CN109200827B - Flat-plate membrane distillation device, distillation method and application - Google Patents
Flat-plate membrane distillation device, distillation method and application Download PDFInfo
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- CN109200827B CN109200827B CN201811375383.5A CN201811375383A CN109200827B CN 109200827 B CN109200827 B CN 109200827B CN 201811375383 A CN201811375383 A CN 201811375383A CN 109200827 B CN109200827 B CN 109200827B
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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
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/08—Flat membrane modules
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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Abstract
The invention provides a flat membrane distillation device, a distillation method and application, wherein the flat membrane distillation device consists of a plurality of distillation units, and each distillation unit comprises a plurality of membrane frames and a plurality of runner grids; the flat plate type distillation device provided by the invention can be assembled and disassembled at will, and the optimal combination and the optimal distillation efficiency are achieved by increasing or reducing the number of the combined layers of the membrane frame and the runner grid; and through the reasonable setting of distillation membrane and condensation membrane, establish cold, hot liquid independent flow channel respectively for two kinds of liquid flow in opposite directions, very big increase the heat exchange efficiency between the fluid, promoted the distillation efficiency, make the output efficiency of distillation liquid promote greatly, output efficiency can reach about 2.0 liters/square meter/hour, and practical application is worth highly.
Description
Technical Field
The invention belongs to the field of chemical separation, and relates to a flat-plate membrane distillation device, a distillation method and application.
Background
The separation of solvent from solute is achieved by utilizing different temperature characteristics of solvent and solute in solution, such as vapor pressure, which is the basic principle of distillation. The traditional distillation method is to heat the solution to the temperature near the boiling point of the solvent, and then condense and collect the solvent vapor, thereby achieving the purpose of separating the solvent from the solute.
With the continuous demand of people for water resources, the seawater desalination technology is gradually developed and matured. The traditional seawater desalination method comprises 1) heating and distilling; 2) membrane separation techniques (ultrafiltration and reverse osmosis membranes). In recent years, with the development of material science, another technique, that is, a membrane distillation (hereinafter abbreviated as MD) technique, has been greatly developed. Membrane distillation (desalination of sea water) uses a hydrophobic porous membrane, which is characterized in that water cannot pass through it but water vapor can pass through it smoothly under a certain pressure. In this way, the water temperature on one side of the membrane does not need to be high, and its vapour can pass through the membrane to the other side of the membrane.
In chemical production, a large amount of mixed solution of an organic solvent and water is generated. If there is a large difference in vapor pressure between the organic solution and water at an appropriate temperature, the membrane distillation technique can be used for the concentration of the organic solvent.
There are generally 4 membrane distillation modes of operation as follows:
1) direct membrane distillation (DCMD), i.e. the side of the hydrophobic membrane that is in communication with the higher temperature distillation medium (raw seawater in desalination applications), while the side through which the vapour passes is in direct contact with the lower temperature cooling medium (fresh water in desalination applications), so that the vapour is directly condensed in the cooling medium. The liquid flow on the high temperature side and the low temperature side is maintained during operation. As heat will be released during condensation of the vapour, the temperature of the distillation medium will decrease and the temperature of the cooling medium will increase. It is therefore necessary to maintain the temperature difference of the liquid on both sides of the distillation membrane by means of heating and cooling devices.
2) Air Gap Membrane Distillation (AGMD), i.e. on the side through which the vapour of the distillation membrane passes, the vapour is condensed on an impermeable membrane (condensation membrane) after passing through an air gap, while on the other side of the condensation membrane a liquid medium is flowed which is kept at a lower temperature. Similarly, the operation is performed while maintaining the temperature difference between the high temperature medium and the low temperature medium. However, the cryogenic medium is not necessarily a pure distilled condensate liquid, which is particularly attractive for sea desalination applications on the sea (island): low temperature seawater may be used as the cold end medium. In addition, this method is very advantageous for membrane distillation concentration of a mixed solution of an organic solvent and water.
