4 replies to this topic

[rodolfoingeniero]

Hi Everybody,

I am trying to simulate an existing liquid LPG sweetening process by using Hysys liquid liquid extraction module. I am using Amine Pkg Li-Mather as property package selection.
The conceptual process is as follows:
A liquid LPG stream (@ 38 ºC and 23 kg/cm2g) 400 m3/day enters to an existing column and is sweetened by using a 200 m3/day solution of DEA 35% strength wt% as the absorbing medium.
I have spent too much time; however I have not been able to get convergence.
Has anybody simulated this kind of process?
Best Regards!

[Bobby Strain]

I always call Huntsman and they simulate the system with T-Sweet, a better simulator for this system.

Bobby

[rodolfoingeniero]

Thanks Bobby Strain.
Best Regards!

[mohamedreza]

Dear,
I’m process plant engineer. I’m working at a LPG rich Gas Plant which has a three high capacity of propane and butane primary sulphur (H2S, COS) and mercaptane removal (RSH). One month ago I led a master science thesis (just industrial points) about LPG treating by virtue of DEA. The simulation was done whole plant and completely detailed by AspenHysys 2006.5. I can attach my simulation results.
I can help you! However, I think that DEA with concentration of 35% wt increase some interactions in plant design and costing variables. Also, TSWEET package that is built in Promax 2, BR&E, and Aspen Plus handle the calculation of whole DEA plant. Are you sure about optimized Lean/Rich loadings? Note that composition of feed can determine your process variables and affect them! What is the feed composition? CO2, RSHs, H2S, COS, C1, C2, C3, C4, etc. Don’t trust laboratory data (as confirm for basic design mass balance document) about lean & rich loading because of 1- amine ionic strength, 2- degradation products, 3- and bad operation.

[rodolfoingeniero]

Hi Mohamedreza,

Thanks for your response.
According to your post, I understand you have successfully simulated the LPG sweetening process by using Aspen Hysys, haven´t you?
If so, could you please explain to me how did you simulate the liquid LPG sweetening by using Hysys liquid/liquid extraction module?

The process I want to study is a existing one in which a liquid stream of LPG is treated with DEA (35% wt) in a packed column. Temperature is 38 °C and pressure is 23 kg/cm2g.
The composition (kg/h) of LPG stream to be treated with DEA is as follows:

Methane: 3,08
Ethylene: 24,98
Ethane: 133,70
Propylene: 2.749,53
Propane: 3.173,17
1,3-Butadiene: 3,10
1-Butene: 261,58
C-2-Butene: 108,21
T-2-Butene: 201,68
I-Butene: 309,93
I-Butane: 1.347,71
N-Butane: 462,81
I-Pentane: 0,49
N-Pentane: 0,062
N-Hexane: 0,002
Hydrogen sulfide (H2S): 5,084
M-Mercaptane: 2,25
E-Mercaptane: 0,30
Water: 0


I will be looking forward to receiving your response.
Best Regards!