EP0042613A2 - Vorrichtung und Verfahren zur Wärmeübertragung - Google Patents

Vorrichtung und Verfahren zur Wärmeübertragung Download PDF

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Publication number
EP0042613A2
EP0042613A2 EP81104809A EP81104809A EP0042613A2 EP 0042613 A2 EP0042613 A2 EP 0042613A2 EP 81104809 A EP81104809 A EP 81104809A EP 81104809 A EP81104809 A EP 81104809A EP 0042613 A2 EP0042613 A2 EP 0042613A2
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EP
European Patent Office
Prior art keywords
fluid flow
heat transfer
passage
layer
boundary
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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Withdrawn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
EP81104809A
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English (en)
French (fr)
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EP0042613A3 (de
Inventor
Richard Adolf Holl
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Individual
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Individual
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Publication date
Application filed by Individual filed Critical Individual
Publication of EP0042613A2 publication Critical patent/EP0042613A2/de
Publication of EP0042613A3 publication Critical patent/EP0042613A3/de
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/003—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by using permeable mass, perforated or porous materials
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F15—FLUID-PRESSURE ACTUATORS; HYDRAULICS OR PNEUMATICS IN GENERAL
    • F15D—FLUID DYNAMICS, i.e. METHODS OR MEANS FOR INFLUENCING THE FLOW OF GASES OR LIQUIDS
    • F15D1/00—Influencing flow of fluids
    • F15D1/02—Influencing flow of fluids in pipes or conduits
    • F15D1/06—Influencing flow of fluids in pipes or conduits by influencing the boundary layer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/02—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by influencing fluid boundary

