Modelling of two phase flow in packed bed using conservation equations

[casualguitar]

Just as a side note to the above, this is what I see as potential 'next steps' to follow in regards to model development:

1. Heat transfer inside the energy storage particles (assuming possible temperature profile inside spherical particles)
2. Splitting of U value into conduction/convection terms
3. Specification of bed flow direction (horizontal or vertical)
4. Pressure gradient (Ergun)
5. Modelling of radial heat transfer (cant be measured/verified in practice unfortunately) but still might be interesting

 

[Chestermiller]

Apologies yes it does vary. Zoomed in plot of enthalpy versus temperature for the two phase region, showing the temperature increase of approx 2-3C :
View attachment 296250

Effectively. The exact mole% breakdown is: N2 = 78.08, O2 = 20.95, Ar = 0.97%
The Argon boiling point falls between that of N2 and O2 so our assumption of a single boiling point rather than an envelope is valid still

Vapour-liquid split (molar) vs enthalpy (J/mol)
View attachment 296251

Enthalpy units: J/mol
Density units: kg/m3

Yes the units are not of the same basis, however I just picked kg/m3 units for the density plot as its easiest to visualise. Are there preferred units? I can provide either easily

Note also these plots are not packed bed related model output plots just plots of various properties of air as a function of enthalpy and pressure

If there is any other enthalpy/pressure dependent info required at this point I can provide it

OK. If you're happy, I'm happy.

For the d(rho)/dH, this comes from the d(rho)/dt term for a tank. Since rho is now a function of H and P, strictly speaking there should be contributions from d(rho)/dH and d(rho)/dP. However, I think that the latter is not going to contribute significantly, and can be neglected. Besides, we are not directly calculating dP/dt for each tank (although, I suppose it can be lagged one time step).

 

[Chestermiller]

Just as a side note to the above, this is what I see as potential 'next steps' to follow in regards to model development:

1. Heat transfer inside the energy storage particles (assuming possible temperature profile inside spherical particles)

I don't think this will be worthwhile, and that the effect can be included in the overall U (which will be a calibration parameter anyway).

1. Splitting of U value into conduction/convection terms

Same point here.

1. Specification of bed flow direction (horizontal or vertical)
2. Pressure gradient (Ergun)
3. Modelling of radial heat transfer (cant be measured/verified in practice unfortunately) but still might be interesting

I guess you mean heat loss from the overall bed. If the bed is well insulated, this won't be too important, but can be included later if necessary.

What about looking at heat transfer coefficient correlations U for fluid flow packed beds?

 

[casualguitar]

For the d(rho)/dH, this comes from the d(rho)/dt term for a tank. Since rho is now a function of H and P, strictly speaking there should be contributions from d(rho)/dH and d(rho)/dP. However, I think that the latter is not going to contribute significantly, and can be neglected. Besides, we are not directly calculating dP/dt for each tank (although, I suppose it can be lagged one time step).

Great

So to get an analytic solution for d(rho)/dH, is it correct to say that you're suggesting using our existing d(rho)/dt, which is dm/dt divided by volume (?), and then using our existing dH/dt to get:
$$\frac{d\rho}{dH} = \frac{d\rho}{dt} * \frac{dt}{dH}$$

Or if not, then we have analytic solutions for a number of property derivatives (post #343) that might be useful?

What about looking at heat transfer coefficient correlations U for fluid flow packed beds?

Sounds good. Referring to your post above, you mentioned U will be used as a tuning parameter once experimental data is generated. I guess if we use correlations for U for fluid flow packed beds, one of the correlation parameters will then be 'tuned' rather than U itself? (I think this will become clear anyway once I start looking). I have a few papers in mind. I'll start looking into this.

