US3257290A - Multi-stage flash evaporators - Google Patents

Multi-stage flash evaporators Download PDF

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Publication number
US3257290A
US3257290A US235359A US23535962A US3257290A US 3257290 A US3257290 A US 3257290A US 235359 A US235359 A US 235359A US 23535962 A US23535962 A US 23535962A US 3257290 A US3257290 A US 3257290A
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United States
Prior art keywords
flash
series
chamber
conduit means
chambers
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Expired - Lifetime
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US235359A
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English (en)
Inventor
Starmer Roy
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Richardsons Westgarth and Co Ltd
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Richardsons Westgarth and Co Ltd
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/2803—Special features relating to the vapour to be compressed
    • B01D1/2812—The vapour is coming from different sources
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/284—Special features relating to the compressed vapour
    • 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)
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/21—Acrylic acid or ester

Definitions

  • This invention relates to multi-stage flash evaporators, particularly evaporators for obtaining distilled water from impure water or sea water.
  • the brine or liquid to be evaporated is passed through a series of heaters the last of which is generally heated by live steam supplied from an external source.
  • the top brine temperature to which the circulating brine may be heated in the steam heated chamber is limited by various operational and design considerations, and particularly by the onset of vscale deposition with higher operating temperatures.
  • this In the case of evaporators for distilling saline water such as sea water, this generally limits the permissible top brine temperature to below 200 F., so that all the heaters in 4the evaporator operate at sub-atmospheric pressures.
  • a multi-stage flash evaporator comprises three or more stages each having aash chamber and an associated heater or vapour receiver, and a heater heated by live steam from an external source which is arranged to be traversed by the liquid to be evaporated before it enters the ash chambers, in which the steam-hea-ted chamber has an inlet connected to the delivery side -of -a mechanical compressor, such as a rotary compressor or piston compressor, the inlet side of the compressor being connected to an intermediate stage of the evaporator so as to withdraw therefrom vapour of the liquid being evaporated and deliver such vapour to the steam-heated chamber.
  • a mechanical compressor such as a rotary compressor or piston compressor
  • the said inlet or another inlet in the steamheated chamber is connected to the delivery side of a steam tur-bine so that the steam-heated chamber receives live steam which has'been expanded in the turbine.
  • the turbine can then be used -to drive the compressor, and it is advantageous where this arrangement is used for the turbine and the compressor to be so constructed and arranged that, during operation, the pressure of the exhaust steam from the turbine is approxi-mately equal to the pressure of the compressed vapour delivered by the compressor.
  • the flash evaporator shown in the drawing comprises a brine path 10 which passes through a series of heatercondensers 12 ea-ch having a heat exchanger 12C therein wherein the brine is gradually brought to a higher temperature by the latent heat of condensation of vapour which is passed into the heater-condensers 12 through passages 13 from a series of flash chambers 14. Dispassed from one heater condenser to another through chamber to the next by conduits 10a.
  • a steam-heated chamber 20 ⁇ is provided which is traversed by the liquid passing through heat exchanger 20a -tillate which condenses in the heater-condensers 12 is condensers 24 is possible.
  • heater-condensers 24 are supplied with vapour through passages 25 from the flash chambers forming the last few dashingoff stages, and these heater-condensers 24 are circulated by fresh cool liquid which serves to remove excess heat from the circulatory system.
  • the fresh liquid ows along a path 26 which includes heat exchangers 24e and is circulated by a pump 28. After leaving the heater-condenser 24a, part of the slightly preheated stream of fresh liquid is discharged to waste while the remainder enters the final flash chamber 14 through a pipeline 30.
  • the fresh liquid mixes with unevaporated brine which has already been circulated along the iiow path 10, and the resultant mixture is withdrawn from the final flash chamber in order that part of the mixture may be discharged to waste while the other part is recirculated to the heatercondensers 12 with the aid of the pump 18.
  • all v the brine used for evaporation enters the evaporating system through the pipeline 30.
  • an important aiml of the present invention is to utilise to the best advantage the pressure drop obtainable from the so-called live steam supplied from the external source 31.
  • This is achieved by passing the steam supply through a steam turbine 32 before it reaches the steam-heated chamber 20, the -turbine being coupled to a rotary compressor 33 so that the steam is used to compress a quantity of brine vapour which is withdrawn by the compressor from one of the intermediate stages of the evaporator.
  • the compressed vapour is then passed, together with the exhaust steam from the turbine, into the steam-heated chamber 20 where the steam and vapour mixture is condensed.
  • the distillate thus formed in the steam-heated chamber 20 can be removed through the pipe-line 21 as boiler feed water or supplied through the pipeline 23 to the final heater-condenser 12.
  • the quantity of live steam required to operate the evaporator under a certain set of conditions can be reduced by a quantity corresponding approximately to the quantity of vapour which is compressed in the rotary compresssor 33. This produces an appreciable saving in steam and heat consumption which can vary between wide limits depending on the thermodynamic cycle used in the evaporator.
  • the turbine 32 and the compressor 33 are so designed that the pressure of the exhaust steam from the turbine is approximately equal to the pressure of the compressed vapour delivered by the compressor.
  • the quantity of vapour withdrawn from the intermediate stage by the compressor 33 will depend, for any given live steam conditions, on the pressure in the evaporator stage from which the vapour is extracted and the pressure in the steam-heated chamber 20 into which it is discharged.
