KR101679768B1 - Fresh water production apparatus by membrane distillation - Google Patents

Fresh water production apparatus by membrane distillation Download PDF

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Publication number
KR101679768B1
KR101679768B1 KR1020150069583A KR20150069583A KR101679768B1 KR 101679768 B1 KR101679768 B1 KR 101679768B1 KR 1020150069583 A KR1020150069583 A KR 1020150069583A KR 20150069583 A KR20150069583 A KR 20150069583A KR 101679768 B1 KR101679768 B1 KR 101679768B1
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KR
South Korea
Prior art keywords
membrane
seawater
membrane distillation
distillation
module
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KR1020150069583A
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Korean (ko)
Inventor
김승현
최용준
이태민
Original Assignee
경남대학교 산학협력단
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Priority to KR1020150069583A priority Critical patent/KR101679768B1/en
Priority to PCT/KR2016/002957 priority patent/WO2016186308A1/en
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Publication of KR101679768B1 publication Critical patent/KR101679768B1/en

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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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
    • 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
    • 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
    • B01D61/368—Accessories; Auxiliary operations
    • 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

Abstract

The present invention relates to an apparatus for producing fresh water by membrane distillation, and more particularly, to an apparatus for producing fresh water using a membrane distillation module in which steam moves through a pore separation membrane with a vapor pressure difference as a driving force, The present invention relates to a device for manufacturing fresh water by membrane distillation which can maximize energy efficiency by using seawater preheated by heat exchange by simultaneously introducing seawater and phase transition material into the module and minimizing temperature gradient in the membrane distillation module by phase transition material .

Description

[0001] FRESH WATER PRODUCTION APPARATUS BY MEMBRANE DISTILLATION [0002]

The present invention relates to a device for producing fresh water by membrane distillation capable of maximizing energy efficiency.

Water is the most important natural resource of human beings, covering about 75% of the Earth's surface. About 97% of the water on Earth is in the sea, and about two-thirds of the remaining 3% exist as ice caps or glaciers in polar regions.

However, the seawater existing in the sea is too salty to be used for human life or industrial water, and there is very little fresh water available for human life.

Moreover, today's increasing industrialization and subsequent environmental pollution are increasingly reducing the amount of fresh water available to human life, which is increasing the shortage of fresh water and depletion.

Therefore, as a method for solving the lack of fresh water and depletion phenomenon, a method for converting a large amount of seawater into fresh water has been sought as described above, and various seawater desalination apparatuses have been developed in order to implement such a scheme.

Generally, seawater desalination methods are largely divided into three stages: distillation, reverse osmosis, electro-dialysis using an electric field, freezing process using cold energy, and membrane distillation using a hydrophobic membrane ).

The seawater desalination technology using the membrane distillation method is advantageous in that the operation method is simple, high operating pressure is not needed, and the purity of the treated fresh water is high compared to other methods.

In Korean Patent Laid-Open Publication No. 2008-0082627, which is based on the above-mentioned membrane distillation method, the liquid to be concentrated in the multi-stage membrane distillation apparatus is isolated from the vapor space by the membrane and, for setting the absolute pressure of the liquid to be concentrated, There has been disclosed a membrane distillation apparatus constituting a distillation process so that a negative pressure lowering the absolute pressure is applied.

Specifically, a) a negative pressure lowering the absolute pressure of the liquid to be condensed is applied to the liquid to be condensed, b) the pressure of the liquid to be condensed is reduced to the negative pressure, the negative pressure of the distillation process, and c) The liquid is isolated from ambient pressure, and d) the absolute pressure of the liquid drops below the boiling vapor pressure corresponding to that temperature. At this time, the absolute pressure of the liquid entering the membrane distillation process is set to substantially correspond to the pressure in the associated membrane distillation apparatus.

The membrane distillation apparatus is disadvantageous in that it has a low energy efficiency due to a large amount of energy consumed by flowing steamized seawater into the membrane module, and the first and second stages constitute a complex apparatus.

An object of the present invention is to provide a desalination plant capable of maximizing energy efficiency by reducing the amount of energy consumed in the desalination process.

In order to achieve the above object, the present invention provides an apparatus for producing fresh water using a membrane distillation module in which steam is moved through a separator membrane of a pore using a vapor pressure difference as a driving force, wherein the seawater and the phase- And a distillation column for separating the fresh water from the fresh water.

