US3291704A - Distillation apparatus having corrugated heat transfer surfaces - Google Patents

Distillation apparatus having corrugated heat transfer surfaces Download PDF

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Publication number
US3291704A
US3291704A US291569A US29156963A US3291704A US 3291704 A US3291704 A US 3291704A US 291569 A US291569 A US 291569A US 29156963 A US29156963 A US 29156963A US 3291704 A US3291704 A US 3291704A
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United States
Prior art keywords
wall
heat transfer
distilland
depressions
inch
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Expired - Lifetime
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US291569A
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English (en)
Inventor
Diedrich Gunther Ernst
Charles W Lotz
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General Electric Co
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General Electric Co
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Publication date
Application filed by General Electric Co filed Critical General Electric Co
Priority to US291569A priority Critical patent/US3291704A/en
Priority to DE1444340A priority patent/DE1444340C3/de
Priority to CH249063A priority patent/CH431456A/de
Priority to NL6404273A priority patent/NL6404273A/xx
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Publication of US3291704A publication Critical patent/US3291704A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
    • 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
    • C02F1/08—Thin film evaporation

Definitions

  • This invention relates generally to distillation apparatus and more particularly to a high performance heat transfer wall to be used in saline water distillation apparatus.
  • water is considered to be saline when it contains 1000 or more parts of salt per million parts of water, while it is considered to be fresh when it has fewer than 1000 parts per million of salt.
  • Sea water contains about 35,000 parts per million of salt.
  • One process for removing dissolved salts from saline water is that of distillation, which may be per formed by bringing the saline water into contact with a hot surface in order to evaporate the water and leave the salt behind, and then condensing the vapors which are produced upon a cool surface in the form of fresh water.
  • the heat needed to produce water vapor from saline water or distilland which is in contact with one surface or side of a heat transfer Wall may be supplied by stream, for example, exhaust steam from a turbine, or by a vapor previously produced in a still, which is condensed on the other side of the heat transfer Wall.
  • the rate at which the distilland is evaporated from a given area of the heat transfer surface is dependent on the rate at which heat is transferred to the distilland, normally measured in terms of B.t.u.s/hr. sq. ft.
  • This heat transfer rate is dependent on the overall thermal resistance presented by the heat transfer wall itself, together with that of the layer of distilland on one Side and the layer of condensate on the other. Every material has a certain resistance to heat transfer and this resistance multipled by the thickness of the material can be used to calculate the thermal resistance of a particular layer or the combined thermal resistance of multiple layers.
  • the thermal resistance of water is quite high, while that of materials from which a heat transfer wall is normally made, for example copper, is relatively low.
  • Other variables being constant, the way to maximize the heat transfer rate is ot keep the layers of distilland and condensate as thin as possible over the whole area of the heat transfer surface, with this limitation; namely, that no part of the surface on the distilland side becomes dry.
  • the advantages of a high heat transfer rate are that the size of the still to produce a given quantity of fresh water of a desired degree of purity from saline water in a given time is minimized.
  • the investment in plant to produce the water is, therefore, less, so that the use of high heat transfer rate distillation apparatus will tend to reduce the cost of the fresh water produced.
  • whether fresh water will be produced from saline water depends on the cost of the water so produced. Any reduction in cost will increase the competitive position of fresh water produced from saline water.
  • the surface described in the above reference is designed for use in condensing steam, and is not particularly suitable for use in evaporating saline water since the small grooves are quite easily clogged by the formation of scale.
  • the formation of scale occurs when the distilland in a particular surface area is completely evaporated, leaving the salts which were previously in solution as a deposite on the surface. This result is avoided, if possible, by not entirely evaporating the distilland; however, over a period of time, perhaps due to slight variations in the distilland feed rate, some scale may be formed.
  • evaporating and condensing surfaces are constructed on opposite sides of a heat transfer wall which may be used in distillation apparatus.
  • the configuration of these surfaces is generally a series of elongated parallel protuberances or convolutions. These protuberances or convolutions are of such dimensions that they can easily be formed by using a die, rolling or extrusion.
  • the saline water or distilland is delivered to the evaporating surface near its top so that it will run down the surface between the protuberances under the influence of gravity. The amount of distilland supplied does not completely fill the area between the protuberances.
  • the heat transferred through the wall from the condensing surface causes the distilland to boil which splashes the distilland over the surfaces of the protuberances.
  • the wall is constructed of a material which the distilland wets or adheres to, but at the same time, the surface tension of the distilland tends to pull any excess distilland into the depressions between the protuberances.
  • the overall eflect is that the distilland spreads in a very thin film over the surfaces of the protuberances. This film is continuously replenished, as it evaporates, by more distilland splashing from the grooves.