  • the ratio of vapour withdrawn to live steam supplied will rise considerably if the ratio of the higher to the lower of the two above-mentioned pressures is reduced, but on the other hand, the thermodynamic performance of the plant is best when the evaporator is operated with as high a top brine temperature as possible and as low a vapour temperature in the coldest heatercondenser 24h as is practicable.
  • the brine vapour is withdrawn by the compressor 33 from an intermediate stage of the evaporator and not from the first or last stages. This is because we have found that a very considerable improvement in the ratio of vapour withdrawn to live steam supplied and therefore in the steam consumption of the plant, can be achieved if the compressor 33 is made to withdraw vapour from a ash chamber or a heater condenser operating at a pressure between the highest and the lowest pressures obtaining in the plant.
  • the selected point of vapour extraction should preferably be the highest pressure fresh heater-condenser 24a if more than one such heater is used, or the lowest pressure heater-condenser 12a.
  • FIG. 34 Broken lines 34, 36 and 38 are shown in the drawing to illustrate the pipeline connections between the heater condenser 24a or the heater condenser 12a and the suction side of the compressor 33 if either of these arrangements is adopted.
  • a specially arranged flash chamber 14a connected by a passage 39 to a simple vapour receiver 40 instead of to an associated heater can be used, the chamber 14a and its receiver 4d forming an intermediate stage of the evaporator, and the .receiver 40 being connected by the pipeline 34 and a branch line 42 to the suction side of the ejector 32.
  • thermodynamic loss is involved in connecting the suction side of the compressor 33 to the coldest heater condenser 12a, but the loss is small as this heater operates at a temperature level approaching the level at which heat is rejected altogether from the plant, and the thermodynamic loss may be more than offset by gains resulting from improved performance of the turbine and compressor.
  • vapour it may be expedient in some circumstances to withdraw vapour from a heater-condenser 12 operating at a pressure above that in the heater-condenser 12a.
  • the increased quantity of vapour handled by the compressor 33 with such an arrangement does not offset the thermodynamic disadvantages following the extraction of vapour at a temperature level at which heat can be usefully transferred to the circulat- Y ing brine.
  • the plant shown in the drawing can easily be arranged to run on a low grade pressure steam supply by supplying the steam ⁇ direct to the steamheated chamber 20 instead of through the turbine 32.
  • the compressor can either be cut out of the evaporating cycle or, alternatively, driven by some other form of prime mover.
  • connections between the turbo-compressor and the heater or heaters, and also between the turbine and the steam supply source 31, include valves or other means for controlling the steam supply and the withdrawal of the vapour, and for dealing with the various conditions encountered when starting up or shutting down the plant.
  • a multi-stage ash evaporator comprising: a series of flash chambers including a first flash chamber, a plurality of intermediate fiash chambers and a last flash chamber, first feed conduit means connected to said first ash chamber, interconnecting conduits connecting said flash chambers in series to enable feed liquid introduced into said first ash chamber to flow therefrom through the series of Hash chambers to sai-d last flash chamber, a first series of heater condenser chambers, a second series of heater condenser chambers, flash vapor conduit means connecting each heater condenser chamber of said first series with vapor space in a respective one of a first group of said flash chambers including said first flash chamber and several further flash chambers immediately succeeding it in the flash chamber series, further ash vapor conduit means connecting each heater condenser chamber of said second series with vapor space in a respective one of a second group of said ash chambers including said last flash chamber and at least one further flash chamber immediately preceding it in the flash chamber series, drain conduit means to drain distillate from
  • An evaporator according to claim 1 comprising feed delivery means delivering feed liquid withdrawn from said last ash chamber to said second feed conduit means.
  • a multi-stage fiash evaporator comprising: a series of flash chambers including a first flash chamber, a plurality of intermediate ash chambers and a last flash chamber, first feed conduit means connected to said first iiash chamber, interconnecting conduits connecting said flash chambers in series to enable feed liquid introduced into said first ash chamber to flow therefrom through the series of flash chambers to said last ash chamber, a first series of heater condenser chambers, a second series of heater condenser chambers, flash vapor conduit means connecting each heater condenser chamber of said first series with vapor space in a respective one of a first group of said flash chambers including said first flash chamber and several further fiash chambers immediately succeeding it in the flash chamber series, further flash vapor conduit means connecting each heater condenser chamber of said second series with vapor space in a respective one of a second ⁇ group of said flash chambers including said last flash chamber, drain conduit means to drain distillate froml all said heater condenser chambers, a first plurality of heat
  • a multi-stage fiash evaporator according to claim 6 wherein said steam-heated chamber is connected to the delivery side of a steam turbine to receive live steam which has been expanded in said turbine, said compressor being driven by said turbine.
  • a multi-stage flash evaporator according to claim 6 wherein said steam-heated chamber is connected to the delivery side of a steam turbine to receive steam which has been expanded in said turbine, said compressor being driven by said turbine, and wherein said turbine and said compressor are so constructed and arranged that, during operation, the pressure of the exhaust steam from said turbine is approximately equal ⁇ to the pressure of the compressed vapour delivered by said compressor.
  • a multi-stage flash evaporator wherein all the flash chambers supply ash vapor to a respective heater-condenser chamber with the exception of one intermediate flash chamber, a vapour receiver being connected to vapor space in said one intermediate ash chamber and the inlet side of said compressor being connected to the said receiver.

