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If the percentage of fuel in a fuel-air mixture falls below a certain value called the lower flammability limit (LFL), which sometimes is referred to as the lower explosion limit (LEL), the mixture cannot be ignited. In addition there is an upper flammability limit (UFL), which also is known as the upper explosion limit (UEL). For example, the LFL of propane in air is 2.3 mole \(\% \mathrm{C}_{3} \mathrm{H}_{8}\) and the UFL is \(9.5 \%^{14}\). If the percentage of propane in a propane-air mixture is greater than \(2.3 \%\) and less than \(9.5 \%,\) the gas mixture can ignite if it is exposed to a flame or spark. A mixture of propane in air containing 4.03 mole \(\% \mathrm{C}_{3} \mathrm{H}_{8}\) (fuel gas) is the feed to a combustion furnace. If there is a problem in the furnace, a stream of pure air (dilution air) is added to the fuel mixture prior to the furnace inlet to make sure that ignition is not possible. (a) Draw and label a flowchart of the fuel gas-dilution air mixing unit, presuming that the gas entering the furnace contains propane at the LFL, and do the degree-of-freedom analysis. (b) If propane flows at a rate of \(150 \mathrm{mol} \mathrm{C}_{3} \mathrm{H}_{8} / \mathrm{s}\) in the original fuel-air mixture, what is the minimum molar flow rate of the dilution air? (c) How would the actual dilution air feed rate probably compare with the value calculated in Part (b)? (>, \(<,=\) ) Explain.

Short Answer

Expert verified
The minimum molar flow rate of the dilution air could be calculated using the given LFL and propane flowrate. The actual dilution air feed rate would likely be greater than this calculated value to include a safety margin and account for non-ideal conditions.

Step by step solution

01

Drawing flowchart and Degree-of-Freedom Analysis

The flowchart would show the inflow of propane and air, possibly merging together into a stream entering the furnace. A separate inlet stream of pure air, labeled 'dilution air', should also be directed to this merge point. Lastly, a single outflow from the furnace should be shown. A degree of freedom analysis reveals there are three specifications: the inflow rates of fuel gas and air, and the composition of fuel gas. The number of unknowns are most likely the same. Hence, the degree of freedom is zero and the system should be solvable.
02

Calculating Minimum Molar Flow Rate of Dilution Air

The LFL for propane is given as 2.3 mole%. To ensure the inflow mixture does not exceed this limit, the molar flow rate for dilution air can be calculated using the formula: \( \text{Dilution air flowrate} = \frac{\text{Propane flowrate}}{LFL} - \text{Propane flowrate} \). Substituting given values, calculate the minimum dilution air flowrate.
03

Comparative Analysis of Actual and Calculated Dilution Air Feed Rate

The actual dilution air feed rate to the furnace would likely be greater than the minimum calculated in part (b). This is because, in practice, a safety margin is usually added to ensure the propane concentration does not exceed the LFL even under non-ideal conditions. Other factors affecting this could include variations in the feed rates, measurement errors, or fluctuations in the propane composition. Verification through experimental methods would provide the most accurate comparison.

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Key Concepts

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

Flammability Limits
When dealing with fuel-air mixtures, understanding flammability limits is crucial for safe operation. Essentially, these limits dictate whether a mixture can ignite. The Lower Flammability Limit (LFL) is the minimum concentration of fuel required for combustion to occur, while the Upper Flammability Limit (UFL) is the maximum concentration before the mixture becomes too rich to ignite. For propane, the LFL is at 2.3% and the UFL is at 9.5%. This means, for a propane-air mixture to ignite, the propane concentration must be between these two values.

If the concentration of propane is below the LFL, the mixture lacks sufficient fuel to sustain combustion. Conversely, if it exceeds the UFL, there is not enough oxygen for the fuel to burn. Safety protocols often involve diluting mixtures outside these limits to ensure that accidental ignition does not occur.
Degree-of-Freedom Analysis
Degree-of-freedom analysis is a pivotal tool in process engineering, helping to determine whether a system of equations can be solved with the provided data. In the case of the propane-air system, conducting this analysis involves counting the knowns and unknowns. The knowns typically include the inflow rates of the main components and their concentrations.

For this particular problem, three specifications are involved: the rates of inflow for fuel gas and air, as well as the composition of the fuel gas. Zero degrees of freedom indicates that the system is perfectly specified — neither under- nor over-constrained. This balance ensures that with the existing information, we can solve for the necessary parameters such as the dilution air flow rate required to maintain safety.
Dilution Air Calculation
In improving combustion safety, calculating the necessary dilution air is vital. This process involves reducing the fuel-air mixture to a point where ignition is impossible. The formula used is:\[ \text{Dilution air flowrate} = \frac{\text{Propane flowrate}}{\text{LFL}} - \text{Propane flowrate} \]By substituting the known propane flow rate and the LFL into this equation, you can find the minimum amount of dilution air needed. This ensures the mixture's propane concentration is below the LFL, rendering it non-flammable.

In practice, more dilution air than this minimum is often added to account for measurement errors and fluctuations, thereby maintaining a margin of safety. Engineers calculate this excess air to encompass all possible operational uncertainties.
Combustion Furnace Safety
Safety in combustion processes is paramount, especially in industrial settings. A combustion furnace relies on controlled reactions to function safely, and controlling the fuel-air ratio is a critical part. By keeping propane concentrations within non-flammable limits using dilution air, the risk of accidental ignition is minimized.

