CN101993123A - Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure - Google Patents

Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure Download PDF

Info

Publication number
CN101993123A
CN101993123A CN2009100905510A CN200910090551A CN101993123A CN 101993123 A CN101993123 A CN 101993123A CN 2009100905510 A CN2009100905510 A CN 2009100905510A CN 200910090551 A CN200910090551 A CN 200910090551A CN 101993123 A CN101993123 A CN 101993123A
Authority
CN
China
Prior art keywords
water
separated
evaporation
liquid level
condensation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN2009100905510A
Other languages
Chinese (zh)
Inventor
杨宇飞
袁卫星
袁修干
王晶
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beihang University
Beijing Institute of Space Launch Technology
Original Assignee
Beihang University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Beihang University filed Critical Beihang University
Priority to CN2009100905510A priority Critical patent/CN101993123A/en
Publication of CN101993123A publication Critical patent/CN101993123A/en
Pending legal-status Critical Current

Links

Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124Water desalination
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124Water desalination
    • Y02A20/138Water desalination using renewable energy
    • Y02A20/142Solar thermal; Photovoltaics
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/20Controlling water pollution; Waste water treatment
    • Y02A20/208Off-grid powered water treatment
    • Y02A20/212Solar-powered wastewater sewage treatment, e.g. spray evaporation
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Abstract

The invention aims to provide a device for distilling and separating water evaporated/boiled under negative pressure. The device has low heating temperature, high efficiency and low cost. The invention provides a scheme, which ensures that the needed negative pressure can be produced in the sea water desalinization systems without vacuum pumps, thus reducing the boiling temperature of the water solution to 30-50 DEG C. The water solution can be boiled as long as the temperature of the heating source is higher than 30-50 DEG C. The heating source for heating and evaporating the water solution in the invention can be water from solar heat collectors, tail water with higher temperature from the power plants, chemical plants, smelting plants and the like or water completing heat exchange with the residual heat from the power plants, chemical plants and smelting plants. The temperature of the heating fluid needed by the invention can be lower than 60 DEG C, preferably 37 DEG C, thus effectively utilizing the solar energy or largely recovering and utilizing the industrial residual heat and having great value in environmental protection and energy saving.

