CHPTE 7 Chemical eaction Engineering (Gate 00). The conversion for a second order, irreversible reaction (constant volume) () k B, in batch mode is given by k C t o ( kcot) (C) k C t o + (D) kcot (B) k C t o kcot ( k C t). The reaction rate constants at two different temperature T and T are related by () ln k E k T T (B) ln k E k T T (C) exp k E k T T (D) exp k E k T T 3. The E-curve for a non ideal reactor defines the fraction of fluid having age between t and t+dt () t the inlet (B) t the outlet (C) In the reactor (D) veraged over the inlet and outlet o 4. The mean conversion in the exit stream, for a second-order, liquid phase reaction in a non-ideal flow reactor is given by () (B) 0 kcot E() t dt k C t o E() t dt k C t 0 o k C t (C) E( t) (D) 0 o 0 exp( ) k C t kcot E () t dt o 5. For a vapor phase catalytic reaction B P Which follows rideal mechanism and the reaction step is rate controlling, the rate of reaction is given by (reaction step is irreversible, product also adsorbs) () (B) (C) (D) dt kppb r K p K p p p kp k pp r K p K p p p kppb r K p K p kppb r K p p p 5 ll ights eserved
6. The first-order, gas phase reaction () (B) k Bis conducted isothermally in batch mode. The rate of change of conversion with time is given by dx k ( x ) ( X ) dt dx dt k X X dx (C) k ( ) X dt (D) ( ) ( 05 ) dx ( ) k X dt ( X ) (Gate 00) 7. For an ideal plug flow reactor the value of the Peclet number is () 0 (B) (C) (D) 0 8. The extent of a reaction is () Different for reactants and products (B) Dimensionless (C) dependent on the stoichiometric coefficients (D) all of the above 9. n exothermic reaction takes place in an adiabatic reactor. The product temperature (choose the correct option)..the reactor feed temperature () is always equal to (B) is always greater than (C) is always less than (D) may be greater or less than 0. pulse tracer is introduced in an ideal CST (with a mean residence time ) at time t = 0. The time taken for exit concentration of the tracer to reach half of its initial value will be () (B) 0.5 (C) /0.693 (D) 0.693. batch adiabatic reactor at an initial temperature of 373 K is being used for the reaction B. ssume the heat of reaction is - kj/mol at 373 K and and the heat capacity of both and B to be constant and equal to 50 J/ mol K. The temperature rise after a conversion of 0.5 will be () 5 0 C (C) 0 0 C (B) 0 0 C (D) 00 0 C. In the hydrodealkylation of toluene to benzene, the following reaction occur C H H C H CH 7 8 6 6 4 C H C H H 6 6 0 Toluene and hydrogen are fed to a reactor in a molar ratio :5. 80% of the toluene gets converted and the selectivity of benzene (defined as moles of benzene formed/ moles of toluene converted ) is 90%. The fractional conversion of hydrogen is () 0.6 (B) 0.44 (C) 0.5 (Gate 003) (D)0.36 6 ll ights eserved
3. For a series of reactions k k B C k << k, the reaction system can be approximated as k k () B (B) B k k (C) C (D) C 4. n elementary liquid phase k decomposition reaction B is to be carried out in a CST. The design equation is () (B) X k X k X ( X ) X X (C) k ( X ) (D) kc o X( X ) ( X ) 5. CST is to be designed in which an exothermic liquid phase first order reaction of the type is taking place. The reactor is `to be provided with a jacket in which coolant is flowing. Following data is given C kmol m X feed temperature o 3 5 / ; 0.5; o reactor temperature 40 C ate constant at 40 o C = min - ; H kj mol kg m C J gm C q 3 o 40 / ; 000 / ; p 4 / ; 3 3 0 m / min ( and C p are same for the reactant and product stream). The amount of heat to be removed is () /3 kw (C) 5/3 kw (B) kw (D) 4 kw 6. liquid phase reaction is to be carried out under isothermal conditions. The reaction rate as a function of conversion has been determined experimentally and is shown in the figure given below. What choice of reactor combination will require the minimum overall reactor volume, if a conversion of 0.9 is desired? () CST followed by a PF (B) CST followed by a PF followed by CST (C) PF followed by a CST followed by a PF Common data questions The following gas phase reactions are carried out isothermally in a CST r k p k mol m bar 3 0 / (sec. ) S r k p k mol m bar 3 3 40 / (sec. ) Total pressure = bar, F o= mol/sec; feed is pure 7. What is the maximum possible value of F (mol/sec) () /3 (B) / (C) /3 (D) 7 ll ights eserved
8. The volume of a CST required for fractional conversion of equal to 0.3 due to the first reaction is () 0. (B) 0. (C) 0.75 (D) 0.375 9. Following isothermal kinetic data are obtained in a basket type of mixed flow reactor for a porous catalyst. Determine the role of pore diffusion and external mass transfer process. Pellet Diamete r () Strong pore diffusion control and mass transfer not controlling (B) Both pore diffusion and mass transfer not controlling (C) Both pore diffusion and mass transfer controlling Leaving concentration Of the reactant (D) Mass transfer controlling Spinning rate of the basket (- r ) High low High () α =, β =, γ = (B) α =, β =, γ = (C) α = /3, β = /3, γ = /3 (D) α = /, β =, γ = ½. The rate of ammonia synthesis for the reaction N 3H NH is given by 3 3 r 0. 8p p 0. 6p. If the reaction is N H NH3 represented as, 0. 5N. 5H NH, the 3 rate of ammonia synthesis is 05. (a) r 0. 8pN 0. 6pNH 0 3 (b) r 0. 8pN ph 3 0. 6p NH 3 (c) r 0. 5 0. 8pN ph 3 0. 6p NH 3 0. 5. 5 (d) r 0. 5 0. 8pN ph 0. 6pNH 3. n endothermic aqueous phase first order irreversible reaction is carried out in an adiabatic plug flow reactor. The rate of reaction () Is maximum at the inlet of the reactor (B) Goes through a maximum along the length of the reactor (C) Goes through a minimum along the length of the reactor (D) Is maximum at the exit of the reactor. (Gate 004) 0. The rate expression for the gaseous phase reaction CO H CH OH is 3 given by r k p p k p CO H CH OH 3 Which of the following is NOT possible? 3. first order gaseous phase reaction is catalyzed by a non-porous solid. The kinetic rate constant and the external mass transfer coefficient are k and kg, respectively. The effective rate constant (keff) is given by k k k eff g 8 ll ights eserved
