Part of Dr. Ritchey’s work in her previous job involved boiling and condensing hydrocarbon mixtures. In one of her experiments, she used a binary mixture of n-pentane (density 39.1 lbm/ft^3) and p-xylene (density 53.8 lbm/ft^3). One outlet stream of her condenser was measured to have a flow rate of 32 ft^3/min and a concentration of 30/70 n-pentane/p-xylene by volume. The other outlet stream was measured to have a flow rate of 24 ft^3/min and a concentration of 50/50 n-pentane/p-xylene by volume. If the system operates at steady state and the only inlet to her condenser has a flow rate of 56 ft^3/min, what is the inlet concentration of n-pentane in % by volume?

Your answer should be between 0 and 100. Round your answer to 1 decimal place for entry into eCampus. Do not enter units. Example: 12.3

Note: 30/70 by volume means that 30% of the volume is n-pentane and 70% of the volume is p-xylene.

1. Calculate the theoretical flame temperature for CO gas burned at constant pressure with 100% excess air, when the reactants enter at 100°C.

Please show work, do not copy the solution founded. show your solution! if you can not answer this question, then do not attempt to copy others' work.  

Question 1: Liquid (A) flows down as a thin film over the outside surface of a vertical flat plate 1.5 m wide (W = 1.5 m) and 3.5 m long (L = 3.5). Inert gas (B) flows across (perpendicular to) the width of the flat plate at a speed of 5 m/s. The supply of (A) is 0.27 mol/s at one end of the plate and the flow is considered to be turbulent. The gas composition of (A) at the edge of the film is 14% and in the bulk 0%. (B) can be assumed non-diffusing (NB = 0). The system is not dilute.

Viscosity of liquid (A), µA = 0.0000161 Pa×s = 1.61x10-5 Pa×s

Diffusion coefficient of A through B, DAB = 1x10-5 m2 /s

Density of A, rA = 1.2 kg/m3

Total concentration, c = 44 mol/m3

How many meters of the plate will be dry from (A)? ‘show your working out’

Q2) Show calculations for the creation of the following solutions from solid and 18.1 M H₂SO₄ stock solution.

a)   25.00 mL of 0.1000 M potassium iodide solution in 0.2000 M H₂SO₄

b)   25.00 mL of 0.1000 M potassium permanganate in 0.1500 M H₂SO₄

c)  To solution “a”, 3 % hydrogen peroxide is added.  In a reddish solution appears.  The reddish color is due to the formation of I_2.   Write the balanced REDOX equation.  Make sure you explain the addition of sulfuric acid.  Is hydrogen peroxide an oxidation or reducing agent?

d) To solution “b”, 3 % hydrogen peroxide is added.  The purple solution becomes clear (formation of Mn²⁺)_.   Write the balanced REDOX equation.  Make sure you explain the addition of sulfuric acid.  Is hydrogen peroxide an oxidation or reducing agent?

A petroleum refinery can handle the processing of two grades of
crude oils, #1 and #2, to produce four kinds of products gasoline, kerosene, fuel oil and
residual.
The total costs include raw material costs and processing costs. The raw material costs for the
crude oils are $24/bbl for #1, and $15/bbl for #2. The processing costs are $0.5/bbl for #1, and
$1.0/bbl for #2.
The sales prices of the products are $36/bbl for gasoline, $24/bbl for kerosene, $21/bbl for fuel
oil and $10/bbl for residual.
The following is the information for the product yield (volume percent of raw material) and
maximum allowable production of each product (bbl/day):
One bbl crude oil #1 can produce 0.80 bbl gasoline, 0.05 bbl kerosene, 0.10 bbl fuel oil, and
0.05 bbl residual. One bbl crude oil #2 can produce 0.44 bbl gasoline, 0.10 bbl kerosene, 0.36
bbl fuel oil, and 0.10 bbl residual. The maximum allowable production for gasoline is 24,000
bbl/day, for kerosene is 2,000 bbl/day, and for fuel oil is 6,000 bbl/day, and no maximum
allowable production limitation for residual.
(1) Based on the data above, derive a mathematical formulation for this linear programming
problem and determine: The optimum feed schedule (bbl/day) of the two crude oils for the
maximum profit, using method of simultaneous equations. How much is the maximum profit
($/day)?
(2) Comment on how variation of raw material costs and sales prices will affect the feed
schedule and profitability on this kind of project in industry.

Fresh orange juice contains 12.0 wt% solids and the balance water is fed to an evaporator for
concentration process. The juice that enters the evaporator is concentrated to 58 wt%
solids. However, the volatile constituent of the juice somehow can escape with the water,
leaving the concentrate with a flat taste. It is suggested for the stream of fresh orange juice
to by-pass the evaporator at certain fraction and mixed with the evaporator product stream to
achieve the desired final concentration, which is 42.0 wt% solids.Calculate the amount of product produced and the fraction of the feed that by-pass the
evaporator. State clearly your assumption and basis of calculation.
Propose another possible way to preserve the volatile ingredients that provide the taste of the
concentrate and thereby obtain an even better tasting product. List down the advantages
and the drawbacks of your suggestion.

