Hi,
I've yet to find a straightforward way to transform the following data

TS (g kg−1)      527.13 ± 7.47
VS (g kg−1)      521.52 ± 7.70
TKN (g kg−1)      10.75 ± 0.11
NH4+–N (mg kg−1)      274.51 ± 77.64
Proteinεκτιμώμενη (g kg−1)      65.48
Fatsoxtec (g kg−1)      432.07 ± 4.80
COD (g kg−1)      1356.03 ± 21.66
CODestimated (g kg−1)      1363.66
Flow (m3/d) 1000

to ADM1 input

Ssu = monosacharides (kg COD/m3)
Saa = amino acids (kg COD/m3)
Sfa = long chain fatty acids (LCFA) (kg COD/m3)
Sva = total valerate (kg COD/m3)
Sbu = total butyrate (kg COD/m3)
Spro = total propionate (kg COD/m3)
Sac = total acetate (kg COD/m3)
Sh2 = hydrogen gas (kg COD/m3)
Sch4 = methane gas (kg COD/m3)
Sic = inorganic carbon (kmole C/m3)
Sin = inorganic nitrogen (kmole N/m3)
Si = soluble inerts (kg COD/m3)
Xc = composites (kg COD/m3)
Xch = carbohydrates (kg COD/m3)
Xpr = proteins (kg COD/m3)
Xli = lipids (kg COD/m3)
Xsu = sugar degraders (kg COD/m3)
Xaa = amino acid degraders (kg COD/m3)
Xfa = LCFA degraders (kg COD/m3)
Xc4 = valerate and butyrate degraders (kg COD/m3)
Xpro = propionate degraders (kg COD/m3)
Xac = acetate degraders (kg COD/m3)
Xh2 = hydrogen degraders (kg COD/m3)
Xi = particulate inerts (kg COD/m3)
scat+ = cations (metallic ions, strong base) (kmole/m3)
san- = anions (metallic ions, strong acid) (kmole/m3)

any suggestions?

Hi

I have almost the same problem, I am working with stillage from distillation of sugar cane, but I have few measures:

DQO 35900mg/l
DBO 6210mg/l
Nitrogen  574mg/l
Phosphorus  436,84mg/l
SS.   22,98mg/l
TS 308mg/l
TSS 46 mg/l

Is there any approximation that i can use?
What simple measure I should do?

Thanks

Thanks

I will consider COD = 100% degradable and 100% soluble.

BendelBoy wrote on Jun 26^th, 2012, 2:03pm:


I am following you valuable advices but I think I have small problem with results interpretation

BOD5      32747      mg/l
VS              34924      mg/l
COD              80310      mg/l
ΤΝ                4870      mg/l


1) Case 1
What I am doing is breaking COD to X_ch, X_pr, X_li and  X_I,
next all TN => Sin (kmol/m3)
I disregard tottaly VS

Following this i have accepted biogas production (within bibliographical data), but VFA destruction is almost 22% and not whithin the 40~60% as it should be. Also, I have ~90% total COD destruction (while I think it should be 40-70%)

2) Case 2
I am not breaking COD at all, instead assign  COD = Xc = composites (kg COD/m3)

Following this i have double biogas production (not according to bibliographical data)

3) Case 3

I am not breaking COD at all, instead assign  1/2 COD = Xc = composites (kg COD/m3)
and VS to Sac = total acetate (kg COD/m3)

Following this i have triple biogas production (not according to bibliographical data)

I am attaching my results printout for case 1. Your opinion would be really great
thanks
https://www.dropbox.com/s/aemxqsg8g1r7q43/case1.txt

ADM1 is probably the best readily-available anaerobic digester model.