3) Working gas blown membrane distillation (SWMD), i.e. by combining with a non-permeable membrane or other material on the vapour permeable side of the distillation membrane, an air channel is created, at one end of which a working gas, such as dry nitrogen, is blown in, bringing the water vapour out of the membrane distillation apparatus, the brought-in working gas containing water vapour is condensed by a condenser to remove water (produce water), and the working gas is blown back into the membrane distillation apparatus.
4) Vacuum-assisted membrane distillation (VSMD) operates on a similar principle to SWMD, except that a vacuum pump is connected to one end of an air channel on the vapor transmission side to pump vapor out of a membrane distillation device, and the pumped vapor is condensed to produce water.
The efficiency of membrane distillation depends on the hydrophobic properties and pore size of the membrane, the temperature difference between the cold/hot media during operation, and the removal rate of the distilled gas at the membrane surface. Therefore, how to develop a device for improving the heat transfer efficiency between cold water and hot water and the distillation efficiency of the membrane has important significance for improving the distillation efficiency of the membrane distillation method.
Disclosure of Invention
In view of the defects of the prior art, the invention aims to provide an Air Gap Method (AGMD) flat membrane distillation device, a distillation method and application, so as to achieve the effects of simple use, simple and convenient assembly and disassembly and high distillation efficiency.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a flat-plate type membrane distillation apparatus, which is composed of a plurality of distillation units, wherein each distillation unit comprises a plurality of membrane frames and a plurality of runner grids;
the two opposite surfaces of the membrane frame are respectively provided with a distillation membrane and a condensation membrane, two adjacent angular positions of the membrane frame are respectively provided with a membrane frame liquid channel, and the membrane frame liquid channel comprises a hot membrane frame liquid channel and a cold membrane frame liquid channel;
the flow channel grating comprises a plurality of linear railings inside, the linear railings divide the flow channel grating to form a plurality of liquid flow channels, fluid inlets are arranged at two opposite corners of the flow channel grating, and a flow channel grating liquid channel is arranged at any one corner adjacent to the fluid inlets;
the membrane frame type distillation unit is characterized in that a runner grating is arranged between the condensation membrane arranged on one surface of the membrane frame and the condensation membrane arranged on the next membrane frame, a runner grating is arranged between the distillation membrane arranged on the other surface of the membrane frame and the distillation membrane arranged on the previous membrane frame, the membrane frame liquid channel is communicated with the runner grating liquid channel, and a plurality of membrane frames and a plurality of runner gratings are alternately arranged to form the distillation unit.
The flat plate type distillation device provided by the invention can be assembled and disassembled at will, and the optimal combination and the optimal distillation efficiency are achieved by increasing or reducing the number of the combined layers of the membrane frame and the runner grid; and through the reasonable setting of distillation membrane and condensation membrane, establish cold, hot liquid independent flow channel respectively for two kinds of liquid flow in opposite directions, very big increase the heat exchange efficiency between the fluid, promoted distillation efficiency, make the output efficiency of distillation liquid promote greatly.
In the invention, the membrane frames and the runner grids are alternately arranged at intervals, two surfaces of the same membrane frame are respectively provided with a distillation membrane and a condensation membrane, the distillation membrane is oppositely arranged with the distillation membrane of the next membrane frame, and the runner grids are clamped between the middle gaps, so that the two distillation membranes and the middle runner grids jointly form a hot water runner; the other side of the membrane frame is provided with an impermeable condensation membrane which is arranged opposite to the condensation membrane of the other membrane frame, and a flow passage grating is clamped in the middle gap, so that the two condensation membranes and the flow passage grating in the middle form a cold water channel together. Therefore, in the distillation unit, the cold water channel and the hot water channel are separated and flow separately, so that the hot water channel is ensured between the distillation membranes on each membrane frame, and the cold water channel is ensured between the condensation membranes; and the distillation units are stacked and arranged to form the whole membrane distillation device.
Preferably, a support grid is arranged between the distillation membrane and the condensation membrane of the membrane frame, and the support grid is positioned in the center of the membrane frame. The support grid is used for supporting the distillation film and the condensation film on the film frame.
