Introduction to Chemical Engineering Thermodynamics
8th Edition
ISBN: 9781259696527
Author: J.M. Smith Termodinamica en ingenieria quimica, Hendrick C Van Ness, Michael Abbott, Mark Swihart
Publisher: McGraw-Hill Education
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- do not type the answersarrow_forwardPLUG FLOW REACTOR/TUBULAR FLOW REACTOR (PFR) Aim: To determine the reaction rate constant (k) for the plug – flow assembly. I want a perfect discussion and analysis for this experimental result n=2arrow_forwardQuestion 1) The gas phase reaction (A→ B+C) must be carried out in a fixed-bed tubular reactor using a solid catalyst in a spherical shape of 0.4 cm in diameter. The reactor must operate isothermally at 573 K and an inlet pressure of 1 atm. The reaction is first order and the reactor is fed with pure A at a molar flow of FA0-1 g-mol/s. The internal diameter of the reactor must be 2.54 cm.It is known: -The reaction on the surface of the catalyst is of the type r₁=kCA.; -The particle density gp=2 g/cm3; -The porosity of the bed gl= 0.40.-This reaction, when carried out using the catalyst in powder form, obtained a speed of R 1 10-3 g-mol/g-cat.s, at a temperature of 573 K and pure reagent A at a pressure of 1 atm .-Consider that the reactor is being operated under conditions free from resistance to external mass transfer to the particle.-The effective molecular diffusivity in the gas phase (DAB) to solve this exercise must also be considered constant with the temperature and composition…arrow_forward
- 4.53 We wish to produce B in the reaction A → B in a continuous reactor at = 5 liter/min with CAo = 4 moles/liter. However, we find that there is a second reaction B → C that can also occur. We find that both reactions are first order and irreversible with k₁ = 1.0 min-¹ and k₂= 0.1 min-¹. Find T, V, CB.SB, and YB for 95% conversion of A in a PFTR and in a CSTR.arrow_forwardQUESTION IN IMAGEEarrow_forwardA → B is carried out isothermally in a continuous reactor. Calculate both the CSTR and PFR reactor volumes necessary to consume 99% of A (i.e. CA = 0.01 CAO) when the entering molar flow rate is nA0 = 5 mol/h assuming the reaction -TA is 1. -TA = k 2. -TA = KCA 3. -TA = KC² The entering volumentric flow rate is V = 10 dm³/h. (Hint: Make use of equality n 40 No consider a Batch Reactor (BR) with a volume of V = 1000 dm³. Take the three reaction O rates from above and caclulate the times necessary to consume 99.9% of species A if the initial concentration is CAO 0.5 mol/dm³. with k = 0.05 mol h-dm3 with k = 0.0001 with k=3 dm³ mol-h :CAO V) =arrow_forward
- You are designing a reactor for a process that has the following decomposition reaction: A →D + 2F The rate law for this reaction is unknown and must be determined by an experiment. Since the reaction takes place in the liquid phase, you choose to build a CSTR reactor. You allow the reactor to fill to a certain volume, V, and then adjust the inlet and outlet volumetric flow rates to equal values, vo, to allow the system to reach steady state. Once the system is at steady state you measure the outlet concentration, CA. The residence time (t = V/v.) is increased by turning off the outlet flow, which allows the volume to increase, then setting the outlet flow to its original value and waiting until steady state is reached. You measure the concentration again and repeat this procedure multiple times to obtain the following table. Measurement 1 2 (ii) 234 in 3 5 Residence Time (min) 15.0 38.0 100 300 1200 Concentration (mol/L) 1.50 1.25 1.00 0.75 0.50 The inlet concentration (containing…arrow_forwardThe liquid phase reaction A + B → C follows an elementary law of velocity and occurs isothermally in a flow-through system. The rules for the feed streams of A and B are 2.0 mol/L before mixing. The volumetric flow rate of each stream is 5 dm3/min, and the inlet temperature is 300 K. The streams are mixed just before entering. Two reactors are available. One is a 200 dm3 CSTR, which can be heated to 77oC or cooled to 0oC; another is an 800 dm3 PFR, operated at 300 K, which cannot be heated or cooled. Note that k = 0.07 dm3 / mol.min at 300K and E = 20 kcal / mol. (A) What conversion would be achieved if the CSTR and PFR were operated at 300K and connected in series? And in parallel with 5 mols/min each? (B)Knowing that the operating times (loading, unloading, heating, cleaning, etc.) of the batch reactor is around 3 h, what volume of batch reactor would be necessary to process, per day, the same amount of species A as in reactors with Flow so as to achieve 90% conversion?arrow_forwardProblem 4 The reversible, exothermic, liquid phase, homogeneous reaction A ₹R is being carried out in two ideal CSTRs. Both reactors operate at 150°C. The molar flow rate of A entering the first CSTR is 55,000 mol/h, the concentration of A in this stream is 6.5 mol/L, and the concentration of R is zero. The fractional conversion of A in the outlet stream from the second CSTR is 0.75. The fractional conversion is based on the molar flow rate entering the first CSTR. The reaction is first order in both directions. The rate constant for the forward reaction is 1.3 h-¹ and the equilibrium constant based on concentration at 150°C is 10.0. If the volume of the second CSTR is 10,000 L, what is the required volume of the first CSTR?arrow_forward
- QUESTION IN IMAGEEarrow_forwardplease work out all the partsarrow_forwardWhich of the following situations can we consider a recycle stream for a process with reacting units? a. The reactants are highly miscible with the products. b. The feed is a mixture of valuable compounds known to be toxic to humans. c. Separation of reactants from the product requires state-of-the-art technology. d. Raw feed to the reactor is extremely valuable and is found to be non-toxic to humans.arrow_forward
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