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WO2007128062A1 - Appareil et procede de dessalement - Google Patents

Appareil et procede de dessalement Download PDF

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Publication number
WO2007128062A1
WO2007128062A1 PCT/AU2007/000597 AU2007000597W WO2007128062A1 WO 2007128062 A1 WO2007128062 A1 WO 2007128062A1 AU 2007000597 W AU2007000597 W AU 2007000597W WO 2007128062 A1 WO2007128062 A1 WO 2007128062A1
Authority
WO
WIPO (PCT)
Prior art keywords
carrier gas
gas
water
air
water vapour
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.)
Ceased
Application number
PCT/AU2007/000597
Other languages
English (en)
Inventor
Behdad Moghtaderi
Elham Doroodchi
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.)
The University of Newcastle
Newcastle Innovation Ltd
Original Assignee
The University of Newcastle
Newcastle Innovation Ltd
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
Priority claimed from AU2006902369A external-priority patent/AU2006902369A0/en
Application filed by The University of Newcastle, Newcastle Innovation Ltd filed Critical The University of Newcastle
Publication of WO2007128062A1 publication Critical patent/WO2007128062A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0041—Use of fluids
    • B01D1/0047—Use of fluids in a closed circuit
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
    • 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
    • C02F1/048—Purification of waste water by evaporation
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates generally to a method and apparatus for the desalination of salt water.
  • the invention has been developed primarily for use in humidification- dehumidification (HDH) desalination, and will be described with reference to this application.
  • HDH humidification- dehumidification
  • brine sources such as sea water, salt water from surface resources like lakes and ponds, and brackish (i.e. salty) water found in deep geothermal reservoirs and aquifers.
  • brackish i.e. salty water found in deep geothermal reservoirs and aquifers.
  • the terms "brine” as used herein is intended to be construed sufficiently broadly to encompass not only any type of water/mineral solution such as brines, salt water or brackish water whether naturally occurring or artificially produced, but also other water and suspensions and mixtures.
  • the conventional desalination processes can be classified into three main groups: 1. Thermal processes, such as multi-stage flash distillation (MSF), multi-effect distillation (MED), thermal vapour compression (TVC), mechanical vapour compression (MVC), and air-based HDH.
  • MSF multi-stage flash distillation
  • MED multi-effect distillation
  • TVC thermal vapour compression
  • MVC mechanical vapour compression
  • air-based HDH air-based HDH
  • Membrane processes such as reverse osmosis (RO), and electrodialysis (ED).
  • RO reverse osmosis
  • ED electrodialysis
  • Electrolysis pro Dates EL
  • conventional desalination processes can be driven by fossil fuel or renewable energy sources (e.g. solar, wind, geothermal).
  • renewable energy sources e.g. solar, wind, geothermal.
  • the majority of common desalination processes are expensive and energy intensive since in such processes either the brine has to be heated up to temperatures well above the ambient temperature using multi-effect heat transfer units (e.g. MSF, MED, TVC, MVC), or high levels of electrical power are required for the process (e.g. RO, ED and EL).
  • desalination technologies such as MSF, MED, TVC, MVC, RO, ED and EL are mostly suitable for large-scale production of freshwater from seawater in densely populated locations where sizable power plants are available.
  • densely populated regions there are circumstances where the desalination needs are relatively small and do not exceed 30 mVday.
  • the potable water usage in most remote rural communities in Australia with populations below 150 is about 10 m 3 /day. This seemingly small demand creates a whole range of logistical problems for communities living in arid to semi-arid regions in terms of transportation and delivery of freshwater.
  • the principle innovation in the HDH process is that heat recoveries equivalent to multi- effect systems are achieved by maintaining a continuous flow of humid air between the evaporator and condenser, and by partially recycling the brine. This minimises the sensible heat losses and allows the desalination process to be carried out at relatively low temperatures (60-90 0 C) in a low energy intensive manner.
  • Desalination of salt water by the HDH process has been the subject of many investigations in the past mainly with the intention of decreasing construction and running costs whilst increasing efficiency. Particular attention has been paid to the use of renewable energy sources for powering the process, especially solar and geothermal energies.
  • studies have been made on the feasibility of using coolant sea water, ejected at a temperature of about 55 0 C from a power plant.
