This document compares the design of a shell and tube heat exchanger with baffles using four different methods: 1) Kern's theoretical method, 2) ASPEN simulation software, 3) HTRI simulation software, and 4) SOLIDWORKS simulation software. The same input parameters were used to design a shell and tube heat exchanger with single segmental baffles in each method. The results from all four methods for shell side pressure drop and heat transfer coefficient were found to be in close agreement. The theoretical Kern method design results closely matched the simulation software results, showing proven theoretical methods can accurately model shell and tube heat exchanger performance.
This presentation was created to provide a quick refresher to single-phase fluid flow line sizing. The content of this presentation was obtained from various literature (handbooks and website).
Please provide your comments
This design project aims to propose a plate type heat exchanger that can meet given heat duty and find the number of plates required. Plate type heat exchanger uses metal plates to transfer heat between two fluids. Starting point of this design is to define given properties
This document compares different methods for designing a shell and tube heat exchanger, including a manual design, HTRI software, and Aspen Exchanger Design and Rating (EDR). It first provides background on heat exchangers and describes the constraints that must be met in a heat exchanger design, including thermal and hydraulic evaluations. It then presents an example design case and shows the initial geometry selection. Finally, it discusses using HTRI and Aspen EDR software for simulation, rating, and designing shell and tube heat exchangers, noting both programs iterate to find a design meeting constraints.
Design Considerations for Plate Type Heat ExchangerArun Sarasan
A plate type heat exchanger consists of corrugated metal plates clamped together in a frame. Fluids flow between the plates, which have a high surface area and induce turbulence, allowing for efficient heat transfer. Key advantages are compact size, ability to handle low flow rates, and the option to perform multiple duties with one unit. Design involves selecting the number and dimensions of plates based on flow rates, properties of the fluids, and heat transfer correlations or manufacturer charts.
This document discusses the advantages of considering compact heat exchangers like plate-and-frame exchangers early in the process design stage. Plate-and-frame exchangers can be significantly smaller than traditional shell-and-tube exchangers while meeting the same heat transfer needs. Specifying design requirements without considering the characteristics of different exchanger types can lead to oversized and more expensive designs. Charts are provided to help estimate the required area of plate-and-frame exchangers for preliminary sizing.
Calculation of Maximum Flow of Natural Gas through a Pipeline using Dynamic S...Waqas Manzoor
This process report highlights the significance of Dynamic Simulation in Aspen HYSYS for calculation of maximum flow rate of natural gas through a pipeline supplying gas to domestic consumers. The gas pressure at the outlet of pipeline has been considered to be equal to 0 psig in order to calculate the maximum possible gas flow rate. Moreover, the reduction of gas pressure at upstream of gas regulating station due to increased downstream pressure has also been calculated using this simulation.
This document summarizes the key steps in designing liquid pipelines according to API 14E standards. It discusses important considerations like ensuring velocity is below 15 feet per second to avoid erosion and pressure drop is below 1 psi per 100 feet. The document then provides an example calculation for sizing a water pipeline using schedule 40 and 80 steel pipes. It determines that an 8-inch schedule 40 pipe meets both velocity and pressure drop requirements and has the lowest annual operating costs.
This document provides an overview of using HTRI software to perform thermal design of heat exchangers. It discusses specifying the geometry, process conditions, and fluid properties required for rating, designing, or simulating shell and tube heat exchangers. Key aspects covered include baffle types, temperature profiles, mean temperature differences, and outputs such as duty, heat transfer area, and pressure drop. The goal is to demonstrate the inputs and calculations used in HTRI to analyze heat exchanger performance.
This presentation was created to provide a quick refresher to single-phase fluid flow line sizing. The content of this presentation was obtained from various literature (handbooks and website).
Please provide your comments
This design project aims to propose a plate type heat exchanger that can meet given heat duty and find the number of plates required. Plate type heat exchanger uses metal plates to transfer heat between two fluids. Starting point of this design is to define given properties
This document compares different methods for designing a shell and tube heat exchanger, including a manual design, HTRI software, and Aspen Exchanger Design and Rating (EDR). It first provides background on heat exchangers and describes the constraints that must be met in a heat exchanger design, including thermal and hydraulic evaluations. It then presents an example design case and shows the initial geometry selection. Finally, it discusses using HTRI and Aspen EDR software for simulation, rating, and designing shell and tube heat exchangers, noting both programs iterate to find a design meeting constraints.
Design Considerations for Plate Type Heat ExchangerArun Sarasan
A plate type heat exchanger consists of corrugated metal plates clamped together in a frame. Fluids flow between the plates, which have a high surface area and induce turbulence, allowing for efficient heat transfer. Key advantages are compact size, ability to handle low flow rates, and the option to perform multiple duties with one unit. Design involves selecting the number and dimensions of plates based on flow rates, properties of the fluids, and heat transfer correlations or manufacturer charts.
This document discusses the advantages of considering compact heat exchangers like plate-and-frame exchangers early in the process design stage. Plate-and-frame exchangers can be significantly smaller than traditional shell-and-tube exchangers while meeting the same heat transfer needs. Specifying design requirements without considering the characteristics of different exchanger types can lead to oversized and more expensive designs. Charts are provided to help estimate the required area of plate-and-frame exchangers for preliminary sizing.
Calculation of Maximum Flow of Natural Gas through a Pipeline using Dynamic S...Waqas Manzoor
This process report highlights the significance of Dynamic Simulation in Aspen HYSYS for calculation of maximum flow rate of natural gas through a pipeline supplying gas to domestic consumers. The gas pressure at the outlet of pipeline has been considered to be equal to 0 psig in order to calculate the maximum possible gas flow rate. Moreover, the reduction of gas pressure at upstream of gas regulating station due to increased downstream pressure has also been calculated using this simulation.
This document summarizes the key steps in designing liquid pipelines according to API 14E standards. It discusses important considerations like ensuring velocity is below 15 feet per second to avoid erosion and pressure drop is below 1 psi per 100 feet. The document then provides an example calculation for sizing a water pipeline using schedule 40 and 80 steel pipes. It determines that an 8-inch schedule 40 pipe meets both velocity and pressure drop requirements and has the lowest annual operating costs.
This document provides an overview of using HTRI software to perform thermal design of heat exchangers. It discusses specifying the geometry, process conditions, and fluid properties required for rating, designing, or simulating shell and tube heat exchangers. Key aspects covered include baffle types, temperature profiles, mean temperature differences, and outputs such as duty, heat transfer area, and pressure drop. The goal is to demonstrate the inputs and calculations used in HTRI to analyze heat exchanger performance.
Impact of No. of Pipe Segments on the flow rate calculated by Pipe Model (Pag...Waqas Manzoor
A dynamic simulation was performed in Aspen HYSYS to calculate the maximum flow rate of natural gas through a 6-inch SCH 80 pipeline 12 km in length. The simulation showed that the pipeline could transport up to 4.01 MMSCFD of gas at a downstream pressure of 100 psig. However, the actual maximum flow rate would be lower due to pipe roughness and aging effects. It was determined that the pipeline would be unable to meet forecasted demand of 5-6 MMSCFD in 2015. A steady-state simulation could not calculate flow rates after specifying the total pressure drop across the pipeline.