k k g ( B) k eff ( C) k eff 4. For a packed bed reactor, the presence of a long tail in the residence time distribution curve is an indication of () Ideal plug flow (B) Bypass (C) Dead zone (D)Channeling 5. The following gas phase reaction is taking place in a plug flow reactor, + ½ B C, The stoichiometric mixture of and B at 300 K is fed to the reactor. t m along the length of the reactor, the temperature is 360 K. The pressure drop is negligible and an ideal gas behavior can be assumed. Identify the correct expression relating the concentration of at the inlet (CO), concentration of at m (C) and the corresponding conversion of (X). () C. C (B) C. C 0 0 (C) C 0. 83 C k k g ( D) k k k eff g 0 x 0. 33x x 0. 5x x 0. 33x (D) C 0. 83 C 0 x 0. 5x 6. second order liquid phase reaction B is carried out in a mixed flow reactor operated in semi-batch mode (no exit stream). The reactant at concentration CF is fed to the reactor at a volumetric flow rate of F. The volume of the reacting mixture is V and the density of the liquid mixture is constant. The mass balance for is () (B) (C) (D) d VC dt d VC dt F C C kc V F F C C kc V d VC dt FC F kc V d VC dt FC F kc V 7. For an isothermal second order aqueous phase reaction B, the ratio of the time required for 90% conversion to the time required for 45% conversion is () (B) 4 (C) (D) 8. n isothermal aqueous phase reversible reaction P is to be carried out in a mixed flow reactor. The reaction rate in (kmol / m3 h) is given by r = 0.5 C P 0.5C. stream containing only P enters the reactor. The residence time required (in hours) for 40% conversion of P is () 0.80 (B).33 (C).60 (D).67 9 ll ights eserved
9. pollutant P degrades according to first order kinetics. n aqueous stream containing P at kmol / m 3 and volumetric flow rate m3/h requires a mixed flow reactor of volume V to bring down the pollutant level to 0.5 kmol / m 3. The inlet concentration of the pollutant is now doubled and the volumetric flow rate is tripled. If the pollutant level is to be brought down to the same level of 0.5 kmol / m 3, the volume of the mixed flow reactor should be increased by a factor of () 7 (B) 6 (C) 3 (D) 7/3 30.Consider a reversible exothermic reaction in a plug flow reactor. The maximum and minimum permissible temperatures are Tmax and Tmin, respectively. Which of the following temperature (T) profiles will require the shortest residence time to achieve the desired conversion? kmol / m3 of each and B enters the reactor at 8 m3 / h. If the temperature of the exit stream is never to exceed 390 K, what is the maximum feed inlet temperature allowed? Data: Heat of reaction = 50 kj / mol, density of the reacting mixture = 000 kg / m3, specific heat of reacting mixture kj / kg.k. The above data can be assumed to be independent of composition and temperature. () 90 (B) 90 (C) 390 (D) 490 3. Pick the WONG design guideline for a reactor in which the reactions (desired) and S (undesired) are to take place. The ratio of the reaction rates is () Use high pressure and eliminate inert when a > b (B) avoid recycle when a > b (C) use batch reactor or plug flow reactor when a > b r r S k k C a b (D) use CST with a high conversion when a > b (Gate005) 33. For the reaction + S T, the rates of formation, r, r S and r T of the substances, S and T respectively, are related by () r = r S = r T 3. n irreversible aqueous phase reaction B P is carried out in an adiabatic mixed flow reactor. feed containing 4 (B) r = r S = r T (C) r = r S = r T (D) r = r S = r T 0 ll ights eserved
34. For the liquid phase reaction P, in a series of experiments in a batch reactor, the half-life t / was found to be inversely proportional to the square root of the initial concentration of. The order of the reaction is () 3/ (B) (C) + / (D) / 35. Which is the correct statement from the following statements on the rrhenius model of the rate constant k =.e -E/T? () is always dimensionless, (B) For two reactions and, if = and E > E, then k (T) > k (T) (C) For a given reaction, the % change of k with respect to temperature is higher at lower temperatures. (D) The % change of k with respect to temperature is higher for higher. 36. The rate expression for the reaction of is given by k C r k C The units of k and k are, respectively, () (mol - m 3 s - ), (mol -/ m 3/ ) (B) (mol - m 3 s - ), (mol / m 3/ ) (C) (mol m 3 s - ), (mol -/ m 3/ s - ) (D) (mol - m 3 s - ), (mol -/ m 3/ s -/ ) 37. The first order liquid phase reaction P is to be carried out isothermally in the following ideal reactor configurations. (P) m 3 CST followed by a m 3 PF, (Q) m 3 CST () m 3 PF followed by a m 3 CST, (S) m 3 CST followed by a m 3 CST, The overall exit conversions X, for the above configurations P, Q, and S, assuming identical inlet conditions and temperature, are related as () X P> X > X S> X Q (B) X P = X > X S> X Q (C) X P = X S = X Q = X (D) X Q> X P> X > X S 38. The gas phase rxn B+C is carried out in an ideal PF achieving 40% convention of. The feed has 70 mol % and 30 mol % units. The inlet temperature is 300 K and outlet to inlet molar uniform pressure is S () 0.60 (B) 0.30 (C) 0.47 (D) 0.35 39. Match the items in Group I with those in Group II Group I (P) Porous catalyst (Q) Parallel reactions () Non-ideal tubular reactor (S) Gas-solid noncatalytic reaction () P-3, Q-, -4, S- (B) P-, Q-3, -, S-4 (C) P-, Q-4, -, S3 Group II () Selectivity () Shrinking core model (3) Thiele modulus (4)Dispersion number ll ights eserved
