GB2211432A - Desalinating water - Google Patents

Desalinating water Download PDF

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Publication number
GB2211432A
GB2211432A GB8824443A GB8824443A GB2211432A GB 2211432 A GB2211432 A GB 2211432A GB 8824443 A GB8824443 A GB 8824443A GB 8824443 A GB8824443 A GB 8824443A GB 2211432 A GB2211432 A GB 2211432A
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United Kingdom
Prior art keywords
water
brine
concentrated
precipitated
concentrating
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.)
Withdrawn
Application number
GB8824443A
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GB8824443D0 (en
Inventor
Jozef Jankowski
Joachim Masarczyk
Jan Kalus
Andrzej Kaplanek
Franciszek Rakowski
Zbigniew Pelc
Jan Dulewski
Janusz Sikora
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.)
ZABRZANSKIE GWARECTWO WEGLOWE
Original Assignee
ZABRZANSKIE GWARECTWO WEGLOWE
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Publication date
Application filed by ZABRZANSKIE GWARECTWO WEGLOWE filed Critical ZABRZANSKIE GWARECTWO WEGLOWE
Publication of GB8824443D0 publication Critical patent/GB8824443D0/en
Publication of GB2211432A publication Critical patent/GB2211432A/en
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • Y02A20/131—Reverse-osmosis

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  • Chemical & Material Sciences (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)
  • Crystallography & Structural Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Description

