Acetobacter aceti bacteria convert ethanol to acetic acid under aerobic conditions. A continuous fermentation process for vinegar production is proposed using nongrowing A cetobacter aceti immobilized in calcium alginate gel beads.
In this process, ethanol is supplied to the beads from the bottom of a fluidized bed bioreactor, while air is supplied from the top. The average residence time of the beads in the bioreactor was estimated to be 20 days. An equation for the overall rate of acetic acid production based on the bioconversion of ethanol to acetic acid by Acetobacter aceti was developed and used to predict the performance of the bioreactor.
A comparison of the theoretical results with experimental results shows good agreement. The model developed was also used to predict the optimum performance of the bioreactor, given certain initial and operating conditions. The model provides a useful tool for optimizing the performance of the bioreactor under various operating conditions.
The results of the study indicate that the proposed continuous fermentation process has the potential to produce high yields of acetic acid while minimizing the cost of production. Total number of words used to describe the process and its implications is 150.
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(c) An electrolysis cell containing MSO4 solution is operated for 1.0 h at a constant current of 0.200 A. If the current efficiency is 95%, and 0.399 g of M plates out, what is the atomic weight and the name of the element M?
[CO2, PO3, C3]
(d) Suppose an old wooden boat, held together with iron screws, has a bronze propeller (bronze is an alloy consisting mainly of copper with a small amount of tin).
i) If the boat is immersed in seawater, what corrosion reaction will occur? What is an E° cell?
ii) Suggest possible approach to reduce and prevent this corrosion from occurring.
(c) In an electrolysis cell, with a given current and current efficiency, a certain amount of metal plates out. By calculating the atomic weight of the plated metal, it can be identified as element M.
(d) When an old wooden boat with iron screws and a bronze propeller is immersed in seawater, a corrosion reaction occurs. The E° cell represents the standard cell potential of the corrosion reaction.
(c) The amount of metal plated out in an electrolysis cell can be used to determine the atomic weight and identify the element. Given the current efficiency of 95% and the plated metal mass of 0.399 g, the total amount of metal that should have plated out can be calculated. By dividing the total plated metal mass by the number of moles, the molar mass or atomic weight can be determined. The element M can be identified based on the calculated atomic weight.
(d) When the old wooden boat with iron screws and a bronze propeller is immersed in seawater, corrosion reactions occur due to the presence of different metals. In this case, a galvanic corrosion reaction takes place, where the bronze propeller acts as the cathode and the iron screws act as the anode. The standard cell potential for this corrosion reaction, known as E° cell, can be calculated based on the half-cell potentials of the metals involved. This potential indicates the driving force for the corrosion reaction.
To reduce and prevent this corrosion, several approaches can be considered. One possible approach is to use sacrificial anodes made of a more active metal, such as zinc or aluminum. These anodes will corrode sacrificially instead of the iron screws, protecting them from corrosion. Another approach is to apply protective coatings, such as paints or sealants, to the iron screws and exposed areas. These coatings act as a barrier, preventing contact between the metal and the corrosive seawater. Additionally, implementing cathodic protection systems, such as impressed current cathodic protection or galvanic cathodic protection, can help to protect the iron screws by providing an external source of electrons to counteract the corrosion process. These approaches aim to minimize the electrochemical reactions and preserve the integrity of the boat's structure.
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For each metal/alloy below, discuss the feasibility of hot working or cold working based on melting temperature, corrosion resistance, elastic limit, and degree of fragility:
1. tin
2. Tungsten
3. Al
Tin is feasible for both hot and cold working, Tungsten is challenging to hot work and Aluminum is suitable for both hot and cold working.
Tin:
Feasibility of hot working: Tin has a relatively low melting temperature of 231.93°C. This makes it feasible for hot working processes such as hot rolling or hot extrusion, where the material is heated above its recrystallization temperature for shaping. Tin is easily deformable at elevated temperatures.
Feasibility of cold working: Tin can also be cold worked, but it has limited ductility and tends to exhibit strain hardening behavior. Cold working processes like cold rolling or cold drawing can be used, but excessive deformation may lead to cracking or brittleness due to the low ductility of tin.
Tungsten:
Feasibility of hot working: Tungsten has a high melting temperature of 3,422°C, which makes it challenging to perform hot working. The extreme temperatures required for hot working tungsten are not practical for most industrial processes. Tungsten is primarily processed using powder metallurgy techniques rather than hot working.
Feasibility of cold working: Tungsten has excellent room temperature ductility and can be cold worked effectively. It can be rolled, drawn, or extruded at room temperature to form desired shapes. Tungsten's high elastic limit and low degree of fragility make it suitable for cold working applications.