Definitions

  • This invention is concerned with new apparatus for heat transfer and with a new process for heat transfer, as employed in such apparatus.
  • More specific objects are to provide new heat transfer apparatus and processes in which the heat transfer is increased with avoidance of turbulence in the presence of laminar wake-interference flow.
  • a'process of heat transfer including establishing in a fluid flow passage, comprising at least one heat transfer surface, a non-turbulent fluid flow consisting of a non-turbulent boundary-layer immediately adjacent each passage surface, and a non-turbulent core-layer interfacing with the resultant boundary I layer or layers;
  • apparatus for heat transfer between two fluids comprising:
  • FJGURE 16 is a graph to show the relative performance ranking of heat exchanger surfaces of the invention as compared with surfaces from prior art tubulus and plate heat exchangers.
  • the simple convection-type heat transfer apparatus 10 of Figure 1 is intended for the transfer of heat carried by a liquid fluid, such as oil or water, to the gaseous ambient atmosphere; such apparatus is commonly used for example as an oil or water cooler.
  • the apparatus consists of a hollow body 12 providing a parallel-walled flow passage containing a fluid flow interrupter structure to be described below.
  • the liquid fluid is fed into the apparatus via an inlet pipe 14 and discharged therefrom via an outlet pipe 16.
  • the exterior of the body may be provided in known manner with spaced parallel fins 18 for more efficient heat transfer to the ambient air.
  • the interior of the body 12 provides a non-turbulent I fluid flow passage comprising two spaced parallel facing heat- transferring wall surfaces 20 (Fig. 3) provided by the walls 22, between which wall surfaces the liquid fluid flows.
  • the passage is completed by two side walls 24 and the enclosure is completed by two transition pieces 26 which progressively change the circular cross-section of the pipes 14 and 16 to the rectangular cross-section of the flow passage.
  • a fluid flow interrupter structure disposed within the passage consists of a plurality of densely packed spheres 28 of a material that will be unaffected by the fluid, such as metal, glass or porcelain, the packing being such that the spheres contact one another.
  • the diameter of the spheres is such that they are each in point contact with the opposed heat transferring wall surfaces 20.
  • the spheres are touching one another they may be joined to each other at their points of mutual contact to form a unitary structure. In other embodiments they may be packed at a lower density at which they are spaced from one another, for example, by an interposed apertured plate having the spheres disposed in the apertures thereof. Other variations will be described below.
  • boundary-layers 30 immediately adjacent the surfaces 20, which act to insulate the wall surfaces from the main body of the fluid flowing in a core layer 32 between and interfacing with the boundary layers 30, and which therefore reduce the heat transfer between the surfaces 20 and the core layer 32.
  • Corresponding boundary layers 30 are also present on the surfaces of the spheres 28.
  • an unobstructed boundary layer increases progressively in thickness in the direction of fluid flow, which will increase its insulating effect.
  • proposals have been made hitherto to disrupt the boundary layers by roughening or ridging the surface over which they flow, but such proposals have the effect of also increasing to a disproportionately greater extent the pumping power required.
  • the boundary layers 30' are interrupted in a "spot-wise" manner at spaced spots 34 by means of the fluid flow interrupter structure interposed between the heat transfer surfaces, while maintaining a non-turbulent fluid flow in the core 32.
  • the heat transfer surfaces 20 not roughened, etc., but on the contrary they are made as smooth as is economically possible, to the extent that in many embodiments the surfaces 20 will be polished to the desired degree of smoothness.
  • the disruption of the boundary layers 30 at the multitude of spaced spots 34 ensures that they stay thin, while the manner of their disruption ensures that turbulence is avoided that would cause unduly high friction drag.
  • the polishing of all surfaces including those of the spheres also assists in the desired minimizing of the friction drag.
  • the invention may be regarded as comprising a fluid flow system for improving the ratio of convective heat transfer to friction power per unit heat transfer surface area by sandwiching specially shaped interrupting and mixing-structures of low friction drag immediately adjacent a smooth heat transfer surface using hydraulic radii that guarantee total laminar flow.
  • the mixing structures contain.cellular voids, which are connected with one another, in each of which the fluid rotates spiral-like as a single laminar eddy. These eddies are very efficient means of mixing laminar streams, and preferably are obtained by coinciding a wake eddy downstream of an interruption point with an advance eddy upstream of a subsequent interruption point so as to produce wake-interference flow, which provides the highest efficiency.
  • boundary layers 30 on the curved surfaces of the mixing-structures are fairly thick, whereas the boundary layers of the flat heat transfer surfaces, situated opposite the mixing-structure surfaces, remain very thin on average because they are reduced regularly and spotwise at the large number of contact points between the surface of the mixing-structure and the heat transfer surface, and are in addition exposed to the highest local velocities which occure predominantly very close to the flat heat transfer surface. This allows rapid heat flow through the heat transfer surface.
  • the general direction of flow of the fluid is indicated by arrows 36%' and the flow interrupter structure causes the production of laminar flow eddies 38 of shape and rotational frequency that depend upon the geometry of the structure.
