Can you help me by solving problem P$3-11$ assuming that all reactors are batch reactors and that the input conditions are the initial ones and with variable volume $($I only need the stoichiometric tables for each section$)$evaluating all constants $($e$.$g$.,,).$ Then, assume the reaction follows an ele$-$

mentary rate law, and write the reaction rate solely as a function of conver$-$

sion, i$.$e$.,-r_A=f(x).$

$($a$)$ For the liquid$-$phase reaction

the initial concentrations of ethylene oxide and water are $1lb-mo\frac{l}{f}{t}^3$ and

$3\mathrm{.}47lb-mo\frac{l}{f^3}(62\mathrm{.}41l\frac{b}{f^3}+18),$ respectively. If $k=0\mathrm{.}1d\frac{m^3}{m}ol-$ s at

$300K$ with $E=12\mathrm{.}500ca\frac{l}{m}ol,$ calculate the space$-$time volume for $90\%$

conversion at $300K$ and at $350K.$

$($b$)$ For the isothermal, isobaric gas$-$phase pyrolysis

$C_2{H}_{6}longrightarrow{C}_2{H}_4+H_2$

pure ethane enters the flow reactor at $6$ atm and $1100K.$ How would

your equation for the concentration and reaction rate change if the reac$-$

tion were to be carried out in a constant$-$volume batch reactor?

$($c$)$ For the isothermal, isobaric, catalytic gas$-$phase oxidation

$C_2{H}_4+O_{2}longrightarrowC{H}_2-C{H}_2$

the feed enters a PBR at $6$ atm and $260C$ and is a stoichiometric mixture

of only oxygen and ethylene.

$($d$)$ For the isothermal, isobaric, catalytic gas$-$phase reaction is carried out in

a PBR

the feed enters a PBR at $6$ atm and $170C$ and is a stoichiometric mix$-$

ture. What catalyst weight is required to reach $80\%$ comersion in a flu$-$

idized CSTR at $170C$ and $270C?$ The rate constant is defined wrt

benzene and $v_0=50d\frac{m^3}{m}in.$

$k_B=\frac{53(mol)}{\text{k}\text{g}\text{c}\text{a}\text{t}*minat{m}^3}at300K$ with $E=80k\frac{J}{m}ol$