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Molten sodium chloride is to be used as a constant-temperature bath for a high-temperature chemical reactor. Two hundred kilograms of solid \(\mathrm{NaCl}\) at \(300 \mathrm{K}\) is charged into an insulated vessel, and a 3000 kW electrical heater is turned on, raising the salt to its melting point of 1073 K and melting it at a constant pressure of 1 atm. (a) The heat capacity \(\left(C_{p}\right)\) of solid \(\mathrm{NaCl}\) is \(50.41 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})\) at \(T=300 \mathrm{K},\) and \(53.94 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})\) at \(T=500 \mathrm{K},\) and the heat of fusion of \(\mathrm{NaCl}\) at \(1073 \mathrm{K}\) is \(30.21 \mathrm{kJ} / \mathrm{mol} .\) Use these data to determine a linear expression for \(C_{p}(T)\) and to calculate \(\Delta \hat{H}\) ( \(\mathrm{kJ} / \mathrm{mol}\) ) for the transition of \(\mathrm{NaCl}\) from a solid at 300 K to a liquid at \(1073 \mathrm{K}\). (b) Write and solve the energy balance equation for this closed system isobaric process to determine the required heat input in kilojoules. (c) If \(85 \%\) of the full power of \(3000 \mathrm{kW}\) goes into heating and melting the salt, how long does the process take?

Short Answer

Expert verified
The linear expression for heat capacity, \(C_{p}(T)\), is \(0.01765T + 44.605 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})\). The total heat change, \(\Delta \hat{H}\), for the transition from solid NaCl at 300K to liquid at 1073K is 83.15 kJ/mol. The required heat input for the process is 285000 kJ, and it takes around 112 hours to complete the process.

Step by step solution

01

Developing the linear expression \(C_{p}(T)\)

Given \(C_{p}\) values at 300K and 500K, the equation of a line can be used to find the linear expression for \(C_{p}(T)\). The formula is \(y = mx + b\), where \(m\) (slope) is \(\Delta y/\Delta x\) and \(b\) (intercept) is \(y - mx\). Here, \(y\) represents \(C_{p}\), \(x\) represents \(T\), and \(m\) is \((53.94 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K}) - 50.41 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K}))/(500 \mathrm{K} - 300 \mathrm{K}) = 0.01765 \mathrm{J} / (\mathrm{mol} \cdot \mathrm{K}^{2})\). The y-intercept \(b\) can be derived with \(y - mx\) using the \(C_{p}\) and \(T\) values at 300K: \(C_{p} - mT = b => 50.41 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K}) - (0.01765 \mathrm{J} / (\mathrm{mol} \cdot \mathrm{K}^{2})) \cdot 300 \mathrm{K} = 44.605 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})\). Therefore, the equation of \(C_{p}(T)\) is \(0.01765T + 44.605 \mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})\).
02

Calculating the enthalpy change \(\Delta \hat{H}\)

Using the developed equation from step 1, \(\Delta \hat{H}\) can be calculated in two parts: the heat gained to increase the temperature (\(\Delta H_{1}\)) and the heat given at the phase change (\(\Delta H_{2}\)). \(\Delta H_{1} = \int_{300}^{1073} C_{p}(T) dT = \int_{300}^{1073} (0.01765T + 44.605) dT\) which can be evaluated as \(\Delta H_{1} = 52.94 \mathrm{kJ/mol}\). \(\Delta H_{2}\) is given as the heat of fusion at 1073K, which is 30.21 kJ/mol. \(\Delta \hat{H}\) is the sum of \(\Delta H_{1}\) and \(\Delta H_{2}\), which is 83.15 kJ/mol.
03

Determining the heat input

Based on the energy balance equation \(Q = \Delta U + W\), and accounting for the process being at constant pressure (isobaric) and in a closed system (no work done), the heat input required (\(Q\)) is equal to \(\Delta H\) (enthalpy change). Given 200kg of NaCl, we can find the molar quantity by dividing by the molar mass of NaCl (58.44 g/mol). Then, multiply it with \(\Delta \hat{H}\) (molar enthalpy change) to get \(Q\), which is \(285000 \mathrm{kJ}\).
04

Computing process time

The time required for the heating process can be calculated by using the formula \(time = Energy/Power\). Knowing that 85% of the full power is used for the process, the actual power used is 0.85 x 3000kW = 2550kW. Therefore, the time required will be \(285000 \mathrm{kJ} /2550 \mathrm{kW} = 112 \mathrm{hours}\).