This document provides an overview of a gasketed plate heat exchanger. It describes the construction of a plate heat exchanger using metal plates and gaskets to transfer heat between two fluids without mixing. It discusses key design considerations like flow pattern, plate materials, mean flow gap, heat transfer coefficient, pressure drop, and heat transfer area. The document highlights advantages of plate heat exchangers like minimizing leakage risk, flexibility in design, efficient heat transfer due to turbulence, compact size, and low fouling characteristics.
This document presents a rule-of-thumb design procedure for wet cooling towers that can be used for power plant cycle optimization. It begins with defining the design problem and specifying inlet/outlet water temperatures and ambient wet-bulb temperature. It then provides methods to calculate the outlet air temperature, tower characteristic, loading factor, and other key parameters. These include using the average of inlet/outlet water temperatures to approximate outlet air temperature, graphically integrating the Merkel equation to determine tower characteristic, and using graphs to determine the optimum loading factor based on design conditions. The goal is to provide simplified methods for estimating cooling tower dimensions, performance, costs and other details needed for power plant analysis without requiring detailed iterative design calculations.
PROCESS STORAGE TANK LAH & LAHH LEVEL CALCULATIONVijay Sarathy
The document contains parameters for a process storage tank including a diameter of 14 feet, height of 18 feet, normal liquid level of 6 feet, and pump inflow of 250 USGPM. It details calculations for the liquid alarm high-high level of 14.74 feet based on filling the tank from the overfill level to that point within 15 minutes, and liquid alarm high level of 8.23 feet calculated from filling within 45 minutes.
A heat exchanger transfers heat between two fluids through conduction. It can transfer heat between fluids that never mix by using a solid wall, or between directly contacted fluids. Heat exchangers are widely used in applications like HVAC, power plants, refineries, and manufacturing. They are classified based on construction and flow configuration, with shell-and-tube and plate heat exchangers being most common. Proper design considers factors like heat transfer rate, pressure drop, fouling, and effectiveness.
This presentation describes the considerations involved in selecting the shell and tube exchanger according to TEMA Designations. Also, it helps to identify whether fluid should be sent tube side or shell side
This document discusses the process design of shell and tube heat exchangers. It begins by classifying heat exchangers and describing different types of shell and tube heat exchangers such as fixed tube sheet, removable tube bundle, floating head, and U-tube designs. The document then discusses various thermal design considerations for shell and tube heat exchangers, including selections for the shell, tube materials and dimensions, tube layout and count, baffles, and fouling considerations. It provides process design procedures and an example problem for shell and tube heat exchanger design.
1. The document is a seminar report submitted for a master's degree in mechanical engineering focusing on heat transfer augmentation for fluid flowing through pipes using computational fluid dynamics (CFD).
2. It analyzes factors that affect heat transfer enhancement techniques using roughened pipes, such as the ratio of pitch to pipe diameter and Reynolds numbers.
3. The results showed that increasing the Reynolds number and decreasing the ratio of pitch to pipe length leads to an increase in the heat transfer coefficient and thermo-hydraulic performance.
The document repeatedly states "Information Handling Services, 2000" with no other details provided. It consists solely of this phrase printed over 100 times, suggesting it relates to information handling services in the year 2000, but without any other context to further summarize.
Mechanical Design of a Heat Exchanger.pdfsarhanfarook
The document describes the design of a heat exchanger to heat distilled fatty acid from 55°C to 85°C using steam as the hot fluid. Key aspects of the design include:
- Using 278 stainless steel tubes in a triangular pitch arrangement with a total heat transfer area of 41.36 m2
- The hot steam enters at 200°C and exits at 138.99°C, with a dry fraction of 0.865988059
- Dimensions of the shell, tubesheet, baffles and other components are calculated and specified
- The design is compared to an existing heat exchanger, with some differences in parameters like number of tubes and tube layout
The document outlines 11 steps for sizing a pipe line to carry water at 100 m3/hr, including: calculating the internal pipe diameter, selecting the nearest available pipe size, determining the fluid velocity, calculating the Reynolds number and friction factor, determining equivalent length, calculating pressure drop, and comparing the available and calculated pressure drops. The goal is to select a pipe size that ensures the available pressure drop is greater than the calculated pressure drop.
Parts of shell and tube heat exchanger
Shell
Shell Side Pass Partition Plate
Baffles
Tube
Tube Side Pass Partition Plate
Tie Rods
Spacers
Tube Sheet
Expansion Joint
Design Calculations of Venting in Atmospheric and Low-pressure Storage Tanks ...Pradeep Dhondi
hi
i have made an excel base software base on API st.2000 "Design Calculations of Venting in Atmospheric and Low-pressure Storage Tanks" to make calculation easy and accurate , i have take many case study and verified my software got positive result.
if you think you need this software for design the vent , please go to "rajiravi.ml" website there you can find complete information base on software and information based on contact etc...
This document provides an overview of the functional design of two types of heat exchangers: shell and tube heat exchangers and plate heat exchangers. It discusses the key components, design considerations, and step-by-step design procedures for shell and tube heat exchangers. These include determining the heat transfer area, number of tubes, tube dimensions, baffle design, and accounting for pressure drops and fouling factors. It also introduces plate heat exchangers and discusses their mechanical characteristics and design methods at a high level.
A heat exchanger transfers heat between two fluids. There are various types including shell and tube, plate and frame, and air cooled. A shell and tube heat exchanger consists of tubes, a shell, baffles, and nozzle inlets and outlets. Proper design of the baffle cut, spacing, and orientation is important for efficient heat transfer and to prevent bypass and leakage streams from reducing effectiveness. Sealing strips are also used to block leakage paths and improve performance.
Pressure Safety Valve Sizing - API 520/521/526Vijay Sarathy
No chemical process facility is immune to the risk of overpressure to avoid dictating the necessity for overpressure protection. For every situation that demands safe containment of process gas, it becomes an obligation for engineers to equally provide pressure relieving and flaring provisions wherever necessary. The levels of protection are hierarchical, starting with designing an inherently safe process to avoid overpressure followed by providing alarms for operators to intervene and Emergency Shutdown provisions through ESD and SIL rated instrumentation. Beyond these design and instrument based protection measures, the philosophy of containment and abatement steps such as pressure relieving devices, flares, physical dikes and Emergency Response Services is employed
Data Ware House System in Cloud EnvironmentIJERA Editor
To reduce Cost of data ware house deployment , virtualization is very Important. virtualization can reduce Cost
and as well as tremendous Pressure of managing devices, Storages Servers, application models & main Power.
In current time, data were house is more effective and important Concepts that can make much impact in
decision support system in Organization. Data ware house system takes large amount of time, cost and efforts
then data base system to Deploy and develop in house system for an Organization . Due to this reason that,
people now think about cloud computing as a solution of the problem instead of implementing their own data
were house system . In this paper, how cloud environment can be established as an alternative of data ware
house system. It will given the some knowledge about better environment choice for the organizational need.
Organizational Data were house and EC2 (elastic cloud computing ) are discussed with different parameter like
ROI, Security, scalability, robustness of data, maintained of system etc
Structural Design and Rehabilitation of Reinforced Concrete StructureIJERA Editor
Effective rehabilitation scheme for failed structure demands methodical analysis of various
causes of failure and intended service loads and other functional details, The actual study under deliberation is
the best example of rehabilitation Structural element – Basement RCC raft, failed to sustain uplift due to ground
water table. This paper dealt with the rehabilitation of basement RCC raft foundation considering various design
aspects like uplift due to ground water table, sub-soil properties and restriction on depth of raft to suffice
available headroom for intended use.
