Re-direction of vapor flow across tubular condensers

Abstract

Vapor flow-diverting devices that re-direct upwardly flowing vapor, for example, in a downward direction across condenser tubes disposed in the upper or top section of a vapor-liquid contacting apparatus, are described. These devices are particularly beneficial in tubular condensers within distillation columns and may be used in combination with other associated equipment (e.g., a deflector plate and divider plate) as well as in combination with the tube surface enhancements to improve the heat transfer coefficient.

Claims

1. An apparatus for vapor-liquid contacting, comprising a vertically oriented column having disposed therein a plurality of condenser tubes; an upper section of the vertically oriented column configured for receiving vapor rising upwardly from a lower contacting section of the column; a vapor flow-directing device disposed within the column and having a vapor inlet above at least a co-current contacting section of the tubes and defining a vapor-liquid disengagement volume, wherein the vapor inlet is in fluid communication with the upper section of the column for redirecting at least a portion of the vapor rising in the upper section downwardly through the co-current contacting section of the tubes; a non-condensed vapor outlet external to the column and in communication with the vapor-liquid disengagement volume; a condensed liquid outlet internal to the column and in communication with the vapor-liquid disengagement volume; and a divider plate extending into the vapor flow-directing device and dividing the co-current contacting section of the tubes, in a contacting volume, from a disengagement section of the tubes, in the vapor-liquid disengagement volume, wherein the divider plate extends substantially vertically and wherein: the condenser tubes extend substantially horizontally and each include a U-bend portion; and the U-bend portions of the condenser tubes are located in the disengagement section.

2. The apparatus of claim 1, wherein the vapor flow-directing device comprises a shroud positioned within the vertically oriented column, and further wherein said shroud includes at least three side surfaces, a bottom surface, a top surface, and wherein the vapor inlet is defined within the top surface of said shroud.

3. An apparatus for vapor-liquid contacting, comprising: a vertically oriented column having disposed therein a plurality of condenser tubes; an upper section of the vertically oriented column configured for receiving vapor rising upwardly from a lower contacting section of the column; a vapor flow-directing device disposed within the column and having a vapor inlet above at least a co-current contacting section of the tubes and defining a vapor-liquid disengagement volume, wherein the vapor inlet is in fluid communication with the upper section of the column for redirecting at least a portion of the vapor rising in the upper section downwardly through the co-current contacting section of the tubes; a non-condensed vapor outlet external to the column and in communication with the vapor-liquid disengagement volume; a condensed liquid outlet internal to the column and in communication with the vapor-liquid disengagement volume; and a divider plate extending substantially vertically within the vapor flow-directing device for dividing the co-current contacting section from the disengagement section, wherein the vapor flow-directing device substantially surrounds the co-current contacting section of the tubes on three sides thereof, while allowing the vapor rising to the upper section of the column to pass upwardly between said vapor flow-directing device and the column along said three sides.

4. The apparatus of claim 3, wherein: the condenser tubes extend substantially horizontally and each include a U-bend portion; and the U-bend portions of the condenser tubes are located in the disengagement section.

5. The apparatus according to claim 3, wherein the divider plate divides the vapor flow-directing device such that the vapor on one side of the divider plate generally flows downwardly and the vapor on the other side of the divider plate generally flows upwardly.

6. The apparatus according to claim 3, wherein at least a portion of the condenser tubes have external surfaces comprising one or more surface enhancements.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 depicts the upper section of a distillation column having an internal tubular condenser, with the tubes extending vertically over a section of the column length.

(2) FIG. 2 depicts the upper section of a distillation column having an internal tubular condenser, with the tubes extending horizontally over a co-current contacting section within a vapor flow-directing device.

(3) FIG. 3 depicts an end view of the upper section of the distillation column shown in FIG. 2.

(4) FIG. 4 depicts a representative internal tubular condenser, with the tubes extending horizontally over a co-current contacting section. A divider plate is used to separate the co-current contacting section of the tubes from a horizontally adjacent vapor-liquid disengagement section.

(5) FIG. 5 depicts a representative section of a tube for a tubular condenser, in which the tube has external surface enhancements in the form of circumferentially extending fins as discreet extensions.

(6) FIG. 5A depicts a representative section of a tube for a tubular condenser, in which the tube has external surface enhancements in the form of circumferentially extending fins as a single, continuously wound, helical spiral.