Wherein the membrane distillation module comprises at least one membrane distillation selected from the group consisting of direct contact membrane evaporation (DCMD), air layer membrane distillation (AGMD), gas flow membrane distillation (SGMD) and calibrated membrane distillation Module.

The phase change material may be encapsulated.

The encapsulated phase change material may have a diameter of 5 mm or more.

Wherein the phase transfer material is selected from the group consisting of CaCl 2揃 6H 2 O, Na 2 SO 4揃 10H 2 O, C 28 H 58 (Octacosane), CH 3 COONa 揃 3H 2 O (Sodium Acetate Trihydrate), and paraffin waxes It can be more than a species.

The present invention also relates to a seawater storage tank for storing inflowed seawater; A phase transition material storage tank storing the phase change material; A heating device for heating the sea water and the phase change material supplied from the sea water storage tank and the phase change material storage tank, respectively; A membrane distillation module having a hollow fiber distillation membrane in a vacuum state, the seawater supplied through the heating unit passing through the hollow fiber distillation membrane to generate steam; And a heat exchange device for exchanging heat between the steam generated in the membrane distillation module and seawater supplied from the seawater storage tank to produce fresh water. The present invention also provides an apparatus for producing fresh water by membrane distillation.

The phase change material may be encapsulated.

The encapsulated phase change material may have a diameter of 5 mm or more.

Wherein the phase transfer material is selected from the group consisting of CaCl 2揃 6H 2 O, Na 2 SO 4揃 10H 2 O, C 28 H 58 (Octacosane), CH 3 COONa 揃 3H 2 O (Sodium Acetate Trihydrate), and paraffin waxes It can be more than a species.

The heat exchanging device may further include a preheated seawater transferring part for inputting the preheated seawater to be heat-exchanged and discharged to the heating device.

The heat exchange may be performed at a portion where the steam moving unit into which the steam generated in the membrane distillation module flows and the seawater moving unit into which the seawater supplied from the seawater storage tank flows is contacted.

The membrane distillation module includes a body equipped with a hollow fiber distillation membrane, an upper cap and a lower cap covering upper and lower portions of the body, respectively, and a pump for discharging the gas present in the membrane distillation module to the outside, The inside of the distillation module can be kept in a vacuum state.

The hollow fiber distillation membrane may include a hollow fiber bundle having a plurality of hollow fiber membranes, and a module case for housing the bundle of hollow fibers.

The membrane distillation module may be arranged in series with the heat exchanger.

The membrane distillation module may include two or more membrane distillation modules.

The apparatus for producing fresh water according to the present invention uses seawater preheated by heat exchange between steam generated from a membrane distillation module and seawater as a raw material and minimizes temperature gradient in the membrane distillation module by phase transition material to maximize energy efficiency There is an advantage to be able to.

In addition, the apparatus for producing fresh water according to the present invention is advantageous in that the film density is higher than that of a conventional flat membrane using a membrane distillation module equipped with a hollow fiber distillation membrane.

Further, the apparatus for producing fresh water according to the present invention is advantageous in that the membrane distillation and the heat exchange are simultaneously performed therein, thereby simplifying and simplifying the processes compared to the conventional processes separately performed.

1 is a schematic view of a fresh water producing apparatus according to an embodiment of the present invention.
Figure 2 shows a schematic diagram of a membrane distillation module in which (a) direct contact membrane evaporation (DCMD), (b) air bed membrane distillation (AGMD), (c) gas flow membrane distillation (SGMD) Formal membrane distillation (VMD).

The present invention relates to a device for producing fresh water by membrane distillation capable of maximizing energy efficiency.

Specifically, the apparatus for producing fresh water by membrane distillation according to the present invention is an apparatus for producing fresh water by using a membrane distillation module in which steam moves through a separation membrane of pores using a vapor pressure difference as a driving force, Phase transition material at the same time.

The membrane distillation module is divided into four types depending on the method of generating the vapor pressure difference and the membrane permeation configuration, specifically, direct contact membrane evaporation (DCMD), air layer membrane distillation (AGMD), gas flow membrane distillation Distillation (VMD) (Fig. 2).

