US3403727A - Crossflow countercurrent heat exchanger with inner and outer-tube sections made up of closely packed coaxially nested layers of helicoidally wound tubes - Google Patents

Crossflow countercurrent heat exchanger with inner and outer-tube sections made up of closely packed coaxially nested layers of helicoidally wound tubes Download PDF

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US3403727A
US3403727A US546383A US54638366A US3403727A US 3403727 A US3403727 A US 3403727A US 546383 A US546383 A US 546383A US 54638366 A US54638366 A US 54638366A US 3403727 A US3403727 A US 3403727A
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tubes
tube
layer
heat exchanger
section
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Becker Rudolf
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Linde GmbH
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Linde GmbH
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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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/024—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of only one medium being helically coiled tubes, the coils having a cylindrical configuration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S165/00—Heat exchange
    • Y10S165/355—Heat exchange having separate flow passage for two distinct fluids
    • Y10S165/40—Shell enclosed conduit assembly
    • Y10S165/401—Shell enclosed conduit assembly including tube support or shell-side flow director
    • Y10S165/405—Extending in a longitudinal direction
    • Y10S165/407—Extending in a longitudinal direction internal casing or tube sleeve

Definitions

  • ABSTRACT OF THE DISCLOSURE having a pair of coaxially nested tube sections separated by a thin sheet-like cylindrical mantle closely surrounding the innertube section and interposed between it and the outer-tube section, the sections each consisting of coaxially nested, closely packed layers of circumferentially spaced parallelwound tubes, all turning in the same sense abo-ut a common axis, the closely packed relationship ensuring that the tubes of each layer are received between a pair of tubes of an adjoining layer so that the centers thereof form an equally lateral triangle whose side is only slightly greater than the diameter of the tubes.
  • the present invention relates to a crossflow countercurrent heat exchangerof the type in which two fiuids are passed generally in countercurrent with respect to one another for heat exchange therebetween via a partition separating the fluids from one another and in which, at each point, the fluids can be considered to move transversely to one another. More particularly, the present invention relates to an improved spiral (or helicoidal) tube heat exchanger structure of this general type adapted to be used effectively in cryogenic processes (eg. for the rectification of air).
  • heat exchangers are characterized by the relative fic-w directions of the tube media and thus can be classified as unidirectional heat exchangers, countercurrent heat exchanges and crossflow heat exchangers.
  • the two fiuids are passed generally parallel to one another in a common direction through the heat exchanger so that, when the exchanger is an elongated unit, both fluids are introduced at one end and removed at the other.
  • the flow of the fluid along opposite sides of the intervening walls is effected generally in opposite directions whereas, in crossflow heat exchangers, the flows of the fluidmedia on oppo-site sides of the walls are intended to be generally transverse to one another.
  • Heat exchangers of the latter type generally comprise a substantially cylindrical shell or housing receiving a nest or bundle of generally coaxial helicoidally or spirally coiled tubes.
  • One of the heat-exchange fluids is fed through the axial extending cylindrical shell or housing from end to end while the other fluid fiows through the tubes in the opposite direction and it can be observed that at any location along the tubes within the heat-exchanger shell, i.e.
  • the fluid passing through the outer chamber is fiowing along the partition surface transversely and approximately perpendicularly to the fluid passing along the inner surface of the tube.
  • the outer fluid flows generally perpendicularly to the fiuid flow through the tube so that the fluid flow overall is both countercurrent (insofar as the axial component of ow is concerned) and perpendicular or crosscurrent.
  • the tubes of each layer or sheet are substantially parallel to one another and spaced apart along a respectivevimaginary cylindrical surface surrounding the axis of the heat exchanger; the tubes of the coils can be considered to be coiled alternately in right hand and in left hand senses about the axis.
  • rods or wires are disposed between the individual layers or tube sheets, these supporting elements having cross-sectional areas corresponding to the requirements for proper physical support of the tubes of the respective coils.