J 221 METHOD OF WATER DESALINATION, PARTICULARLY MINING WATERS This
invention relates to the method of water desalination, particularly mining water.
Polish patent specification No. 50342 discloses a method of water desalination, consisting in vaporising brine in multi-effect configuration of adiabatic evaporating apparatus, in precipitation from concentrated brine of calcaneous hardness in form of calcium sulfate and guiding the crystallization process in such a way so as to precipitate only NaCl crystals and dispose all remaining impurities in form of end lye. The deficiency of this method is that it is power consuming and requires 200 kWh for vaporizing 1 cu.m of saline water. Since the evaporators operate in a multi-effect configuration, it is also material- consuming and the installations used for this method cover vast spaces.
Another known method of mining waters desalination is presented in Polish patent application No. P.264215. It consists in that, depending on the rate of mineralization of saline waters, the method is a two- or threestage one. The first stage is applied in cases of saline water with mineralization ranging from 3 to 70 g/cu.dm, wherein the mechanically and chemically treated water is thermally concentrated to the degree of mineralization of 130-150 g/cu.dm. Water with mineralization exceeding 70 g/cu.dm is directed onto the second stage of thermal concentrating, together with water concentrated at the first stage. The products of the second stage of concentration are: calcium sulfate, socium chloride, end lye and usable water with a low mineralization degree. At the third stage the process includes concentration and treatment of end lyes in order to reclaim usable elements and chemical compounds, for example iodine, bromine, magnesium chloride and other. Although this method provides a complex solution for utilization of saline waters, it is nevertheless also power and material-consuming due to concentrating the brine at first and second stages in adiabatic evaporators of multi-effect type. Moreover, installations used in the above mentioned methods occupy large areas in manufacturing bays.
It is the object of this invention to provide a new method of water desalination, excluding the previous deficiencies, particularly to reduce power consumption required for utilization of 1 cu.m of saline water.
The gist of the method according to the invention, in which water, particularly mining water, with the concentration of dissolved ions below 40 g/cu.dm is concentrated in the reverse osmosis installation and then thermally and in cases of dissolved ion concentration exceeding 40 g/cu. dm is directly thermally concentrated, consists in that brine is concentrated in a single-effect evaporator and during concentrating it is recycled in the recirculation installation and the vapour obtained during concentrating brine is compressed in a water vapour compressor and returned to the single-effect evaporator as a heating medium, whereas brine concentrated to above 300 g/cu.dm of dissolved ions is passed to crystallizers where salts are precipitated.
Precipitation of undesired chemical compounds from brine is done either in a side chamber through which brine passed during recirculation or in the crystallizer through which the brine passes before its concentrating in the single-effect evaporator or, else, in the crystallizer used for treating concentrated brine with over 300 g/cu.dm dissolved ions.
The use of the invention in utilization of moderately saline water, i.e. with mineralization degree up to 40 g/cu.dm, using the reverse osmosis method at the first stage of concentrating to obtain brine concentration to about 70.g/cu.dm allows to obtain considerable power savings, as compared with known evaporator methods. Power consumption measured in electric power amounts to 3.0 - 4.0 kWh/cu.m of treated water. Furthermore, thermal concentrating of brine at the second stage, i.e. to the concentration of 70-300 g/cu.dm, using single-effect evaporator with recirculation of brine and utilization of produced water vapour as a heating medium gives considerable material and power savings as compared with known methods of saline water desalination. Power consumption expressed as electric power at the second stage of brine concentrating amounts to 25-30 kWh/cu.m of treated water. Material - 4 savings result from the fact, that one evaporator with recirculation takes on the function'of several evaporators necessary to obtain the same end product. For this reason cubic capacity and area of buildings required for installations according to the invention may be several times smaller than previously needed. Due to considerable reduction of power consumption there is no further need of building a large power plant nor installations for protection of natural environment, e.g. installations for dedusting and desulphurizing waste gases or storage of flv-ashes and slaQ.
The invention allows to shorten considerably the cycle of building the installations for saline waters utilization and to obtain significant labour cuts both in erecting the buildings and in operating the process. The invention affords possibilities for constructing small desalination installations at every mine, thus allowing for quick solving of the ecologic problem of contamination of surface waters with saline mining water.
The invention is presented in the drawing, in which Fig. explains the method of desalination of water in which dissolved ions amount to 40 glcu. dm, Fig. 2 shows the method of desalination of water with dissolved ions exceeding 40 g/cu.dm, Fig. 3 presents the method of desalination of water in which the amount of dissolved ions exceeds 40 g/cu.dm and undesired chemical compounds are precipitated in a side chamber built into the recirculation, Fig. 4 presents the - 5 method of desalination of water in which the amount of dissolved ions exceeds 40 g/cu.dm and undesired chemical compounds are precipitated in a side chamber built into the recirculation, Fig. 5 presents the method of desalination of water in which the amount of dissolved ions is below 40 g/cu.dm and undesired chemical compounds are precipitated before the brine enters the evaporator, Fig. 6 presents the method of deslination of water in which dissolved ions amount to ocver 40 g/cu.dm and undesired chemical compounds are precipitated before the brine enters the evaporator, Fig. 7 presents the method in which the amount of dissolved ions is below 40 g/cu.dm and undesired chemical compounds are precipitated after concentrated brine leaves the evaporator and Fig. 8 shows the method of desalination of water in which dissolved ions amount to over 40 g/cu.dm and undesired chemical compounds are precipitated after concentrated brine leaves the evaporator.
1. Example of desalination of water, particularly mining water, with a low degree of salinity, e.g. below 40 glcu.dm. of dissolved ions, is as follows: saline water from duct 8 is chemically and mechanically pretreated in apparatus 4 of brine pretreatment, from where it is driven to reverse osmosis installation 5 in which it is concentrated with the reverse osmosis method to a concentration of about 70 g/cu.dm, being the first stage of brine concentrating. During concentrating the brine in installation 5 25-80% of usable water with mineralization of - 6 500-600 mgIcu.dm is obtained, and this water is carried away with duct 10, whereas concentrated brine is carried on with duct 9 onto the second stage of concentrating, to a single-stage thermal evaporator 1 and recirculated through recirculating installation 6. Water vapour obtained during concentrating of brine is compressed in water vapour compressing installation 14 and returned to the thermal single-stage evaporator 1 as a heating medium. The recirculated brine is concentrated in thermal single-stage evaporator 1 to the form of saturated brine pulp with concentration of dissolved ions amounting to about 300 g/cu.dm and the pulp is directed via duct 13 to crystallizers 3 in which salts are precipitated. Usable water is carried away with duct 11.