The DCMD (Direct Contact MD) is widely used because of its simple process and high permeate permeability. Specifically, it is a method in which evaporation and condensation occur simultaneously at the film surface by directly contacting the hot influent in the liquid state and the cold treated water. Such a DCMD is divided into a flat sheet, a capillary, or a hollow fiber (Fig. 2 (a)).

The AGMD (Air Gap MD) is an improvement of the problem of heat transfer and mass transfer which is a disadvantage of DCMD, and the condensed surface is separated from the film due to air gap. In other words, a thin air layer is placed on the treated water side (between the cold treated water and the membrane) to prevent heat from being transmitted. The air layer serves as a medium for transporting and transferring the water vapor passing through the membrane (Fig. 2 (b)).

The SGMD (Sweep Gas MD) is similar to DCMD but has a condensed surface formed by a cold sweep gas. Continuous flow of cold inert gas through the water vapor through the separator allows for faster condensation. In other words, the sweep gas carries and condenses the gas passing through the separation membrane, specifically, an inert gas such as nitrogen and argon can be used (FIG. 2C).

The SGMD has a separate collecting device for collecting the sweep gas. When separating the gas other than the liquid, a process of separating the gas from the sweep gas is added.

The VMD (Vacuum MD) employs a gas in a vacuum state to apply a vacuum gas to the treated water to form a higher pressure difference to increase the flux. The VMD requires a separate device (Fig. 2 (d)) in which a closed chamber is provided on the treated water side of the module to keep the internal environment in a vacuum state and to collect vapor permeated through the membrane.

The phase change material may be encapsulated, and the encapsulated phase change material may have a diameter of 5 mm or more. The phase change material is selected from the group consisting of CaCl 2 .6H 2 O, Na 2 SO 4 .10H 2 O, C 28 H 58 (Octacosane), CH 3 COONa 3H 2 O (Sodium Acetate Trihydrate), and paraffin waxes It may be more than one kind. These phase transition materials are described in more detail below.

Hereinafter, a fresh water producing apparatus according to an exemplary embodiment of the present invention will be described in detail with reference to the accompanying drawings.

1 is a schematic view of a fresh water producing apparatus according to an embodiment of the present invention.

1, the apparatus 10 for producing fresh water according to the present invention includes a seawater reservoir 20 for storing seawater introduced thereinto; A phase transition material storage tank (60) for storing a phase change material; A heating device 30 for heating seawater supplied from the seawater storage tank 20 and the phase change material storage tank 60 and a heating device for heating the phase change material, respectively; a heating device 30 for heating seawater supplied from the seawater storage tank 20; A membrane distillation module (40) having a hollow fiber distillation membrane (41) in a vacuum state, the seawater supplied through the heating unit (30) passing through the hollow fiber distillation membrane (41) and generating steam; And a heat exchanger (50) for exchanging heat between the steam generated in the membrane distillation module (40) and seawater supplied from the seawater reservoir (20) to produce fresh water.

The desalination plant 10 according to the present invention simultaneously employs a membrane distillation module 40 having a hollow fiber distillation membrane 41 and a heat exchanger 50 while performing a vacuum membrane distillation process.

Specifically, the present invention can improve the degree of integration of a membrane module compared to a conventional membrane by using hollow fiber as a membrane used for membrane distillation.

In addition, the membrane distillation module 40 and the heat exchanging device 50 are simultaneously employed, so that the device configuration is simplified and simplified compared with the conventional one.

Also, since the temperature gradient inside the module is minimized by introducing the seawater preheated by the heat exchanger 50 using seawater as a coolant and the phase change of the phase transition material introduced together with seawater into the membrane distillation module Energy efficiency can be maximized.

The seawater storage tank 20 serves to store the seawater introduced from the outside. The seawater storage tank 20 is not particularly limited as long as it has a shape capable of storing seawater, but may be cylindrical or rectangular, for example.

The seawater stored here is not particularly limited as long as the water contains saline. However, in order to minimize the occurrence of fouling or scale occurring in the hollow fiber membrane to be described later, the seawater may be filtered or further pretreated by FO or the like.

The phase transition material storage tank 60 serves to store the phase transition material flowing along with the seawater. The phase change material storage tank 60 is not particularly limited as long as a space for storing the phase change material can be provided.