  • the rods or wires have only a limited utility because of the nature of the supporting function; consequently, the supporting wires or tubes cannot augment adequately the turbulence within the heat-exchanger chamber and the heat exchange efficiency-which is related to the degree of turbulence-nor can they be so designed as to obtain an optimal flow velocity. It follows, therefore, that conventional spiral-tube heat exchangers have been severely limited in practical respects by the prior methods ernployed for positioning and supporting the spaced-apart tubes of the helicoidal arrays or layers and were not amenable to improvement with respect to the heat-transfer efficiency, the heat-transfer rate and the uniform channeling of the low-pressure gas stream constituting the outer heat-transfer fluid in cryogenic processes.
  • H is the axial length or height of the crossow countercurrent heat exchanger (i.e., the axial length Iof the outer chamber from end to end rand the axial length of each helicoidal-coil layer);
  • z is the number of mutually parallel and circumferentially spaced helicoidally coiled tubes of each cylindrical tube sheet or layer;
  • w is the number of turns per tube of each layer
  • h is the perpendicular distance between the center lines of the tubes of each layer.
  • LW-Zm' (2) where L is the actual tube length and r is the radius of a turn.
  • the pitch N of each coil is determined by the ratio of the axial height or length H of the heat exchanger to the tube length L:
  • the axial length (or height if the exchanger is vertical) of the crossflow countercurrent heat exchanger and h, the perpendicular distance between the center lines of adjacent tubes of each layer should be substantially constant and are so selected that, on the one hand, the pressure drop through the heat exchanger is not excessively large and, on the other hand, the turbulence in the interests of a high heat-exchange rate is not too small.
  • L should, as 'has already been proposed, be maintained substantially constant over all the layers and it will be evident from Equation 2 supra that such a uniformity of the length L of the tubes can be :attained with an increasing radius r from layer to layer if w is reduced; w is, moreover, determined in accordance with Equation 1 so that the product z-w must remain constant and there must, accordingly, be a corresponding increase in the value of z from layer to layer outwardly of the axis of the heat exchanger.
  • a further object of the present invention is to provide a crossow countercurrent heat exchanger characterized by a relatively high turbulence along the heat-exchange surfaces and partitions.
  • Another object of the present invention is to provide a crossflow-countercurrent heat exchanger of the general character described in which the packing of the coiled tubes and their mutual spacing is not determined by the type of support members hitherto required and 1a general improvement of the structural integrity of the coil layers can be obained a relatively small intertube spacings.
  • a crossow-countercurrent heat exchanger comprises a multiplicity of generally coaxial arrays or layers of helicoidal and circumferentially spaced tubes centered essentially upon respective imaginary coaxial cylinders is provided with a generally lcylindrical thin sheet-metal mantel centered upon the axis of the helicoidal coils intermediate a coil section surrounding at least one tube layer.
  • shell as used hereinafter will be assigned exclusively to the outer cylindrical casing in which the tube bundle is housed and to designate the enclosure forming the outer lluid-ow chamber.
  • the tube bundle is defined las the entire assembly of tubes and it will be understood that the tubes themselves can be of conventional construction; more particularly, it will be understood that the tubes are composed of metals with high thermal conductivity (e.g., copper, stainless steel or other steel alloys).
  • the expression tube sections will be used to identify annular groups of a plurality of cylindrical tube sheets of helically coiled and mutually parallel spaced-apart tubes.
  • the sheets of tubes or layers of each section are coaxial and have center lines lying along helices upon 1a respective imaginary cylindrical surface centered upon the axis of the heat exchanger.
  • the heat exchanger is also provided in the conventional manner common with so-called spiral-tube exchangers, with manifolds or bonnets at the opposi-te ends of the shell and communicating with one or more tube sections or individual layers and adapted to supply the high-pressure fluid to the tube layers at one end and removing the high-duid at the ⁇ other end of the shell.
  • the shell is provided at axially spaced locations which an inlet and an outlet in the usual manner.
  • the present invention provides a crossflow-countercurrent heat exchanger which comprises at least one helicoidal layer of spirally (helicoidally) wound tubes surrounded by a spiral (helicoidal)tube section advantageously comprising a plurality of spiral (helicoidal)- tube layers and a sheet-metal mantle disposed between the inner layer of coil tubes and the outer tube section.
