Explain briefly the difference between a conventional power plant and a combined cycle power plant with the aid of neat diagrams.

Develop enzymatic rate expressions for competitive, noncompetitive, uncompetitive inhibitions using rapid equilibrium assumption.

One method of exploitation of an ore mine that contains 1 million metric tons of ore will result in a recovery of 70% of the available ore deposit and will cost $25 per ton of material removed. Another method of exploitation will recover 60% and will cost $20 per metric ton of material removed. Subsequent processing of the removed ore recovers 200 kg of metal from each ton of processed ore and cost $50 per metric ton of ore processed. The recovered metal can be sold for $2.0 per kg. Which method for developing the mine is preferred to maximize total profit from the mine?

One alternative to accelerate oil well production is to install a booster pump at the wellhead to reduce the pressure drop between the oil reservoir and the oil gathering station (onshore) or production platform (offshore). Make an economic analysis to verify if the production increment (between with and without booster pump) is economically attractive. The following data from an oil well subsea boosting project is available: Subsea equipment installation cost: $ 1.5 million 1 MW (Mega Watts) Pump system unit cost: $ 25.0 million Deep-water vessel rent for pipeline laying: $ 40 million total cost Overhead cost: assume 10% to total investment cost The installation and construction of the boosting system will be performed in one year. The revenue of this project is generated by oil well production increment using the booting system. An increment of 5,000 bopd (barrels of oil per day) in the first year of operation (after one year for installation and construction) is predicted, then, it will decline by 10% every year for a study period of 10 years. For example, 5000 bopd (initial increment), then 4500 bopd (in the next year), 4050 bopd, 3645 bopd, etc. Assume the oil well operates 330 days per year. The remaining 30 days, the well will not produce because it will be in maintenance (also called workover). Assume the well will produce oil only (no water). The market value of this equipment will be negligible at the end of the 10-year study period. Use MARR = 20% Calculate the present worth (PW) for this project assuming an oil-selling price of $40 per barrel and a production cost of $15 per barrel. In addition, add a constant value of $5 million per year for energy cost to run the pump boosting system. Is this project economically attractive? Draw a cash flow diagram for this project

Problem 2 (10%)

Estimate the simple payback period and the discounted payback period of problem 1.

Just answer problem 2 please

One alternative to accelerate oil well production is to install a booster pump at the wellhead to reduce the pressure drop between the oil reservoir and the oil gathering station (onshore) or production platform (offshore). Make an economic analysis to verify if the production increment (between with and without booster pump) is economically attractive. The following data from an oil well subsea boosting project is available: Subsea equipment installation cost: $ 1.5 million 1 MW (Mega Watts) Pump system unit cost: $ 25.0 million Deep-water vessel rent for pipeline laying: $ 40 million total cost Overhead cost: assume 10% to total investment cost The installation and construction of the boosting system will be performed in one year. The revenue of this project is generated by oil well production increment using the booting system. An increment of 5,000 bopd (barrels of oil per day) in the first year of operation (after one year for installation and construction) is predicted, then, it will decline by 10% every year for a study period of 10 years. For example, 5000 bopd (initial increment), then 4500 bopd (in the next year), 4050 bopd, 3645 bopd, etc. Assume the oil well operates 330 days per year. The remaining 30 days, the well will not produce because it will be in maintenance (also called workover). Assume the well will produce oil only (no water). The market value of this equipment will be negligible at the end of the 10-year study period. Use MARR = 20% Calculate the present worth (PW) for this project assuming an oil-selling price of $40 per barrel and a production cost of $15 per barrel. In addition, add a constant value of $5 million per year for energy cost to run the pump boosting system. Is this project economically attractive? Draw a cash flow diagram for this project

Suggest two methods for making the PStyrene-PButadiene-PStyrene (polystyrene-polybutadiene-polystyrene)
triblock copolymer in a batch reactor using n-BuLi as an initiator.

The following data are obtained at 0°C in a constant-volume batch reactor using pure gaseous

The stoichiometry of the decomposition is A → 2.5 R. Find a rate equation which satisfactorily represents this decomposition.