(7) FIG. 6 depicts a cross-sectional view of the tube section of FIG. 5, through A-A.

(8) FIG. 7A depicts a modification of the tube of FIGS. 5 and 6, in which a plurality of axially aligned notches, having a curved cross-sectional shape, are included on outer edges of circumferentially extending fins.

(9) FIG. 7B depicts a further modification of the tube of FIGS. 5 and 6, in which a plurality of axially aligned notches, having a triangular cross-sectional shape, are included on outer edges of circumferentially extending fins.

(10) FIG. 7C depicts a representative section of a tube having circumferentially extending fins as shown in FIG. 7B, but with the notches being bent at their respective corners outside of the plane of the circumferentially extending fins, and in opposite directions.

(11) FIG. 8 depicts a representative section of a tube having surface enhancements in the form of small shaped recessions aligned in axially extending rows that alternate, about the radial tube periphery, with larger, axially extending shaped recessions in the form of troughs, as well as internal spiral ridges.

(12) FIG. 9 depicts a representative section of a tube having surface enhancements in the form of axially extending shaped recessions or troughs that form axially extending ridges resulting from the axial extension of sections or points of the external tube surface that do not form the recessions.

(13) FIG. 10A depicts a cross-sectional view of a tube having surface enhancements in the form of axially extending shaped recessions having a semi-circular cross-sectional shape and spaced about the radial tube periphery.

(14) FIG. 10B depicts a cross-sectional view of a tube having surface enhancements in the form of axially extending shaped recessions having a triangular cross-sectional shape and spaced about the radial tube periphery.

(15) FIG. 10C depicts a cross-sectional view of a tube having surface enhancements including both axially extending shaped recessions, having a notched, triangular cross-sectional shape, that form alternating axially extending ridges.

(16) FIG. 10D depicts a cross-sectional view of a tube having surface enhancements in the form of axially extending shaped recessions having a semi-circular cross-sectional shape, with the axially extending ridges formed between these shaped recessions also having a semi-circular cross-sectional shape.

(17) FIG. 11 depicts a representative section of a tube having surface enhancements in the form of axially extending fins that are spaced about the radial tube periphery.

(18) FIG. 12 depicts a cross-sectional view of the tube section of FIG. 11, through A-A.

(19) FIG. 13A depicts a representative section of a tube having a twisted tube geometry as a tube enhancement.

(20) FIG. 13B depicts a cross-sectional view of the tube of FIG. 13A.

(21) The same reference numbers are used to illustrate the same or similar features throughout the drawings. The drawings are to be understood to present an illustration of the invention and/or principles involved. As is readily apparent to one of skill in the art having knowledge of the present disclosure, vapor-liquid contacting apparatuses, and particularly those comprising vertically oriented columns having tubular condensers disposed therein, according to various other embodiments of the invention, will have configurations (e.g., a number of tube passes) and components determined, in part, by their specific use.

DETAILED DESCRIPTION

(22) The invention is associated with improvements in heat exchangers and particularly internal tubular condensers used in vapor-liquid contacting apparatuses such as distillation columns. Internal tubular condensers, often referred to the in art as column installed or stabbed-in tubular condensers when used to condense vapors generated in distillation, are normally installed in the upper vapor-liquid contacting section of a column. These condensers may be installed either vertically from the top, as shown in FIG. 1 or horizontally from the side, as shown in FIG. 2. References to tubes extending vertically or horizontally are based on their general direction of orientation with respect to a vertically or substantially vertically oriented column in which they are disposed. Therefore, vertically extending tubes will extend, over the majority of their length, in the same general direction as the axis of the column, while horizontally extending tubes will extend, over the majority of their length, in the direction generally perpendicular to the axis of the column. Vertically or horizontally extending condensers refer in particular to heat exchangers having a tube bundle in which the tubes extend, respectively, vertically (or substantially vertically) or horizontally (or substantially horizontally) over a section (e.g., a top or overhead section) of the column length.

