### Chemical and Process Engineering Resources ## Steam Tracing with MS Excel

May 24 2012 06:50 PM | adelange in Heat Transfer      Results and Discussion

Due to the nature of the project, definite answers are not possible to obtain, but rather different simulations could be run and each time the answers could be evaluated. As an example, one specific run could be described in terms of its equations as follows:

Consider the Bare Tracer.

Firstly, the inputs field has to be completed (see Table 1): After this has been done, the outputs section may be calculated:

Some of the outputs are values found in making use of references from other tables. These are shown first in Table 2. This information can now be used together with the inputs section to calculate the remaining outputs.

Firstly, the Average Insulation Temperature is calculated from Eq. (9): it is found that Tins=36.67 ÂºC

It should be noted that the Process fluid Temperature is not known yet, so this is not a final answer.

Secondly, the Annulus Temperature may be calculated from Eq. (8): Tann=76.4 ÂºC

Since Tp is not known yet, and Tins has not yet been assigned a definite value, this value is also not fixed yet.

Now, the Average Surface Temperature needs to be calculated. This value may be approximated by assuming that about 80% of the average surface temperature is due to the process fluid temperature and the remaining 20% is made up of the surface temperature on the tracer side. The Average Surface Temperature may then be calculated as follows.

From Eq.(13) and (14):  for the tracer side

and for the process fluid pipe side

Therefore The surface temperature is now calculated by making use of iterations to obtain the final value of

Tsurf-Avg = 14.991 ÂºC

This causes the value of q to change until it stabilizes to its final answer.

Technically speaking, one has to calculate the area ratios that the process fluid pipe, annulus length and tracer each contribute, calculate each areaâ€™s surface temperature, and obtain the average value for the surface temperature accordingly, but due to the limited capacity of Microsoft Excel, this method was tried and it failed, because Excel could not perform all the iterations necessary to do the calculations. The above calculation has shown to give satisfactory results for most situations.

As a next step, the surface coefficient needs to be calculated using Eq.(15): The value for the surface coefficient then becomes:

h0=10.1

k1 is calculated using Eq.(10): but according to Eq.(5), and therefore, k1=18.21340591
k2 may then be calculated using Eq.(11): and therefore amounts to k2= 0.489641399

Finally the Process Fluid Temperature can be calculated using Eq.(12): Excel is then programmed to perform iterations automatically, since a circular reference is created, but it causes all of the values to converge consequently, and the final answers are obtained, and with the final values of Tins known, the correct thermal conductivity values can be obtained and used in the equations:

kins = 0.02712 W/m K
kw = 53.3 W/m K

References

Le Roux, D.F. (1997) â€œThermal Insulation and Heat Tracingâ€, Guideline presented by line manager D.F. le Roux, Secunda.

Foo, K.W. (1994) â€œSizing tracers quickly (Part 1)â€. Hydrocarbon Processing, p93-97. January. â€œSizing tracers quickly (Part 2)â€. Hydrocarbon Processing, p93-97. February.

Fisch, E. (1984) â€œWinterising process plantsâ€. Chemical Engineering, p128-143, 20 August.

Kenny, T.M. (1992) â€Steam tracing: do it rightâ€. Chemical Engineering Progress, p40-44, August.

Coulson, J.M and Richardson, J.F. (1999) Chemical Engineering, R.K. Sinnot, London.

Le Roux, D.F. (2005) Theoretical discussion and problem description, Sasol Limited, Secunda.

Van der Spuy, E. (2005) Theoretical advice, and steam traps, Spirax Sarco, Secunda.

Smit, J. (2005) Practical information, Sasol Limited, Secunda.

Technical committee of specification SP 50-4, (2004) Specification SP 50-4 Revision 2 for Steam and Hot Water Tracing, Sasol Limited, Secunda.

## 3 Comments rhonaldeliexer
Hi, very useful your spreadsheet calculation, but I have a trouble related about this. I have another conditions in wind speed, I mean my wind velocity is out of range (77 ft/s). In addition to this, I need to use another quantity of tracers, for above of 5. Could you help me? Best regards. Rhonald. Shakil
Thanks for that info. My problem is little different: I have a Ethylene Cylinder @70 bar pressure. I need to use Ethylene in the range of minimum 1bar to 50 bar in downstream reactor. If i throtle the Pressure using Pressure regulator the temp. will go as low as -104 0C if throtled to 1bar & 10.5 0C if throtled to 50bar from cylinder pressure 70 bar. Minimum design Metal Temperature(MDMT) is 5.5 0C? What can be done to deliver the Ethylene above MDMT? If i want to use Steam Tracing for heating the Ethylene after throttling how to calculate Steam tracing requirement? Plz. suggest! GarethBarnes

Hi, there seem to be a discrepancy between equation 7 and equation 21 which should be the same.

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