  • This intervening sheet-metal layer serves to strengthen the coils so that the strength and thickness of any support and spacing members can be reduced to a minimum.
  • the inner annular helicoidal tube section in accordance with this invention, comprises only a single layer of the tubes, it has been found to be advantageous to wind around the tubes wires whose thickness alone serves to maintain the desired spacing between the sheetmetal mantle and the tube.
  • the inner annular helicoidal tube section comprises only a single layer of the tubes, it has been found to be advantageous to wind around the tubes wires whose thickness alone serves to maintain the desired spacing between the sheetmetal mantle and the tube.
  • a multiplicity of single-layer sections each separated by intervening sheet-metal mantles or partitions whose thickness may be a fraction of the diameter of the tube and advantageously is equal to the spacing between cylindrical surfaces tangent to the tubes of the adjoining layers which it contacts at their confronting faces, it is found that a dense or close packing of the tubes can be maintained and the closeness of the packing can be greater than any which have been obtainable heretofore with alternately right-handed and left-handed layers of coils.
  • a coil section surrounds an inner section consisting of a plurality of tube layers and this surrounding coil section has a multiplicity of layers of turns coiled spacedly in the same sense and such that the distance between the coils of each layer and between the surrounding coils of the adjacent layers is substantially identical.
  • each tube of an intermediate layer of the surrounding tube section has approximately six closest-neighbor tubes at the vertices of a hexagon (in the maximum spacing) centered upon the axis of the respective central tube in, substantially, a hexagonal close-packed relationship such that the perpendicular distance between each tube and all of its closest neighbors is the same.
  • the resulting arrangement is, in section, a lattice of spacedapart tubes coiled in the same sense about a common axis. It will be seen that the closeness of the packing of the'tubes is further augmented by the staggered arrangement of the tubes of the arrays and in a preferred system, it is possible for adjacent arrays to overlap or interleave as will become apparent hereinafter in practice. Moreover, such close packing fixes the positions of the tubes and eliminates the need, hitherto apparent in earlier spiral-coil arrangements in which the layers were wound in the same sense, for relatively thick support elements or rods. The only limit for the spacing between the layers is, therefore, the desired pressure drop so that the rods or support elements need have a thickness only sufficient to maintain this distance.
  • the tubes of each layer have their centerlines lying upon respective imaginary cylindrical surfaces and a radial spacing between the imaginary cylindrical surfaces of each layer is at most equal to twice the outer radius or the diameter o-f a tube and may be appreciably less until, in the limiting sense, the tubes contact one another.
  • the lattice-like close packing of each tube section does not permit a solution to the problem of the constancy of the length of the tubes in the conventional manner since it is not possible to reduce the number of tubes per layer in dependence upon the radius of the latter. Consequently, it is a feature of the present invention that the number of the tubes per layer of each annular tube section remains constant in spite of the fact that each layer is at a different distance from the center of the heat exchanger.
  • the tube section terminates and a thin-wall sheet-metal mantle is interposed between this outermost tube layer and the next outer layer which, according to this invention, then constitutes the innermost layer of the next tube section.
  • the number of tubes per layer of each of the layers of this next section is also constant but, according to a specic feature of the invention, is increased in ⁇ dependence upon the layer diameter or radius of the coil.
  • the number of turns as has already been demonstrated by the requirement for constancy of the product zw of this latter tube section requires that the pitch of the coils decrease.
  • the average pitch of the successively more outwardly tube section is, however, maintained substantially equal to the average pitch of the more inwardly tube sections.
  • each tube section having at least two layers of similarly coiled tubes in closepacked relationship and surrounding at least two inner layers of similarly wound tubes in close-packed relationship has a number of tubes per l-ayer which is greater than the corresponding number of tubes per layer of the more inwardly set while the number of tubes per layer of each group of close-packed layers is constant.
  • the number of tubes per layer in each case is such that the average length from innermost layer to outermost layer of the tubes does not exceed by more than 10 to 15% the ength of the respective inner tube.
  • the distance a between each tube and its nearest-neighbor tubes should advantageously be between 0.2 and 2 mm.