Impact of No. of Pipe Segments on the flow rate calculated by Pipe Model (Pag...Waqas Manzoor
A dynamic simulation was performed in Aspen HYSYS to calculate the maximum flow rate of natural gas through a 6-inch SCH 80 pipeline 12 km in length. The simulation showed that the pipeline could transport up to 4.01 MMSCFD of gas at a downstream pressure of 100 psig. However, the actual maximum flow rate would be lower due to pipe roughness and aging effects. It was determined that the pipeline would be unable to meet forecasted demand of 5-6 MMSCFD in 2015. A steady-state simulation could not calculate flow rates after specifying the total pressure drop across the pipeline.
This document provides an overview of a gasketed plate heat exchanger. It describes the construction of a plate heat exchanger using metal plates and gaskets to transfer heat between two fluids without mixing. It discusses key design considerations like flow pattern, plate materials, mean flow gap, heat transfer coefficient, pressure drop, and heat transfer area. The document highlights advantages of plate heat exchangers like minimizing leakage risk, flexibility in design, efficient heat transfer due to turbulence, compact size, and low fouling characteristics.
This document presents a rule-of-thumb design procedure for wet cooling towers that can be used for power plant cycle optimization. It begins with defining the design problem and specifying inlet/outlet water temperatures and ambient wet-bulb temperature. It then provides methods to calculate the outlet air temperature, tower characteristic, loading factor, and other key parameters. These include using the average of inlet/outlet water temperatures to approximate outlet air temperature, graphically integrating the Merkel equation to determine tower characteristic, and using graphs to determine the optimum loading factor based on design conditions. The goal is to provide simplified methods for estimating cooling tower dimensions, performance, costs and other details needed for power plant analysis without requiring detailed iterative design calculations.
PROCESS STORAGE TANK LAH & LAHH LEVEL CALCULATIONVijay Sarathy
The document contains parameters for a process storage tank including a diameter of 14 feet, height of 18 feet, normal liquid level of 6 feet, and pump inflow of 250 USGPM. It details calculations for the liquid alarm high-high level of 14.74 feet based on filling the tank from the overfill level to that point within 15 minutes, and liquid alarm high level of 8.23 feet calculated from filling within 45 minutes.
A heat exchanger transfers heat between two fluids through conduction. It can transfer heat between fluids that never mix by using a solid wall, or between directly contacted fluids. Heat exchangers are widely used in applications like HVAC, power plants, refineries, and manufacturing. They are classified based on construction and flow configuration, with shell-and-tube and plate heat exchangers being most common. Proper design considers factors like heat transfer rate, pressure drop, fouling, and effectiveness.
This presentation describes the considerations involved in selecting the shell and tube exchanger according to TEMA Designations. Also, it helps to identify whether fluid should be sent tube side or shell side
This document discusses the process design of shell and tube heat exchangers. It begins by classifying heat exchangers and describing different types of shell and tube heat exchangers such as fixed tube sheet, removable tube bundle, floating head, and U-tube designs. The document then discusses various thermal design considerations for shell and tube heat exchangers, including selections for the shell, tube materials and dimensions, tube layout and count, baffles, and fouling considerations. It provides process design procedures and an example problem for shell and tube heat exchanger design.
1. The document is a seminar report submitted for a master's degree in mechanical engineering focusing on heat transfer augmentation for fluid flowing through pipes using computational fluid dynamics (CFD).
2. It analyzes factors that affect heat transfer enhancement techniques using roughened pipes, such as the ratio of pitch to pipe diameter and Reynolds numbers.
3. The results showed that increasing the Reynolds number and decreasing the ratio of pitch to pipe length leads to an increase in the heat transfer coefficient and thermo-hydraulic performance.
The document repeatedly states "Information Handling Services, 2000" with no other details provided. It consists solely of this phrase printed over 100 times, suggesting it relates to information handling services in the year 2000, but without any other context to further summarize.
Mechanical Design of a Heat Exchanger.pdfsarhanfarook
The document describes the design of a heat exchanger to heat distilled fatty acid from 55°C to 85°C using steam as the hot fluid. Key aspects of the design include:
- Using 278 stainless steel tubes in a triangular pitch arrangement with a total heat transfer area of 41.36 m2
- The hot steam enters at 200°C and exits at 138.99°C, with a dry fraction of 0.865988059
- Dimensions of the shell, tubesheet, baffles and other components are calculated and specified
- The design is compared to an existing heat exchanger, with some differences in parameters like number of tubes and tube layout
The document outlines 11 steps for sizing a pipe line to carry water at 100 m3/hr, including: calculating the internal pipe diameter, selecting the nearest available pipe size, determining the fluid velocity, calculating the Reynolds number and friction factor, determining equivalent length, calculating pressure drop, and comparing the available and calculated pressure drops. The goal is to select a pipe size that ensures the available pressure drop is greater than the calculated pressure drop.
Parts of shell and tube heat exchanger
Shell
Shell Side Pass Partition Plate
Baffles
Tube
Tube Side Pass Partition Plate
Tie Rods
Spacers
Tube Sheet
Expansion Joint
Design Calculations of Venting in Atmospheric and Low-pressure Storage Tanks ...Pradeep Dhondi
hi
i have made an excel base software base on API st.2000 "Design Calculations of Venting in Atmospheric and Low-pressure Storage Tanks" to make calculation easy and accurate , i have take many case study and verified my software got positive result.
if you think you need this software for design the vent , please go to "rajiravi.ml" website there you can find complete information base on software and information based on contact etc...
This document provides an overview of the functional design of two types of heat exchangers: shell and tube heat exchangers and plate heat exchangers. It discusses the key components, design considerations, and step-by-step design procedures for shell and tube heat exchangers. These include determining the heat transfer area, number of tubes, tube dimensions, baffle design, and accounting for pressure drops and fouling factors. It also introduces plate heat exchangers and discusses their mechanical characteristics and design methods at a high level.
A heat exchanger transfers heat between two fluids. There are various types including shell and tube, plate and frame, and air cooled. A shell and tube heat exchanger consists of tubes, a shell, baffles, and nozzle inlets and outlets. Proper design of the baffle cut, spacing, and orientation is important for efficient heat transfer and to prevent bypass and leakage streams from reducing effectiveness. Sealing strips are also used to block leakage paths and improve performance.
Pressure Safety Valve Sizing - API 520/521/526Vijay Sarathy
No chemical process facility is immune to the risk of overpressure to avoid dictating the necessity for overpressure protection. For every situation that demands safe containment of process gas, it becomes an obligation for engineers to equally provide pressure relieving and flaring provisions wherever necessary. The levels of protection are hierarchical, starting with designing an inherently safe process to avoid overpressure followed by providing alarms for operators to intervene and Emergency Shutdown provisions through ESD and SIL rated instrumentation. Beyond these design and instrument based protection measures, the philosophy of containment and abatement steps such as pressure relieving devices, flares, physical dikes and Emergency Response Services is employed
Data Ware House System in Cloud EnvironmentIJERA Editor
To reduce Cost of data ware house deployment , virtualization is very Important. virtualization can reduce Cost
and as well as tremendous Pressure of managing devices, Storages Servers, application models & main Power.