Aluminum:
Feasibility of hot working: Aluminum has a relatively low melting temperature of 660.32°C, which makes it easily amenable to hot working processes. Hot working methods like hot rolling, hot extrusion, or hot forging can be used to shape aluminum at elevated temperatures. Aluminum exhibits good ductility and can be readily deformed during hot working.
Feasibility of cold working: Aluminum can also be cold worked with relative ease. It has good room temperature ductility and can be cold rolled, cold extruded, or cold drawn. The elastic limit of aluminum is relatively low, but it has good corrosion resistance and a low degree of fragility, making it suitable for cold working applications.
Tin is feasible for both hot and cold working, but its limited ductility and low melting temperature should be considered when determining the extent of deformation.
Tungsten is challenging to hot work due to its extremely high melting temperature, but it is highly suitable for cold working processes.
Aluminum is suitable for both hot and cold working, with hot working taking advantage of its low melting temperature and cold working utilizing its good ductility and corrosion resistance.
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what is the oxidation numbers for CaCl3
Answer:
IMPOSSIBLE
Explanation:
Oxidation can only occur in CaCL2 because of Alfred Wegner's law of conservative elliptical nation.
A reversible gas phase reaction, A+B=C is carried out in a tubular reactor (ID = 100 cm) packed with catalyst particles (spherical, D₂ = 0.005 m). Pure reactants at their stoichiometric amount are fed to the reactor at 100 atm and 400 °C and the reaction is carried out isothermally. The feed enters the reactor at vo-5 m³/h. The specific rate of reaction, k and the reaction equilibrium constant, K at reaction temperature are 0.0085 m² kmol-¹ kgcat¹ s¹ and 4.5 m³mol¹ respectively. a) Based on the following data plot the pressure ratio (y), rate of reaction and conversion as a function of weight of catalyst in the reactor. (µ- 3.21x10 kg/m.s; po-1.4 kg/m³; -0.4; P-1500 kg/m³) b) Estimate the maximum production rate of C (kmol/s) in the reactor. c) Analyse the effect of catalyst particle size on the conversion (D, from 0.0025 -0.0075 m). d) A chemical engineer suggests decreasing the diameter of the reactor by two times while other parameters remain the same (Dp-5 mm; bed and fluid properties are assumed same as in (a). Evaluate the proposal in terms of achieved conversion. e) A chemical engineer suggested to use a membrane reactor to increase the productivity of the reactor. Sketch the reactor and write the differential mole balance equations for A, B and C.
a) The rate of reaction can be calculated using the rate equation and the given specific rate of reaction (k) and equilibrium constant (K).
a) To plot the pressure ratio (y), rate of reaction, and conversion as a function of the weight of catalyst, we need to consider the ideal gas law, the rate equation, and the equilibrium constant:
Ideal Gas Law:
PV = nRT
Rate Equation:
Rate = k * (PA * PB - PC / K)
Equilibrium Constant:
K = (PC / (PA * PB))
Pressure ratio (y) can be calculated using the ideal gas law and the given data:
y = PC / PA
The rate of reaction can be calculated using the rate equation and the given specific rate of reaction (k) and equilibrium constant (K).
Conversion can be calculated using the equilibrium constant and the pressure ratio:
Conversion = (1 - (1 / K)) / (1 + (y / K))
b) The maximum production rate of C (kmol/s) in the reactor can be estimated by considering the limiting reactant. In this case, the limiting reactant is the reactant with the lowest stoichiometric coefficient. Let's assume it is A, and its stoichiometric coefficient is a.
Maximum production rate of C = Rate * a
c) The effect of catalyst particle size (D) on conversion can be analyzed by considering different particle sizes. The conversion can be calculated using the equilibrium constant and pressure ratio for each particle size.
d) To evaluate the proposal of decreasing the reactor diameter by two times while keeping other parameters the same, the conversion needs to be calculated using the new reactor diameter (Dp = 5 mm) and compared with the previous conversion.
e) In a membrane reactor, a membrane is used to separate the reactants from the products. The reactor can be sketched as a tube with the membrane placed inside. The differential mole balance equations for A, B, and C can be written as:
dNA/dt = R₁ - R₂
dNB/dt = R₁ - R₂
dNC/dt = R₂
Where R₁ represents the rate of reaction and R₂ represents the rate of diffusion through the membrane.
By performing the necessary calculations and analyses, the pressure ratio, rate of reaction, and conversion as a function of the weight of catalyst can be plotted.
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6. Which of the following is an example of a first order system O(i). Viscous damper O (ii). U tube manometer 1 point (iii). Mercury thermometer without well O (iv). mercury thermometer with well
An example of a first order system is a viscous damper.
Viscous Damper is an example of a first order system. A first order system is a type of linear system that has one integrator. The system's input-output relationship is defined by a first-order differential equation or a first-order difference equation.