Modelling of radial heat transfer (cant be measured/verified in practice unfortunately) but still might be interesting

Lastly here what I meant was that the packed bed is a cylinder, so we could assume that there will be a temperature gradient in the radial direction also

Just as another side note - the ultimate goals here are to assess the performance of a packed bed to store thermal energy (using liquid air as a medium), to verify the model with experimental data and to publish the findings

I'll spend some time on the heat transfer coefficient correlations this evening

And again thanks for all your guidance on this. Its been of huge importance to me

 

[casualguitar]

Side note - two phase (liquid/gas) packed bed papers seem to be very rare. I have found a useful pair of papers by the same authors though that model steam condensing in a packed bed:
https://link.springer.com/article/10.1023/A:1016271213503
https://link.springer.com/article/10.1007/s11242-004-5740-5

I'll be reading through these tomorrow and hopefully extracting useful heat transfer coefficient info

 

[Chestermiller]

Great

So to get an analytic solution for d(rho)/dH, is it correct to say that you're suggesting using our existing d(rho)/dt, which is dm/dt divided by volume (?), and then using our existing dH/dt to get:
$$\frac{d\rho}{dH} = \frac{d\rho}{dt} * \frac{dt}{dH}$$

Or if not, then we have analytic solutions for a number of property derivatives (post #343) that might be useful?

No. In the mass balance equation, we had to provide a relationship for ##d\rho/dt##. This was done by expressing it as $$\frac{d\rho}{dh}\frac{dh}{dt}$$. ##d\rho/dh## comes exclusively from the thermodynamics.

Sounds good. Referring to your post above, you mentioned U will be used as a tuning parameter once experimental data is generated. I guess if we use correlations for U for fluid flow packed beds, one of the correlation parameters will then be 'tuned' rather than U itself? (I think this will become clear anyway once I start looking). I have a few papers in mind. I'll start looking into this.

You are trying to get a reasonable starting value for U based on literature correlations. Then you fine tune it for your system.

Lastly here what I meant was that the packed bed is a cylinder, so we could assume that there will be a temperature gradient in the radial direction also

If the bed is well insulated, this will approach zero.

 

[Chestermiller]

Side note - two phase (liquid/gas) packed bed papers seem to be very rare. I have found a useful pair of papers by the same authors though that model steam condensing in a packed bed:
https://link.springer.com/article/10.1023/A:1016271213503
https://link.springer.com/article/10.1007/s11242-004-5740-5

I'll be reading through these tomorrow and hopefully extracting useful heat transfer coefficient info

See also literature on 2 phase flow and immiscible flow in porous media. See for example Flow of Fluids Through Porous Materials by R. E. Collins.

 

[casualguitar]

You are trying to get a reasonable starting value for U based on literature correlations. Then you fine tune it for your system.

Got it

If the bed is well insulated, this will approach zero.

Yes it looks to be exceedingly well insulated

No. In the mass balance equation, we had to provide a relationship for dρ/dt. This was done by expressing it as dρdhdhdt. dρ/dh comes exclusively from the thermodynamics

Ok, so you're saying that ##\frac{d\rho}{dH}## comes from the thermodynamics. Does this mean we can use existing derivates to 'chain rule' to ##\frac{d\rho}{dH}##? Thermo library provides a number of these derivatives. Would any of the derivatives in post #343 be suitable here?

See also literature on 2 phase flow and immiscible flow in porous media. See for example Flow of Fluids Through Porous Materials by R. E. Collins.

Ah I have read some material by R.E. Collins. It actually may have been sections of this text. I'll take a look at this today for info on heat transfer coefficient correlations

 

[Chestermiller]

Ok, so you're saying that ##\frac{d\rho}{dH}## comes from the thermodynamics. Does this mean we can use existing derivates to 'chain rule' to ##\frac{d\rho}{dH}##? Thermo library provides a number of these derivatives. Would any of the derivatives in post #343 be suitable here?

Just evaluate it as drho/dT divided by dH/dT at constant P and overall mixture.

 

[casualguitar]

Just evaluate it as drho/dT divided by dH/dT at constant P and overall mixture.