  • Wake-eddies will be produced around the spots of interruption downstream of the flow, while advance eddies will be produced upstream of the flow. If the spacing of the interruption spots 34 is made such that the advance- and wake-eddies of immediately successive spots coincide, then wake-interference flow is obtained whereby, in the absence of turbulent friction-drag, very efficient non-turbulent mixing is obtained between the interrupted boundary-layers 30 and the adjacent core layer 32.
  • a turbulent flow which is to be avoided, may be distinguished from an eddy in that the former is irregular and there is no observable pattern as with an eddy. Eddies and swirls therefore do not constitute turbulence. Again a laminar eddy or vortex is confined by solid boundaries or by laminar fluid flows, while a turbulent eddy or vortex will be surrounded by other eddies and vortices which interact with the turbulent eddy or vortex.
  • the conditions for maintenance of laminar flow with a particular structure can be observed for example by providing suitable windows in an experimental structure and adding visible fluids to the fluid flow if required.
  • the diameter of the spheres is equal to the spacing between the surfaces 20 and the spots of interruption 34 by the spheres 2,8 are their points of contact with the walls.
  • the connections provided by these contact points gives high heat transfer at the points and also serve to support the walls against external pressures greater than the internal pressure. These effects can be increased even more by making the connections solid, e.g. by brazing or otherwise fixing the structure to the surfaces at the contact points.
  • the portion of each spherical surface around the actual point of contact and submerged in the boundary layer will also be effective in this interrupting function.
  • the interrupter structure may therefore be suspended within the enclosure and not actually touch the walls, or touch the walls at fewer points than there are interruption points.
  • Figure 4a shows in plan view the profile of spherical interrupter structure elements of the structure of Figures 1 to 3, taken in the direction of flow of the fluid in the passage; the profile is of course a circle.
  • Other profiles can be used and should be such as to present a smoothly contoured surface to the fluid flow, so as to reduce friction losses to a minimum and also to ensure the maintenance of laminar flow.
  • Figure 4b shows for example an ellipsoidal profile
  • Figure 4c shows an egg-shaped profile
  • Figure 4d shows a drop-shaped profile; in the latter two profiles the face of largest radius faces upstream.
  • Figure 5 illustrates the statement above that the elements of the interrupter structure do not necessarily contact the heat exchange surface and a chain-dotted profile 40 is illustrated in which this is not the case, the highest point of the profile being spaced a minimum distance d from the surface 20; in the case of a convex curvilinear surface spaced from a flat surface 20 this distance d should not be more than about 10% of the effective diameter of the curved surface.
  • a pyrimidal surface 42 is also illustrated in broken lines terminating at the contact point 34 and this is unsatisfactory for use in flow interrupting structures of the invention, principally because there is a drastically reduced opportunity for the establishment of high fluid flow velocities at the boundary layer, with consequent less disrupting of the layer and much less effective heat exchange at the surface;
  • the preferred form of the profile may be characterised as being convex curvilinear and this is arranged to provide the maximum possible velocity as close as possible to the flat and smooth heat transfer surface while main- faining laminar flow.
  • the fluid is very viscous, such as a viscous oil that is to be heated.
  • the spacing apart of the parallel walls 20 of the passage can be increased considerably without the establishment of turbulent flow, but such a fluid is usually of low thermal conductivity and a thermal boundary layer will be established immediately adjacent to the heat transfer surface that is much thinner than the respective boundary layer.
  • the interposed structure must be arranged to interrupt this thinner thermal boundary-layer irrespective of the thickness of the boundary-layer.
  • the principal factor in the determination of the thickness of the thermal boundary layer is the Prandtl number, which is high when the viscosity is high and the thermal conductivity is low.
  • Figure 6 illustrates another form that may be taken by the interrupter structure consisting of a sheet 44 in which alternate convex and concave profiles 28 and 46 respectively have been formed, so that the convex profile 28 on one side forms the concave profile 46 on the other side.
  • a "convex- concave” sheet can be manufactured inexpensively by roll-forming from a thin metal sheet to a thickness such that it can just be slid into the space between the two walls 22. It will be noted that the convexities on one side in successive rows are staggered transversely of the direction of flow so that there are no channels permitting straight-through flow without interruption of the respective adjacent boundary layer 30.
  • Figure 7a illustrates the application of the interrupter structure 0 $ Figure 6 to a two-path, two-fluid heat exchanger in which the heat exchange takes place through the material of the sheet 40.
  • inlet 14 and outlet 16 are for the path on one side of the sheet
  • inlet 48 and outlet 50 are for the path on the other side of the sheet.
  • a number of parallel passages will be formed by a stack of spaced sheets 22, each passage containing a sheet 44, the heat exchange between adjoining paths taking place through the walls 22 as well as the sheet 44.
  • Figure 7b serves to illustrate the application of the interrupter structure of Figures 1 to 3 to such a two-path, two-fluid heat exchanger, the heat exchange taking place through the wall 22 between the two paths.
  • the invention has been described above principally in connection with heat exchange apparatus of the kind known generally as of plate type, since the heat exchange takes place through a plate.
  • the invention is also applicable to heat exchangers of the equally well known shell and tube type.
  • the flow passage is a tube of square cross-section having two pairs of opposed parallel wall surfaces 20 and the interrupter structure is a row of closely packed spheres 28 touching both pairs of surfaces at spaced interrupter spots.