(D) P-3, Q-4, -, S- 40. The rate of the liquid phase reversible reaction B in (kmol m -3 min - ) at 98 K, is r = 0.0 C 0.0C B,where the concentrations C and C B are expressed in (kmol m -3 ). What is the maximum limiting conversion of achievable in an isothermal CST at 98 K, assuming pure is fed at the inlet () (B) /3 (C) / (D) /3 Linked nswer Questions 4 4 The residence time distribution E(t) (as shown below) of a reactor is zero until 3 minutes and then increases linearly to a maximum value E max at 8 minutes after which it decreases linearly back to zero at 5 minutes. 43. The reaction + B C occurs on a catalyst surface. The reactants and B diffuse to the catalyst surface and get converted completely to the product C, which diffuses back. L The steady state molar fluxes of, B and C are related by () N = N B = N C (B) N = (/) N B = N C (C) N = N B = N C (D) N = (/) N B = N C 44. n irreversible gas phase reaction 5B is conducted in an isothermal batch reactor at constant pressure in the presence of an inert. The feed contains no B. If the volume of the gas at complete conversion must not exceed three times the initial volume, the minimum mole percent of the inert in the feed must be () 0 (B) 0 (C) 33 (D) 50 4. What is the value of E max? () /6 (B) /8 (C) /4 (D) / 4. What is the value of the mean residence time in minutes? () 5.7 (B) 8 (C) 8.7 (D) (Gate006) 45. first order reversible reaction B occurs in a batch reactor. The exponential decay of the concentration of has the time constant. B k k C k k 46. Consider the following reactions between gas and two solid spherical particles, B and C of the same size. + B gaseous product, + C ash The ash does not leave the particle C, let t and t be the times required for to completely consume particles B and C, D k k ll ights eserved
respectively, If k and k are equal at all temperatures and the gas phase mass transfer resistance is negligible, then () t = t at all temperatures (B) t = t at high temperatures (C) t> t at high temperatures (D) t< t at high temperatures 47. reaction B is to be conducted in two CSTs in series. The steady state conversion desired is Xf. The reaction rate as a function of conversion is given by r = -/(+X). If the feed contains no B, then the conversion in the first reactor that minimizes the total volume of the two reactors is () Xf (B) 0. Xf (C) 0.5 Xf (D) 0.5 ( Xf) 48. Consider the following elementary reaction network B 3 4 C D The activation energies for the individual reactions are E = 00 kj/mol, E = 50 kj/mol, E3 = 00 kj/mol, and E4 = 00kJ/mol. If the feed is pure and the desired product is C, then the desired temperature profile in a plug flow reactor in the direction of flow should be () Constant at low temperature (B) Constant at high temperature (C) Increasing (D) Decreasing. 3 ll ights eserved 49. The exit gage distribution in a stirred reactor is given by E t e t /. Fluid elements e and e enter the reactor at times t = 0 and t = 0 > 0, respectively. The probability that e exits the reactor before e is () / (B) e- θ / τ (C) e- θ / τ (D) zero. (Gate007) 50. well-stirred reaction vessel is operated as a semi-batch reactor in which it is proposed to conduct a liquid phase first order reaction of the type B. The reactor is fed with the reactant at a constant rate of liter/min having feed concentration equal to mol/liter. The reactor is initially empty. Given k = min-, the conversion of reactant based on moles of fed at t = min is () 0.36 (B) 0.43 (C) 0.57 (D) 0.864 5. liquid phase exothermic first order reaction is being conducted in a batch reactor under isothermal conditions by removing heat generated in the reactor with the help of cooling water. The cooling water flows at a very high rate through a coil immersed in the reactor such that there is negligible rise in its temperature from inlet to outlet of the coil. If the rate constant is given as k, heat of reaction ( ΔH ), volume of the reactor, V, initial concentration as CO, overall heat transfer coefficient, U, heat transfer area of the coil is equal to, the required cooling water inlet temperature, Tci is given by the following equation :
() T ci (B) T ci (C) T (D) ci T ci T T T T H VkC0 U 0 H VkC e U H VC0 Ut e H VC0 Ut kt kt 5. The following liquid phase reaction is taking place in an isothermal CST k k B C k 3 D eaction mechanism is same as the stochiometry given above. Given k = min - ; k = min - ; k 3 = 0.5 lit / (mol)(min); C O = 0 mol / liter, C BO = 0 mol / liter and C B = 0 mol / liter, the solution for F / N (flow rate/reactor volume in min - ) yields () 6.7 (B) 6 and 0.5 (C) and 4/3 (D) 8 53. pulse of concentrated KC solution is introduced as tracer into the fluid entering a reaction vessel having volume equal to m 3 and flow rate equal to m 3 /min. The concentration of tracer measured in the fluid leaving the vessel is shown in the figure given below. The flow model parameters that fit the measured TD in terms of one or all of the following mixing elements, namely, volume of plug flow reactor, V p, mixed flow volume, V m, and dead space, V d, are () V p = /6 m 3, V m = / m 3,V d= /3m 3 (B) V p = V m = V d = /3 m 3 (C) V p = /3 m 3,V m = / m 3,V d = /6m 3 (D) V m = 5/6 m 3, V d = /6 m 3 54. The first order reaction of to is run in an experimental mixed flow reactor. Find the role played by pore diffusion in the run given below. C O is 00 and W is fixed. gitation rate was found to have no effect on conversion. d p F O X 4 0.8 6 4 0.4 () (B) (C) (D) Strong pore diffusion control Diffusion free Intermediate role by pore diffusion External mass transfer 55. packed bed reactor converts to by first order reaction with 9 mm pellets in strong pore diffusion regime to 63.% level. If 8 mm pellets are used what is the conversion. () 0.39 (B) 0.6 (C) 0.63 (D) 0.865 56. The following rate-concentration data are calculated from experiment. Find the activation energy temperature (E/) of the first order reaction. d p C r T 0 480 40 480 40 3 500 () 43.8 (B) 4865.6 (C) 973. (D) 383.3 4 ll ights eserved
