WO2006054936A1 - Ensemble echangeur de chaleur a evaporation - Google Patents

Ensemble echangeur de chaleur a evaporation Download PDF

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Publication number
WO2006054936A1
WO2006054936A1 PCT/SE2005/001658 SE2005001658W WO2006054936A1 WO 2006054936 A1 WO2006054936 A1 WO 2006054936A1 SE 2005001658 W SE2005001658 W SE 2005001658W WO 2006054936 A1 WO2006054936 A1 WO 2006054936A1
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WO
WIPO (PCT)
Prior art keywords
heat exchanger
plant
stages
liquid
supplied
Prior art date
Application number
PCT/SE2005/001658
Other languages
English (en)
Inventor
Ralf Erik Blomgren
Henning Paaske
Bo Juul Andersen
Joakim Krantz
Original Assignee
Alfa Laval Corporate Ab
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 Alfa Laval Corporate Ab filed Critical Alfa Laval Corporate Ab
Priority to JP2007541135A priority Critical patent/JP4762997B2/ja
Priority to KR1020077011093A priority patent/KR101225303B1/ko
Priority to DE112005002537T priority patent/DE112005002537T5/de
Publication of WO2006054936A1 publication Critical patent/WO2006054936A1/fr

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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
    • 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
    • C02F1/08—Thin film evaporation
    • 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
    • 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)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B01D5/0015—Plates
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F28F3/08—Elements constructed for building-up into stacks, e.g. capable of being taken apart for cleaning
    • F28F3/083—Elements constructed for building-up into stacks, e.g. capable of being taken apart for cleaning capable of being taken apart
    • 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