Description

The negative pressure evaporation water fractionation by distillation device that low temperature heat energy drives
Technical field
The present invention relates to the negative pressure evaporation water fractionation by distillation device that a kind of low temperature heat energy drives, specifically is a kind ofly to utilize low-temperature heat sources such as sun power, used heat that water to be separated (as seawater, impure water, contain polluted water or the like) is carried out isolation of purified to handle.
Background technology
Existing method for purifying water has distillation method, electrolytic process, reverse osmosis method etc.Distillation method is to utilize thermal source to heat water to be separated (as seawater, impure water, contain polluted water or the like, below also be referred to as " water to be separated "), to distill out water vapor, then with this water vapor condensation to be purified the method for fresh water.Because the boiling point of water therefore in order to obtain a large amount of water vapors, must adopt high temperature heat source (as fire coal, fuel oil etc.) just heating can achieve the goal up to 100 ℃ under normal pressure.Electrolytic process is meant earlier with direct current electrolysis water to be separated, obtaining oxygen and hydrogen, and then makes oxygen and combustion of hydrogen to generate the method for fresh water.No matter be distillation method or electrolytic process, all need to consume a large amount of high-grade energies.But reverse osmosis method is to utilize the permeate water molecule and can not see through the film of other compound molecule to isolate the method for fresh water, has the few advantage of energy consumption, but the price of filtering membrane is too expensive, and the life-span is not long, easily contaminated, thereby has limited its application.
In the process of carrying out the water sepn purification with distillation, in order to reduce or to avoid using fuel to heat water to be separated, the water water separating method to be separated of many use sun power is developed.The common ground of these methods is to utilize solar energy collector to collect the energy in the sunlight, removes to heat water to be separated with this thermal source then.But because the water temp to be separated that obtains of solar energy collector can not too high (generally being lower than 100 ℃), so the fresh water productive rate of solar seawater desalination system is not high usually.The heat-collecting temperature that improves solar energy collector is seemingly feasible, as adopt condensing apparatus can make the temperature out of solar energy collector reach 200-300 ℃, but the condensing apparatus processing difficulties, and need carry out solar tracking etc., cause it to cost an arm and a leg, be difficult to large-scale application equally.
Because the boiling point of water is directly related with its residing pressure, therefore try every possible means to reduce the pressure of system in the water fractionation by distillation process, just can effectively reduce the boiling temperature of water to be separated, so promptly use the very low flat type solar heat collector of heat-collecting temperature also can heat effectively to it, until the above temperature of its boiling point, the output capacity of fractionation by distillation water is improved.
The pressure that reduces the fractionation by distillation system is generally taked the method for finding time, and utilizes a cover vacuum pump system that the distiller upper space is vacuumized to cause negative pressure.Though reduced evaporation of water temperature to be separated, make system very complex, safeguard to be difficult for that the operation of vacuum pump also needs to consume a large amount of high-grade electric energy.
Summary of the invention
The objective of the invention is to overcome deficiency and the defective that exists in the existing distillation type water sepn purification techniques, the negative pressure evaporation water fractionation by distillation device of the low temperature heat energy driving of a kind of high-level efficiency, low cost, low Heating temperature is provided.
The present invention proposes a kind of scheme, making does not need to use vacuum pump promptly can produce required negative pressure in seawater desalination system, thereby the boiling temperature of water to be separated is reduced to 30-50 ℃ level, is higher than this value, just can make water boiling to be separated as long as heat the temperature of thermal source.
The negative pressure evaporation water fractionation by distillation device that low temperature heat energy according to an embodiment of the invention drives mainly comprises an evaporator-condenser, a water receptacle to be separated, and one is separated tail water container, a condensed water container.
Evaporator-condenser is a core apparatus of the present invention, and it is installed on the position than water liquid level to be separated and the high about 8-10 rice of water of condensation liquid level.Evaporator-condenser comprises evaporation part and condensation part, water to be separated is evaporation part evaporation (especially and preferably explosive evaporatoin), the water vapor that the produces portion's condensation that is condensed immediately, the water of condensation of generation is collected by the condense water disk of bottom, condensation part, and this water of condensation is the purification fresh water that will produce.
Evaporator-condenser is an encloses container, by three pipelines respectively with water receptacle to be separated, separate the tail water container, condensed water container communicates.Its annexation is: the evaporation part by two pipelines respectively with water receptacle to be separated with separate the tail water container and link to each other, condense water disk links to each other with condensed water container by a pipeline, the opening of all pipelines is all below the liquid level of corresponding container.
Water receptacle to be separated, separation tail water container communicate with atmosphere with the liquid level of condensed water container.Water receptacle to be separated, separation tail water container and condensed water container all are equiped with upflow tube, the aperture position of upflow tube more than the aperture position of above-mentioned three pipelines, with the liquid level of keeping three containers at certain altitude.
