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Problem 29-6E. Natural gas from a "fracking" operation containing hydrogen sulfide vapor enters to the headspace of an enclosed, continuous-flow tank, as shown below (Figure 29-6Ea). The gas exiting the headspace contains 98 mole% CH4 gas and 2 mole% H₂S vapor (A = H₂S). Fresh liquid brine water (salt water) containing no dissolved H₂S enters the tank at a volumetric rate of 0.324 m³/hr. We are concerned that some of the H₂S vapor in the gas space may dissolve into the brine water at the gas/liquid interface. The process operates at 40 °C, and the gas headspace is pressurized at 1.5 atm total system pressure. Both the bulk liquid and gas headspace are well mixed, with gas film coefficient for H₂S transfer of ky = 7.5 x 10³ gmole/m²-sec, and liquid film mass transfer coefficient of kx = 1.4 gmole/m²-sec. The brine water has a mass density of 1030 kg/m³, with an average molecular weight of 18.4 g/gmole. Linear equilibrium distribution data for H₂S vapor in brine water at 40 °C are presented in Figure 29-6Eb. The diameter of the cylindrical tank is 4.0 m. (a) What is the overall gas phase mass transfer coefficient, KG? (b) What is the concentration of dissolved H₂S in the outlet liquid, CAL? As part of this analysis, develop a material balance model in algebraic form. CH4 + H₂S GAS IN brine water IN D = 4.0 m Vo = 0.324 m³/hr CAL,O=0 gmole/m³ P = 1.5 atm, T = 40 °C YA = 0.02 CAL ㄒ well-mixed Figure 29-6Ea. Transfer of H₂S from fracking gas to brine tank. LIQ gas OUT liquid OUT V=0.324 m³/hr CAL = ? gmole/m³

Problem 29-6E. Natural gas from a "fracking" operation containing hydrogen sulfide vapor enters to the headspace of an enclosed, continuous-flow tank, as shown below (Figure 29-6Ea). The gas exiting the headspace contains 98 mole% CH4 gas and 2 mole% H₂S vapor (A = H₂S). Fresh liquid brine water (salt water) containing no dissolved H₂S enters the tank at a volumetric rate of 0.324 m³/hr. We are concerned that some of the H₂S vapor in the gas space may dissolve into the brine water at the gas/liquid interface. The process operates at 40 °C, and the gas headspace is pressurized at 1.5 atm total system pressure. Both the bulk liquid and gas headspace are well mixed, with gas film coefficient for H₂S transfer of ky = 7.5 x 10³ gmole/m²-sec, and liquid film mass transfer coefficient of kx = 1.4 gmole/m²-sec. The brine water has a mass density of 1030 kg/m³, with an average molecular weight of 18.4 g/gmole. Linear equilibrium distribution data for H₂S vapor in brine water at 40 °C are presented in Figure 29-6Eb. The diameter of the cylindrical tank is 4.0 m. (a) What is the overall gas phase mass transfer coefficient, KG? (b) What is the concentration of dissolved H₂S in the outlet liquid, CAL? As part of this analysis, develop a material balance model in algebraic form. CH4 + H₂S GAS IN brine water IN D = 4.0 m Vo = 0.324 m³/hr CAL,O=0 gmole/m³ P = 1.5 atm, T = 40 °C YA = 0.02 CAL ㄒ well-mixed Figure 29-6Ea. Transfer of H₂S from fracking gas to brine tank. LIQ gas OUT liquid OUT V=0.324 m³/hr CAL = ? gmole/m³

Introduction to Chemical Engineering Thermodynamics
Introduction to Chemical Engineering Thermodynamics
8th Edition
ISBN:9781259696527
Author:J.M. Smith Termodinamica en ingenieria quimica, Hendrick C Van Ness, Michael Abbott, Mark Swihart
Publisher:J.M. Smith Termodinamica en ingenieria quimica, Hendrick C Van Ness, Michael Abbott, Mark Swihart
Chapter1: Introduction
Section: Chapter Questions