2. Example of desalination of water, particularly mining waters, in which the amount of dissolved ions exceeds 40 g/cu.dm: Saline water from duct 9 is chemically and mechanically pretreated in apparatus 4 for brine pretreatment and then it is directed to thermal single-stage evaporator 1 and recycled in recirculation installation 6. Water vapour produced during concentrating of brine is compressed in water vapour compressor 14 and returned to evaporator 1 as a heating medium. Recycled brine is concentrated in thermal single-stage evaporator 1 to the form of saturated brine pulp with concentration of about 300 g/cu.dm dissolved ions and carried on in duct 13 to crystallizers 3 in which salts are precipitated. Usable water is disposed through duct 11.
3. Example of desalination of water, particularly mining waters, in which the amount of dissolved ions does not exceed 40 g/cu.dm: Saline water from duct 8 is chemically and mechanically pretreated in apparatus 4 for brine pretreatment and then brine is directed to the reverse osmosis installation 5 in which it is concentrated with the reverse osmosis method to a concentration of about 70 g/cu.dm, being the first stage of brine concentration. During concentrating brine in the reverse osmosis installation 5, 25-80% of usable water is obtained, with mineralization of 500-600 mg/cu.dm. This water is carried away by duct 10 and concentrated brine is conveyed via duct 9 to the second stage of concentrating, to thermal single-stage evaporator 1 and recycled in recirculation installation 6. During recirculating the brine in recirculation installation 6, brine is directed through a side chamber 2, in which, in order to obtain a high degree of purity of NaCl salt, undesired chemical compounds, mainly alkaline earth metal sulfates are precipitated and disposed by duct 12. Water vapour produced during concentrating of brine is compressed in water vapour compressor 14 and returned to the thermal evaporator 1 as a heating medium. The recycled brine is being concentrated in thermal single-stage evaporator 1 to the form of saturated brine pulp with concentration of about 300 g/cu.dm of dissolved ions and transferred via duct 13 to crystallizers 3 in which salts, mainly NaCl is precipitated. Usable-water is disposed through duct 11.
4. Example of desalination of water, particularly mining waters, in which the amount of dissolved ions exceeds 40 g/cu.dm: Saline water from duct 9 is chemically and mechanically pretreated in brine pretreatment apparatus 4 and then transferred to a thermal single-stage evaporator 4 and recycled in recirculation installation 6. During recirculation in installation 6, brine is directed through a side chamber 2 in which, in order to obtain high degree of purity of NaCl salt, undesired chemical compounds, mainly alkaline earth metal sulfates are precipitated and disposed through duct 12. Water vapour produced during concentrating of brine is compressed in water vapour comDressor 14 and returned to the thermal single-stage evaporator 1 as a heating medium. Recirculated brine is concentrated in a thermal single-stage evaporator 1 to the form of saturated brine pulp, with a concentration of about 300 g/cu.dm of dissolved ions and the pulp is conveyed through duct 13 to crystallizers 3 where salts, mainly NaCl are precipitated. Usable water is disposed through duct 11.
5. ExamDle of desalination of water, particularly mining waters, in which salination is moderate, for instance, the amount of dissolved ions does not exceed 40 g/cu.dm: Saline water from duct 8 is chemically and mechanically pretreated in brine pretreatment apparatus 4 and then directed to the reverse osmosis installation 5 in 9 - which it is concentrated with the reverse osmosis method to J1 a concentration of about 70 g/cu.clrft, being the first stage of brine concentrating. During concentrating brine in the reverse osmosis installation 5, 25-80% of usable water is obtained, with mineralization ranging between 500-600 mg/eu.dm. This water is carried away through duct 10. Pre-concentrated brine is carried rom. the reverse osmosis installation 5 to the second stage of concentrating, to the thermal single-stage evaporator 1 through crystallizator 7, in which, in order to obtain high degree oil purity of NaCl salt, undesired chemical compounds, mainly alkaline earth metal sulfates are precipitated and disposed through duct 12. At the second concentrating stage brine is recycled in recirculation installation 6. Simultaneously, water vapour produced during concentrating of brine is compressed in water vapour compressor 14 and returned to the thermal single-stage evaporator 1 as a heating medium. Re-cycled brine is concentrated in the thermal single-stage evaporator 1 to the form of saturated brine pulp, with a concentration oil about 300 g/cu.dm of dissolved ions and then the pulp is directed via ducts 13 to crystallizers 3 in which salts, mainly NaCl are precipitated. Usable water is disposed through duct 11.
6. Example of desalination of water, particularly.mining waters, in which the amount of dissolved ions exceeds 40 g/cu.dm: Saline water from duct 9 is chemically and mechanically pretreated in brine pretreatment apparatus 4 and then directed to a thermal single-stage evaporator 1 through crystallizer 7 in which, in order to obtain a high degree of purity of NaCl, undesirable chemical compounds, mainly alkaline earth metal sulfates are precipitated and disposed through duct 12. Brine delivered to the thermal single-stage evaporator 1 is then recycled in recirculation installation 6. Simultaneously, water vapour produced during brine concentrating is compressed in water vapour compressor 14 and returned to the thermal single-stage evaporator 1 as a heating medium. Recycled brine is concentrated in the thermal single-stage evaporator 1 to the form of saturated brine pulp with a concentration of about 300 g/cu.dm of dissolved ions and the pulp is transferred to crystallizers 3 in which salts, mainly NaCl are precipitated. Usable water is disposed through duct 11.
7. Example of desalination of water, particularly mining waters, moderately saline, in which for instance, the amount of dissolved ions does not exceed 40 glcu.dm: Saline water from duct 8 is chemically and mechanically pretreated in brine pretreatment apparatus 4 and then brine is directed to reverse osmosis installation 5 in which it is concentrated with the reverse osmosis method to a concentration of about 70 g/cu.dm of dissolved ions, being the first stage of concentration. During concentrating of brine in reverse osmosis installation 5, 25-80% of usable water is obtained, with mineralization ranging from 500-600 mc/eu. dm. This water is carried away - 11 with duct 10. Initially concentrated brine is transferred to the second stage of concentrating, to a thermal single-stage evaporator 1 with recirculation. Simultaneously, water vapour produced during concentrating brine is compressed in water vapour compressor 14 and returned to the thermal single-stage evaporator 1 as a heating agent. Recycled brine is concentrated in a thermal single-stage evaporator 1 to the form of saturated brine pulp with a concentration of about 300 g/cu. dm of dissolved ions and directed via duct 13 to crystallizers 7 in which, in order to obtain a high degree of purity of NaCl salt, undesired chemical compounds, mainly alkaline earth metal sulfates are precipitated and then the pulp is transferred to crystallizers 3 in which salts, mainly NaCl are precipitated. Usable water is disposed through duct 11. Undesired chemical compounds, precipitated in crystallizer 7 are disposed through duct 12.
8. Example of desalination of water, particularly mining waters, in which the amount of dissolved ions exceeds 40 g/cu.dm: Saline water from duct 9 is chemically and mechanically pretreated in brine pretreatment apparatus 4 and then riven to thermal single-stage evaporator 1 and recycled in recirculation installation 6. Water vapour produced during concentrating of brine is simultaneously compressed in water vapour compressor 14 and returned to the thermal single-stage evaporator 1 as a heating agent. Recycled brine is concentrated in the - 12 thermal single-stage evaporator 1 to the form of saturated brine pulp with concentration of about 300 g/cu.dm of dissolved ions. The pulp is then transferred to crystallizer 7 through duct 13. In order to obtain a high degree of purity of NaCl, undesired chemical compounds, mainly alkaline earth metal sulfates are precipitated in crystallizer 7 and disposed through duct 12. The pulp is then driven to crystallizer 3 in which slats mainly NaCl, are precipitated. Usable water is disposed through duct 11.
R