A viscous damper consists of a piston that moves through a fluid, creating resistance to motion. Its input is a velocity that results in an output force. Therefore, it is an example of a first-order system.
A viscous damper is a hydraulic system that uses a fluid to provide resistance to motion. In vehicles, it is used to prevent suspension components from bouncing excessively. It works by using a piston that moves through oil. When the piston moves quickly, it creates resistance to motion due to the viscosity of the oil. This helps to smooth out the motion of the vehicle's suspension.
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During a spectrophotometric titration, a 10.00 mL sample was titrated with 0.50 mL of titrant and gave absorbance of 0.3219. The corrected absorbance will be Selected Answer: A=0.3380 Answers: A=0.306
The corrected absorbance will be A=0.306. The corrected absorbance takes into account the volume of the titrant added during the spectrophotometric titration.
To find the corrected absorbance, we need to account for the volume of the titrant added during the titration. The corrected absorbance is calculated using the following formula:
Corrected Absorbance = Absorbance * (Sample Volume / Total Volume)
Absorbance = 0.3219
Sample Volume = 10.00 mL
Titrant Volume = 0.50 mL
Total Volume = Sample Volume + Titrant Volume
Total Volume = 10.00 mL + 0.50 mL
= 10.50 mL
Substituting the values into the formula:
Corrected Absorbance = 0.3219 * (10.00 mL / 10.50 mL)
Corrected Absorbance ≈ 0.306
Therefore, the corrected absorbance will be A=0.306.
The corrected absorbance takes into account the volume of the titrant added during the spectrophotometric titration. By multiplying the initial absorbance by the ratio of the sample volume to the total volume, we obtain the corrected absorbance value. In this case, the corrected absorbance is found to be A=0.306.
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Two hundred grams (200 g) of pure methane is burned with 90 %
excess air and 33 % of its carbon content is converted to CO and
the rest to CO2. About 70 % of its hydrogen burns to water, the
rest rema
a) The mole composition of the wet stack gas is approximately as follows:
CH4: 12.47 mol
O2: 24.94 mol
CO: 4.11 mol
CO2: 8.36 mol
H2O: 34.92 mol
N2: 29.85 mol
b) The volume of air supplied per gram of methane is approximately 1.39665 L/g.
a) The mole composition of the wet stack gas:
To calculate the mole composition of the wet stack gas, we need to determine the moles of each component based on the given information.
Mass of methane (CH4) = 200 g
Excess air = 90% (meaning 10% of stoichiometric air is supplied)
Determine the moles of methane (CH4):
Molar mass of CH4 = 12.01 g/mol (C) + 4(1.01 g/mol) (H)
= 16.05 g/mol
Moles of CH4 can be determined by dividing the Mass of CH4 by Molar mass of CH4.
Moles of CH4 = 200 g / 16.05 g/mol
≈ 12.47 mol
Determine the moles of oxygen (O2) supplied:
For complete combustion of CH4, the stoichiometric ratio of CH4 to O2 is 1:2.
Moles of O2 can be determined by multiplying Moles of CH4 with 2.
Moles of O2 = 2 * 12.47 mol
= 24.94 mol
Determine the moles of carbon monoxide (CO):
33% of the carbon content of CH4 is converted to CO.
Moles of CO = 0.33 * Moles of CH4
Moles of CO = 0.33 * 12.47 mol
≈ 4.11 mol
Determine the moles of carbon dioxide (CO2):
Moles of CO2 = Moles of CH4 - Moles of CO
Moles of CO2 = 12.47 mol - 4.11 mol
≈ 8.36 mol
Determine the moles of water (H2O):
70% of the hydrogen content of CH4 is converted to H2O.
Moles of H2O = 0.70 * (4 * Moles of CH4)
Moles of H2O = 0.70 * (4 * 12.47 mol)
≈ 34.92 mol
Determine the moles of unburned hydrogen (H2):
Moles of unburned H2 = 4 * Moles of CH4 - Moles of H2O
Moles of unburned H2 = 4 * 12.47 mol - 34.92 mol
≈ 12.38 mol
Determine the moles of nitrogen (N2) in the wet stack gas:
Since excess air is supplied, we can assume that the nitrogen content in the wet stack gas is the same as in the air.
Moles of N2 in the wet stack gas = Moles of nitrogen in the supplied air
To determine the moles of nitrogen in the supplied air, we need to consider the temperature, pressure, and relative humidity (RH) of the air.
Temperature (T) = 26°C
= 26 + 273.15 K
= 299.15 K
Pressure (P) = 761 mm Hg
Relative Humidity (RH) = 90%
The mole fraction of water vapor (H2O) in the air can be determined using the vapor pressure of water at the given temperature and the RH.