Key of the present invention is to reduce the pressure of evaporator-condenser, with effective reduction vaporization temperature and condensing temperature, thereby reduces the temperature that heats thermal source in the vaporizer.The present invention utilizes the difference between normal atmosphere and evaporation/condensation liquid level and three the nearly 10 meters high water column pressure that vessel level produced to realize.
According to an aspect of the present invention, the negative pressure evaporation water fractionation by distillation device that provides a kind of low temperature heat energy to drive is characterized in that comprising:
The container for evaporation of a sealing,
A water liquid level retaining part to be separated,
Article one, water lines to be separated is used to make described water liquid level retaining part to be separated and the mutually airtight connection in the inside of described container for evaporation,
One is separated tail water liquid level retaining part,
Article one, separate the tail water pipeline, be used to make described separation tail water liquid level retaining part and the mutually airtight connection in the inside of described container for evaporation,
Be located at the generating tube tank nest in the described container for evaporation,
Be located at the cooling tube bundle on spatial top in the described container for evaporation,
Be located at the condense water disk of described cooling tube bundle below,
A water of condensation liquid level retaining part,
, a condensate line is used to make interior airtight connection of desalination water of described water of condensation liquid level retaining part and described condense water disk.
Description of drawings
Fig. 1 is a specific embodiment of the present invention.
Embodiment
From application of the present invention, the water that the negative pressure evaporation water fractionation by distillation device that is suitable for driving with low temperature heat energy of the present invention is handled includes, but is not limited to:
-seawater;
The landlocked surface water or the underground water of-salt concentration;
-be contained in the contaminated surface water or the underground water of the solute of non-vaporising under the water boiling point temperature;
-other the water that is contained in the solute of non-vaporising under the water boiling point temperature;
-or the like.
" water to be separated " in the present specification can be the water of (but being not limited to) above-mentioned any kind.
In the embodiment of the invention as shown in Figure 1, in the tubular container for evaporation 1 of a sealing, be provided with generating tube tank nest 7 and cooling tube bundle 2.Condenser bundles 2 arranged beneath have condense water disk 3, are used for receiving and the splendid attire condensed water.Container 16 is water storage tanks to be separated, is used to store isolating water to be distilled.Container 18 is to separate the tail water storage tank, is used to deposit the separation tail water through after the fractionation by distillation.Container 20 is water of condensation storage tanks, is used to deposit the fresh water of generation.
The liquid level of water storage tank 16 to be separated, separation tail water storage tank 18, water of condensation storage tank 20 is communicated with atmosphere.Water storage tank 16 to be separated separates tail water storage tank 18 by linking to each other with container 1 communicating pipe 9 by linking to each other with container 1 communicating pipe 8, and water of condensation storage tank 20 is by linking to each other with condense water disk 3 communicating pipe 10.The lower ending opening of communicating pipe 6, communicating pipe 9 and communicating pipe 12 all is positioned at the liquid level of corresponding storage tank with upper/lower positions.
When system reached balance, below relation was set up:
p v+p w=p B
P in the formula vRepresent the pressure of the gaseous space that container 1 top forms by water vapor, p wFor height is the pressure that fluid column produced of H, p BBe normal atmosphere.Thus formula as can be known, the pressure of gaseous space 5 is negative pressure.
As a typical operating conditions, be that the situation of seawater is an example with water to be separated, establishing normal atmosphere is 101325Pa (this is the value of 1 standard atmospheric pressure), sea water density is 1.02 * 10 3Kg/m 3(urnormal density), liquid level 6 is 9.5m with the discrepancy in elevation of the liquid level of water storage tank to be separated, and then the pressure of the gaseous space 5 on the liquid level 6 is about 6300Pa, and the temperature of saturation of Dui Ying water vapour is about 37 ℃ with it.As long as therefore make the temperature of the heating fluid of the generating tube tank nest 7 of flowing through be higher than 37 ℃, just can make seawater boiling to be separated.Generally getting the heating temperature difference is 3-10 ℃, and the temperature of promptly getting heating fluid is 40-47 ℃.This temperature is more much lower than the boiling temperature (100 ℃) of water under the normal pressure, and common solar energy collector promptly can satisfy this requirement.Equally, as long as make the temperature of the cooling fluid in the cooling tube bundle 2 of flowing through be lower than 37 ℃, just can make water vapor become liquid water at the surface condensation of cooling tube bundle 2.Generally getting the condensation temperature difference is 3-10 ℃, and the temperature of promptly getting cooling fluid is 27-34 ℃.Cooling fluid can use the seawater (its year-round average temperature is lower than 37 ℃) under the state of nature, or the atmosphere in the environment for use (its year-round average temperature also is lower than 37 ℃).
