Design of Shell and Tube Heat Exchanger
Crude oil at 198°C is to be cooled to 39°C. The oil flow-rate is 6.127 kg/s. Cooling water
is available at 29°C and at the rate of 27.127 kg/s. The pressure drop allowance for each stream
is 100 kN/m2
. Design a suitable shell and tube heat exchanger for this duty.

The following are the properties of the two streams at the average temperature:

Data:
Assume overall heat transfer coefficient of 502 W/m2 K.
Tubes: 20 mm o.d., 16 mm i.d. tubes, 4 m long, square pitch 1.25do, carbon steel.
Pull through head, Floating Head type heat exchanger.
Baffle = 1/5 of the shell diameter and 25 % cut baffles
Fouling factors 0.0003 m2 K/ W for cooling water and 0.0002 m2 K/ W for crude oil
Thermal conductivity of metal = 57 W/m K

Present your results with detailed calculations to design Shell and Tube Heat Exchanger. Mention the various assumptions made in the calculations.

Estimate the cost of the heat exchanger.

Define (i.e. physical meaning) SRT, HRT, F/M ratio, SVI and indicate their importance during the operation of an activated sludge process in wastewater treatment plants.

Q1. What is the dominant form of benzoic acid at pH 2. Suggest the dominant form of caffeine at pH 2.

Q2. This lab uses a C18-reverse phase column. What does the stationary phase consists of? Is it polar or nonpolar?

Q3. Predict whether benzoic acid or caffeine will come out of the C18-reverse phase column first at pH 2.

Q4. To prepare the calibration standard solutions, calculate how much of each stock solution of sodium benzoate and caffeine should be added to each of the 25 mL volumetric flasks (See the procedure).

Q5. What are the peak absorption wavelengths of sodium benzoate and caffeine, respectively?

Describe the process of carbon dioxide absorption by a named solvent in a plate tower.

For IEUBK Model) 1.What assumptions are made when using this type of model? That is what values or relationships must the model include, which you did not supply. 2.What are the model supplied (“fixed") parameters which are assumed? 3.What are the user-supplied input variables required to run the model?

Discuss a number of waste removal/ disposal methods for chlorinated hydrocarbon solvents in the petrochemical industry

A gasoline storage tank drains by gravity to a tank truck; see the drawing. The pipe line between the tank and the truck is 100 m of 0.1 m diameter commercial steel pipe. The properties of gasoline are given as, density=720 kg/m3, dynamic viscosity = 0.0006 kg/m.s. Both tank and truck are open to the atmosphere, and the level in the tank is 10 m above the level in the truck. What is the volumetric flow rate of the gasoline? and how we choose moody chart

A gasoline storage tank drains by gravity to a tank truck; see the drawing. The pipe line between the tank and the truck is 100 m of 0.1 m diameter commercial steel pipe. The properties of gasoline are given as, density=720 kg/m3, dynamic viscosity = 0.0006 kg/m.s. Both tank and truck are open to the atmosphere, and the level in the tank is 10 m above the level in the truck. What is the volumetric flow rate of the gasoline? and how we choose moody chart

What types of analytes can be analyzed using gas chromatography? What types of analytes are unsuitable for analysis with this technique? Which would be expected to elute first on a polydimethyl sioxane column, butane, or butanol? Why? What factors determine relative retention time with gas chromatography?

What is the basis for separation in gas chromatography? (I.e. adsorption, partition, size exclusion, ion exchange, or affinity?)

1. A gas mixture containing a solute with a concentration of Y₁=0.02 to be absorbed in a packed tower. The gas-liquid equilibrium is described by: Y^*=1.0X.

(a) (10%) To achieve a 99% solute recovery, calculate the required gas phase overall mass transfer unit N_tOG and the composition X₁ at the liquid exit. X₂=0.0001 at the liquid inlet with L/G=1.2.

(b) (10%) For pure liquid inlet with L/G=0.8, what is the maximum percentage solute recovery?

2. For a packed tower for gas absorption operation, under a given operating condition, it is found that kya=kxa=0.026 kmol/m2.s. The equilibrium equation is given by: y=5x. Given that ky?G0.8, calculate the percentage reduction in overall mass transfer coefficient if the gas flow rate is doubled while the liquid flow rate remains unchanged.

Describe three techniques for “perpetual storage” of hazardous wastes. If you had to make a decision among the three techniques for disposing of dioxin-contaminated waste, would you be able to recommend one?

500 kmol/h of an air stream at a pressure of 2 atm is to be heated from 15 celsius to 90 celsius in a heat exchanger with 600 kPa steam condensing in the shell side of the heat exchanger. Steam enters the exchanger as a saturated vapor and leaves as a saturated liquid.

A) How much steam would be required if a conventional heat exchanger were used? what is the total entropy change during this process?
B) How much steam would be required if the process of heating the air was carried out by using the heat transferred from the steam to drive a reversible carnot engine and by using the air stream as the heat sink? what would be the total work output of this engine?

An air stream at 87.8°C having a humidity H = 0.030 kg H2O/kg dry air is contacted in an adiabatic saturator with water. It is cooled and humidified to 90% saturation. (a) What are the final values of H and T? (b) For 100% saturation, what would be H and T?

Air entering a dryer has a temperature (dry bulb) of 60°C and a dew point of 26.7°C. Using the humidity chart, determine the actual humidity H, percentage humidity HP, humid heat cS and humid volume vH.

An evaporator is used to concentrate 4536 kg/h of a 20% NaOH solution entering at 60?C to a product of 50% solids. The pressure of the saturated steam used is 170 kPa and the vapour space pressure of the evaporator is at 12 kPa. The overall coefficient U is 1560 W/m2K. Calculate the steam used, the steam economy (kg vaporized / kg steam used) and the heating surface area.