(23) The use of tubular condensers within vapor-liquid contacting apparatuses is often economically attractive compared to external heat exchangers or internal, welded plate exchangers. However, in conventional internal tubular condensers, vapor flows generally upwardly through the tube bundle, whether the bundle is arranged vertically or horizontally. In either case, but especially for horizontally aligned internal tubular condensers, it is possible for vapor velocities in the upward direction to hold up or even re-entrain falling liquid condensate, thereby flooding the tube bundle and limiting its capacity. As discussed above, aspects of the invention are associated with the discovery of commercial benefits that can result from diverting the vapor flow from its generally upward flow direction in an overhead section of a column, prior to contacting this vapor with tubes of a tube bundle of an internal condenser. In particular, diverting the flow of vapor (containing condensable material), can enhance the overall performance of the condenser by reducing the detrimental entrainment of condensed liquid by otherwise upwardly flowing vapor and thereby improving the condensed liquid/non-condensed vapor separation. The performance of tubular condensers may therefore be increased using devices that beneficially direct vapor flow in particular directions across, and/or in particular sections of, a tube bundle positioned within a vapor-liquid contacting apparatus.

(24) FIG. 1 shows an upper section of a distillation column 20 having a conventional internal tubular condenser 30, with a plurality of tubes 2 extending vertically over a section 4 of the column length. It is recognized that the entire length of the tube will generally not extend only in one direction, but will normally curve, for example in a U-bend, as shown in FIG. 1, to redirect fluid passing through the tubes back to a common tube sheet 6 securing the two ends of each of the tubes so that they are in communication with respective tube-side inlet 8 and outlet 10 conduits. During operation, upwardly flowing vapor 12a in the upper section of the distillation column 20 contacts tubes 2, through which cooling fluid (e.g., cooling water) is passed from the tube-side inlet 8 to the tube-side outlet 10. Contact between the relatively hot vapor 12a, comprising condensable material, and the relatively cool external surfaces of tubes 2 causes condensation, with condensed liquid falling back into the column interior and non-condensed vapor exiting through a non-condensed vapor outlet 14 that may be in communication with the column exterior. Both (i) the upwardly flowing vapor 12a and (ii) the fraction of this upwardly flowing vapor 12a that is the non-condensed vapor exiting the column are enriched, as a result of the distillation, in a lower boiling component initially present in an impure mixture. Compared to the upwardly flowing vapor 12a within the column, the non-condensed vapor exiting the column will normally be more enriched in this component, as a result of removing additional, higher boiling impurities through condensation. To improve contacting with tubes 2, the flow of upwardly-flowing vapor 12a may be passed from one side of the column 20 to the other side, using baffles 16, as it travels generally upwardly through tube bundle.

(25) Aspects of the invention are therefore directed to vapor flow-diverting devices that can act as a shroud around the tube bundle and re-direct vapor rising in the upper section of a vapor-liquid contacting device, such as from the top contacting stage of a distillation column, downwardly (rather than upwardly as shown in FIG. 1) through a co-current contacting section of the tubes in a tube bundle. For example, FIGS. 2 and 3 depict front and side views, respectively, of an upper section of a distillation column 20 containing a plurality of condenser tubes 2 in a horizontally aligned tube bundle (i.e., extending horizontally over a section 4 of the column length) of internal tubular condenser 30. Also disposed within the column is a vapor flow-directing device 50 that has a vapor inlet 52 above the tubes, such that the flow of vapor 12b is diverted downwardly through condenser tubes 2, causing vapor 12b and liquid condensed from this vapor to flow co-currently across the tube bundle. FIG. 3 illustrates a vapor inlet 52 having a reduced inlet area, with the width of this area being smaller than the diameter of the tube bundle. Decreasing or increasing the area over which vapor enters into the interior of the vapor flow-directing device 50 allows the velocity of the incoming vapor to be increased or decreased, respectively. After contacting condenser tubes 2, the resulting condensed liquid and non-condensed vapor then pass below the bundle these tubes 2 to a vapor-liquid disengagement volume 54 defined within a lower portion of the vapor flow-directing device 50, as shown in FIGS. 2 and 3.

(26) The vapor-liquid disengagement volume 54 provides a space for the settled, condensed liquid and non-condensed vapor to separate. Both a non-condensed vapor outlet 14, directed externally to the column and a condensed liquid outlet 58, directed internally to the column (e.g., back to an internal upper stage contacting device, such as a tray) are in communication with the vapor-liquid disengagement volume 54. FIGS. 2 and 3 further illustrate the use of a deflector plate 56 below the tubes and within the vapor-liquid disengagement volume 54, to aid the separation of vapor and liquid exiting the tube bundle co-currently. The deflector plate 56 may extend horizontally or may be inclined relative to horizontal, in order to improve drainage of condensed liquid in the disengagement volume 54 and ultimately to condensed liquid outlet 58. Condensed liquid outlet 58 may be operated with a liquid seal provided by draining, condensed liquid to prevent vapors in the upper section of column 20 from entering into the interior of vapor flow-directing device 50 upwardly through condensed liquid outlet 58.