Preferably, the edge side of the membrane frame is provided with a plurality of water producing pores.
And a plurality of small water producing holes are formed in the side face of the edge of the membrane frame, and condensed liquid generated by distillation flows out of the small holes and is collected to obtain distillate.
Preferably, the edge of the membrane frame is provided with a membrane frame fitting hole.
The mounting holes are typically symmetrically located at the edges of the membrane frame, which facilitates assembly of the device.
Preferably, the thickness of the tail ends of the linear railings inside the runner grid is alternately reduced.
The thickness of the tail end of the linear railing is reduced alternately, and the design can enable liquid to flow in the flow channel according to the fixed flow channel direction.
Preferably, the edge of the runner grid is provided with a runner grid assembly hole.
Preferably, the distillation membrane is a polytetrafluoroethylene membrane or a polyvinylidene fluoride membrane.
In the present invention, the distillation membrane is not limited to the membranes of the above two materials, and any membrane made of a material having a hydrophobic function can be applied as the distillation membrane in the present invention.
Preferably, the condensation film is an ethylene-tetrafluoroethylene copolymer film or a polyester film.
The condensation membrane is impermeable to liquid and gas. An air gap is formed between the condensation film and the distillation film on the same film frame.
Preferably, the thickness of the distillation film is 100 to 150 μm, and may be, for example, 100 μm, 105 μm, 110 μm, 115 μm, 120 μm, 125 μm, 130 μm, 135 μm, 140 μm, 145 μm, 150 μm, or the like.
Preferably, the condensation film has a thickness of 40-60 μm, such as 40 μm, 45 μm, 50 μm, 55 μm, or 60 μm.
Preferably, the length of the membrane frame is 200-300 mm, for example, 200 μm, 210 μm, 220 μm, 230 μm, 240 μm, 250 μm, 260 μm, 270 μm, 280 μm, 290 μm or 300 μm, preferably 250 mm.
Preferably, the width of the membrane frame is 200-300 mm, such as 200 μm, 210 μm, 220 μm, 230 μm, 240 μm, 250 μm, 260 μm, 270 μm, 280 μm, 290 μm or 300 μm, preferably 250 mm.
In a second aspect, the present invention provides a distillation method of the flat plate type membrane distillation apparatus according to the first aspect, the method comprising: cooling liquid flows in from a fluid inlet of the runner grid and flows out from a fluid inlet at an opposite angle, the flowing cooling liquid passes through a cold film frame liquid channel of the film frame, a (hot) runner grid liquid channel and a next-stage cold film frame liquid channel and then enters a fluid inlet of a next-stage (cold) runner grid, and at the moment, the cooling liquid flows out from the fluid inlet at the opposite angle of the first-stage runner grid and continues to flow into the next stage through a similar liquid channel to circulate;
the distilled liquid flows in from the fluid inlet of the runner grid different from the cooling liquid and flows out through the fluid inlet positioned at the diagonal, the flowing distilled liquid enters the fluid inlet of the next-stage (hot) runner grid after passing through the hot film frame liquid channel, the runner grid liquid channel and the next-stage hot film frame liquid channel of the film frame, and at the moment, the distilled liquid flows out from the fluid inlet positioned at the diagonal of the first-stage runner grid and continues to flow into the next stage through the similar liquid channel for circulation;
the distillation liquid flows in the opposite direction to the cooling liquid.
The distilled liquid of the present invention has a higher temperature relative to the cooling liquid.
More specifically, cooling liquid flows in from a fluid inlet of the runner grid and flows out from a fluid inlet at an opposite angle, the flowing cooling water flows through a cold film frame liquid channel of the film frame and a runner grid liquid channel and then enters a fluid inlet of a runner grid at the next stage, the cooling liquid flows in a cold water channel at the opposite angle of the runner grid at the moment and then flows out from the fluid inlet at the opposite angle of the runner grid at the next stage, and the cold water flowing out from the fluid inlet passes through the same channel and then continuously flows into the next stage and also flows in the cold water channel for circulation;
the distillate liquid flows in the same manner as the cooling liquid, except that the fluid inlet is different and it flows in the hot film frame liquid channel.
