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Column/side reactor

DESIGN AND CONTROL OF COLUMN/ SIDE REACTOR SYSTEMS... [Pg.431]

The column/side reactors process has a large number of design optimization variables. A number of specifications and assumptions ate made to leduee this number to a manageable level. The design objective is to obtain 95% conversion for fixed fresh feed flowrates of 12.6 mol/s of each reactant. The product purities of distillate stream x c and bottoms stream xb,d are both 95 mol%. The two fresh feedstreams of reactants A and B ate fed into the column at the trays immediately above the lower and upper trap-out trays, respectively. [Pg.434]

Figure 16.6 Results for column/side reactors process with different 0390 values. Figure 16.6 Results for column/side reactors process with different 0390 values.
The lower gr h in Figure 16.7 compares the economic optimum steady-state design of the column/side reactor process with those of the reactive distillation column and the multiunit conventional process. The reactive distillation column is the most economical alternative for the a39o = 2, where thoe is noreaction/separation temperature mismatch. The column/ side reactor process becomes more attractive as the mismateh of reaction/separation temperatures becomes more severe. The distillation column with a side reactor is economically superior for reference relative volatilities that arc smaller than 1.5 for this case study. [Pg.442]

Comparing the lower graphs in Figures 16.7 and 16.8 shows that the break-even point between the reactive distillation and column/side reactor process moves from an of about 1.5 down to about 1.4. [Pg.446]

DESIGN OF COLUMN/SIDE REACTOR PROCESS FOR ETHYL ACETATE SYSTEM... [Pg.458]


See other pages where Column/side reactor is mentioned: [Pg.432]    [Pg.441]    [Pg.452]    [Pg.456]   
See also in sourсe #XX -- [ Pg.431 ]




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Column reactor

Side-reactors

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