WO2007030851A1 - Apport de chaleur solaire de chauffage destine au dessalage de l'eau de mer - Google Patents

Apport de chaleur solaire de chauffage destine au dessalage de l'eau de mer Download PDF

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Publication number
WO2007030851A1
WO2007030851A1 PCT/AT2006/000378 AT2006000378W WO2007030851A1 WO 2007030851 A1 WO2007030851 A1 WO 2007030851A1 AT 2006000378 W AT2006000378 W AT 2006000378W WO 2007030851 A1 WO2007030851 A1 WO 2007030851A1
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WO
WIPO (PCT)
Prior art keywords
distillate
msf
med
plant according
distillation
Prior art date
Application number
PCT/AT2006/000378
Other languages
German (de)
English (en)
Inventor
Martin Hadlauer
Original Assignee
Martin Hadlauer
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 Martin Hadlauer filed Critical Martin Hadlauer
Publication of WO2007030851A1 publication Critical patent/WO2007030851A1/fr

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Classifications

    • 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
    • B01D3/06—Flash distillation
    • B01D3/065—Multiple-effect flash distillation (more than two traps)
    • 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
    • C02F1/06—Flash evaporation
    • 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
    • C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/138—Water desalination using renewable energy
    • Y02A20/142—Solar thermal; Photovoltaics
    • 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
    • Y02A20/211—Solar-powered water purification
    • 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