  • the length of the wall and the rate at which the distilland is supplied are chosen so that no precipitation of salts occurs from the distilland.
  • the vapor evolved from the evaporating surface is thereafter exposed to a condensing surface of another similarly constructed heat transfer wall positioned in the vicinity of the evolved vapors. If desired, the vapor may be condensed on the opposite or condensing side of the same heat transfer wall, provided a sufficient elevation in pressure is first given the vapor.
  • the condensing surface of the heat transfer wall is cooled, by the transfer of heat to the distilland, below the vaporization temperature of water at the pressure involved, so that the vapor condenses on this surface.
  • This condensed vapor or distillate flows from the crests of the protuberances into the adjacent grooves under the influence of gravity and surface tension and is collected at the bottom of the wall.
  • the thickness of the condensate layer on the protuberances is, therefore, kept very thin so that the heat transfer rate is maximized.
  • FIGURE 1 is a schematic isometric of a portion of a heat transfer wall in accordance with one embodiment of the invention
  • FIGURE 2 is a schematic plan, in a cross-section of a wall having a heat transfer surface in accordance with the invention
  • FIGURE 3 is a schematic elevation of a distillation apparatus incorporating the heat transfer wall of this invention.
  • FIGURE 4 is a schematic elevation of a modified form a portion of the apparatus of FIGURE 3.
  • Heat transfer wall is of a generally corrugated appearance so that both of the surfaces are provided with a plurality of protuberances 12 separated by depressions 14.
  • One surface of wall 10, for example surface 16 may be utilized as an evaporating surface while the opposite surface 18 is operated as a condensing surface.
  • Evaporating surface 16 can be effectively used by applying distilland near the upper end of this surface so that it flows downwardly under the influence of gravity.
  • surface 16 is properly designed and constructed, it is found that the distilland does not flow evenly over the entire surface, but instead collects in depressions 14, leaving only a thin film of distilland on protuberances 12.
  • condensing surface 18 it is observed that the condensate tends to collect in depressions 14, thereby continually exposing protuberances 12 to new steam or vapor and keeping the overall thermal resistance of the condensing surface low.
  • the condensate flows down influence of gravity so that it may be conveniently collected at the bottom of the wall.
  • a chamber 20 is provided with heat transfer walls 22 and 24 constructed in accordance with the invention as illustrated in FIGURE 1, to divide the chamber into three compartments 26, 28 and 30.
  • steam from any source such as a boiler, exhaust steam from a turbine, etc. is admitted through inlet pipe 32 so that the left or condensing surface of heat transfer 'wall 22 is heated to a temperature 1 Due to the transfer of heat from the steam to wall 22, steam condenses on this surface and the condensate flows into the grooves down the condensing surface of the wall in the manner previously described.
  • Outlet pipe 34 is provided to remove this condensate from compartment 26.
  • Saline water or distilland is admitted to compartment 28 through inlet pipe 36.
  • Deflector 38 is provided to distribute this distilland substantially evenly over the width of the right or evaporating surface of heat transfer wall 22 at or near the top of this surface.
  • tube 39 having perforations along its length has been used to spray distilland on the evaporating surface.
  • the distilland is preferably provided at a rate which fills the depressions of the evaporating surface without overflowing the crests of the protuberances so that the full advantages of this invention are realized.
  • the distilland is admitted to compartment 28 at a temperature t lower than temperature t on the opposite side of wall 22. Heat is transferred through wall 22 to the distilland due to the temperature difference.
  • distilland evaporates while any excess flows down wall 22 and is discharged through outlet pipe 40 as a concentrated salt solution or brine. About 75 percent of the distilland supplied can be safely evaporated without causing the precipitation of the salts in the brine.
  • Outlet pipe 42 is provided to remove this distillate (now fresh water) from compartment 28. Barrier 44 prevents mixing of the distillate with the excess distilland.
  • the vapors which condense on the condensing surface of heat transfer wall 24- raise the temperature of this surface to a temperature i
  • the right surface of this wall is cooled to a temperature t lower than temperature t within chamber 28 by cool saline Water which is admitted to compartment 30 through inlet pipe 46 and spread across the right surface of heat transfer wall 24 by deflector 48.
  • Tube 49, illustrated in FIGURE 4 may be substituted for deflector 48.
  • the cool saline water is elevated in temperature during its passage down this surface and discharged through outlet pipe 50. This heated saline water may be the supply for inlet pipe 36. 1
  • H represents the height of the protuberance from depressions 14 under the base to peak or the depth of the depression
  • P represents the pitch, or distance between similar points on adjacent protuberances
  • T represents the thickness of the heat transfer wall
  • L represents the length of the wall.
  • a copper sheet of thickness (T) of about 0.040 inch was corrugated to yield a height (H) of about 0.062 inch and a pitch (P) of about 0.125 inch.
  • An average temperature difference between condensing surface 18 and evaporating surface 16 over the length (L) of the wall of F. was maintained with L made about 54 inches.
  • height (H) may be from 0.025 to 0.250 inch
  • pitch (P) may be from 0.050 to 0.500 inch
  • Thickness (T) as in any heat transfer wall should be minimized.
