Question

Gas absorption is used in the field of purification by allowing the transfer of pollutants from the gas phase to the liquid phase, and it helps in meeting the regulatory requirements for the release of gases into the environment. Assume that you are a newly employed Chemical Engineer and your supervisor wants to test how well you understand mass transfer concepts through the following question that deals with the separation of component A. A gas stream contains 4.0 mol% A, and its content must be reduced to 0.5 mol% in a packed absorption tower that operates at 101.325 kPa and 293 K. The inlet pure solvent B flow is 68.0 kmol/h and the total inlet gas flow is 57.8 kmol/h. The tower diameter is 747 mm. The gas-liquid equilibrium data is listed in Table 1, and the local film mass-transfer coefficients are as follows: ka = 0.0739 kmol/m3.s.mol fraction; ka = 0.169 kmol/m.s.mol fraction. If the system obeys Henry's law and/or using the design methods for dilute gas mixtures, determine the height of the absorption tower in cm. Table 1. The gas-liquid equilibrium data at 1 atm Mole fraction of A in liquid Partial pressure of A in gas (mm Hg) 20C 30C 0.0 0.0208 0.0268 0.0309 0.0405 0.0503 0.0737 0.0960 0.1370 0.0 9.0 15.0 18.2 24.9 31.7 50.0 69.9 114.0 0.0 19.3 24.4 29.6 40.1 51.0 79.7 110 179

          Gas absorption is used in the field of purification by allowing the transfer of pollutants from the gas phase to the liquid phase, and it helps in meeting the regulatory requirements for the release of gases into the environment. Assume that you are a newly employed Chemical Engineer and your supervisor wants to test how well you understand mass transfer concepts through the following question that deals with the separation of component A. A gas stream contains 4.0 mol% A, and its content must be reduced to 0.5 mol% in a packed absorption tower that operates at 101.325 kPa and 293 K. The inlet pure solvent B flow is 68.0 kmol/h and the total inlet gas flow is 57.8 kmol/h. The tower diameter is 747 mm. The gas-liquid equilibrium data is listed in Table 1, and the local film mass-transfer coefficients are as follows: ka = 0.0739 kmol/m3.s.mol fraction; ka = 0.169 kmol/m.s.mol fraction. If the system obeys Henry's law and/or using the design methods for dilute gas mixtures, determine the height of the absorption tower in cm.

Table 1. The gas-liquid equilibrium data at 1 atm
Mole fraction of A in liquid
Partial pressure of A in gas (mm Hg)
20C
30C
0.0 0.0208 0.0268 0.0309 0.0405 0.0503 0.0737 0.0960 0.1370
0.0 9.0 15.0 18.2 24.9 31.7 50.0 69.9 114.0
0.0 19.3 24.4 29.6 40.1 51.0 79.7 110 179
        
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gas absorption is used in the field of purification by allowing the transfer of pollutants from the gas phase to the liquid phase and it helps in meeting the regulatory requirements for the 54831

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Chemistry: Structure and Properties
Chemistry: Structure and Properties
Nivaldo Tro 2nd Edition
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Gas absorption is used in the field of purification by allowing the transfer of pollutants from the gas phase to the liquid phase, and it helps in meeting the regulatory requirements for the release of gases into the environment. Assume that you are a newly employed Chemical Engineer and your supervisor wants to test how well you understand mass transfer concepts through the following question that deals with the separation of component A. A gas stream contains 4.0 mol% A, and its content must be reduced to 0.5 mol% in a packed absorption tower that operates at 101.325 kPa and 293 K. The inlet pure solvent B flow is 68.0 kmol/h and the total inlet gas flow is 57.8 kmol/h. The tower diameter is 747 mm. The gas-liquid equilibrium data is listed in Table 1, and the local film mass-transfer coefficients are as follows: ka = 0.0739 kmol/m3.s.mol fraction; ka = 0.169 kmol/m.s.mol fraction. If the system obeys Henry's law and/or using the design methods for dilute gas mixtures, determine the height of the absorption tower in cm. Table 1. The gas-liquid equilibrium data at 1 atm Mole fraction of A in liquid Partial pressure of A in gas (mm Hg) 20C 30C 0.0 0.0208 0.0268 0.0309 0.0405 0.0503 0.0737 0.0960 0.1370 0.0 9.0 15.0 18.2 24.9 31.7 50.0 69.9 114.0 0.0 19.3 24.4 29.6 40.1 51.0 79.7 110 179
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question-3-a-counter-current-packed-bed-absorption-column-is-to-be-designed-to-remove-sulphur-dioxide-soz-from-an-air-stream-using-pure-waterthe-column-operates-at-atmospheric-pressure-and-r-77386