In the embodiment in figure 1, cooling fluid is a water to be separated.The low temperature water to be separated that comes from environment (sea, river, the face of land/underground water source etc.) enters water storage tank 16 to be separated through valve 13 and pipe 14.(part is prepared deletion in expanding number:, be transported in the cooling tube bundle 2 through pump 25, take away the heat that discharges in the water recovery process, return water storage tank 16 to be separated then.The benefit of doing like this is that the heat in the condensation process is used to heat the water to be separated in the water storage tank 16 to be separated, improves the utilization ratio of heat.But the seawater temperature in the water storage tank 16 to be separated can not rise De Taigao, otherwise is unfavorable for the condensation of water vapor, must limit the top temperature of seawater in the water storage tank 16 to be separated for this reason.This can realize with mixing recently of hot sea water thereby regulate low temperature seawater by the aperture of regulated valve 26 with valve 27.
In the present embodiment, though the installation site of evaporation-condensation container 1 is higher, but because of the water sucking mouth of water inlet pipe 8 below the liquid level of water storage tank 16 to be separated, made full use of siphonage, therefore 25 need of pump overcome the resistance acting of pipeline along journey, and need not overcome gravity acting, so wasted work is few.)
According to embodiments of the invention shown in Figure 1, water to be separated is being entered elder generation and interchanger 10 heat exchange between the container 1 by water storage tank 16 to be separated, thereby improves temperature; The separation tail water that leaves container 1 simultaneously is by water cooling to be separated, and temperature reduces.Make the heat that separates in the tail water obtain reclaiming like this, improved heat utilization ratio.Interchanger 10 can be any liquid-liquid interchanger such as double-tube heat exchanger, plate-type heat exchanger, shell and tube heat exchanger, plate-fin heat exchanger, or their combination.
After the water evaporation to be separated in the container for evaporation 1, its liquid level 6 can descend, but owing to atmospheric effect, has new water to be separated and replenish into continuously through water inlet pipe 8 in water storage tank 16 to be separated.When the liquid level of water storage tank 16 to be separated descends, float(ing)valve 15 will be opened, and make the water to be separated from the water source enter water storage tank 16 to be separated through valve 13 and pipeline 14, for water storage tank 16 to be separated replenishes.Water storage tank 16 to be separated also is equipped with upflow tube 17, unnecessary water to be separated is flowed out, thereby the liquid level of water storage tank 16 to be separated is kept within a certain height all the time.
The separation tail water of after separating can by the bottom of container 1 (because of the water-mass density of container for evaporation 1 bottom higher) drop to along draft tube 9 and to separate in the tail water storage tank 18.Separate tail water storage tank 18 upflow tube 19 is housed, the liquid level of keeping separation tail water storage tank 18 all the time is at certain altitude.
The effect of the upflow tube 21 on the water of condensation storage tank 20 is also identical, can keep the liquid level of water of condensation storage tank 20 all the time at certain altitude.
When the Various Seasonal of normal atmosphere in the different periods or 1 year in one day changes, or the water temperature in the water storage tank to be separated is when constantly changing with environment, can cause the Level Change of the water liquid level 6 to be separated in the container 1, and then cause the fluctuation of working parameters such as system's evaporation pressure.The height of liquid level 6 can be controlled by the flow through temperature or the flow of heating fluid of generating tube tank nest 7 of adjusting.When liquid level 6 is too high, illustrate that the pressure of the water vapor 5 in the container 1 reduces, need to improve the temperature of the heating fluid of the generating tube tank nest 7 of flowing through this moment, or strengthen the flow of the heating fluid of the generating tube tank nest 7 of flowing through.Otherwise, cross when low the temperature of the heating fluid of the generating tube tank nest 7 that need reduce to flow through, or the flow of the heating fluid of the generating tube tank nest 7 that reduces to flow through when liquid level 6.
Flow through the heating fluid that is used to heat and evaporate seawater of generating tube tank nest 7, can be water from solar energy collector, also can be the higher tail water of temperature of power station, chemical plant, smeltery etc., or carry out water after the heat exchange with the waste heat of power station, chemical plant, smeltery.
If the waste heat of power station, chemical plant, smeltery directly is discharged in the environment, can cause the serious environmental thermal pollution, this thermal pollution has become serious global environment problem at present.On the other hand, because the temperature of these waste heat of plant is lower, still lack effective means so far to its recycling.Because the temperature of heating fluid required for the present invention can only be 40-47 ℃, can recycle above-mentioned industrial exhaust heat effectively in a large number, thereby have great value aspect environmental protection.
In the embodiment of the invention as shown in Figure 1, a pump 11 is used to make cooling-water flowing overcooling tube bank 2, to take away the heat that discharges in the water recovery process.The water to be separated of evaporation/condensation container 1 bottom evaporates and preferably explosive evaporatoin under the heating of heating tube bundle 7; The water vapor that evaporation is generated is condensed into water of condensation at cooling tube bundle 2 places, falls in the condense water disk 3, arrives water of condensation storage vessel 20 through condensate line 10 again.
According to a specific embodiment, the water coolant that flows through cooling tube bundle 2 is directly from the water source of described water to be separated.
According to a specific embodiment, cooling tube bundle 2 and water storage vessel to be separated 16 are communicated with, and are used for making the water to be separated after cooling tube bundle 2 heat absorptions to enter water storage vessel 16 to be separated.

