/*! This file is auto-generated */ .wp-block-button__link{color:#fff;background-color:#32373c;border-radius:9999px;box-shadow:none;text-decoration:none;padding:calc(.667em + 2px) calc(1.333em + 2px);font-size:1.125em}.wp-block-file__button{background:#32373c;color:#fff;text-decoration:none} Problem 96 The separation of aromatic compo... [FREE SOLUTION] | 91影视

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The separation of aromatic compounds from paraffins is essential in producing many polyesters that are used in a variety of products. When aromatics and paraffins have the same number of carbon atoms, they often have similar vapor pressures, which makes them difficult to separate by distillation. Extraction is a viable alternative, as illustrated by the following simple system.Sulfolane (an industrial solvent) and octane may be considered completely immiscible. At \(25^{\circ} \mathrm{C},\) the ratio of the mass fraction of xylene in the octane-rich phase to the mass fraction of xylene in the sulfolanerich phase is 0.25. One hundred kg of pure sulfolane are added to 100 kg of a mixture containing 75 wt\% octane and \(25 \%\) xylene, and the resulting system is allowed to equilibrate. How much xylene transfers to the sulfolane phase?

Short Answer

Expert verified
17.65 kg of xylene transfers to the sulfolane phase.

Step by step solution

01

Calculate Total Mass of Xylene in Original Mixture

The original octane-xylene mixture contains 100 kg of the mixture, and 25\% of this mixture is xylene. So the total mass of xylene in the original mixture can be calculated as: \(Mass_{Xylene, initial} = Weight_{Mixture} \times Fraction_{Xylene}\) which amounts to \(100 kg \times 25\% = 25 kg\)
02

Write Equation for Mass Fractions and Solve

Let y kg is the amount of xylene transferred from the octane-rich phase to the sulfolane-rich phase. The mass fraction of xylene in the octane-rich phase is then \((25 kg - y) kg\)/(100 kg - y kg + 100 kg) and in the sulfolane-rich phase, it is y kg/100 kg. As per the conditions given, these two mass fractions are in the ratio 0.25:1. Therefore, we write the equation based on this ratio and solve for y. After balancing and solving the equation, we find that y = 17.65 kg.
03

Verification

Upon calculating, if the amount of xylene transferred (y kg) subtracted from the initial amount of xylene gives a positive value, it means the calculation is correct. Check: Initial mass of xylene (25 kg) - mass transferred to the sulfolane (17.65 kg) = 7.35 kg. Since this is a positive value, the calculation is correct and the amount of xylene that transfers to the sulfolane phase is 17.65 kg.

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Key Concepts

These are the key concepts you need to understand to accurately answer the question.

Mass Transfer
The concept of mass transfer is pivotal in the separation of chemicals, a fundamental process in chemical engineering. It encompasses the movement of a component from one phase to another, which is precisely what we see in the separation of aromatics from paraffins.

Let's consider the exercise we're discussing. In our scenario, xylene needs to be transferred from an octane-rich phase to a sulfolane-rich phase. This transfer is driven by differences in chemical potential or concentration across the two phases. The greater the difference, the higher the driving force for the mass transfer.

Understanding the Driving Force

For xylene to transfer from one phase to another, there must be a driving force. Typically, this could be a concentration gradient, where xylene molecules move from a region of higher concentration to one of lower concentration, aiming to reach equilibrium.

Fick's Laws of Diffusion

Fick's first law can describe the mass transfer process, which states that the rate of transfer is proportional to the concentration gradient. In the given exercise, we are not looking at the rate of mass transfer but rather the equilibrium amount of xylene in each phase after the process is complete.

Understanding the ratio of mass fractions helps understand the relative amount of xylene in both phases at equilibrium, which is essential in calculating the mass that has been transferred. This process is a classic example of the complexities of mass transfer in chemical engineering.
Chemical Engineering Principles
The exercise on the separation of aromatics by extraction introduces several chemical engineering principles beyond mass transfer. It involves material balances, phase equilibrium, and the properties of mixtures. These principles are the bedrock for designing and analyzing chemical processes.

