/*! 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 64 Methane at \(25^{\circ} \mathrm{... [FREE SOLUTION] | 91Ó°ÊÓ

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Methane at \(25^{\circ} \mathrm{C}\) is burned in a boiler furnace with \(10.0 \%\) excess air preheated to \(100^{\circ} \mathrm{C}\). Ninety percent of the methane fed is consumed, the product gas contains \(10.0 \mathrm{mol} \mathrm{CO}_{2} / \mathrm{mol} \mathrm{CO},\) and the combustion products leave the furnace at \(400^{\circ} \mathrm{C}\). (a) Calculate the heat transferred from the furnace, \(-\dot{Q}(\mathrm{kW}),\) for a basis of \(100 \mathrm{mol} \mathrm{CH}_{4}\) fed/s. (The greater the value of \(-\dot{Q}\), the more steam is produced in the boiler.) (b) Would the following changes increase or decrease the rate of steam production? (Assume the fuel feed rate and fractional conversion of methane remain constant.) Briefly explain your answers. (i) Increasing the temperature of the inlet air; (ii) increasing the percent excess air for a given stack gas temperature; (iii) increasing the selcctivity of \(\mathrm{CO}_{2}\) to \(\mathrm{CO}\) formation in the furnace; and (iv) increasing the stack gas temperature.

Short Answer

Expert verified
The heat transferred from the furnace can be calculated based on the change in enthalpy during the combustion of methane. Increasing the temperature of the inlet air, increasing the percent excess air, and increasing the selectivity of CO2 to CO formation in the furnace will increase the rate of steam production, while increasing the stack gas temperature will decrease the rate of steam production.

Step by step solution

01

Establish the Combustion Reaction

First, the combustion reaction of methane (CH4) in excess oxygen is set up. As we know, the complete combustion of methane forms carbon dioxide (CO2) and water (H2O) as follows: \(CH4 + 2O2 -> CO2 + 2H2O\). In our problem, only 90% of methane is consumed, and the product gas contains 10 mol CO2 per mol CO. Thus, the actual combustion reaction in the furnace is: \(0.9 CH4 + 2*1.1 O2 -> 0.1 CO + 0.9 CO2 + 1.8 H2O\).
02

Calculate the Heat of the Reaction

Second, we employ the table of standard enthalpies of formation to calculate the heat of reaction. The heat of reaction (\(\Delta H\)) can be calculated using the equation: \(-\dot{Q} = -\Delta H * \dot{n}_{CH4}\), where \(\Delta H\) is the heat of reaction and \(\dot{n}_{CH4}\) is the mol/s flow of methane. The 'minus' sign indicates that the reaction is exothermic, i.e., heat is released during the combustion.
03

Analyze the Changes on Steam Production

(i) If the temperature of the inlet air is increased, the combustion would become more vigorous, leading to a higher \(\Delta H\), thus more heat transferred. So, steam production will increase. (ii) More excess air for a given stack gas temperature means more oxygen for combustion, hence more heat transferred and more steam produced. (iii) Increasing the selectivity of CO2 to CO in the furnace means more complete combustion, which will also result in more heat transferred and more steam produced. (iv) Increasing the stack gas temperature will reduce the furnace heat transfer (since heat transfer is proportional to the temperature difference between the furnace and the stack gas). Hence, steam production will decrease.

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Key Concepts

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

Enthalpy of Combustion
The enthalpy of combustion is a fundamental concept in understanding how chemical reactions release or absorb energy. It refers to the amount of heat released when a substance undergoes complete combustion with oxygen under standard conditions. For any hydrocarbon, like methane in our exercise, the reaction typically produces carbon dioxide and water, releasing heat in the process.

In the context of the exercise, the heat of combustion can be calculated from the reaction enthalpy, taking into account the stoichiometry and the percentages provided. For instance, since only 90% of methane reacts and there are 10.0% excess air, the calculation must include these variations. The enthalpy change, \( \Delta H \), is a crucial factor in determining the efficacy of combustion processes, such as those in boilers to produce steam.

Since heat release is an exothermic process, in our problem's terms, the larger the negative value of \( -\dot{Q} \) (heat transfer rate), the more energy is available for steam production. This, in turn, can be used to generate electricity or provide heating in industrial applications.
Excess Air in Combustion
Excess air in combustion plays a vital role in ensuring the complete burning of fuel, thus maximizing the efficiency of the combustion process. It is defined as the amount of air in excess of what is theoretically required for the complete oxidation of the fuel. This concept is especially significant in boilers where maintaining an ideal combustion environment is critical for energy efficiency and reducing emissions of uncombusted gases.

