The most basic rule of heat transfer is that heat always flows from a warmer medium to a colder medium. Heat exchangers are devices to facilitate this heat transfer with the highest possible efficiency. A good heat exchanger is able to transfer energy (heat) from the hot side to the cold side with small thermal losses and high efficiency. Good heat exchangers are typically small pressure vessels with a small pressure drop, and can exploit small temperature differences between two media.
Heat transfer between media is controlled by a few simple but fundamental rules:
There must be a temperature difference to enable energy transfer.
Energy (heat) will always flow from the warmer medium towards the colder medium.
The energy (heat) rejected from the warm medium is equal to the heat absorbed by the cold medium plus losses to the surroundings.
In single-phase heat exchange, there is no phase change in the media. Transfer may be liquid/liquid or gas/liquid or even gas/gas, with no change of phase between the brazed plate heat exchangers inlet and its outlet. An example of such a process is a water-to-water application where the water flow on side 1 changes temperature from 30 to 50 °C and the flow on side 2 changes temperature from 65 to 45 °C, i.e. without a phase change. The most common single-phase applications for brazed plate heat exchangers are water-to-water and oil-to-water. The main purpose of the brazed plate heat exchanger in oil applications is to cool engine oils, hydraulic oils, transmission oils, compressor oils, etc., with water
In two-phase heat exchange, there is a phase change on the cold side, the warm side or both. What happens when a liquid or gas changes phase is described below.
If heat is added to a liquid, the temperature of the liquid will rise until it reaches its boiling point. Adding further heat will not raise the temperature. Instead, it increases the gas content of the liquid, resulting in a two-phase mixture of liquid and gas. The gas generated forms bubbles during boiling. The temperature will not rise until all liquid has been vaporized. When the temperature of the gas becomes higher than the boiling point, the gas is described as superheated. This process is typical of what happens inside an evaporator in a cooling system. The refrigerant enters the evaporator as a liquid and leaves as superheatedvapor.
The opposite occurs in a condenser. First, superheated gas is cooled until it reaches its saturation point, where liquid droplets are formed. When all the gas has been transformed to liquid, the bubble point is reached. Maintaining the same pressure in the vessel while further cooling the liquid leads to a lower temperature, the result being described as a subcooled liquid.
The heat added or lost when the temperature changes without a phase change is called the sensible heat, while the heat added or lost during a phase change is called the latent heat. The latent heat of the phase transition between liquid and gas is many times higher than the sensible heat of the liquid phase. The latent heat that must be added to transform water (100 °C, 1 atm) to steam (100 °C, 1 atm) is 2257 kJ/kg, while the sensible heat added in transforming water (0 °C, 1 atm) to water (100 °C, 1 atm) is only 419 kJ/kg.
This image shows what happens when water in different states is mixed.
The water example illustrates why evaporation and condensation are used commercially to gain or lose, respectively, the large amount of latent heat involved in the transition between the liquid and gas phases.
The ability to transfer heat in liquid and gaseous media depends on the turbulence of the medium. High turbulence is desirable for efficient transfer. Near a plane wall, there is always a film with laminar flow of gas or liquid, depending on the type of medium present (cf. Energy Balance section). The heat transfer in a film with laminar flow is poor, because convectional heat transfer is negligible. However, if higher turbulence can be achieved, the insulating film becomes thinner, convection increases and, consequently, heat can be transported more efficiently, as shown here:
The Reynolds (Re) number is a dimensionless number used to describe the “state” of a fluid (turbulent or laminar flow). The Reynolds number is defined as in equation 1:
(For SWEP heat exchangers, the hydraulic diameter can be approximated as twice the brazed plate heat exchangers pressing depth.)
High turbulence is achieved by increasing the disturbances in a flow. A corrugated surface thus results in a more turbulent flow than a plane surface.
The flow inside a brazed plate heat exchanger can be much more turbulent than the flow inside a shell & tube (S&T) heat exchanger, for example. This is because the plates of the brazed plate heat exchanger are corrugated and folded due to the herringbone pattern, like you see in this image:
By contrast, in an S&T the fluids flow through flat pipes. Full turbulence is reached at approximately Re = 4000 in a tube, but as low as approximately Re = 150 in a brazed plate heat exchanger, which indicates that a smaller flow velocity is needed in a brazed plate heat exchanger than in an S&T.