57. Determine the level of (high, low, intermediate), temperature profile (high, low, increasing, decreasing), which will favor the formation of the desired product indicated in the reaction scheme given below. 3 S U () e (B) t (C) t k (D) Kt t k k t n E n E n 3 E 3 5 35 3 45 () High C O increasing T, PF (B) Low C O increasing T, PF (C) High C O decreasing T, MF (D) High C O decreasing T, PF Common Data for Questions 58 & 59: 58. The following liquid phase reaction is taking place in an isothermal batch reactor k first order k zero order B C Feed concentration = mol / liter The time at which the concentration of B will reach its maximum value is given by k () t ln k k k (B) t ln k k k k (C) t ln k k k (D) t ln k k 59. The time at which the concentration of B will become zero is given by the following equation: (Gate 008) 60. species () reacts on a solid catalyst to produce and S as follows : ) r = k C ) S r S = k C ssume film resistance to mass transfer is negligible. The ratio of instantaneous fractional yield of in the presence of pore diffusion to that in the absence of pore diffusion is () (B) > (C) < (D) Zero 6. The gas phase reaction +3B C is conducted in a PF at constant temperature and pressure. The PF achieves a conversion of 0% of. The feed is a mixture of, B and an inert I. It is found that the concentration of remains the same throughout the reactor. Which ONE of the following ratios of inlet molar rate (F,in: F B,in: F I,in) is consistent with this observation? ssume the reaction mixture is an ideal gas mixture. () : 3 : 0 (B) : : (C) 3 : : (D) : : 6. The elementary liquid phase series parallel reaction scheme B C 5 ll ights eserved
is to be carried out in an isothermal CST. The rate laws are given by r = k C r B = k C kc B Feed is pure. The space time of the CST which results in the maximum exit concentration of B is given by figure. ssume dilute concentration and neglect any variations in the axial direction. () (C) kk ' k k ' (B) (D) k ' k k ' k k k ' 63. The liquid phase reaction Products is governed by the kinetics - r = k C / If the reaction undergoes 75% conversion of in 0 minutes in an isothermal batch reactor, the time (in minutes) for complete conversion of is. () 40/3 (B) 0 (C) 30 (D) 64. The homogeneous reaction + B C is conducted in an adiabatic CST at 800 K so as to achieve a 30% conversion of. The relevant specific heats and enthalpy change of reaction are given by C P = 00 J / (mol K), C PC = 50 J / (mol K), C PB = 50 J / (mol K), ΔH rxn = -00 kj / mol, If the feed, a mixture of and B, is available at 550 K, the mole fraction of in the feed that is consistent with the above data is () 5/7 (B) /4 (C) / (D) /7 65. The irreversible zero order reaction B takes place in a porous cylindrical catalyst that is sealed at both ends as shown in the The steady state concentration profile is C 0 r CS 4 where ф o is the Thiele modulus. For ф o = 4, the range of r where C = 0 is r () 0 r (B) 0 r 3 (C) 0 r r (D) 0 r 4 Common Data Questions 66 and 67: liquid is flowing through a reactor at a constant flow rate. step input of tracer at a molar flow rate of mol/min is given to the reactor at time t =0. The time variation of the concentration (C) of the tracer at the exit of the reactor is as shown in the figure: 66. The volumetric flow rate of the liquid through the reactor (in L / min) is () (B) (C).5 (D) 4 6 ll ights eserved
67. The mean residence time of the fluid in the reactor (in minutes) is () (B) (C) 3 (D) 4 Linked nswer Questions 68 and 69: The liquid phase reaction P is to be carried out at constant temperature in a CST followed by a PF in series. The overall conversion of achieved by the reactor system (CST + PF) is 95%. The CST has a volume of 75 liters. Pure is fed to the CST at a concentration C O = mol/liter and a volumetric flow rate of 4 liters/min. The kinetics of the reaction is given by mol r 0.C liter.min 68. The conversion achieved by the CST is () 40% (B) 50% (C) 60% (D) 80% 69. The volume of the PF required (in liters) is () 380 (B) 350 (C) 75 (D) 35 (Gate009) 70. For a homogeneous reaction system, where C j = is the concentration of j at time t N j = is the number of moles of j at time t V = is the reaction volume at time t t = is the reaction time. The rate of reaction for species j is defined as dc () j dt (C) dnj V dt (B) (D) dc j dt dn j V dt 7. The half-life of a first order liquid phase reaction is 30 seconds. Then the rate constant, in min -, is () 0.03 (B) 0.60 (C).386 (D).0 7. For a solid-catalyzed reaction, the Thiele modulus is proportional to B int rinsic reaction rate diffusion rate diffusion rate int rinsic reaction rate int rinsic reaction rate C diffusion rate int diffusion rate D rinsic reaction rate 73. The liquid-phase reaction B is conducted in an adiabatic plug flow reactor. Data: Inlet concentration of = 4.0 k.mol/m 3 Density of reaction moisture (independent of temperature = 00 kg / m 3. verage heat capacity of feed stream (independent of temperature = 000 J/kg.k Heat of reaction (independent of temperature) = 0 kj / mol of reacting 7 ll ights eserved