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Problem 29-6E. Natural gas from a "fracking" operation containing hydrogen sulfide vapor enters to the headspace of an enclosed, continuous-flow tank, as shown below (Figure 29-6Ea). The gas exiting the headspace contains 98 mole% CH4 gas and 2 mole% H₂S vapor (A = H₂S). Fresh liquid brine water (salt water) containing no dissolved H₂S enters the tank at a volumetric rate of 0.324 m³/hr. We are concerned that some of the H₂S vapor in the gas space may dissolve into the brine water at the gas/liquid interface. The process operates at 40 °C, and the gas headspace is pressurized at 1.5 atm total system pressure. Both the bulk liquid and gas headspace are well mixed, with gas film coefficient for H₂S transfer of ky = 7.5 x 10-³ gmole/m²-sec, and liquid film mass transfer coefficient of kx = 1.4 gmole/m²-sec. The brine water has a mass density of 1030 kg/m³, with an average molecular weight of 18.4 g/gmole. Linear equilibrium distribution data for H₂S vapor in brine water at 40 °C are presented in Figure 29-6Eb. The diameter of the cylindrical tank is 4.0 m. (a) What is the overall gas phase mass transfer coefficient, KG? (b) What is the concentration of dissolved H₂S in the outlet liquid, CÂ? As part of this analysis, develop a material balance model in algebraic form. CH4 + H₂S GAS IN brine water IN V = 0.324 m³/hr CAL,O = 0 gmole/m³ D = 4.0 m P = 1.5 atm, T = 40 °C YA = 0.02 CAL LIQ well-mixed Figure 29-6Ea. Transfer of H₂S from fracking gas to brine tank. gas OUT liquid OUT V = 0.324 m³/hr = ? gmole/m³ CAL
Transcribed Image Text:Problem 29-6E. Natural gas from a "fracking" operation containing hydrogen sulfide vapor enters to the headspace of an enclosed, continuous-flow tank, as shown below (Figure 29-6Ea). The gas exiting the headspace contains 98 mole% CH4 gas and 2 mole% H₂S vapor (A = H₂S). Fresh liquid brine water (salt water) containing no dissolved H₂S enters the tank at a volumetric rate of 0.324 m³/hr. We are concerned that some of the H₂S vapor in the gas space may dissolve into the brine water at the gas/liquid interface. The process operates at 40 °C, and the gas headspace is pressurized at 1.5 atm total system pressure. Both the bulk liquid and gas headspace are well mixed, with gas film coefficient for H₂S transfer of ky = 7.5 x 10-³ gmole/m²-sec, and liquid film mass transfer coefficient of kx = 1.4 gmole/m²-sec. The brine water has a mass density of 1030 kg/m³, with an average molecular weight of 18.4 g/gmole. Linear equilibrium distribution data for H₂S vapor in brine water at 40 °C are presented in Figure 29-6Eb. The diameter of the cylindrical tank is 4.0 m. (a) What is the overall gas phase mass transfer coefficient, KG? (b) What is the concentration of dissolved H₂S in the outlet liquid, CÂ? As part of this analysis, develop a material balance model in algebraic form. CH4 + H₂S GAS IN brine water IN V = 0.324 m³/hr CAL,O = 0 gmole/m³ D = 4.0 m P = 1.5 atm, T = 40 °C YA = 0.02 CAL LIQ well-mixed Figure 29-6Ea. Transfer of H₂S from fracking gas to brine tank. gas OUT liquid OUT V = 0.324 m³/hr = ? gmole/m³ CAL
PA (atm) 0.06 0.05 0.04 0.03 0.02 0.01 0.00 0.0 0.5 1.0 CAL (gmole/m³) 1.5 2.0 Figure 29-6Eb. Equilibrium distribution of H₂S between gas phase and brine water at 40 °C.
Transcribed Image Text:PA (atm) 0.06 0.05 0.04 0.03 0.02 0.01 0.00 0.0 0.5 1.0 CAL (gmole/m³) 1.5 2.0 Figure 29-6Eb. Equilibrium distribution of H₂S between gas phase and brine water at 40 °C.
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