Methylamine using the following gas-phase reaction: 2CH,NH,→ (CH,),NH+NH, This reaction converts the methylamine to dimethylamine at 130°C, using a silica-alumina catalyst. The molar flow rate into a packed-bed reactor is 30 mol/s and the entering pressure is 16 atm. Assume there is no pressure drop or temperature change in the reactor. The reaction rate follows an elementary rate law. k₁-4.25 x 10-6 and K, -2.5 mol atm-gcatalyst-s a) Write the rate law solely in terms of conversion. b) What is the equilibrium conversion, Xe? c) How many kilograms of catalyst would be needed to load in a PBR to obtain a conversion of 0.9Xe? d) Plot X, and rate law interms of catalyst weight.

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13.7 mole Boron Trichloride (BCl3) enter a reactor with 52.4 mole water for the following reaction: BCl3 + 3 H2O → H3BO3 + 3 HCl 18.2 mole HCl are formed.  Calculate the fractional conversion of the limiting reactant.Note: fractional conversions go from 0 to 1

* The standard reaction enthalpy for the hydrogenation of propene is -124 KJ/mole. The standard reaction enthalpy for the combustion of propane is -2220 KJ/mole. What is the standard enthalpy of combustion (in KJ/mole) of propene given that the enthalpy of formation for liquid water is -285.5 KJ/mole? NOTE: Express answer in the NEAREST WHOLE NUMBER.

Direct dehydrogenation of ethylbenzene to styrene is carried out in the vapor phase with steam over a catalyst consisting primarily of iron oxide. The reaction is endothermic, and can be accomplished either adiabatically or isothermally. Both methods are used in practice. The major reaction is the reversible, endothermic conversion of ethylbenzene to styrene and hydrogen: C6H3CH₂CH CoHsCHCH₂ + H₂ AH= 124.9 kJ/mol Competing thermal reactions degrade ethylbenzene to benzene C6H3CH₂CH3C6H6+ C₂H4 AH 101.8 kJ/mol Styrene also reacts catalytically to toluene: CH3CH₂CH3 + H2 CH3CH3 + CH4 AH=64.5 kJ/mol The reactions take place at 620°C. The costs are as shown in Table 1. The production rate of styrene is 200 mol/h. Chemical name Formula Cost (S/kmol) Ethylbenzene C6H5CH₂CH3 57.1 Styrene C.HSCHCH₂ 75.9 Benzene C6H6 32.8 Toluene C6H5CH3 25.8 Hydrogen H₂ 1.2 (as fuel) Methane CH4 4.0 (as fuel) Ethylene C₂H4 6.7 (as fuel) Correlation for the product selectivity and distribution are given as…

Please help me with this one as soon as you can and show all the work for the enthalpy table. I provided the problem statement and the enthalpy table I need filled out please show the work for it.

Two perfectly mixed vessels of 10 liters each and both at 1 atm and 120 °C are respectively filled with n-butanol C4H9OH and air. At time t = 0, the two vessels are via a pipe connected to each other at 120 °C and 1 atm. This pipe has a length of 10 cm and a diameter of 1 cm. No reaction occurs during the mixing of the gases. All performing gas phases are assumed to be ideal. For the calculation of the molecular diffusivity, the Fuller's equation used. How long does it take for the partial pressure of n-butanol in the air vessel to reach 0.01 atm (in h)? Hints for the second part: - at any time point (so also at t= 0) forms the formula derived in the course for equimolar counter-diffusion under steady state conditions is a good approximation for the occurring flux. - at any time holds that c(butanol, vessel 1) = 31 mol/m3 - c(butanol, vessel 2) with the two concentrations in mol/m3 answer: t = 2.45 h

Product B is produced in a batch reactor according to the elemental reversible reaction (A⇋B) in liquid phase. The reactor volume is 10 L and the reaction temperature is 60°C. The initial concentration of reagent A is 3 lbmol/L, the rate constant for the forward reaction is k1=6.0 h-1, and the rate constant for the reverse reaction is k2=0.53h-1. Determine: (a) Plot the concentration of each species as a function of reaction time(b) Plot the conversion as a function of reaction time

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One of the ways that benzene is produced on a large scale is the hydrodealkylation of toluene. C,H,CH; + H, C,H, + CH4 A stream of toluene is mixed with a recycle stream and enters a reactor along with a stream of pure hydrogen. The reaction products at 550 °C enter a condenser, where they are cooled to 41.0 °C. A vapor stream containing Y5CH, = 0.600 mol CH,/mol leaves the process, and a liquid stream containing x66 = 0.810 mol benzene/mol and x6 = 0.190 mol toluene/mol enters a distillation column. The distillate of the column leaves the process at n7 = 668.0 mol/h and contains y7h = 0.9000 mol benzene/mol and y7 = 0.1000 mol toluene/mol. The bottoms of the column contains X8b = 0.250 mol benzene/mol and xgt = 0.750 mol toluene/mol and is recycled back to the fresh feed. Hydrogen is fed into the process at ni = 1183 mol H,/h. This process is carried out at 760 mmHg. A n, mol/h mol H/mol YSH2 YSCH, mol CH_/mol Ysh mol b/mol Ys mol t/mol n̟ mol/h n, mol/h Condenser Улн, тol H/mol Усн,…