  • length (L) may be selected in accordance with the dimensions of height (H) in a ratio of from 50:1 to 5000zl. The particular length selected is determined by the operating condition of the distillation apparatus in which the wall is to be used. Since the evaporating heat transfer surface 16 only operates as described when the distilland collects in depressions 14 leaving the crests of protuberances 12 with only a thin film, distilland should be applied to the upper end of surface 16 at a rate which achieves this. In addition, it can be seen that as the distilland progresses downward, more and more will be evaporated and eventually surface 16 could become completely dry. This result is undesirable since the salts form on the surface as scale.
  • Evaporation occurs at a rate which increases as the temperature difference between condensing surface 18 and evaporating surface 16 increases provided the pressures associated with these processes are not varied. Where this temperature difference is high, the length of the wall may be shorter; while as the temperature difference decreases, the length may be increased. The length of the wall should not be increased to the point where the distillate upon the condensing surface completely fills the depressions so that the protuberances cannot be drained and exposed to new vapors.
  • the factor (t -t represents the difference between the temperatures on the opposite sides of the wall, while R represents the resistance to heat flow of the wall. It is evident that decreasing R increases Q, the heat transfer rate.- Since both evaporation and condensation occur on the surfaces of whatever thicknesses of liquid may be present on the wall, it is necessary for the heat to be transferred from the surface of the condensing liquid through this layer of liquid to the wall. The heat, after then passing through the wall, passes through the layer of distilland to the surface of this liquid where the surface molecules evaporate.
  • R and R represent the individual resistances of the liquid condensing layer and liquid evaporating layer respectively.
  • the forming of the heat transfer wall of this invention is preferably accomplished by corrugating a thin metal sheet, in some cases it may be desirable to use a heavier gage stock and to form the protuberances by some other method. In such cases, the protuberance of one surface need not also be the depression of the other surface.
  • the evaporating and condensing surfaces of this invention can be used individually.
  • said protuberances being substantially parallel and having (1) a pitch P of from 0.050 inch to 0.500
  • a heat transfer wall for water distillation apparatus comprising:
  • corrugated copper sheet having a thickness T of from 0.025 inch to 0.125 inch; the corrugations on said sheet providing an evaporating surface on one side of said wall and a condensing surface on the other side thereof, said surfaces consisting of a plurality of elongated protuberances separated by depressions,
  • said protuberances being substantially parallel and having (1) a pitch P of from 0.050 inch to 0.500
  • said protuberances being substantially parallel and having (1) a pitch P of from 0.050 inch to 0.500
  • said sheet being formed into parallel convolutions comprising closely spaced parallel depressions separated by crests between said depressions on both surfaces of the sheet,
  • a chamber having a side wall comprised of material of high thermal conductivity, the inner surface of said sidewall being convoluted to provide a plurality of closely spaced parallel depressions separated by crests between said depressions, said crests and depressions extending in a substantially vertical direction down the inner surface of said sidewall;
  • said sidewall have a length L which comprises to H in a ratio range of approximately 50:1 to 500021, thereby to cause said distilland to be attracted from the crests to the depressions by surface tension; means to apply heat to the external surface of said sidewall suflicient to cause said distilland to boil in the depressions producing vapor bubbles therein which break spreading distilland from the depressions thin 1y over the crests thereby increasing production of vapor from the crests and eliminating dry areas; and
  • a vaporization chamber having two broadside substantially vertical walls of high heat conductive material
  • both of said walls comprising parallel convolutions extending lengthwise of said exterior and interior surfaces thereof
  • the convolutions of said walls having a pitch P measured between successive crests, a height H measured from the crests to the depths of said depressions, and a thickness T of from approximately 0.025 inch to 0.125 inch, and wherein the ratio P/H is approximately 2:1 so that liquid on the crests is attracted to the depressions by surface tension whereby said depressions provide drainage down said interior surfaces leaving said interior crests with thin films of liquid thereby increasing heat transfer through said walls and increasing distillation.
  • a vaporization chamber having two broadside substantially vertical walls of high heat conductive material
  • both of said walls comprising parallel convolutions extending lengthwise of said exterior and interior surfaces thereof
  • the convolutions of said walls having a pitch P measured between successive crests, a height H measured from the crests to the depths of said depressions, and a thickness T of from approximately 0.025 inch to 0.125 inch, said wall having a length L which compares to H in a ratio range of approximately 50:1 to 500011, whereby in operation liquid on the crests is attracted to the depressions by surface tension whereby said depressions provide drainage down said surfaces leaving the crests with thin films of liquid for increased vaporization on said one surface and increased condensation at the other of said surfaces.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
US291569A 1963-06-28 1963-06-28 Distillation apparatus having corrugated heat transfer surfaces Expired - Lifetime US3291704A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US291569A US3291704A (en) 1963-06-28 1963-06-28 Distillation apparatus having corrugated heat transfer surfaces
DE1444340A DE1444340C3 (de) 1963-06-28 1963-12-19 Verwendung eines Wärmeaustauscherelements mit gewellter Wand für eine Salzwasserd estilliereinrichtung
CH249063A CH431456A (de) 1963-06-28 1964-01-20 Wärmetauscher-Element
NL6404273A NL6404273A (de) 1963-06-28 1964-04-20