In current time, data were house is more effective and important Concepts that can make much impact in
decision support system in Organization. Data ware house system takes large amount of time, cost and efforts
then data base system to Deploy and develop in house system for an Organization . Due to this reason that,
people now think about cloud computing as a solution of the problem instead of implementing their own data
were house system . In this paper, how cloud environment can be established as an alternative of data ware
house system. It will given the some knowledge about better environment choice for the organizational need.
Organizational Data were house and EC2 (elastic cloud computing ) are discussed with different parameter like
ROI, Security, scalability, robustness of data, maintained of system etc
Structural Design and Rehabilitation of Reinforced Concrete StructureIJERA Editor
Effective rehabilitation scheme for failed structure demands methodical analysis of various
causes of failure and intended service loads and other functional details, The actual study under deliberation is
the best example of rehabilitation Structural element – Basement RCC raft, failed to sustain uplift due to ground
water table. This paper dealt with the rehabilitation of basement RCC raft foundation considering various design
aspects like uplift due to ground water table, sub-soil properties and restriction on depth of raft to suffice
available headroom for intended use.
Number of iterations needed in Monte Carlo Simulation using reliability analy...IJERA Editor
There are many methods in geotechnical engineering which could take advantage of Monte Carlo Simulation to
establish probability of failure, since closed form solutions are almost impossible to use in most cases. The
problem that arises with using Monte Carlo Simulation is the number of iterations needed for a particular
simulation.This article will show why it’s important to calculate number of iterations needed for Monte Carlo
Simulation used in reliability analysis for tunnel supports using convergence – confinement method. Number if
iterations needed will be calculated with two methods. In the first method, the analyst has to accept a distribution
function for the performance function. The other method suggested by this article is to calculate number of
iterations based on the convergence of the factor the analyst is interested in the calculation.
Reliability analysis will be performed for the diversion tunnel in Rrëshen, Albania, by using both methods
mentioned and results will be confronted
Investigation of Different Types of Cement Material on Thermal Properties of ...IJERA Editor
One of the challenges in sustainable development is to optimize the energy efficiency of buildings during their
lifespan. Nowadays the applying of different types of cements in modern concretes provide low embodied CO2
with the intrinsic property called “thermal mass” that reduces the risk of overheating in the summer and
provides passive heating in the winter. Thermal mass is affected by thermal properties of concrete which it is the
ability of the element to exchange heat with the environment and is based on thermal capacity, conductivity, and
density. Laboratory experiments measured density, specific capacity and thermal conductivity of sustainable
concrete mixes with various percentages of GGBS, PFA, SF. The results contribute to the investigation of the
performance of thermal properties performance in sustainable concrete.
Mechanistic Aspects of Oxidation of P-Bromoacetophen one by Hexacyanoferrate ...IJERA Editor
The kinetics of oxidation of p-bromoacetophenone by hexacyanoferrate (III) has been studied in alkaline
medium. The order of reaction with respect of both acetophenone and hexacynoferrate (III) has been found to be
unity. The rate of reaction increases with increase in the concentration of sodium hydroxide.On addition of
neutral KCl, reaction rate increases. The effects of solvent and temperature have been also studied. The product
p-bromophenyl glyoxal have been characterized by IR studies.
Many of mobile devices suffer from limited computation resources (memory and processors), limited network
connection, bandwidth and limited battery life. For minimizing these problems mobile agents are premising
technology. However, for clients and servers most mobile agent systems are very resources demanding. This
research paper describes an approach to run mobile agents on different devices from mobile phones and
Personal Digital Assistants (PDAs) to powerful PCs. It proposes a simple mobile agent architecture and
middleware that makes it possible for accessing a mobile agent system on different devices. This architecture
and middleware proposes that clients will state their abilities. Depending on these abilities, the client will either
run the full mobile agent on the device or only run a light-weight version of the agent on the device. The mobile
agents are basically same on all clients, but code of the mobile agent is removed for small devices. This means
that only the data of the agent can be changed for mobile devices with minimal resources. The code of this agent
is stored at the server. When the agent returns to the server, the two parts are joined and the agent is ready to be
executed. The joined mobile agent can migrate to other agent servers and clients. A middleware is also proposed
that makes it possible to establish communication between different heterogeneous devices.
Direct Kinematic modeling of 6R Robot using Robotics ToolboxIJERA Editor
The traditional approaches are insufficient to solve the complex kinematics problems of the redundant robotic
manipulators. To overcome such intricacy, Peter Corke’s Robotics Toolbox [1] is utilized in the present study.
This paper aims to model the direct kinematics of a 6 degree of freedom (DOF) Robotic arm. The Toolbox uses
the Denavit-Hartenberg (DH) Methodology [2] to compute the kinematic model of the robot.
An Improved Bandwidth for Electromagnetic Gap Coupled Rhombus Shaped Microstr...IJERA Editor
This paper presents simulation and analysis of a Stacked Electromagnetic Gap Coupled Rhombus Shaped
Microstrip Patch Antenna (SEGCRSMPA) to increase the bandwidth. The aim of this paper is to improve the
bandwidth of Electromagnetic Gap Coupled Rhombus Shaped Microstrip Patch Antenna (EGCRSMPA). To
improve the bandwidth, stacking principle has been used. In this paper an assembly of one central rectangular
patch with four triangular patches forming rhombus shaped microstrip patch antenna is discussed. IE3D
simulation software is used for simulation. The performance of the proposed microstrip patch antenna is
compared with that of a conventional rectangular microstrip antenna and EGCRSMPA having same dimensions.
The proposed designed microstrip patch antenna offers much improved impedance bandwidth 47.62%.
Development and Comparison of Image Fusion Techniques for CT&MRI ImagesIJERA Editor
Image processing techniques primarily focus upon enhancing the quality of an image or a set ofimages to derive
the maximum information from them. Image Fusion is a technique of producing a superior quality image from a
set of available images. It is the process of combining relevant information from two or more images into a
single image wherein the resulting image will be more informative and complete than any of the input images. A
lot of research is being done in this field encompassing areas of Computer Vision, Automatic object detection,
Image processing, parallel and distributed processing, Robotics and remote sensing. This project paves way to
explain the theoretical and implementation issues of seven image fusion algorithms and the experimental results
of the same. The fusion algorithms would be assessed based on the study and development of some image
quality metrics
A Review of Intel Galileo Development Board’s TechnologyIJERA Editor
Intel Galileo, A Smart Arduino Based Development Board is cost-effective and efficient development board by
Intel Corporation. Three variants- Gen 1, Gen 2 and Edison is already being launched in the market. Intel, being
a market leader in development of Processor Technology is constantly researching and improving the Galileo
Technology. The board can lay strong foundation for embedded system researchers to develop various DIY
projects and build more energy efficient and cost effective products taking Galileo as the central controller. The
aim of this research paper is to highlight Intel Galileo Development Board Technology- Its features, Board
Components, Technology Available till date and Platform for programming various projects.
