AIChE Symposium Series, Volume 91, Issue 304American Institute of Chemical Engineers, 1972 - Chemical engineering |
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Page 82
... cost for the HEN and the minimum utility cost for the MEN . In other words , only two pinch problems , one for the MEN and one for the HEN , need be solved . The HEN problem is solved first . Only streams R1 ( cold ) and R2 ( hot ) are ...
... cost for the HEN and the minimum utility cost for the MEN . In other words , only two pinch problems , one for the MEN and one for the HEN , need be solved . The HEN problem is solved first . Only streams R1 ( cold ) and R2 ( hot ) are ...
Page 83
... cost for the MEN as a function of the operating temperature of the MEN . The middle portion of the curve is shown in Fig . 5 . The MEN minimum utility cost over all temperatures is $ 1.07 / s , and is achievable for a range of ...
... cost for the MEN as a function of the operating temperature of the MEN . The middle portion of the curve is shown in Fig . 5 . The MEN minimum utility cost over all temperatures is $ 1.07 / s , and is achievable for a range of ...
Page 291
... costs in % when comparing configurations against the base structure . Cost reduction ranges from 11 % ( pinch configuration ) to 16 % ( NLP configuration ) . Table 2. Energy and Cost Comparison of Differ- ent Structures ( Prices in 1992 ) ...
... costs in % when comparing configurations against the base structure . Cost reduction ranges from 11 % ( pinch configuration ) to 16 % ( NLP configuration ) . Table 2. Energy and Cost Comparison of Differ- ent Structures ( Prices in 1992 ) ...
Contents
Keynote Address | 1 |
Separation System Synthesis and Design | 7 |
Modeling and Analysis of Multicomponent Separation Processes | 19 |
Copyright | |
30 other sections not shown
Common terms and phrases
acetic acid activities AIChE algorithm alternatives analysis application approach attainable region azeotrope azeotropic distillation batch branch and bound calculations cess Chem Chemical Engineering chemical process complex components composition concepts constraints cost CSTR data models decision-mapping defined described developed distillation column dynamic energy Engng environment equations equilibrium equipment example feed Figure Floudas flow flowsheet formulation function global optimization Grossmann hierarchical implementation industrial integration interface linear liquid logic mass material mathematical methanol methods methyl acetate MILP MINLP mixture n-dim network synthesis Newton's method nonlinear nonlinear programming paper parameters phase pinch plant pressure problem procedure process design process modelling process synthesis programming properties reac reaction reactive distillation reactor network recycle Seider separation system SimRefinery simulation solution solvent solving specific stage strategy stream structure target task techniques temperature tion unit operations values vapor variables