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Previous year question hub

Distillation and Absorption - Mass Transfer - Chemical Engineering Previous Year Questions

Practice Distillation and Absorption - Mass Transfer - Chemical Engineering previous year questions organised from real papers, with year-wise coverage and clear topic navigation.

17Papers
17Years
44Questions
1Topics

Distillation and Absorption question pattern

Every graph below is calculated only from this selection.

Questions by year

Year-wise coverage for Distillation and Absorption. Each bar uses a separate theme-derived color.

Difficulty distribution

How the classified questions are distributed by difficulty.

Medium 33 75%
Easy 8 18.2%
Hard 3 6.8%

Question type distribution

MCQ, numerical, multiple-select and other formats found in these papers.

MCQ 32 72.7%
Numerical Answer Type (NAT) 11 25%
Fill in the blanks 1 2.3%

Subject weightage

Top subjects by unique question coverage.

Chemical Engineering
44 Qs

Most asked topics

Top topics across the included previous year papers.

Mass Transfer
44 Qs

Subtopic coverage

Top subtopics inside this exact selection.

Distillation and Absorption
44 Qs

Paper coverage

Question coverage for the most populated papers. Every active PYP paper remains listed below.

Chemical Engineering (CH) 2026
4 Qs
Chemical Engineering (CH) 2024
3 Qs
Chemical Engineering (CH) 2023
2 Qs
Chemical Engineering (CH) 2022
1 Qs
Chemical Engineering (CH) 2021
1 Qs
Chemical Engineering (CH) 2020
3 Qs
Chemical Engineering (CH) 2019
4 Qs
Chemical Engineering (CH) 2018
2 Qs
Chemical Engineering (CH) 2017
2 Qs
Chemical Engineering (CH) 2014
2 Qs
Chemical Engineering (CH) 2013
3 Qs
Chemical Engineering (CH) 2012
2 Qs
Chemical Engineering (CH) 2011
2 Qs
Chemical Engineering (CH) 2010
1 Qs
Chemical Engineering (CH) 2009
6 Qs
Chemical Engineering (CH) 2008
4 Qs
Chemical Engineering (CH) 2007
2 Qs

Included previous year papers

Newest papers appear first. Sort by year, question coverage or name.

PaperYear / sessionQuestions in this viewOpen
Chemical Engineering (CH) 202620264View paper
Chemical Engineering (CH) 202420243View paper
Chemical Engineering (CH) 202320232View paper
Chemical Engineering (CH) 202220221View paper
Chemical Engineering (CH) 202120211View paper
Chemical Engineering (CH) 202020203View paper
Chemical Engineering (CH) 201920194View paper
Chemical Engineering (CH) 201820182View paper
Chemical Engineering (CH) 201720172View paper
Chemical Engineering (CH) 201420142View paper
Chemical Engineering (CH) 201320133View paper
Chemical Engineering (CH) 201220122View paper
Chemical Engineering (CH) 201120112View paper
Chemical Engineering (CH) 201020101View paper
Chemical Engineering (CH) 200920096View paper
Chemical Engineering (CH) 200820084View paper
Chemical Engineering (CH) 200720072View paper

All Distillation and Absorption previous year questions

Practice every matching question in batches of 20, with every available option.

1
2007 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2007
If \(T_A\) and \(T_B\) are the boiling points of pure A and pure B respectively and \(T_{AB}\) is that of a non-homogeneous immiscible mixture of A and B, then
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2
2007 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2007
In a distillation operation, it is desired to have a very high purity bottom product. Initially, a kettle-type reboiler is used at the bottom of the column and the following analytical equation is used to obtain the equilibrium trays in the exhausting section of the column
\[ N_p - m + 1 = \frac{\log \left[ \frac{x_m - x_w/\alpha}{x_w - x_w/\alpha}(1 - \bar{A}) + \bar{A} \right]}{\log(\bar{A})} \]
where \(x_m\) is the composition of the liquid leaving tray \(m\). Tray \(m\) is the last equilibrium tray obtained by a McCabe Thiele graph of the exhausting section. If the kettle-type reboiler is replaced by a thermo-syphon reboiler, the analytical equation, for the exhausting section will be
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3
2008 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2008
Q.16 In a countercurrent gas absorber, both the operating and equilibrium relations are linear. The inlet liquid composition and the exit gas composition are maintained constant. In order to increase the absorption factor
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4
2008 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2008

