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WO2009135618A1 - Procédé et dispositif d'extraction d'eau à partir d'air ambiant humide - Google Patents

Procédé et dispositif d'extraction d'eau à partir d'air ambiant humide Download PDF

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Publication number
WO2009135618A1
WO2009135618A1 PCT/EP2009/003125 EP2009003125W WO2009135618A1 WO 2009135618 A1 WO2009135618 A1 WO 2009135618A1 EP 2009003125 W EP2009003125 W EP 2009003125W WO 2009135618 A1 WO2009135618 A1 WO 2009135618A1
Authority
WO
WIPO (PCT)
Prior art keywords
absorbent
desorber
water
distillate
evaporator
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/EP2009/003125
Other languages
German (de)
English (en)
Other versions
WO2009135618A8 (fr
Inventor
Mike Blicker
Alexander Karos
Siegfried Egner
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.)
Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
Original Assignee
Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
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 Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV filed Critical Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
Publication of WO2009135618A1 publication Critical patent/WO2009135618A1/fr
Publication of WO2009135618A8 publication Critical patent/WO2009135618A8/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
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/263—Drying gases or vapours by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0029—Use of radiation
    • B01D1/0035—Solar energy
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0088—Cascade evaporators
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • B01D3/103—Vacuum distillation by using a barometric column
    • 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
    • B01D5/0048—Barometric condensation
    • E—FIXED CONSTRUCTIONS
    • E03—WATER SUPPLY; SEWERAGE
    • E03B—INSTALLATIONS OR METHODS FOR OBTAINING, COLLECTING, OR DISTRIBUTING WATER
    • E03B3/00—Methods or installations for obtaining or collecting drinking water or tap water
    • E03B3/28—Methods or installations for obtaining or collecting drinking water or tap water from humid air
    • 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
    • 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
    • Y02A20/20—Controlling water pollution; Waste water treatment
    • Y02A20/208—Off-grid powered water treatment
    • Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation

