INDIRECT HEAT EXCHANGE DEVICE AND METHOD OF EXCHANGING HEAT
Indirect heat exchange device comprising heat exchanger tubes arranged in at least 2 layers each of which layers comprises at least 2 heat exchanger tubes wherein the heat exchanger tubes are eccentrically finned (53) heat exchanger tubes having a ratio of surface area of the fins to surface area of the tube of at least 5, and in which device the heat exchanger tubes have similar eccentricity; and method of exchanging heat with the help of such device.
The present invention relates to an indirect heat exchange device comprising finned heat exchanger tubes and to a method of exchanging heat between a first fluid and a second fluid.
BACKGROUND OF THE INVENTIONFinned heat exchanger tubes can be used in indirect heat exchange devices wherein a first fluid, which is passed through the interior of the finned tubes, can exchange heat with a second fluid outside the tubes.
For a variety of reasons, the geometric centroid of the cross-section of the envelope defined by the fins of a heat exchanger tube sometimes does not coincide with the axis of the tube. DE-A-1451143 describes an indirect heat exchange device of which the fins of the outer heat exchanger tubes contain additions to shade these outer fins from the sun or other sources of heat. GB-A-281,289 describes finned heat exchanger tubes of which the fins are arranged eccentric relatively to the centre of the tube, which tubes are arranged in layers having opposite eccentricity in order to force gases to take a sinuous path in order to increase the efficiency of the apparatus. U.S. Pat. No. 4,002,198 describes a desublimator for isolating sublimation products comprising finned tubes intended to be alternately subjected from the inside to a heating medium and a coolant, the transverse fins of which tubes are arranged in rows staggered laterally in opposite directions by an amount corresponding to the whole spacing between adjacent fin edges to provide additional turbulence surfaces causing greater pressure drops. U.S. Pat. No. 4,440,216 teaches to foreshorten the fins at the top of a heat exchanger tube in order for liquid to be more uniformly distributed over the tubes. The fins of liquid treated heat exchanger tubes have a relatively small surface area, i.e. the ratio of surface area of fins to surface area of the tube will be substantially less than 5.
Finned heat exchanger tubes may in particular be used in air-cooled heat exchanger devices, wherein the fluid outside the tubes is air.
Air-cooled heat exchangers can also be referred to as air coolers. Air coolers are described in Perry's Chemical Engineers' handbook, 7th edition, 1997, pages 11-47 to 11-52. Air coolers are for example used in refinery, petrochemical and chemical processes to cool or condense process fluids inside the tube with air outside the tube. Air coolers typically include a bundle of finned tubes, and a fan, which fan moves air across the tubes.
In air-cooled heat exchangers, the heat transfer from the fluid inside the tube to the tube itself is typically much more efficient than the heat transfer between the fluid outside the tube (air) and the tube itself. The efficiency of heat transfer can for example be expressed by a so-called film coefficient as defined in Perry's, pages 5-12 to 5-19. In order to compensate for a difference in film coefficients, the external surface area of the heat exchanger tube is increased by means of fins, so that the product of film coefficient and surface area inside and outside of the heat exchanger tube is of the same order of magnitude.
Heat transfer due to free convection can be described by the following equation:
The rate dQ/dt of heat exchanged Q (also referred to as duty) with the surrounding fluid is proportional to the object's exposed area A, and the difference between the object temperature Tw and the fluid free-stream temperature T∞. The constant of proportionality h is termed the convection heat-transfer coefficient, also referred to as film coefficient [units W/(m2.K)].
The flow of fluid outside the tube is typically induced by a fan. The higher the air velocity, the higher the heat transfer coefficient and the higher the duty. However, the air velocity is often limited, such as by the maximum noise level of a fan, e.g. 80 dBa. For a given fan rotating at a certain speed, the air velocity across a bundle of finned tubes is determined by the static pressure drop (resistance) of the bundle. A higher air velocity will be achieved if the pressure drop (resistance) is lower.
Finned tubes are also employed in heaters or furnaces, such as fired heaters, for improving the heat transfer from the heating fluid surrounding the tubes to fluid that is flowing inside the tubes. It has been observed that coking of fluid inside heat exchanger tubes occurs preferentially at the upstream (upwind) side of the flow of fluid outside the tubes, for example in heaters for crude oil entering a crude distillation unit. Typically the heating fluid is combustion gas from the combustion of a fuel, rising upwardly in a heater.