(27) An alternative embodiment is illustrated in FIG. 4, where a divider plate 59 extends vertically into the vapor flow-directing device 50 and divides a co-current contacting section of the tubes, in a contacting volume 60, from a disengagement section of the tubes, in the vapor-liquid disengagement volume 54a. In this case, vapor inlet 52 is located above the co-current contacting section of the tubes 2, while the disengagement section of the tubes receives the non-condensed vapor only after it passes in a downwardly flowing direction across the co-current contacting section of the tubes 2. Divider plate 59, in the configuration of FIG. 4, therefore causes non-condensed vapor exiting contacting volume 60 to reverse flow again, flowing generally upwardly through disengagement volume 54a prior to exiting the non-condensed vapor outlet 14. Divider plate 59 can therefore advantageously reduce the vapor-liquid disengagement volume 54 below the tube bundle and instead allow some of this volume to be positioned horizontally adjacent the contacting volume 60.

(28) Thus, features described above include (i) the vapor flow-diverting device, which substantially surrounds (e.g., on three sides) the tube bundle and diverts vapor flow to the top of the bundle and downward therethrough, and (ii) the vapor-liquid disengagement volume defined by the vapor flow-diverting device, optionally in conjunction with a divider plate that provides separate (e.g., horizontally spaced apart) sections of the tube bundle for contacting and disengagement of the condensed liquid from the non-condensed vapor. These features can improve the performance of tubular heat exchanges and particularly those which are internal to vapor-liquid contacting apparatuses (e.g., internal distillation column condensers) by mitigating or eliminating flooding concerns, particularly in the tube bundles, enhancing heat transfer by improving vapor and liquid flow over the bundles, and/or providing improved vapor-liquid disengagement. Those having skill in the art will appreciate that changing the sizes and locations of the co-current contacting section and the vapor-liquid disengagement section, as well as the positions of the inlets to and outlets from, the vapor flow-diverting device (e.g., the non-condensed vapor outlet and condensed liquid outlet) can be used to create various flow paths of vapor and liquid across the condenser tubes, to further optimize the performance of the tubular condenser in terms of its heat transfer coefficient and thereby minimize its size. For example, it may be desired to use a vapor-flow diverting device to direct incoming vapor in a horizontal direction, or in an inclined direction, across the tubes of a tube bundle.

(29) In addition to these improvements, tubes having one or more surface enhancements as discussed above may be used to effectively improve their heat transfer coefficient when used in combination with a vapor flow-diverting device and optionally a deflector plate and/or divider plate. These external surface enhancements may optionally be combined with an internal surface coating and/or non-linear or twisted geometries, also as discussed above, to further improve the tube performance. The various tube surface enhancements described herein may serve, alone or in combination, to facilitate this condensate drainage and/or reduce the layer thickness of formed condensate. In representative embodiments, for example, the use of such surface enhancement(s) will generally increase the tube heat transfer coefficient in a given condensing service (e.g., in a distillation column used in the product recovery section in the commercial production of phenol via cumene oxidation) by a factor of at least about 1.5, typically from about 2 to about 10, and often from about 3 to about 5, relative to the heat transfer coefficient obtained with identical tubes but lacking the surface enhancement(s).

(30) As discussed above, this improvement in heat transfer coefficient decreases the tube area needed, such that tubular condensers employing these enhancements can be feasibly installed in larger-diameter distillation columns, for example those having a diameter of generally greater than about 0.9 meters (3 feet), typically in the range from about 1.07 meters (3.5 feet) to about 6.10 meters (20 feet), and often in the range from about 1.22 (4 feet) to about 4.88 meters (16 feet). The use of tube bundles in tubular condensers, in which at least a portion of the individual tubes have surface enhancements as described herein, may in some cases provide an economically attractive alternative, relative to external condensers or even welded plate, internal condensers. Any of the tubes described below, having surface enhancements, will generally have an outer diameter in the range from about 13 mm (0.5 inches) to about 38 mm (1.5 inches), and often from about 19 mm (0.75 inches) to about 32 mm (1.25 inches). The inner diameters of such tubes are generally in the range from about 6 mm (0.25 inches) to about 32 mm (1.25 inches), and often from about 13 mm (0.5 inches) to about 25 mm (1 inch). The inner and outer diameters can be determined and/or optimized for a given service based on a number of factors, including the design flow rates, pressure drops, and heat transfer coefficients, as will be appreciated by those having skill in the art and knowledge of the present disclosure.