If the maximum allowable temperature in the reactor is 800 K, then the feed temperature (in K) should not exceed. () 400 (B) 500 (C) 600 (D) 700 74. n isothermal pulse test is conducted on a reactor and the variation of the outlet tracer concentration with time is shown below: () 0. (B) 0. (C) 0.4 gmol liter (D) 0.4 liter gmol gmol liter liter gmol 0.5.min 0.5.min 0.5.min 0.5.min 76. The concentration of (in mol / liter) at the exit of the plug flow reactor is () 0.5 (B).0 (C).0 (D).5 The mean residence time of the fluid in the reactor (in minutes) is () 5.0 (B) 7.5 (C) 0.0 (D) 5.0 Linked nswer Questions 75 and 76: The liquid-phase reaction B + C is conducted isothermally at 50 C in a continuous stirred tank reactor (CST). The inlet concentration of is 8.0 mol / liter. t a space time of 5 minutes, the concentration of at the exit of CST is 4.0 mol / liter. The kinetics of the reaction is 0.5 gmol r kc liter.min plug flow reactor of the same volume is added in series after the existing CST. (Gate 00) 77. For a first order isothermal catalytic reaction, P, occurring in an infinitely long cylindrical pore, the relationship between effectiveness factor, ε, and Thiele modulus, ϕ, is () (C) (B) (D) 78. Two reactors (reactor and reactor ) with average residence times, τ and τ, respectively, are placed in series. eactor has zero dispersion and reactor has infinite dispersion. The residence-time distribution, E(t) of this system, is given by 75. The rate constant (k) for this reaction at 50 C is () 0 t t exp t 8 ll ights eserved
0 t (B) t exp t 0 t (C) t exp t (D) 0 t t exp t 79. n autocatalytic liquid phase reaction, + is conducted in an isothermal batch reactor with a small initial concentration of. ssume that the order of reaction with respect to both reactants is positive. The rate of reaction (-r ) versus concentration, C, as the reaction proceeds, is depicted by 80. The value of K in mole / litre is () (B) 9 (C) 5 (D) 8. If the same reaction is conducted in a series of two CSTs with residence times s and 0.s, then the inlet concentration of, in mole / liter, required to attain an outlet concentration of of mole / liter, is ().64 (B).00 (C).64 (D) 0.54 (Gate 0) 8.Consider an irreversible, solid catalyzed, liquid phase first order reaction. The diffusion and the reaction resistances are comparable. The overall rate constant (k 0) is related to the overall mass transfer coefficient (k m) and the reaction rate constant (k) as kkm () k 0 k k (B) k k k 0 kk m k k (C) k m 0 (D) k k k 0 m 83. eactant forms three products X, Y and Z irreversibly, as shown below, m m Linked nswer Questions 80 and 8: liquid phase reaction, B, is conducted isothermally in a CST having a residence time of s. The inlet concentration of species is mole / litre, and the outlet concentration is mole / liter. kc The rate law for the reaction is r, K C where k = 5 mole / liter / s. The reaction rates are given by r x= k x C, r y = k y C.5 and r z = k z C. The activation energies for formation of X, Y and Z are 40, 40 and 5 kj / mol respectively. The pre exponential factors for all reactions are nearly same. The desired conditions for MXIMIZING the yield of X are 9 ll ights eserved
() High temperature, high concentration of (B) High temperature, low concentration of (C) Low temperature, high concentration of (D) Low temperature, low concentration of 84. For a first order catalytic reaction the Thiele modulus (ф) of a spherical pellet is defined as s 3 kpa D where, ρ p = pellet density, s = pellet radius, De = effective diffusivity k = first order reaction rate constant If ф> 5, then the apparent activation energy (E a) is related to the intrinsic (or true) activation energy (E) as () E a = E 0.5 e (B) E a = 0.5 E (C) E a = E (D) E a = E 85. The following figures show the outlet tracer concentration profiles (c vs. t) for a pulse input. () P II, Q IV, III (B) P IV, Q III, I (C) P III, Q IV, II (D) P I, Q III, II Linked nswer Questions 86 and 87: 86. In an aqueous solution, reaction P Q occurs under isothermal conditions following first order kinetics. The feed rate is 500 cm 3 / min and concentration of P in the feed is.5x0 4 mole / cm3. The reaction is carried out in a 5 litre CST. t steady state, 60 % conversion is observed. The rate constant (in min ) is () 0.06 (B) 0.5 (C) 0. (D) 0.8 87. The 5 liter CST is replaced by five CSTs is series. If the capacity of each new CST is liter, then the overall conversion (in %) is () 65 (B) 67 (C) 73 (D) 8 (Gate 0) th 88. The half-life of an n order reaction in a batch reactor depends on Match the figures in Group I with the reactor configurations in Group II. Group I Group II P Figure I PF Q Figure II CST Figure 3 III PF and CST in Series IV PF and CST in Parallel () Only the rate constant (B) Only the rate constant and the order of the reaction (C) Only the rate constant and the initial reactant concentration 30 ll ights eserved