  • the sheet-metal mantle in accordance with a more specific feature of the present invention, can be composedof one or more relatively wide bands in mutually parallel and axially extending relationship, of a cylindrical member with or without openings to permit the outer fluid to. pass between the tube sections, or of one or more bands helicoidally surrounding the axis of the heat exchanger and wound in the same or opposite sense with respect to the winding of the tubes of the annular section which it surrounds. Between the individual bands, a clearance is maintained to ensure a uniform gas distribution over the interior of the shell and throughout the coil sections. It is, however, desirable under certain circumstances to constitute the mantle as a cylinder with a continuous or nonperforated surface and open axially at its extremities.
  • FIGS. 1 and 2 are diagrammatically cross-sectional iews through the tulbe bundle of a spiral-tube heat exchanger of the crosstiow-countercurrent type in accordance with the principles of this invention
  • FIG. 3 is an elevational view of a heat exchanger embodying the invention with parts broken away and in cross section;
  • FIG. 4 is a fragmentary cross-sectional view from above a portion of the heat exchanger.
  • a crossow-countercurrent heat exchanger in accordance with the principles of the instant invention, suitable for use in cryogenic processes such as air rectification, can include a generally cylindrical outer shell 10 of cast iron (advantageously lined with stainless steel) which surrounds an axis 11 and is provided with an inlet fitting 12 and an outlet fitting 13 for the throughow of a lowpressure gas in axial direction (arrow 14). At opposite extremities of the shell 10, there are provided the usual plates (one of which is shown at 15) to which the tube 'bundle 16 are anchored in the usual manner. Stationary heads or channels 17 and 18 are mounted as bonnets on opposite ends of the shell 10 and form manifolds communicating with the tube bundle 16.
  • the head 17 is provided ⁇ with an inlet fitting 19 for the high-pressure fluid while a further fitting 20 is formed on the head 18 to lead the high-pressure gases away.
  • the tube bundle 16 ⁇ cornprises, in accordance with the principles of the present invention, a plurality of annular tube sections two of which can be seen at 21 and 22, each section being constituted of a plurality of layers 23 of helicoidally wound and mutually parallel but spaced-apart tubes.
  • the tubes may be fabricated from drawn copper tubing. Between the tube sections 21, 22, etc., there are provided ⁇ sheetmetal mantles two of which can be seen in FIG. 3.
  • a sheet-metal mantle can consist of a band of sheet metal helicoidal wound about at least one inner layer of tube coils and surrounded by the outer section 22 thereof. The turns of the mantle 25 can be spaced apart as seen at 25 in FIG. 3 or may abut one another in the manner described earlier.
  • a practical embodiment of the heat exchanger of the irnproved type adapted to be used in an air-rectification installation comprises 705 helicoidal or coil tubes in the spiral-tube bundle with a diameter d of 15 mm. Each tube is spaced from the proximal tubes of the next adjacent layer by a distance a of about 2 mm. while the center-to-center distance between the tubes of each pair of mutually overlying layers is given by (d-
  • the heat exchanger comprises six tube sections of which the innermost can be considered to be illustrated in FIGS. l and 2.
  • a sheetmetal mantle M Between each iive layers of a respective tube section and the layers of the next adjacent tube section there is provided a sheetmetal mantle M.
  • each tube section the length of the tubes from the innermost to the outermost layer is reduced and, accordingly, the pitch of the respective helices or coils and the respective pitch angles from the innermost layer to the outermost layer are reduced so that the inclinations of the tube sections are attened.
  • FIG. l which represents a vertical cross-sectional view through half of two adjacent coil sections of a heat exchanger of the general type illustrated in FIGS. 3 and 4, it will be seen that the inner section 30 comprises ve layers designated generally at 31, 32, 33, 34 and 35, respectively.
  • the center lines of each tube of each layer represented at center points 31C of FIG. l, run helicoidally along a cylindrical surface represented by the dot-dash line 31s and centered upon axis A of the heat exchanger.
  • the cylindrical surfaces 31s etc. are, of course, imaginary and are common to the tubes of each layer. While the tubes of each layer are shown in circular cross Section in FIGS.
  • FIG. 1 there is shown the maximum spacing of the successive layers 31, 32, etc. from one another and it will be evident that the spacing between the nearest-neighbor tubes from one another at the point of closest approach is represented by the dimension a and may be 2 mm. in accordance with the principles of this invention as set forth earlier.
  • the center-to-center distance between the tubes of each array is represented by the dimension h while the outer diameter of each tube is represented at d.