In the whole process, cold liquid always flows in the cold channel, and hot liquid always flows in the hot channel.
In practice, the cooling liquid flows in a direction opposite to the direction of the distillate flow to take advantage of the temperature difference between the hot and cold liquids to the maximum extent. The skilled person can increase or decrease the number of combined layers of the membrane frame and the flow grid to achieve the optimal combination according to the actual needs and the operating conditions, such as the pressure of the cold and hot water flows, the temperature difference, and the variation of the operating parameters.
Preferably, the flowing pressure of the distillation liquid and the cooling liquid is 0.1 to 0.2MPa, and may be, for example, 0.1MPa, 0.11MPa, 0.12MPa, 0.13MPa, 0.14MPa, 0.15MPa, 0.16MPa, 0.17MPa, 0.18MPa, 0.19MPa or 0.2 MPa.
Preferably, the distilled or cooled liquid flows out of the water producing pores.
Preferably, dry air is blown in at the side of the water producing pores remote from the outflow of the distilled or cooled liquid.
When the distillation unit operates, condensed water flows out of the small holes at the lower part, the small holes at the side surfaces can be sealed, but the small holes at the upper part are kept to be opened, so that the condensed water can flow out smoothly. In addition, the rate of evaporation is related to the air flow at the evaporation surface, which can entrain the vapor to reduce the vapor concentration at the evaporation surface, resulting in an increased evaporation rate. When the distillation unit of the invention is operated, air is blown into the side of the small hole far away from the liquid outflow, so that the membrane distillation efficiency is effectively improved.
In the invention, the distilled liquid flowing out from the small water-producing holes can be collected by a collecting device. When the equipment is actually assembled, a person skilled in the art can combine the flat plate type distillation device and a reasonable collection device to form a more complete distillation recovery device.
In a third aspect, the present invention provides a use of the flat-plate type membrane distillation apparatus according to the first aspect in desalination of sea water or separation of organic solvent.
The flat-plate membrane distillation device provided by the invention can be used for efficiently distilling seawater to realize seawater desalination; in addition, separation between organic solvents may also be achieved, for example, separation between dimethyl sulfoxide and water, separation between petroleum ether and ethyl acetate, and the like. The organic solvent may be miscible with each other or may be two liquids that are not soluble with each other.
Compared with the prior art, the invention has the following beneficial effects:
the flat plate type distillation device provided by the invention can be assembled and disassembled at will, and the optimal combination and the optimal distillation efficiency are achieved by increasing or reducing the number of the combined layers of the membrane frame and the runner grid; and through the reasonable setting of distillation membrane and condensation membrane, establish cold, hot liquid independent flow channel respectively for two kinds of liquid flow in opposite directions, very big increase the heat exchange efficiency between the fluid, promoted the distillation efficiency, make the output efficiency of distillation liquid promote greatly, output efficiency can reach about 2.0 liters/square meter/hour, and practical application is worth highly.
Drawings
FIG. 1 is a view of a flat-plate type membrane distillation apparatus provided in example 1 of the present invention.
Fig. 2 is a schematic diagram of a membrane frame in a flat plate type membrane distillation apparatus provided in example 1 of the present invention, 1-the membrane frame, 2-a support grid, 3-a distillation membrane, 4-a condensation membrane, 5-a membrane frame liquid channel, 501-a hot membrane frame liquid channel, 502-a cold membrane frame liquid channel, 6-a water producing aperture, and 7-an assembly aperture.
Fig. 3 is a schematic view of a flow channel grid, 8-flow channel grid, 9-fluid inlet, 10-liquid flow channel, 11-flow channel grid liquid channel in the flat plate type membrane distillation apparatus provided in example 1 of the present invention.
FIG. 4 is a schematic view showing the disassembly of the distillation apparatus in the distillation in example 2 of the present invention, wherein 6-water producing holes, 8-grid channels, 9, 9a, 9b, 9c, 12, 12a are all fluid inlets.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitations of the present invention.