Definitions

  • the present invention refers generally to a heat exchanger plant for distillation.
  • the invention refers especially to heat exchanger plants for desalination of seawater. More specifically, it is referred to a heat exchanger plant for distillation, comprising at least one proc ⁇ ess line with least two successive heat exchanger stages which each comprises a plate package of heat exchanger plates provided in such a way in the plate package that first plate interspaces for condensation and second plate interspaces for evaporation are formed, wherein each heat exchanger stage is adapted to perform condensation of steam and evaporation of a liquid in such a way that the first heat exchanger stage is adapted to be supplied with steam to the first plate interspaces and a liquid to the second plate interspaces, wherein the supplied steam is condensed to a liquid and the supplied liquid is evaporated and supplied to the first plate interspaces in the next heat exchanger stage for evaporation of a liquid supplied to the second plate interspaces in this next heat ex- changer stage, and wherein the plant comprises a
  • the applicant produces since many years equipment for desalina ⁇ tion of seawater, where packages with heat exchanger plates form the main components in the process.
  • the plates have no ports for steam, but instead the plate packages are positioned in containers, and the space outside the plates is used as one or several flow paths for the steam, depending on the type of process.
  • the large plants use cylindrical pressure vessels, and the plate packages are positioned in the longitudinal direction of the cylinder. A large plant frequently has five or even six plate packages.
  • the process takes place in several so-called effects at a pressure that everywhere is below the atmospheric pressure.
  • Steam from the first effect which has the highest pressure and temperature, passes to the second effect where it is condensed in the plate interspaces for condensation.
  • the heat emitted provides an evaporation of salt water in intermediate interspaces for evaporation, and the steam formed passes to the next effect.
  • the process is repeated in the other effects, and finally a condensation takes place in the con ⁇ denser, where the cooling medium is water.
  • the plate packages should not have more than 1000-1200 plates, so that if more plates are required two parallel plate packages are included in each effect.
  • US-A-4, 511 ,436 discloses a plant for desalination of seawater.
  • the plant comprises a process line with several successive heat ex ⁇ changer stages which each comprises a plate package of heat ex ⁇ changer plates that are welded in pairs to each other and provided in such a way in the plate package that first interspaces for conden- sation and second interspaces for evaporation are formed.
  • the process line of heat exchanger plates extends vertically, wherein the first stage is located at the top.
  • the two lines are provided in a closed pressure container, which is schematically disclosed in this docu ⁇ ment.
  • US-A-4, 514, 260 discloses a similar plant with a number of plate packages provided on each other in a vertical pile having a height which is substantially larger than the width and the length in a horizontal plane.
  • the plate packages are enclosed in a casing.
  • the casing has two vertical opposite plane sides and two vertical opposite outwardly curved sides.
  • the object of the invention is to provide a heat exchanger plant which has a very large capacity and which can be manufactured and mounted in a favourable manner with regard to the costs.
  • a fur- ther object of the invention is to provide such a heat exchanger plant that has such a construction that the plant can be large and include a large number of heat exchanger stages.
  • the heat exchanger plant ini- tially defined which is characterized in that it comprises at least two such process lines with successive heat exchanger stages, that said process lines extend in parallel to each other in the inner space, wherein the heat exchanger stages form rows with heat ex ⁇ changer stages which are provided after each other and trans- versely to said process lines in the inner space within the casing, and that the casing seen in a cross-section transversely to said process lines has a rectangular shape.
  • Each such row of heat exchanger stages which each comprises a plate package, form a so-called effect of the plant. Since an enclos ⁇ ing casing with a rectangular shape is used instead of conventional cylindrical containers, the costs may be significantly reduced. The shape of the casing may then in a better way be adapted to the outer contour formed by the rows of heat exchanger stages in the plant seen transversally to said lines.