It is desired to increase the efficiency of heat transfer in heat exchange devices comprising finned heat exchanger tubes.
SUMMARY OF THE INVENTIONTo this end there is provided an indirect heat exchange device comprising heat exchanger tubes arranged in at least 2 layers each of which layers comprises at least 2 heat exchanger tubes wherein the heat exchanger tubes are eccentrically finned heat exchanger tubes having a ratio of surface area of the fins to surface area of the tube of at least 5, and in which device the heat exchanger tubes have similar eccentricity.
Finned heat exchanger tubes have an axis and are provided with fins, the fins defining an envelope having a cross-section, wherein the cross-section of the envelope has a geometric centroid. In eccentrically finned heat exchangers, this geometric centroid is spaced apart from the axis of the tube.
The geometric centroid of an area, such as of the cross-section of the envelope of the fins, is similar to the center of mass of a body. Calculating the centroid is based on the geometrical shape of the area. Cartesian co-ordinates Cx, Cy of the geometric centroid can for example be determined by integration over the area A, Cx=∫x dA/A, Cy=∫y dA/A, A=∫ dA.
The axis of the tube is the longitudinal axis of the interior of the tube.
Eccentricity is defined as the spacing, both in magnitude and direction, between the axis of the tube and the geometrical centroid of the envelope of the tube as positioned in the device. Finned heat exchanger tubes of similar eccentricity in the heat exchange device are finned tubes having an eccentricity which is the same both in magnitude and in direction for their position in the heat exchange device. The influence of the position in the device on the eccentricity of a tube is clear from FIGS. 1, 3 and 4 of GB-A-281,289 where the eccentriciy of tubes in adjacent layers is opposite in direction due to the different position of tubes in adjacent layers.
In the indirect heat exchange device according to the present invention, most, preferably all, finned heat exchanger tubes of the device have a similar eccentricity. Preferably, the finned heat exchanger tubes of the device according to the present invention have the same eccentricity both in magnitude and direction.
It is preferred that the direction of the eccentricity of the heat exchanger tubes of the device is parallel, i.e. either the same or opposite in direction, to the direction in which fluid outside the tubes normally flows.
A substantial part of the static pressure drop due to a finned heat exchanger tube is caused by the fins. It has now been found that the effectiveness of finning with respect to heat transfer is higher at the upstream side of the tube than at the downstream side. In the description and in the claims, the upstream (also referred to as upwind) side is the side at which the fluid flow direction outside the tubes is towards the finned tubes, and at the downstream (downwind) side the fluid flow outside the tubes is away from the tubes.
The different effectiveness can be observed for conventional concentric circular fins in that the temperature of the tips of such fins is lower on the upstream side than on the downstream side. The difference in temperature between the fin tip and the fluid surrounding the fin tip, hereinafter referred to as the differential temperature, is also higher for the fins at the upstream side of such conventional heat exchanger tubes. For this reason it is advantageous to arrange the finning eccentrically on the tubes, or in other words, to use non-concentric fins. It will be clear that the difference in effectiveness is more pronounced for heat exchanger tubes having a relatively high surface area, i.e. having a ratio of surface area of the fins to surface area of the tube of more than 5, more specifically at least 6, more specifically at least 7, more specifically at least 8, more specifically at least 9, and most specifically at least 10. It is especially preferred for the indirect heat exchange devices of the present invention to contain such high surface area heat exchanger tubes. The ratio of surface area of the fins to surface area of the tube preferably is at most 25. The surface area of the fins is the surface area of the fins to be in contact with the fluid outside the tube while the surface area of the tube is the surface area of the tube in contact with the fluid inside the tube.
A particular phenomenon in heat transfer by finned tubes is recirculation, i.e. eddies formed in the fluid at the downstream side, which hamper efficient heat transfer. This effect is also minimized by having the larger part of the fin surface at the upstream side. By proper design for a particular application it can be achieved that the upstream and downstream differential temperatures at the tips of the fins of the heat exchanger tubes are substantially equal.
The fin can have any suitable shape such as circular, elliptical, oval, polygonal, or egg-shaped (i.e. roughly oval with somewhat different radii at the tips; the larger radius can suitably be arranged at the downstream side). An elliptical shape has shown good results.
Because the heat transfer is optimised, less finning is required to achieve the same duty. Moreover, if less finning is used, the static pressure drop over a bundle will reduce so that the maximum air velocity for a given fan capacity will increase, so that the overall duty can be increased.