It is preferred that the phase change material is encapsulated and incorporated in the capsule so as not to affect the membrane distillation during the state change. The content of the phase transition material contained in the capsules is not particularly limited, and is preferably within a range that does not affect the shape of the capsules when the state changes. The composition of the capsule is preferably selected in consideration of the reactivity with seawater, the reactivity in the film distillation process conditions (temperature, pressure, time), and the like.

Preferably, the encapsulated phase change material has a diameter of 5 mm or more, preferably 5 mm to 50 mm. If the diameter is less than 5 mm, the hollow fiber membrane may be damaged and the efficiency of membrane distillation may be lowered.

Wherein the phase transfer material is selected from the group consisting of CaCl 2揃 6H 2 O, Na 2 SO 4揃 10H 2 O, C 28 H 58 (Octacosane), CH 3 COONa 揃 3H 2 O (Sodium Acetate Trihydrate), and paraffin waxes It can be more than a species.

The phase transition material serves to raise the temperature of the seawater degraded by the heat generated when the phase of the seawater is changed from the liquid phase to the solid phase in the membrane distillation module described later. Specifically, in the membrane distillation module, the temperature of the heated seawater flowing in from the upper part is lowered as the temperature is lowered, and the membrane distillation efficiency is lowered. To improve this, the temperature of the seawater is increased by the heat of the phase transition material causing the phase change to a certain temperature, thereby minimizing the temperature gradient inside the membrane distillation module, thereby improving the efficiency of membrane distillation.

The heating device 30 serves to heat seawater supplied from the seawater storage tank 20, seawater preheated by heat exchange, and phase change material supplied from the phase transition material storage tank 60. The seawater preheated by the heat exchange is supplied through the preheated seawater transfer unit 53 of the heat exchange unit 50.

 The heating device 30 preferably heats the seawater to an optimal temperature for performing the membrane distillation process in the membrane distillation module 40, which will be described later.

Specifically, the temperature is preferably 50 to 90 占 폚. If the temperature is less than 50 ° C, the temperature is low and evaporation may be difficult in the membrane distillation module 40. If the temperature is more than 90 ° C, the energy efficiency may be significantly reduced.

The heating device 30 is not particularly limited as long as it is commonly used in the related art. For example, a heater, a heat collecting device using solar light, or the like can be applied to the heating device 30, and a heat collecting device using sunlight is more preferably applied to reduce energy consumption.

The membrane distillation module 40 serves to generate steam from the seawater and the phase transition material supplied through the heating device 30.

The membrane distillation module 40 includes a body 42 provided with a hollow fiber distillation membrane 41 in a vacuum state and an upper cap 43 and a lower cap 44 covering upper and lower portions of the body 42, do.

The membrane distillation module includes a seawater inlet through which heated seawater flows, a steam outlet through which the steam distilled by the hollow fiber distillation membrane is discharged, and a seawater outlet through which the remaining seawater is discharged after being distilled by the hollow fiber distillation membrane . The positions of the seawater inlet, the steam outlet and the seawater outlet are not particularly limited and may be provided at a position where the seawater can be easily introduced, the steam is discharged, the seawater is discharged, and the vacuum state of the membrane distillation module can be maintained smoothly.

Part of the introduced seawater is discharged as steam by the hollow fiber distillation membrane, and the remainder is discharged through the seawater outlet. In the case of using multiple membrane distillation modules, the seawater discharged from one membrane distillation module can be used as the influent of another membrane distillation module.

The heat-treated seawater passes through the hollow fiber distillation membrane 41 provided in the body 42 so that the concentrated water in the seawater is separated from the membrane surface, and only the vapor passes through the pores of the membrane and is released.

At this time, the size of the membrane distillation module 40 can be appropriately changed according to the inflow amount of the seawater to be treated, but it is preferable that sufficient space remains even after the hollow fiber distillation membrane 41 is provided inside the body 42 . This is to ensure a space in which the heat-treated seawater can circulate before passing through the hollow fiber distillation membrane 41.

In addition, at least one membrane distillation module 40 may be provided. If the number is two or more, it is possible to arrange them freely in consideration of efficiency within a range not deviating from the object of the present invention.

The hollow fiber distillation membrane 41 of the membrane distillation module 40 may include a hollow fiber bundle 41a having a plurality of hollow fiber membranes and a module case 41b for housing the hollow fiber bundle 41a. have. The number of the hollow fiber bundles and the membrane distillation modules to be accommodated is suitably adjusted in consideration of the desired production amount of fresh water and installation standards of the apparatus.