Definitions

  • An important advantage of sorbing with a liquid absorbent is that it is relatively easy and reliable to operate.
  • Absorption takes place by absorbing moisture from the liquid absorbent.
  • the absorbent usually a strongly saline solution, diluted. Since the water absorption takes place via the interface between the absorbent and the ambient air, a large interface is sought. The larger the interface, the more effective is the absorption of moisture in the air.
  • substantially vertically aligned guide elements are provided for this purpose, which protrude upwards in the manner of a tower or are integrated in a tower-like construction.
  • a storage for liquid absorbent is arranged above these guide elements. Absorbent is discharged from the reservoir in a controlled manner, so that the absorbent flows down on these guide elements driven by gravity. The absorbent absorbs moisture from the air and thereby thins.
  • a collecting container is present, in which the diluted absorbent is collected.
  • This first sub-process "absorption" of water extraction from the humidity can be carried out with the device described in DE 10 2004 026 334 Al in a very advantageous manner and at low cost.
  • the second sub-process "desorption” is to add the water contained in the diluted absorbent from the absorbent separate and thereby recover pure water. This separation is usually by evaporation.
  • Desorber a device for obtaining water from humid air in arid and semi-arid areas
  • Desorber the apparatus design of such a desorption device, hereinafter referred to as "desorber”
  • Desorber must also be robust and still require the least possible thermal or electrical energy.
  • a supply should be made from renewable energy sources.Only then are such systems for water production to operate economically and without large consumption of resources.
  • the invention has for its object to provide a method and apparatus for obtaining water from moist ambient air, which is preferably powered by renewable energy, in particular solar radiation and / or waste heat. Furthermore, the system should be simple in construction and operation, so it works reliably with low maintenance and low maintenance costs.
  • Figure 1 shows the basic structure of an inventive
  • Figure 3 shows another embodiment of a device according to the invention with two-stage
  • FIG 4 shows another embodiment of a device according to the invention also with two-stage evaporation and Figure 5 a plurality of superimposed inventive
  • FIG. 1 schematically shows an absorber 1 known from DE 10 2004 026 334 A1. With regard to the operation of the absorber 1, reference is therefore made to this document.
  • a component of the absorber 1 is a storage 3 for the concentrated absorbent, which is arranged above a plurality of guide elements 5.
  • the guide elements 5 consist of a plurality of balls, which are strung on a steel cable or on a string.
  • a collecting container 7 is provided below the guide elements 5, in which the now diluted absorbent drops in from the guide elements 5.
  • the absorber 1 has a large dimension in the vertical direction.
  • the length of the guide elements 5 in the vertical direction is an important parameter for influencing the performance of the absorber 1. Basically, the longer the guide elements 5 are, the larger the interface between the absorbent and the ambient air and the more moisture can be from the ambient air be recorded under otherwise identical conditions.
  • the second sub-process namely the desorption, preferably takes place above the absorber 1, so that the desorber 9 is arranged at executed plants about 6 m to 12 m above the ground.
  • the Desorber 9 works with a vacuum evaporation.
  • the desorber 9 of the diluted absorbent from the container 7 again concentrated and the distillate, namely water, can be separated the diluted absorbent is conveyed through a first line 11 from the collecting container 7 in the desorber 9. Because a negative pressure prevails in the desorber 9, the liquid absorbent is drawn in through the first line 11. Any required further feed pumps and shut-off valves are not shown.
  • the desorber 9 is shown in Figure 1 only as a "black box". The operation of the desorber 9 will be explained in more detail with reference to the other figures.
  • the Desorber 9 includes a vapor and airtight housing.
  • the first line 11 opens. Furthermore, go from this housing from a second line 13, with the aid of which the concentrated absorbent is withdrawn from the desorber 9 and discharged into a collecting container 15.
  • a third line 17 starts from the desorber 9 and flows into a second collecting tank 19 for the distillate, namely the water obtained from the atmospheric moisture.
  • the water levels in the containers 15 and 19 are approximately at the same geodetic height and by an amount ⁇ H below the desorber 9.
  • the geodetic height difference ⁇ H between the desorber 9 and the collection containers 15 and 19 may typically be 6 m to 10 m, so that due to the liquid column located in the lines 13 and 17 and the gravity acting on the liquid columns, a pressure in the housing of the desorber 9 of 0.4-0 bar absolute, corresponding to a negative pressure of 0.6 bar to almost 1 bar, sets.
  • the liquid level is in the collection containers 15 and 19 below the collecting container 7. This makes it possible that in the desorption of the influx of concentrated absorbent 'is sucked through the first conduit 11 and then can flow into the lines 13 and 17.
  • a vent valve which at the top of the desorber. 9 is provided.
  • a bleed valve is provided for each stage. "About the vent valve of the desired suppressors can be set starting regular operation before.