  • Pressure vessels are normally made to be cylindrical since it is an optimum shape with respect to the strength and which thus gives a minimum need of material. If the pressure vessel is subjected to external over pressures, this axiom is not as self evident, since the construction could collapse due to instability.
  • the casing is provided with strengthening rings, but in spite thereof a thickness, which is 4-5 times larger than in a cylindrical vessel subjected to an inner over pressure, is required. Since desalination plants operate at a deep vacuum the statements made above are valid. A cylindrical container does not give a particularly large saving of material in comparison with a square one, and the more parallel plate packages that are positioned in the container the smaller is the material saving. It should be remembered that the material merely constitutes a small part of the costs for a final container, and it is not at all sure that the construction having the smallest material need gives the lowest cost. There are several factors which are important for the total economy.
  • the plant comprises at least three such parallel process lines with successive heat exchanger stages.
  • Each row comprises thus three beside each other arranged heat exchanger stages, which together form an ef ⁇ fect of the plant.
  • a plant may advantageously com- prise at least four such parallel process lines with successive heat exchanger stages.
  • each heat ex ⁇ changer stage is designed as a module comprising a part of the casing and adapted to be connected with respect to the flow to at least one of a preceding and a successive module in the same process line.
  • each heat ex ⁇ changer stage is designed as a module comprising a part of the casing and adapted to be connected with respect to the flow to at least one of a preceding and a successive module in the same process line.
  • the rectangular casing is advantageous since it in an easy manner may be divided in two such modules which can be manufactured in a rational manner at the factory and then trans ⁇ ported in a relatively easy manner to the mounting site.
  • each module is designed as either an inner module, which is adapted to be pro ⁇ vided between two adjacent modules in the same row, or an outer module, which is adapted to be provided adjacent to merely one ad ⁇ jacent module in the same row. From a designing point of view there are thus two modules.
  • the outer module is present in a right design and a left design, but since these can be made completely symmetrical they only form one construction.
  • each module may be adapted to be connected with respect to the flow to at least one adjacent module in the same row.
  • said part of the casing of each module may be adapted to be connected mechanically to at least one adjacent module in the same row and to at least one of a preceding and successive module in the same process line.
  • each process line comprises at least three such successive heat exchanger stages, wherein at least a part of the liquid which is evaporated in the second heat exchanger stages is supplied to the first plate interspaces of the third heat exchanger stages for evaporation of a liquid supplied to the second plate interspaces of the third heat ex ⁇ changer stages.
  • each process line may advanta ⁇ geously comprise at least four such successive heat exchanger stages, wherein at least a part of the liquid which is evaporated in the third heat exchanger stages is supplied to the first plate inter ⁇ spaces of the fourth heat exchanger stages for evaporation of a liq ⁇ uid supplied to the second plate interspaces of the fourth heat ex ⁇ changer stages.
  • Each process line may of course comprise further such successive heat exchanger stages, for instance five, six, seven, eight, nine or more.
  • the casing is designed to permit the maintaining of a substantially lower pressure in the inner space then in the surroundings outside the casing.
  • the plant is de ⁇ signed in such a way that the rows with the heat exchanger stages extend substantially horizontally.
  • the plant is de ⁇ signed in such a way that the process lines extend substantially horizontally.
  • the plant is de ⁇ signed in such a way that the process lines extend substantially vertically.
  • the costs for the casing may be fur ⁇ ther reduced if the plate packages are positioned in several rows in several planes. With such a design, the outer surface and the re- quired ground area may be minimized.
  • the first plate interspaces and the second plate interspaces in the plate packages are sealed by means of gaskets. In such a way the plate packages may be opened for cleaning and repair.