Effect of Petrophysical Parameters on Water Saturation in Carbonate FormationIJERA Editor
This document summarizes a study on the effect of petrophysical parameters on water saturation in carbonate formations. The study analyzed data from two wells, including porosity, resistivity, and water saturation measurements from well logs and core analysis. Cementation factors ranged from 1.44 to 1.93 from core analysis and logs respectively. Tortuosity factors were 1.11 from logs and 1.6 from core analysis. Saturation exponents were 2.58 from logs and 2.095 from core analysis. Average water saturation from logs was 0.54% and from core analysis was 0.39%. The study aimed to obtain more accurate water saturation estimates by analyzing variations in cementation factor and saturation exponent from different measurement techniques
Transport properties of Gum mediated synthesis of Indium Oxide (In2O3) Nano f...IJERA Editor
Two- Step method has been applied to prepare stable In2O3 nano fluids in Ethylene Glycol with PVP (Polyvinyl
pyrrolidone) used as stabilizing agent having In2O3 concentrations of 1% by volume, where the In2O3 nano
particles are obtained by biosynthesis of Indium (III) Acetyl Acetonate and Gum Acacia. Since the two-step
method is more versatile as it provides the opportunity to disperse a wide variety of nano particles in different
types of base fluids. The nano fluids were characterised by UV-vis spectroscopy, FTIR, SEM, EDAX, and
TEM, and systematically investigated for Thermal conductivity (TC), density, viscosity, specific gravity and
electrical conductivity for different polymer concentrations. The size of nano particles was found to be in the
range of 5-30nm for two different nano particle to PVP ratios. For higher concentration of polymer in nano
fluid, nano particles were 20nm in size showing increase in Thermal conductivity but a decrease in density and
viscosity which is due to the polymer structure around nano particles. It is observed that the viscosity, density &
specific gravity increases with the increase in PVP concentration and decreases with temperature. The thermal
conductivity measurements of nano fluids show substantial increment relative to the base fluid (Ethylene
glycol). Effect of PVP Polymer on viscosity, density, specific gravity can have a significant effect on magnitude
and behaviour of the Thermal conductivity enhancement confirming the Newtonian behaviour of nano fluid.
This offers tremendous scope for developing compact and effective heat transfer equipment. An enhancement of
20-25% for 1:5 volume concentration are observed at an average voltage of 60V when compared with EG
(Ethylene glycol) at the same voltage. This method is simple, fast and reliable for the synthesis of Newtonian
nano fluids containing In2O3 nano particles.
An Evaluation System of Surface Water Quality in Algeria (Application on the ...IJERA Editor
Easily accessible surface waters remain very fragile and very vulnerable to various types of pollution. Chellif,
Macta and Tafna Basins are considered as the main water resources feeding the North West of Algeria; however,
protection and conservation of these water resources become the major concern of the researchers. The
evaluation system of the water quality is based on the measure of physic-chemical parameters of the surface
water according to the uses of water for drink, industry or agriculture. In this work we have to proceed to an
application of this system to the surface waters on the three basins. Physic-chemical analyses are used for a
period of three years (2012-2014) and several points chosen on the three catchments are taken into account.
In this paper we shall apply the quality index calculation method for the Water Quality Evaluation system
(WQES) and the follow-up of the impacts of the anthropologic activities on the natural environment The main
results are the validation of the WQES method for different type of pollution as mineral, organic, heavy metals
in the West of Algeria, this methodology give us possibility for better investigation of the water pollution
Model formulation and Analysis of Total Weight of Briquettes after mixing for...IJERA Editor
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Comparison of Shell and Tube Heat Exchanger using Theoretical Methods, HTRI, ASPEN and SOLIDWORKS simulation softwares
1. Ambekar Aniket Shrikant.et. al Int. Journal of Engineering Research and Application www.ijera.com
ISSN : 2248-9622, Vol. 6, Issue 3, ( Part -5) March2016, pp.99-107
www.ijera.com 99 | P a g e
Comparison of Shell and Tube Heat Exchanger using Theoretical
Methods, HTRI, ASPEN and SOLIDWORKS simulation
softwares
Ambekar Aniket Shrikant*, R. Sivakumar**, M. Vivekanandan***
*(M.Tech. Student, National Institute of Technology, Tamil Nadu India,
**(Mechanical Engg. Dept., M.V.J. College of Engg., Bangalore, Karnataka, India,
***(Uttam Industrial Engg. Pvt. Ltd., Tiruchirapalli, Tamil Nadu, India.
ABSTRACT
The aim of this article is to compare the design of Shell and Tube Heat Exchanger with baffles. Baffles used in
shell and tube heat exchanger improve heat transfer and also result in increased pressure drop. Shell and tube
heat exchanger with single segmental baffles was designed with same input parameters using 1) Kern’s
theoretical method; 2) ASPEN simulation software and 3) HTRI simulation software 4) SOLIDWORKS
simulation software. Shell side pressure drop and heat transfer coefficient are predicted. The results of all the
three methods indicated the results in a close range. The proven theoretical methods are in good agreement with
the simulation results.
Keywords – ASPEN, HTRI, Kern’s theoretical method, Segmental baffles, Shell and Tube Heat Exchanger
I. INTRODUCTION
For the past few decades, shell and tube
exchangers are widely used in many engineering
applications, such as chemical engineering
processes, power generation, petroleum refining,
refrigeration, air-conditioning, food industry, etc.
Shell and tube heat exchangers are relatively simple
to manufacture, and have multi-purpose application
possibility when compared with other types of Heat
exchangers. It was reported that more than 30% of
the heat exchangers in use are of the shell-and-tube
type.
Baffles play a significant role in Shell and
tube heat exchanger assembly. They provide
support for tubes, enable a desirable velocity to be
maintained for the shell-side fluid flow, and prevent
the tubes from vibrating. Baffles also guide the
shell-side flow to move forward across the tube
bundle, increasing fluid velocity and heat transfer
coefficient. If one takes the most commonly used
single segmental baffles as an example, heat transfer
is improved as the baffles guide the shell side fluid
to flow in a zigzag pattern between the tube bundle,
which enhances the turbulence intensity and the
local mixing.
Gaddis D [1] reported that the 9th
edition of
standards and design recommendations of Tubular
Exchanger Manufacturers Association (TEMA) was
released in 2007.
Kern method [2] and Bell–Delaware
method [3] are the most commonly used correlations
based approaches for designing the shell side. While
Kern method gives conservative results, suitable for
the preliminary sizing, Bell–Delaware method is a
detailed accurate in estimating heat transfer
coefficient and the pressure drop on the shell side for
common geometric arrangements. Bell–Delaware
method can indicate the existence of possible
weaknesses in the shell side design, but cannot point
out where these weaknesses are.
Gaddis and Gnielinski [4] studied the
pressure drop on the shell side of STHX with
segmental baffles.
Karno and Ajib [5] reported from their
studies on baffle spacing that baffle cut and baffle
spacing are the most important geometric parameters
that effect pressure drop as well as heat transfer
coefficient on the shell side of a STHX.
Bin Gao et al [6] carried out experimental
studies on discontinuous helical baffles at different
helical angles of 8o
, 12o
, 20o
, 30o
and 40o
and
reported that the performance of baffle at 40o
helix
angle was the best among those tested.
Sirous et al [7] replaced a segmental tube
bundles by a bundle of tubes with helical baffles in a
shell and tube heat exchanger to reduce pressure
drop and fouling and hence reduce maintenance and
operating cost in Tabriz Petroleum Company.
Farhad et al [8] reported from simulation
studies that for same helix angle of 40o
and same
mass flow rate, heat transfer per unit area decreases
with increase in baffle space. However, for same
pressure drop, the most extended baffle space
obtains higher heat transfer. Pressure gradient
decreases with increase in baffle space.