  • non-condensable gases can be removed from the desorber, if necessary. These gases are introduced with the liquid absorbent in the desorber. 9 Alternatively, it is also possible to Use vacuum pump.
  • an optional feed line 21 and an optional return line 23 are connected to the desorber 9, which provide cooling water for a heat exchanger or condenser located in the desorber 9.
  • a usually required circulation pump is not shown.
  • most of the components of the device according to the invention are passive components. All that is needed is a pump 25 to convey the concentrated absorbent from the first sump 15 into the reservoir 3 and to overcome the geodetic difference in height between sump 15 and reservoir 3.
  • a pump 27 is required to remove the diluted absorbent from the receiver 7 in the desorber 9 to promote. If possible, one tries to avoid the use of the pump 27.
  • the flow line 21 and the return line 23 are optional.
  • FIG. 2 shows a further exemplary embodiment of a device according to the invention.
  • the lines 21 and 23 are not shown. Otherwise, the same components are provided with the same reference numerals and only the differences from FIG. 1 will be explained. Otherwise, what has been said with regard to FIG. 1 applies correspondingly.
  • the desorber 9 consists of an evaporator section 29 in which absorbent is present in liquid form. Above a liquid level, a steam atmosphere is present in the evaporator section 29 as well as in a distillate tank 31 of the desorber 9.
  • the evaporator part 29 and the distillate container 31 are connected to one another via a connecting part 33 which lies above the liquid level in the evaporator part 29.
  • the connecting part 33 is inclined inclined relative to the horizontal in such a way that the connecting part 39 opens at a lower geodetic height in the distillate tank 31 as in the evaporator section 29th
  • a first heat exchanger 35 is arranged, which is connected via tm2] lines, for example to a solar collector, a waste heat source and / or another heat source. Via this first heat exchanger 35, the absorbent located in the evaporator section 29 is heated until it has reached or exceeded a boiling point corresponding to the negative pressure prevailing in the desorber 9, so that the water contained in the liquid absorbent diluted by water evaporates.
  • a second heat exchanger 37 or condenser is arranged, which is cooled by a cooling medium, such as water, so that condenses on its cold, in contact with the vapor located in the desorber condensed water vapor. It is also conceivable that the outer wall of the desorber 9 itself serves as a capacitor. Then, the condensate is formed on the inner surface of the distillate container 31.
  • Distillate container 31 is arranged sloping down, the distillate runs on the surface of the second heat exchanger in the direction of distillate tank 31 and drips, as soon as it has reached the lowermost end of the second heat exchanger 37, in the distillate tank 31. From the distillate tank 31, the distillate flows through the third Line 17 in the second collection container 19th
  • Solar thermal cooling units could still be mentioned, since they would have the advantage that you can use the solar panels required for the energy supply of could use vacuum evaporation.
  • Other options that can also be very advantageous depending on the location with photovoltaic operated refrigeration units or floor / air heat exchanger. At locations where there is a strong cooling of the air temperatures at night, the cold of the night can be stored for condensation on the day.
  • the guide elements 5 of the absorption section are designed like a tube, the distillate produced in the desorber in the vacuum evaporation can be guided in the interior of the guide elements and thus be used to cool the absorbent flowing outside via the guide elements 5 and thereby achieve a higher water yield .
  • a saline solution eg, LiCl
  • the temperature should be kept below 40 ° C., preferably even below 30 ° C., in order to be able to ensure effective mass transfer of the water into the salt solution.
  • the temperature of the distillate is in a temperature range of 15 ° C to 25 ° C move, so that a heat exchange is possible here.
  • the air flow through the absorption system can also be used to assist the condensation in the desorber 9 by heat is removed from the desorber 9. This brings another energetic advantage
  • the absorbent As the absorbent is recirculated, the only source of contamination is the air itself. Particles, such as sand and dust, can be deposited continuously in a simple mechanical manner (eg, filters). With the right choice of the absorbent (eg salt and distilled water as the starting solution) is also avoided that deposits on the heat exchanger surfaces, which are primarily caused by calcium or magnesium compounds.
  • the deposition problem is a general problem in evaporator systems, the avoidance greatly increases the service life and process stability. Because of the mentioned geodetic height difference .DELTA.H between the distillate container 31 and the second reservoir 19 is formed in the third line 17 from a water column, which maintains the desired negative pressure in the desorber 9.
  • the cooling of the second heat exchanger 37 can take place, for example, with the aid of the supply and return lines 21 and 23 shown in FIG.
  • the device according to the invention is very simple and can be operated virtually maintenance-free. She works as follows:
  • the now diluted absorbent passes via the first line 11 into the evaporator section 29 of the desorber.
