Heat Exchanger Puzzler: Make the Best of a Blunder

Readers suggest ways to get an incorrect exchanger to do the job.

1 of 2 < 1 | 2 View on one page

We heat heavy oil with steam before sending it to a reactor. The oil, which is pumped through the shell of the heat exchanger, enters at 100°F and exits at 250°F; 125-psig steam goes through the tubes. The old exchanger had four shell passes and eight tube passes. Someone at corporate engineering mistakenly ordered a heat exchanger with three shell passes and six tube passes. The new shell is rated for 250 psig. The oil/steam overall external heat transfer coefficient is 100 BTU/lb-hr-°F. Is there anything we can do to use this unit so we don't have to order a new heat exchanger and delay production?

Switch the flow of oil and steam, i.e., pump the oil through the six tube passes of the new heat exchanger and the steam on the shell side. Very often the heat transfer coefficient of a liquid on the shell side is relatively low, usually due to a small flow velocity. The heat transfer coefficient of condensing steam is high either on the shell or tube side; it is not sensitive to flow velocity. However, the pressure drop on the oil side will increase, leading to a question regarding the available pump pressure. Therefore, performing a detailed calculation of heat transfer and pressure drop is necessary to make a decision.
Dr. Walter Schicketanz, consultant

Assuming the area is similar to the current exchanger, I would recommend increasing the oil flow rate and using higher pressure steam if it is available. A higher oil flow rate will increase the overall heat transfer coefficient and the higher steam pressure will raise the log mean temperature difference (LMTD).
Donald Phillips, manager
Phillips Engineering, Melbourne, Fla.

As a heat flux of 1,500 BTU/hr-ft2-°F is reasonable, I would move the steam to the shell side. Put the oil through the tubesheet. Knock holes in the baffles to allow steam condensate to escape and add additional nozzles for steam traps — see Figure 1.
Norman Terrelg, production engineer
BASF, Freeport, Texas

The obvious solution is to increase the steam pressure, if high pressure steam is available. The highest pressure steam that can be used is about 75% of the shell rating pressure: 0.75 × 250 = 188 psig. If the pressure reaches around 80%, the relief valve may start to open. If we assume 200 psig steam is available, it must be reduced to a safe limit, say, 180 psig.

Flow through a regulator is the same as through a valve or orifice — it is an isenthalpic process, not adiabatic as often is assumed. If we ignore supersonic flow and assume it is unchoked, the temperature drop will be slight. For real gases, a drop in temperature resulting from throttling is described by the Joule-Thompson (Kelvin) coefficient: mJT = (dT/dP)H.

Throttling a wet gas produces a superheated vapor. Using an online calculation program I found by googling "superheat steam table," I estimated a temperature drop of 7.2°F for a drop from 200 psig to 180 psig for a constant total enthalpy of 1,119.3 BTU/lb, which is the total enthalpy of saturated steam at 200 psig. I solved the problem by iterating with the program using the superheated temperature as a variable and the enthalpy of 1,199.3BTU/lb as the target. The steam starts with a saturated temperature of 387.8°F and exits the regulator at 380.6°F — the saturation temperature at 180 psig is 379.5oF. The temperature entering the heat exchanger is 380.6°F.

1 of 2 < 1 | 2 View on one page
Show Comments
Hide Comments

Join the discussion

We welcome your thoughtful comments.
All comments will display your user name.

Want to participate in the discussion?

Register for free

Log in for complete access.


No one has commented on this page yet.

RSS feed for comments on this page | RSS feed for all comments