Yonghua et al [9] developed a numerical
model of STHX based on porosity and permeability
considering turbulence kinetic energy and its
dissipation rate. The numerical model was solved
RESEARCH ARTICLE OPEN ACCESS
2. Ambekar Aniket Shrikant.et. al Int. Journal of Engineering Research and Application www.ijera.com
ISSN : 2248-9622, Vol. 6, Issue 3, ( Part -5) March2016, pp.99-107
www.ijera.com 100 | P a g e
over a range of Re from 6813 to 22,326 for the shell
side of a STHX with flower baffles. Simulations
results agreed with that of experiments with error
less than 15%.
Yingshuang et al [10] carried out
experimental investigations on flower baffled STHX
and the original segmental baffle STHX models and
reported that the overall performance of the flower
baffled heat exchanger model is 20–30% more
efficient than that of the segmental baffle heat
exchanger under same operating conditions.
Edward et al [11] presented the procedure
for evaluating the shell side pressure drop in shell-
and-tube heat exchangers with segmental baffles.
The procedure is based on correlations for
calculating the pressure drop in an ideal tube bank
coupled with correction factors, which take into
account the influence of leakage and bypass streams,
and on equations for calculating the pressure drop in
a window section from the Delaware method.
Young et al [12] reported from simulation
studies on STHX with helical baffles using
commercially available CFX4.2 codes and
concluded that the performance of STHX with
helical baffles is superior to that of a conventional
STHX. Fluid is in contact with the tubes flowing
rotationally in the shell and hence reduced the
stagnation zones in the shell side, thereby improving
heat transfer.
Sparrow & Reifschneider [13], Eryener
[14], Karno & Ajib [15] carried out studies on the
effects of baffle spacing in a STHX on pressure drop
and heat transfer.
Li and Kottke [16,17] and Karno and Ajib
[18] carried out investigations on the effect of tube
arrangement in STHX from heat transfer view point.
From literature review, it is observed that
different studies on heat transfer coefficient and
pressure drop in STHX with different baffle shape,
spacing, and tube spacing have been carried out. It
is observed that comparison of theoretical design
methods of STHX with that of simulations using
software have not been done.
II. DESIGN OF SHELL AND TUBE
HEAT EXCHANGER
A shell and tube heat exchanger with single
segmented baffles is designed. Single segmented
baffle are chosen as they are the most widely used,
large data is available and hence can be theoretically
designed.
A water-water 1-2 pass shell and tube heat
exchanger is designed considering the data in the
following Table 1.
Table 1 Data for design of heat exchanger
Shell Side Fluid-Hot Water
Property Unit Value
THI
o
C 90
THO
o
C 70
Density kg/m3
971.8
Specific Heat Capacity kJ/kgK 4.1963
Viscosity mPas 0.354
Conductivity W/mK 0.67
Fouling Factor - 0.0002
Flow Rate kg/s 0.3
Tube Side Fluid-Cold Water
TCI
o
C 30
TCO
o
C 38
Density kg/m3
984
Specific Heat Capacity kJ/kgK 4.178
Viscosity mPas 0.725
Conductivity W/mK 0.623
Fouling Factor - 0.0002
Flow Rate kg/s 0.7533
Hot fluid is considered to flow in the shell
as a thumb rule says that fluid with low flow rate
should always be in shell side. A vice versa heat
exchanger was also designed which was inferior
with respect to hot fluid shell side design. Thus,
confirming the thumb rule. With the above basic
data a shell and tube heat exchanger was designed
by
1) Theoretical Method (Kern’s Method).
2) ASPEN Simulation Software.
3) HTRI Simulation Software
4) Solidworks Simulation Software.
2.1 Design of STHX by Kern’s Theoretical
Method:
This method is employed as it is simple to
use and the design is reliable. All the empirical
equations in this section are as proposed by Donald
Q. Kern.
Design of heat exchanger with this method is
illustrated as follows:
Logarithmic Mean Temperature Difference
LMTD is calculated as:
( Tlm) =
CiHo
CoHi
CiHoCoHi
TT
TT
TTTT
ln
(1)
= 45.74
For One shell pass and two tube passes,
R =
CiCo
HoHi
TT
TT
= 2.5 (2)
S =
CiHi
CiCo
TT
TT
= 0.133 (3)
LMTD correction factor is read from graph
given by Kern D.Q. [2] for one shell pass and two or
more tube passes using R and S values as
Ft = 0.99
Corrected Tlm = Ft Tlm (4)
= 0.99 45.74 = 45.15o
C
3. Ambekar Aniket Shrikant.et. al Int. Journal of Engineering Research and Application www.ijera.com
ISSN : 2248-9622, Vol. 6, Issue 3, ( Part -5) March2016, pp.99-107
www.ijera.com 101 | P a g e
It is assumed that U = 785W/m2
K
Heat Load is given by:
(Q) = mC (5)
= 0.3 4.1963 (90-70) = 25.18kW
Provisional Area is given by:
A =
lm
TU
Q
(6)
=
15.45785
25180
= 0.71m2
Choose 21.34mm OD, 18.04mm ID, 1.068m
long Copper tubes.
Allowing for tube-sheet thickness, take
L = 1.038m
Area of one tube = Ld o
(7)
= π 0.02134 1.038 = 0.0696m2
Number of tubes N is given by
(N) =
0696.0
71.0
= 10 (8)
1.35 triangular pitch is used to maintain good
ligament
Bundle Diameter Db is given by
(Db)=
207.2
1
249.0
N
d o
(9)
207.2
1
249.0
10
34.21
=113.73mm
Fixed U-tube Head is used. From FigureA3,
Bundle diametrical Clearance = 10mm
Shell diameter (Ds) = Db + 10 = 113.73 + 10 =
123.73mm
Nearest Standard Pipe size of 168.28mm is
considered as Shell Diameter.
1.1.1 Prediction of Tube Side Heat Transfer
Coefficient
Tube cross-sectional area is given by
2
4
i
d
=
2
04.18
4
= 255.6mm2
(10)
Tubes per pass =
2
N
=
2
10
= 5
Total Flow Area = 5 255.6 = 1.278 10-3
m2
Cold Water mass velocity = 3-
10×1.278
753.0
= 597.3kg/sm2
Linear velocity (u) =
984
3.597
= 0.6m/s
Re =
i
ud
= 3
3
10725.0
1004.186.0984
= 14666.3
Pr =
k
C
=
623.0
10725.0178.4
3
= 4.86
i
d
L
=
04.18
1038
= 57.54
Jh = 4
3
10
is taken from graph given by Kern
D.Q. [2]
14.0
33.0
PrRe
wi
h
i
d
kJ
h
(11)
=
14.0
3
33.03
9.0
1004.18
623.086.43.14666104
= 3072.3W/m2o
C
1.1.2 Prediction of Shell Side Heat Transfer
Coefficient:
Baffle Spacing (B) = 50.8mm
Tube Pitch (Pt) =1.35 di = 1.35 21.34 =
28.8mm
Cross Flow Area (As) is given by:
BD
P
dP
s
t
ot
(12)
=
6
108.503.168
8.28
34.218.28
= 2.2146 10-3
m2
Hot water mass velocity = 3
102146.2
3.0
= 135.47kg/sm2
Equivalent Diameter is given by
de = 22
34.21917.0
1.1
t
i
P
d
= 21.23mm
Re =
e
ud
= 3
3
10354.0
1023.2147.135
= 8124
Pr =
k
C
=
67.0
10354.0.01963.4
3
= 2.22
Choose 29% baffle cut, from figureA4, Jh = 7
10-3
14.0
33.0
PrRe
we
h
s
d
kJ
h
=
14.0
3
33.03
9.0
1023.21
67.022.28124107
4. Ambekar Aniket Shrikant.et. al Int. Journal of Engineering Research and Application www.ijera.com
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= 2101.5W/m2o
C
1.1.3 Prediction of Overall Heat Transfer
Coefficient:
F
d
d
k
d
d
d
hhU i
o
s
i
o
o
si
2
2
ln
111
(13)
0002.02
04.18
34.21
3852
04.18
34.21
ln1034.21
5.2101
1
3.3072
11
3
U
U = 782W/m2
Well near the assumed value of 785W/m2o
C
1.1.4 Prediction of Pressure Drop on Tube side
From graph given by Kern DQ [2], for Re =
14666.3
Jf =
3
105
2
5.28
2
14.0
u
d
L
JNP
wi
fp
(14)
= 1.8kPa
1.1.5 Prediction of Pressure drop on Shell-Side
From graph given by Kern DQ [2], at Re = 8124
Jf = 4.5 10-2
2
8
2
14.0
u
B
L
d
D
JP
we
s
f
(15)