  • Such a structure will exhibit improved heat exchange through all four of the tube walls 22.
  • the flow passage is a tube 22 of circular cross-section and the interrupter structure spheres must be of smaller diameter than its internal diameter so as not to block the passaged
  • the minimum diameter for the spheres is about 75% of the tube internal diameter, more preferably from about 90% to about 95% thereof. In practice the difference should be as small as possible consistent with obtaining the necessary flow capacity and ensuring that the flow path.cannot be blocked by retained solid material in the fluid.
  • Figure 9a shows a preferred configuration in which the spheres are distributed helically around the longitudinal axis 52, while Figure 9b shows a less satisfactory structure in which all of the spheres are to the same side of the axis.
  • the structures of Figures 8, 9a and 9b can be used as the basis for a heat exchanger of the so-called bayonet type.
  • Figures 10 and 11 illustrate a single tube-in-shell' exchanger in which one fluid path with inlet and outlet 14 and 16 respectively is formed by the annular space between an outer shell 54 and the inner circular cross-section tube 22, while the other fluid path with inlet 48 and outlet 50 is of course formed by the tube 22.
  • the annular shell space is of radial dimension just sufficient to receive the spheres 28 and the spaces between the spheres and the inner wall of the outer shell are completely filled with a suitable-cementitious material 56 to prevent fluid flow therethrough that would be wasted.
  • the interrupter system employed within the tube 22 can be that shown in Figures 9a or 9b, but preferably is as shown in Figures 10 and 11 in which rows of smaller spheres are used to provide the necessary flow capacity with a sufficiently large number of interrupting points 34 both along the length of the tube and also around its circumference.
  • a cementitious or other suitable material 58 such as concrete or ceramic cement.
  • Figures 12 and 13 illustrate a multiple tube in shell heat exchanger in which a plurality of parallel tubes 22 are disposed within a single outer shell 54.
  • Each tube 22 is surrounded by spheres 28 in rows, circles or helixes thereof with some of the spheres contacting two adjacent tubes, so that it disrupts the boundary layers of both tubes.
  • the tubes 22 thus take the place of the cement 58 of the structure of Figures 10 and 11 and only the cement 56 is required between the outermost spheres and the shell 54.
  • the interrupter structure within the tubes 22 can be of the form illustrated by Figures 9a or 9b.
  • Figures 14 and 15 illustrate a particular form of tube-in-shell exchanger in which the shell-side interrupter structure is provided by a plurality of outer rods 60 of hemispherical cross-section and a plurality of inner rods 62.of circular cross-section that are assembled into the form of stackable grids of square shape in end elevation.
  • the grids form a plurality of parallel passages 64 of square cross-section through each of which a respective tube 22 of circular cross-section is threaded with the convex curvilinear faces of the rods 60 and 62 in contact with the tubes external walls to provide the necessary interrupter structure; these passages 64 thus form the shell side flow path and the unwanted space is filled by the cementitious material.
  • the passages 64 can instead be of some polygonal cross-section other than square, i.e. with less or more than four sides, for example triangular or hexagonal, a space-filling configuration being chosen to ensure that all of the available space is utilised.
  • the invention can also be applied in the apparatus of Figure 1 to the air fluid flow paths constituted by the spaces between the fins 18, these spaces being provided with any of the flow interrupter structures of the invention, such as those specifically illustrated.
  • the interposed structure can be made to increase the efficiency of the heat transfer between the fins and the air over the fins. Such an arrangement can be made to be more efficient than the "split fin" structures proposed hitherto in which the fins are split and staggered in order to disrupt the boundary layers.
  • Figure 16 is a plot of the ranking of surfaces in accordance with this method, comparing surfaces of the invention with a surface provided by a tube of 1.2 cm diameter and a plate heat exchanger of 0.5 cm plate pitch.
  • the vertical plot indicates the number of heat transfer units (NTU) per unit volume of the heat exchanger core (V), while the horizontal plot indicates the pumping power (E) required to move the fluid through the core per unit volume of the heat exchanger core (V).
  • NTU heat transfer units
  • E pumping power
  • An improvement in heat exchanger performance is indicated by the line being higher on the vertical plot, and the increase in performance can be measured along any vertical line.
  • the test fluid was water and the lowest chain-dotted line A is for heat transfer in a tube of 1.2 cm diameter, using data obtained from the above-mentioned paper of Soland, Mack and Rohsenow.
  • the broken line B is for a "APV” plate heat exchanger of 0.5 cm plate pitch, using data obtained from the "AP V Heat Transfer Handbook, 2nd Edition, published by APV Inc. of T onawanda, New York, U.S.A.” It will be seen that line B represents an improvement of 28% in performance over line A.
  • the lower solid line C plots the performance of a heat exchanger of the invention employing closely packed spheres of 6.35 mm diameter between plates of that spacing, while the higher solid line D plots the maximum performance so far obtained with a heat exchanger of the invention. It will be seen that line C represents an improvement of respectively 100% and 52% over lines A and B, while line D represents an improvement of respectively 415% and 290%.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Fluid Mechanics (AREA)
  • Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
EP81104809A 1980-06-24 1981-06-22 Vorrichtung und Verfahren zur Wärmeübertragung Withdrawn EP0042613A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US16241480A 1980-06-24 1980-06-24
US162414 1993-12-03