(31) Any of the tube enhancements, including internal enhancements, as well as different tube geometries (e.g., twisted tubes) described herein are applicable to internal condensers having vertically extending tubes as depicted in FIG. 1, as well as those having horizontally extending tubes as depicted in FIG. 4. In the case of internal distillation column condensers having vertically (or substantially vertically) or horizontally (or substantially horizontally) oriented condenser tubes, surface enhancements, in at least the region of the tubes extending over a section of the column length, include circumferentially extending fins, as illustrated in FIG. 5. FIG. 5A shows circumferentially extending fins 15a provided by a single, continuously wound, helical spiral rather than discreet extensions, as shown in FIG. 5. In the case of tubes 2 comprising circumferentially extending fins 15a, a fin height of less than about 6.4 mm (0.25 inches) is representative, with fin heights typically being in the range from about 0.51 mm (0.02 inches) to about 5.1 mm (0.20 inches), and often being in the range from about 0.76 mm (0.03 inches) to about 3.8 mm (0.15 inches). As is illustrated in the cross-sectional view of FIG. 6, circumferentially extending fins 15a may be in the form of flat plates or discs having a circular cross section that is concentric with circular cross sections of internal surface 25 and external surface 27 with these cross sections being circles with inner and outer diameters, respectively, of tubes 2. The fin height can therefore be measured as the distance from the external surface 27 of a tube 2 to the outer edge 29 of circumferentially extending fin 15a. In cases where the fins have geometries that are not circular (e.g., elliptical or rectangular), where the fin cross sectional shape is not concentric with the central axis of the tube 2, or where the tube 2 itself has a non-circular (e.g., flattened or elliptical) cross section, the fin height may be the average distance from the outer edge 29 of circumferentially extending fin 15a to the external surface 27 of tube 2.

(32) FIG. 7A shows a cross-sectional view of a tube 2 having surface enhancements in the form of fins 15a, as shown in FIGS. 5 and 6. In the embodiment illustrated in FIG. 7A, however, a plurality of notches 35 are cut from, or shaped in, the outer edges 29 of fins 15a. Notches 35 shown in FIG. 7A have a curved cross-sectional shape (e.g., semi-circular), but other curved cross-sectional shapes or rectangular cross-sectional shapes may be used for notches 35. For example, FIG. 7B shows notches 35 having a triangular cross-sectional shape. Also as illustrated in FIGS. 7A and 7B, notches may be spaced evenly about the outer edge 29 or periphery of fin 15a. In a particular embodiment, in which circumferentially extending fins 15a, as surface enhancements, have outer edges 29 that include notches 35 having a triangular (or other) cross-sectional shape, these notches 35 may be bent at their respective corners 37 outside of the plane of the circumferentially extending fins, for example opposing corners 37 of a triangular cross section may be bent in the same or opposite directions. In the particular embodiment illustrated in FIG. 7C, for example, these notches 35 are bent at their respective corners 37 in opposite directions. In a preferred embodiment, and particularly in the case in which the tubes are used in vertical, column-installed condensers, all or a portion of notches 35, whether or not they are bent, may be aligned axially, with one or more corresponding notch(es) in the outer edge of one or both adjacent circumferentially extending fins (e.g., in both of the circumferentially extending fins located immediately above and immediately below, in the case of a vertically extending tube). Axial alignment of notches is also illustrated in the representative embodiment of FIG. 7C. This axial alignment of notches can promote improved drainage of condensate from the tubes, particularly in the vertical direction.

