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This is particularly important when vacuum steam is being used, since small changes in steam pressure can give significant alterations in the temperature at which the steam condenses. Plate Liquid heat exchanger equations Exchangers also are used for gas cooling.

The problems are similar to those of steam heating since the gas velocity changes along the length of the plate due either to condensation or to pressure fluctuations. Designs usually are restricted by pressure drop, therefore machines with low-pressure drop plates are recommended. A typical allowable pressure loss would be 3. The plate heat exchanger can also liquid heat exchanger equations used for evaporation of highly viscous fluids when the evaporation occurs in plate or the liquid flashes after leaving the plate.

Applications generally have been restricted to the soap and food industries. The advantage of these units is their ability to concentrate viscous fluids liquid heat exchanger equations up to pascal seconds. The unit is particularly suitable for high concentration especially as a finishing stage to a larger evaporator where the quantity of vapor is low and can be handled by the comparatively small ports of the plate [Jackson and Trouper ]. One other field suitable for the plate heat exchanger is that of liquid heat exchanger equations flow heat transfer.

It has been previously pointed out that the exchanger can save surface by handling fairly viscous fluids in turbulent flow because the critical Reynolds number is low. Once the viscosity exceeds cP, however, most plate heat exchanger designs fall into the viscous flow range. Considering only Newtonian fluids since most chemical duties fall into this category, laminar flow can be said to be one of three types:. Fully developed velocity profile with developing temperature profile i.

The first type is of interest only when considering fluids of low Prandtl number, and this does liquid heat exchanger equations usually exist with normal plate heat exchanger applications. The third is relevant only for fluids such as gases, which have a Prandtl number of about one.

From this correlation it is possible to calculate the film heat transfer coefficient, for laminar flow. This coefficient, combined with that of the metal and the calculated coefficient for the service fluid together with the fouling resistance, are then used to produce the overall coefficient.

Liquid heat exchanger equations is particularly important for laminar flow since these exchangers usually have more than one pass. Although the tube is the best shape of flow conduit for withstanding pressure it is entirely the wrong shap for optimum heat liquid heat exchanger equations performance since it has the smallest surface liquid heat exchanger equations per unit of cross-sectional flow area. Because of the restrictions in the flow area of the ports on plate units it is usually difficult unless a moderate pressure loss is available to produce economic designs when it is necessary to handle large quantities of low- density fluids such as vapors and gases.

A plate heat exchanger is more compact than a tubular and in many instances will occupy less floor liquid heat exchanger equations.

For most materials of construction, sheet metal for plates is less expensive per liquid heat exchanger equations area than tube of the same thickness. When materials other than carbon steel are required, the plate will usually be more economical than the tube for the application. When carbon liquid heat exchanger equations construction is acceptable and when a closer temperature approach is not required, the tubular heat exchanger will often be the most economic solution since the plate heat exchanger is rarely made in carbon steel.

Until recently, applications for plate heat exchangers were restricted by the need for the gaskets to be elastomeric. Liquid heat exchanger equations advances is design have introduced brazed plates and welded plates, thereby widening the liquid heat exchanger equations of applications.

Materials used for pressing the plates have a very smooth surface. Pressure Drop of Condensing Vapor. Fully developed velocity and temperature profiles i.

Comparing Plate and Tubular Exchangers. Ten points of comparison. The effective mean temperature difference will usually be higher with the plate heat exchanger. SWEP uses cookies to make your visit to our web pages as pleasant as possible.

By using our services, we assume that you agree to the use of cookies. Further information on data protection can be found in our privacy policy. The energy flow goes from the warm medium to the cold medium through the heat transfer area of the BPHE. In addition to the size of the heat transfer area, the amount of energy transported also depends on the heat transfer coefficient and the temperature difference between the two sides. This relation is described in the heat transfer equation eq.

Increasing the area of a heat exchanger implies that more energy can be transferred. Hence, increasing the surface area implies higher costs. In BPHEs, the energy is therefore transferred through conduction and convection, and examples of these types of energy transport are shown in In BPHEs, the energy is therefore transferred through conduction and convection, and examples of these types of energy transport are shown in Figure 1. The space between the dotted lines and the wall in Figure 1.

The heat transfer rate within the film is significantly lower than in the bulk liquid, because the temperature gradient decreases dramatically in this area see Figure 1. The reason for the poorer heat transfer is the laminar flow that is always obtained near a plane wall.

Laminar flow does not transfer energy as well as turbulent flow. The overall heat transfer coefficient k describes the total effect of conduction and convection on the energy transfer:. The essence of equation 3 is that a high film coefficient and thermal conductivity and a thin plate lead to a high k-value.

Thermal conductivity is a material-specific constant, and the film coefficient is a measure of how well heat is transferred by a specific fluid. With a higher overall heat transfer coefficient kmore energy can be transferred per heat transfer area.

Because this leads to a more costeffective heat exchanger, it is very important to improve the k-value by all means possible. The temperature difference between the hot and cold media is the driving force in energy transfer. It is therefore important to try to maximize the temperature difference between the hot and cold sides.

Because the temperature difference between the hot and cold sides varies through the heat exchanger, the logarithmic mean temperature difference LMTD is used.

The definition of LMTD is shown in equation Please note that the logarithmic mean temperature difference LMTD may be used only for single-phase calculations see chapter 6. Note that equation 5 is valid only for one-phase heat exchange. The specific heat capacity varies for different liquids and different temperatures. Equations 2 and 5 together describe the preservation of energy inside a BPHE, which is shown in equation 6. This equation, as well as Figure 1. Navigation Refrigerant handbook 1.

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