  • the desorber 9 prevails, because of the water column present in the lines 13 and 17 and the geodetic height difference ⁇ H between the desorber 9 and the ends of the lines 13 and 17, a negative pressure, so that the Boiling point of the dissolved in the diluted absorbent water to, for example, 40 0 C to 60 0 C is lowered.
  • the evaporator section 29 of the desorber 9 is a first heat exchanger, which is supplied for example via a solar collector 36 with solar generated heat.
  • the liquid absorbent located in the evaporator part 29 heats up and the water dissolved in the liquid absorbent evaporates.
  • This water vapor is condensed by means of the cooled by a cooling medium condenser 37 and deposited on the outer surface of the second heat exchanger 37.
  • the distillate namely water, drips into the distillate tank 31 and flows via the third line 19 into the second collecting tank 19 for the distillate.
  • Heat transfer circuit with which (not shown) of the second heat exchanger 37 is supplied with a cold heat transfer medium.
  • FIG. 3 shows a further embodiment of a desorber according to the invention, in which the desorber is designed in two stages [m4j.
  • the second evaporator part 29.2 is, for example, thermally conductively connected to the first distillate container 31.1 or to the connecting piece 33.1 [m5]. In the first stage of the desorber there is a slightly higher pressure than in the second stage of the desorber. This means that the boiling temperature of the absorbent present in the first evaporator part 29.1 is higher than that of the absorbent present in the second evaporator part 29.2.
  • the absorbent located in the first evaporator part 29.1 is heated with the aid of the first heat exchanger 35, the water contained in the absorbent evaporates and fills the entire space located above the liquid level. Since the second evaporator section 29.2 extends into the first distillate tank 31.1 and the boiling point of the absorbent located in the second evaporator section 29.2 is lower than the temperature of the steam present in the first distillate tank 31.1, the steam present in the first distillate tank 31.1 condenses on the outer surface of the second evaporator section 29.1 and is discharged via the line 17 into the second reservoir 19.
  • the heat released during the condensation of the vapor condensed in the first distillate container 31 is used to heat the absorbent present in the second evaporator portion 29.2.
  • This also evaporates the water contained in this absorbent, is condensed by means of the second heat exchanger 37 and then passes into the second distillate tank 31.2. From there, the distillate also passes through the third conduit 17 into the second collection container 19 for the distillate. It is of course possible and in many cases also useful to carry out a more than two-stage desorption.
  • the number of stages within the desorber 9 ultimately depends on the external conditions and a profitability analysis. Thermodynamically, the highest possible number of stages is desirable, while for economic reasons, the number of stages is limited.
  • the first line 11 opens into the second evaporator part 29.2.
  • a connecting line 39 is present between the second evaporator part 29.2 and the first evaporator part 29.1.
  • the removal of the concentrated by evaporation absorbent takes place from the first evaporator part 29.1 via the second line 13. This can be done for example by the difference in height in both containers. Alternatively, a small pump, not shown, can be used.
  • the first evaporator part 29 and the second evaporator part 29. 2 are supplied directly with dilute absorbent via the first line 11. Likewise, the removal of the concentrated absorbent takes place directly and not via the second line 13. A connecting line between the first evaporator part 29.1 and the second evaporator part 29.2 is not present in this embodiment. There is also another option, namely to use a separate line for each stage to 17,11 and 13.
  • the advantage of the circuit variant according to FIG. 3 is the simpler structural design and the simpler piping.
  • An advantage of the variant according to FIG. 4 is the simpler control of the removal of the concentrated absorbent.
  • the concentration of the absorbent in the first evaporator section 29.1 and in the second evaporator section 29.2 are not coupled together.
  • FIG. 5 shows the schematic structure of a "cascade" of a plurality of superimposed apparatus according to the invention for obtaining water, this construction with several modules, each comprising the sub-processes absorption and desorption, one above the other leads to further savings of pumps and containers, for example, concentrate discharge of a module in each case In order to move the absorbent and the distillate would thus be in the entire system only one pump needed, which greatly simplifies the overall structure and also other template, storage and intermediate container would be saved ,
  • the distillate could also be used to each support the condensation of the underlying Desorptionsmoduls 9 through a heat exchanger. For this, however, either different condensation temperatures in the individual desorption modules 9 would have to be realizable, or the distillate would have to be cooled further than necessary in order to allow condensation in the next module. Overall, then there is the advantage that the structure is further simplified, because not for each module own cooling unit and a cooling circuit must be provided.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Public Health (AREA)
  • Hydrology & Water Resources (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Toxicology (AREA)
  • Drying Of Gases (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