  • the invention provides a humidification- dehumidification desalination apparatus including: a humidifier for mixing a water based solution with a substantially non-air based carrier gas to evaporate water from the solution thereby humidifying the carrier gas; a dehumidifier for condensing water vapour from the carrier gas and thereby dehumidifying the carrier gas; and a substantially closed loop circulation system including a blower, to circulate the carrier gas between the humidifier and dehumidifier.
  • air refers to the mixture of gases comprising the earth's atmosphere. This is understood to include approximately 78% Nitrogen, and approximately 21% Oxygen with small amounts of Argon, Carbon Dioxide and other gases. '
  • non-air refers to any gas which is substantially dissimilar to the composition of "air” with regard to the constituent components and/or the relative proportions thereof.
  • water based solution includes any liquid solution, suspension, mixture or combination thereof including water as a constituent component.
  • the carrier gas is selected such that the ratio of the gas constant of the carrier gas, to the gas constant of the water vapour, (Rg/R-v) is greater than the ratio of the gas constant of the air, to the gas constant of the water vapour, (R a /R v ).
  • the carrier gas is selected such that the ratio of the specific heat of the carrier gas, to the specific heat of the water vapour, (Cp g /C pV ) is greater than the ratio of the specific heat of the air, to the specific heat of the water vapour, (C pa /c P v).
  • the carrier gas is selected such that the ratio of the thermal conductivity of the carrier gas, to the thermal conductivity of the water vapour, (k g /k v ) is greater than the ratio of the thermal conductivity of the air, to the thermal conductivity of the water vapour, (k a /k v ).
  • the carrier gas includes H 2 , He and/or NH 3 gas. More preferably, the carrier gas is composed substantially entirely of one or more gases selected from the group consisting of H 2, He, and NH 3 .
  • the closed loop circulation system both recycles the carrier gas and minimises contact between the outside air and the carrier gasses.
  • lighter gasses such as H 2 , He or NH 3 gas
  • Thermodynamically gases like H 2 and He can accommodate larger quantities of water vapour while exhibiting much better heat and mass transfer rates than air.
  • the issues associated with the density difference between the water vapour and low molecular weight carrier gases can be easily resolved if the mixture is circulated by forced convection. The increase in the pumping power associated with forced convection will be negligible because much smaller volumes of the carrier gas are needed.
  • the invention at least in a preferred form proposes an HDH based process which integrates the non-air carrier gas and forced convection principles into a unified platform for increasing the production rate of freshwater per unit volume of the brine fed to the system, thereby, substantially reducing the construction, operation and maintenance costs per unit volume of freshwater produced.
  • the humidifier is a packed tower evaporator and the dehumidifier is a shell and tube heat exchanger.
  • the humidifier and dehumidifier are fluidly connected at respective upper ends by means of an insulated duct.
  • a water solution catchment sump is located at a lower end of the humidifier and a water catchment sump is located at a lower end of the dehumidifier.
  • the closed loop circulation system includes a heat exchanger.
  • the invention provides a method of selecting a suitable carrier gas for use in a humidification-dehumidification desalination apparatus, said method including the steps of: determining an initial series of candidate gases; for each member of the series of candidate gases, determining a series of relative candidate parameters including: an absorption parameter, indicative of the capability of the gas to absorb water vapour relative to air; a transport parameter, indicative of the heat and mass transfer capability of the gas relative to air; and a heat exchanger parameter, indicative of the heat exchanger size required to operate as an evaporator under equivalent conditions, relative to air; selecting one or more suitable carrier gas from the series of candidate gases which provide superior performance to that of air based on the combined influence of said parameters.
  • said relative candidate parameters include at least any one of: a cost parameter, indicative of the cost of the gas; an availability parameter, indicative of the availability of the gas; a flammability parameter, indicative of the potential flammability risks of the gas; a toxicity parameter, indicative of the toxicity of the gas; and a solubility parameter, indicative of the solubility of the gas in water.
  • the invention provides a method of desalinating water in a humidification-dehumidification desalination process, said method including the steps of: humidifying a substantially non-air based carrier gas in a humidifier by means of mixing a water based solution with the carrier gas to evaporate water from the solution; dehumidifying the carrier gas in a dehumidif ⁇ er to extract water; and forcibly recirculating the carrier gas between the humidifier and dehumidifier in a closed loop circulation system.
  • Fig. 1 is a flow diagram displaying the algorithm used to determine the suitability of various carrier gasses
  • Fig. 2 is a schematic representation of a Humidification-Dehumidification plant in accordance with the invention
  • Fig. 3 A is a schematic cross section of a shell and tube heat exchanger with an in-line tube bundle configuration
  • Fig. 3B is a schematic cross section of a shell and tube heat exchanger with a staggered tube bundle configuration.