Hmm to confirm - drho/dT is found by (1/V)*dm/dt and we get dH/dt values from the energy balance. Then d(rho)/dH = d(rho)/dt * dt/dH

Two questions on that -
1) We will be calculating d(rho)/dt, an expression that depends on dm/dt while dm/dt itself depends on d(rho)/dt also. Do I need to calculate d(rho)/dH values at time j, from d(rho)/dt and dt/dH values at time j-1?
2) Leading on from that, at time t=0 we don't seem to have values for either of these. Can I Assume both derivates = 0 at t=0?

I can code this if the above is all true

Side note: I didn't find anything useful in the R.E. Collins text in relation to heat transfer coefficient correlations. That said, its fairly advanced in parts so maybe I missed it. I did find this text that gives correlations for both the thermal conductivity and the fluid-solid heat transfer coefficients: https://www.sciencedirect.com/science/article/pii/001793109090255S

I think that was actually a reason why other papers split up the U heat transfer coefficient, because there are correlations available for k and h

I'll put a shape on what that paper is saying in relation to heat transfer coefficients and see If its of any use

If it is, if possible I would like to talk with you about extracting conduction and convection terms out of U

 

[Chestermiller]

Hmm to confirm - drho/dT is found by (1/V)*dm/dt and we get dH/dt values from the energy balance. Then d(rho)/dH = d(rho)/dt * dt/dH

No. To get ##\frac{dm_j}{dt}=\frac{V}{n}\frac{d\rho_j}{dt}##, we write $$\frac{d\rho_j}{dt}=\left(\frac{\partial \rho}{\partial h}\right)_{j,P}\frac{dh_j}{dt}$$and $$\frac{\partial \rho}{\partial h}=\frac{\frac{\partial \rho}{\partial T}}{\frac{\partial h}{\partial T}}$$with the latter obtained strictly from the thermodynamics.

Side note: I didn't find anything useful in the R.E. Collins text in relation to heat transfer coefficient correlations.

The Collins book has information on immiscible flow through porous media, and relative permeabilities, which provide a better estimate of the pressure gradient in the 2 phase region.

That said, its fairly advanced in parts so maybe I missed it. I did find this text that gives correlations for both the thermal conductivity and the fluid-solid heat transfer coefficients: https://www.sciencedirect.com/science/article/pii/001793109090255S

I think that was actually a reason why other papers split up the U heat transfer coefficient, because there are correlations available for k and h

I'll put a shape on what that paper is saying in relation to heat transfer coefficients and see If its of any use

If it is, if possible I would like to talk with you about extracting conduction and convection terms out of U

In my judgment, you should consider the conduction as just lumped in with the convection, since, in the end this is all going to involve calibration with respect to the convection dispersivity (grid spacing).

 

[casualguitar]

No. To get dmjdt=Vndρjdt, we write dρjdt=(∂ρ∂h)j,Pdhjdtand ∂ρ∂h=∂ρ∂T∂h∂Twith the latter obtained strictly from the thermodynamics.

Ah I follow now. Great. This is now implemented in the model also. The temperature derivatives are available in the thermo library so I used those. So now we have analytic solutions for all of d(rho)/dH, T(H.P) and rho(H,P), meaning that there are no hand derived correlations in use

The Collins book has information on immiscible flow through porous media, and relative permeabilities, which provide a better estimate of the pressure gradient in the 2 phase region.

Interesting, I see those sections. Actually right now pressure is not varying across the bed in the model. To implement that I guess I'd have the Ergun equation for the gas and liquid phases, and sum the pressure drops across each. I hadn't considered the two-phase zone as its so small. I will look into modelling the two-phase pressure drop via the Collins relative permeability approach

In my judgment, you should consider the conduction as just lumped in with the convection, since, in the end this is all going to involve calibration with respect to the convection dispersivity (grid spacing).

Next most important job on my end is to get a ballpark range for the U value. I understand what you mean about lumping convection and conduction, however getting correlations for a lumped term has proved difficult. I did not actually find any. There are a few options for non-lumped models though where conduction and convection are separate. Do you think it is reasonable to use the non-lumped model on the basis that there are obvious correlations available? Have you seen correlations for lumped conduction and convection?

since, in the end this is all going to involve calibration with respect to the convection dispersivity (grid spacing).