Claims (9)

13 C L A I M S
1. A method of desalinating water wherein, after chemical and mechanical pre-treatment, saline water with a concentration of dissolved ions below 40 g/cu.dm is concentrated in a reverse osmosis installation and then concentrated thermally, and/or saline water with a concentration of dissolved ions exceeding 40 g/cu.dm is directly thermally concentrated; wherein concentrating of the brine is carried out in a single-stage evaporator, and during concentrating it is recycled in a recirculation installation; and wherein water vapour produced during the concentrating of the brine is compressed in a water vapour compresscr and returned to the single-stage evaporatLor as a heating agent, whereas t-he brine when concentrated to more than 300 g/cu.dm c-E dissolved ions is directed to a 1 crystallizer in which salts are precipitated.
2. A method as claimed in claim 1, wherein the brine being recycled is directed through a side chamber in which undesired chemical compounds are precipitated.
3. A method as claimed in claim 1, wherein prior to said concentrating in a single-stage evaporator, the brine is directed into a crystallizer in which undesired chemical compounds are precipitated.
4. A method as claimed in any one of claims 1 to 3, wherein the brine concentrated to above 300 g/cu.dm. of dissolved ions is directed to the or a first crystallizer in which undesired chemical compounds are precipitated and then to said crystallizer in which said salts are precipitated.
5. A method of desalinating water, substantially as hereinbefore described with reference to the accompanying drawings.
6. A method according to any one of the preceding claims, wherein the water being desalinated is mining water.
14 -
7. Apparatus for desalinating water, comprising a thermal concentrator, a brine pre-treatment apparatus in the brine feed line to said thermal concentrator, a crystallizer in the brine outlet from said thermal concentrator, and an outlet for water vapour from said thermal concentrator, said water vapour outlet being connected to a warm water inlet to said thermal concentrator by way of a recycle line including a water vapour compressor.
8. Apparatus for desalinating water, constructed and adapted to operate substantially as hereinbefore described with reference to the accompanying drawings.
9. Water which has been desalinated by the method of anv one of claims 1 to 6, or using the apparatus of claim 7 or 8.
4 Published 1989 atThe Patent Office, State House. 66171 High Holborn, Londcr. WC1R4TP. Further copies maybe obtamedfromThe PatentOffice. Sales Branch, St Mary Cray. Orpington, Kent BR5 3RD. Printed by Multiplex techniques ltcL St Mary Cray, Kent, Con. 1187
GB8824443A 1987-10-23 1988-10-19 Desalinating water Withdrawn GB2211432A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PL1987268423A PL268423A1 (en) 1987-10-23 1987-10-23 Method of water desalting,especially coal mine water

