Table 11
Basic data and assumptions for reactor-design example dealing with optimization of yields for benzene chlorinator
Data for chlorobenzene reactor-design example The feed rate of the dry chlorine is 1.4 lb mole of chlorine/(h) (lb mole of initial benzene charge). The following rate constants are estimated values for the catalyst used at 55°C (assumed for this problem):
Jt,= 510 (lb mol/ft3)-'(h)-' jfc,= 64 (lb mol/ft3)-1 (h)_l k} = 2.1 (lb mol/ft3)"1 (h)-'
There is negligible liquid or vapor holdup in the reflux condenser.
Volume changes in the reacting mixture are negligible, and the volume of liquid in the reactor remains constant at 1.46 ft3 /lb mole of initial benzene charge.
Hydrogen chloride has a negligible solubility in the liquid mixture.
The chlorine gas fed to the system goes into the liquid solution immediately up to its solubility limit of 0.12 lb mole of chlorine/lb mole of original benzene, and this value then remains constant.
Each reaction is second order as written.
Nomenclature
F - feed rate of chlorine as (lb mol/h)/(lb mole of initial benzene charge) = 1.4 yb = volume of reactor liquid contents s 1.4&V, ; ( Vt,/N0 = 1.46)
lb moles of benzene present at time 0 Ng = lb moles of benzene present at time t Net = lb m°les °f chlorine present in liquid at time t No = lb moles of dichlorobenzene present at time t Nm = lb moles of monochlorobenzene present at time t Nt - lb moles of trichlorobenzene present at time f t = time in hours
For trichlorobenzene,
AfRNa K K
For chlorine, subject to the solubility limit of Nct/N{) = 0.12, there is an input flow term in Eq. (37). Therefore, the rate expression for the consumption of chlorine can be written as
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