In the exercise, we are given that the combustion occurs with 10.0% excess air. While excess air is important to ensure complete combustion and thus maximizing the heat release, too much of it can lead to heat losses because the excess air needs to be heated as well. The balance between sufficient excess air for complete combustion and the energy loss due to heating the additional air is delicate and requires precise control.

As the solution indicates, increasing the excess air, given a constant stack gas temperature, increases the rate of steam production because it ensures more complete combustion. However, it's also crucial to optimize the amount of excess air to avoid unnecessary energy consumption in heating the extra air.
Steam Production in Boilers
Boilers are essential components in many industrial processes, serving to generate steam by applying heat energy to water. The efficiency of steam production in boilers is heavily dependent on the combustion process where fuel, such as methane, is burned to heat the water. The more effective the combustion, the more heat is available to convert water into steam, which can then be used for heating, powering turbines, or other industrial processes.

The enthalpy of combustion, as covered earlier, directly influences the \( -\dot{Q} \) value representing the heat transfer from the furnace. If \( -\dot{Q} \) is higher, more energy is transferred to the water in the boiler, resulting in higher steam production. The step-by-step solution provided outlines several factors that can increase or decrease the rate of steam production, such as the inlet air temperature and stack gas temperature. These factors affect the overall heat transfer efficiency within the boiler.
Chemical Reaction Stoichiometry
Chemical reaction stoichiometry refers to the quantitative relationship between reactants and products in a chemical reaction. It ensures that the conservation of mass is maintained by accounting for the molar ratios of the substances involved. Stoichiometry is the foundation for reaction calculations, balancing chemical equations, and determining the yield from reactions.

In our methane combustion example, the stoichiometry becomes complex as the reaction does not proceed to complete conversion—only 90% of methane reacts. Additionally, the presence of 10.0% excess air changes the proportions of reactants. Stoichiometry allows us to calculate the actual amounts of reactants and products based on these percentages, as showcased in the solution. For example, the formation of CO and CO2 in the reaction must align with the stoichiometric coefficients and the quantities provided, such as 10 mol CO2 per mol CO, to accurately determine the enthalpy of the reaction and therefore the heat transferred for steam production.

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Most popular questions from this chapter

A bituminous coal is burned with air in a boiler furnace. The coal is fed at a rate of \(40,000 \mathrm{kg} / \mathrm{h}\) and has an ultimate analysis of 76 wt\% \(\mathrm{C}, 5 \%\) H, \(8 \%\) O, negligible amounts of \(\mathrm{N}\) and \(\mathrm{S}\), and \(11 \%\) noncombustible ash (see Problem 9.58), and a higher heating value of 25,700 kJ/kg. Air enters a preheater at \(30^{\circ} \mathrm{C}\) and 1 atm with a relative humidity of \(30 \%,\) exchanges heat with the hot flue gas leaving the furnace, and enters the furnace at temperature \(T_{\mathrm{a}}\left(^{\circ} \mathrm{C}\right) .\) The flue gas contains 7.71 mole\% \(\mathrm{CO}_{2}\) and 1.29 mole \(\%\) CO on \(a\) dry basis, and the balance is a mixture of \(\mathrm{O}_{2}, \mathrm{N}_{2},\) and \(\mathrm{H}_{2} \mathrm{O}\). It emerges from the furnace at \(260^{\circ} \mathrm{C}\) and is cooled to \(150^{\circ} \mathrm{C}\) in the preheater. Noncombustible residue (slag) leaves the furnace at \(450^{\circ} \mathrm{C}\) and has a heat capacity of \(0.97 \mathrm{kJ} / \mathrm{kg} \cdot^{\cdot} \mathrm{C}\) ).. (a) Prove that the air-to-fuel ratio is 16.1 standard cubic meters/kg coal and that the flue gas contains \(4.6 \% \mathrm{H}_{2} \mathrm{O}\) by volume. (b) Calculate the rate of cooling required to cool the flue gas from \(260^{\circ} \mathrm{C}\) to \(150^{\circ} \mathrm{C}\) and the temperature to which the air is preheated. (Note: A trial-and-error calculation is required.) (c) If \(60 \%\) of the heat transferred from the furnace \((-Q)\) goes into producing saturated steam at 30 bar from liquid boiler feedwater at \(50^{\circ} \mathrm{C},\) at what rate \((\mathrm{kg} / \mathrm{h})\) is steam generated?