(33) In the same manner as described above with respect to notches on outer edges of fins, notches or recessions having various cross-sectional shapes may be formed directly on the outer surfaces of heat exchanger tubes to provide surface enhancements. Extending these notches in the axial direction on the tube surface results in elongated troughs about the tube periphery. Alternatively, discreet, shaped recessions may be formed on the external tube surface. While the recessions themselves may be small, if desired, in order to provide an effective capillary action that reduces condensate layer thickness, such smaller recessions may be aligned axially to provide an axial or generally axial flow path for condensed liquid. FIG. 8 depicts tubes 2 having shaped recessions 36a, 36b on the external surface, where a portion of these recessions 36a are smaller and are aligned in axially extending rows 22a, for example, with outer edges of the recessions in a row 22a forming a line that extends axially along the external surface of the tube. As discussed above, these smaller, discreet shaped recessions 36a on the tube surface can act as capillaries, such that the surface tension of the condensed liquid is drawn into recessions 36a. In a representative embodiment, in order to provide capillary action, each individual shaped recession will normally have only a small area, typically less than about 5 mm.sup.2 (7.810.sup.3 in.sup.2) and often in the range from about 0.1 mm.sup.2. (1.610.sup.4 in.sup.2) to about 4 mm.sup.2 (6.210.sup.3 in.sup.2). Aligning at least some of the recessions in one or more axially extending rows may improve drainage of the condensed liquid, particularly in the case of a vertically extending internal tubular condenser. In the embodiment shown in FIG. 8, the axially aligned, smaller, discreet shaped recessions 36a are used as surface enhancements in combination with axially elongated shaped recessions 36b (i.e., with the individual recessions extending over a longer axial portion). Both of these surface enhancements may be used in a common region of the tube that extends over a section of the length of a distillation column where condensation occurs. In the particular embodiment illustrated in FIG. 8, rows 22a of discreet, shaped recessions 36a alternate radially about the tube periphery with rows 22b of larger, axially extending shaped recessions 36b (e.g., in the form of troughs), between which rows the external surface 27 of tube 2 may be smooth. FIG. 8 also depicts internal enhancements on internal surface 25, namely spiral ridges 21, which may be used for improved heat exchange. In FIG. 9, the axially extending, shaped recessions 36b are in the form of troughs having a triangular cross-sectional shape.

(34) FIGS. 10A-10C illustrate in more detail some representative cross sections of tubes having shaped recessions 36 on their external surfaces 27. In particular, the shaped recessions 36 in FIG. 10A have a curved cross-sectional shape that is semi-circular, while the shaped recessions 36 in FIG. 10B have a triangular cross-sectional shape. Other curved and rectangular (e.g., semi-elliptical and square) cross-sectional shapes are possible. Another embodiment in which tube surfaces are enhanced with shaped recessions 36 is shown in FIG. 10C, where, as in FIG. 10B, the cross-sectional shapes of recessions 36, spaced (e.g., uniformly) about the periphery of the surface of tube 2, are triangles. In the embodiment shown in FIG. 10C, however, these triangles are broad enough such that only small sections or points of the external surface 27 of tube 2 remain (or are not part of the shaped recessions), with these sections being spaced radially about the periphery of tube 2. The axial extension of these sections or points results in axially extending ridges. Such a tube with axially extending, shaped recessions 36b or troughs aligned in axial rows 22b is also illustrated in the front view of FIG. 9.

(35) In FIG. 10D, the axially extending ridges, similarly formed between these shaped recessions, have a smooth, curved (e.g., semi-circular) cross-sectional shape of the same or similar dimension as the curved cross sectional shape forming the shaped recessions. The cross sectional shape of this tube therefore has a generally circular perimeter defined by alternating, concave and convex curves (e.g., semi-circles). The resulting, smooth external surface contrasts with the embodiment shown in FIG. 10A, where the shaped recessions form edges. Therefore, as shown, for example in the embodiment of FIG. 10D, the shaped recessions can provide a fluted profile of a fluted tube. Fluted tubes or other tubes having axially extending shaped recessions or discreet, shaped recessions aligned in axially extending rows as depicted, for example, in FIGS. 10A-10D may be characterized as having two outer diameters. Smaller and larger outer diameters may be the distances, respectively, to opposing deepest points of recessions 36 and opposing external surfaces 27, with each of these distances being measured through the center of the cross section of tube 2. Representative tubes having axially extending shaped recessions will have smaller and larger outer diameters in the ranges from about 13 mm (0.5 inches) to about 32 mm (1.25 inches) and from about 19 mm (0.75 inches) to about 38 mm (1.5 inches), respectively. In exemplary embodiments, such a tube will have outer diameters of about 19 mm (0.75 inches) and about 25 mm (1.0 inches) or outer diameters of about 25 mm (1.0 inches) and about 32 mm (1.25 inches).