  • a liquid separa ⁇ tor is provided in each process, line in connection to substantially each heat exchanger stage.
  • the plant com ⁇ prises a thermo compressor which is adapted to be operated through the supply of external steam at a high pressure and which is adapted to receive at least a part of the steam produced in at least the last heat exchanger stages for mixing of this part and the external steam, wherein the mixture forms said steam supplied to the first heat exchanger stages.
  • Fig. 1 discloses a sectional view from the side through a heat exchanger plant according to a first embodiment of the invention.
  • Fig. 2 discloses a sectional view from above through the plant in Fig. 1.
  • Fig. 3 discloses a side view of a heat exchanger stage of the plant in Fig. 1.
  • Fig. 4 discloses a sectional view through the plant in Fig. 1 along the line IV-IV.
  • Fig. 5 discloses a view of a first outer module of the heat ex ⁇ changer plant in Fig. 1.
  • F Fiigg.. 6 6 discloses a view of an inner module of the heat ex ⁇ changer plant in Fig. 1.
  • Fig. 7 discloses a view of a second outer module of the heat exchanger plant in Fig. 1.
  • Fig. 8 discloses a side view of the plant in Fig. 1.
  • F Fiigg.. 99 discloses a first sectional view from the side through a heat exchanger plant according to a second embodiment of the invention.
  • Fig. 10 discloses a second sectional view through the heat ex ⁇ changer plant in Fig. 9 along the line X-X.
  • Figs. 1-4 disclose a heat exchanger plant for distillation, especially for desalination of seawater.
  • the heat exchanger plant disclosed comprises a four process lines 1.
  • Each process line 1 which ex- tends in a longitudinal direction of the plant, comprises five successive ⁇ sive heat exchanger stages 2a-2e, which each comprises a plate package 3 of heat exchanger plates 4 provided in such a way in the plate package 3 that first plate interspaces 5 and second plate interspaces 6 are formed.
  • the four process lines 1 extend in paral- IeI to each other in such a way that the heat exchanger stages 2a- 2e form rows 8 of heat exchanger stages 2a-2e.
  • rows 8 lies after each other and extend in a transversal di ⁇ rection of the plant, i.e. transversally to the process lines 1.
  • the rows 8 extend in the embodiment disclosed substantially perpen ⁇ dicularly to the parallel longitudinal process lines 1. It is to be noted that the plant according alternative designs may comprise another number of rows 8 and process lines 1 then the ones disclosed.
  • the plant comprises a closed casing 10, which encloses an inner space 11 in which the four process lines 1 with heat exchanger stages 2a-2e are provided.
  • the casing 10 is designed as a pressure container permitting the maintaining of a substantially lower pres ⁇ sure in the inner space 11 than in the surrounding atmosphere di ⁇ rectly outside the casing 10.
  • a separation wall 12 extends substan ⁇ tially horizontally in the casing 10 and divides the inner space 11 into substantially two longitudinal halves.
  • the different heat exchanger stages 2a-2d are separated from each other through vertical walls 18, 18'.
  • the walls 12, 18 and 18' thus create a number of upper spaces 13 and a number of lower spaces 14, see Fig. 3.
  • Each plate package 3 is provided in such a way that it ex ⁇ tends through the separation wall 12, wherein an upper part of the plate package 3 is located in such an upper space 13, and a lower part of the plate package 3 in such a lower space 14.
  • Each plate package 3 may be kept together by for instance four tie bolts (not disclosed), which extend through a frame plate and a pressure plate (not disclosed) of each plate package 3.
  • tie bolts not disclosed
  • pressure plate not disclosed
  • gaskets 15 and 15' are provided for sealing the plate interspaces 5 and 6.
  • gaskets 15 are pro ⁇ vided in such a way that the first plate interspaces 5 for condensa- tion are sealed against the respective lower space 14, and gaskets 15' are provided in such a way that the second plate interspaces 6 for evaporation are sealed against the respective upper space 13, see Fig. 3.
  • the plant comprises a passage through the separation wall 12 between each heat exchanger stage 2a-2b, 2b-2c, 2c-2d and 2d-2e.
  • a liquid separator 16a-16d is provided in substantially each such passage.
  • the plant also comprises a thermo compressor 20 which is adapted to be operated through the supply of external steam at a high pres ⁇ sure in a manner known per se.
  • the external steam is supplied to the thermo compressor 20 via a supply conduit 21.