(D) Only the rate constant and the initial reactant concentration, and the order of the reaction 89. Consider the reaction scheme shown B C first order. The activation energies for k and k are 80 and 0 kj / mol k K. Both the reactions are respectively. To maximize the yield of B, it is preferable to use () CST and high temperature (B) PF and high temperature (C) CST and low temperature (D) PF and low temperature 90. The rate controlling step for the solid catalyzed irreversible reaction B C is known to be the reaction of adsorbed w- ith adsorbed Bto give adsorbed C. if P, is the partial pressure of component i and K is the adsorption equilibrium constant of component I, then the form the Langmuir Hinshel wood rate expression will be () PP B ate K P K P K P B B c C (B) ate PP B K P K P K P B B C C PP (C) ate B K P K P K P PP (D) ate P 0.5 C B B B C C 9. The elementary reversible exothermic gas-phase reaction 3B C is to be conducted in non-isothermal, non-adiabatic plug flow reactor. The maximum allowable i reactor temperature is Tmax to minimize the total reactor volume the variation of reactor temperature (T) with axial distance from the inlet (z) should be Linked nswer Question 9 and 93: The first order liquid phase reaction P is conducted isothermally in a plug flow reactor having 5 liter volume. The inlet volumetric flow rate is liter/min and the inlet concentration of is mol / liter. 9. If the exit concentration of is 0.5 mole/liter, then the constant, in min, is () 0.06 (B) 0.8 (C) 0.4 (D) 0.64 93. The plug flow reactor is replaced by 3 mixed flow reaction in series, each of.0 liters volume. The exit conversion is () 35.9 (B) 5.5 (C) 73.7 (D) 94.8 (Gate 03) 94. The exit age distribution for a reactor is given by E(t) = δ(t 4), where t is in 3 ll ights eserved
seconds. first order liquid phase reaction (k = 0.5 s ) is carried out in this reactor under steady state and isothermal conditions. The mean conversion of the reactant at the exit of the reactor, up to digits after the decimal point, is 95. n isothermal liquid phase zero order reaction B (k = 0.5 mol/m 3 -s) is carried out in a batch reactor. The initial concentration of is mol/m 3. t 3 seconds from the start of the reaction, the concentration of in mol/m 3 is 96. The overall rates of an isothermal catalytic reaction using spherical catalyst particles of diameters mm and mm are r and r (in mol (kg-catalyst) h ), respectively. The other physical properties of the catalyst particles are identical. If pore diffusion resistance is very high, the ratio r /r is 97. The gas phase decomposition of azomethane to give ethane and nitrogen takes place according to the following sequence of elementary reactions. Using the pseudo-steady-stateapproximation for [(CH 3) N ]*, the order with respect to azomethane in the rate expression for the formation of ethane, in the limit of high concentrations of azomethane, is 98. first order liquid phase reaction is carried out isothermally at a steady state in a CST and 90% conversion is attained. With the same inlet conditions and for the same overall conversion, if the CST is replaced by two smaller and identical isothermal CSTs in series, the % reduction in total volume, to the nearest integer, is Common Data Questions 99 00 Liquid reactant decomposes as follows: n aqueous feed of composition C 0 = 30 mol/m 3, C 0 = mol/m 3, and C S0= mol/m 3 enters a CST in which the above reactions occur. ssume isothermal and steady state conditions. 99. If the conversion of is 80 %, the concentration of in the exit stream in mol/m 3, to the nearest integer, is 00. What is the % conversion of, to the nearest integer, so that the concentration of S in the exit stream is.8 mol/m 3 (Gate 04) 0. In order to achieve the same conversion under identical reaction conditions and feed flow rate for a nonautocatalytic reaction of positive order, the volume of an ideal CST is () lways greater than that of an ideal PF (B) lways smaller than that of an ideal PF (C) Same as that of an ideal PF (D) Smaller than that of an ideal PF only for first order reaction 0. The vessel dispersion number for an ideal CST is 3 ll ights eserved
() - (B) 0 (C) (D) 03. homogeneous reaction ( P ) occurs in a batch reactor. The conversion of the reactant is 67% after 0 minutes and 80% after 0 minutes. The rate equation for this reaction is () (C) r k (B) r kc r kc (D) 3 r kc 05. 04. vapour phase catalytic reaction (Q + S) follows ideal mechanism ( and S are not adsorbed). Initially, the mixture contains only the reactants in equimolar ratio. The surface reaction step is rate controlling. With constants a and b, the initial rate of reaction ( r 0 ) in terms of total pressure (P T) is given by ap ap T () r (B) r T 0 0 bp bp ap T (C) r 0 (D) bp 05. Match the following: T T r T ap T 0 bp Group Group (P) Tank in series (I) Non-isothermal model reaction (Q)Liquid-liquid (II) Mixer-settler extraction ()Optimum (III) PF with axial temperature mixing progression (S) Thiele modulus (IV) Solid catalyzed reaction T (B) P I, Q II, III, S IV (C) P III, Q I, II, S IV (D) P III, Q II, I, S IV (Gate 05) 06. For which reaction order, the halflife of the reactant is half of the full lifetime (time for 00% conversion) of the reactant? () Zero order (B) Half order (C) First order (D) Second order 07. n irreversible, homogeneous reaction products, has the rate expression: ate of. C 0. C 50C,where C is the concentration C varies in the range 0.5 50 mol/m 3. For very high concentration of, the reaction order tends to: () 0 (B) (C).5 (D) 08. Which of the following can change if only the catalyst is changed for a reaction system? () Enthalpy of reaction (B) ctivation energy (C) Free energy of the reaction (D) Equilibrium constant nswer () P II, Q IV, I, S III 33 ll ights eserved