When and where did the Exxon Valdez oil spill occur? How large was the tanker? How much oil did it carry? What is the use of these types of tankers? What were the causes of the spilling? What species have been affected? Describe the water quality now approximately 25 yrs after the spill. What new rules or regulations have been put into place to help prevent such a spill from happening again? What methods were in used at the time of the sill? What methods are used now? Don't forget the references used!!! WIKIPEDIA IS NOT A SCIENTIFIC ENCYCLOPEDIA!!!

In the production of sunflower oil, sunflower solid containing 13.5 wt% oil and 86.5 wt% solids
are ground and fed to the stirred tank, along with the recycled stream of liquid ethanol,
C2H5OH. The ground sunflowers are suspended in liquid for certain time to allow maximum
extraction of sunflower oil into the ethanol. The stirred tank effluent passes to a filter.
The filter cake contains 75.0 wt% sunflower solids and the balance sunflower oil and ethanol,
the latter two in the same ratio in which they emerge from the stirred tank. The filter cake is
discarded and the liquid filtrate is fed to a heated evaporator in which the ethanol is vaporized
and the oil remains as a liquid product. Subsequently, the ethanol vapor is cooled and
condensed, and the liquid ethanol condensate is recycled to the stirred tank.
By taking a feed ratio of 3 kg ethanol/kg sunflower, construct a complete block diagram with
label. Calculate flowrate and compositions at each stream. State clearly your assumptions
and basis of calculation.
An additional unit operation (heat exchanger) might be added to the process. With brief
explanation, suggest the most suitable location to install the unit. Write down your opinion
and conclusions on how the incorporation of this unit might or might not improve the process
economics.

(23marks)

Ice balls of 10 mm diameter at – 30°C are exposed to an air current at 15°C with a convection heat transfer coefficient of 200 W/m2 -K. Determine the time when the surface layer will begin to melt. Also determine the center temperature. Use the following property values: density = 920 kg/m3 , specific heat 2040 J/kg-K, thermal conductivity = 2.00 W/m-K.

1. A feed of 4,535 kg/h of a 2% wt. salt solution at 38 C enters continuously a single-effect evaporator and is being concentrated to 3% wt. The efficiency of the evaporator is at 85%. The evaporator is at atmospheric pressure and the area of the evaporator is A= 69.7 m2. Saturated steam at 110 C is supplied for heating (90% quality). Since the solution is dilute, it can be assumed to have the same boiling point as water. The heat capacity of the feed can be taken as Cp=4.10 Kj/kg C. If the evaporator is operating at atmospheric pressure 101.3 kPa (absolute). Calculate
   1. Amount of steam needed (kg/h) per one kg/h of water removed
   2. Calculate overall heat transfer coefficient, U. if the heat exchanger works in a counter-current flow

Sulfur dioxide is emitted at a rate of 2 kg/s from the top of a chimney that is 120m high. The plume initially rises vertically a further 10m above the chimney exit, before being convected horizontally by a wind speed of 15m/s under conditions of neutral stability. The daytime isolation is moderate. Calculate

a) The concentration on the plume centre-line at a distance of 800m downwind of the chimney

b) The ground level concentration at a distance of 800m downwind of the chimney

c)The concentration at 1542m location

An adiabatic dehumidifier is used to extract excess moisture from the air inside your hostel room with dimension 8 x 6 x 3 m3 . The room was initially at a dry bulb temperature of 30 oC, 70 % relative humidity is to be humidified to 40 % relative humidity. a) Sketch the process in the phsychrometric chart provided b) Estimate the adiabatic saturation temperature of the entrance air and the final temperature (dry bulb) of the air. c) Calculate the amount moisture removed by the humidifier (in kg) d) Briefly explain how could you reduce the humidity further using the humidifier

a. Why does water become less dense as it freezes?
b. Why the ΔG mix , for nonideal solution is not always negative
c. To the thermodynamics of mixing of 2 components, find the mol fraction that has
the largest impact on the thermodynamic quantities of the final solution.
d. Calculate the effect that mixing 2 moles of nitrogen and 3 moles of oxygen has on the
entropy of the final solution at 27 o C.

A system undergoes a change in volume from 100 cm3 /mol to 225 cm3 /mol. The pressure of the model is predicted by, P = aT + B/T^3,

where a = 2.13x10-3 bar/K and

ß = 2.6x10-5 bar^3K^3.

Calculate AS at 350 K (in J/mol-K) b. What is the heat required at 350 K (in J/mol)? c.

Calculate AU for the system described (in J/mol-K)

SHOW ALL WORK.THANKS