  • the thermo compressor 20 supplies steam at a pressure and a temperature to the first heat exchanger stages 2a via an inlet conduit 22. This pressure and this temperature correspond to the pressure and tem ⁇ perature in the first heat exchanger stages 2a, but is lower than the surrounding atmospheric pressure and the surrounding tempera ⁇ ture, respectively.
  • the pressure and the temperature decrease then successively in the successive heat exchanger stages 2b-2e.
  • thermo compressor 20 A part of the steam which is discharged from one or several of the last heat exchanger stages, in this example the penultimate heat ex- changer stages 2d, is returned to the thermo compressor 20 via a conduit 23.
  • the thermo compressor 20 comprises a nozzle for the recirculation of the returned steam to the inlet conduit 22 by means of the external steam.
  • the liquid to be distilled in this example a salt-bearing liquid, so called brine, is supplied via a schematically disclosed feed conduit 30.
  • the feed conduit 30, which may be more complex than dis ⁇ closed in Fig. 1 , is arranged to provide a salt-bearing liquid at a temperature that is adapted to the temperature in each stage 2a-2d.
  • the salt-bearing liquid is supplied to the second plate interspaces 6 in each plate package 3 in the four first heat exchanger stages 2a- 2d via the feed conduit 30 and a port channel 31 in each plate package 3, see Fig. 4.
  • the liquid supplied will be heated and at least partly evaporated by the steam in the adjacent first plate inter ⁇ spaces 5.
  • the last heat exchanger stages 2e are pure condensation stages for the condensation of the steam from the preceding heat exchanger stages 2d.
  • the condensation may be provided through circulation of an external cooling agent by means of a circulation conduit 32 and suitable port channels in each plate package 3 in the last heat exchanger stages 2d. At least a part of the external cooling agent may via the feed conduit 30 be supplied to the different heat exchanger stages 2a-2d.
  • the heat exchanger stage 2e is then used for preheating of a salt-bearing liquid, see Fig. 1.
  • Each heat exchanger stage 2a-2e is thus adapted to perform con ⁇ densation of steam in the first plate interspaces 5. Furthermore, each heat exchanger stage 2a-2d, except the last heat exchanger stages 2e, are adapted to perform evaporation of a liquid in the second plate interspaces 6. More specifically, the first heat ex ⁇ changer stages 2a are supplied with steam to the first plate inter ⁇ spaces 5 via the inlet conduit 22 and the upper space 13. A salt- bearing liquid is supplied to the second plate interspaces 6 of the first heat exchanger stages 2a via the feed conduit 30. The supplied steam is condensed to a liquid that is discharged from the first heat exchanger stages 2a via the port channels 34 and the discharge conduit 35.
  • All liquid, which is discharged via the discharge conduit from all heat exchanger stages 2a-2e has a high purity with a very low salt content.
  • the supplied liquid is partly evaporated and dis ⁇ charged in the lower space 14. From the lower space 14, the steam may pass to the upper space 13 via the first liquid separator 16a.
  • Liquid droplets of the salt-bearing liquid, which has not been evapo ⁇ rated and which in the embodiment disclosed contains salt, will then be catched and conveyed back as excess liquid to a bottom space 37 in a lower part of lower space 14.
  • This bottom space 37 is thus in the embodiment disclosed adapted to contain a salt-bearing ex- cess liquid, so called brine.
  • brine salt-bearing ex- cess liquid
  • the steam that passes through the first liquid separator 16a is sup ⁇ plied to the upper space 13 and the first plate interspaces 5 in the second heat exchanger stage 2b for evaporation of the liquid sup ⁇ plied to the second plate interspaces 6 in the second heat ex ⁇ changer stages 2b via the feed conduit 30.
  • the steam that is con- densed in the first plate interspaces 5 in the second heat exchanger stages 2b is discharged via the port channels 34 in the plate pack ⁇ ages 3 and via the discharge conduit 35.
  • the supplied liquid is evaporated and discharged in the lower space 14. From the lower space 14, the steam may pass to the upper space 13 of the third heat exchanger stages 2c via the second liquid separator 16b. Liq ⁇ uid, which in the embodiment disclosed contains salt, will then be catched and conveyed back as excess liquid to the bottom space 37.
  • the steam that passes through the second liquid separator 16b is supplied to the upper space 13 and the first plate interspaces 5 in the third heat exchanger stages 2c for evaporation of the liquid supplied to the second plate interspaces 6 in the third heat ex ⁇ changer stages 2c via the feed conduit 30.