Not sure what convection dispersivity is. I'll take note of it and we can return to it when the time comes

 

[casualguitar]

Just as a side note - I have found a few papers that talk about Nusselt number correlations. This is obviously closely related to the actual U value, so if there was a way to convert Nusselt number to U value then we could use that approach. The only equation that comes to mind is ##Nu = \frac{hL}{k}## however again this is in effect splitting the U value into conduction and convection it seems

Final update on this - I just found a paper that does lump convection and conduction for two phase flow, and it seems to do it in a way that would slot nicely into our model. Here is the section on lumping h and k:

Does this look suitable to you? If it is then I can code this, it looks straightforward

Link to paper if you're interested (actually a very nice paper): https://aiche.onlinelibrary.wiley.com/doi/abs/10.1002/aic.690250413

Also as a note, the Prandtl and Reynolds number will not be constant, meaning that U (or h in this model) will not be constant across the system

 

[Chestermiller]

Final update on this - I just found a paper that does lump convection and conduction for two phase flow, and it seems to do it in a way that would slot nicely into our model. Here is the section on lumping h and k:

View attachment 296361
View attachment 296362

Does this look suitable to you? If it is then I can code this, it looks straightforward

Link to paper if you're interested (actually a very nice paper): https://aiche.onlinelibrary.wiley.com/doi/abs/10.1002/aic.690250413

Also as a note, the Prandtl and Reynolds number will not be constant, meaning that U (or h in this model) will not be constant across the system

Yes. This is what I had in mind. That reference looks a little old, so maybe you can find some more recent work that could be even more accurate.

 

[Chestermiller]

https://www.google.com/books/editio...AQBAJ?hl=en&gbpv=1&pg=PA1&printsec=frontcover

Also, Google "Heat Transfer in Porous Media"

Also see section 14.5 Heat transfer coefficients for Forced Convection Through Packed beds, Transport Phenomena, Bird et al.

 

[casualguitar]

Yes. This is what I had in mind. That reference looks a little old, so maybe you can find some more recent work that could be even more accurate.

I think I can. That paper actually has 400+ references so its fairly well cited. Google scholar allows viewing of all papers that referenced that one, so I guess at least one of the more modern ones will use a similar lumped approach

https://www.google.com/books/editio...AQBAJ?hl=en&gbpv=1&pg=PA1&printsec=frontcover

Ah very interesting, there's really fairly endless things that could be implemented in the model. Its difficult to draw a line in what is useful and what isnt.

Actually section 12.5 here 'Moving evaporation of condensation front' looks particularly useful. I guess this is the section you were pointing towards? The only issue with these is that they use different model equations to the ones we have, so its rarely directly applicable in our model I would guess

Also see section 14.5 Heat transfer coefficients for Forced Convection Through Packed beds, Transport Phenomena, Bird et al.

I can compare the output from this approach to the lumped parameter model I found in that old paper

Looks like I have some heat transfer coefficient model implementation work to do

 

[Chestermiller]

I think I can. That paper actually has 400+ references so its fairly well cited. Google scholar allows viewing of all papers that referenced that one, so I guess at least one of the more modern ones will use a similar lumped approachAh very interesting, there's really fairly endless things that could be implemented in the model. Its difficult to draw a line in what is useful and what isnt.

Actually section 12.5 here 'Moving evaporation of condensation front' looks particularly useful. I guess this is the section you were pointing towards?

Not really. I never saw the entire book. I was focused on the possible correlations for convective heat transfer.

The only issue with these is that they use different model equations to the ones we have, so its rarely directly applicable in our model I would guess

I can compare the output from this approach to the lumped parameter model I found in that old paper

Not in the bed model. I strongly recommend making the comparisons off-line, looking at comparison plots of Nu vs Re at constant values of Pr.

 

[casualguitar]

Hi Chet, just updating to say I'm working through some small model issues (no convergence in some cases). Will update you once these have been solved

EDIT: The error is actually that I have set up the code for the ICs/BCs incorrectly it seems. Working through this

EDIT2: At some point in this code I am setting an incorrect condition (IC or BC). I'm actually not fully sure on the ICs/BCs. Could I possibly post the code here with comments to show my thoughts?