The membrane distillation module 40 having the above-described structure is provided with the hollow fiber distillation membrane 41, so that it is possible to secure a large membrane area per unit volume as compared with the conventional membrane.

In addition, the hollow fiber distillation membrane 41 is preferably formed of a hydrophobic polymer material so that only steam passes without passing water.

For example, the hollow fiber distillation film 41 is preferably formed of at least one material selected from the group consisting of polyethylene, polypropylene, polyvinylidenedifluoride, and polytetrafluoroethylene, more preferably polytetrafluoroethylene . The polytetrafluoroethylene is a chemically stable polymer and can perform powerful chemical cleaning when fouling or scale removal occurs in the hollow fiber membrane.

The size of the hollow fiber distillation membrane 41 is preferably selected in consideration of the pressure loss, membrane strength, and filling efficiency, such as the size of the outer diameter and inner diameter, the pore size of the hollow fiber distillation membrane 41, and the like.

The module case 41b for accommodating the hollow fiber bundle 41a may be formed of a material commonly used in the related art, for example, stainless steel having excellent impact resistance and reusability.

The membrane distillation module 40 thus configured maintains the interior thereof in a vacuum state. Specifically, the lower cap 44 may be provided with a pump 45 for discharging the gas present in the membrane distillation module 40 to the outside, thereby maintaining the inside of the membrane distillation module 40 in a vacuum state.

As described above, the membrane distillation module 40 in which the interior is kept in a vacuum can generate steam at a boiling point lower than the boiling point of seawater, and at the same time can improve the evaporation rate.

The steam generated in the membrane distillation module 40 is transferred to the heat exchanger 50 to be described later by the steam passage 46 integrally coupled to the lower portion of the lower cap 44.

The heat exchanger 50 performs heat exchange between steam generated in the membrane distillation module 40 and seawater supplied from the sea water storage tank 20 to produce fresh water.

The heat exchanger (50) is a device that performs heat exchange between fluids by directly contacting two low temperature and high temperature fluids with different temperatures. In the present invention, in consideration of the heat exchange efficiency of the heat exchange device 50, the low-temperature fluid may be seawater at about 5 to 25 ° C, and the high-temperature fluid may be steam at about 40 to 80 ° C.

The heat exchanger 50 can be applied to a structure generally employed in the related art, and can be easily formed by a person skilled in the art, so a detailed description thereof will be omitted.

The heat exchange in the heat exchange unit 50 is performed by a steam moving unit 51 in which the steam generated in the membrane distillation module 40 flows into the steam passage 46 and the sea water supplied from the sea water storage tank 20 Can be performed at the portion where the incoming seawater moving section (52) touches. At this time, the steam of the steam moving part 51 and the seawater of the seawater moving part 52 preferably flow in / out in opposite directions. For example, the steam of the steam moving part 51 may flow from the lower part to the upper part, and the seawater of the seawater moving part 52 may flow in / out from the upper part to the lower part.

In this way, steam is condensed to produce fresh water by heat exchange between the steam and the seawater. In the seawater moving unit 52, the heat-exchanged and preheated seawater is passed through the preheating seawater transfer unit 53, 30).

Although not shown in the drawing, the produced fresh water is stored in a separate fresh water storage tank and can be used for domestic water, industrial water, and agricultural water.

At this time, seawater as a raw material for desalination is used as a refrigerant for condensing the steam, so that the cost of procuring the refrigerant is not required.

The membrane distillation module 40 may be arranged in series with the heat exchanger 50 and the membrane distillation module 40 and the heat exchanger 50 may be provided in one unit set, And may be provided in plural.

The membrane distillation module 40 and the heat exchanger 50 may be provided in consideration of the amount of seawater to be treated and the treatment efficiency.

Here, all the fluid flowing in the fresh water producing apparatus 10 of the present invention can be introduced and discharged through a supply line (not shown).

The fresh water producing apparatus 10 according to the present invention having the above-described structure can improve the permeability of the membrane by the hollow fiber distillation membrane 41 and perform heat exchange between steam and seawater by the heat exchanger 50, This is possible.