  • the steam that is con ⁇ densed in the first plate interspaces 5 in the second heat exchanger stages 2c is discharged via the port channels 34 in the plate pack- ages 3 and via the discharge conduit 35.
  • the supplied liquid is evaporated and discharged in the lower space 14. From the lower space 14, the steam may pass through the upper space 13 of the fourth heat exchanger stages 2d via the third liquid separator 16c. Liquid, which in the embodiment disclosed contains salt, will then be catched and conveyed back as excess liquid to the bottom space 37.
  • the steam that passes through the third liquid separator 16c is supplied to the upper space 13 and the first plate interspaces 5 in the fourth heat exchanger stages 2d for evaporation of the liquid supplied to the second plate interspaces 6 in the fourth heat ex ⁇ changer stages 2e via the feed conduit 30.
  • the steam, which is condensed in the first plate interspaces 5 in the fourth heat ex ⁇ changer stages 2d, is discharged via the port channels 34 in the plate packages 3 and via the discharge conduit 35.
  • the supplied liquid is evaporated and discharged in the lower space 14. From the lower space 14, the steam may pass to the upper space 13 of the fifth heat exchanger stages 2e via the fourth liquid separator 16d. Liquid, which in the embodiment disclosed contains salt, will then be catched and conveyed back as excess liquid to the bottom space 37.
  • the steam that passes through the fourth liquid separator 16d is supplied to the upper space 13 of the fifth heat exchanger stages 2e. From this upper space a part of the steam is sucked to the thermo compressor 20 via the conduit 23 whereas the rest of the steam is supplied to the first plate interspaces 5 in the fifth heat ex ⁇ changer stages 2e.
  • the steam, which is condensed in the first plate interspaces 5 in the fifth heat exchanger stages 2e, is discharged via the discharge conduit 35.
  • the fifth heat ex ⁇ changer stages 2e which are adapted to perform the final condens ⁇ ing, may comprise heat exchanger stages of another kind than the preceding stages 2a-2d, for instance plate packages with plates of another type or completely different types of heat exchangers, for instance tube condensers.
  • One or several of the heat exchanger stages 2a-2d may also com ⁇ prise a preheater 40 for preheating the salt-bearing liquid which is to be supplied to the first plate interspaces 5 via the feed conduit 30.
  • a preheater 40 is schematically disclosed in Fig. 1 for pre ⁇ heating of the salt-bearing liquid by means of the steam supplied to the heat exchanger stages 2c.
  • the discharge conduit 35 may also be connected to a flash tank 39 downstream at least some of the heat exchanger stages, in the em ⁇ bodiment disclosed downstream the heat exchanger stages 2b, 2c and 2d.
  • the condensate from the respective plate package 3 is conveyed via the discharge conduit 35 to the flash tank 39 where a lower pressure than in the respective plate package 3 prevails. Due to the pressure decrease, a part of the condensate will be evapo ⁇ rated through flashing.
  • the steam formed is returned to the process in the next row 8 with heat exchanger stages via suitable conduits (not disclosed).
  • the remaining condensate is discharged from the tanks 39 via the conduit 40.
  • the casing 10 has, seen in the cross-section shown in Fig. 4, a rec ⁇ tangular shape.
  • the opposite upper and lower walls 51 and 52 are plane, substantially horizontal and substantially parallel.
  • the oppo ⁇ site side walls 53 and 54 are plane, substantially vertical and sub- stantially parallel.
  • the plant is also constructed of a number of modules 61-63 for an easy premanufacturing at a factory and an easy mounting at the site where the plant is to be mounted.
  • Each module 61-63 comprises one of the plate packages 3 and a part of the casing 10.
  • Each module 61-63 is adapted to be connected with respect to the flow to at least one of a preceding and a successive module in the same process line 1.
  • each module 61- 63 is adapted to be connected with respect to the flow to at least one adjacent module 61-63 in the same row 8.
  • the steam flow may pass from one heat exchanger stage to the next. There is however no partition between adjacent plate package as in each row 8, which means that the steam flow in one process line 1 may be spread over to adjacent process lines 1 in the successive row 8.
  • Each module 61-63 may be designed as either an inner module 61 , which is adapted to be provided between two adjacent modules in the same row 8, or as an outer module 62-63, which is adapted to be provided adjacent to merely one adjacent module 61 , 63 and 61 , 62, respectively, in the same row 8.