Publications (2)

Publication Number Publication Date
GB8824443D0 GB8824443D0 (en) 1988-11-23
GB2211432A true GB2211432A (en) 1989-07-05

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GB8824443A Withdrawn GB2211432A (en) 1987-10-23 1988-10-19 Desalinating water

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DE (1) DE3835965A1 (en)
GB (1) GB2211432A (en)
PL (1) PL268423A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2395946A (en) * 2002-12-05 2004-06-09 Thomas Altmann Extracting sodium chloride from seawater, using nanofiltration
WO2010018249A1 (en) * 2008-07-30 2010-02-18 Desalacion Integral Systems, S.L. Improved plant for the desalination/purification of industrial waste and brackish water with zero liquid discharge
ES2565014A1 (en) * 2015-12-16 2016-03-30 Sociedad Anónima Depuración Y Tratamientos Brackish water desalination system with zero discharge (Machine-translation by Google Translate, not legally binding)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5238574A (en) * 1990-06-25 1993-08-24 Kawasaki Jukogyo Kabushiki Kaisha Method and apparatus having reverse osmosis membrane for concentrating solution
DE4410347A1 (en) * 1994-03-25 1995-09-28 Rene Leutwyler Process for removing inorganic metal compounds from solutions
ITTO20100270A1 (en) * 2010-04-09 2011-10-10 Scam S P A WATER DESALINATION PLANT
NL2008728C2 (en) * 2012-04-27 2013-10-29 Dutch Water Technologies B V System and method for recovering salts from a liquid flow.
CN109970262B (en) * 2017-12-28 2024-01-09 江苏久吾高科技股份有限公司 Zero discharge treatment method and device for reclaimed water
CN114368844B (en) * 2021-12-15 2023-03-21 庆阳新庄煤业有限公司新庄煤矿 Data monitoring method and device for high-salinity mine water treatment

