Heat Exchanger Rating (Bell-Delaware Method)

# Heat Exchanger Rating (Bell-Delaware Method)

In Bell Delaware method, the fluid flow in the shell is divided into a number of individual streams. Each of these streams introduces a correction factor which is used to correct heat transfer coefficient and pressure drop across the shell. This article gives step-by-step guidance on doing heat exchanger rating analysis based on Bell-Delware method.

### Shell Side Heat Transfer Coefficient, hs

Cross flow area, Sm is the minimum flow area in one baffle space at the center of the tube bundle. It is calculated by following equation:

``Sm = B[(Ds - DOTL) + (DOTL - Do)(PT - Do)/PT,eff ]``

where, PT is tube pitch, B is central baffle spacing, DOTL is outer tube limit diameter, Ds is shell diameter and Do is tube outside diameter.

````PT,eff = PT for 30° and 90° layouts`
`PT,eff = 0.707*PT for 45° layout````

Shell side cross flow mass velocity, GS is defined as:

``GS = mS/Sm``

where, mS is shell side mass flow rate. Shell side Reynolds number ReS is then calculated from

``ReS = Do.GS / μS``

where, μS is the shell side fluid dynamic viscosity at average bulk temperature.

Shell side Prandtl number PrS is calculated as following :

``PrS = CP,S.μS / kS``

where, CP,S is the shell side fluid specific heat and kS is the shell side fluid thermal conductivity.

Colburn j-factor for an ideal tube bank is defined as:

where a1, a2, a3 and a4 are correlation constants listed below.

The ideal tube bank based coefficient is calculated from –

where, μS,W is shell side fluid viscosity at wall temperature.

#### Correction factor for Baffle Window Flow, JC

The factor JC accounts for heat transfer in the baffle windows. It has a value of 1.0 for exchanger with no tubes in the windows.

````JC = 0.55 + 0.72FC`
`FC = 1 - 2FW`
`FW = (θCTL - Sin(θCTL))/2π`
`θCTL = 2cos-1(Ds(1 - 2*Bc/100)/DCTL)`
`DCTL = DOTL - Do````

where, Bc is segemental baffle cut in %.

#### Correction factor for Baffle Leakage, JL

The correction factor JL considers the effects of the tube-to-baffle and shell-to-baffle leakage streams on heat transfer.

````JL = 0.44(1-rS) + (1-0.44(1-rS))exp(-2.2rL)`
`rS = Ssb /(Ssb + Stb)`
`rL = (Ssb + Stb)/ Sm`
`Ssb = Ds*DSB(π - 0.5θDS)`
`Stb = (π/4)((Do+LTB)2 - Do2)Nt(1-FW)`
`θDS = 2cos-1(1 - 2Bc/100)````

where, Nt is number of tubes, DSB is diametral clearance between shell & baffle and LTB is diametral clearance between tube and baffle.

#### Correction factor for Bundle Bypass effects, JB

Bundle bypass correction factor JB accounts for the bundle bypass stream flowing in the gap between the outermost tubes and the shell. The number of effective rows crossed in one cross flow section, Ntcc between the baffle tips is provided by following equation.

````Ntcc = (Ds/Pp)(1 - 2Bc/100)`
`Pp = PT 30.5/2 for 30° layout`
`Pp = PT / 20.5 for 45° layout`
`Pp = PT for 90° layout````

Ratio of sealing strips to tube rows rss is provided by

``rss = Nss/ Ntcc``

where Nss is number of sealing strips (pairs) in one baffle.

The bundle bypass flow area, Sb is defind as

``Sb = B(Ds - DOTL - Do/2)``

where, B is central baffle spacing. Correction factor JB is then calculated as following –

````JB = exp(-Cj(Sb / Sm)(1 - (2rss)1/3)) for rss < 0.5`
`JB = 1 for rss >= 0.5`
`Cj = 1.35 for ReS < 100`
`Cj = 1.25 for ReS >= 100````

The factor JR accounts for the decrease in the heat transfer coefficient with downstream distance in laminar flow.