  • An inner module 61 is disclosed in Fig. 6.
  • Each outer module 62, 63 may be designed as a left mod ⁇ ule 62 or a right module 63.
  • a left module 62 is disclosed in Fig. 5 and a right module 63 is disclosed in Fig. 7.
  • each module 61-63 is adapted to be connected mechanically to at least one adjacent module 61-63 in the same row 8 and to at least one of a preceding and a successive module 61-63 in the same process line 8.
  • the mechanical connection may be achieved by connecting the modules 61-63 to each other by means of weld joints, i.e. the casing 10 of each module 61-63 is welded to the casing 10 of an adjacent module 61-63.
  • each inner module 61 may com ⁇ prise vertical longitudinal flanges 70 adapted to abut corresponding vertical longitudinal flanges 70 of an adjacent module 61-63.
  • each module 61-63 may then be connected to each other through suit- able connections, for instance screw connections.
  • the outer mod ⁇ ules 62-63 differ from the inner modules 61 since they merely com ⁇ prise flanges 70 on one side.
  • each module 61-63 may comprise vertical transversal flanges 71 adapted to abut corre ⁇ sponding vertical transversal flanges 71 of an adjacent module 61- 63 in the same process line 1. These flanges 71 are indicated in Fig. 8.
  • the first and last module 61-63 in each process line may be closed by means of a cover 73 of a suitable design.
  • gaskets 74 may be provided, see Figs. 5 and 7.
  • the flash tanks 39 have in the embodiment disclosed been located outside the casing 10, but it is also possible to arrange them inside the casing 10.
  • Figs. 9 and 10 disclose schematically a heat exchanger plant ac ⁇ cording to a second embodiment. Elements having substantially the same function have been given the same reference signs in the two embodiments.
  • the process lines 1 with successive heat exchanger stages 2a-2g extend not in a longitudinal horizontal direction but in a longitudinal vertical direc ⁇ tion.
  • the rows 8 with plate packages 3 extend as in the first em ⁇ bodiment horizontally and transversally to the longitudinal process lines 1.
  • the width of the last row 8 with the last heat exchanger stages 2g, which are adapted for the final condensation, is in this embodiment larger than the width of the preceding rows 8 with re ⁇ spect to the heat exchanger stages 2a-2f.
  • the heat exchanger stages 2g that are disclosed in Figs.
  • the second embodiment is suitable for very large plants and comprises as appears three thermo com ⁇ pressors 20 with three feed conduits 22.
  • the casing 10 is in this embodiment approximately cubic, which means that the outer sur- face area of the casing 10 is minimized.
  • the compact construction also results in very short distances for piping.
  • the required ground area is very small in comparison with the ground area required for a plant with horizontally lying process lines 1.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L’invention a trait à un échangeur de chaleur pour distillation comprenant au moins deux chaînes de travail parallèles (1), elles-mêmes comprenant au moins deux étages échangeurs de chaleur successifs (2a, 2b) comprenant chacun un ensemble de plaques d’échangeur de chaleur à plaques disposées de telle sorte que la première plaque forme des intervalles pour la condensation et la deuxième plaque des intervalles pour l’évaporation. Les étages échangeurs de chaleur sont alignés (8) chacun avec les étages échangeurs de chaleur placés l’un après l’autre et transversalement aux chaînes de travail. Chaque étage est conçu pour la condensation de vapeur et l’évaporation d’un liquide, la vapeur étant générée dans les intervalles de la première plaque et le liquide dans les intervalles de la deuxième plaque. La vapeur générée est condensée en un liquide qui est évaporé et transmis aux intervalles de la première plaque de l’étage échangeur de chaleur suivant pour évaporation d’un liquide transmis aux intervalles de la seconde plaque dudit étage échangeur de chaleur suivant. L’ensemble échangeur de chaleur comprend par ailleurs une enveloppe fermée (10) entourant un espace intérieur (11) où se trouvent les chaînes de travail. Vue en coupe transversale transversalement aux chaînes de travail, l’enveloppe a une forme rectangulaire.
PCT/SE2005/001658 2004-11-17 2005-11-03 Ensemble echangeur de chaleur a evaporation WO2006054936A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
JP2007541135A JP4762997B2 (ja) 2004-11-17 2005-11-03 蒸発用熱交換器プラント
KR1020077011093A KR101225303B1 (ko) 2004-11-17 2005-11-03 증발용 열교환기 플랜트
DE112005002537T DE112005002537T5 (de) 2004-11-17 2005-11-03 Wärmetauscheranlage zum Verdampfen

