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9410036300Heat exchanger Design
TOC o “1-3” h z u Introduction PAGEREF _Toc530514343 h 2SWOT Analysis PAGEREF _Toc530514344 h 2Classification of Heat Exchanger by Construction Type PAGEREF _Toc530514345 h 7Methodology / Deign Steps PAGEREF _Toc530514346 h 10Assumptions PAGEREF _Toc530514347 h 11Equations and Calculations PAGEREF _Toc530514348 h 12Result and Discussion PAGEREF _Toc530514349 h 16Takeaways and Learning PAGEREF _Toc530514350 h 17Nomenclature PAGEREF _Toc530514351 h 18Reference PAGEREF _Toc530514352 h 20
Thermodynamic theory is at the core of heat exchanger design; it incorporates a range of necessary fluid and solid parameters, flow dynamics and required heat duties to achieve specific temperature changes. The fundamental background of heat-transfer theory can be found in Coulson et al. (1999) which discusses energy relationships and heat transfer in the chemical engineering industry. Many of the basic laws of thermodynamic behavior can be derived from this source to provide additional contextual background to heat exchanger principles. This design process uses the design procedure outlines in Sinnott (2005) for a shell and tube heat exchanger. The fundamental features of a shell and tube heat exchanger can be seen in Figure 1. A tube side fluid enters the heat exchanger through an inlet on the heat exchanger shell. Its flow is directed through the heat exchanged by baffles, allowing axial and perpendicular flow across the tubes allowing for heat transfer. The baffles are also responsible for holding the tube bundle together and in the correct shape. Additional shell passes can also be achieved by axial baffles direction shell side fluid flow. The tube side fluid enters the unit through a front-end stationary head. This head piece is mounted to the shell and to plant piping. A rear end head piece is also attached, although its design can also be fixed (hence no allowing the tube bundle to be removed) or floating. The number of tube side passes is determined by the arrangement of the tube bundle and determined the shells diameter. TEMA nomenclature is used to describe the head and shell types of heat exchangers. This same nomenclature is used in this report and refences can be found in Sinnott (2005).
SWOT analysis of heat exchanger can summaries the key takeaways behind the selection of the heat exchanger.
Table 1: SWOT analysis
Fulfills the criteria and constraints given
Good heating and cooling capacity
Fully completed heat exchanger design Weaknesses
Is not optimized completely and extra pressure drop and low residence time
Show linear velocities
Based on assumptions that thermal conductivity along the length remain same
Using Aspen Plus or Aspen HYSYS the exact thermal and transport properties can be calculated
Conducting more research related to thermal conductivities of the wall
Pressure drop calculations can be carried out using different process simulators for accurate rigorous calculations Threats
No simulation was conducted to improve the design and rating performance
Minor error in calculations are possible
Fig. 1, Typical Shell and Tube Heat Exchanger (Shah, 1981)
According to the TEMA design and through evaluation it was found that the most appropriate design for the heat exchanger was AFT heat exchanger with a pull-through floating head will be used as it was the best for cleaning and it is the most common configuration for chemical processes (Mukherjee, 1998).
The recommended design is to have two shell passes and four tube passes as outlined in graphs in (Sinnot, 2013). Whilst this report has been extensive in calculating the various design specifications found in the heat exchanger, it is advised that further study take place whether it be simulating or removing assumptions as these will lead to a more valid and reliable heat exchanger. The principle parameter of the calculations is the overall heat transfer coefficient of the system, which relies on shell and tube side fluid properties and heat exchanger sizing and materials. This coefficient is used to size the heat exchanger and perform calculations to determine the required shell and tube parameters. Although since an approximated overall heat transfer coefficient is required to start the design process, an iterative methodology is used through the design until the calculated heat transfer coefficient reached an acceptable deviation from the assumed heat transfer coefficient.
Fig. 2 Construction based heat exchangers
Fig. 3 Parts of different heat exchangers TEMA
Classification of Heat Exchanger by Construction TypeHeat exchangers also can be classified according to their construction features. For example, there are tubular, plate, plate-fin, tube-fin, and regenerative exchangers. An important performance factor for all heat exchangers is the amount of heat transfer surface area within the volume of the heat exchanger. This is called its compactness factor and is measured in square meters per cubic meter.
Tubular exchangers are widely used, and they are manufactured in many sizes, flow arrangements, and types. They can accommodate a wide range of operating pressures and temperatures. The ease of manufacturing and their relatively low cost have been the principal reason for their widespread use in engineering applications. A commonly used design, called the shell-and-tube exchanger, consists of round tubes mounted on a cylindrical shell with their axes parallel to that of the shell. The principle components of this type of heat exchanger are the tube bundle, shell, front and rear end headers, and baffles. The baffles are used to support the tubes, to direct the fluid flow approximately normal to the tubes, and to increase the turbulence of the shell fluid. There are various types of baffles, and the choice of baffle type, spacing, and geometry depends on the flow rate allowable shell-side pressure drop, tube support requirement, and the flow-induced vibrations. Many variations of shell-and-tube exchanger are available; the differences lie in the arrangement of flow configurations and in the details of construction.
The character of the fluids may be liquid-to-liquid, liquid-to-gas, or gas-to-gas. Liquid-to-liquid exchangers have the most common applications. Both fluids are pumped through the exchangers; hence, the heat transfer on both the tube side and the shell side is by forced convection. Since the heat transfer coefficient is high with the liquid flow, generally there is no need to use fins.
Some basic types of baffles has been shown in the figure.
