11. For the liquid phase parallel reactions:

The desired product is R. The higher selectivity of R will be achieved, if. The reaction is conducted at (A) The low temperature in an ideal continuous stirred tank reactor (CSTR) (B) The high temperature in an ideal continuous stirred tank reactor (CSTR) (C) The low temperature in an ideal plug flow reactor (PFR) (D) The high temperature in an ideal plug flow reactor (PFR) mol

12. The desired liquid-phase reaction , is accompanied by the side reaction ,from dt the standpoint of favourable product distribution, the most desirable contacting scheme is (A) An ideal plug flow reactor (PFR) with the mainstream of '"D" and "E" (B) An ideal plug flow reactor (PFR) with the mainstream of "D" and side stream of "E" (C) An ideal plug flow reactor (PFR) with the mainstream of "E" and side stream of "D" (D) An ideal mixed flow reactor (MFR) with the mainstream of "D" and "E"

13. For the uni-molecular type elementary reactions, the fractional yield of B in MFR for the given conversion of A (A) remains constant with increase in k₂/k₁ (B) increases with the increase in k₂/k₁ (C) decreases with the increase in k₂/k₁ (D) increase linearly with increase in k₂/k₁

14. Consider the liquid phase reactions shown in the schematic below carried out in a flow reactor at steady state.
Keeping the reaction system isothermal, the yield of the desired product can be maximized by maintaining Keeping the reaction system isothermal, the yield of the desired product can be maximized by maintaining (A) Low concentration of A and high concentration of B (B) The high concentration of A and high concentration of B (C) Low concentration of B and low concentration of B (D) The high concentration of A and low concentration of B

15. For the irreversible elementary reaction in parallel is, the rate of disappearance of reactant A is given by (A)(k₁-k₂)C_A (B) (k₁+k₂)C_A (C)0.5(k₁+k₂)C_A (D) kIC_A

申論題 (9)

Problem 3 (10%) (a) (8) A vessel, divided into two parts by a partition, contains 4 mol of A gas at 350K and 30 bar on one side and 3 mol of B gas at 350K and 20 bar on the other. If the partition is removed and the gases mix completely to form a gas mixture also at 350K, what are the changes in enthalpy, entropy and Gibbs free energy? Assume both A and B gases are ideal gases with C_v = 2.5R. R = (b) (2) The enthalpy of a C-D binary system at fixed T and P is represented by the equation: H = 600x_c + 400x_D+x_cx_D(40x_c+20x_D). Is this binary system an ideal solution? Why or why not?

(a) What is the degree of freedom of azeotrope according to phase rule?

(b). If the gas phase is an ideal solution, is the liquid phase an ideal solution as well? Why or why not?

(d) Draw the curves of Gibb free energy VS. composition for both gas and liquid phases at 70℃.

(e) Draw the curves of Gibb free energy Vs. composition for both gas and liquid phases at 65℃.

Problem 5 (10%) A gas-phase, reversible reaction, , with both rate constants obeying the Arrhenius Law. Please show that the difference of activation energy between forward (k₁) and backward (k₂) rate constants is equal to the reaction enthalpy; i.e., indicate the activation energy of the forward and backward rate constants, respectively.

Problem 6(10%)

A liquid-phase irreversible reaction: P +Q →R+S follows the elementary reaction rate law. This reaction is carried out in a series of three, equal volume CSTRs at the same reaction temperature. The concentrations of P and O in the feed to the first reactor are the same

If the rate constant (k) for this reaction is 3.50 L/mol-h at the operation temperature. The final conversion is 0.75. If the total volume of these three reactors is 9300 L, what is the volume flow rate (in L/h) to the first reactor? What are the conversions in reactors 1 and 2?

Problem 7(10%)
The elementary irreversible gas phase catalytic reaction A-B is carried out isothermally in a batch reactor with rate constant of 0.2 dm³/kgcat *min at 300K. The catalyst deactivation follows a first order decay law (with decay rate constant of 0.1 at 300K) and is independent of the concentrations of both A and B. Calculate the conversion in the reactor after 10 minutes at 300 K. Additional Information:

Initial concentration of A = 1 mol/dm³

Batch reactor volume (V₀) = 1 dm³ Catalyst weight (W)= 1 kg