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE0402809A SE527868C8 (sv) 2004-11-17 2004-11-17 Värmeväxlaranläggning för indunstning
SE0402809-8 2004-11-17

Publications (1)

Publication Number Publication Date
WO2006054936A1 true WO2006054936A1 (fr) 2006-05-26

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SE2005/001658 WO2006054936A1 (fr) 2004-11-17 2005-11-03 Ensemble echangeur de chaleur a evaporation

Country Status (6)

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JP (1) JP4762997B2 (fr)
KR (1) KR101225303B1 (fr)
CN (1) CN100557365C (fr)
DE (1) DE112005002537T5 (fr)
SE (1) SE527868C8 (fr)
WO (1) WO2006054936A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3184950A1 (fr) 2015-12-22 2017-06-28 Alfa Laval Corporate AB Installation de distillation avec des échangeurs de chaleurs à plaques amovibles

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103180022B (zh) * 2010-07-21 2016-02-17 阿奎巴克技术公司 具有用于薄膜蒸发的涂抹器和用于移除沉积物的刮除器的蒸馏器
DE102016107984A1 (de) * 2016-04-29 2017-11-02 Wärtsilä Serck Como Gmbh Meerwasserentsalzungsvorrichtung zum Entsalzen von Meerwasser

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US4497689A (en) * 1980-08-22 1985-02-05 Energiagazdalkodasi Intezet Heat engineering apparatus for carrying out thermodynamical processes comprising a pair of mutually opposite phase transitions of a work medium
US4511436A (en) * 1982-05-24 1985-04-16 D.V.T. Buro Fur Anwendung Deutscher Verfahrenstechnik H. Morsy Apparatus for the desalination of sea water
US4514260A (en) * 1982-05-24 1985-04-30 D.V.T. Buro Fur Anwendung Deutscher Verfahrenstechnik H. Morsy Apparatus for the desalination of sea water

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JPS5236577A (en) * 1975-09-17 1977-03-19 Hisaka Works Ltd Plate type evaporation equipment
DE4431546A1 (de) * 1994-09-05 1996-03-07 Jakob Dr Ing Hois Verfahren und Vorrichtung zum Entsalzen von Meerwasser
US5744009A (en) * 1995-07-07 1998-04-28 The M. W. Kellogg Company Method and apparatus for recovering condensables in vapor from a urea vacuum evaporator
JPH09108653A (ja) * 1995-10-16 1997-04-28 Nkk Corp 海水淡水化装置
FI106296B (fi) 1998-11-09 2001-01-15 Amsco Europ Inc Suomen Sivulii Menetelmä ja laite haihdutettavan veden käsittelemiseksi
NO314619B1 (no) * 2001-12-20 2003-04-22 Gnd Water As Anordning og framgangsmåte for destillasjon av for eksempel ferskvann fra saltvann
JP3889326B2 (ja) * 2002-07-09 2007-03-07 株式会社ササクラ 高純度純水の蒸発式製造方法及びその装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4497689A (en) * 1980-08-22 1985-02-05 Energiagazdalkodasi Intezet Heat engineering apparatus for carrying out thermodynamical processes comprising a pair of mutually opposite phase transitions of a work medium
US4511436A (en) * 1982-05-24 1985-04-16 D.V.T. Buro Fur Anwendung Deutscher Verfahrenstechnik H. Morsy Apparatus for the desalination of sea water
US4514260A (en) * 1982-05-24 1985-04-30 D.V.T. Buro Fur Anwendung Deutscher Verfahrenstechnik H. Morsy Apparatus for the desalination of sea water

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3184950A1 (fr) 2015-12-22 2017-06-28 Alfa Laval Corporate AB Installation de distillation avec des échangeurs de chaleurs à plaques amovibles
WO2017108380A1 (fr) 2015-12-22 2017-06-29 Alfa Laval Corporate Ab Installation de distillation dotée d'échangeurs de chaleurs amovibles à plaques
US10634433B2 (en) 2015-12-22 2020-04-28 Alfa Laval Corporate Ab Distillation plant

Also Published As

Publication number Publication date
JP4762997B2 (ja) 2011-08-31
JP2008520410A (ja) 2008-06-19
DE112005002537T5 (de) 2007-10-18
SE0402809D0 (sv) 2004-11-17
CN100557365C (zh) 2009-11-04
CN101061070A (zh) 2007-10-24
KR20070094733A (ko) 2007-09-21
SE527868C2 (sv) 2006-06-27
SE527868C8 (sv) 2006-09-26
SE0402809L (sv) 2006-05-18
KR101225303B1 (ko) 2013-01-22

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