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Key Concepts

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

Heat Capacity
In thermodynamics, heat capacity is a crucial concept that describes the amount of heat energy required to raise the temperature of a substance by a specific amount. It is often represented as \(C_p\) when measurements are taken at constant pressure. The heat capacity is given in units of \(\text{J/(mol}\cdot\text{K)}\), demonstrating the energy needed to heat one mole of a substance by one Kelvin.

Key factors to remember about heat capacity include:
  • It varies with temperature; hence, it's important to obtain values at different temperatures, as demonstrated with NaCl at 300 K and 500 K.
  • In this exercise, the linear relationship of \(C_p(T)\) was established using the provided data, allowing us to predict \(C_p\) across temperatures.
The linear expression related to heat capacity for NaCl was derived using the formula \(y = mx + b\), where the slope \(m\) captured the change of heat capacity with temperature. Understanding this provides insight into the energy needed for heating processes in practical applications.
Enthalpy Change
Enthalpy change, denoted as \(\Delta \hat{H}\), represents the total heat content change of a system under constant pressure. It's a vital concept to comprehend the energy transactions during chemical processes, particularly those involving phase transitions.

In our scenario of molten sodium chloride:
  • Enthalpy change was evaluated in two stages: heating the solid to its melting point and then allowing it to transition into a liquid phase.
  • The calculation combined the integrated heat capacity function over the temperature range and added the heat of fusion at 1073 K.
  • Mathematically, this involved evaluating \(\int_{300}^{1073} C_p(T)\, dT\) and adding the latent heat of fusion, quantified here as \(\Delta H_2 = 30.21 \, \text{kJ/mol}\).
Gaining an understanding of enthalpy change enhances one's ability to predict how much heat energy a process will need, which is crucial for designing and operating thermal systems.
Energy Balance Equation
In order to thoroughly analyze a thermodynamic system, one must employ the energy balance equation. For an isobaric process like the melting of sodium chloride, the energy equation simplifies as the work done is zero (since the system is closed and pressure is constant).

The equation used was \(Q = \Delta U + W\), where \(Q\) is the heat added to the system, \(\Delta U\) is the change in internal energy, and \(W\) is work done. For this type of process, since work done \(W = 0\), the heat input \(Q\) is directly equal to the enthalpy change \(\Delta H\).

Steps involved include:
  • Calculating the total mole quantity using NaCl's molar mass, essential for determining the entire heat input with \(\Delta \hat{H}\).
  • Identifying that the heat input \(Q\) needed for the process is \(285,000 \, \text{kJ}\).
  • Converting the energy needs into time, considering actual power usage (85% efficiency of the heater), to obtain process duration.
Through mastering the energy balance, engineers and chemists can precisely determine the necessary power supply and duration for thermal operation, an essential step in planning large-scale thermal systems.

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Most popular questions from this chapter

An adiabatic membrane separation unit is used to dry (remove water vapor from) a gas mixture containing 10.0 mole \(\% \mathrm{H}_{2} \mathrm{O}(\mathrm{v}), 10.0\) mole \(\% \mathrm{CO},\) and the balance \(\mathrm{CO}_{2} .\) The gas enters the unit at \(30^{\circ} \mathrm{C}\) and flows past a semipermeable membrane. Water vapor permeates through the membrane into an air stream. The dried gas leaves the separator at \(30^{\circ} \mathrm{C}\) containing \(2.0 \mathrm{mole} \% \mathrm{H}_{2} \mathrm{O}(\mathrm{v})\) and the balance \(\mathrm{CO}\) and \(\mathrm{CO}_{2}\). Air enters the separator at \(50^{\circ} \mathrm{C}\) with an absolute humidity of \(0.002 \mathrm{kg} \mathrm{H}_{2} \mathrm{O} / \mathrm{kg}\) dry air and leaves at \(48^{\circ} \mathrm{C}\). Negligible quantities of \(\mathrm{CO}, \mathrm{CO}_{2}, \mathrm{O}_{2},\) and \(\mathrm{N}_{2}\) permeate through the membrane. All gas streams are at approximately 1 atm. (a) Draw and label a flowchart of the process and carry out a degree of freedom analysis to verify that you can determine all unknown quantities on the chart. (b) Calculate (i) the ratio of entering air to entering gas (kg humid air/mol gas) and (ii) the relative humidity of the exiting air. (c) List several desirable properties of the membrane. (Think about more than just what it allows and does not allow to permeate.)

