (7) in prime membrane distillation unit, this grade of membrane distillation unit
The material liquid tank (1) be sequentially connected to the booster pump (2), constitute the second to the n-th closed loop；And n-th grade of institute
State the shell-and-tube heat exchanger (7) in membrane distillation unit shell side import and shell-side outlet respectively with the cooler (8)
Water outlet is connected to water inlet, to constitute cooling circuit；
The shell-side outlet of the hollow fiber film assembly (4) in membrane distillation unit described in per level-one and the shell-and-tube heat exchanger
(7) tube side import is connected；In the first order to (n-1)th grade of membrane distillation unit, the tube side of the shell-and-tube heat exchanger (7) exports
After being connected with the shell-side outlet of the hollow fiber film assembly (4) in membrane distillation unit described in next stage again with next stage institute
The tube side import for stating the shell-and-tube heat exchanger (7) in membrane distillation unit is connected, also, n-th grade of membrane distillation unit
In the shell-and-tube heat exchanger (7) tube side outlet connect with the vacuum pump (3)；
Per in membrane distillation unit described in level-one, the tube side import of the shell-and-tube heat exchanger (7) also with the finished product collecting tank (5)
Connection, meanwhile, the booster pump (2) is provided with the thermometer in the connecting pipeline of the hollow fiber film assembly (4)
(6)。
2. the apparatus according to claim 1, which is characterized in that described device further includes filter, the filter setting
On the feeding line of the material liquid tank (1).
3. the apparatus according to claim 1, which is characterized in that described device further includes fixed gas heat exchanger (10), described
Fixed gas heat exchanger (10) be arranged the shell-and-tube heat exchanger (7) in n-th grade of membrane distillation unit tube side outlet with
In connecting pipeline between the vacuum pump (3).
4. device according to claim 3, which is characterized in that described device further includes pressure vacuum gauge (11), described true
In the connecting pipeline that hollow pressure gauge (11) is arranged between the fixed gas heat exchanger (10) and the vacuum pump (3).
5. the apparatus according to claim 1, which is characterized in that the tube side inlet line of the hollow fiber film assembly (4)
On be both provided with flowmeter.
6. the apparatus according to claim 1, which is characterized in that the cooler (8) is water cooler or air cooler.
7. the apparatus according to claim 1, which is characterized in that the shell-and-tube heat exchanger (7) is polymer heat exchanger, institute
It includes tubular outer shell, a plurality of polymer heat exchanger tube, end cap to state polymer heat exchanger；
The polymer heat exchanger tube is in doughnut structure, while tube wall dense non-porous, a plurality of polymer heat exchanger tube is along axis
To being arranged at intervals on inside the tubular outer shell, and the both ends of the tubular outer shell are fixed on by solidified resin；
The end cap is removably attached to the both ends of the tubular outer shell, and is provided on the end cap and the polymer
The cap bore that the central through hole of heat exchanger tube is connected, to cooperatively form the tube side of the polymer heat exchanger；
The tubular outer shell is respectively arranged with the inlet tube being connected with the inner cavity of the tubular outer shell on the outer wall of two close end
And outlet tube, to cooperatively form the shell side of the polymer heat exchanger.
8. device according to claim 7, which is characterized in that the polymer heat exchanger tube is polyfluortetraethylene pipe, outer diameter
For 0.5-0.9mm, internal diameter 0.3-0.5mm.
9. a kind of method carrying out vacuum membrane distillation using claim 1-8 any one of them devices, which is characterized in that described
Method includes：
In membrane distillation unit described in per level-one, after feed liquid is heated to predetermined temperature in the material liquid tank (1), pass through the supercharging
It is detached in the tube side that pump (2) enters in the doughnut membrane distillation component, obtains dope and steam；
For membrane distillation unit described in the first order, the dope by this grade of hollow fiber film assembly (4) tube side according to
It is secondary to enter this grade of material liquid tank (1) and this grade of booster pump (2), and recycled in first closed loop；It is right
For the second level to n-th grade of membrane distillation unit, the dope will be by the tube side of this grade of hollow fiber film assembly (4)
Into the shell side of shell-and-tube heat exchanger described in prime (7), this grade of material liquid tank (1) and this grade of supercharging are then sequentially entered
Pump (2), and recycled in the second to the n-th closed loop, at the same in shell-and-tube heat exchanger described in prime (7) tube side
Steam carry out heat exchange condensation；
Shell side of the steam through this grade of hollow fiber film assembly (4) enters the pipe of this grade of shell-and-tube heat exchanger (7)
Journey carries out heat exchange condensation with the dope from hollow fiber film assembly (4) described in next stage in shell side, obtains condensation pure water simultaneously
It is flowed into this grade of finished product collecting tank (5) by self-gravity action；Meanwhile into described in n-th grade of membrane distillation unit
The cooling water in the cooler (8) in water vapour and shell side in shell-and-tube heat exchanger (7) tube side exchange heat cold
It is solidifying, it obtains condensation pure water and is flowed into this grade of finished product collecting tank (5) by self-gravity action；
At the same time, the membrane distillation units at different levels are sucked by vacuum using the vacuum pump (3), so that in described
Steam in empty fiber membrane component (4) shell side enters in the tube side of this grade of shell-and-tube heat exchanger (7).
10. according to the method described in claim 9, it is characterized in that, the method further includes：When the steam is in the shell
When carrying out generating fixed gas after the heat exchange condenses in formula heat exchanger (7), using the fixed gas heat exchanger (10) to by described
The fixed gas that the tube side outlet of shell-and-tube heat exchanger (7) is discharged carries out heat exchange condensation.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7459084B2 (en) * | 2001-06-22 | 2008-12-02 | Petro Sep International Ltd. | Membrane-assisted fluid separation apparatus and method |
| CN104415664A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | Internal-pressure-type vacuum membrane distillation concentration method of ethylene glycol solution |
| CN205988675U (en) * | 2016-08-12 | 2017-03-01 | 北京惠源三达水处理设备有限公司 | A kind of parallel multiple-effect vacuum distillation device |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7459084B2 (en) * | 2001-06-22 | 2008-12-02 | Petro Sep International Ltd. | Membrane-assisted fluid separation apparatus and method |
| CN104415664A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | Internal-pressure-type vacuum membrane distillation concentration method of ethylene glycol solution |
| CN205988675U (en) * | 2016-08-12 | 2017-03-01 | 北京惠源三达水处理设备有限公司 | A kind of parallel multiple-effect vacuum distillation device |
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