Publications (2)

Publication Number Publication Date
EP0042613A2 true EP0042613A2 (de) 1981-12-30
EP0042613A3 EP0042613A3 (de) 1982-08-11

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JP (1) JPS5767796A (de)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0065679A1 (de) * 1981-05-21 1982-12-01 Hoechst Aktiengesellschaft Flächenhaftes flexibles Wärmeaustauscherelement
EP0124584A1 (de) * 1982-11-01 1984-11-14 Vapor Corp Verbesserungen an oder betreffend fluidabehandlungsvorrichtungen.
EP0160662A1 (de) * 1983-10-05 1985-11-13 Vapor Corp Wärmetauscher mit mantel und rohrbündel und verfahren dafür.
US4670103A (en) * 1982-11-01 1987-06-02 Holl Richard A Fluid handling apparatus
WO1988006707A1 (en) * 1987-02-24 1988-09-07 Metsafe Aktiebolag Heat exchanger
WO1988006706A1 (en) * 1987-02-24 1988-09-07 Metsafe Aktiebolag A heat exchanger
US4784218A (en) * 1982-11-01 1988-11-15 Holl Richard A Fluid handling apparatus
EP0679812A4 (de) * 1992-03-31 1995-06-23 Vida Nikolaus Profilierte oberfläche.
WO1996008677A1 (en) * 1994-09-14 1996-03-21 Kvaerner Pulping Ab Process for cleaning superheaters and other heat-transferring surfaces in recovery boilers
WO1996008658A1 (de) * 1994-09-16 1996-03-21 Forschungszentrum Jülich GmbH Vorrichtung zur brechung von strömungswirbeln an einer turbulent umströmten fläche
WO2001087477A1 (de) * 2000-05-17 2001-11-22 Basf Aktiengesellschaft Längsstromreaktor mit einem kontaktrohrbündel
EP2566656A4 (de) * 2010-05-04 2017-05-17 9343598 Canada Inc. Verfahren zur herstellung einer wärmetauscherkomponente mithilfe von drahtmaschensieben
CN112728990A (zh) * 2020-12-30 2021-04-30 佛山科学技术学院 一种内插球体换热管
CN113899237A (zh) * 2021-11-10 2022-01-07 哈尔滨工程大学 一种采用中空结构球床的强化换热管
CN113899236A (zh) * 2021-11-10 2022-01-07 哈尔滨工程大学 一种球形颗粒填充的微肋换热管

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE872212C (de) * 1943-07-01 1953-03-30 Brown Waermeaustauscher mit Innenberippung der Stroemungskanaele, insbesondere fuer den Waermeaustausch zwischen zwei gasfoermigen Mitteln
DE895459C (de) * 1951-12-23 1953-11-02 Metallgesellschaft Ag Laengsrohr-Waermeaustauscher
US2834582A (en) * 1953-06-24 1958-05-13 Kablitz Richard Plate heat exchanger
US3372743A (en) * 1967-01-25 1968-03-12 Pall Corp Heat exchanger
GB1163953A (en) * 1965-12-28 1969-09-10 Air Preheater Method of increasing the Rate of Heat Transfer in Heat Exchangers
GB1257041A (de) * 1968-03-27 1971-12-15
GB1314097A (en) * 1970-02-11 1973-04-18 Raytheon Co Heat exchange system
US3732919A (en) * 1970-07-01 1973-05-15 J Wilson Heat exchanger
FR2249704A1 (en) * 1973-11-05 1975-05-30 Klosse Jan Fluid component mixing system - for components buffered by air cushions
US3921711A (en) * 1972-05-30 1975-11-25 American Standard Inc Turbulator
US3921712A (en) * 1970-03-02 1975-11-25 American Standard Inc Heat exchanger structure for a compact boiler and the like
FR2362354A1 (fr) * 1976-08-18 1978-03-17 Pronko Vladimir Echangeur de chaleur a treillis