  • the desalination apparatus 1 includes a pair of heat exchangers in the form of a humidifier 2, and dehumidifier 3, which respectively evaporate a brine water source to water vapour and subsequently condense the water vapour to pure water.
  • the invention utilises a closed loop re-circulation system wherein the carrier gas and carrier gas-water vapour mixture are circulated under forced convection. Furthermore, the invention replaces air, which ordinarily acts as a carrier gas, by another gas (or a mixture of gases) which is selected to have overall superior carrier gas characteristics than air. Those characteristics include at least one of, but are not limited to having a greater gas constant (R g ), specific heat (c pg ) and thermal conductivity (k g ) than those of air and water vapour (i.e. R v> c pv , andk ⁇ ).
  • R g gas constant
  • c pg specific heat
  • k g thermal conductivity
  • this configuration allows comparatively larger quantities of water vapour to be mixed with the carrier gas in a mixture for which the ratios of (R g / R v ), (C pg / Cp V ), and (k g / k v ), are greater than those of air-water vapour. This ultimately enhances the efficiency and productivity of the plant.
  • the solubility of H 2 , He and NH3 in water are also much smaller than those of CO 2 and air.
  • the mole fraction solubility of H 2 and He in water at 298.15 K and 101.325 kPa partial pressure of gas are 1.4IxIO "5 and 0.7IxIO "5 , respectively, while the solubility of CO 2 under similar conditions is 61.48xlO '5 .
  • Fig 1 the algorithm described above and used to select suitable carrier gasses is shown in flow chart form. While the gases analysed above are limited to H 2 , He, NH 3 and CO 2 , it will be appreciated that other substantially pure gases, as well as other mixtures of gases might be considered in a similar manner.
  • gases which may be considered include, organic fluids such as propane and iso-butane, HFC based refrigerants, such as difluoromethane (R-32), pentafluoroethane (R- 125), 1,1,1-trifluoroethane (R- 143 a) and 1,1,1,2- tetrafluoroethane (R-134a), as well as mixtures of such gases, for example H 2 and He or He and NH 3 or R- 125 and R32, or any other combination of two, three or more gases.
  • organic fluids such as propane and iso-butane
  • HFC based refrigerants such as difluoromethane (R-32), pentafluoroethane (R- 125), 1,1,1-trifluoroethane (R- 143 a) and 1,1,1,2- tetrafluoroethane (R-134a)
  • mixtures of such gases for example H 2 and He or He and NH 3 or R
  • Suitable carrier gases should be considered when selecting suitable carrier gases.
  • One such parameter is the prior mentioned absorption of the gas in water. Some gases dissolve more readily and to a greater degree than others in water. This parameter is of little concern when using air as a carrier gas however, in a closed system, it is generally preferable that the carrier gas is not lost via dissolution as it can add to expense, be harmful to the environment or flavour the water. The requirement to install and run additional apparatus to remove dissolved gas from the output water should be considered.
  • Another parameter is whether the gas is hazardous due to toxicity, flammability or for other reasons. Use of a such gases at best will require the use of special operating procedures and/or filtering of the output water and at worst render the output unusable for consumption or other purposes.
  • a further parameter is that of the cost and availability of the gas.
  • Alternative carrier gasses are unlikely to be both free and as readily available as air. Cost and logistically issues of rare gases may render them as unsuitable.
  • a further parameter is the degree of pumping required to force convection of the gas though the apparatus. Extreme, pumping energy costs may render a gas as unsuitable as a carrier gas relative to other gases.
  • the humidifier 2 and dehumidifier 3 are connected by a duct 4 at respective top ends.
  • the humidifier 2 is a packed tower type and the dehumidifier 3 is a shell and tube type.
  • the lower ends of the heat exchangers 2 and 3 are effectively sealed from the surrounding atmosphere by brine and water catchment sumps respectively, 5 and 6.
  • a hot brine manifold 7 is located at the top end of the humidifier 2 and a carrier gas manifold 8 is located at the lower end of the humidifier 2.
  • the carrier gas manifold 8 is connected, by a dry gas return line 9, to the water catchment sump 6 under the dehumidifier 3.
  • the return line 9 also includes a blower 10, a gas heat exchanger 11, a flow control valve 12 and a gas heat exchanger by-pass line 13.