  • the diameter (half shown) of the innermost helical coil 31 of the tube section 30 is represented at Dmin 1 and represents the minimum diameter of the tube section 30 while the outermost layer 35 of the rst tube section here illustrated is represented at Dmaxl and the mean diameter of the first tube section is designated at Dml.
  • the spacing between each layer and the next overlying layer is given by (d-j-a) V3.
  • the pitch of the turns is somewhat reduced and the pitch angle attened from the innermost to the outermost layer of each tube section.
  • the pitch of the innermost layer of the tube sections decreases from innermost section to outermost section while the pitch of the outermost layer of each section increases from innermost section to outermost section so that the average pitch of the turns of each section, corresponding to the pitch of the intermediate tube layer and the average tube length of each section remains constant over the entire tube bundle of the heat exchanger.
  • the first tube section is separated from the second tube section by a sheet-metal partition M of the type previously described and that the tube section 60 is, in turn, separated from an outer section by another sheet-metal mantle M".
  • the lratio of the difference between the tube length of the outermost layer Lmx and the tube length of the innermost layer Lmin of each tube section to t-he average or mean tube length Lm thereof can be determined in the following manner:
  • Equations 6 and 7 demonstrate:
  • Equation 9 for a constant ZL, the length difference l falls with an increasing z and rises, at a constant z, with increasing ZL.
  • Equation 9 The formula for l associated with hmm has been given in Equation 9 and it will be readily seen that the corresponding value of l for the value of Hmax can be derived in a similar manner and is:
  • the spacing between the tubes of each turn is greater than that corresponding to the hexagonal-close packed arrangement described above so that the successive layer of tubes can be interleaved or intertted.
  • h (dla) ⁇ /3
  • the transverse or horizontal distance between a tube of each layer and the nearest-neighbor tube of the next layer is shown at a and may have a value of, say 0.2 mm.
  • Equations l0-12 can be rendered as follows:
  • Equation 12 From a consideration of Equation 12, it can be seen that with a constant pressure drop, the reduction of the heating surface RL and a reduction of the tube spacing a is coupled with an increase in the gas velocity wo.
  • a conventional heat exchanger and one embodying the principles of the present invention to have the same gas velocity wo it can be seen from Equation (with wo held constant) and from Equation 12 with F constant that R 'L 'a constant
  • a reduction in the value of a requires, therefore, a reduction in the value of zw and, according to Equation 11, a decrease in the pressure drop Ap, in accordance with Equation 11.
  • a reduction in the axial height of the heat exchanger results.
  • a value of F :constant ensures that the heat exchanger according to the invention, which has a smaller value of the intertube distance a and correspondingly more tube layers, has a larger diameter.
  • a heat exchanger according to the invention has a larger diameter, a reduced axial height and a reduced pressure drop.
  • a crossow-countercurrent heat exchanger comprising:
  • a generally cylindrical shell having an inlet and an outlet for the throughflow of the first heatexchange uid in generally axial direction through said shell;
  • a helicoidal-tube bundle within said shell having inlet and outlet means for the passage of a second heatexchange iiuid through said bundle in a generally axial direction counter to the direction of fiow of said first fluid
  • said helicoidal-tube bundle comprising an annular inner tube section constituted of a plurality of coaxially nested inner layers each comprising a plurality of circumferentially spaced parallel-wound tubes having a plurality of helicoidal turns surrounding a common axis, and an annular outer tube section constituted of a coaxially nested plurality of outer layers surrounding said inner tube section, each of said outer layers comprising a plurality of circumferentially spaced parallel-wound tubes having helicoidal turns surrounding said axis, the tube length of the tubes of each section being substantially constant and the axial length of Said layers being substantially equal, the layers of each of said sections being wound in the same sence about said axis with the tubes of each section in a closepacked relationship with a tube
  • At least one relatively thin sheet-like mantle closely surrounding said inner tube section and interposed between said inner and Said outer tube section.
  • a heat exchanger as defined in claim 1 wherein the maximum perpendicular center-to-center spacing between the tubes of each layer ranges between hmm: (d-l-a) and 1maX (d-la) ⁇ /3, where d is the outer diameter of the tubes and a is the spacing between each tube and a nearest-neighbor tube of another layer.