Ammonia scrubbing is one of many processes for removing sulfur dioxide from flue gases. The gases are bubbled through an aqueous solution of ammonium sulfite, and the SO_reacts to form ammonium bisulfite: $$\left(\mathrm{NH}_{4}\right)_{2} \mathrm{SO}_{3}(\mathrm{aq})+\mathrm{SO}_{2}(\mathrm{g})+\mathrm{H}_{2} \mathrm{O}(\mathrm{l}) \rightarrow 2 \mathrm{NH}_{4} \mathrm{HSO}_{3}(\mathrm{aq})$$ Subsequent process steps yield concentrated SO \(_{2}\) and regenerate ammonium sulfite, which is recycled to the scrubber. The sulfur dioxide is either oxidized and absorbed in water to form sulfuric acid or reduced to elemental sulfur. Flue gas from a power-plant boiler containing \(0.30 \% \mathrm{SO}_{2}\) by volume enters a scrubber at a rate of \(50,000 \mathrm{mol} / \mathrm{h}\) at \(50^{\circ} \mathrm{C} .\) The gas is bubbled through an aqueous solution containing \(10.0 \mathrm{mole} \%\) ammonium sulfite that enters the scrubber at \(25^{\circ} \mathrm{C}\). The gas and liquid effluents from the scrubber both emerge at \(35^{\circ} \mathrm{C}\). The scrubber removes \(90 \%\) of the \(S O_{2}\) entering with the flue gas. The effluent liquid is analyzed and is found to contain 1.5 moles \(\left(\mathrm{NH}_{4}\right)_{2} \mathrm{SO}_{3}\) per mole of \(\mathrm{NH}_{4} \mathrm{HSO}_{3}\). The heat of formation of \(\left(\mathrm{NH}_{4}\right)_{2} \mathrm{SO}_{3}(\mathrm{aq})\) at \(25^{\circ} \mathrm{C}\) is \(-890.0 \mathrm{kJ} / \mathrm{mol},\) and that of \(\mathrm{NH}_{4} \mathrm{HSO}_{3}(\mathrm{aq})\) is \(-760 \mathrm{kJ} / \mathrm{mol} .\) The heat capacities of all liquid solutions may be taken to be \(4.0 \mathrm{J} /\left(\mathrm{g} \cdot^{\circ} \mathrm{C}\right)\) and that of the flue gas may be taken to be that of nitrogen. Evaporation of water may be neglected. Calculate the required rate of heat transfer to or from the scrubber ( \(\mathrm{kW}\) ).

The equilibrium constant for the ethane dehydrogenation reaction, $$\mathrm{C}_{2} \mathrm{H}_{6}(\mathrm{g}) \rightleftharpoons \mathrm{C}_{2} \mathrm{H}_{4}(\mathrm{g})+\mathrm{H}_{2}(\mathrm{g})$$ is defined as $$K_{p}(\mathrm{atm})=\frac{y_{\mathrm{C}_{2} \mathrm{H}_{4}} y_{\mathrm{H}_{2}}}{y_{\mathrm{C}_{2} \mathrm{H}_{6}}} P$$ where \(P(\text { atm })\) is the total pressure and \(y_{i}\) is the mole fraction of the ith substance in an equilibrium mixture. The equilibrium constant has been found experimentally to vary with temperature according to the formula $$K_{p}(T)=7.28 \times 10^{6} \exp [-17,000 / T(\mathrm{K})]$$ The heat of reaction at \(1273 \mathrm{K}\) is \(+145.6 \mathrm{kJ}\), and the heat capacities of the reactive species may be approximated by the formulas $$\left.\begin{array}{rl}\left(C_{p}\right)_{\mathrm{C}_{2} \mathrm{H}_{4}} & =9.419+0.1147 T(\mathrm{K}) \\\\\left(C_{p}\right)_{\mathrm{H}_{2}} & =26.90+4.167 \times 10^{-3} T(\mathrm{K}) \\ \left(C_{p}\right)_{\mathrm{C}_{2} \mathrm{H}_{6}} & =11.35+0.1392 T(\mathrm{K}) \end{array}\right\\}[\mathrm{J} /(\mathrm{mol} \cdot \mathrm{K})]$$ Suppose pure cthane is fed to a continuous constant-pressure adiabatic reactor at \(1273 \mathrm{K}\) and pressure \(P(\text { atm }),\) the products emerge at \(T_{\mathrm{f}}(\mathrm{K})\) and \(P(\mathrm{atm}),\) and the residence time of the reaction mixture in the reactor is large enough for the outlet stream to be considered an equilibrium mixture of ethane, ethylene, and hydrogen. (a) Prove that the fractional conversion of ethane in the reactor is $$f=\left(\frac{K_{p}}{P+K_{p}}\right)^{1 / 2}$$ (b) Write an energy balance on the reactor, and use it to prove that $$f=\frac{1}{1+\phi\left(T_{\mathrm{f}}\right)}$$ where Finally, substitute for \(\Delta H_{\mathrm{r}}\) and the heat capacities in Equation 4 to derive an explicit expression for \(\phi\left(T_{\mathrm{f}}\right)\) (c) We now have two expressions for the fractional conversion \(f\) : Equation 2 and Equation 3 . If these expressions are equated, \(K_{p}\) is replaced by the expression of Equation \(1,\) and \(\phi\left(T_{\mathrm{f}}\right)\) is replaced by the expression derived in Part (b), the result is one equation in one unknown, \(T_{\mathrm{f}}\). Derive this equation, and transpose the right side to obtain an expression of the form $$\psi\left(T_{\mathrm{f}}\right)=0$$ (d) Prepare a spreadsheet to take \(P\) as input, solve Equation 5 for \(T_{\mathrm{f}}\) (use Goal Seek or Solver), and determine the final fractional conversion, \(\left.f \text { . (Suggestion: Set up columns for } P, T_{\mathrm{f}}, f, K_{p}, \phi, \text { and } \psi .\right)\) Run the program for \(P(\text { atm })=0.01,0.05,0.10,0.50,1.0,5.0,\) and \(10.0 .\) Plot \(T_{\mathrm{f}}\) versus \(P\) and \(f\) versus \(P,\) using a logarithmic coordinate scale for \(P\).