Fig. 4, Classification of heat exchanger
Fig. 5 Baffles types
Methodology / Deign StepsHere are the steps for rating of Heat Exchanger
Perform energy balance
Select heating and cooling media
Calculate the steam flowrate
Determine or extract physical and transport properties of fluid
Allocate heating and cooling fluids side
Decide the heat exchanger type
Calculate the LMTD
Guess the value of overall heat transfer coefficient
Estimate the provisional area requirement
Estimate the actual area from the given information
Calculate individual shell and tube side heat transfer coefficients
Calculate the overall coefficient
Calculate heat transfer rate
Keep on iterating to reach exact solution
AssumptionsNegligible heat loss to the surroundings.
Negligible kinetic and potential energy changes.
Steady state operation
Velocity of both fluids entering and leaving the heat exchanger are same over the cross section
Counter current heat exchanger is assumed
There are no thermal sink or heat source attached to the heat exchanger
Thermal resistance of wall remains same over the whole length of tube
Saturated steam is assumed to be a heating media
Saturated liquid is leaving the heat exchanger (condensing steam)
Individual and overall heat transfer coefficients remains same along the length
Ratio of viscosity of fluid and viscosity at the wall is assumed to be 1
No extended surfaces are being used
Fluid flow is uniformly distributed
Specific heat of fluids remains same throughout the heat exchanger
Equations and Calculations:
Basis data is as follows:
Compute Energy balance
Using the below equation, we can calculate the heat transfer for the heat exchanger;
Q = 12539442.08 kJhrSelect heating medium (Given)
Saturated steam as a heating media at 300 kPa
Compute utility flowrate
Steam flowrate = Q / (Lambda )
Steam flowrate = 5794.57 kg/hr
Compute physical properties
Stream ID Water_In (1) Water_Out (2) Steam_In (3) Steam_Out (4)
T ? 10 70 134 134
Mass Heat Capacity kJ/kg-C 4.1798 4.1798 2.199 2.199
Lambda kJ/kg 2164 2164 2164 2164
Mass Density kg/m3 992.0203 992.0203 1.6509 1.6509
Viscosity cP 0.6514 0.6514 0.0133 0.0133
Thermal Conductivity W/m-K 0.6315 0.6315 0.0272 0.0272
Allocate fluids side
Condensing steam is allocated in the shell side due to volume change and water is in the tube side.
Decide the exchanger type
The most used shell and tube type is chosen.
LMTD = 30.85 C
Select value of overall coefficient, U
Assumed value of overall heat transfer coefficient is 800 W/m2-C
Estimate the tentative area requirement
Area = 508.07 m2
Estimate the actual area (based on given geometry)
Actual Area = 29.48 m2
Calculate the shell and tube side heat transfer coefficient
Re = 5360; Pr = 1.08
ho = 104 W/m2-C
Calculate the overall coefficient
Uo = 8000 W/m2-C
Calculate heat transfer rate
Pressure drop for the tube side
f = 0.00708
Pressure Drop = 6.03 psia
Pressure drop for the shell side
Pressure drop = 4.65 psia
Fig. 6: Counter-Current Heat Exchanger
Result and DiscussionThe result indicated that the heat exchanger is under-designed due to which it is impractical to use such heat exchangers. Usually, heat exchangers are overdesigned to incorporate leakage, losses, and other factors. This heat exchanger can be used to process part of flowrate but to meet the heat exchange requirement, it is required to increase the area of heat transfer. Other way is to install a parallel heat exchanger to meet the requirement.
Takeaways and LearningThis problem helped us to apply the heat transfer fundamentals to deal with a pragmatic problem. Moreover, this problem ease to develop deep understand of heat exchanger and to explore different types of heat exchangers along with application in real life. It facilitated to incorporate different concepts to analyze the practical problem and imply some valid assumption to made calculations simpler to build a solid base for further improvements.
NomenclatureSymbol Meaning Units
? Density kg/m3
µ Viscosity ?T Change in temperature ?
?TlmLog mean temperature difference ?
?Tm Mean temperature difference ?
kw Wall thermal conductivity W/ m °C
kf Fluid thermal conductivity W/ m °C
Q Heat Duty kj/hr
U Overall heat transfer coefficient W/m2-C
A Area m2
Nt Number of tubes ?? Mass flow rate kg/hr
Cp Heat capacity kJ/kg-?
ut Tube side velocity m/s
us Shell side velocity m/s
jh Tube side heat transfer factor jn Shell side heat transfer factor ?Pt Tube side pressure drop kPa
Re Reynolds number PrPrandlt number Nu Nusselt number do Outer tube diameter mm
di Inner tube diameter mm
de Equivalent shell diameter mm
L Tube length mm
Db Bundle diameter mm
Ds Shell diameter mm
lb Baffle spacing mm
As Shell side cross section area m2
hi Tube side heat transfer coefficient W/m2-C
ho Shell side heat transfer coefficient W/m2-C
hid Tube side fouling factor hod Shell side fouling factor jfFriction factor Np Number of tube side passes ?Ps Shell side pressure drop psia
Mueller, A. C. 1973. “Heat exchangers.” In Handbook of Heat Transfer . McGraw-Hill. Mukherjee, R. 1998. “Effectively Design Shell and Tube Heat Exchangers.” Chemical Engineering
Polar, J. P. 1961. “A Guide to Corrosion Resistence-304, 316, 317, ’20’ and Ni-O-Nel.” Climax Molybdenum Company.
Sinnott, R. K. 2005. Chemical Engineering Design, 4th Edition. Oxford: Butterworth-Heinemann.
Tinker, T. 1951. “Proceedings of the general discussion on heat transfer.” In Shell-side characteristics of shell and tube heat exchangers, 89. London: Institution of Mechanical Engineers.
Coulson, J. M., J. F. Richardson, J. Backhurst, and J. H. Harker. 1999. Chemical Engineering (6th Ed, Vol 1). Oxford : Butterworth-Heinemann.
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