(36) Additional surface enhancements to improve heat transfer for vertically extending tubes are shown in FIG. 11, which depicts tubes having a plurality of axially extending fins 15b that may, for example, be in the form of flat plates raised above the external surface 27 of the tube 2 and extending axially along the length of the tube. Representative fins may have a fin height as described above with respect to the heights of circumferentially extending fins, with the fin height also being based on the distance (or average distance) between the outer edge 29 of axially extending fin 15b and the external surface 27 of tube 2. Otherwise, the fin heights of axially extending fins may be relatively higher, for example with ranges from about 3.2 mm (0.125 inches) to about 25 mm (1 inch), and often from about 6.4 mm (0.50 inches) to about 19 mm (0.75 inches) being representative.

(37) A cross-sectional view of the tube shown in FIG. 11, having a plurality of axially extending fins 15b, in this case spaced uniformly about the radial periphery of the tube 2, is shown in FIG. 12. As discussed above with respect to circumferentially extending fins (15a in FIG. 5), axially extending fins 15b may also have notches with various cross-sectional shapes. FIG. 13A illustrates a tube having a twisted tube geometry to provide an overall helical fluid flow path within the tube. As seen in the cross-sectional view of FIG. 13B the eccentric profile tube has an oval-shaped cross section 50, with the major axis 55 that rotates clockwise or counterclockwise along the linear direction of the tube).

(38) Any of the axially extending features (i.e., in the same or substantially the same direction as the central axis of the tube) discussed above, such as axially extending shaped recessions, axially extending rows of shaped recessions, or axially extending fins, are therefore vertically or horizontally extending features, depending on whether the tubes are aligned vertically or horizontally, respectively. In alternative embodiments, any of the described, axially extending features may extend or be aligned generally in the axial direction along the length of the external surface of the tube, in a non-linear path such as a wave, spiral, jagged line, etc. Such embodiments provide a generally axial flow path (e.g., corresponding to the downward flow path of condensed liquid along the tube when positioned vertically) for fluid contacting the heat exchange surface, where this flow path provided by the features is not directly, but only generally, axially.

(39) The use of axially or generally extending shaped recessions and/or fins, in this manner, as tube surface enhancements, can reduce condensate film thickness and/or facilitate condensate drainage, thereby improving the heat transfer coefficient of the tube. Such features as surface enhancements for tubes are particularly advantageous in internal tubular condensers (e.g., disposed in distillation columns), where the heat exchange surface area, as well as the total weight of equipment that can be practically installed (e.g., at or near the top of the column or tower), is limited. The tube surface enhancements discussed above may be used alone or in combination. The tube surface enhancements may also be used in combination with internal enhancements as discussed above, and particularly spiral ridges that may act to further improve heat transfer. Otherwise, these surface enhancements may be combined with a coating, such as a porous metallic matrix used to form an enhanced boiling layer as discussed above, that is bonded onto internal surfaces of the tubes, for example, in at least the same region of the tubes (e.g. extending over a section of the column height) as the surface enhancements. The surface enhancements may also be used in tube bundles in which all or a portion of the tubes have a non-linear central axis (e.g., a helical axis), or otherwise have a twisted tube geometry as discussed above, in at least the same region of the tubes as the surface enhancements. In a representative embodiment, for example, a tube bundle of a condenser, having tubes with a fluted tube profile and an internal enhancement including one or more spiral ridges, is aligned vertically in the upper section of a distillation column. Various other combinations of surface enhancements, optionally with an internal surface coating and/or non-linear or twisted geometries, can be incorporated into tubes to improve their heat transfer coefficient, particularly when the tubes are used in a tube bundle that is oriented vertically and used in a service in which condensate drains vertically from the external surfaces of the tubes (i.e., on the shell side of the condenser).

(40) Overall, aspects of the invention are directed to improvements in heat exchangers and particularly tubular exchangers oriented horizontally or vertically within contacting apparatuses such as distillation columns. Those having skill in the art, with the knowledge gained from the present disclosure, will recognize that various changes can be made in the above apparatuses, heat exchangers, tubes, and vapor-liquid contacting (e.g., distillation) methods without departing from the scope of the present disclosure. Mechanisms used to explain theoretical or observed phenomena or results, shall be interpreted as illustrative only and not limiting in any way the scope of the appended claims.