````Ntcw = (0.8/Pp)(Ds(Bc/100) - (Ds-(DOTL-Do))/2 )`
`NB = 1 + (int)(L - 2Ls - LBIn - LBOut)/B`
`NC = (Ntcw + Ntcc)(1 + NB)`
`JRL = (10/NC)0.18`
`JR = 1, ReS > 100`
`JR = JRL + (20-ReS)(JRL - 1)/80, ReS <= 100, ReS > 20`
`JR = JRL, ReS <= 20````

where, L is tube length, Ls is tubesheet thickness, LBIn is inlet baffle spacing and LBOut is outlet baffle spacing.

#### Correction factor for unequal baffle spacing, JS

````n1 = 0.6, ReS >= 100`
`n1 = 1/3, ReS < 100`
`JS = ((NB-1)+(LBIn/B)1-n1 + (LBOut/B)1-n1)/((NB-1)+(LBIn/B) + (LBOut/B))````

Shell side heat transfer coefficient is calculated as

``hs = hIdeal(JC.JL.JB.JS.JR)``

### Shell Side Pressure Drop, ΔPs

Friction factor for ideal tube bank is calculated as following –

where b1, b2, b3 and b4 are correlational constants listed below.

Pressure drop for an ideal tube bank is calculated from

``ΔPIdeal = 2f(GS²/ρS)(μS/μS,W)0.14 Ntcc``

#### Correction factor for Baffle Leakage, RL

````RL = exp(-1.33(1+rS)rLp)`
`p = 0.8 - 0.15(1+rS)````

#### Pressure drop for window section, ΔPW

Following terms are calculated as –

````SWG = (Ds²/8)(θDS - Sin(θDS))`
`SWT = Nt.FW(πDo²/4)`
`SW = SWG - SWT`
`GW = mS/(Sm.SW)0.5`
`DW = 4.SW /(π.Do.Nt.FW + θDS.Ds)````

Pressure drop for laminar and turbulent flow is calculated.

``ΔPW, Turb = NB.RL(2+0.6*Ntcw).GW²/(2.ρS)``

````ΔPW = ΔPW, Turb , ReS >= 100`
`ΔPW = ΔPW,Laminar , ReS < 100````

#### Correction factor for Bundle Bypass effect, RB

````RB = exp(-Cr(Sb / Sm)(1 - (2rss)1/3)) for rss < 0.5`
`RB = 1 for rss >= 0.5`
`Cr = 4.5 for ReS < 100`
`Cr = 3.7 for ReS >= 100````

#### Correction factor for unequal baffle spacing, RS

````n = 0.2, ReS >= 100`
`n = 1.0, ReS < 100`
`RS = 0.5((B/LBIn)2-n + (B/LBOut)2-n)````

Pressure drop in Central Baffle spaces, ΔPC is defined as –

``ΔPC = (NB - 1)ΔPIdeal.RL.RB``

Pressure drop in entrance & exit baffle spaces, ΔPE is calculated as –

``ΔPE = ΔPIdeal(1 + Ntcw/Ntcc).RB.RS``

Shell side pressure drop is calculated as following –

``ΔPS = ΔPW + ΔPC + ΔPE``

### Tube Side Heat Transfer Coefficient, ht

Reynold’s number and Prandtl number are calculated as following –

````ReT = Di.v.ρt/μt`
`PrT = Cp,t.μt/kt````

where, Di is tube inside diameter, v is velocity, ρt is density, μt is viscosity, kt is thermal conductivity and Cp,t is specific heat for fluid on tube side.

For laminar flow, ReT < 2300, Sieder and Tate correlation is used for Nusselt’s nubmer.

````Nu = 1.86(ReT.PrT.Di/Leff)1/3`
`Leff = L - 2*Ls````

For turbulent flow, ReT > 10,000, following equation developed by Petukhov-Kirillov can be used.

````Nu = (f/2)ReT.PrT/(1.07+12.7(f/2)0.5(PrT2/3-1))`
`f = (1.58 ln(ReT) - 3.28)-2````

For transient flow, Nusselt number can be interpolated from Nu Laminar & Nu Turbulent.

Heat transfer coefficient is calculated as following –

``ht = Nu.(kt/Di)(μt/μt, w)0.14``

### Tube Side Pressure Drop, ΔPt

Tube side pressure drop is calculated by following equation –

``ΔPt = (4.f.Leff.Np/Di + 4.Np)ρt.v²/2``

where, Np is number of tube passes.

### Overall Heat Transfer Coefficient, U

Resistance due to tube wall is calculated as following

``Rtube = Do/(2.ln(Do/Di).ktube)``

where, ktube is thermal conductivity of tube material. Overall clean heat transfer coefficient, UClean is calculated as per below equation

``UClean = 1/(hS + Do/(Di.ht) + Rtube)``

Overall dirty heat transfer coefficient, UDirty is calculated as per below expression

``UDirty = 1/(1/UClean + fshell + ftube)``

where, fshell & ftube are fouling factors for shell and tube side.

Heat transfer coefficient required, URequired is calculated as following

``URequired = Q /(A x LMTDcorrected)``

where, Q is heat duty, A is heat transfer area and LMTDcorrected is corrected logarithmic mean temperature difference.