 

[casualguitar]

Hi Chet, bug found! The model itself is fine now. The last remaining issue seems to be with d(rho)/dH.

So, you mentioned using d(rho)/dT and dH/dT to get d(rho)/dH. If you see post #343, the library I’m using provides both of these derivatives, however, it specifies that the there must be some property that remains constant when the derivative is taken (Gibbs energy, internal energy, helmholtz energy,etc). I randomly picked constant enthalpy for both derivatives, however, the results vary widely depending on what property is constant so it is actually important that the derivative picked is the correct one.

With reference to post #343, what derivative should be used? i.e. what property (or properties) remain constant through these derivatives?

 

[Chestermiller]

Hi Chet, bug found! The model itself is fine now. The last remaining issue seems to be with d(rho)/dH.

So, you mentioned using d(rho)/dT and dH/dT to get d(rho)/dH. If you see post #343, the library I’m using provides both of these derivatives, however, it specifies that the there must be some property that remains constant when the derivative is taken (Gibbs energy, internal energy, helmholtz energy,etc). I randomly picked constant enthalpy for both derivatives, however, the results vary widely depending on what property is constant so it is actually important that the derivative picked is the correct one.

With reference to post #343, what derivative should be used? i.e. what property (or properties) remain constant through these derivatives?

drho/dH is at constant pressure, and dH/dt is at constant tank number.

 

[casualguitar]

drho/dH is at constant pressure, and dH/dt is at constant tank number.

Perfect I had switched to that in the meantime

Ok so it looks like next is to implement the U value model, which as you say looks like it will be a lumped parameter model. I'll use the correlation I found in that 70s paper unless your reference below has something more suitable

Also see section 14.5 Heat transfer coefficients for Forced Convection Through Packed beds, Transport Phenomena, Bird et al.

And lastly yes:

looking at comparison plots of Nu vs Re at constant values of Pr.

These plots should be fine to make

Will be working on this this evening

 

[casualguitar]

Perfect I had switched to that in the meantime

Ok so it looks like next is to implement the U value model, which as you say looks like it will be a lumped parameter model. I'll use the correlation I found in that 70s paper unless your reference below has something more suitable

And lastly yes:

These plots should be fine to make

Will be working on this this evening

Hi Chet, back working on this model this evening. I will be working on the Nu vs Re plots (the U correlation) first thing tomorrow. Will update here with results.

I was curious - now that we seem to be out of the woods on this model, do you think there is value in taking an existing model and recreating it?

For example, the paper that provided the lumped heat transfer coefficient correlation seems to provide a two phase model also. I'll link the paper below, however these are the model equations:

Link to paper: https://aiche.onlinelibrary.wiley.com/doi/abs/10.1002/aic.690250413

My question is just do you think there is value in either:
1) comparing this model with the model you developed in this post
2) replacing our model with this one

 

[casualguitar]

Hi Chet, plot of T vs U using the above reference. Looks like U will vary from 9970+/-30 across our range of temperatures (I thought this seemed high so I checked it versus some known values and it looks ok) :

In addition, here is a plot of Re vs Nu for some constant values of Pr. I checked the range of Pr values we got for the above plot, and just picked 5 evenly split across the range of Pr values. Here it is:

If the above looks ok to you I'll include this U functionality in the main model!

 

[Chestermiller]

Hi Chet, back working on this model this evening. I will be working on the Nu vs Re plots (the U correlation) first thing tomorrow. Will update here with results.

I was curious - now that we seem to be out of the woods on this model, do you think there is value in taking an existing model and recreating it?