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE872212C (de) * 1943-07-01 1953-03-30 Brown Waermeaustauscher mit Innenberippung der Stroemungskanaele, insbesondere fuer den Waermeaustausch zwischen zwei gasfoermigen Mitteln
DE895459C (de) * 1951-12-23 1953-11-02 Metallgesellschaft Ag Laengsrohr-Waermeaustauscher
US2834582A (en) * 1953-06-24 1958-05-13 Kablitz Richard Plate heat exchanger
GB1163953A (en) * 1965-12-28 1969-09-10 Air Preheater Method of increasing the Rate of Heat Transfer in Heat Exchangers
US3372743A (en) * 1967-01-25 1968-03-12 Pall Corp Heat exchanger
GB1257041A (de) * 1968-03-27 1971-12-15
GB1314097A (en) * 1970-02-11 1973-04-18 Raytheon Co Heat exchange system
US3921712A (en) * 1970-03-02 1975-11-25 American Standard Inc Heat exchanger structure for a compact boiler and the like
US3732919A (en) * 1970-07-01 1973-05-15 J Wilson Heat exchanger
US3921711A (en) * 1972-05-30 1975-11-25 American Standard Inc Turbulator
FR2249704A1 (en) * 1973-11-05 1975-05-30 Klosse Jan Fluid component mixing system - for components buffered by air cushions
FR2362354A1 (fr) * 1976-08-18 1978-03-17 Pronko Vladimir Echangeur de chaleur a treillis

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0065679A1 (de) * 1981-05-21 1982-12-01 Hoechst Aktiengesellschaft Flächenhaftes flexibles Wärmeaustauscherelement
US4784218A (en) * 1982-11-01 1988-11-15 Holl Richard A Fluid handling apparatus
EP0124584A1 (de) * 1982-11-01 1984-11-14 Vapor Corp Verbesserungen an oder betreffend fluidabehandlungsvorrichtungen.
EP0124584A4 (de) * 1982-11-01 1985-04-25 Vapor Corp Verbesserungen an oder betreffend fluidabehandlungsvorrichtungen.
US4670103A (en) * 1982-11-01 1987-06-02 Holl Richard A Fluid handling apparatus
EP0160662A1 (de) * 1983-10-05 1985-11-13 Vapor Corp Wärmetauscher mit mantel und rohrbündel und verfahren dafür.
EP0160662A4 (de) * 1983-10-05 1986-02-20 Vapor Corp Wärmetauscher mit mantel und rohrbündel und verfahren dafür.
US4964459A (en) * 1987-02-24 1990-10-23 Hypeco Ab Heat exchanger
WO1988006706A1 (en) * 1987-02-24 1988-09-07 Metsafe Aktiebolag A heat exchanger
US4960167A (en) * 1987-02-24 1990-10-02 Hypeco Ab Heat exchanger
WO1988006707A1 (en) * 1987-02-24 1988-09-07 Metsafe Aktiebolag Heat exchanger
AU625672B2 (en) * 1987-02-24 1992-07-16 Stenhex Aktiebolag Heat exchanger
EP0679812A4 (de) * 1992-03-31 1995-06-23 Vida Nikolaus Profilierte oberfläche.
EP0679812A1 (de) * 1992-03-31 1995-11-02 Vida, Nikolaus Profilierte oberfläche
WO1996008677A1 (en) * 1994-09-14 1996-03-21 Kvaerner Pulping Ab Process for cleaning superheaters and other heat-transferring surfaces in recovery boilers
WO1996008658A1 (de) * 1994-09-16 1996-03-21 Forschungszentrum Jülich GmbH Vorrichtung zur brechung von strömungswirbeln an einer turbulent umströmten fläche
WO2001087477A1 (de) * 2000-05-17 2001-11-22 Basf Aktiengesellschaft Längsstromreaktor mit einem kontaktrohrbündel
EP2566656A4 (de) * 2010-05-04 2017-05-17 9343598 Canada Inc. Verfahren zur herstellung einer wärmetauscherkomponente mithilfe von drahtmaschensieben
CN112728990A (zh) * 2020-12-30 2021-04-30 佛山科学技术学院 一种内插球体换热管
CN113899237A (zh) * 2021-11-10 2022-01-07 哈尔滨工程大学 一种采用中空结构球床的强化换热管
CN113899236A (zh) * 2021-11-10 2022-01-07 哈尔滨工程大学 一种球形颗粒填充的微肋换热管

Also Published As

Publication number Publication date
EP0042613A3 (de) 1982-08-11
JPS5767796A (en) 1982-04-24

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