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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)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
US235359A 1961-11-08 1962-11-05 Multi-stage flash evaporators Expired - Lifetime US3257290A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB40091/61A GB1047981A (en) 1961-11-08 1961-11-08 Improvements in or relating to multi-stage evaporators

Publications (1)

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US3257290A true US3257290A (en) 1966-06-21

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US (1) US3257290A (enrdf_load_stackoverflow)
DE (1) DE1517493A1 (enrdf_load_stackoverflow)
GB (1) GB1047981A (enrdf_load_stackoverflow)
NL (1) NL285240A (enrdf_load_stackoverflow)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3344041A (en) * 1963-12-20 1967-09-26 Wulfson Dov Multistage flash distillation of saline water
US3396086A (en) * 1964-12-23 1968-08-06 Applied Res And Engineering Lt Recompression evaporators
US3433717A (en) * 1965-03-01 1969-03-18 Aqua Chem Inc Multistage flash still with vapor compression plant
US3501384A (en) * 1965-12-21 1970-03-17 Applied Research & Eng Ltd Low pressure degassing of feed water in multi-stage flash evaporators
US3511756A (en) * 1967-03-13 1970-05-12 Lummus Co Flash evaporation with series arranged with solar heating zone
US3514375A (en) * 1967-05-25 1970-05-26 Fives Lille Cail Water desalination distillation including evaporator and compressor
US3515646A (en) * 1967-04-19 1970-06-02 Weir Westgarth Ltd Vertical multi-stage flash evaporator with separate horizontal condensing chamber
US3859174A (en) * 1972-11-14 1975-01-07 Fred W Taylor Recovery of potable water from sanitary waste using solid wastes and refuse as a heat source
US4110174A (en) * 1976-12-16 1978-08-29 Uop Inc. Power generation and potable water recovery from salinous water
US4313305A (en) * 1979-09-18 1982-02-02 Dan Egosi Feedback energy conversion system
US4434027A (en) 1980-03-17 1984-02-28 Stork Friesland B.V. Method for the evaporation of a liquid solution using mechanical compression
WO2012127406A1 (en) * 2011-03-21 2012-09-27 I.D.E. Technologies Ltd. A compound multi effect distillation system
US9539522B1 (en) * 2015-12-01 2017-01-10 Kuwait Institute For Scientific Research Combination multi-effect distillation and multi-stage flash evaporation system
CN113753919A (zh) * 2021-09-24 2021-12-07 天津黄埔盐化工程技术有限公司 一种从垃圾焚烧飞灰水洗液中提取钾盐的方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2219292C2 (de) * 1972-04-20 1982-12-09 Kali Und Salz Ag, 3500 Kassel Verfahren und Vorrichtung zum Eindampfen von im Kreislauf geführten Lösungen oder von Meerwasser
DE102008004107A1 (de) 2008-01-11 2009-07-16 Babcock Borsig Service Gmbh Verfahren und Anlage zur Entsalzung von Salzwasser unter Verwendung von MSF-Entsalzungseinheiten mit einem Dampfumlaufsystem