  • a cold brine circulation loop 14 fluidly connects the brine sump 5 to the dehumidifier 3 and includes a pump 15, a flow control valve 16, a by-pass line 17 and a brine heat exchanger 18.
  • the brine sump 5 includes makeup and discharge ports 19 and 20.
  • An outlet port 21 is provided for draining brine from the dehumidifier and a water extraction port 22 for extracting fresh water collected in the water sump 6.
  • the apparatus includes a control system comprising temperature, flow rate, velocity and moisture probes, solenoid valves, an A/D data converter, and a CPU mother board.
  • Hot brine is fed to the manifold 7 through an inlet port 23.
  • the hot brine can be from a variety of sources, for example, hot brackish water from a geothermal reservoir, hot/warm waste water from an industrial process (e.g. sea water heated up by the waste heat from a coal fired power station, or reject hot geothermal fluid from a geothermal power plant) or cold brine heated up by the exhaust gases of a diesel engine.
  • the manifold 7 includes an array of nozzles 24 which spray the brine over the top of packing material 25 within the humidifier 2.
  • the hot brine trickles through the packing material under the influence of gravity.
  • relatively dry carrier gas is blown into the lower end of the humidifier through the gas manifold 8.
  • the gas rises through the packing material and is exposed to the hot brine.
  • water vapour and heat are given up from the brine to the counter-current dry gas stream.
  • the temperature of the brine drops leaving the tower almost at the ambient temperature.
  • one packed tower humidifier or several in series may be used.
  • the choice of packed towers over other types of heat exchangers is to provide a greater contact surface area between the gas and brine, hence, .maximise the efficiency of the process. Nevertheless, other forms of heat exchangers may be employed depending on the specific design requirements.
  • the cooled brine is collected in the sump 5 at the bottom of the humidifier 2.
  • a portion of the concentrated brine is discharged via the discharge port 20 as blowdown while make-up brine is added via the make-up port 19 on a continuous basis to maintain the level of the cold brine in the sump 5.
  • the make-up brine is supplied from a separate tank (not shown) and is obtained by bleeding a portion of the hot brine and letting it cool under atmospheric conditions. Meanwhile, the moist, humidified carrier gas stream leaves the top of the humidifier 2 and passes through the connecting duct 4 to the dehumidifier 3.
  • the connecting duct is completely insulated to ensure that the humid gas maintains temperature and does not lose enthalpy.
  • the dehumidifier is a shell-and-tube heat exchanger whereby the temperature of the humidified air is reduced to cause water formation by condensation.
  • the moist gas is passed between an array of fluid cooled, cooling tubes 26 within the shell 27.
  • the cooling fluid for the dehumidifier is the cold brine collected in the sump 5 under the humidifier.
  • the cold brine is pumped through the circulation loop 14 by pump 15.
  • the temperature of the brine may be adjusted by directing it either through the brine heat exchanger 18 or bypass line 17 as required.
  • the heat exchanger may be air or water-cooled.
  • the humid carrier gas moves down through the shell of the dehumidifier, between the cooling tubes.
  • Water vapour carried by the relatively warm carrier gas condenses on the external walls of cooling tubes effectively extracting water from the carrier gas. In addition this results in latent heat restitution of the brine circulating inside the tubes.
  • the condensing water eventually drips down through the dehumidifier and is collected in the sump 6 at the bottom of the dehumidifier where it is extracted through port 22. Similarly, the now mildly warm brine solution is discharged via outlet port 21.
  • a horizontal-tube falling film type shell-and-tube heat exchanger is used to enhance the heat exchange process and maximise the yield of fresh water.
  • Both in-line or staggered tube bundle configurations as shown in Fig. 3 A and 3B may be used.
  • External surfaces of the tubes may be also fitted with fins so that the liquid film thickness on a given tube wall does not rise to undesirable levels. This is essential as the presence of a thick liquid film creates a barrier between the water vapour and cold tube walls thus slowing down the condensation process.
  • the gas leaving the condenser is almost devoid of moisture and at the ambient temperature. It should be highlighted that the entire carrier gas loop is closed to the external atmosphere. This not only allows the carrier gasses to be used repeatedly in a cyclic manner without any contact with air, but also minimises safety concerns if using a flammable or otherwise hazardous carrier gas.
  • the dry carrier gas is forced out of the closed sump 5 using a small blower 10.