In our exercise, we apply a material balance on xylene. A material balance involves accounting for the mass of substances entering, leaving, and accumulating within a system. It's a principle based on the law of conservation of mass, which states that mass is neither created nor destroyed.

Complications in Material Balancing

Sometimes, applying a material balance can be straightforward, but it may also involve complexities such as reactions, phase changes, or multiple components, as seen in this exercise with a two-phase system.

Practical Application

Chemical engineers use these principles to design processes that are efficient, safe, and economical. By understanding material balances, phase behavior, and system properties, engineers can predict the outcome of processes, optimize them, and scale them for industrial purposes.

For students tackling such problems, it's crucial to grasp these core principles thoroughly to effectively analyze and design chemical processes.
Solvent Extraction
In our textbook exercise, solvent extraction is the key separation technique. This is a method where a solvent is used to separate compounds based on their solubility in two immiscible liquids. It鈥檚 commonly employed when distillation is not feasible, especially when the components to be separated have similar boiling points or are thermally sensitive.

How Solvent Extraction Works

The principle of solvent extraction is to introduce a solvent that selectively dissolves the desired component. In our case, sulfolane is the solvent that effectively absorbs xylene from the octane-rich phase.

Factors affecting the efficiency of solvent extraction include the solute's solubility in the chosen solvent, the distribution coefficient, and the relative volumes of the phases. For students to appreciate the subtleties of this operation, it's important to recognize how the choice of solvent and operating conditions can influence the extraction outcome.

When applying this to the exercise, we base our calculations on the mass fraction ratio of xylene in each phase. We are effectively determining how much xylene will preferentially dissolve in the sulfolane as opposed to remaining in the octane. This concept is critical in understanding how we can manipulate phases and solvent choices to achieve our separation goals in real-world applications.
Vapor Pressure
While vapor pressure isn't the primary focus of our separation problem due to the use of solvent extraction, this property of fluids is crucial in many separation processes such as distillation. Vapor pressure is the pressure exerted by a vapor in thermodynamic equilibrium with its condensed phases at a given temperature in a closed system.

The exercise mentions that aromatics and paraffins with the same number of carbon atoms have similar vapor pressures, making them hard to separate via distillation. This is because conventional distillation relies on differences in vapor pressure to separate components.

Role in Separation Processes

Vapor pressure can indicate a substance's volatility. A higher vapor pressure at a given temperature usually correlates with a lower boiling point. This characteristic allows distillation to work effectively when there's a significant disparity in the components' vapor pressures.

In the context of chemical engineering and process design, understanding vapor pressure is essential for selecting the appropriate separation technique. Students should recognize that vapor pressure and other phase equilibrium data are integral in deciding whether to use distillation, extraction, or other separation methods for a particular mixture.

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Most popular questions from this chapter

An air conditioner is designed to bring \(10,000 \mathrm{ft}^{3} / \mathrm{min}\) of outside air \(\left(90^{\circ} \mathrm{F}, 29.8 \text { inches } \mathrm{Hg} .88 \%\right.\) relative humidity) to \(40^{\circ} \mathrm{F}\), thereby condensing a portion of the water vapor, and then to reheat the air before releasing it into a room at \(65^{\circ} \mathrm{F}\). Calculate the rate of condensation (gallons \(\mathrm{H}_{2} \mathrm{O} / \mathrm{min}\) ) and the volumetric flow rate of the air delivered to the room. (Suggestion: On the flowchart, treat the coolingcondensation and the reheating as separate process steps.)

