Process Intensification and Integration for Sustainable Design. Группа авторов

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Process Intensification and Integration for Sustainable Design - Группа авторов


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>87 7.50 2 81–87 28.33 3 75–81 28.33 4 69–75 28.33 5 <69 7.50
Composition (mol%) Feed #1 Feed #2 Feed #3 Feed #4 Feed #5
Methane 94.11 83.62 77.78 71.94 56.34
Ethane 2.59 7.54 9.42 11.55 16.13
Propane 0.02 4.68 7.26 9.60 16.06
n‐Butane 0.25 2.11 2.65 3.15 4.96
i‐Butane 0.26 1.08 1.27 1.61 2.62
n‐Pentane 0.02 0.30 0.60 0.82 1.60
i‐Pentane 0.03 0.30 0.53 0.76 1.44
Neopentane 0.00 0.00 0.00 0.02 0.04
Carbon dioxide 2.71 0.38 0.49 0.56 0.81
Composition (mol%) HA feed
Methane 74.35
Ethane 9.00
Propane 6.94
n‐Butane 2.54
i‐Butane 1.22
n‐Pentane 0.57
i‐Pentane 0.51
Neopentane 0.00
Carbon dioxide 4.78
Hydrogen sulfide 0.10

      2.4.2 Process Simulations and Economic Evaluation

      The simulation results were then used to size process equipment, develop mass and energy balances, and determine operating conditions and utility consumption of process equipment. Aspen process economic analyzer [25] was used to estimate the equipment purchase costs. The Hand factor was utilized to account for installation and other costs. The fixed capital investment (FCI) for each processing unit was then estimated [26].

      (2.1)equation

      where FCIi, fixed capital investment for a given processing unit; images, Hand factor for equipment q; and images, the purchased cost of equipment q.


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Parameter Values Units References
Variable cost parameters
TEG price 0.93 $/lb [27]