It will be understood by those skilled in the art that the foregoing description of the present invention is for illustrative purposes only and that those of ordinary skill in the art can readily understand that various changes and modifications may be made without departing from the spirit or essential characteristics of the present invention. will be. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive. For example, each component described as a single entity may be distributed and implemented, and components described as being distributed may also be implemented in a combined form.

The scope of the present invention is defined by the appended claims rather than the detailed description and all changes or modifications derived from the meaning and scope of the claims and their equivalents are to be construed as being included within the scope of the present invention do.

10: Desalination plant
20: Sea water storage
30: Heating device
40: Membrane distillation module 41: Hollow fiber distillation membrane
41a: hollow fiber bundle 41b: module case
42: body 43: upper cap
44: Lower cap 45: Vacuum pump
46: Steam channel
50: Heat exchanger 51: Steam moving part
52: Seawater transfer section 53: Preheated seawater transfer section
60: phase transition material storage tank

Claims (15)

delete delete delete delete delete A seawater reservoir for storing incoming seawater;
A phase transition material storage tank storing an encapsulated phase change material having a diameter of 5 mm to 50 mm;
A heating device for heating the sea water and the phase change material supplied from the sea water storage tank and the phase change material storage tank, respectively;
A membrane distillation module having a hollow fiber distillation membrane in a vacuum state, the seawater supplied through the heating unit passing through the hollow fiber distillation membrane to generate steam;
And a heat exchange device for exchanging heat between the steam generated in the membrane distillation module and seawater supplied from the sea water storage tank to produce fresh water,
Wherein the phase change material is at least one selected from the group consisting of CaCl2.6H2O, Na2SO4 · 10H2O, C28H58 (Octacosane) and CH3COONa · 3H2O (Sodium Acetate Trihydrate)
The membrane distillation module includes a body equipped with a hollow fiber distillation membrane, an upper cap and a lower cap covering upper and lower portions of the body, respectively, and a pump for discharging the gas present in the membrane distillation module to the outside, The inside of the distillation module is kept in a vacuum state,
Wherein the hollow fiber distillation membrane comprises a hollow fiber bundle having a plurality of hollow fiber membranes, and a module case for housing the bundle of hollow fibers,
Wherein the heat exchanger includes a preheated seawater transfer unit for inputting preheated seawater, which is heat-exchanged and discharged, into a heating device,
The heat exchange is performed in a portion where the steam moving part into which the steam generated in the membrane distillation module flows and the sea water moving part into which the sea water supplied from the sea water storage tank flows,
Wherein the membrane distillation module is arranged in series with the heat exchanger.
delete delete delete delete delete delete delete delete [7] The apparatus for producing fresh water by membrane distillation according to claim 6, wherein the membrane distillation modules are provided in two or more.
KR1020150069583A 2015-05-19 2015-05-19 Fresh water production apparatus by membrane distillation KR101679768B1 (en)

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PCT/KR2016/002957 WO2016186308A1 (en) 2015-05-19 2016-03-24 Fresh water production apparatus using membrane distillation

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102215050B1 (en) * 2019-09-16 2021-02-10 한국과학기술연구원 Apparatus for membrane distillation using solar absorber and heat pump
KR102217318B1 (en) * 2019-09-02 2021-02-18 한국과학기술연구원 Apparatus for membrane distillation using solar absorber

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
Hawlader. Encapsulated phase change materials for thermal energy storage:Experiments and simulation. International Journal of Energy Research. 2002, 26, 159-171*
Joo&Kwak. Experimental evaluation for the freshwater production characteristics according to the salinity conditions of vacuum membrane distillation module. DWT. 2015.04.29, 57, 10005-10011*
Mohan. Solar Desalination with Latent Heat Storage Materials and Solar Collector. Journal of Mechanics Engineering and Automation. 2011, 1, 126-134*
Summers. Cycle performance of multi-stage vacuum membrane distillation(MS-VMD) systems. IDA world congress on desalination and water reuse. 2013, TIAN13-202*

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102217318B1 (en) * 2019-09-02 2021-02-18 한국과학기술연구원 Apparatus for membrane distillation using solar absorber
KR102215050B1 (en) * 2019-09-16 2021-02-10 한국과학기술연구원 Apparatus for membrane distillation using solar absorber and heat pump
US11052349B2 (en) 2019-09-16 2021-07-06 Korea Institute Of Science And Technology Apparatus for membrane distillation using solar absorber and heat pump

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