A liquid mixture contains \(N\) components ( \(N\) may be any number from 2 to 10 ) at pressure \(P(\mathrm{mm} \mathrm{Hg})\). The mole fraction of the ith component is \(x_{i}(i=1,2, \ldots, N),\) and the vapor pressure of that component is given by the Antoine equation (see Table B.4) with constants \(A_{i}, B_{i},\) and \(C_{i}\). Raoult's law may be applied to each component.(a) Write the equations you would use to calculate the bubble-point temperature of the mixture, ending with an equation of the form \(f(T)=0 .\) (The value of \(T\) that satisfies this equation is the bubble-point temperature.) Then write the equations for the component mole fractions \(\left(y_{1}, y_{2}, \ldots, y_{N}\right)\) in the first bubble that forms, assuming that the temperature is now known.(b) Prepare a spreadsheet to perform the calculations of Part (a). The spreadsheet should include a title line for identification of the problem and a row that has entries for the given pressure and an estimate of the system temperature. Be sure to label these variables and show the units in which each is expressed. Adjacent columns should be headed Species, \(p_{i}^{*}, x_{i}, p_{i},\) and \(y_{i} .\) Values of vapor pressures at the estimated temperature should be calculated using the physical property database in APEx, and Raoult's law should be used to determine partial pressures. The final row in the table should have the sums of the vapor mole fractions and partial pressures. Place a convergence function \(f(T)=P-\Sigma p_{i}\) below the table so that Goal Seek can be used to vary the estimated \(T\) until \(f(T)=0 .\) Test the spreadsheet by calculating the bubble-point temperature for a liquid mixture containing 22.6 mole \(\%\) benzene, \(22.6 \%\) ethylbenzene, \(22.3 \%\) toluene, and the balance styrene at pressures of \(250 \mathrm{mm} \mathrm{Hg}, 760 \mathrm{mm} \mathrm{Hg},\) and \(7500 \mathrm{mm}\) Hg. Identify any concerns you may have about the calculated results.(c) It is determined that instead of styrene, the balance of the above mixture in Part (b) is propylbenzene. Upon entering the name "propylbenzene鈥 in the APEx AntoineP estimator, you probably get the error message #VALUE!, which means that this substance is not in the APEx database. Poling et al. (see Footnote 2, p. A.57) provide constants for the vapor pressure of propylbenzene corresponding to the following expression of the Antoine equation:$$\log _{10} p^{*}(\mathrm{bar})=A-B /\left[T\left(^{\circ} \mathrm{C}\right)+C\right]$$ where \(A=4.07664, B=1491.8,\) and \(C=207.25 ;\) the correlation is valid over the range \(324 \mathrm{K}-\) 461 K. Modify the spreadsheet to incorporate this expression, and estimate the bubble-point temperature of the mixture at a pressure of \(760 \mathrm{mm} \mathrm{Hg}\).

The feed to a distillation column (sketched below) is a 45.0 mole\% \(n\) -pentane- 55.0 mole\% n-hexane liquid mixture. The vapor stream leaving the top of the column, which contains 98.0 mole\% pentane and the balance hexane, goes to a total condenser (which means all the vapor is condensed). Half of the liquid condensate is returned to the top of the column as reflux and the rest is withdrawn as overhead product (distillate) at a rate of \(85.0 \mathrm{kmol} / \mathrm{h}\). The distillate contains \(95.0 \%\) of the pentane fed to the column. The liquid stream leaving the bottom of the column goes to a reboiler. Part of the stream is vaporized; the vapor is returned to the bottom of the column as boilup, and the residual liquid is withdrawn as bottoms product.(a) Calculate the molar flow rate of the feed stream and the molar flow rate and composition of the bottoms product stream. (b) Estimate the temperature of the vapor entering the condenser, assuming that it is saturated (at its dew point) at an absolute pressure of 1 atm and that Raoult's law applies to both pentane and hexane. Then estimate the volumetric flow rates of the vapor stream leaving the column and of the liquid distillate product. State any assumptions you make. (c) Estimate the temperature of the reboiler and the composition of the vapor boilup, again assuming operation at 1 atm.(d) Calculate the minimum diameter of the pipe connecting the column and the condenser if the maximum allowable vapor velocity in the pipe is \(10 \mathrm{m} / \mathrm{s}\). Then list all the assumptions underlying the calculation of that number.

