P4.36 100 gmol/min of a solution of 70 mol % ethanol/30 mol % water is fed to a reactor operating at steady state, along with 80 gmol/min of air (79 mol % N₂, 21 mol % O₂). Ethanol (C₂H5OH) reacts with oxygen to make acetaldehyde (CH,CHO). Acetaldehyde is further oxidized to acetic acid (CH₂COOH). Write the two stoichiometrically balanced chemical equations. What is the byproduct of the reactions? What is the limiting reactant? If there is 100% conversion of the limiting reactant and the production rate of acetaldehyde is 25 gmol/min, calculate the fractional conversion of the excess reactant, the yield of acetaldehyde from ethanol, and the composition and flow rate of the reactor effluent stream.

1) A 2.000 [m^3] tank is receiving an influent of 500 [m^3/d]. a. What is the hydraulic retention time [d] for the given flow rate! b. Assume that the design safety-factor (SF) for this tank 1s 2.What is the design minimum hydraulic retention time (Omin) for this tank?

The Air Quality Standard for sulfur dioxide(SO2) is 0.03 ppm. Express this as mg/m3 at 1 atm and 25 °C. a) 0.786 mg/m3 b) 0.0846 mg/m3 c) 0.846 mg/m3 d) 0.0786 mg/m3

3. In a shell-and-tube heat exchanger under design condition, the cooling water gets heated from 30°C to 45°C while the process stream is cooled from 100°C to 60°C. Due to fouling only in the process side, the mass flowrate of water has to be increased to 160% of the design flow to maintain the process side outlet temperature at its design value with the same design flowrate of the process stream. Express the fouling heat transfer coefficient (ho), which is the inverse of the fouling heat transfer resistance, as a multiple of process side heat transfer coefficient (ho). Assume that under design condition, there is no fouling. Also assume that all the resistance to heat transfer is on the process side.

1. It is desired that the heating duty of a shell-and-tube heat exchanger be scaled up as much as possible. Under nominal condition a process stream (a liquid) is heated from 120°C to 160°C without any phase change by condensing steam on the shell side at 250°C. The process side has a bypass which remains closed under nominal condition. The maximum increase in the process side pressure drop through the heat exchanger can be only 44%. Some portion of the process stream can be bypassed, if needed, but it is desired that the temperature of the mixed stream after the bypass and the exchanger outlet streams are mixed remains at 160°C. The maximum increase in the steam flowrate is 50%, but the pressure of the condensing steam can be changed to change the condensation temperature. Show your work. Assume that both the tube-side and shell-side heat transfer coefficients do not change due to scaleup. Assume that the change in the density and specific heat of the process stream due to temperature is negligible. a. What is the maximum possible scaleup? b. What would be the required steam condensation temperature for the maximum scaleup?

4. In a packed-bed absorber, solvent and gas inlet flow rates are 25 kmol/h and 90 kmol/h,respectively under design conditions. Under these design conditions, solute mole fractions in the gas at the inlet and outlet are 0.012 and 0.006, respectively. The absorber has 25 transfer units and its operating pressure is 2 bar. Assume tower is operating isothermally (note absorption is generally exothermic, but for simplicity assume isothermal operation) at 60°C under base case condition a. The solvent flowrate got decreased by 20% due to some issue with the solvent pump.What is the new outlet mole fraction of solute? b. Since the solvent pump problem cannot be solved in a while, it is decided to decrease the tower operating temperature by decreasing the solvent temperature. When the tower temperature (assume the tower operates isothermally) became 30°C, outlet mole fraction of solute becomes same as the design condition. What are the values of A and B in the Antoine Equation for the solute? Assume that the solute follows Raoult's law. Vapor pressure of the solute is given by the Antoine equation: In p* = A- B/T when P* is in bar and T is in K

2. Fill in the blanks. Batch ___________ Semi Batch Transient, ______ Steady State, Open _____, ______ Coffee is made using a variety of methods, but all of them involve using hot water to extract the flavor compounds out of coffee beans. A simplified process for making coffee is given below. 1) Grind roasted coffee beans using a coffee grinder. 2) Heat water. 3) Pour hot water over ground coffee in a filter. 4) Collect the water in a pot. 5) Dispose of spent coffee grounds. 1. Using the process description above, create a basic block flow diagram of the CO2 process for decaffeination showing all the steps. 2. Now create a new process flow diagram by substitute equipment symbols (see below) for the blocks. 3. Label the streams. 4. Create a stream table.

Answer the following question, using the equilibrium diagram of water-ethylene glycol-furfural system given in following link Determine the percentage of water when furfural composition is 60 wt.%.

B) the time-value solution once the step is applied, (3 points)

P4.14 Dimethyl carbonate (DMC, C₂H₂O3) can be synthesized by a process called oxidative carbonylation of methanol: A gas containing 80 mol % CH3OH and 20 mol % CO at 2000 gmol/h is mixed with air (79 mol % N₂ and 21 mol % O₂) and then fed to a reactor operating at steady state, where the reaction takes place. The flow rate of the stream leaving the reactor is 2264 gmol/h, and this stream contains no O₂. Draw a flow diagram and write the correct form of the material balance equations for all compounds in this system. Determine the flow rate of air to the reactor, the extent of reaction 4, and the composition (mol %) of the reactor effluent.