09. The impulse response to a tracer pulse experiment for a flow reactor is given below: It is observed that when the recycle ratio = 0.5, the exit conversion X f = 50% When the recycle ratio is increased to =, the new exit conversion (in percent) will be: () 50.0 (B) 54.3 (C) 58.7 (D) 63. In the above figure, c is the exit tracer concentration. The corresponding E or E θ (normalized E) curve is correctly represented by which of the following choices? Here, θ is dimensionless time. 0. n isothermal steady state mixed flow reactor (CST) of m 3 volume is used to carry out the first order liquid-phase reaction products. Fresh feed at a volumetric flow rate of Q containing reactant at a concentration C 0 mixes with the recycle steam at a volumetric flow rate Q as shown in the figure below.. catalyst slab of half-thickness L (the width and length of the slab>> L) is used to conduct the first order reaction B. t 450 K, the Thiele modulus for this system is 0.5. The activation energy for the first order rate constant is 00 kj/mol. The effective diffusivity of the reactant in the slab can be assumed to be independent of temperature, and external mass transfer resistance can be neglected. If the temperature of the reaction is increased to 470 K, then the effectiveness factor at 470 K (up to two decimal place) will be. Value of universal gas constant = 8.34 J/mol.K. Consider two steady isothermal flow configuration shown schematically as Case I and Case II below. In case I, a CST of volume V is followed by a PF of volume V, while in Case II a PF of volume V is followed by a CST of volume V. In each case, a volumetric flow rate Q of liquid reactant is flowing through the two units in series. n irreversible reaction products (order n) takes place in both cases, with a reactant concentration C0 being fed into the first unit. 34 ll ights eserved
represent the first order rate constants in unit of s. (Gate 06) 3. For a non catalytic homogeneous reaction B, the rate expression at 300 K 0C 3 is r, mol m s where C is 5C the concentration of (in mol / m 3 ). Theoretically, the upper limit for the magnitude of the reaction rate ( r in mol m 3 s, rounded off to the first decimal place) at 300 K is 4. The variations of the concentrations (C, C and C S) for three species (, and S) with time, in an isothermal homogeneous batch reactor are shown in the figure below. Select the reaction scheme that correctly represents the above plot. The numbers in the reaction schemes shown below, 5. Hydrogen iodide decomposes through the reaction HI H + I. The value of the universal gas constant is 8.34 J mol K. The activation energy for the forward reaction is 84000 J mol. The ratio (rounded off to the first decimal place) of the forward reaction rate at 600 K to that at 550 K is 6. The liquid phase reversible reaction B is carried out in an isothermal CST operating under steady state conditions. The inlet stream does not contain B and the concentration of in the inlet stream is 0 mol/lit. the concentration of at the reactor exit, for residence times of s and 5 s are 8 mol/lit and 5 mol/lit, respectively. ssume the forward and backward reactions are elementary following the first order rate law. lso assume that the system has constant molar density. The rate constant of the forward reaction (in s, rounded off to the third decimal place) is 7. liquid phase irreversible reaction B is carried out in an adiabatic CST operating under steady state conditions. The reaction is elementary and follows the first order rate law. For this reaction, the figure below shows the conversion (X ) of as a 35 ll ights eserved
function of temperature (T) for different values of the rate of reaction ( in mol ms ) denoted by the numbers to the left of each curve. This figure can be used to determine the rate of the reaction at a particular temperature, for a given conversion of. (B) Since the reaction rate is much greater than the diffusion rate, Scenario occurs (C) Since the reaction rate is much lower than the diffusion rate, Scenario occurs (D) Since the reaction rate is much lower than the diffusion rate, Scenario occurs 9. CST has a long inlet pipe. tracer is injected at the entrance of the pipe. The E-curve obtained at the exit of the CST is shown in the figure below. The inlet stream does not contain B and the concentration of in the inlet stream is 5 mol/m 3. The molar feed rate of is 00 mol/s. steady state energy balance for this CST results in the following relation: T=350+5 X where T is the temperature (in K) of the exit stream and X is the conversion of in the CST. For an exit conversion of 80 % of, the volume (in m 3, rounded off to the first decimal place) of CST required is 8. porous pellet with Pt dispersed in it is used to carry out a catalytic reaction. Following two scenarios are possible. Scenario : Pt present throughout the pores of the pellet is used for catalyzing the reaction. Scenario : Pt present only in the immediate vicinity of the external surface of the pellet is used for catalyzing the reaction. t a large value of Thiele modulus, which one of the following statements is TUE? ssuming plug flow in the inlet pipe, the ratio (rounded off to the second decimal place) of the volume of the pipe to that of the CST is (Gate 07) 0. The following reaction rate curve is shown for a reaction P. Here, r and x represent reaction rate conversion, respectively. The feed is pure and 90% conversion is desired () Since the reaction rate is much greater than the diffusion rate, Scenario occurs 36 ll ights eserved