For a proper comparison between the Reynolds numbers of different passages, their geometries should be exactly the same. This is of course not the case for a comparison between a brazed plate heat exchanger channel and an S&T channel, which have different hydraulic diameters. However, the practical fact remains: fully turbulent flow in a brazed plate heat exchanger is achieved with a lower flow velocity.
In addition to the herringbone pattern on the plates, other parameters that lead to a high Reynolds number include:
- Small cross-sectional channel area
- Low fluid viscosity
At constant pump power, a smaller cross-sectional channel area leads to a higher velocity and better heat transfer. For brazed plate heat exchangers, a smaller cross-sectional area is obtained if a narrower plate is chosen, while lower velocity is obtained when more plates are added. The “cost” of high velocity and small cross-sectional area is an increased pressure drop through the heat exchanger. When a heat exchanger is designed, e.g. in the SWEP Software Package (SSP), the heat exchanger with the calculated pressure drop closest to the maximum allowed should be selected to achieve maximum efficiency.
Viscosity is also an important factor when discussing flow regimes. For example, oil has a higher viscosity than water, and it is therefore more difficult to achieve turbulent oil flows. A medium with a low viscosity might therefore be more useful as a heat conductor.
The energy flow (Q) goes from the warm medium to the cold medium through the heat transfer area (A) of the brazed plate heat exchanger. In addition to the size of the heat transfer area, the amount of energy transported also depends on the heat transfer coefficient (k) and the temperature difference between the two sides (dT). This relation is described in the heat transfer equation (eq. 2):
Increasing the area of a heat exchanger implies that more energy can be transferred. For brazed plate heat exchangers, a larger area can be achieved by increasing the size and/or number of plates, which means more stainless steel and copper brazing. Hence, increasing the surface area implies higher costs.
Heat transfer coefficient (k)
Energy may be transported from a hot fluid to a colder fluid in three ways:
- Conduction – The heat is conducted through solid material or a stationary liquid. In the stainless steel walls of a heat exchanger and in laminar flow (slow-moving) regions, heat is transported only by conduction. The conductivity varies with the physical properties of the medium.
- Convection – Movements of the fluid itself also transport energy. Turbulently flowing media and boiling/condensing fluids are very agitated and will therefore transport energy mostly by convection.
- Radiation – For very hot surfaces (T > 1000 °C), electromagnetic radiation becomes the most important means of heat transport. Radiation does not contribute significantly to heat transfer in brazed plate heat exchangers, due to their considerably lower working temperature.
In brazed plate heat exchangers, energy is therefore transferred by conduction and convection. Examples of these types of energy transport are shown here.
The space between the dotted lines and the wall in the following image is often called the film thickness. The heat transfer rate within the film is significantly lower than in the bulk liquid, because the temperature gradient decreases dramatically in this area .
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. The factor α is always higher for turbulent flows than for laminar flows.
With a higher overall heat transfer coefficient (k), more energy can be transferred per heat transfer area. This makes the heat exchanger more cost-effective, so it is very important to improve the k-value by all means possible.
Temperature difference (dT)
The temperature difference between the hot and cold media is the driving force in energy transfer. A large temperature difference means that a smaller heat transfer area and/or a smaller heat transfer coefficient may be used to achieve the same energy transfer. It is therefore important to try to maximize the temperature difference between the hot and cold sides.
Here you see a single-phase temperature profile through a brazed plate heat exchanger.
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 4:
Note that the logarithmic mean temperature difference (LMTD) may be used only for single-phase calculations.
Conservation of energy
The energy in a liquid flow can be described with the following formula:
Note that equation 5 is valid only for single-phase heat exchange.
The specific heat capacity can be interpreted as the amount of energy required to increase the temperature of 1 kg liquid by 1 °C at constant pressure. The specific heat capacity varies for different liquids and different temperatures.
Equations 2 and 5 together describe the conservation of energy inside a brazed plate heat exchanger, which is shown in equation 6. This equation, as well as the image below indicate that there are no theoretical heat losses to the surroundings in a brazed plate heat exchanger.
