Heat exchangers coiled tube

The shape of the coohng and warming curves in coiled-tube heat exchangers is affected by the pressure drop in both the tube and shell-sides of the heat exchanger. This is particularly important for two-phase flows of multicomponent systems. For example, an increase in pressure drop on the shellside causes boiling to occur at a higher temperature, while an increase in pressure drop on the tubeside will cause condensation to occur at a lower temperature. The net result is both a decrease in the effective temperature difference between the two streams and a requirement for additional heat transfer area to compensate for these losses. 

Optimization of the coiled-tube heat exchanger is quite complex. There are numerous variables, such as tube and shell flow velocities, tube diameter, tube pitch, and layer spacing. Other considerations include single-phase and two-phase flow, condensation on either the tube or shell side, and boiling or evaporation on either the tube or shell side. Additional complications come into play when multicomponent streams are present, as in natural gas liquefaction, since mass transfer accompanies the heat transfer in the two-phase region. 

The laminar flow data of Figure 3.39 have a higher slope (0.52 than predicted by theory (0.33)-probably because of "secondary flow effects". The data were taken in a spiral flow thin channel device. Whenever fluid passes through a curved tube or channel, centrifugal forces tend to throw fluid outward from the center of the channel. It then recirculates inward along the walls of the channel (see Figure 3.40). It is well known that coiled tube heat exchangers possesses superior heat transfer characteristics because of secondary flow effects. 

Single-phase flow of either gas or liquid on the tube side is generally well represented by either the Colburn correlation or modified forms of the Dittus-Boelter relationships. Table 5.3 provides suggested heat transfer and corresponding pressure drop relationships for a coiled-tube heat exchanger with either banks of staggered or in-line tubes in the annulus space as detailed by Fig. 5.5. 

Flows are usually turbulent on both the tube and shell sides of coiled tube heat exchangers. To calculate pressure drops for single-phase tube side flows, it is simplest to use the normal Fanning friction factor correlation for... 

Coiled-tube heat exchangers frequently have flow distribution problems that include (1) tube distribution (2) two-phase tube distribution and (3) two-phase shell distribution. Good flow distribution within the tubes can be obtained by designing the headers in such a way that their pressure drop is considerably less than that for the frictional pressure drop in the tubes. To obtain good shell-side distribution one must use symmetric bundles and separately introduce the vapor and liquid phases to the bundles. It is also advisable to arrange for downflow of the shell-side fluid. For two-phase annular flow, the vapor will flow mostly in the space between the tube layers while the liquid needs to be carefully distributed in the radial direction for proportionate vapor-liquid flow normal to each tube layer. To avoid convection on the shell side due to density gradients, it is normal practice to use sufficiently large pressure drops on the shell side. 

The largest coiled-tube heat exchangers have been constructed for LNG base load plants. These heat exchangers can handle liquefaction rates up to and above 100,000 m h at 289 K and 0.101 MPa. Such a heat exchanger has... 

Fig. 5.9. Schematic of a coiled-tube heat exchanger utilized in base-load LNG production.

Determine the friction factor and pressure drop for the low-pressure side of a coiled-tube heat exchanger where the fluid flows past 100 tubes in a staggered-tube arrangement. An air flow rate of 0.5 kg/s enters the low-pressure side of the heat exchanger at 0.121 MPa and 183 K. The outside diameter of each tube is 10 mm while the minimum flow area between each tube is 0.0125 m. The transverse pitch is 0.0003 m. 

Calculate the heat transfer coefficient for the air flow in the low-pressure side of the coiled-tube heat exchanger described in Problem 5.8. 

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