= 64.77Pa
The results of this method are the
1. Overall Heat Transfer Coefficient U=
782W/m2
C
2. Tube-side Pressure Drop ∆P = 1.8kPa
3. Shell-side Pressure Drop ∆P = 64.77Pa.
2.2 Design of STHX using ASPEN simulation
software:
This software can be used to design, rate,
simulate and do cost prediction of a heat exchanger.
Here ASPEN is used to simulate the heat exchanger
designed by Kern’s theoretical method. In
simulation mode of this software all the data related
to geometry of heat exchanger and the properties of
fluids are to be stated as input to the software. Flow
rates and input temperatures of the fluid streams are
also to be stated. The software then gives output in
terms of the output temperature attained by the
streams. It generates a specification sheet called
TEMA sheet which indicates the overall Heat
transfer coefficient, Pressure Drop in both shell-side
and tube-side and many other parameters involved in
heat exchanger design.
The input for ASPEN simulation software
in this case is as shown in the following Table 2,
Table2 Input to ASPEN simulation Software
I. Problem Definition
A. Application Options
1. General
Calculation Mode Simulation
Location of Hot fluid Shell-Side
Select Geometry Based on SI standards
Calculation Method Advanced method
2. Hot side
Application Liquid, no phase change
Simulation Calculation Output temperature
3. Cold side
Application Liquid, no phase change
Simulation Calculation Output temperature
B. Process Data
Fluid Name Shell-Side
hot water
Tube-
Side
cold
water
Mass flow rate (kg/s) 0.3 0.753
Inlet Temperature ( ) 90 30
Operating Pressure abs (bar) 1 1
Fouling Resistance (m2
K/W) 0.0002 0.0002
II. Property Data
Properties of fluids were imported form ASPEN database
III. Exchanger Geometry
A. Shell/Heads
Front Head Type B-bonnet bolted or
integral tube-sheet
Shell Type E-one pass shell
Rear Head Type U – U-tube bundle
Exchanger Position Horizontal
Shell Inner diameter (mm) 154.05
B. Tube
Number of Tubes 10
Number of Tubes Plugged 0
Tube length (mm) 1038
Tube Type Plain
Tube Outside Diameter (mm) 21.34
Tube wall Thickness (mm) 1.65
Tube Pitch (mm) 28.8
Tube Pattern 45
Tube Material Copper
C. Baffles
Baffle Type Single Segmental
Baffle Cut (%) 29
Baffle Orientation Horizontal
Baffle Thickness (mm) 3.2
Baffle Spacing (mm) 50.8
Number of Baffles 16
D. Nozzles
Outside diameter of shell side
Inlet nozzle (mm)
26.645
Inside diameter of shell side
Inlet nozzle (mm)
26.645
Outside diameter of tube side
Inlet nozzle (mm)
26.645
Inside diameter of tube side
Inlet nozzle (mm)
26.645
IV. Construction Specifications
A. Materials of Construction
Shell Carbon Steel
Tube-Sheet Carbon Steel
Baffles Carbon Steel
Heads Carbon Steel
Nozzle Carbon Steel
Tube Copper
B. Design Specifications
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1. Codes and Standards
Design Code ASME Code Sec VIII
Div 1
Service Class Refinery Service
TEMA Class C-General Class
Material Standard ASME
Dimensional Standard ANSI - American
Figure 1 Heat Exchanger Specification sheet by
ASPEN Simulation.
Figure 2 TEMA Construction details of Shell and
Tube Heat Exchanger given by ASPEN Simulation
The output of APSEN Simulation software
gives the specification sheet shown in Fig. 1 and
TEMA specification sheet shown in Fig. 2.
2.3 Design of STHX HTRI Simulation Software:
This software can be used to design, rate
and simulate a heat exchanger. Here HTRI is used to
simulate the heat exchanger designed by Kern’s
theoretical method. In simulation mode of this
software all the data related to geometry of heat
exchanger and the properties of fluids are to be
stated as input to the software. Flow rates and input
temperatures of the fluid streams are also to be
stated. The software then gives output in terms of the
output temperature attained by the streams. It
generates a specification sheet called TEMA sheet
which indicates the overall Heat transfer coefficient,
Pressure Drop in both shell-side and tube-side and
many other parameters involved in heat exchanger
design. This Software also provides necessary
drawings of the heat exchanger.
The input for HTRI simulation software in this
case is as shown in the following Table 3.
Table 3 Input data to HTRI Simulation Software
I. Case Mode Simulation
II. Exchanger Service Generic Shell and Tube
III. Process Conditions
Fluid Name Shell-Side
hot water
Tube-Side
cold water
Mass flow rate (kg/s) 0.3 0.753
Inlet Temperature ( ) 90 30
Operating Pressure abs (bar) 1 1
Fouling Resistance (m2
K/W) 0.00
02
0.000
2
IV. Shell Geometry
TEMA Type B-E-U
Shell ID (mm) 154.05
Orientation Horizontal
Hot Fluid Shell Side
V. Baffle Geometry
Type Single Segmental
Orientation Perpendicular
Baffle Cut (%) 29
Baffle Spacing (mm) 50.8
Baffle Thickness (mm) 3.2
Crosspasses 17
VI. Tube Geometry
Type Plain
Length (m) 1.038
Tube OD (mm) 21.34
Wall Thickness (mm) 1.65
Pitch (mm) 28.8
Layout Angle 45
Tube Pass 2
Tube Count 10
Tube Material Copper
VII. Nozzles
Standards ANSI
Outside diameter of shell side
Inlet nozzle (mm)
26.645
Inside diameter of shell side Inlet
nozzle (mm)
26.645
Outside diameter of tube side Inlet
nozzle (mm)
26.645
Inside diameter of tube side Inlet
nozzle (mm)
26.645
Inlet Type Radial
Outlet Type Radial
Radial Position of inlet
nozzle on shell
Top
Longitudinal Position of
inlet nozzle on shell
At Rear Head
Radial Position of inlet
nozzle on shell
Opposite Side
Location of nozzle at U-
bend
Before U-bend
Number at each location 1
VIII. Property Data
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Properties of fluids were imported form HTRI database
The output of HTRI Simulation software
gives the specification sheet shown in Fig. 3 and
TEMA specification sheet shown in Fig. 4.