Methane is burned completely with 40\% excess air. The methane enters the combustion chamber at \(25^{\circ} \mathrm{C},\) the combustion air enters at \(150^{\circ} \mathrm{C},\) and the stack gas \(\left[\mathrm{CO}_{2}, \mathrm{H}_{2} \mathrm{O}(\mathrm{v}), \mathrm{O}_{2}, \mathrm{N}_{2}\right]\) exits at \(450^{\circ} \mathrm{C} .\) The chamber functions as a preheater for an air stream flowing in a pipe through the chamber to a spray dryer. The air enters the chamber at \(25^{\circ} \mathrm{C}\) at a rate of \(1.57 \times 10^{4} \mathrm{m}^{3}(\mathrm{STP}) / \mathrm{h}\) and is heated to \(181^{\circ} \mathrm{C}\). All of the heat generated by combustion is used to heat the combustion products and the air going to the spray dryer (i.e., the combustion chamber may be considered adiabatic). (a) Draw and completely label the process flow diagram and perform a degree- of-freedom analysis. (b) Calculate the required molar flow rates of methane and combustion air (kmol/h) and the volumetric flow rates \(\left(\mathrm{m}^{3} / \mathrm{h}\right)\) of the two effluent streams. State all assumptions you make. (c) When the system goes on line for the first time, environmental monitoring of the stack gas reveals a considerable quantity of CO, suggesting a problem with either the design or the operation of the combustion chamber. What changes from your calculated values would you expect to see in the temperatures and volumetric flow rates of the effluent streams [increase, decrease, cannot tell without doing the calculations]?

Coke can be converted into \(\mathrm{CO}-\mathrm{a}\) fuel gas- -in the reaction $$\mathrm{CO}_{2}(\mathrm{g})+\mathrm{C}(\mathrm{s}) \rightarrow 2 \mathrm{CO}(\mathrm{g})$$ A coke that contains \(84 \%\) carbon by mass and the balance noncombustible ash is fed to a reactor with a stoichiometric amount of \(\mathrm{CO}_{2}\). The coke is fed at \(77^{\circ} \mathrm{F}\), and the \(\mathrm{CO}_{2}\) enters at \(400^{\circ} \mathrm{F}\). Heat is transferred to the reactor in the amount of \(5859 \mathrm{Btu} / \mathrm{lb}_{\mathrm{m}}\) coke fed. The gascous products and the solid reactor effluent (the ash and unburned carbon) leave the reactor at \(1830^{\circ} \mathrm{F}\). The heat capacity of the solid is \(0.24 \mathrm{Btu} /\left(\mathrm{lb}_{\mathrm{m}} \cdot^{\circ} \mathrm{F}\right)\) (a) Calculate the percentage conversion of the carbon in the coke. (b) The carbon monoxide produced in this manner can be used as a fuel for residential home heating, as can the coke. Speculate on the advantages and disadvantages of using the gas. (There are several of each.)

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