Claims (7)

1. negative pressure evaporation water fractionation by distillation device that available low temperature heat energy drives is characterized in that comprising:
The evaporation/condensation container (1) of a sealing,
A water liquid level retaining part to be separated (16),
, a water lines to be separated (8) is used to make the mutually airtight connection in inside of described water liquid level retaining part to be separated (16) and described evaporation/condensation container (1),
One is separated tail water liquid level retaining part (18),
Article one, separate tail water pipeline (9), be used to make the mutually airtight connection in inside of described separation tail water liquid level retaining part (18) and described evaporation/condensation container (1),
Be located at the generating tube tank nest (7) in the described evaporation/condensation container (1),
Be located at the cooling tube bundle (2) on the interior spatial of described evaporation/condensation container (1) top,
Be located at the condense water disk (3) of described cooling tube bundle (2) below,
A water of condensation liquid level retaining part (20),
, a condensate line (10) is used to make interior airtight connection of desalination water of described water of condensation liquid level retaining part (20) and described condense water disk (3).
2. negative pressure evaporation water fractionation by distillation device as claimed in claim 1, it is characterized in that described evaporation/condensation container (1) is set at suitable height, is subatmospheric negative pressure thereby make described negative pressure evaporation water fractionation by distillation device pressure in the described evaporation/condensation container (1) when reaching balance.
3. negative pressure evaporation water fractionation by distillation device as claimed in claim 2 is characterized in that:
Described water liquid level retaining part to be separated (16) is a water storage vessel to be separated (16),
Described water storage vessel to be separated (16) has water upflow tube to be separated (17), is used for controlling the liquid level of described water storage vessel to be separated (16);
Described separation tail water liquid level retaining part (18) is a separation tail water storage vessel (18),
Described separation tail water storage vessel (18) has and separates tail water upflow tube (19), is used for controlling the liquid level of described separation tail water storage vessel (18),
Described water of condensation liquid level retaining part (20) is a water of condensation storage vessel (20),
Described water of condensation storage vessel (20) has condensate spill over pipe (21), is used for controlling the liquid level of described water of condensation storage vessel (20).
4. negative pressure evaporation water fractionation by distillation device as claimed in claim 2 is characterized in that
Described generating tube tank nest (7) is set at the inner bottom of described evaporation/condensation container (1), thereby described generating tube tank nest (7) all is under the liquid level (6) of the water to be separated in the described evaporation/condensation container (1).
5. negative pressure evaporation water fractionation by distillation device as claimed in claim 4 is characterized in that further comprising:
A pump (11) is used for the direct water from the water source of described water to be separated is transported to described cooling tube bundle (2),
The water return pipeline of described cooling tube bundle of airtight connection (2) and described water storage vessel to be separated (16) is used for making the water described to be separated after described cooling tube bundle (2) heat absorption to return described water storage vessel to be separated (16).
6. negative pressure evaporation water fractionation by distillation device as claimed in claim 5 is characterized in that further comprising:
A float(ing)valve (15), be used for when the liquid level of described water storage vessel to be separated (16) drops to a predetermined height, opening, thereby make water described to be separated from described water source through a water water intaking valve to be separated (13) and enter described water storage vessel to be separated (16), thereby be that described water storage vessel to be separated (16) replenishes water to be separated.
7. negative pressure evaporation water fractionation by distillation device as claimed in claim 5 is characterized in that:
The inflow port of described separation tail water pipeline (9) is set at the bottom of described evaporation/condensation container (1),
Described water lines to be separated (8) go out the position that head piece is set at the generating tube tank nest (7) that is higher than described evaporation/condensation container (1) in the described evaporation/condensation container (1).
CN2009100905510A 2009-08-20 2009-08-20 Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure Pending CN101993123A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2009100905510A CN101993123A (en) 2009-08-20 2009-08-20 Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2009100905510A CN101993123A (en) 2009-08-20 2009-08-20 Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure

Publications (1)

Publication Number Publication Date
CN101993123A true CN101993123A (en) 2011-03-30

Family

ID=43783960

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2009100905510A Pending CN101993123A (en) 2009-08-20 2009-08-20 Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure

Country Status (1)

Country Link
CN (1) CN101993123A (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103232083A (en) * 2013-05-07 2013-08-07 广东工业大学 Solar wind energy low-pressure sea water desalinating apparatus
CN103253722A (en) * 2013-06-07 2013-08-21 浙江大学 Plate type low-temperature multieffect seawater desalting device and method
CN103691141A (en) * 2014-01-13 2014-04-02 林文浩 Energy-saving distiller
CN103717095A (en) * 2011-05-17 2014-04-09 微球公司 System for concentrating industrial products and by-products

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103717095A (en) * 2011-05-17 2014-04-09 微球公司 System for concentrating industrial products and by-products
CN103232083A (en) * 2013-05-07 2013-08-07 广东工业大学 Solar wind energy low-pressure sea water desalinating apparatus
CN103232083B (en) * 2013-05-07 2015-08-05 广东工业大学 A kind of solar wind-energy Low pressure seawater desalination plant
CN103253722A (en) * 2013-06-07 2013-08-21 浙江大学 Plate type low-temperature multieffect seawater desalting device and method
CN103691141A (en) * 2014-01-13 2014-04-02 林文浩 Energy-saving distiller
CN103691141B (en) * 2014-01-13 2015-07-22 林文浩 Energy-saving distiller

Similar Documents

Publication Publication Date Title
US9428403B2 (en) Large scale insulated desalination system
Saidur et al. An overview of different distillation methods for small scale applications
Kalogirou Seawater desalination using renewable energy sources
US20120292176A1 (en) Water treatment process
US8202402B2 (en) System and method of passive liquid purification
CN102695676A (en) Leverage of waste product to provide clean water
CN102630216B (en) Thermal distillation system and technique
Chen et al. On the thermodynamic analysis of a novel low-grade heat driven desalination system
CN102126767B (en) Distillation and separation device for aqueous solution by negative pressure evaporation driven by solar energy/low temperature heat energy and method for obtaining distilled water
US20160002073A1 (en) Renewable desalination of brines
US10144655B2 (en) Systems and methods for distillation of water from seawater, brackish water, waste waters, and effluent waters
CN103501870B (en) Regenerative adsorption Distallation systm
US20170233264A1 (en) Desalination system for the production of potable water
CN101993122A (en) Low-temperature heat energy driven double-container device for distilling and separating water evaporated under negative pressure
CN104150671A (en) Sea water desalting device for heating sea water by using residual heat of waste gas
CN101993123A (en) Low-temperature heat energy driven device for distilling and separating water evaporated under negative pressure
CN102329035B (en) Fresh water collecting and supplying system
CN103613155B (en) Heat pipe-type low temperature two sea water desalting equipment
US20120267231A1 (en) System and method of passive liquid purification
US10414670B2 (en) Systems and methods for distillation of water from seawater, brackish water, waste waters, and effluent waters
CN104108760B (en) A kind for the treatment of unit of oily(waste)water and treatment process thereof
US20090255797A1 (en) Apparatus for desalinization utilizingtemperature gradient/condensation and method thereof
CN201605177U (en) Vacuum membrane distilled water treatment device utilizing solar energy
CN106587238A (en) Sea water desalination system and method with low temperature exhaust heat utilization function
JP2015020163A (en) Nanofiber membrane distillation apparatus

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C02 Deemed withdrawal of patent application after publication (patent law 2001)
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20110330