In a binary mixture containing components A and B, the relative volatility of A with respect to B is 2.5 when mole fractions are used. The molecular weights of A and B are 78 and 92 respectively. If the compositions are however expressed in mass fractions the relative volatility will then be

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5
2008 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2008

A batch distillation operation is carried out to separate a feed containing 100 moles of a binary mixture of A and B. The mole fraction of A in the feed is 0.7. The distillation progresses until the mole fraction of A in the residue decreases to 0.6. The equilibrium curve in this composition range may be linearized to y* = 0.7353 x + 0.3088. Here x and y are the mole fractions of the more volatile component A in the liquid and vapor phases respectively. The number of moles of residue is

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6
2008 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2008

A packed tower containing Berl saddles is operated with a gas-liquid system in the countercurrent mode. Keeping the gas flow rate constant, if the liquid flow rate is continuously increased,

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7
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009
The ratio of the liquid to gas flow rate in a counter-current gas absorption column is increased, at otherwise identical conditions. Which ONE of the following statements is TRUE ?
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8
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009

The feed to a binary distillation column has 40 mol % vapor and 60 mol % liquid. Then, the slope of the q-line in the McCabe-Thiele plot is

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9
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009
An equi-molar mixture of four hydrocarbons (1, 2, 3, 4) is to be separated into high purity individual components using a sequence of simple distillation columns (one overhead and one bottom stream). Four possible schemes are shown below.
Component\(K_i\)
16
23
32.5
41.1

Using the \(K_i\) (\(= y_i^*/x_i\)) values given above, the optimal scheme is

Question diagram

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10
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009
Match the equipment in Group I to the internals in Group II.
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11
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009
The mole fraction of methanol in the distillate is

Question diagram

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12
2009 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2009
If the enthalpy of the distillate with reference to the feed is 3000 kJ/kmol, and the enthalpy of the bottoms with reference to the feed is -1000 kJ/kmol, the heat duty of the preheater (\( Q_h \) in kJ/hr) is
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13
2010 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2010

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

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14
2011 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2011
The MINIMUM reflux ratio is
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15
2011 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2011
The feed is
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16
2012 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2012
In the McCabe-Thiele diagram, if the \( x \)-coordinate of the point of intersection of the \( q \)-line and the vapor-liquid equilibrium curve is greater than the \( x \)-coordinate of the feed point, then the quality of the feed is
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17
2012 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2012

An equimolar mixture of A and B (A being more volatile) is flash distilled continuously at a feed rate of 100 kmol/h, such that the liquid product contains 40 mol % of A. If the relative volatility is 6, then the vapor product, in kmol/h, is

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18
2013 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2013
The vapor-liquid equilibrium curve of a binary mixture A-B, may be approximated by a linear equation over a narrow range of liquid mole fractions (\(0.2 < x_A < 0.3\)) as follows \(y_A^* = 1.325 x_A + 0.121\). Here \(y_A^*\) is the mole fraction of A in the vapor. 100 moles of a feed (\(x_{A,F} = 0.28\)) is batch distilled to a final residue (\(x_{A,W} = 0.2\)). Using the Rayleigh equation, the number of moles of the residue left behind in the distillation unit, up to 2 digits after the decimal point, is ______
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19
2013 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2013
The vapor liquid equilibrium relation for an ideal binary system is given by y_A^* = \frac{\alpha_{AB} x_A}{1 + (\alpha_{AB} - 1) x_A} Here x_A and y_A^* are the mole fractions of species A in the liquid and vapor, respectively. The relative volatility (\alpha_{AB}) is greater than unity. The liquid mole fraction x_A at which the maximum difference between the equilibrium vapor mole fraction and liquid mole fraction occurs is
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20
2013 · Chemical Engineering · Mass Transfer · Distillation and Absorption
Chemical Engineering (CH) 2013
A liquid having the composition found in the first part of the linked answer question, is flash distilled at a steady state to a final liquid mole fraction of 0.25. If \alpha_{AB} is 2.5, the fraction of the feed vaporized is
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Showing 20 of 44 questions