Table A2
Details of validation of the different thermodynamic packages in simulation of the existing NGL plant.
| Parameter | Current value | PR | Error (%) | Mod. PR | Error (%) | SRK | Error (%) |
|---|---|---|---|---|---|---|---|
| Temp. of 52 (°C) | −35.00 | −36.30 | 3.70 | −36.02 | 2.91 | −35.28 | 0.79 |
| Temp. of 54 (°C) | −66.80 | −66.96 | 0.24 | −66.70 | 0.15 | −65.94 | 1.29 |
| Temp. of 56 (°C) | 16.20 | 17.31 | 6.87 | 16.82 | 3.83 | 16.34 | 0.86 |
| Temp. of 58 (°C) | 36.30 | 37.71 | 3.89 | 37.88 | 4.35 | 36.28 | 0.04 |
| Temp. of 63 (°C) | 8.70 | 7.69 | 11.65 | 7.74 | 11.06 | 7.30 | 16.06 |
| Temp. of 64 (°C) | 104.60 | 104.50 | 0.10 | 104.61 | 0.01 | 104.59 | 0.01 |
| Temp. of 86 (°C) | 89.50 | 91.62 | 2.37 | 91.70 | 2.46 | 90.70 | 1.45 |
| Temp. of 91 (°C) | 60.00 | 60.36 | 0.60 | 60.34 | 0.57 | 59.96 | 0.07 |
| Temp. of 248 (°C) | −87.20 | −87.10 | 0.12 | −87.13 | 0.08 | −86.63 | 0.65 |
| Flow of 58 (kmol hr−1) | 1729 | 1709 | 1.19 | 1695 | 1.92 | 1775 | 2.62 |
| Flow of 63 (kmol hr−1) | 954 | 924 | 3.15 | 909 | 4.63 | 989 | 3.74 |
| Flow of 91 (kmol hr−1) | 920 | 938 | 2.02 | 939 | 2.08 | 938 | 1.98 |
| C5+ content of 89 (%mol) | ≤0.0032 | 0.0120 | 275.72 | 0.0019 | 0.00 | 0.0119 | 272.79 |
| Deethanizer cond. duty (kW) | 4020 | 3585 | 10.83 | 3548 | 11.47 | 3545 | 11.83 |
| Depropanizer cond. duty (kW) | 11 980 | 11 744 | 1.97 | 11 759 | 1.85 | 11 805 | 1.46 |
| Debutanizer cond. duty (kW) | 6500 | 5532 | 14.89 | 6338 | 2.49 | 5546 | 14.68 |
| Demethanizer reb. duty (kW) | 3450 | 3648 | 5.75 | 3568 | 3.43 | 3016 | 12.57 |
| Deethanizer reb. duty (kW) | 7670 | 7253 | 5.43 | 7182 | 6.36 | 7499 | 2.23 |
| Depropanizer reb. duty (kW) | 11 430 | 11 093 | 2.95 | 11 112 | 2.78 | 11 116 | 2.74 |
| Debutanizer reb. duty (kW) | 4695 | 3878 | 17.41 | 4686 | 0.19 | 3867 | 17.64 |
| Average error (%) | 18.54 | 3.13 | 18.28 |