An application-oriented design procedure is presented for completely by neg
lecting the heat capacity of the vessel and attributing suitable values to
three scale-independent control parameters: the initial concentration (c(0)
); the inlet coolant temperature (T-c,T-i); and the Newtonian cooling time
(t(N)). For given dimensionless values of the reaction order n, heat-transf
er capacity beta (n), and inlet coolant temperature epsilon, the design val
ue alpha* of the dimensionless adiabatic temperature rise must satisfy alph
a (c) > alpha* < <alpha>(m,a). This can help avoid both runaways (alpha* <
<alpha>(c)) and overstep of the maximum allowable temperature rise (alpha*
< <alpha>(m,a)). A model is derived to calculate alpha (c) and alpha (m,a)
for three different reaction orders. Simulated relationships are verified w
ith experimental results concerning the hydration of 2,3-epoxypropanol in a
0.27-L agitated batch reactor.