The indirect heat exchange device according to the present invention comprises at least 2 layers, preferably at least 3 layers, more preferably at least 4 layers of heat exchanger tubes. Preferably, the number of layers is at most 10, more preferably at most 9. Further, each layer comprises at least 2, more preferably at least 3, more preferably at least 4 heat exchanger tubes. The number of layers and the number of tubes is the number of times the tube is present independent from whether the tubes are connected to each other such as via a tube bend.
The heat exchanger tubes in adjacent layers are preferably arranged staggered with respect to each other while the tubes in the device still have similar eccentricity.
The heat exchange device according to the present invention can further comprise a fan having a blow or suck direction across the heat exchanger tubes and defining an upstream side of the heat exchanger tubes, and wherein the geometric centroid of the cross-section of the envelope defined by the fins is arranged upstream from the axis of the tube.
The problem of preferential coking in a heater can also be solved with the help of the heat exchange device according to the present invention. According to the present invention, the geometric centroid of the cross-section of the envelope defined by the fins preferably is arranged downstream from the axis of the tubes with respect to the direction of heating fluid flow across the heat exchange device (typically the upper side). Accordingly, in a particular aspect the invention provides an indirect heat exchange device arranged in a heater having flow direction of heating fluid across the heat exchange device and defining a downstream side of the heat exchanger tubes of the device, and wherein the geometric centroid of cross-section of the envelope defined by the fins is arranged downstream from the axis of the tubes. In this way a more equal heat transfer around the circumference of the tube is achieved, so that temperature differences at the inner wall between the upstream and downstream sides are minimized. This will suppress preferential coking at the upstream side within the tubes.
In the description and in the claims the expression “the geometric centroid of the cross-section of the envelope defined by the fins is arranged upstream (or downstream) from the axis of the tube” refers to a position of the geometric centroid in a plane parallel to a plane through the tube axis and perpendicular to the direction of the flow of fluid outside the tubes, and which plane is more upstream (or more downstream) than the plane through the tube axis, respectively. In advantageous embodiments the geometric centroid is in an upstream (or downstream) position along the direction of fluid flow outside the tubes with respect to the axis of the tube.
The invention also provides the use of the indirect heat exchange device according to the invention for exchanging heat between a first fluid inside the tubes and a second fluid outside the tubes. Accordingly, the invention provides a method of exchanging heat between a first fluid and a second fluid, the method comprising
providing an indirect heat exchange device according to the invention;
passing first fluid through the heat exchanger tubes of the device;
passing second fluid along a flow direction across the heat exchanger tube, wherein the direction of the eccentricity of the heat exchanger tubes is parallel to the flow of direction of the second fluid.
Preferably, the upstream and downstream differential temperatures, as defined above and with respect to the flow of fluid outside the tubes, at the tip of the fins of the heat exchanger tubes are substantially equal during use in the method according to the invention.
The second fluid can be gas optionally in combination with a limited amount of liquid. Preferably, the second fluid is gas only.
When the second fluid is a cooling fluid, in particular air, the geometric centroid is preferably arranged upstream from the axis of the tube. When the second fluid is a heating fluid, in particular comprising combustion products, the geometric centroid is preferably arranged downstream from the axis of the tube.
Heat exchanger tubes for use in the device according to the present invention can be manufactured in many different ways. A suitable method of manufacturing comprises
providing a tube having an outer surface and a circumference;
providing an elongated strip of fin material having a length direction, the strip having a straight side along its length direction, and a side opposite the straight side, wherein the width of the strip varies along the length direction defining maxima and minima, wherein the maxima are spaced apart in length direction substantially by the circumference of the tube;
spirally winding the strip around the tube so that the straight side is attached to the outer surface of the tube.
Using this method a finned heat exchanger tube can be obtained, which has an eccentric envelope with respect to the axis of the tube, wherein the geometric centroid of cross-sections of the envelope extends a line parallel to the longitudinal axis of the tube. The elongated strip can be efficiently manufactured by cutting from an elongated strip with parallel straight sides, so that two elongated strips are obtained.
The invention will now be described in more detail and with reference to the accompanying drawings, wherein
Where the same reference numerals are used in different Figures, they refer to the same or similar objects.
DETAILED DESCRIPTION OF THE INVENTIONReference is made to
Reference is now made to
Reference is now made to
During operation of the assembly 54, a first fluid is passed through the interior 62 of the tubes 53, and the fan blows second fluid (e.g. air) across the tubes along the blow direction 58, so as to exchange heat between the first and second fluids, e.g. to cool the first fluid against air.