  • the present invention relates to a special method for thermal heat input via solar panels in plants for the production of industrial and drinking water by means of a multi-stage distillation process according to the MSF (Mufti Stage Flash) or MED (Multi Effect Distillation) principle.
  • MSF Mofti Stage Flash
  • MED Multi Effect Distillation
  • Generic systems can also be operated via thermal energy from solar systems.
  • solar-powered systems a reheating of the seawater after exiting the preheating column usually takes place via coupler-type heat exchangers with media separation between the seawater circuit and the collector circuit.
  • this heat exchanger is loaded on the secondary side of heavy deposits and thus maintenance-intensive.
  • an attempt is made to use directly with seawater flowed through collectors. This results in the savings of the heat exchanger between seawater and collector cycle, but shifts the problem of corrosion and deposits on collectors and buffer memory.
  • the temperature of the incoming seawater from the preheating column is too high to still achieve efficient heat dissipation or the desired cooling target. This is especially true for the use of novel hybrid collectors for electricity and heat.
  • the return temperature of the inflowing cooling medium should be substantially lower than the operating temperature of the uppermost preheating chamber. By keeping the return temperature low also results in the Advantage that buffer memory to compensate for the load fluctuations can be designed to be relatively small, since due to the difference of supply to return temperature, a higher energy storage potential is given.
  • the object of the present invention is now to eliminate the risk of corrosion and deposits in the collector circuit, without interposing a heat exchanger with media separation between primary and secondary circuit.
  • the development of special materials for collectors and buffer storage is not discussed, but a process engineering solution for avoiding direct contact of seawater in the collectors is offered.
  • Another key objective is to keep the return temperature to the collectors low.
  • distillate is removed from the preheating, passed through the (the) heat exchanger of the heater (s) and then returned to the distillate cycle of the preheating.
  • the distillate recycling takes place either via a separate expansion chamber, or directly into one of the condensation stages of the preheating column.
  • Crucial for the process engineering function is the admixture in the distillate stream of the preheating and not in the seawater cycle.
  • the basic version is to operate a system exclusively via thermal heat from thermal collectors.
  • Distillate according to the invention is removed from the distillation column, heated in the collectors to about 115 to 165 0 C and then introduced into a flash chamber with steam supply to the seawater circuit.
  • This expansion chamber may be either the uppermost chamber of the preheating column, but may also be an outboard vapor deposition chamber via which the condensate is indirectly directed further into the uppermost chamber of the preheating column.
  • the attachment of an external chamber fulfills the purpose of a small buffer memory to adjust load fluctuations from the collector circuit accordingly. Pressure equal to the outer distillate buffer, a chamber for the introduction of seawater and steam is connected upstream of the expansion chambers for seawater evaporation.
  • the steam from the flash evaporation serves for the residual heating of the seawater emerging from the preheating column, which is then passed in descending order through the individual pressure stages of the flash evaporation.
  • a correspondingly large buffer memory is to be provided in the collector circuit, regardless of the buffer volume of the preheating column. The greater the difference between flow temperature and return temperature in the collector circuit, the smaller this buffer memory can be designed. Both from this point of view and the endeavor to keep the average collector temperature as low as possible, the distillate for the collector circuit from the bottom of the preheating column, or after emerging from the lowest stage recommended.
  • An extended variant provides for connecting hybrid collectors in addition to the thermal collectors. These are tracked collectors with cooled solar cells, which are acted upon by mirrors with high radiation intensity.
  • the hybrid collectors have a supporting effect on the distillation of distillate during the day, but are mainly used to generate electricity. In symbiosis with the desalination plant these collectors can be flowed through with deposit-free distillate at a low return temperature. Depending on the feed temperature (70-100 0 C), the distillate at the corresponding temperature level of the Voreriermkolonne is recycled to the distillate stream.
  • This invention interconnection makes it possible to use hybrid collectors for industrial purposes. As a result, hydrogen can be generated via the solar power generated by these collectors.
  • thermal collectors instead of the thermal collectors use a compressor system for the base load.
  • steam is removed from the distillation column and brought via the compressor unit in the chamber for residual heating of the preheated seawater.
  • the hybrid collectors can now be integrated in the manner according to the invention.
  • this concept is ideal for retrofitting existing compressor-driven systems that operate according to a staged distillation process. Large buffer tanks are not necessary because the system can be kept in continuous operation via the compressor unit in a kind of base load.
  • the invention does not relate exclusively to the above-mentioned variants, but to all possible combinations resulting from these variants.
  • the use of the inventive method of distillate removal from the preheating, heating via one or more heaters and return to the distillate of the preheating, is limited not only to distillation plants of seawater, but also to plants for the distillation of brackish water and biologically and chemically contaminated water for custom - and drinking water production.
  • Fig. 1 is a schematic representation of an MSF-MED distillation plant with several heating connections in accordance with the usual state of the art, and a connection of collectors according to the interconnection of the invention.
  • FIG. 2 shows two calculations of an MSF distillate column, one for seawater heating via a heating device 3 and the other for distillate heating with removal from the lowest stage and heating via a heating device 1.
  • Fig. 3 is a schematic representation of an MSF distillation plant with heat supply via solar panels according to the general state of the art.
  • Fig. 4 is a schematic representation of an MSF distillation plant with the inventive connection of thermal collectors.
  • Fig. 5 is a schematic representation of an MSF distillation plant, with the inventive connection of thermal collectors and hybrid collectors.
  • Fig. 6 is a schematic representation of an MSF distillation plant with steam supply via a compressor system and a connection of hybrid collectors.
  • Fig. 1 shows a schematic representation of a MSF-MED distillation plant with several heating connections 13, 3 according to the usual state of the art, and a connection of panels 1 according to the interconnection of the invention.
  • the different methods for heating heat input are purely for comparison purposes and are not usually united in a single system.
  • a MED process can be activated via film evaporation equipment.
  • the MED vaporization is put into operation via the compressor 12 and overlaps the normal MSF process.
  • the MSF process can now be operated independently via different possibilities of energy input.
  • Variant a is usually branched off when coupled to thermal power plants with a favorable possibility of process steam. Regardless of these couplings, process steam can also be taken from the MSF column. For this purpose, a further evaporation stage is provided after the lowest condensation stage. The vapor deposited in this stage is now compressed and introduced as process steam 13 in the uppermost stage. Basically, this plant is driven by technical work by compressors.
  • Variant b is a typical application for heat input via thermal collectors. Basically, three options should be set forth with the heater 3. On the one hand, this can be a heat exchanger with primary-side connection of a closed collector circuit, - on the other hand, an open collector circuit with direct seawater flow. In both cases, as mentioned above, relatively high heating temperatures are present, whereby problems with deposits from the seawater are to be expected.
  • Variation c represents the interconnection according to the invention for heat input via collectors 1.
  • the condensate can be taken from the uppermost stage of the preheating column 6 and returned to this stage after heating in the collectors 1.
  • the temperature in the collectors is about the same as in the case of heating with direct seawater flow, but the problem with the deposits is solved.
  • the distillate yield 14 is lower by the proportion of condensate vaporized in the introduction into the first (uppermost) stage than in variant b. At 20 MSF levels, a distillate loss of 12% is expected. This loss is measured against the savings on maintenance quite economically justifiable.
  • the distillate yield 14 decreases in Relative to the heat energy input accordingly.
  • the exact behavior can not be estimated easily, but can only be determined by a calculation.
  • the distillate removal at the lowest point at the exit from the preheating column 6 still achieves a very high desalting performance. The explanation is given based on the following calculation results.
  • FIG. 2 shows two computations of an MSF distillate column with distillate heating via a heating device 1, on the one hand a variant A with distillate removal from the uppermost stage, and on the other hand a variant B with distillate removal from the lowest stage.
  • a seawater temperature of 85 ° C is used in both cases.
  • the supply of sea water in the Vormérmkolonne 6 occurs by definition at a temperature of 25 0 C.
  • the heating is carried out of the distillate in the heater 1 to a predetermined temperature of 120 ° C.
  • the distillate yield 14 is kept constant, a comparison of the heat to be supplied via the heating device 1 is made. As you can see, the efficiency of distillate extraction drops from variant A to variant B in about 100% to 66%.
  • efficiency is understood to mean the amount of distillate obtained in relation to the heat energy introduced.
  • An essential aspect, that still a comparatively high efficiency of 66% is achieved, is explained by the fact that due to the differently sized countercurrent mass flows in the heat exchangers, less steam is needed for the residual heating of the seawater 2, since the preheating to a comparatively higher temperature ( 81 0 C instead of 79 ° C) takes place. Which removal height is chosen depends on the collector behavior. High-quality thermal collectors can be coupled most efficiently to Variant A - Hybrid collectors with cooled solar cells according to Variant B. In general, there is a wide range of options for interconnecting different collector types in parallel and in series. It should also be borne in mind that with the integration of buffer storage for the night, the volume for variant B is about half as large as for variant A.
  • the prior art shown in Fig. 3 is a well-known process of MSF (Multi Stage Flash) distillation equipment for recovering service water according to a thermal process.
  • the heat from the collector 1 is passed from a buffer memory 4 via a heat exchanger 3 to the preheated seawater 2.
  • FIG. 4 shows a schematic representation of an MSF distillation plant with the inventive connection of thermal collectors 1.
  • the removal of distillate 5_1 from the preheating column 6 for the collector circuit is carried out at a medium stage temperature.
  • the return of the heated distillate 5_2 to the preheating column 6 takes place via an upstream expansion chamber 7 with steam supply line 8 into a condensation chamber 9 for residual heating of the seawater.
  • the interposition of a buffer memory 4 ensures that the system can be kept in operation day and night. Apart from the pumps, the system is only driven thermally.
  • FIG. 5 shows a schematic representation of an MSF distillation plant, with the inventive connection of thermal collectors 1 and hybrid collectors 10.
  • the distillate decoupling 5_1 for both collector circuits takes place at the exit from the preheating column 6.
  • the thermal collectors 1 From the thermal collectors 1, the heated distillate via a buffer memory 4 introduced into the expansion chamber 7.
  • the hybrid collectors 10 pass the heated distillate 5_2 directly into one of the upper stages of the preheating column 6.
  • the distillate introduction is variably selectable in that stage in which approximately the temperature of the supplied distillate (5_2) prevails. Apart from the pumps, the system is only driven thermally.
  • FIG. 6 shows a schematic representation of an MSF distillation plant which is operated in the base load via a compressor installation 11.
  • the connection of the hybrid collectors 10 is used primarily for power generation.
  • the distillate 5_1 is withdrawn on leaving the preheating column and, after being heated by the hybrid collectors 10, is returned to one of the upper stages of the preheating column 6. Due to the low feed temperature, the hybrid collectors 11 can not independently operate the MWE plant without compressor assistance, but make a significant contribution to increasing the distillate output.
  • FIG. 7 shows a representation of a hybrid collector in the middle section.
  • a large part of the radiation is conducted via the mirror 15 onto a cooled solar cell module 16.
  • the radiation reflected at the solar cells is absorbed in the thermal absorber 17.
  • the temperature of the incoming cooling medium in this case distillate from the preheating column, must be kept low.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne une installation de dessalage de l'eau de mer destinée à la production d'eau sanitaire et d'eau potable à l'aide d'un procédé de distillation multi-étape selon MSF (Multi Stage Flash) ou MED (Multi Effect Distillation) avec apport de chaleur de chauffage. L'invention est caractérisée en ce que le distillat (5_1) est prélevé de la colonne de préchauffage (6), est chauffé par au moins un dispositif de chauffage (1) puis renvoyé au circuit de distillat de la colonne de préchauffage (6). Le distilllat (5_2) chauffé est renvoyé par une chambre (7) vorgelagerte avec transfert de la vapeur (8) dans la chambre (9) pour le chauffage résiduel de l'eau de mer.
PCT/AT2006/000378 2005-09-15 2006-09-13 Apport de chaleur solaire de chauffage destine au dessalage de l'eau de mer WO2007030851A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA1523/2005 2005-09-15
AT0152305A AT502797B1 (de) 2005-09-15 2005-09-15 Solare heizwärmeeinbringung zur meerwasserentsalzung

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WO2007030851A1 true WO2007030851A1 (fr) 2007-03-22

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WO (1) WO2007030851A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001070929A (ja) * 1999-09-07 2001-03-21 Kawasaki Heavy Ind Ltd 太陽熱および光電池ハイブリット型淡水化装置
WO2002032813A1 (fr) * 2000-10-21 2002-04-25 Pb Power Ltd. Procede et installation de dessalement eclair d'eau
AT412274B (de) * 2003-07-21 2004-12-27 Martin Dipl Ing Hadlauer Mehrstufige verdampfungseinrichtung mit kompressorunterstützung zur heizwärmeabgabe an meerwasserentsalzungsanlagen

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3239816A1 (de) * 1982-05-24 1983-11-24 Dvt Deutsch Verfahrenstech Verfahren zur destillation von suesswasser aus meerwasser

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001070929A (ja) * 1999-09-07 2001-03-21 Kawasaki Heavy Ind Ltd 太陽熱および光電池ハイブリット型淡水化装置
WO2002032813A1 (fr) * 2000-10-21 2002-04-25 Pb Power Ltd. Procede et installation de dessalement eclair d'eau
AT412274B (de) * 2003-07-21 2004-12-27 Martin Dipl Ing Hadlauer Mehrstufige verdampfungseinrichtung mit kompressorunterstützung zur heizwärmeabgabe an meerwasserentsalzungsanlagen

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Publication number Publication date
AT502797B1 (de) 2007-06-15
AT502797A4 (de) 2007-06-15

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