Example 1
The present embodiment provides a flat type membrane distillation apparatus.
The flat type membrane distillation apparatus is composed of four distillation units each of which comprises a membrane frame 1 (shown in fig. 2) and a flow channel grill 8 (shown in fig. 3).
The two opposite surfaces of the membrane frame are respectively provided with a distillation membrane 3 and a condensation membrane 4, a support grid 2 is arranged between the distillation membrane 3 and the condensation membrane 4 of the membrane frame, two adjacent angular positions of the membrane frame are respectively provided with a membrane frame liquid channel 5, the membrane frame liquid channel comprises a hot membrane frame liquid channel 501 and a cold membrane frame liquid channel 502 (in actual assembly, the two liquid channels only need to be adjacent, and the positions can be changed randomly), and the membrane frame liquid channel comprises a hot membrane frame liquid channel and a cold membrane frame liquid channel; the water producing small holes 6 are formed in the side face of the edge of the membrane frame, and the assembling holes 7 are symmetrically formed in the edge of the membrane frame.
The flow channel grid 8 comprises a plurality of linear railings, the thicknesses of the tail ends of the linear railings are reduced alternately, the linear railings separate the interior of the flow channel grid to form a plurality of liquid flow channels 10, fluid inlets 9 are arranged at two opposite corners of the flow channel grid, a flow channel grid liquid channel 11 is arranged at any one corner adjacent to the fluid inlets 9, and the flow channel grid liquid channel 11 allows another independent (heat flow or cooling liquid) liquid to pass through without interfering with the liquid flow channels determined by the flow channel grid.
A flow channel grating 8 is arranged between the condensation membrane 3 arranged on one surface of the membrane frame and the condensation membrane 3 of the next membrane frame, and a flow channel grating 8 is arranged between the distillation membrane 4 arranged on the other surface of the membrane frame and the distillation membrane 4 of the previous membrane frame, and the liquid channel 5 of one membrane frame is ensured to be communicated with the liquid channel 11 of the flow channel grating, so that a complete channel from the hot (cold) liquid flow channel of the previous stage to the hot (cold) liquid flow channel of the next stage is formed. A membrane frame and a runner grid constitute a distillation unit, which is further arranged alternately to form a flat-plate type membrane distillation device, as shown in FIG. 1.
Wherein the distillation membrane is polytetrafluoroethylene biaxial tension composite membrane with average pore diameter of 0.2 μm and thickness of 120 μm, the condensation membrane is ethylene-tetrafluoroethylene copolymer transparent membrane with thickness of 50 μm, the membrane frame is 250mm × 250mm, and the effective area is 0.0625m2The membrane frame of (1).
The membrane adopted in the embodiment 1 of the invention is matched with the device in terms of water production, energy consumption and cost in unit area, and can achieve the best effect.
Example 2
The flat type membrane distillation apparatus provided in example 1 was assembled and then subjected to distillation. The distillation method is as follows, and the disassembly schematic diagram of the distillation device can refer to FIG. 4.
Cooling water flows in from a fluid inlet 9 of the runner grid 8, flows out through a fluid inlet 9a at a diagonal position, flows through a cold film frame liquid channel of the film frame, a runner grid liquid channel and a next-stage cold film frame liquid channel (specifically, the flow direction is indicated by an arrow at 9a in fig. 4), enters a fluid inlet 9b of the next-stage runner grid, flows in a cold water channel in which the cooling liquid is positioned, flows out from a fluid inlet 9c at the diagonal position of the first-stage runner grid, flows through the same channel, continues to flow through the similar liquid channel, flows into the next stage, also flows in the cold water channel, and circulates;
distilled water flows in from a fluid inlet 12 of a runner grid different from cooling water, reaches a hot water fluid inlet 12a, flows out through a fluid inlet at a diagonal position, and flows out through a hot film frame liquid channel of a film frame, a runner grid liquid channel and a next-stage hot film frame liquid channel, and then enters a fluid inlet of a next-stage runner grid, and at the moment, the distilled water flows out from the fluid inlet at the diagonal position of the first-stage runner grid, continues to flow into a next stage through a similar liquid channel, and circulates (because flowing holes cannot be shown in the figure, the holes are not marked);
the flow direction of the distilled water is opposite to that of the cooling water, namely, independent flow channels of cold water and hot water are established, when the water cooling device operates, condensed water flows out from the water producing small holes 6 positioned below, at the moment, the small holes on the side surfaces can be sealed, and the small holes above are kept open, so that the condensed water can smoothly flow out. During operation, the number of combined layers of the membrane frame and the runner grid can be increased or decreased according to actual needs and operation conditions, such as the pressure and temperature difference of cold and hot water flows and the change of operation parameters, so that the optimal effect is achieved.