molar flowrate of B leaving the reactor, rounded to decimal is places, is mol/s 3. The C-curve measured during a pulse tracer experiment is shown below, in the figure C (t) is the concentration of the tracer measured at the reactor exit in mol/liter at time t seconds. Which amongst the following reactor configurations gives the lowest total volume of the reactor (s)? (a) CST followed by PF (b) Two CST in series (C) PF followed by CST (d) single PF. The flowing liquid second order reaction is carried out in an isothermal CST at steady state 3 0 005 r. C mol / m.hr Where, C is the concentration of reactant in the CST. The reactor volume is m 3, the inlet flow rate flow rate is 0.5 m 3 /hr and the inlet concentration of the reactant is is 000 mol/m 3 the fractional conversion, rounded to decimal places is.. eaction B is carried out in a reactor operating at steady state and mol/s of pure at 45 0 C enters the reactor. The outlet stream leaves the reactor a 35 0 C. The heat input to the reactor is 7 kw. The heat of reaction at the reference temperature of 5 0 C is 30 kj mol. The specific heat capacities (in kj/mol.k) of and B are 0. and 0.5, respectively, The The mean residence time in the reactor, rounded to decimal place, is s. 4. The reversible reaction of t butyl alcohol (TB) and ethanol (EtOH) to ethyltbuty ether (ETBE)is TB + EtOH ETBE + H O The equilibrium constant for this reaction is K C =. Initially, 74 g of TB is mixes with 00g of aqueous solution containing 46 weight % ethanol. The molecular weights are : 74 g /mol for TB. 46 g/mol for EtOH, 0 g/mol for ETBE, and 8 g/mol for water. The mass of ETBE at equilibrium rounded to decimal place is g. 5. The following gas phase reaction is carried out in a constant volume isothermal batch reactor + B +S The reactants and B as well as the product S are non condensable gases. t the 37 ll ights eserved
operating temperature, the saturation pressure of the product is 40 kpa. Initially, the batch reactor contains equimolar amounts of and B (and no products) at a total pressure of 00 k Pa. The initial concentrations of the reactants are C C. 56 mol/m 3. The 0 0. B. rate of reaction is given by 0 08 r. C C B mol/m 3.s The time at which just starts condensing, rounded to decimal place, is (Gate 08) 6. For a chemical reaction, the ratio of rate constant at 500K to that at 400K is.5. Given = 8.34 J mol - K -, the value of activation energy (in kj/mol) is () 0.5 (B).0 (C) 5. (D) 8.4 7. Liquid phase isomerization of o-xylene to p-xylene using a zeolite catalyst was carried out in a CST. Three sets of kinetic data at different temperatures and stirring speeds were obtained as shown below. Set Temperature(K) 500 500 500 Stirring 000 speed(rpm) 000 3000 eaction rate (mol L - s ) 0.00 0.05 0.05 Set B Set C 600 700 600 700 600 700 000 000 3000 0.037 0.047 0.047 000 000 3000 0.069 0.078 0.086 The operating condition at which the reaction rate is not controlled by external mass transfer resistance is () T = 500 K ; rpm = 3000 (B) T = 600 K ; rpm = 000 (C) T = 700 K ; rpm = 000 (D) T = 700 K ; rpm = 000 8. CST and a PF of equal volume are connected in series to carry out a first order, isothermal, liquid phase reaction P. The rate constant is 0. s -. The space-time is 5 s for both the reactors. The overall fractional conversion of is (rounded off to third decimal place ) 9. The elementary second-order liquid phase reaction B C D is carried out in an isothermal plug flow reactor of m 3 volume. The inlet volumetric flow rate is 0 m 3 /hr. The initial concentrations of both and B are kmol/m 3. The rate constant is given as.5 m 3 kmol - h -. The percentage conversion of is 30. set of standard stainless steel pipes, each of internal diameter 6.65mm and 6000 mm length, is used to make a plug flow reactor by joining them in series to carry out degradation of polyethylene. Seven such pipes are required to obtain a conversion of 66% at 450K. The minimum number of standard 8000 mm long pipes of the same internal diameter to be procured for obtaining at least 66% conversion under the same reaction conditions is. 3. Hydrogenation of benzene is to be carried out using Ni (density = 890 kg/m 3 ) as catalyst, cast in the form of non-porous hollow cylinders, as shown below. The reaction occurs on all the surfaces of the 38 ll ights eserved
hollow cylinder. During an experiment, one such cylinder is suspended in the reactant stream. If the observed rate of reaction is 0.39 mol (m of catalyst surface ) - min -, then the rate of reaction in mol (kg of catalyst) - min - is (rounded off to three decimal places). 0.40, then the value of Y Q at 60 o C is rounded off to second decimal place) 3. In a laboratory batch setup, reaction of P over a catalyst was studied at various temperatures. The reactions occurring are P Q; P t the end of one hour of operation, the batch contains x, x Q and x mole fractions P of P, Q and components respectively. The mole fractions of product components ( x and x ) were found to vary linearly with Q temperature as given in the figure If the yield of Q based on reactant P consumed (Y Q) at 5 o C was found to be 39 ll ights eserved
nswer Key Table B B 3 B 4 5 6 C 7 B 8 C 9 B 0 D B C 3 D 4 5 C 6 C 7 C 8 D 9 0 B 3 D 4 B 5 C 6 D 7 C 8 C 9 30 B 3 B 3 D 33 D 34 35 C 36 37 B 38 D 39 40 C 4 4 C 43 C 44 D 45 46 D 47 C 48 D 49 B 50 C 5 B 5 B 53 C 54 55 D 56 B 57 58 59 60 6 C 6 D 63 B 40 ll ights eserved
64 65 C 66 67 C 68 C 69 B 70 C 7 C 7 73 C 74 B 75 C 76 B 77 D 78 79 80 B 8 C 8 83 B 84 B 85 86 B 87 C 88 D 89 B 90 B 9 C 9 C 93 C 94 0.63 95 0.5 96 0.5 97 98 5 99 0 00 90 0. 0. D 03. B 04. C 05. D 06. 07. B 08. (B) 09. (C) 0. ().0. 7. (B) 3. 4. (C) 5. 8.5 6. 0.667 7. 8m 8. (B) 9. 0.5 0. (). 0.80. 0.6 3..0 4. 0.4 5. 4 6. (C) 7. () 8. 0.8 9. 50% 30. 6 3. 0.0385 3. 0.4 4 ll ights eserved
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