The flows inside a heat exchanger can be arranged in various ways to fulfil different purposes. The possibilities are counter-current flow, co-current flow and cross-flow, the first two of which are shown here.
There are different forms of so-called cross-flow heat exchangers in which the flows are more or less mutually perpendicular.
In brazed plate heat exchangers, counter-current flow is by far the most common arrangement. In this case, it is possible for the cooling liquid to leave at a higher temperature than that of the leaving heating liquid. One of the great advantages of counter-current flow is the possibility of extracting a higher proportion of the heat content of the heating fluid. It is important to note that the LMTD value for counter-current flow is much larger than for co-current flow at the same terminal temperature:
The motive for using counter-current flow becomes obvious by referring to equation 6.
A high LMTD implies that a smaller heat transfer area is needed, i.e. the brazed plate heat exchanger can be manufactured with fewer plates. However, co-current flow is also used in brazed plate heat exchangers when the application so demands, e.g. in flooded evaporators. A consequence of a co-current arrangement is that the outlet temperature of the cooling medium can never exceed the outlet temperature of the hotter medium. It is also worth noting that in a co-current arrangement there is a large temperature gradient at the beginning of the evaporator, which makes boiling start earlier:
The thermal length demand is a measure of how “difficult” a certain operational case is to solve for the heat exchanger. The thermal length can be expressed as the number of heat transfer units (NTU or Θ). As shown here, the NTU can be calculated for each side of the heat exchanger:
A brazed plate heat exchanger with a long thermal length can solve cases that are thermodynamically more problematic than can a brazed plate heat exchanger with short thermal length. Different cases are shown in the 3 following diagrams, and the possible solutions for these cases are discussed below.
Operations with close temperature programs (diagram above - "High") demand long brazed plate heat exchanger plates or a multi-pass brazed plate heat exchanger. The purpose of those solutions is to enhance heat transfer through the brazed plate heat exchanger.
Another solution is to design the brazed plate heat exchanger with a high-theta pattern (see image of the plates), which will increase the turbulence of the fluid and thus increase the heat transfer efficiency.
An easier case, i.e. with small temperature changes on each side (diagram above- "Low"), will most probably be solved with a short single-pass brazed plate heat exchanger. The plate pattern for easy jobs may very well be a low-theta pattern (see image of the plates), which leads to a low pressure-drop through the heat exchanger.
Asymmetric operation (diagram above - "High and Low") occurs when the temperature change on one side of the brazed plate heat exchanger is much larger than on the other. The solution for this is a two-pass over one-pass brazed plate heat exchanger, as shown in the below image, or an asymmetric brazed plate heat exchanger. An asymmetric brazed plate heat exchanger uses a design with a mixture of high-theta and low-theta plates.
When a flow is disturbed, a pressure drop (ΔP) is created, i.e. the flow pressure at the beginning of a passage is higher than at its end. Pressure drop is a phenomenon with both positive and negative consequences for the heat transfer process.
Pressure drop utilization
Excessive pressure drop is of course negative, because the flow through the brazed plate heat exchanger requires a lot of pump power. High pump power can be achieved only with large pumps, which demand a large amount of electricity and thus make the operation expensive.
The positive result of pressure drop is the greater turbulence. Turbulence is desirable in heat exchangers, because it improves heat transfer (cf. Flow Regimes section).
There are some proportional (~) relations that are useful to keep in mind when designing a brazed plate heat exchanger:
Relation  tells that decreasing the area, A, by reducing the number of plates or channels, increases the flow velocity by the same factor. The interpretation of relation  is that if the velocity, for example, is doubled, the pressure drop is increased four times. The interpretation of relation  is that if the pressure drop, for example, is increased four times, the heat transfer coefficient becomes 41/3 = 1.26 times higher than the original value, i.e. a 26% increase. Note that these proportionalities only apply to fully turbulent flow.
Pressure drop relations
The pressure drop in a CBE channel mainly depends on different variables as shown in the following table:
The plate pattern is one of the tools the designer can use to increase or decrease the performance and the pressure drop through the brazed plate heat exchanger. A high-theta pattern leads to bigger pressure drop than a low-theta pattern. In practice, the high-theta pattern is much more common due to the greater turbulence it creates. The difference between high-theta and low-theta patterns is visualized here: