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Heat Exchangers: Design ConsiderationsPowerPoint Presentation

Heat Exchangers: Design Considerations

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### Heat Exchangers:Design Considerations

Counterflow

Heat Exchanger Types

TypesHeat exchangers are ubiquitous to energy conversion and utilization. They involve heat exchange between two fluids separated by a solid and encompass a wide range of flow configurations.

- Concentric-Tube Heat Exchangers

- Simplest configuration.

- Superior performance associated with counter flow.

Unmixed

Unfinned-One Fluid Mixed

the Other Unmixed

Types (cont.)- Cross-flow Heat Exchangers

- For cross-flow over the tubes, fluid motion, and hence mixing, in the transverse
direction (y) is prevented for the finned tubes, but occurs for the unfinned condition.

- Heat exchanger performance is influenced by mixing.

One Shell Pass and One Tube Pass

Types (cont.)- Shell-and-Tube Heat Exchangers

- Baffles are used to establish a cross-flow and to induce turbulent mixing of the
shell-side fluid, both of which enhance convection.

- The number of tube and shell passes may be varied, e.g.:

One Shell Pass,

Two Tube Passes

Two Shell Passes,

Four Tube Passes

Types (cont.)

- Compact Heat Exchangers

- Widely used to achieve large heat rates per unit volume, particularly when
one or both fluids is a gas.

- Characterized by large heat transfer surface areas per unit volume, small
flow passages, and laminar flow.

(a) Fin-tube (flat tubes, continuous plate fins)

(b) Fin-tube (circular tubes, continuous plate fins)

(c) Fin-tube (circular tubes, circular fins)

(d) Plate-fin (single pass)

(e) Plate-fin (multipass)

Overall Heat Transfer Coefficient

Overall Coefficient1 / U A = 1 / h1 A1 + dxw / k A + 1 / h2 A2

where

U = the overall heat transfer coefficient (W/m2K)

A = the contact area for each fluid side (m2)

k = the thermal conductivity of the material (W/mK)

h = the individual convection heat transfer coefficient for each fluid (W/m2K)

dxw = the wall thickness (m)

Overall Coefficient

- where
- kw - Thermal Conductivity of Fluid
- DH - Hydraulic Diameter
- Nu - Nusselt Number

- where:
- ν : kinematic viscosity, ν = μ / ρ, (SI units : m2/s)
- α : thermal diffusivity, α = k / (ρcp), (SI units : m2/s)
- μ : dynamic viscosity, (SI units : Pa s)
- k: thermal conductivity, (SI units : W/(m K) )
- cp : specific heat, (SI units : J/(kg K) )
- ρ : density, (SI units : kg/m3 ).
- V : Fluid velocity (SI units m/s)
- L : Pipe Internal Diameter (SI units m)

n = 0.4 for heating (wall hotter than the bulk fluid) and 0.33 for cooling (wall cooler than the bulk fluid)

Evaluation of depends on the heat exchanger type.

A Methodology for Heat Exchanger

Design Calculations

- The Log Mean Temperature Difference (LMTD) Method -

LMTD Method- A form of Newton’s Law of Cooling may be applied to heat exchangers by
- using a log-mean value of the temperature difference between the two fluids:

LMTD Method (cont.)

- Parallel-Flow Heat Exchanger:

- Note that Tc,ocan not exceed Th,ofor a PF HX, but can do so for a CF HX.

- For equivalent values of UA and inlet temperatures,

- Shell-and-Tube and Cross-Flow Heat Exchangers:

Energy Balance

- Application to the hot (h) and cold (c) fluids:

- Assume negligible heat transfer between the exchanger and its surroundings
- and negligible potential and kinetic energy changes for each fluid.

- Assuming no l/v phase change and constant specific heats,

- Case (a): Ch>>Cc or h is a condensing vapor

- Case (b): Cc>>Ch or c is an evaporating liquid

- Negligible or no change in

- Negligible or no change in

Special Operating Conditions

Special Conditions- Case (c): Ch=Cc.

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