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GB627707A (en) * 1945-04-03 1949-08-15 Little Inc A Improvements in or relating to distillation apparatus
GB780272A (en) * 1953-12-08 1957-07-31 Henri Coanda Method and device for distilling aqueous salt solutions to obtain potash water
GB863393A (en) * 1958-10-02 1961-03-22 Davey Paxman And Company Ltd Controlling scale formation in evaporators
GB881958A (en) * 1958-08-27 1961-11-08 Richardsons Westgarth & Co Improvements in or relating to evaporators and turbine-driven compressors for use inevaporators
GB935178A (en) * 1961-04-26 1963-08-28 Aqua Chem Inc Maintaining free from scale the heating surfaces of evaporators
GB983242A (en) * 1962-11-15 1965-02-17 Asriel Osdor Plant and process for the desalinization of saline water
GB1055437A (en) * 1962-10-16 1967-01-18 Garrett Corp Improvements relating to distillation apparatus
US4265701A (en) * 1980-01-07 1981-05-05 Ecodyne Corporation Liquid concentration method
EP0210888A1 (en) * 1985-06-28 1987-02-04 Institut Français du Pétrole Distillation process with energy recuperation by an ejection stream compressor

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US4105556A (en) * 1976-02-18 1978-08-08 Combustion Engineering, Inc. Liquid waste processing system
US4083781A (en) * 1976-07-12 1978-04-11 Stone & Webster Engineering Corporation Desalination process system and by-product recovery
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DE3041209A1 (en) * 1980-11-03 1982-05-13 Josef van Opbergen GmbH & Co KG, 4040 Neuss METHOD FOR THE TREATMENT OF IN PARTICULAR NITRATE-CONTAINING WATER

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB627707A (en) * 1945-04-03 1949-08-15 Little Inc A Improvements in or relating to distillation apparatus
GB780272A (en) * 1953-12-08 1957-07-31 Henri Coanda Method and device for distilling aqueous salt solutions to obtain potash water
GB881958A (en) * 1958-08-27 1961-11-08 Richardsons Westgarth & Co Improvements in or relating to evaporators and turbine-driven compressors for use inevaporators
GB863393A (en) * 1958-10-02 1961-03-22 Davey Paxman And Company Ltd Controlling scale formation in evaporators
GB935178A (en) * 1961-04-26 1963-08-28 Aqua Chem Inc Maintaining free from scale the heating surfaces of evaporators
GB1055437A (en) * 1962-10-16 1967-01-18 Garrett Corp Improvements relating to distillation apparatus
GB983242A (en) * 1962-11-15 1965-02-17 Asriel Osdor Plant and process for the desalinization of saline water
US4265701A (en) * 1980-01-07 1981-05-05 Ecodyne Corporation Liquid concentration method
EP0210888A1 (en) * 1985-06-28 1987-02-04 Institut Français du Pétrole Distillation process with energy recuperation by an ejection stream compressor

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2395946A (en) * 2002-12-05 2004-06-09 Thomas Altmann Extracting sodium chloride from seawater, using nanofiltration
GB2395946B (en) * 2002-12-05 2006-01-18 Thomas Altmann Method for the production of sodium chloride from seawater
WO2010018249A1 (en) * 2008-07-30 2010-02-18 Desalacion Integral Systems, S.L. Improved plant for the desalination/purification of industrial waste and brackish water with zero liquid discharge
ES2565014A1 (en) * 2015-12-16 2016-03-30 Sociedad Anónima Depuración Y Tratamientos Brackish water desalination system with zero discharge (Machine-translation by Google Translate, not legally binding)

Also Published As

Publication number Publication date
PL268423A1 (en) 1989-05-02
DE3835965A1 (en) 1989-05-03
GB8824443D0 (en) 1988-11-23

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