A small laboratory fixed bed 10.16 cm in diameter and 16 cm in length containing 600 g of activated carbon (C), has been used to adsorb n-butanol (B) from air containing 365 ppm of B. Measurements of the effluent concentration in terms of cout/cF as a function of time t are:

Cout/cF	0.0019	0.003	0.008	0.18	0.04	0.07	0.15	0.24	0.66	0.81	0.94	1.00
t, hr	5	5.5	6	6.5	7	7.5	8	8.5	10	11	12	13

Other pertinent data are: entering superficial gas velocity, us = 58 cm/s; T = 25C; P = 737 mm Hg; bed porosity, =0.456; average particle diameter, dp = 0.37cm; and butanol MW = 74.12 g/mol. A cylindrical vessel with an inside diameter of 2 ft and a height of 5 ft is available to conduct the adsorption on an industrial scale. The vessel can be packed with carbon to a 4 ft height. Plot the laboratory data and determine: (a) the mass velocity of the gas as it enters the bed in g gas/cm2 h, (b) the equilibrium loading of the carbon laboratory bed in g B/g C, and (c) the fraction of the laboratory bed utilied in the experiment if the breakthough time is taken at cout/cF = 0.05. For the industrial application calculate (d) the gas flow rate in kg/h for the same entering superficial velocity used in the laboratory experiment, (e) the fraction of the industrial bed that can be utilized, and (f) the estimated breakthrough time in h.