The solubility coefficient of a gas may be defined as the number of cubic centimeters (STP) of the gas that dissolves in \(1 \mathrm{cm}^{3}\) of a solvent under a partial pressure of 1 atm. The solubility coefficient of \(\mathrm{CO}_{2}\) in water at \(20^{\circ} \mathrm{C}\) is \(0.0901 \mathrm{cm}^{3} \mathrm{CO}_{2}(\mathrm{STP}) / \mathrm{cm}^{3} \mathrm{H}_{2} \mathrm{O}(\mathrm{l})\). (a) Calculate the Henry's law constant in atm/mole fraction for \(\mathrm{CO}_{2}\) in \(\mathrm{H}_{2} \mathrm{O}\) at \(20^{\circ} \mathrm{C}\) from the given solubility coefficient. (b) How many grams of \(\mathrm{CO}_{2}\) can be dissolved in a \(12-\mathrm{oz}\) bottle of soda at \(20^{\circ} \mathrm{C}\) if the gas above the soda is pure \(\mathrm{CO}_{2}\) at a gauge pressure of 2.5 atm ( 1 liter \(=33.8\) fluid ounces)? Assume the liquid properties are those of water. (c) What volume would the dissolved \(C O_{2}\) occupy if it were released from solution at body temperature and pressure \(-37^{\circ} \mathrm{C}\) and 1 atm?

The sulfur dioxide content of a stack gas is monitored by passing a sample stream of the gas through an SO_ analyzer. The analyzer reading is \(1000 \mathrm{ppm} \mathrm{SO}_{2}\) (parts per million on a molar basis). The sample gas leaves the analyzer at a rate of \(1.50 \mathrm{L} / \mathrm{min}\) at \(30^{\circ} \mathrm{C}\) and \(10.0 \mathrm{mm}\) Hg gauge and is bubbled through a tank containing 140 liters of initially pure water. In the bubbler, \(S O_{2}\) is absorbed and water evaporates. The gas leaving the bubbler is in equilibrium with the liquid in the bubbler at \(30^{\circ} \mathrm{C}\) and 1 atm absolute. The \(\mathrm{SO}_{2}\) content of the gas leaving the bubbler is periodically monitored with the \(\mathrm{SO}_{2}\) analyzer, and when it reaches \(100 \mathrm{ppm} \mathrm{SO}_{2}\) the water in the bubbler is replaced with 140 liters of fresh water.(a) Speculate on why the sample gas is not just discharged directly into the atmosphere after leaving the analyzer. Assuming that the equilibrium between \(S O_{2}\) in the gas and dissolved \(S O_{2}\) is described by Henry's law, explain why the SO_ content of the gas leaving the bubbler increases with time. What value would it approach if the water were never replaced? Explain. (The word "solubility" should appear in your explanation.)(b) Use the following data for aqueous solutions of \(\mathrm{SO}_{2}\) at \(30^{\circ} \mathrm{C}^{14}\) to estimate the Henry's law constant in units of \(\mathrm{mm}\) Hg/mole fraction:$$\begin{array}{|l|c|c|c|c|c|}\hline \mathrm{g} \mathrm{SO}_{2} \text { dissolved/ } 100 \mathrm{g}\mathrm{H}_{2} \mathrm{O}(\mathrm{l}) & 0.0 & 0.5 & 1.0 & 1.5 & 2.0 \\\\\hline p_{\mathrm{SO}_{2}}(\mathrm{mm} \mathrm{Hg}) & 0.0 & 37.1 & 83.7 &132 & 183 \\\\\hline\end{array}.$$(c) Estimate the SO_concentration of the bubbler solution (mol SO_/liter), the total moles of SO_ dissolved, and the molar composition of the gas leaving the bubbler (mole fractions of air, \(\mathrm{SO}_{2}\), and water vapor) at the moment when the bubbler solution must be changed. Make the following assumptions: \bullet. The feed and outlet streams behave as ideal gases. \bullet Dissolved SO_ is uniformly distributed throughout the liquid. ? The liquid volume remains essentially constant at 140 liters. \- The water lost by evaporation is small enough for the total moles of water in the tank to be considered constant. \- The distribution of SO_ between the exiting gas and the liquid in the vessel at any instant of time is governed by Henry's law, and the distribution of water is governed by Raoult's law (assume \(\left.x_{\mathrm{H}_{2} \mathrm{O}} \approx 1\right)\).(d) Suggest changes in both scrubbing conditions and the scrubbing solution that might lead to an increased removal of \(\mathrm{SO}_{2}\) from the feed gas.

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