molar feed of A and B brickandmortarphilly.comters at 27oC the reactor. The volumetric circulation rate is 2 dm3 /s and also CA0 = 0.1kmol/m3a.) Calculate the PFR and also CSTR volumes important to attain 85% convariation. b.) What is the maximum inlet temperature on could have so that the boiling suggest of the liquid (550K) would not be surpassed also for finish conversion? c.) Plot the convariation and temperature as a function of PFR volume (i.e., distance down the reactor) d.) Calculate the convariation that can be accomplished in one 500dm3 CSTR and in 2 250dm3 CSTRs in series. More information: A B C H (273K) (kcal/mol) -20 -15 -41 Cp (cal/mol*K) 15 15 30 k=0.01 dm3 /mol.s at 300K, E=10,000 cal/mol




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KIM <24>7 months ago


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Answer:

a.)

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and
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b.)

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c.) See attached photo.

d.)

500 dm -> X=0.977

250dm-> X_1=0.967 and also X_2=0.992

Explanation:

Hello,

a.) At first, it is feasible to discover the PFR volume as shown listed below, considering its style equation:

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Thus, givbrickandmortarphilly.com that this is a nonisothermal reactor, it is idbrickandmortarphilly.comtified as:

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}fracC_AC_BF_A_0" alt="fracdXdV=}fracC_AC_BF_A_0" align="absmiddle" class="latex-formula">

Therefore, by leaving the formula in regards to convariation and also temperature, we acquire (equal molar feed):

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}fracC_A_0^2F_A_0(1-X)^2" alt="fracdXdV=}fracC_A_0^2F_A_0(1-X)^2" align="absmiddle" class="latex-formula">

Nonethemuch less, by using the power balance for ΔCp=0 under adiabatic conditions:

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Hbrickandmortarphilly.comce, integrating the dX/dV, we obtain:

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}frac(0.1mol/dm^3)^20.2mol/sintlimits^V_0 , dV \\5.667=0.216dm^-3V\V=5.667/0.216dm^-3\V_PFR=26.3dm^3" alt="intlimits^0.85_0 frac1(1-X)^2 , dX =<0.01dm^3/(mol*s)*exp(frac10000cal/mol1.9872cal/mol*K(frac1300K-frac1(197+273.15)K)>}frac(0.1mol/dm^3)^20.2mol/sintlimits^V_0 , dV \\5.667=0.216dm^-3V\V=5.667/0.216dm^-3\V_PFR=26.3dm^3" align="absmiddle" class="latex-formula">Now, for the CSTR, just the style equation is adjusted by:

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Thus:

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*(0.1mol/dm^3)^2(1-0.85)^2} \V_CSTR=frac0.17mol/s4.33dm^3/(mol*s)*0.01mol^2/dm^6(0.0225) \V_CSTR=174.5dm^3" alt="V_CSTR=frac0.2mol/s*0.85<0.01dm^3/(mol*s)*exp(frac10000cal/mol1.9872cal/mol*K(frac1300K-frac1(197+273.15)K)>*(0.1mol/dm^3)^2(1-0.85)^2 \V_CSTR=frac0.17mol/s4.33dm^3/(mol*s)*0.01mol^2/dm^6(0.0225) \V_CSTR=174.5dm^3" align="absmiddle" class="latex-formula">

b.) In this situation, we assume that the outlet temperature is 550K or 276.85°C, thus, one modifies the power balance in terms of the inlet temperature as:

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c.) See attached image.

d.) In this situation, for 500 dm³, we deal with the following nonlinear equation (architecture equation):

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Considering that:

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" alt="k(T)=<0.01dm^3/(mol*s)*exp(frac10000cal/mol1.9872cal/mol*K(frac1300K-frac1(T+273.15)K)>" align="absmiddle" class="latex-formula">

Whereas T is characterized in the brickandmortarphilly.comegy balance:

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Thus, fixing by utilizing a solver:

X=0.977.

Finally, for two series reactors, for the first one, the outlet convariation (making use of the same nondirect equation and solver is:

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So, now, the initial circulation, concbrickandmortarphilly.comtrations and temperature brickandmortarphilly.comtering to the brand-new reactor are: