1000-1-design
The type of tray which gives greatest flexibility in distillation columns is:
1992-10-c-design
In the layout plan for a vacuum distillation unit, operating at 60 mm Hg, supported by a barometric condenser, the appropriate place for the location of vacuum drum for collecting the distillate will be
1995-2-j-design
Use of Raschig rings in place of crushed stones as packing in packed beds (other things being same)
1996-1-12-design
The reason for preferring packed towers over plate towers in distillation practice is that the packed tower operation gives
1997-1-28-design
Two iron pipes of the same nominal diameter but different schedule numbers will have
1997-1-30-design
In distillation columns, the number of bubble caps per tray primarily depends on the
1998-1-13-design
The advantage of using a 1-2 shell and tube heat exchanger over a 1-1 shell and tube heat exchanger is
1999-1-31-design
In a heat exchanger, floating head is provided to
2002-1-12-design
If the baffle spacing in a shell and tube exchanger increases, then the Reynolds number of the shell side fluid
2003-27-design
The variables required to be known in correlations used for estimating the horse power of gas compressor and hence its cost are
| P. inlet pressure | Q. compressor RPM |
| R. delivery pressure | S. volumetric flow rate at inlet |
2003-84-design
In distillation column sizing calculations by short cut methods, match the following:
| P. Underwood's equation | 1. Number of real trays |
| Q. Fenske's equation | 2. Column diameter |
| R. Gilliland's equation | 3. Minimum number of ideal trays |
| S. Vapor velocity at flooding | 4. Actual number of ideal trays |
| 5. Minimum reflux ratio | |
| 6. Tray efficiency |
2005-15-design
Baffles are used in heat exchangers in order to
2009-47-design
Match the equipment in Group I to the internals in Group II.
| GROUP I | GROUP II |
|---|---|
| P. Centrifugal pump | 1. Baffle |
| Q. Distillation column | 2. Impeller |
| R. Heat exchanger | 3. Tray |
| 4. Volute |
2010-25-design
The flooding velocity in a plate column, operating at 1 atm pressure, is 3 m/s. If the column is operated at 2 atm pressure, under otherwise identical conditions, the flooding velocity will be
2010-6-design
Which ONE of the following statements about baffles in a shell and tube heat exchanger is FALSE? Baffles
2011-24-design Two systems are available for compressing 6 m3/h of ambient air to 10 bar. The first one uses a single stage compressor (\(K_1\)) and the second one uses a multistage compressor with inter-stage cooling (\(K_2\)). Which ONE of the following
statements is INCORRECT?
2005-75-design What is the actual power required to drive a reciprocating air compressor which has to compress 34 m3 of air per minute from \(1.013\times 10^5\) N/m2 to \(4.052\times 10^5\) N/m2? Assume that \(PV^{1.25}\) is constant,
where \(P\) is the pressure and \(V\) is the volume, and the efficiency of the compressor is 85%.
2005-76-design
A separation column for vapor-liquid processes 200 kmol/h of vapor. The flooding velocity is 3 m/s. If the column operates at 85% of flooding velocity and the downcomer area is 10% of the total cross sectional area, what is the diameter of the column? Average density of vapor = 2 kg/m3 and its molecular weight = 44.
2006-65-design A saturated vapor is fed to a distillation column at 180 kmol/h. Both the rectifying and stripping sections of the column operate at 60% of their respective flooding velocities. The flooding velocity of the rectifying section is twice that of the stripping
section. The assumptions of constant molar overflow and constant molar vapor density throughout the column are valid. If the boil-up rate is 60 kmol/h, then the relationship between the diameters of the rectifying section (\(d_r\)) and the stripping
section (\(d_s\)) is
2007-46-design
The following list of options P, Q, R and S are some of the important considerations in the design of a shell and tube heat exchanger.
Pick out the correct combination of TRUE statements from the following:
2007-66-design
In a double pipe heat exchanger the ID and OD of the inner pipe are 4 cm and 5 cm respectively. The ID of the outer pipe is 10 cm with a wall thickness of 1 cm. Then, the equivalent diameters (in cm) of the annulus for heat transfer and pressure drop respectively are
2008-67-design In a shell and tube heat exchanger, if the shell length is \(L_S\), the baffle spacing is \(L_B\) and the thickness of the baffle is \(t_b\), the number of baffles on the shell side, \(N_B\), is
2012-45-design
In a 1-1 pass floating head type shell and tube heat exchanger, the tubes (od = 25 mm; id = 21 mm) are arranged in a square pitch. The tube pitch is 32 mm. The thermal conductivity of the shell side fluid is 0.19 W/m.K, and the Nusselt number is 200. The shell-side heat transfer coefficient (in W/m2.K), rounded off to the nearest integer, is __________
2001-19-design A packed gas liquid contactor employs ceramic Intalox saddles (38 mm). The gas flow rate, \(G\) = 1.5 kg/s and gas density, \(\rho_G\) = 1.5 kg/m\(^3\).
The liquid flow rate, \(L\) = 30 kg/s and liquid density, \(\rho_L\) = 1000 kg/m\(^3\). The column is to be designed for a pressure drop of 42 mm .
Norton's correlation for this pressure drop is \[K = \frac{13.1 G_w^2 F_p(\mu_L/\rho_L)^{0.1}}{\rho_G(\rho_L-\rho_G)}\] where \(K\) = flow coefficient, \(\mu_L\) = liquid viscosity = 10\(^{-3}\) N.s/m\(^2\), \(G_w\) = gas flow rate per unit cross sectional area, kg/m\(^2\).s,
\(F_p\) = packing factor = 170 m\(^{-1}\). \(K\) is given by the equation: \(K=0.62-0.5(m-0.5)\) for \(0.5\le m \le 1.0\) where \[m = \frac{L}{G}\sqrt{\frac{\rho_G}{\rho_L}}\] What is the diameter of the contactor (in m)?
Last Modified on: 02-May-2024
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