Example 3
This example followed the procedure of example 2, distillation was carried out.
Wherein the water inlet pressure of the cooling water is 0.15MPa, the water inlet temperature is controlled by the cooler to be constant at 28 ℃, the water inlet pressure of the hot water is 0.15MPa, and the water inlet temperature is maintained at 50 ℃ by the controllable heater. The condensed water flows out of the water producing small hole 6, the total effective area of the experimental device is 0.25 square meter, and the water producing efficiency is 2.03 liter/square meter/hour when the water producing efficiency is 1.015 liter measured in 2 hours.
Example 4
This example followed the procedure of example 2, distillation was carried out.
Wherein the water inlet pressure of the cooling water is 0.14MPa, the water inlet temperature is controlled by the cooler to be constant at 27 ℃, the water inlet pressure of the hot water is 0.14MPa, and the water inlet temperature is maintained at 49 ℃ by the controllable heater. The condensed water flows out of the water producing small holes 6, and the water producing efficiency is 2.26 liters per square meter per hour.
Example 5
This example followed the procedure of example 2, distillation was carried out.
Wherein the water inlet pressure of the cooling water is 0.16MPa, the water inlet temperature is controlled by the cooler to be constant at 30 ℃, the water inlet pressure of the hot water is 0.16MPa, and the water inlet temperature is maintained at 52 ℃ by the controllable heater. The condensed water flows out from the small holes 6 at the bottom, and the water production efficiency is 1.98 liters per square meter per hour.
In the embodiment, the conductivity of the raw water is 21.5 millisiemens, and the conductivity of the produced water is 3.74 millisiemens, so that the drinking standard is completely met.
Example 6
This example was carried out by concentrating and separating the DMSO aqueous solution in the same manner as in example 2.
Wherein the water inlet pressure of the cooling water is 0.15MPa, and the water inlet temperature is controlled at 15 ℃. Preparing a DMSO aqueous solution with the weight ratio of 0.5% as a distilled liquid, wherein the water inlet pressure of the distilled liquid is 0.15MPa, and the temperature is controlled to be stable at 60 ℃. The condensed water flows out of the water producing small holes 6, and the water producing efficiency is 2.48 liters per square meter per hour. The concentration of DMSO was calibrated by UV spectrometer at 200nm, and the concentration of DMSO in the product water was 0.08%.
The applicant states that the present invention is illustrated by the above examples of the flat plate type membrane distillation apparatus, distillation method and application of the present invention, but the present invention is not limited to the above process steps, i.e., it is not meant that the present invention must rely on the above process steps to be carried out. It will be apparent to those skilled in the art that any modification of the present invention, equivalent substitutions of selected materials and additions of auxiliary components, selection of specific modes and the like, which are within the scope and disclosure of the present invention, are contemplated by the present invention.