Figure 3 Heat Exchanger Specification sheet by
HTRI Simulation.
Figure 4 TEMA Construction details of Shell and
Tube Heat Exchanger given by HTRI Simulation
2.3 Design of STHX using Solidworks Flow
Simulation Software:
A commercially available CFD code
(SOLIDWORKS FLOW SIMULATION) has been
used to carry out the numerical calculations for the
studied geometries. A three dimensional geometrical
model of the problem is developed with
SOLIDWORKS software. Mesh generation is done.
The physical model is presented in Fig. 5. The tube
material is Copper while the other components are
carbon steel. The physical properties of carbon steel
and copper are taken from the SOLIDWORKS
database. Thermal properties of water are also taken
from the SOLIDWORKS database.
The water inlet boundary conditions are set
as Flow opening inlets and outlet boundary
conditions are set as Pressure opening outlets. The
exterior wall is modeled as adiabatic. The simulation
is solved to predict the heat transfer and fluid flow
characteristics by using k-ɛ turbulence model.
Following are the boundary conditions
assumed:
1) Shell Side Inlet was set as Flow opening the mass
flow rate varied from 0.1kg/s to 0.5kg/s for different
simulations and temperature was set to 363.15K.
2) Tube Side Inlet was set to Flow opening the mass
flow rate was set to 0.7533kg/s and the
temperature was set to 303.15K.
3) Both shell side and tube side were set as Pressure
openings with pressure set to Atmospheric
Pressure.
Figures 6, 7 and 8 show the variations in
pressure, temperature, and velocity within the
STHX with single segmental baffles simulated
using Solidworks Simulation software.
Figure 5 2D view of the Shell and Tube Heat
Exchanger designed
Figure 6 Pressure variation in STHX
Figure 7 Temperature variatiion in STHX
Figure 8 Velocity variation in STHX
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III. RESULTS AND DISCUSSION
Table 4 shows the variations in the Overall
Heat transfer coefficient, Shell side outlet
temperature, and shell side temperature difference.
Table 4 Comparison of Overall Heat Transfer
Coefficient, Shell side outlet temperature and Shell
side temperature difference predictions
Heat Exchanger
Design Method
ShellSide
Outlet
Temperature
°C
OverallHTC
W/m2
KShellSide
Temperature
Difference
°C
Kern's method 70 782 20
ASPEN Simulation 70.08 790.2 19.92
HTRI Simulation 70.84 781.91 19.16
CFD Simulation 68.79 852.46 21.21
It is observed from Fig. 9 that Kern’s
method, and HTRI simulations have similar values
of Overall Heat transfer coefficient, while that
obtained from ASPEN simulation is little higher, and
that obtained from CFD simulations using
Solidworks software is the highest with variation of
over 9% when compared to Kern’s theoretical
method. This is variation in Solidworks software
results may be due to better grid convergence of the
solution while the theoretical values are based o
empirical correlations only.
Similarly, It is observed from Fig. 10 that
shell side temperature difference is almost similar
with Kern’s method and ASPEN method, while that
with HTRI simulation showed a lesser value, while
that with CFD simulation using Solidworks software
is higher by 6%. This variation in Solidworks
software results may be owing to improvement in
computation capability due to finer meshes in flow
field.
Fig. 11 shows that the Shell side outlet
temperature is very similar with Kern’s method, and
APSEN simulation. On the other hand, HTRI
simulation is greater by 1.2% while that by
Solidworks Simulation is lesser by 1.7%.
Figure 9 Variation in Overall Heat Transfer
coefficient with different design softwares
Figure 10 Variation in Shell Side Temperature
Difference with different design softwares
Figure 11 Variation in Tube Side Outlet
Temperature with different design softwares
IV. CONCLUSIONS
A Shell and Tube Heat Exchanger was
designed with same input parameters using Kern’s
method, ASPEN simulation software, HTRI
simulation software and by SolidWorks Flow
Simulation software and the Overall heat transfer
coefficient values are 782, 790.2, 781.9 and 852.6
W/m2
K respectively. Simulation results of Overall
heat transfer coefficient with Kern’s method ASPEN
and HTRI software are similar while, that with
SolidWorks software is greater by 9%. Shell side
temperature drop is greater by 6% with Solid works
software. All the three Methods obtained almost
same results for the same geometry of heat
exchanger. Thus, it can be concluded that the results
generated with single segmental baffle configuration
are real time.
REFERENCES
[1] Gaddis D, editor. Standards of the Tubular
Exchanger Manufacturers Association.
(Tarrytown (NY): TEMA Inc. 2007).
[2] Kern DQ, Process heat transfer. (New York
(NY): McGraw-Hill, 1950).
[3] Bell KJ. Delaware method for shell side
design. In: Kakac S, Bergles AE, Mayinger
F, editors. Heat exchangers: thermal–
hydraulic fundamentals and design. New
York: Hemisphere, 1981, 581–618.
[4] Gaddis ES, and Gnielinski V., Pressure
drop on the shell side of shell-and-tube
heatexchangers with segmental baffles.
Chem Eng Process 36, 1997, 149–59.
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[5] Karno A, Ajib S., Effects of baffle cut and
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7, 2006, 299–322.
[6] Bin Gao, Qincheng Bi, Zesen Nie and
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Nemati Taher, Kazem Razmi and Reza
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[12] Young-Seok Son and Jee-Young Shin,
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15(11), 2001, 1555-1562.
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of interbaffle spacing on heat transfer and
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NOMENCLATURE
A Area (m2
)
As Cross Flow Area (m2
)
B Baffle Spacing (m)
C Specific Heat Capacity (J kg-1
K-1
)
Db Bundle Diameter (m)
Di Inside diameter of shell (m)
Ds Outside diameter of shell (m)
de Equivalent Diameter (m)
di Inside diameter of tube (m)
do Outside diameter of tube (m)
F Fouling Factor.
Ft Log Mean Temperature Difference
Correction Factor
h Enthalpy (J kg-1
K-1
)
hi Tube side Film Heat Transfer Coefficient
(W m-2
K-1
)
hs Shell side Film Heat Transfer Coefficient
(W m-2
K-1
)
Jf Friction Factor
Jh Heat Transfer Factor
k Thermal Conductivity, Turbulent kinetic
energy.
L Length (m)
m Mass Flow Rate (kg s-1
)
N Number of tubes.
Np Number of tube side passes
Pin Pressure at inlet of the shell
Pout Pressure at outlet of the shell (
∆P Pressure Drop.
Pt Pitch.
Q Heat Load.
TCi Tube side fluid inlet temperature.
TCo Tube side fluid outlet temperature.
THi Shell side fluid inlet temperature.
THo Shell side fluid outlet temperature.
9. Ambekar Aniket Shrikant.et. al Int. Journal of Engineering Research and Application www.ijera.com
ISSN : 2248-9622, Vol. 6, Issue 3, ( Part -5) March2016, pp.99-107
www.ijera.com 107 | P a g e
∆Tlm Log Mean Temperature Difference.
t Time.
U Overall Heat Transfer Factor.
u Velocity.
Le Lewis Number.
Re Reynolds number.
Pr Prandtl Number.
x Co-ordinate.
y Co-ordinate.
z Co-ordinate.
Greek Letters
ρ Density.
µ Dynamic Viscosity.
ɛ Turbulent dissipation energy.