For example, the paper that provided the lumped heat transfer coefficient correlation seems to provide a two phase model also. I'll link the paper below, however these are the model equations:

View attachment 297110

View attachment 297111
View attachment 297112
View attachment 297113
View attachment 297114
View attachment 297115Link to paper: https://aiche.onlinelibrary.wiley.com/doi/abs/10.1002/aic.690250413

My question is just do you think there is value in either:
1) comparing this model with the model you developed in this post
2) replacing our model with this one

For what it's worth, in my judgment, there is no value in doing either of these things. My feeling is that the model you have in hand will be an excellent tool for what you want to do. Your model contains many clever innovations that have never been used before.

Based on my many successful years of modeling experience in industry, I have rarely done things the exact same way that others have done them. The saying I have coined is "If you always do things the same way as everybody else, then you're the same as everybody else."

 

[Chestermiller]

Hi Chet, plot of T vs U using the above reference. Looks like U will vary from 9970+/-30 across our range of temperatures (I thought this seemed high so I checked it versus some known values and it looks ok) :
View attachment 297153

These are very large values of U. Are you sure of this. why is there a temperature dependence.

In addition, here is a plot of Re vs Nu for some constant values of Pr. I checked the range of Pr values we got for the above plot, and just picked 5 evenly split across the range of Pr values. Here it is: View attachment 297154

If the above looks ok to you I'll include this U functionality in the main model!

Is this from the Bird et al correlation? How are Re and Nu defined in this? Why are the Pr numbers so low? Did you also include a heat transfer resistance for inside the packing, like that other article I referred you to? The BSL correlation is only for the gas phase.

Please show the equations you used for this, and the comparison of the various correlations available in the literature.

You have provided me with inadequate information to arrive at a confident assessment of this.

Chet

 

[casualguitar]

For what it's worth, in my judgment, there is no value in doing either of these things. My feeling is that the model you have in hand will be an excellent tool for what you want to do. Your model contains many clever innovations that have never been used before.

Got it, and I agree. I would like to do a full model walkthrough at some point to check if I have missed any of your innovations (would be a pity if I missed any),like using l/2 to produce an upwind scheme etc. Also at some point this Spring I'll be working with a postdoc to tune this model to experimental data (and publish the results). I would like to have your name as a contributor on the paper (if this is ok with you)

Based on my many successful years of modeling experience in industry, I have rarely done things the exact same way that others have done them. The saying I have coined is "If you always do things the same way as everybody else, then you're the same as everybody else."

Well it takes a certain level of knowledge/ability (and cojones!) to go out on your own. One day I hope to get to this kind of level.

These are very large values of U. Are you sure of this. why is there a temperature dependence.

I will check these. The temperature dependence comes from the temperature dependent parameters in the Pr and Re equations (shown below)

Is this from the Bird et al correlation? How are Re and Nu defined in this? Why are the Pr numbers so low? Did you also include a heat transfer resistance for inside the packing, like that other article I referred you to? The BSL correlation is only for the gas phase.

Please show the equations you used for this, and the comparison of the various correlations available in the literature.

No its not from Bird et al, its from Dixon et al: https://aiche.onlinelibrary.wiley.com/doi/abs/10.1002/aic.690250413

The heat transfer coefficient model from this reference is this:

The Reynolds and Prandtl numbers are defined as:

Where k is the fluid thermal conductivity and G is the superficial mass flow rate. I checked that I was using the right units for these.

So the temperature dependence comes from the temperature dependent parameters (heat capacity, thermal conductivity of the fluid, viscosity of the fluid). Having these parameters as non-constant only seems to affect U by <0.5% anyway

So I will check the U and Pr to see if I've made any errors. Also to your question about having internal packing heat transfer resistance, I haven't thought about this. It doesn't seem to mention it in this reference, however it looks like this is the second term in equation 29?

Thanks and I'll get to checking the U/Pr calculations

 

[Chestermiller]

What is the void fraction in your packed bed?