La présente invention concerne un dispositif et un procédé permettant une absorption de l'humidité contenue dans l'air ambiant sur un agent absorbant liquide, puis une désorption de l'agent absorbant dilué dans un désorbeur (9) avec l'aide de la force gravitationnelle dans une large mesure. Le besoin de recourir à une énergie auxiliaire ou externe est ainsi très faible. Le dispositif fonctionne dans la plus grande mesure possible avec des éléments passifs et est par conséquent très simple à construire et ne nécessite que peu d'entretien. En variante, le désorbeur (9) peut être chauffé au moyen d'énergie solaire, par exemple à l'aide d'un capteur solaire (36), de chaleur résiduelle ou également d'énergie externe.
PCT/EP2009/003125 2008-05-05 2009-04-30 Procédé et dispositif d'extraction d'eau à partir d'air ambiant humide Ceased WO2009135618A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008023566A DE102008023566A1 (de) 2008-05-05 2008-05-05 Verfahren und Vorrichtung zur Wassergewinnung aus feuchter Umgebungsluft
DE102008023566.0 2008-05-05

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Publication Number Publication Date
WO2009135618A1 true WO2009135618A1 (fr) 2009-11-12
WO2009135618A8 WO2009135618A8 (fr) 2010-03-18

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WO (1) WO2009135618A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109562303A (zh) * 2016-06-19 2019-04-02 亚伯·M·谢尔 用于将空气除湿并且生产水的方法、设备、组件和系统
DE102017127011A1 (de) 2017-11-16 2019-05-16 Aquahara Technology GmbH Verfahren und Vorrichtung zur Gewinnung von Wasser aus der Umgebungsluft
DE102017127012A1 (de) 2017-11-16 2019-05-16 Aquahara Technology GmbH Verfahren und Vorrichtung zur Gewinnung von Wasser aus der Umgebungsluft

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102031803B (zh) * 2010-11-23 2012-06-27 东南大学 一种利用溶液收集大气中水分的装置
DE102013013214A1 (de) * 2013-08-09 2015-02-12 Logos-Innovationen Gmbh "Vorrichtung zur Gewinnung von Wasser aus atmosphärischer Luft"
CN103469848A (zh) * 2013-09-29 2013-12-25 上海海事大学 一种太阳能空气取水系统
AU2017266711B2 (en) 2016-05-17 2020-07-09 Aquahara Technology GmbH Method and device for obtaining water from ambient air
DE102016212566A1 (de) * 2016-06-29 2018-01-04 Siemens Aktiengesellschaft Verfahren und Anordnung zur Wassergewinnung aus einem Gasgemisch mittels einer Absorptionseinheit in Kombination mit einer thermischen Wassergewinnungsanlage
CN111528057A (zh) * 2018-06-15 2020-08-14 庄臣酿酒（福建）有限公司 一种沙漠造林灌溉器
CN110185090A (zh) * 2019-05-17 2019-08-30 上海交通大学 空气取水及净化装置