````Over Surface, % = (UClean/URequired - 1)*100`
`Over Design,  % = (UDirty/URequired - 1)*100````

Web based calculation available at CheCalc.com

Spreadsheet for Heat Exchanger Rating based on Bell-Delaware Method

## 18 Replies to “Heat Exchanger Rating (Bell-Delaware Method)”

1. Pablo Jimenez says:

Realy usefull and grat job, thanks so much

2. Pablo Jimenez says:

There is some criterion for the dynamic pressure(DensityxVelocity^2) in the nozzles in existing equipment.

3. Excellent Spreadsheet, It can be increased with Triffin tubes.

4. Fabio says:

Very interesting. A real great job. I have one curiosity. How to compute the effect of baffle orientation? I mean, those correlations are for vertical baffle cuts. I’ve checked in HTRI, and if you use horizontal the baffle cuts, the Reynolds number will increase by about 12%, and shell heat transfer coefficient will increase by about 17%. Do you have the correlations for that correction? I know horizontal baffle cuts are unusual due to accumulation of solids, but I know one case of heat exchanger with this configuration.

5. Alexandra Colello says:

There is a discrepancy between the Excel spreadsheet calculation and the online website calculation. The shell-side h seems to be incorrect in the Excel spreadsheet.

1. Alexandra Colello says:

1. Alexandra Colello says:

Nevermind again. There is definitely an error with the shell-side HT coefficient calculation in the Excel spreadsheet.

1. Alexandra Colello says:

JL was off — found discrepancy in G-K61: Diametral Shell-Baffle Clearance calculation. One website, it is an input, not a calculation – regardless, these numbers are what caused the biggest discrepancy. I am still looking for one more discrepancy that relates to Js.

6. Franta says:

Hello, great job!
But I have one question, my appologies if I’m wrong but shouldn’t this equation:
NB = 1 + (int)(L – 2Ls – LBIn – LBOut)/(Bc/100)
be this:
NB = 1 + (int)(L – 2Ls – LBIn – LBOut)/(B) ?
It makes more sense.

1. Franta says:

Also you have it in spreadsheet as NB = 1 + (int)(L – 2Ls – LBIn – LBOut)/(B/100), but dividing B by 100 doesn’t make any sense. I believe you corrected Bc to B and then forgot to delete the 100?

2. CheGuide says:

Thanks for finding it, I have corrected the equation.

7. Katsuhide Kita says:

Is the equation for number of baffles “NB” correct?
“Bc” in equation[NB = 1 + (int)(L – 2LS – LBin – LBout ) / (Bc/100)] is baffle cut %. I think that the center baffle spacing “LBc” is correct. Actually, “LBc” is using in spreadsheet. But the calculation for “NB” in this spreadsheet may be not correct,too. I think it is not “(Bc/100)” but “(LBc) in equation and it is not “LBc/100” but “LBc/1000”.

1. CheGuide says:

Thanks for finding it, I have corrected it in the spreadsheet.

1. Katsuhide Kita says:

Thank you for your reply. I undestand that abbrevation “B” means the central baffle spacing in this text. But the abbrevation of the central baffle spacing is “LBc” in spreadsheet. I think this is slightly confusing.

8. Katsuhide Kita says:

One more comment. Is the equation for “Overall H.T.C Dirty (UDirty)” in spread sheet correct? Equation is [= 1/(1/Uclean + “Tube Side Fouling Factor” + “Shell Side Fouling Factor”)] I think there is no correction of tube diameter for the tube side fouling factor and it is not “Tube Side Fouling Factor” but “(Tube Side Fouling Factor) x (Do / Di)”.
Anyway your information in this site was very useful for me. Thank you very much.