Claims (12)
1. A flat-plate membrane distillation device is characterized by comprising a plurality of distillation units, wherein each distillation unit comprises a plurality of membrane frames and a plurality of runner grids;
the two opposite surfaces of the membrane frame are respectively provided with a distillation membrane and a condensation membrane, two adjacent angular positions of the membrane frame are respectively provided with a membrane frame liquid channel, and the membrane frame liquid channel comprises a hot membrane frame liquid channel and a cold membrane frame liquid channel;
the flow channel grating comprises a plurality of linear railings inside, the linear railings divide the flow channel grating to form a plurality of liquid flow channels, fluid inlets are arranged at two opposite corners of the flow channel grating, and a flow channel grating liquid channel is arranged at any one corner adjacent to the fluid inlets;
a flow passage grating is arranged between the condensation film arranged on one surface of the film frame and the condensation film of the next film frame, a flow passage grating is arranged between the distillation film arranged on the other surface of the film frame and the distillation film of the previous film frame, the liquid channels of the film frames are communicated with the liquid channels of the flow passage grating, and a plurality of film frames and a plurality of flow passage gratings are alternately arranged to form a distillation unit;
a support grid is arranged between the distillation film and the condensation film of the film frame, and the support grid is positioned in the center of the film frame;
the side face of the edge of the membrane frame is provided with a plurality of water producing small holes;
the thickness of the tail end of the linear railing in the runner grid is alternately reduced;
the distillation membrane is a polytetrafluoroethylene membrane or a polyvinylidene fluoride membrane;
the condensation film is an ethylene-tetrafluoroethylene copolymer film or a polyester film;
the thickness of the distillation membrane is 100-150 mu m;
the thickness of the condensation film is 40-60 mu m.
2. A flat plate type membrane distillation apparatus according to claim 1, wherein the edges of the membrane frame are provided with membrane frame fitting holes.
3. The flat plate type membrane distillation apparatus according to claim 1,
and a runner grid assembly hole is formed in the edge of the runner grid.
4. The flat plate type membrane distillation apparatus as claimed in claim 1, wherein the length of the membrane frame is 200 to 300 mm.
5. A flat plate type membrane distillation apparatus according to claim 1, wherein the length of the membrane frame is 250 mm.
6. The flat plate type membrane distillation apparatus as claimed in claim 1, wherein the width of the membrane frame is 200 to 300 mm.
7. A flat plate type membrane distillation apparatus according to claim 1, wherein the width of the membrane frame is 250 mm.
8. The distillation method of a flat-plate type membrane distillation apparatus according to any one of claims 1 to 7, wherein the method comprises: cooling liquid flows in from a fluid inlet of the runner grid and flows out from a fluid inlet at an opposite angle, the flowing-out cooling liquid passes through a cold film frame liquid channel of the film frame, a runner grid liquid channel and a next-stage cold film frame liquid channel and then enters a fluid inlet of the next-stage runner grid, and at the moment, the cooling liquid flows out from the fluid inlet at the opposite angle of the runner grid and continues to flow into the next stage for circulation;
the distilled liquid flows in from the fluid inlet of the runner grid different from the cooling liquid and flows out through the fluid inlet positioned at the diagonal position, the flowing distilled liquid enters the fluid inlet of the runner grid of the next stage after passing through the hot film frame liquid channel of the film frame, the runner grid liquid channel and the hot film frame liquid channel of the next stage, and at the moment, the distilled liquid flows out from the fluid inlet positioned at the diagonal position of the runner grid of the first stage and continuously flows into the next stage for circulation;
the distillation liquid flows in the opposite direction to the cooling liquid.
9. The distillation method according to claim 8, wherein the flow pressure of the distillation liquid and the flow pressure of the cooling liquid are each independently 0.1 to 0.2 MPa.
10. Distillation method according to claim 8, wherein the distilled or cooled liquid is discharged from the water-producing pores.
11. Distillation method according to claim 8, characterised in that drying air is blown in at the side of the small holes for water production, remote from the outflow of the liquid after distillation or cooling.
12. Use of the flat-plate type membrane distillation apparatus according to any one of claims 1 to 7 for desalination of sea water or separation of organic solvents.
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| CN205164512U (en) * | 2015-09-15 | 2016-04-20 | 南开大学 | Air -gap membrane distillation plant |
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| JP2011200809A (en) * | 2010-03-26 | 2011-10-13 | Sekisui Chem Co Ltd | Film reactor |
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