  • the blower may be located in a different location or replaced by other means for forcing convection of the carrier gas.
  • the gas is returned to the humidifier 2 via dry gas return line 9.
  • the dry gas may be passed through the gas heat exchanger 11 to adjust its temperature otherwise, the flow control valve 12 directs the gas to by-pass the heat exchanger.
  • the gas heat exchanger 11 may be water or air-cooled.
  • thermocouples for controlling the flow rates of the gas and brine as well as the temperature of the various components of the plant.
  • hygrometers moisture meters
  • solenoid valves for controlling the flow rates of the gas and brine as well as the temperature of the various components of the plant.
  • AJO fast analogue to digital
  • CPU central processing unit
  • the invention proposes an improved efficiency method and apparatus for the desalination of water by HDH. It achieves an advantage over existing HDH methods by use of a carefully selected non-air carrier gas which provides superior water vapor absorption characteristics and heat and mass transfer rates.
  • the non-air gas is reused and recirculated between the humidifier and dehumidifier in a closed loop forced convection system.
  • the invention represents a practical and commercially significant improvement over the prior art.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Drying Of Gases (AREA)

Abstract

L'invention concerne un appareil (1) de dessalement à humidification-déshumidification, comprenant un humidificateur (2) destiné à mélanger une solution aqueuse à un gaz porteur qui n'est pas à base d'air. Le gaz porteur évapore l'eau de la solution, humidifiant ainsi le gaz porteur. Un déshumidificateur (3) condense le gaz porteur chargé d'humidité, extrayant ainsi l'eau dessalée, qui est collectée dans une cuve (6). Un système de circulation sensiblement en boucle fermée comprenant une soufflante (10) fait circuler le gaz porteur entre l'humidificateur et le déshumidificateur. Le gaz porteur préféré est l'hydrogène, l'hélium ou l'ammoniac. L'invention concerne également un procédé de sélection d'un gaz porteur approprié consistant à déterminer différents paramètres et à comparer les gaz.
PCT/AU2007/000597 2006-05-05 2007-05-04 Appareil et procede de dessalement Ceased WO2007128062A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2006902369 2006-05-05
AU2006902369A AU2006902369A0 (en) 2006-05-05 Desalination method and apparatus

Publications (1)

Publication Number Publication Date
WO2007128062A1 true WO2007128062A1 (fr) 2007-11-15

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Cited By (26)

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US20110139600A1 (en) * 2010-11-29 2011-06-16 King Fahd University Of Petroleum And Minerals Gaseous density convective desalination and cooling system
CN102757102A (zh) * 2011-04-28 2012-10-31 中国科学院理化技术研究所 海水或苦咸水淡化方法及装置
WO2012159203A1 (fr) * 2011-05-24 2012-11-29 Saltworks Technologies Inc. Procédé, appareil et système pour la concentration de solutions en utilisant l'évaporation
EP2532401A1 (fr) * 2011-06-07 2012-12-12 International For Energy Technology Industries L.L.C Système de purification d'eau
WO2014195110A1 (fr) * 2013-06-05 2014-12-11 Siemens Aktiengesellschaft Installation et procédé de traitement d'eau
US20150047963A1 (en) * 2012-04-25 2015-02-19 Saltworks Technologies Inc. Modular humidification-dehumidification apparatus for concentrating solutions
US9221694B1 (en) 2014-10-22 2015-12-29 Gradiant Corporation Selective scaling in desalination water treatment systems and associated methods
WO2016000862A1 (fr) * 2014-07-03 2016-01-07 Siemens Aktiengesellschaft Concept de câble d'une installation de préparation thermique
CN105366753A (zh) * 2014-08-25 2016-03-02 成都安捷宜康环保科技有限公司 利用煤气吹脱法处理氨氮废水的方法
WO2016180387A1 (fr) * 2015-05-13 2016-11-17 Westfälische Hochschule Gelsenkirchen Bocholt Recklinghausen Procédé et dispositif d'évaporation entraîné par un gaz vecteur
US9643102B2 (en) 2014-06-05 2017-05-09 King Fahd University Of Petroleum And Minerals Humidification-dehumidifaction desalination system
US9969638B2 (en) 2013-08-05 2018-05-15 Gradiant Corporation Water treatment systems and associated methods
CN108840384A (zh) * 2018-07-23 2018-11-20 大连理工大学 小型模块式热法高盐废水脱盐系统及方法
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