Design Considerations for Shell and Tube Heat Exchangers

7/28/2019 Design Considerations for Shell and Tube Heat Exchangers

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Design Considerations for Shell and Tube HeatExchangers

When preparing to design a heat exchanger, do you ever wonder where to start?You've done it before, but you hate that feeling of getting half way through the design

and realizing that you forgot toconsider one important element. Thethought process involved is just asimportant as the calculationsinvolved. Let's try to map out a heatexchanger design strategy. We'll doso with a series of questions followed

by information to help you answer the questions. 1. Is there a phase change involvedin my system?

A quick look at the boiling points

compared with the entrance and exittemperatures will help you answer this question. 2. How many "zones" are involved in my system?

"Zones" can best be defined as regimes of phase changes where the overall heattransfer coefficient (Uo) will vary. UsingT-Q (Temperature-Heat) diagrams are the

best way to pinpoint zones. The system isdefined as co-current or countercurrentand the diagram is constructed. Thediagram on the left illustrates the use of T-Q diagrams. These diagrams should

accompany your basic (input-output)diagram of the heat exchanger. Chemical

#1 enters the shell at 2000C as a

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superheated vapor. In Zone 1, it releasesheat to the tubeside chemical (Chemical #2). Zone 1 ends just a Chemical #1 begins tocondense. The tubeside (Chemical #2) enters as a liquid or gas and does not change

phase throughout the exchanger. Chemical #1 leaves Zone 1 and enters Zone 2 at its boiling temperature, Tb1. T* marks the temperature of Chemical #2 when Chemical#1 begins to condense. In Zone 2, Chemical #1 condenses to completion whileChemical #2 continues to increase in temperature. The temperature of Chemical #2

when Chemical #1 is fully condensed is denoted at T**. Finally, in Zone 3, bothchemicals are liquids. Chemical #1 is simply liberating heat to Chemical #2 as it

becomes a subcooled liquid and exits the shell at 1000C.

Defining zones is one of the most important aspects of heat exchanger design. It isalso important to remember that if your process simulator does not support zonedanalysis (such as Chemcad III), you should model each zone with a separate heatexchanger. Thus, the previous illustration would require 3 heat exchangers in thesimulation. BUT, do not draw 3 exchangers on your PFD (Process Flow Diagram).This is all happening in one exchanger. 3. What are the flowrates and operating pressures involved in my system?

This information is critical in establishing the mass and energy balance around the

exchanger. Operating pressures are particularly important for gases as their physical properties vary greatly with pressure. 4. What are the physical properties of the streams involved?

If you're using a process simulator, obtaining the physical properties of your streamsshould be just a click of the mouse away. However, if performing the calculation byhand, you may have to do some estimating as the streams may not be of pure

substances. Also, you should get the physical properties for each zone separately toensure accuracy, but in some cases it is acceptable to use an average value. This would

be true of Chemical #2 in the tubes since it is not changing phase or undergoing a truly

significant temperature change (over 1000C). Physical properties that you will want to

collect for each phase of each stream will include: heat capacity, viscosity, thermal

conductivity, density, and latent heat (for phase changes). These are in addition to the boiling points of the streams at their respective pressures. 5. What are the allowable pressure drops and velocities in the exchanger?

Pressure drops are very important in exchanger design (especially for gases). As the pressure drops, so does viscosity and the fluids ability to transfer heat. Therefore, the pressure drop and velocities must be limited. The velocity is directly proportional tothe heat transfer coefficient which is motivation to keep it high, while erosion andmaterial limits are motivation to keep the velocity low. Typical liquid velocities are 1-3 m/s (3-10 ft/s). Typical gas velocities are 15-30 m/s (50-100 ft/s). Typical pressuredrops are 30-60 kPa (5-8 psi) on the tubeside and 20-30 kPa (3-5 psi) on the shellside. 6. What is the heat duty of the system?

This can be answered by a simple energy balance from one of the streams. 7. What is the estimated area of the exchanger?

Unfortunately, this is where the real fun begins in heat exchanger design! You'llneed to find estimates for the heat transfer coefficients that you'll be dealing with.These can be found in most textbooks dedicated to the subject or in Perry's ChemicalEngineers' Handbook. Once you've estimated the overall heat transfer coefficient, use

the equation Q=UoADTlm

to get your preliminary area estimate. Remember to use the

above equation to get an area for each zone, then add them together. 8. What geometric configuration is right for my exchanger?

Now that you have an area estimate, it's time to find a geometry that meets your

needs. Once you've selected a shell diameter, tubesheet layout, baffle and tube spacing,etc., it's time to check your velocity and pressure drop requirements to see if they're

being met. Experienced designers will usually combine these steps and actually obtaina tube size that meets the velocity and pressure drop requirements and then proceed.







Some guidelines may be as follows: 3/4 in. and 1.0 in. diameter tubes are the most

popular and smaller sizes should only be used for exchangers needing less than 30 m2

of area. If your pressure drop requirements are low, avoid using four or more tube passes as this will drastically increase your pressure drop. Once you have a geometryselected that meets all of your needs, it's on to step #9. 9. Now that I have a geometry in mind, what is the actual overall heat transfer

coefficient? This is where you'll spend much of your time in designing a heat exchanger.

Although many textbooks show Nu=0.027(NRE

)0.8

(NPR

)0.33

as the "fundamental

equation for turbulent flow heat transfer", what they sometimes fail to tell you is thatthe exponents can vary widely for different situations. For example, condensation inthe shell has different exponents than condensation in the tubes. Use this fundamentalequation if you must, but you should consult a good resource for accurate equations. Ihighly recommend the following: Handbook of Chemical Engineering Calculations,2nd Ed., by Nicholas P. Chopey from McGraw-Hill publishers (ISBN 0070110212).Also, don't forget to include the transfer coefficient across the tube wall and the foulingcoefficient. These can be very significant! 10. What is the actual area of the exchanger using the 'actual' heat transfer coefficient?

If you recall, you used estimated heat transfer coefficients to get an initial area. Nowit's time to recalculate the area.

THE LOOP

Now you're on your way, pick a new geometry corresponding to your new ("actual")area, check the velocity and pressure drop, calculate the overall heat transfer coefficientagain. How does it compare with the previously calculated value? If it is not within 5-10%, recalculate the process over and over (using your new value for Uo) until it does!Sounds like alot of work. Add in the fact that some of the individual heat transfer coefficients require iterative solutions and it's not hard to see why people usually use acomplex spreadsheet or a program to do this. You can save some time by using

estimates that you've undoubtedly seen, however you must realize that each time youestimate, you're losing accuracy.

Remember two main items:1. ZONED ANALYSIS 2. ACCURACY OF INITIAL OVERALL HEAT TRANSFER COEFFICIENT The zoned analysis is the key to starting the process correctly. The accuracy of theinitial overall heat transfer coefficient will in part determine how many time you will

be going through the calculation. Other Considerations:

l Materials of Construction l Ease of Maintenance l Cost of Exchanger l Overall Heat Integration







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Design Considerations for Shell and Tube Heat Exchangers

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