Beyond setting precise air flow rates, the key to safety also involves account for unexpected variations in fuel composition or flow. This often means implementing systems for monitoring and adjusting air flows automatically in real time. Regular maintenance and equipment checks further ensure the furnace operates under safe conditions.

Such measures prevent situations where the mixture might accidentally enter the flammable range, avoiding potential hazards. Understanding and controlling these factors are part of a broader approach to creating a safer working environment in facilities using combustion furnaces.

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Most popular questions from this chapter

A liquid mixture containing 30.0 mole \(\%\) benzene \((\mathrm{B}), 25.0 \%\) toluene \((\mathrm{T}),\) and the balance xylene \((\mathrm{X})\) is fed to a distillation column. The bottoms product contains 98.0 mole \(\% \mathrm{X}\) and no \(\mathrm{B},\) and \(96.0 \%\) of the \(\mathrm{X}\) in the feed is recovered in this stream. The overhead product is fed to a second column. The overhead product from the second column contains \(97.0 \%\) of the \(\mathrm{B}\) in the feed to this column. The composition of this stream is 94.0 mole\% B and the balance T. (a) Draw and label a flowchart of this process and do the degree-of-freedom analysis to prove that for an assumed basis of calculation, molar flow rates and compositions of all process streams can be calculated from the given information. Write in order the equations you would solve to calculate unknown process variables. In each equation (or pair of simultaneous equations), circle the variable(s) for which you would solve. Do not do the calculations. (b) Calculate (i) the percentage of the benzene in the process feed (i.e., the feed to the first column) that emerges in the overhead product from the second column and (ii) the percentage of toluene in the process feed that emerges in the bottom product from the second column.

Ethylene oxide is produced by the catalytic oxidation of ethylene: $$ 2 \mathrm{C}_{2} \mathrm{H}_{4}+\mathrm{O}_{2} \longrightarrow 2 \mathrm{C}_{2} \mathrm{H}_{4} \mathrm{O} $$ An undesired competing reaction is the combustion of ethylene: $$ \mathrm{C}_{2} \mathrm{H}_{4}+3 \mathrm{O}_{2} \longrightarrow 2 \mathrm{CO}_{2}+2 \mathrm{H}_{2} \mathrm{O} $$ The feed to the reactor (not the fresh feed to the process) contains 3 moles of ethylene per mole of oxygen. The single-pass conversion of ethylene is \(20 \%,\) and for every 100 moles of ethylene consumed in the reactor, 90 moles of ethylene oxide emerge in the reactor products. A multiple-unit process is used to separate the products: ethylene and oxygen are recycled to the reactor, ethylene oxide is sold as a product, and carbon dioxide and water are discarded. (a) Assume a quantity of the reactor feed stream as a basis of calculation, draw and label the flowchart, perform a degree-of-freedom analysis, and write the equations you would use to calculate (i) the molar flow rates of ethylene and oxygen in the fresh feed, (ii) the production rate of ethylene oxide, and (iii) the overall conversion of ethylene. Do no calculations. (b) Calculate the quantities specified in Part (a), either manually or with an equation-solving program. (c) Calculate the molar flow rates of ethylene and oxygen in the fresh feed needed to produce 1 ton per hour of ethylene oxide.

A mixture of 75 mole \(\%\) methane and 25 mole \(\%\) hydrogen is burned with \(25 \%\) excess air. Fractional conversions of \(90 \%\) of the methane and \(85 \%\) of the hydrogen are achieved; of the methane that reacts, \(95 \%\) reacts to form \(\mathrm{CO}_{2}\) and the balance reacts to form CO. The hot combustion product gas passes through a boiler in which heat transferred from the gas converts boiler feedwater into steam. (a) Calculate the concentration of \(\mathrm{CO}\) (ppm) in the stack gas. (b) The CO in the stack gas is a pollutant. Its concentration can be decreased by increasing the percent excess air fed to the furnace. Think of at least two costs of doing so. (Hint: The heat released by the combustion goes into heating the combustion products; the higher the combustion product temperature, the more steam is produced.)

The reaction between ethylene and hydrogen bromide to form ethyl bromide is carried out in a continuous reactor. The product stream is analyzed and found to contain 51.7 mole \(\% \mathrm{C}_{2} \mathrm{H}_{5} \mathrm{Br}\) and 17.3\% HBr. The feed to the reactor contains only ethylene and hydrogen bromide. Calculate the fractional conversion of the limiting reactant and the percentage by which the other reactant is in excess. If the molar flow rate of the feed stream is \(165 \mathrm{mol} / \mathrm{s}\), what is the extent of reaction?

One thousand kilograms per hour of a mixture containing equal parts by mass of methanol and water is distilled. Product streams leave the top and the bottom of the distillation column. The flow rate of the bottom stream is measured and found to be \(673 \mathrm{kg} / \mathrm{h}\), and the overhead stream is analyzed and found to contain 96.0 wt\% methanol. (a) Draw and label a flowchart of the process and do the degree-of-freedom analysis. (b) Calculate the mass and mole fractions of methanol and the molar flow rates of methanol and water in the bottom product stream. (c) Suppose the bottom product stream is analyzed and the mole fraction of methanol is found to be significantly higher than the value calculated in Part (b). List as many possible reasons for the discrepancy as you can think of. Include in your list possible violations of assumptions made in Part (b).

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