A gas stream containing \(n\) -hexane in nitrogen with a relative saturation of \(90 \%\) is fed to a condenser at \(75^{\circ} \mathrm{C}\) and 3.0 atm absolute. The product gas emerges at \(0^{\circ} \mathrm{C}\) and 3.0 atm at a rate of \(746.7 \mathrm{m}^{3} / \mathrm{h}\). (a) Calculate the percentage condensation of hexane (moles condensed/mole fed) and the rate \((\mathrm{kW})\) at which heat must be transferred from the condenser. (b) Suppose the feed stream flow rate and composition and the heat transfer from the condenser are the same as in Part (a), but the condenser and outlet stream pressure is only 2.5 atm instead of 3.0 atm. How would the outlet stream temperatures and flow rates and the percentage condensations of hexane calculated in Parts (a) and (b) change (increase, decrease, no change, no way to tell)? Don't do any calculations, but explain your reasoning.

A sheet of cellulose acetate film containing 5.00 wt\% liquid acetone enters an adiabatic dryer where \(90 \%\) of the acetone evaporates into a stream of dry air flowing over the film. The film enters the dryer at \(T_{\mathrm{f} 1}=35^{\circ} \mathrm{C}\) and leaves at \(T_{\mathrm{f} 2}\left(^{\circ} \mathrm{C}\right) .\) The air enters the dryer at \(T_{\mathrm{al}}\left(^{\circ} \mathrm{C}\right)\) and 1.01 atm and exits the dryer at \(T_{\mathrm{a} 2}=49^{\circ} \mathrm{C}\) and 1 atm with a relative saturation of \(40 \% . C_{p}\) may be taken to be \(1.33 \mathrm{kJ} /\left(\mathrm{kg} \cdot^{\circ} \mathrm{C}\right)\) for dry film and \(0.129 \mathrm{kJ} /\left(\mathrm{mol} \cdot^{\circ} \mathrm{C}\right)\) for liquid acetone. Make a reasonable assumption regarding the heat capacity of dry air. The heat of vaporization of acetone may be considered independent of temperature. Take a basis of \(100 \mathrm{kg}\) film fed to the dryer for the requested calculations. (a) Estimate the feed ratio [liters dry air (STP)/kg dry film]. (b) Derive an expression for \(T_{\mathrm{al}}\) in terms of the film temperature change, \(\left(T_{\mathrm{f} 2}-35\right),\) and use it to answer Parts (c) and (d). (c) Calculate the film temperature change if the inlet air temperature is \(120^{\circ} \mathrm{C}\). (d) Calculate the required value of \(T_{\mathrm{al}}\) if the film temperature falls to \(34^{\circ} \mathrm{C},\) and the value if it rises to \(36^{\circ} \mathrm{C}.\) (e) If you solved Parts (c) and (d) correctly, you found that even though the air temperature is consistently higher than the film temperature in the dryer, so that heat is always transferred from the air to the film, the film temperature can drop from the inlet to the outlet. How is this possible?

An aqueous slurry at \(30^{\circ} \mathrm{C}\) containing \(20.0 \mathrm{wt} \%\) solids is fed to an evaporator in which enough water is vaporized at 1 atm to produce a product slurry containing 35.0 wt\% solids. Heat is supplied to the evaporator by feeding saturated steam at 2.6 bar absolute into a coil immersed in the liquid. The steam condenses in the coil, and the slurry boils at the normal boiling point of pure water. The heat capacity of the solids may be taken to be half that of liquid water. (a) Calculate the required steam feed rate ( \(\mathrm{kg} / \mathrm{h}\) ) for a slurry feed rate of \(1.00 \times 10^{3} \mathrm{kg} / \mathrm{h}\). (b) Vapor recompression is often used in the operation of an evaporator. Suppose that the vapor (steam) generated in the evaporator described above is compressed to 2.6 bar and simultaneously heated to the saturation temperature at 2.6 bar, so that no condensation occurs. The compressed steam and additional saturated steam at 2.6 bar are then fed to the evaporator coil, in which isobaric condensation occurs. How much additional steam is required? (c) What more would you need to know to determine whether or not vapor recompression is economically advantageous in this process?

Estimate the specific enthalpy of steam (kJ/kg) at \(100^{\circ} \mathrm{C}\) and 1 atm relative to steam at \(350^{\circ} \mathrm{C}\) and 100 bar using: (a) The steam tables. (b) Table B.2 or APEx and assuming ideal-gas behavior. What is the physical significance of the difference between the values of \(\hat{H}\) calculated by the two methods?

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