Of digester models that would predict the methane content I am aware of

Mosey - poorly documented for calibration; difficult to set up and run reliably
Droste - fairly simple
Siegrist - no experience
Vavilin's - seemed to have the have same problems of getting to run reliably when we used it, back in the days when it was available as a DOS program
Various units in GPS-X: no real experience; one is in the Droste mould, another in the ADM1 mould
Biowin - no experience; documentation does not let you know fully what processes are modelled

and then ADM1

widely used; free MATLAB implementation available; I have used the STOAT version which (mostly) produces sensible results, and seems easier to use than the Mosey model, and more realistic than the Droste. ADM1 used in various academic projects looking at food, food & sewage, and agricultural waste anaerobic digestion.

Not easy to see a good reason why not to start with ADM1 and look at alternatives only after deciding that ADM1 is not suitable - either through being too complex (try Droste) or not including processes important to you (such as sulphur or phosphorous cycles)

Have you purchased Simulink?

Have you set your working directory to the folder holding all the ADM1 files?

Those are the two most likely explanations I can think of.

Hi

I'm having problems with my characterization of the effluent to the ADM1 model.

I am able to run the model and data from other articles answers are accurate, but still can not define a right strategy for the characterization of the effluent.

I tried to use the strategy that Zaher used, but I think that is best suited for solid waste. I wonder what the best strategy and if there is something new in the field to implement the characterization directly to ADM1.

Thanks

I got this results from analyzes:
COD                 50000 mg/l
BOD                 20000 mg/l
Nitrogen              1000 mg/l
Phosphorus          250  mg/l
Total Solids         308 mg/l

I tried break the COD to X_ch, X_pr, X_li and  X_I, next all TN => Sin (kmol/m3)

But didn't work.

I would like a better strategy to put the data in the correct manner.

My effluent is vinasse(stillage) from a small scale distillery working with sugar cane.

Would require more analysis of this effluent to the best use of ADM1?
Thanks

I tried to use your chacterization and I have better results.

I would to receive some references to try another ways.

Thanks a lot.

Hello

The characterization of the effluent has been made ​​and the inoculum also some doubts, but followed the usual made ​​for effluent characterization.

I wonder if anyone has worked with the manipulation of time of detention or retention time. If yes, where the manipulation was done, because I'm doing this, but I did not find corroborating article or work with this manipulation.

Thanks a lot

Hell

I just change the input flow, leaving the fixed volume in the volume of the reactor experiment.

But now I'm working on a reactor that different. It is a UASB reactor, but has recirculation, so I thought if would simulate a retention time different from what is done usually.

Because the input flow is always the same, and the reactor volume as well, just vary the amount of time the reactor is recirculating the same volume.

Sorry if it is hard to understand.

Thanks a lot

Hi Everyone
I too am working on an ADM1 implementation.
I have started by attempting to replicate Ulf's work in Matlab following the equations and data given in the 'Aspects on ADM1 Implementation within the BSM2 Framework' paper. I have gone over it a few times now and am not getting the same output as Ulf.
I am trying to use the ode15s solver in Matlab. I am using the S_h+ solver but not the Sh2 solver at this point as I am getting relatively quick solving speeds as it is.

I am unsure about the initial conditions, particularly those related to initial gas concentrations (Sgas,h2/ch4/co2) pressures, and ion concentrations. Can somebody point me in the right direction with these? I currently have them set to 0 (which causes an initial negative q_gas).

As far as I can see, my equations and variables are exactly the same as Ulf so it is frustrating I cannot move past this point.

BendelBoy - I made your suggested adjustments to my initial conditions without success - I still end up with the same equilibrium outputs.

I think you are right - there must be an issue somewhere in my program. I will try contacting Ulf.

Just some extra details: I have gotten rid of the mexmac files and have the correct ones now. When I go to run Simulink, I get the error:
Error evaluating parameter 'VariableName' in 'ADM1_R14/From Workspace'

Caused by:
   Not enough input arguments.

Does anyone know how to fix this?

Hello all,

I am a student researcher learning modelling of wastewater treatment. I would be grateful if anyone could provide me ADM1 MATLAB files.

Thanks!