CO2 removal from Amine plant

[get...jung]

Who can help me please?? I have any question from hysys simulation. In sample from hysys simulation there have amine plant (G1) but when I change composition in sour gas it can not simulate I don't understand. my ploblem is: I want to remove CO2 from feed gas(Sour gas) from round 50% to 5% in sweet gas(top of absorber) and new composition are
c1 44.64% mole
c2 6.48%
c3 2.96%
i-c4 0.62%
n-c4 0.72%
i-c5 0.24%
n-c5 0.16%
c6 0.08%
c7 0.04%
co2 40.49%
n2 3.57%

thank you for your answer.

[cristianciornei]

Who can help me please?? I have any question from hysys simulation. In sample from hysys simulation there have amine plant (G1) but when I change composition in sour gas it can not simulate I don't understand. my ploblem is: I want to remove CO2 from feed gas(Sour gas) from round 50% to 5% in sweet gas(top of absorber) and new composition are
c1 44.64% mole
c2 6.48%
c3 2.96%
i-c4 0.62%
n-c4 0.72%
i-c5 0.24%
n-c5 0.16%
c6 0.08%
c7 0.04%
co2 40.49%
n2 3.57%

thank you for your answer.

I had a similar problem.
There is a bug that works like this:
when you add in component list ammonia (NH3), even if the NH3 composition is set to 0.0, the results are poor.
Removing ammonia from component list gives acceptable results.

Check your simulation without N2.
Just remove it from component list.
Run it again and observ results.

And of course give me feedback

Best regards

[guga23]

which version of hysys are you using?. v2006 has an fuildpackage for amine, but if you are using win vista you need v2006.5. Before I had a problem with trying to taking water off the natural gas using TEG, the problem was that there wasnt an fluidpackage for that, so the result were all wrong (new version has an fluidpackage for that)

[omli]

dear...get

the probleme here is the " le taux de charge" tau = mole de MEA/mole de CO2, in general it is taken between 0.3-0.5 mole de CO2/mole de MEA, you must calculat the the amount of CO2 in the sour gas (feed) in mole and then you have to calculate the required quantity of MEA pure and then set it to about 15% pd (pd:masse).
1/ calculate the total quatity of co2 in feed gas
2/ use Tau of 0.45 and determine the amount of pure MEA needed ( each mole of MEA can absorbe 0.45 mole of CO2) EXEMPLE /
if you have 1000 mole of CO2 you need 1000/0.45 = 2222.22 mole of MEA = 2222.22*61.08 mol/g = 135.73 kg of MEA

3/ prepare a solution of 15 % of pour mea

from the same exemple
135.73 represente 15% ==> 100 % = 904.86 kg

then you need 904.86 kg of a solution of 15% pd MEA
4/ tray number must be calculated or began by using 15trays and see if not ok add one and see you swt gas composition .......repeat unitil satisfied

if you want send me your simulation data completly and i help you
if you understand frensh it will better to comunocate (my english is bad)

[get...jung]

thank you everybody for your answer I will try to simulation by follow from reccommend

[get...jung]

cristianciornei: i have to already change simulation by without n2 but still can not simulation.
guga23: i use hysys 3.2 for sim. and this version have amine pkg.
omli: can you send your email to me? may be help me for simulation (my enlish same you)

thank a lot everybody
my email: get_en39@hotmail.com

[omli]

dear get jug, it it not a solution when removing N2, before making simulation you must prepare a good database, in a proper sheet, all data needed by the program must be put correctly, and fix your trajet, a premlemenary caculations are always needed , try other think but not modifying the composition !!!, try to encrease MEA concentration, or flow rate or the tray number, and do not touch in many variables at the same time you, try one and observe changes...

send me you problem l :lagah_omar@yahoo.fr

[get...jung]

omli;
now i can solve that problem but i have new problem, maximum flowrate which it can simulate in sour gas is 6 mmscfd. i want to increase flowrate to 25-50 mmscfd. how do i do? ( i already increase tray no., increase tray dia. but still cannot simulate) and i use model G-1 in sample folder from hysys 3.2 version.

thank you very much for help me.
get...jung

[kp2008]

Hi brother,

From your simulation, about the CO2 remove process for a small plant, I think the membrane process is really suitable for CO2 remove for 2-100 MMscfd as well, Now i design on this process for 150 MMscfd and process is low price than amine (the oldest technology)

Before process will be simulated, you should take the e-book about this process to clarify before, and then you is to be the best on this process,

Cheers
Pang ChE#14

[omli]

dear get..jung

the tray number is funcion of the the efficiency of the column, if you want a hight purty of sweet gas ( CO2 remaining is very small quantity ) increase the it, it is possible that the column will converge but the quantity of XO2 i the sweet gas remains important so you have to increase the tray number until reaching the value desired of CO2 in sweet gas, generally the number of trays in such process is about 22 to 28 trays,

for the diameter it is function of the velocity of gas inside the column Q = V*A

you have tu uses the tray sizing utility from tool==>utilities==>tray sizing ==> select TS ==>choose your absorber .

choose auto selection == choose the tray to use (sieve) = in the spec tab you find the tray diameter which is the column diameter you find also the tray spacing you can use it to determine the column high L = nuber of trays * tray spacing.

if the diameter is very large > 3m you have to devid (by 2) the total flow rate of the sour gas and propotional rate of calculated MEA solution, use again the tray sizing utility if ok your conclusion is that this feed of gas must be treated in two parallel train. else try three equal part ......

send me more details and i can do it for you and than w compare our results

[get...jung]

Thank you vary much P' Pang. I will try by myself before. If it can not I will ask you for guideline again.
(My simulation is rough sizing, then I have to simulate by use G-1 from Hysys 3.2)

[rooky2000]

Anybody has AMSIM V7.3 ?