Derive the Kremser equation analytically to solve dilute-gas absorption based design problems. Kremser equation is defined in Wankat Equation 12-22 (pp. 466; section 12.4 of 3rd edition textbook). Remember to define all variables/parameters used and clearly state all assumptions.

Ironmaking and steelmaking face challenges of reducing energy consumption and environment pollution. What is your proposal to make ironmaking and steelmaking more sustainable?

Pressure in a storage tank is maintained at 1 MN/m² to supply water at 20^oC and atmospheric pressure through 200 m (equivalent length, including fittings) of drawn steel tubing (30 mm OD, 6 mm wall thickness). What flow rate of water can be maintained?

Calculate the dew point temperature (to the nearest ºC); the corresponding vapor pressures of ethanol and methanol (units of mm Hg); and the equilibrium liquid molar compositions associated with a saturated vapor mixture containing 30% by mole ethanol and the balance methanol. Pressure of the system is 1 atm(abs).

Assume 400 ft3/min (measured at STP) of a gas mixture (Stream F) at 150 °F and 1.70 atm is fed to a reactor. The mixture consists of 65 mol% methane and 35 mol% ethane. Air (Stream A) at 75 °F and 1.20 atm is fed to the reactor in 20% excess. Aside from the excess air, the flue gas from the reactor contains only CO2 and H2O(vapor), and comes out at 1300 °F and 1.0 atm. Assume all pressures are observed by reading a pressure gauge. Keep the units used in your solution consistent with those in the problem statement.

a). Draw a labeled flowchart. Be sure to show units for all rates and compositions. Use the names (F, A, etc.) given in the description.

b). Calculate the molar flow rate (lbmol/min) of the gas mixture (Stream F) fed to the reactor.

c). Solve for the required volumetric flow rate of the air stream. Express your answer as ft3/min of air at STP conditions.

d). Calculate the volumetric flow rate of the furnace stack gas in units of ft3/min.

A particular power plant operates with a heat-source reservoir at 350°C and a heat-sink reservoir at 30°C. It has a thermal efficiency equal to 67% of the Carnot-engine thermal efficiency for the same temperatures.

What is the thermal efficiency of the plant?

The thermal efficiency of the plant is  .

A steady-flow adiabatic turbine (expander) accepts gas at conditions T₁, P₁ and discharges at conditions T₂, P₂. Assuming ideal gases, determine (per mole of gas) W, W_ideal, W_lost, and S_G for the following case. Take T_σ = 300 K and R = 8.314 J·mol⁻¹·K⁻¹.

T₁ = 530 K, P₁ = 8 bar, T₂ = 424 K, P₂ = 1.6 bar, and C_P/R = 7/2.

The following data were obtained for the adsorption of n-butane on a porous solid (catalyst).  

Calculate the area (in m²) occupied by a n-butane molecule at 150°C.

You have nitrogen at a temperature of 145 K and a volume of 0.061629 m3 / kmol. Determine the pressure of this gas with the following methods (with R=8.314 KPam^3/kmolK). And determine the percentage deviation presented by each equation of state if the actual nitrogen pressure at these conditions is 100 atm.

a) ideal gas

b) Vander Walls

c) Beattie Bridgeman. with A0 =136.2315, a=0.02617, B0=0.05046, b=-0.0061, c=4.20x10^4

d) Redlich Kwong

e) Peng Robison With w=0.038

f) Benedict web rubin. With a=2.54, A0=106.73, b=0.002328, B0=0.4074, c=7.379x10^4, C0=8.164x10^5, α=1.272x10^-4, ϒ=0.0053

consider a natural gas pipeline. The pipeline is made of steel of thickness 2.00 cm. The steel is coated on the inside with a 0.100 mm layer of Ni. The concentration of natural gas inside the pipeline is 0.100 kg/m3. The concentration outside is 0 kg/m3. The diffusion coefficient of natural gas in Ni is 2.01 x 10-21 m2/s and the diffusion coefficient of natural gas in steel is 7.00 x 10-17 m2/s. Calculate the flux of natural gas through the pipe assuming steady-state and linear geometry.

a. 1.89 x 10-15 kg/(m2.s)

b. 5.27 x 10-16 kg/(m2.s)

c. 2.00 x 10-18 kg/(m2.s)

d. 9.91 x 10-15 kg/(m2.s)

100 moles/min of a mixture of 40 mol% n-pentane and 60 mol% n-heptane are fed through a valve into a flash tank. The flash tank operates at 600 mmHg. A T-xy diagram is provided on the next page. (a) Determine the bubble point and dew point of the feed mixture at 600 mmHg. (b) If the flash tank is operating at 60 0C determine; a. the compositions of the streams leaving the flash tank b. the flow rate in liters/min of the stream leaving the top of the flash tank.

The steam used during the production of alumina in the Bayer process serves as both a heating and process fluid. Some steam is recycled, but some is condensed, clarified, and used for hot water in the plant before being cooled in a forced draft cooling tower and discharged.Most of worldwide bauxite mining and alumina production takes place in Jamaica. Therefore, the source of process water for most plants is the Caribbean Sea. Seawater is desalinized and sent as “slightly saline” water to the plant for use as makeup water.Bleedoff is removed from the tower when it has reached approximately thesaltconcentration of the seawater to which it is discharged.What is the makeup rate (in kg/h) of slightly saline water to a 75 kW-ratedcooling tower?

i need the solution with comsol

Consider a large plane wall of thickness L 5 0.4 m, ther- mal conductivity k 5 2.3 W/m·K, and surface area A 5 20 m 2 . The left side of the wall is maintained at a constant temperature of 95°C, while the right side loses heat by convection to the surrounding air at T ` 5 15°C with a heat transfer coefficient of h 5 18 W/m 2 ·K. Assuming steady one-dimensional heat transfer and taking the nodal spacing to be 10 cm, ( a ) obtain the finite difference formulation for all nodes, ( b ) determine the nodal temperatures by solving those equations, and ( c ) evaluate the rate of heat transfer through the wall

The molar enthalpy of a binary liquid system of species 1 and 2 at fixed T and P is represented by the equation:

H=400x1+600x2+x1x2(40x1+20x2)

where H is in J/mol. Determine expressions for Hbar1 and Hbar2 as functions of x2, numerical values for the pure-species enthalpies H1 and H2, and numerical values for the partial enthalpies at infinite dilution Hbae1infinity and Hbar2infinity.