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2841217A (en) * 1956-01-27 1958-07-01 Goetz Michael Bernard Absorbent regenerator and thermal recirculator and method of operating same
FR2754736A1 (fr) * 1996-10-18 1998-04-24 Procedes Et Services Proser Procede de regeneration d'un compose liquide de la famille des glycols, utilise dans la deshydratation d'un gaz
DE19952639A1 (de) * 1999-10-22 2001-05-10 Igema Verwaltungsgesellschaft Verfahren und Vorrichtung zur Luftkonditionierung
DE102004026334A1 (de) * 2003-05-26 2005-01-05 Logos-Innovationen Gmbh Vorrichtung zur Gewinnung von Wasser aus atmosphärischer Luft
DE102005017007A1 (de) * 2004-04-07 2005-10-27 Andreas Buchmann Meerwasserentsalzungsanlage mit schwerkraftunterstütztem Vakuum
DE102005043257A1 (de) * 2005-09-09 2007-03-15 Logos-Innovationen Gmbh Vorrichtung zur Gewinnung von Wasser aus atmosphärischer Luft
FR2890650A1 (fr) * 2005-09-12 2007-03-16 Emile Weisman Dispositif de dessalement sous vide de l'eau de mer
DE102006038983A1 (de) * 2006-08-21 2008-02-28 Logos-Innovationen Gmbh Verfahren zur Herstellung von Trinkwasser aus atmosphärischer Luft

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19527908A1 (de) * 1995-07-29 1997-01-30 Heinz Stoehr Vorrichtung zur Entspannungsverdampfung von Meerwasser
DE10205670A1 (de) * 2002-02-12 2003-08-21 Amo Therm Ag Verfahren zur Verdampfung von Flüssigkeiten und Vorrichtung zur Durchführung des Verfahrens

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2841217A (en) * 1956-01-27 1958-07-01 Goetz Michael Bernard Absorbent regenerator and thermal recirculator and method of operating same
FR2754736A1 (fr) * 1996-10-18 1998-04-24 Procedes Et Services Proser Procede de regeneration d'un compose liquide de la famille des glycols, utilise dans la deshydratation d'un gaz
DE19952639A1 (de) * 1999-10-22 2001-05-10 Igema Verwaltungsgesellschaft Verfahren und Vorrichtung zur Luftkonditionierung
DE102004026334A1 (de) * 2003-05-26 2005-01-05 Logos-Innovationen Gmbh Vorrichtung zur Gewinnung von Wasser aus atmosphärischer Luft
DE102005017007A1 (de) * 2004-04-07 2005-10-27 Andreas Buchmann Meerwasserentsalzungsanlage mit schwerkraftunterstütztem Vakuum
DE102005043257A1 (de) * 2005-09-09 2007-03-15 Logos-Innovationen Gmbh Vorrichtung zur Gewinnung von Wasser aus atmosphärischer Luft
FR2890650A1 (fr) * 2005-09-12 2007-03-16 Emile Weisman Dispositif de dessalement sous vide de l'eau de mer
DE102006038983A1 (de) * 2006-08-21 2008-02-28 Logos-Innovationen Gmbh Verfahren zur Herstellung von Trinkwasser aus atmosphärischer Luft

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109562303A (zh) * 2016-06-19 2019-04-02 亚伯·M·谢尔 用于将空气除湿并且生产水的方法、设备、组件和系统
DE102017127011A1 (de) 2017-11-16 2019-05-16 Aquahara Technology GmbH Verfahren und Vorrichtung zur Gewinnung von Wasser aus der Umgebungsluft
DE102017127012A1 (de) 2017-11-16 2019-05-16 Aquahara Technology GmbH Verfahren und Vorrichtung zur Gewinnung von Wasser aus der Umgebungsluft
WO2019096898A1 (fr) 2017-11-16 2019-05-23 Aquahara Technology GmbH Procédé et dispositif pour obtenir de l'eau à partir de l'air ambiant
WO2019096889A1 (fr) 2017-11-16 2019-05-23 Aquahara Technology GmbH Procédé et dispositif pour obtenir de l'eau à partir de l'air ambiant
CN112020390A (zh) * 2017-11-16 2020-12-01 阿夸海瑞技术有限公司 从环境空气中获取水的方法和装置

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