The elliptical fins are non-concentrically arranged such that the geometric centroid of their envelope is below the axis of the tubes in
Computational Fluid Dynamics calculations have been performed, in order to compare the heat transfer duty and pressure drop of a four layer bank of finned heat exchanger tubes according to the invention with an analogous arrangement of conventional circular finned tubes. The calculations were performed using a so-called EFD. Lab software package.
The model assumes copper tube cores with aluminium fins. The tube core has a fixed temperature of 100° C. The ambient temperature of the air is 30° C. The tubes are in cross flow, with an ambient air velocity of 4 m/s. The following parameters were used in the calculations.
Finned tube dimensions (all examples):
Bare inner tube outer diameter: 25.4 mm
Fin thickness: 0.4 mm
Fin pitch (10 fins/inch): 2.54 mm
Fin spacing: 2.14 mm
Ratio of surface area of fins to surface area of tube: 20
Bank dimensions:
Tube pitch: 63 mm
Stagger angle: 60 degrees
4 layers each comprising several tubes
The device according to the invention comprised ellipsoid and eccentrically finned tubes.
Major diameter: 74.4 mm
Minor diameter: 42.98 mm
Minimum fin height: 10 mm
Maximum fin height: 39 mm
Magnitude of eccentricity: 15 mm
The device not according to the invention comprised conventional concentric circular finned tubes.
Fin height: 15.88 mm
Outer diameter of fin envelope: 57.15 mm
In Example 1, a duty of 1366.9 W per meter length of the finned tube was obtained, at a pressure drop of 101.5 Pa. In the Comparative Example 2, the duty was somewhat higher, 1505.5 W/m, but at a much higher pressure drop namely 132.0 Pa. The ratio of duty to pressure drop was 18% higher in the Example 1 according to the invention.
The embodiment of a heater wherein preferential coking is to be suppressed would be similar to
Claims
1. Indirect heat exchange device comprising heat exchanger tubes arranged in at least 2 layers each of which layers comprises at least 2 heat exchanger tubes wherein the heat exchanger tubes are eccentrically finned heat exchanger tubes having a ratio of surface area of the fins to surface area of the tube of at least 5, and in which device the heat exchanger tubes have similar eccentricity.
2. Indirect heat exchange device according to claim 1, wherein the ratio of surface area of the fins to surface area of the tube is at least 7.
3. Indirect heat exchange device according to claim 2, wherein the direction of the eccentricity is parallel to the direction in which fluid outside the tube normally flows.
4. Indirect heat exchange device according to claim 3 further comprising a fan having a blow or suck direction across the heat exchanger tubes and defining an upstream side of the heat exchanger tubes, wherein the geometric centroid of the cross-section of the envelope defined by the fins of the heat exchanger tubes is arranged upstream from the axis of the tubes.
5. The indirect heat exchange device according to claim 3 arranged in a heater having flow direction of heating fluid across the heat exchanger tubes and defining a downstream side of the heat exchanger tubes, wherein the geometric centroid of the cross-section of the envelope defined by the fins is arranged downstream from the axis of the tubes.
6. A method of exchanging heat between a first fluid and a second fluid, the method comprising:
- providing a indirect heat exchange device according to any one of claim 1;
- passing first fluid through the heat exchanger tubes of the device; and
- passing second fluid along a flow direction across the indirect heat exchange device, wherein the eccentricity of the heat exchanger tubes is parallel to the flow direction of second fluid.
7. The method according to claim 6, wherein the first fluid is a cooling fluid, in particular air, and wherein the geometric centroid of the fins of each of the heat exchanger tubes is arranged upstream from the axis of the tubes.
8. The method according to claim 6, wherein the first fluid is a heating fluid, in particular comprising combustion products, and wherein the geometric centroid of the fins of each of the heat exchanger tubes is arranged downstream from the axis of the tubes.
9. The method according to claim 8, wherein the upstream and downstream differential temperatures at the tip of the fins of the heat exchanger tubes are substantially equal.
Type: Application
Filed: May 14, 2008
Publication Date: Jan 6, 2011
Inventor: Dominicus Fredericus Mulder (Amsterdam)
Application Number: 12/599,930
International Classification: F28D 15/00 (20060101); F28F 1/10 (20060101);