Exchanger
1. Problem Statement & Scope of Work
Ethylbenzene is manufactured by alkylation of benzene with ethylene. The reaction
products are separated in a series of distillation columns. Ethylbenzene is obtained as
the distillate from the last column (called the ethylbenzene column). In a 70 ton per
day ethylbenzene plant, the final product leaves the overhead condenser at 1350C.
This is required to be cooled to 400C before pumping it to the storage tank. Cooling
water is available at 300C for cooling. Please provide a proposal for the design of a
multi-pass counter-current Shell & Tube Heat Exchanger (Figure-1) that fulfils the
specifications in Section 3 (Process Data) and includes the following items:
Item 1: Do energy balance and find heat duty (Q) and water flow rate
Item2: First start trial with 1-1 pass counter current exchanger and do LMTD
calculation and find out area, assuming overall heat transfer coefficient
based on outside area, Udo
Item 3: Select tube BWG (i.d, o.d and length) from available market and number of
tubes required and linear velocity of water (a velocity above 1 m/s should be
maintained).Do selection of tube side and shell side fluid with proper
justification
Item 4: Start second trial with suitable tentative selection of tube passes (say 1-4
pass) and repeat calculation and find out tube specifications and number of
tubes (You may use Tube-sheet layout and tube count of a shell and tube
heat exchanger Table which are available in standard data book)
Item-5: Select 25% cut segmental baffles with 0.15 m (6 inch) baffle spacing and
shell specification
Item 6: Estimate the tube-side and shell-side heat transfer coefficient (hi) using any
suitable correlation. Number of correlations are available such as Dittus-
Boelter equation, Colburn jH factor etc. At this stage there are number of
decision options on baffle spacing, number of tube passes etc are available to
get reasonably high local heat transfer coefficients.
Item 7: Calculate the ‘clean’ Overall coefficient, U on the outside tube area basis.
and repeat the above calculation to get area required, tube specifications,
number of required tubes. Neglect dirt factor calculation for U.
Item-8: No need to do pressure-drop calculation exercise but you may discuss this
variable and its role on design calculation.
N.B. You may be referred for various data from standard data book or from
Chemical Eng handbook- by Perry if required
2
go through S&T H.E. design calculation from Process Heat Transfer book by D.
Q. Kern. My expectations are your approaches and method of calculations
2. Project Report
This is an individual self-study mini-project on Shell & Tube Heat Exchanger
equipment design. Individual student is to require a report writing covering all
sections of design items. The report should also include an executive summary, along
with brief conclusions and recommendations. Your approaches and method of
calculations are also important and carry significant weightage
3. Process Data
The allowable pressure drop is 0.15 kg/cm2 on both tube and shell sides.
Ethylbenzene at the mean liquid temperature (87.50C):
Density: 840 kg/m3
Specific heat: 2.093 kJ/kg.K
Viscosity: 0.33 cp =3.3 x 10-4 kg/m-s
Thermal conductivity: 0.1156 W/m K = 0.0994 kcal/h m K
Water at 350C (mean temperature)
Density: 993 kg/m3
Viscosity: 8 x 10-4 kg/m s
Specific heat: 4.175 kJ/kg K = 1.0 kcal/kg K
Thermal conductivity: 0.623 W/m.K = 0.536 kacl/h m2K
.

Explain the meaning of the pour point, flash point for crude oil

Explain in details why crude oil requires to be refined and explain how this process is done with suitable diagram.

i) Determine the sedimentation coefficient of sphere particles with 0.1 micrometer size and density of 1200 kg/m^3 in tetrahydrofuran (THF) at 25 degrees celcius which density of THF is 889 kg/m^3 and its viscosity is 0.456 mPa.s. ii) Assume the particle size is doubled, determine the sedimentation coefficient.

One of the primary functions of impact testing is to determine whether a material experiences a ductile-to-brittle transition. Clearly explain what it means when a material exhibits “ductile-to-brittle transition” behavior?