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2759882A (en) * 1954-07-30 1956-08-21 Bethlehem Steel Corp Combined flash and vapor compression evaporator
US2893926A (en) * 1957-06-13 1959-07-07 Bethlehem Steel Corp Combined flash type distilling plant and back-pressure turbo-generator
US3021265A (en) * 1957-07-05 1962-02-13 Chicago Bridge & Iron Co Multiple effect evaporating system
US3152053A (en) * 1960-07-26 1964-10-06 Joseph P Lynam Sea water conversion apparatus

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2759882A (en) * 1954-07-30 1956-08-21 Bethlehem Steel Corp Combined flash and vapor compression evaporator
US2893926A (en) * 1957-06-13 1959-07-07 Bethlehem Steel Corp Combined flash type distilling plant and back-pressure turbo-generator
US3021265A (en) * 1957-07-05 1962-02-13 Chicago Bridge & Iron Co Multiple effect evaporating system
US3152053A (en) * 1960-07-26 1964-10-06 Joseph P Lynam Sea water conversion apparatus

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3344041A (en) * 1963-12-20 1967-09-26 Wulfson Dov Multistage flash distillation of saline water
US3396086A (en) * 1964-12-23 1968-08-06 Applied Res And Engineering Lt Recompression evaporators
US3433717A (en) * 1965-03-01 1969-03-18 Aqua Chem Inc Multistage flash still with vapor compression plant
US3501384A (en) * 1965-12-21 1970-03-17 Applied Research & Eng Ltd Low pressure degassing of feed water in multi-stage flash evaporators
US3511756A (en) * 1967-03-13 1970-05-12 Lummus Co Flash evaporation with series arranged with solar heating zone
US3515646A (en) * 1967-04-19 1970-06-02 Weir Westgarth Ltd Vertical multi-stage flash evaporator with separate horizontal condensing chamber
US3514375A (en) * 1967-05-25 1970-05-26 Fives Lille Cail Water desalination distillation including evaporator and compressor
US3859174A (en) * 1972-11-14 1975-01-07 Fred W Taylor Recovery of potable water from sanitary waste using solid wastes and refuse as a heat source
US4110174A (en) * 1976-12-16 1978-08-29 Uop Inc. Power generation and potable water recovery from salinous water
US4313305A (en) * 1979-09-18 1982-02-02 Dan Egosi Feedback energy conversion system
US4434027A (en) 1980-03-17 1984-02-28 Stork Friesland B.V. Method for the evaporation of a liquid solution using mechanical compression
WO2012127406A1 (en) * 2011-03-21 2012-09-27 I.D.E. Technologies Ltd. A compound multi effect distillation system
US10220328B2 (en) 2011-03-21 2019-03-05 Yaniv Schmidt Combined multi effect distillation system
US10780369B2 (en) 2011-03-21 2020-09-22 I.D.E. Technologies Ltd Combined multi effect distillation system
US9539522B1 (en) * 2015-12-01 2017-01-10 Kuwait Institute For Scientific Research Combination multi-effect distillation and multi-stage flash evaporation system
CN113753919A (zh) * 2021-09-24 2021-12-07 天津黄埔盐化工程技术有限公司 一种从垃圾焚烧飞灰水洗液中提取钾盐的方法

Also Published As

Publication number Publication date
DE1517493A1 (de) 1969-05-22
GB1047981A (en) 1966-11-09
NL285240A (enrdf_load_stackoverflow)

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