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  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
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US546383A 1965-04-30 1966-04-29 Crossflow countercurrent heat exchanger with inner and outer-tube sections made up of closely packed coaxially nested layers of helicoidally wound tubes Expired - Lifetime US3403727A (en)

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Cited By (7)

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EP0351247A3 (en) * 1988-07-15 1990-04-25 Roberts, E. Dawson Recovery of heat from flue gases
WO1999034162A1 (en) * 1997-12-31 1999-07-08 Flowserve Management Company Helical coil heat exchanger with removable end plates
US6186223B1 (en) 1998-08-27 2001-02-13 Zeks Air Drier Corporation Corrugated folded plate heat exchanger
US6244333B1 (en) 1998-08-27 2001-06-12 Zeks Air Drier Corporation Corrugated folded plate heat exchanger
US20070039569A1 (en) * 2004-02-20 2007-02-22 Continental Engineers B.V. Apparatus provided with heat-exchanging means
CN112052550A (zh) * 2019-06-05 2020-12-08 无锡化工装备股份有限公司 一种壳程沸腾螺旋绕管式换热器的设计方法
WO2021144682A1 (en) 2020-01-13 2021-07-22 Stamenic Aleksandar Energy exchange device between media with improved structure and performances

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DE2736489C2 (de) * 1977-08-12 1986-12-04 Linde Ag, 6200 Wiesbaden Wärmetauscher
US8327923B2 (en) 2005-07-22 2012-12-11 Linde Aktiengesellschaft Wound heat exchanger with anti-drumming walls
DE102005034949A1 (de) * 2005-07-22 2007-01-25 Linde Ag Gewickelter Wärmetauscher mit Antidröhnwänden
BRPI0614699A2 (pt) 2005-07-29 2011-04-12 Linde Ag trocador de calor enrolado consistindo em diferentes materiais
EP1790932A1 (de) 2005-11-24 2007-05-30 Linde Aktiengesellschaft Gewickelter Wärmetauscher
DE102006001351A1 (de) * 2006-01-11 2007-07-12 Ohl Technologies Gmbh Spiralwärmetauscher
DE102007059541A1 (de) 2007-12-11 2009-06-25 Linde Aktiengesellschaft Wärmetauscher
DE102010050087A1 (de) 2010-10-29 2012-05-03 Linde Aktiengesellschaft Durchströmbare Einsätze für Wärmetauscher
CN113776356B (zh) * 2021-07-02 2023-01-17 清华大学 螺旋管式换热器

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US3130779A (en) * 1958-05-05 1964-04-28 Huet Andre Light boiler for nuclear energy installation
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US1892778A (en) * 1931-04-08 1933-01-03 Babcock & Wilcox Co Heat transfer device
US2199216A (en) * 1937-12-22 1940-04-30 Conti Piero Ginori Vaporizer
US2160898A (en) * 1938-03-16 1939-06-06 Peff Peter Heat exchange apparatus for rectifying columns
US2508247A (en) * 1945-09-25 1950-05-16 Research Corp Heat interchanger
US2645209A (en) * 1947-10-20 1953-07-14 Thomas J Digby Ammonia containing water heating unit
GB791843A (en) * 1955-03-12 1958-03-12 Ostbo Nils Recuperative heat exchanger
US3116790A (en) * 1958-03-28 1964-01-07 Kohlenscheidungs Gmbh Tube heat exchanger
US3130779A (en) * 1958-05-05 1964-04-28 Huet Andre Light boiler for nuclear energy installation
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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0351247A3 (en) * 1988-07-15 1990-04-25 Roberts, E. Dawson Recovery of heat from flue gases
WO1999034162A1 (en) * 1997-12-31 1999-07-08 Flowserve Management Company Helical coil heat exchanger with removable end plates
US6076597A (en) * 1997-12-31 2000-06-20 Flowserve Management Company Helical coil heat exchanger with removable end plates
US6186223B1 (en) 1998-08-27 2001-02-13 Zeks Air Drier Corporation Corrugated folded plate heat exchanger
US6244333B1 (en) 1998-08-27 2001-06-12 Zeks Air Drier Corporation Corrugated folded plate heat exchanger
US20070039569A1 (en) * 2004-02-20 2007-02-22 Continental Engineers B.V. Apparatus provided with heat-exchanging means
CN112052550A (zh) * 2019-06-05 2020-12-08 无锡化工装备股份有限公司 一种壳程沸腾螺旋绕管式换热器的设计方法
CN112052550B (zh) * 2019-06-05 2023-09-19 无锡化工装备股份有限公司 一种壳程沸腾螺旋绕管式换热器的设计方法
WO2021144682A1 (en) 2020-01-13 2021-07-22 Stamenic Aleksandar Energy exchange device between media with improved structure and performances

Also Published As

Publication number Publication date
DE1501519A1 (de) 1969-06-26
JPS5114741B1 (enrdf_load_stackoverflow) 1976-05-12
DE1501519B2 (de) 1971-02-25
GB1136292A (en) 1968-12-11

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