Linnhoff

Figure 1.2 Process design starts with the reactor. The reactor design dictates the separation and recycle problem. (From Smith and Linnhoff, Trans. IChemE, ChERD, 66 195, 1988 reproduced by permission of the Institution of Chemical Engineers.)...

Stephanopoulos, G., Linnhoff, B., and Sophos, A., Synthesis of Heat Integrated Distillation Sequences, IChemE Symp. Ser., 74 111, 1982. 

Cerda, J., Westerberg, A. W., Mason, D., and Linnhoff, B., Minimum Utility Usage in Heat Exchanger Network Synthesis—A Transportation Problem, Chem. Eng. ScL, 38 373 1983. 

Linnhoff, B., and de Leur, J., Appropriate Placement of Furnaces in the Integrated Process, IChemE Symp. ries No 109, 1988. 

FIgura 7.1 Two alternative graphs. (Reprinted from Linnhoff, Mason, and Wardle, Understanding Heat Exchan r Networks Computers Ckem. Engg., 3 295, 1979 with permission from Elsevier Science, Ltd.)... 

Figure 7.8 Designs with a temperature approach or small temperature cross can be accommodated in a single 1-2 shell, whereas designs with a large temperature cross become infeasible. (From Ahmad, Linnhoff, and Smith, Trans. ASME, J. Heat Transfer, 110 304, 1988 reproduced by permission of the American Society of Mechanical Engineers.)...

Townsend, D. W., and Linnhoff, B., Surface Area Targets for Heat Exchanger Networks, IChemE Annual Research Meeting, Bath, U.K., 1984. 

Linnhoff, B., and Ahmad, S., Cost Optimum Heat Exchanger Networks I. Minimum Energy and Capital Using Simple Models for Capital Cost, Computers Chem. Eng., 14 729, 1990. 

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