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CH (1) CH431456A (de)
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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3453181A (en) * 1965-12-21 1969-07-01 Gen Electric Evaporator unit with integral liquid heater
US3458405A (en) * 1966-04-22 1969-07-29 John N Akers Distillation system with vertically stacked horizontally inclined evaporators
US3568766A (en) * 1969-03-11 1971-03-09 Atomic Energy Commission Corrugated heat exchange member for evaporation and condensation
US3664928A (en) * 1969-12-15 1972-05-23 Aerojet General Co Dimpled heat transfer walls for distillation apparatus
US3895676A (en) * 1971-12-17 1975-07-22 Phillips Petroleum Co Heat exchanger distributor
US4253519A (en) * 1979-06-22 1981-03-03 Union Carbide Corporation Enhancement for film condensation apparatus
US4398596A (en) * 1978-08-09 1983-08-16 Commissariat A L'energie Atomique Plate-type heat exchangers
US4731159A (en) * 1983-03-01 1988-03-15 Imperial Chemical Industries Plc Evaporator
US4853088A (en) * 1988-04-12 1989-08-01 Marathon Oil Company Solar enhanced separation of volatile components from a liquid
US5045155A (en) * 1989-09-11 1991-09-03 Arnold Ramsland Centrifugal distillation apparatus
US5411640A (en) * 1990-11-09 1995-05-02 Ramsland; Arnold Centrifugal distillation apparatus
US5417805A (en) * 1993-03-09 1995-05-23 Rosenblad; Axel E. Brushed film evaporator
US5558748A (en) * 1995-05-12 1996-09-24 Basf Corporation Plate-type distillation/condensation apparatus and method of use
US20050279620A1 (en) * 2004-06-17 2005-12-22 Ovation Products Corporation Blade heat exchanger
US20080135529A1 (en) * 2006-12-08 2008-06-12 Kuchuk-Yatsenko Viktor S Method of resistance butt welding
US20080237026A1 (en) * 2007-03-26 2008-10-02 Zanaqua Technologies Blade-type-heat-exchanger distiller with inter-blade passages