Question 3. A counter-current packed-bed absorption column is to be designed to remove sulphur dioxide (SO2) from an air stream using pure water. The column operates at atmospheric pressure and room temperature, 25°C. The inlet gas at a flow rate of 120 kmol/h contains 6 mol% of SO2. The column is designed to reduce SO2 concentration in exit gas to 0.5%. The overall mass transfer coefficient based on gas phase (K'y) is 3x10^-5 mol/(m^2 s mole fraction of A / mole inert). The absorption column has a dimension of 1.5 m^2 cross-sectional area and 3.5 m packed height and operates at 50% efficiency. The equilibrium relationships of SO2 in the gas and liquid phase can be represented in the table as follows where; Table 1. Equilibrium data of Water-SO2 system. x, mole fraction of A in liquid phase | y, mol fraction of A in gas phase 0 | 0 0.0002 | 0.00668 0.0004 | 0.01336 0.0006 | 0.02004 0.0008 | 0.02672 0.0010 | 0.03340 0.0012 | 0.04008 0.0014 | 0.04676 0.0016 | 0.05344 0.0018 | 0.06012 0.0020 | 0.06680 (i) Write the operating line equation of this process. [2 MARKS] (ii) Calculate the minimum and actual amount of water required for this absorption. (Rule of thumb: the solvent rate used is 1.5 of the minimum solvent rate). [8 MARKS] (iii) Estimate the number of theoretical and actual stages of absorption required. [4 MARKS] (iv) Determine the flux of mass transfer at the top of the column. [3 MARKS] (v) Calculate the number of transfer unit required and height of transfer unit for this absorption column. [5 MARKS] (vi) Discuss the effect of solvent flowrate in sizing and operating the absorption column. [3 MARKS]

Sri K.

quostion-ihito-160-marks-in-an-absorption-tower-or-absorber-gas-conlacled-wilh-liquid-under-condilions-such-ihal-cne-or-more-species-ihe-gas-dissolve-in-the-liquid-stripping-tower-or-strippe-58443

In an absorption tower (or absorber), a gas is contacted with a liquid under conditions such that one or more species in the gas dissolve in the liquid. A stripping tower (or stripper) also involves a gas contacting a liquid, but under conditions such that one or more components of the feed liquid come out of solution and exit in the gas leaving the tower. A process consisting of an absorption tower and a stripping tower is used to separate the components of a gas containing 30.0 mole% carbon dioxide and the balance methane. A stream of this gas is fed to the bottom of the absorber. A liquid containing 0.500 mole% dissolved CO2 and the balance methanol is recycled from the bottom of the stripper and fed to the top of the absorber. The product gas leaving the top of the absorber contains 1.00 mole% CO2 and essentially all of the methane fed to the unit. The CO2-rich liquid solvent leaving the bottom of the absorber is fed to the top of the stripper and a stream of nitrogen gas is fed to the bottom. Ninety percent of the CO2 in the liquid fed to the stripper comes out of solution in the column, and the nitrogen/CO2 stream leaving the column passes out to the atmosphere through a stack. The liquid stream leaving the stripping tower is the 0.500% CO2 solution recycled to the absorber. The absorber operates at temperature Ta and pressure Pa and the stripper operates at Ts and Ps. Methanol may be assumed to be nonvolatile—that is, none enters the vapor phase in either column—and N2 may be assumed insoluble in methanol. (i) In your own words, explain the overall objective of this two-unit process and the functions of the absorber and stripper in the process. (ii) Taking a basis of 100 mol/h of gas fed to the absorber, draw and label a flowchart of the process. For the stripper outlet gas, label the component molar flow rates rather than the total flow rate and mole fractions. (iii) Do the degree-of-freedom analysis and write in order the equations you would solve to determine all unknown stream variables except the nitrogen flow rate entering and leaving the stripper. Circle the variable(s) for which you would solve each equation (or set of simultaneous equations), but don't do any of the calculations yet. (iv) Calculate the fractional CO2 removal in the absorber (moles absorbed/mole in gas feed) and the molar flow rate and composition of the liquid feed to the stripping tower. (v) Calculate the molar feed rate of gas to the absorber required to produce an absorber product gas flow rate of 1000 kg/h.

Adi S.

question-3-a-counter-current-packed-bed-absorption-column-is-to-be-designed-to-remove-sulphur-dioxide-soz-from-an-air-stream-using-pure-waterthe-column-operates-at-atmospheric-pressure-and-r-77386

Question 3. A counter-current packed-bed absorption column is to be designed to remove sulphur dioxide (SO2) from an air stream using pure water. The column operates at atmospheric pressure and room temperature, 25°C. The inlet gas at a flow rate of 120 kmol/h contains 6 mol% of SO2. The column is designed to reduce SO2 concentration in exit gas to 0.5%. The overall mass transfer coefficient based on gas phase (K'y) is 3x10^-5 mol/(m^2 s mole fraction of A / mole inert). The absorption column has a dimension of 1.5 m^2 cross-sectional area and 3.5 m packed height and operates at 50% efficiency. The equilibrium relationships of SO2 in the gas and liquid phase can be represented in the table as follows where; Table 1. Equilibrium data of Water-SO2 system. x, mole fraction of A in liquid phase | y, mol fraction of A in gas phase 0 | 0 0.0002 | 0.00668 0.0004 | 0.01336 0.0006 | 0.02004 0.0008 | 0.02672 0.0010 | 0.03340 0.0012 | 0.04008 0.0014 | 0.04676 0.0016 | 0.05344 0.0018 | 0.06012 0.0020 | 0.06680 (i) Write the operating line equation of this process. [2 MARKS] (ii) Calculate the minimum and actual amount of water required for this absorption. (Rule of thumb: the solvent rate used is 1.5 of the minimum solvent rate). [8 MARKS] (iii) Estimate the number of theoretical and actual stages of absorption required. [4 MARKS] (iv) Determine the flux of mass transfer at the top of the column. [3 MARKS] (v) Calculate the number of transfer unit required and height of transfer unit for this absorption column. [5 MARKS] (vi) Discuss the effect of solvent flowrate in sizing and operating the absorption column. [3 MARKS]

Adi S.


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