 

[Chestermiller]

In terms of the Nusselt number and Reynolds number definitions in the BSL correlation, the Dixon et al correlation reads $$\frac{Nu}{Pr^{1/3}}=\frac{2.55}{\epsilon(1-\epsilon)^{1/3}\psi^{1/3}}Re^{2/3}\tag{1}$$where ##\psi## is a shape factor very close to 1.0. The maximum value of the term involving ##\epsilon## in this equation is 0.47, which corresponds to a minimum value of ##Nu/Pr^{1/3}## of: $$\frac{Nu}{Pr^{1/3}}=\frac{5.4}{\psi^{1/3}}Re^{2/3}\tag{2}$$This compares with the BSL correlation of $$\frac{Nu}{Pr^{1/3}}=2.19Re^{1/3}+0.78Re^{0.619}\tag{3}$$I'm going to prepare a log-log plot of these equations to see how they compare for a typical range of Re for packed beds running from 1 to 10000.

 

[Chestermiller]

The blue curve is Dixon et al correlation with ##\epsilon=0.75## (minimum curve over all ##\epsilon## values) and ##\psi=1.0 (spheres)##. The red curve is BSL correlation. These are based on BSL definitions of Re and Nu.

The Dixon correlation is 1.8X higher at the lower Re=1 and about 9X higher at Re = 10000. I recommend the BSL correlation which is much more modern, and based on much more data.

 

[casualguitar]

This compares with the BSL correlation of $$\frac{Nu}{Pr^{1/3}}=2.19Re^{2/3}+0.78Re^{0.619}\tag{3}$$

Would the first term be ##2.19Re^{1/3}##? As we will have ##Re * Re^{-2/3}##

The Dixon correlation is 1.8X higher at the lower Re=1 and about 9X higher at Re = 10000. I recommend the BSL correlation which is much more modern, and based on much more data.

So to use the BSL correlation, does this mean we would using the Nu/Re definitions in the BSL correlation to predict ##h_{fs}## from eq.30 (post #376), and then continuing to use eq.29 to predict h? If so I can code this up now

 

[Chestermiller]

Would the first term be ##2.19Re^{1/3}##? As we will have ##Re * Re^{-2/3}##

Yes, typo. Corrected.

So to use the BSL correlation, does this mean we would using the Nu/Re definitions in the BSL correlation to predict ##h_{fs}## from eq.30 (post #376), and then continuing to use eq.29 to predict h? If so I can code this up now

View attachment 297228

Yes. But the version I gave is better because it gives Nu directly

 

[casualguitar]

Yes, typo. Corrected.

Yes. But the version I gave is better because it gives Nu directly

One point of confusion - does the Dixon version not give Nu directly also via equation 30?

 

[Chestermiller]

One point of confusion - does the Dixon version not give Nu directly also via equation 30?

They use different definitions of Re and Nu than BSL

 

[casualguitar]

They use different definitions of Re and Nu than BSL

Ah got it, I'll replace the Dixon version with yours/the BSL one

Looking at how you set up your plots, you chose a range of Re numbers. To set up my plots above I actually chose a range of temperatures. I suppose choosing a range of Re values, to get a range of Nu values (at a few constant values of Pr), then subbing into eq.29 is better?

This would seem to mean that I would have to choose a single temperature/pressure value, and use the values of cp, mu, etc at these T/P values, which would assume that U is not temperature dependent. Is that correct?

I suppose I could choose 5 values of temperature (across the 80-300K range), and calculate the Pr number at each value of T. Then use these Pr values to create 5 graphs of Re vs Nu using your algorithm above? Is that reasonable?

 

[Chestermiller]

Ah got it, I'll replace the Dixon version with yours/the BSL one

Looking at how you set up your plots, you chose a range of Re numbers. To set up my plots above I actually chose a range of temperatures. I suppose choosing a range of Re values, to get a range of Nu values (at a few constant values of Pr), then subbing into eq.29 is better?

The objective of my plot was to compare the two correlations on a common basis. I don't care about anything else.

Eqn. 29 is for use inside the bed/tank model. There is a different U value for each tank in the model. The U value for each tank should be calculated within the bed/tank model. Given P, T, and ##G=\dot{m}/A## for a given tank, you calculate Pr and Re for the tank, then calculate U for that tank. This value of U also varies with time. Use the value of U at the beginning of the time step (end of the previous time step.)