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US491028A (en) * 1893-01-31 Water-distilling apparatus
US1359276A (en) * 1919-06-28 1920-11-16 William A Rushworth Distilling apparatus
US2440245A (en) * 1944-03-13 1948-04-27 Standard Telephones Cables Ltd Cooling of high-temperature bodies
US2445471A (en) * 1944-05-09 1948-07-20 Salem Engineering Company Heat exchanger
US2514944A (en) * 1945-02-22 1950-07-11 Atlantic Refining Co Falling film distillation apparatus
FR978997A (fr) * 1942-01-16 1951-04-20 évaporateur continu pouvant fonctionner à la pression atmosphérique, sous pression ou sous vide et applications diverses de cet appareil
FR1000940A (fr) * 1948-12-11 1952-02-18 Escher Wyss Ag échangeur de chaleur
US2642897A (en) * 1948-05-13 1953-06-23 Rover Co Ltd Heat interchange apparatus
US2894879A (en) * 1956-02-24 1959-07-14 Kenneth C D Hickman Multiple effect distillation
US3047271A (en) * 1958-08-07 1962-07-31 Stewart Warner Corp Brazed plate and ruffled fin heat exchanger
US3175962A (en) * 1961-02-28 1965-03-30 Gen Electric Falling film evaporator

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US491028A (en) * 1893-01-31 Water-distilling apparatus
US1359276A (en) * 1919-06-28 1920-11-16 William A Rushworth Distilling apparatus
FR978997A (fr) * 1942-01-16 1951-04-20 évaporateur continu pouvant fonctionner à la pression atmosphérique, sous pression ou sous vide et applications diverses de cet appareil
US2440245A (en) * 1944-03-13 1948-04-27 Standard Telephones Cables Ltd Cooling of high-temperature bodies
US2445471A (en) * 1944-05-09 1948-07-20 Salem Engineering Company Heat exchanger
US2514944A (en) * 1945-02-22 1950-07-11 Atlantic Refining Co Falling film distillation apparatus
US2642897A (en) * 1948-05-13 1953-06-23 Rover Co Ltd Heat interchange apparatus
FR1000940A (fr) * 1948-12-11 1952-02-18 Escher Wyss Ag échangeur de chaleur
US2894879A (en) * 1956-02-24 1959-07-14 Kenneth C D Hickman Multiple effect distillation
US3047271A (en) * 1958-08-07 1962-07-31 Stewart Warner Corp Brazed plate and ruffled fin heat exchanger
US3175962A (en) * 1961-02-28 1965-03-30 Gen Electric Falling film evaporator

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3453181A (en) * 1965-12-21 1969-07-01 Gen Electric Evaporator unit with integral liquid heater
US3458405A (en) * 1966-04-22 1969-07-29 John N Akers Distillation system with vertically stacked horizontally inclined evaporators
US3568766A (en) * 1969-03-11 1971-03-09 Atomic Energy Commission Corrugated heat exchange member for evaporation and condensation
US3664928A (en) * 1969-12-15 1972-05-23 Aerojet General Co Dimpled heat transfer walls for distillation apparatus
US3895676A (en) * 1971-12-17 1975-07-22 Phillips Petroleum Co Heat exchanger distributor
US4398596A (en) * 1978-08-09 1983-08-16 Commissariat A L'energie Atomique Plate-type heat exchangers
US4253519A (en) * 1979-06-22 1981-03-03 Union Carbide Corporation Enhancement for film condensation apparatus
US4731159A (en) * 1983-03-01 1988-03-15 Imperial Chemical Industries Plc Evaporator
US4853088A (en) * 1988-04-12 1989-08-01 Marathon Oil Company Solar enhanced separation of volatile components from a liquid
US5045155A (en) * 1989-09-11 1991-09-03 Arnold Ramsland Centrifugal distillation apparatus
US5411640A (en) * 1990-11-09 1995-05-02 Ramsland; Arnold Centrifugal distillation apparatus
US5417805A (en) * 1993-03-09 1995-05-23 Rosenblad; Axel E. Brushed film evaporator
US5558748A (en) * 1995-05-12 1996-09-24 Basf Corporation Plate-type distillation/condensation apparatus and method of use
US20050279620A1 (en) * 2004-06-17 2005-12-22 Ovation Products Corporation Blade heat exchanger
US7427336B2 (en) * 2004-06-17 2008-09-23 Zanaqua Technologies, Inc. Blade heat exchanger
US20080135529A1 (en) * 2006-12-08 2008-06-12 Kuchuk-Yatsenko Viktor S Method of resistance butt welding
US8426762B2 (en) * 2006-12-08 2013-04-23 E.O. Paton Electric Welding Institute Of The National Academy Of Sciences Of Ukraine Method of resistance butt welding using corrugated flux-filled metal inserts
US20080237026A1 (en) * 2007-03-26 2008-10-02 Zanaqua Technologies Blade-type-heat-exchanger distiller with inter-blade passages

Also Published As

Publication number Publication date
DE1444340A1 (de) 1968-11-28
DE1444340B2 (de) 1975-01-30
NL6404273A (de) 1964-12-29
DE1444340C3 (de) 1975-09-25
CH431456A (de) 1967-03-15

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