Vapor Pressure of Water at 26°C ≈ 25.21 mm Hg
Mole fraction of H2O = (RH / 100) * (Vapor Pressure of Water / Total Pressure)
Mole fraction of H2O = (90 / 100) * (25.21 / 761)
Mole fraction of H2O ≈ 0.0297
Mole fraction of N2 = 1 - Mole fraction of H2O
Mole fraction of N2 ≈ 1 - 0.0297
≈ 0.9703
Now, we can calculate the moles of nitrogen in the supplied air:
Moles of nitrogen in the supplied air = Mole fraction of N2 * Total Moles of Air
Assuming ideal gas behavior, the mole fraction of N2 is the same as the mole fraction of nitrogen in the air.
Moles of nitrogen in the supplied air ≈ Mole fraction of N2 * (Total Pressure / R * Temperature)
(0.0821 L atm/(mol K)) is the ideal gas constant R.
Moles of nitrogen in the supplied air ≈ 0.9703 * (761 mm Hg / (0.0821 L·atm/(mol·K) * 299.15 K)
Moles of nitrogen in the supplied air ≈ 29.85 mol
Therefore, the mole composition of the wet stack gas is approximately as follows:
CH4: 12.47 mol
O2: 24.94 mol
CO: 4.11 mol
CO2: 8.36 mol
H2O: 34.92 mol
N2: 29.85 mol
b) The volume of air supplied per gram of methane:
To calculate the volume of air supplied per gram of methane, we need to consider the molar volumes of methane and air.
Molar volume of methane (CH4) = 22.4 L/mol
Molar volume of air (considering 21% O2 and 79% N2) = 22.4 L/mol
Moles of CH4 = 12.47 mol (calculated in part a)
Volume of air supplied = Moles of CH4 * Molar volume of air
Volume of air supplied = 12.47 mol * 22.4 L/mol
Volume of air supplied ≈ 279.33 L
Mass of methane = 200 g
Volume of air supplied per gram of methane = Volume of air supplied / Mass of methane
Volume of air supplied per gram of methane = 279.33 L / 200 g
Volume of air supplied per gram of methane ≈ 1.39665 L/g
Therefore, the volume of air supplied per gram of methane is approximately 1.39665 L/g.
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Two hundred grams (200 g) of pure methane is burned with 90 % excess air and 33 % of its carbon content is converted to CO and the rest to CO2. About 70 % of its hydrogen burns to water, the rest remains as unburned H2. Air supplied is at 26ºC, 761 mm Hg with 90% RH, Calculate:
a.) % mole composition of the wet stack gas
b.) m3 of air supplied per g methane
You are asked to evaluate the possibility of using the distillation column you used in the continuous distillation experiment to separate water from ethanol. The feed enters the column as saturated liquid with concentration of 50% mol methanol. The concentration of methanol in the bottom must be 5% mol maximum and in the distillate it must be 90% mol minimum. Is the current column is capable of separating this mixture. Determine the minimum reflux ratio. Over all column efficiency. If the current column is not good to give the required separation; what you recommend? The following data will help you in your calculations The feed flow rate is 5 L/min. Reflux ratio is 3 times of the minimum reflux. The distillation was atmospheric The equilibrium data can be found in the literature. In addition to the above make justified assumptions when it is needed. Useful references: W. L. McCabe, J.C. Smith and P. Harriot, "Unit Operations of Chemical Engineering" 7th Ed., McGraw- Hill, New York (2005). R. H. Perry and D. W. Green, "Perry's Chemical Engineers' Handbook", 8th ed., McGraw-Hill, USA (2008) R. E. Treybal, "Mass-Transfer Operations", 3rd Ed., McGraw-Hill, New York (1981)
Based on the given conditions and requirements, it is not possible to achieve the desired separation of water and ethanol using the current distillation column.
To determine the minimum reflux ratio and overall column efficiency, detailed calculations and analysis are required. This involves considering the equilibrium data, operating conditions, and column design parameters. Unfortunately, without access to specific equilibrium data and column design details, it is not possible to provide precise values for the minimum reflux ratio and overall column efficiency in this context.
If the current column is not suitable for the separation, several recommendations can be considered. One option is to modify the existing column by adjusting its internals, such as the number of trays or the packing material, to improve separation efficiency. Another option is to explore alternative separation techniques, such as extractive distillation or azeotropic distillation, which may offer better performance for the specific water-ethanol separation. These alternatives can involve additional equipment or specialized processes to achieve the desired separation more effectively. The choice of the most appropriate solution depends on factors such as cost, energy requirements, and the specific needs of the separation process.
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Propose the synthesis of the below compounds from the given substrates and the necessary inorganic and/or organic reagents. a) benzonitrile (phenylcarbonitrile) from benzene (you can use other organic reagents) . b) butanone from ethyl acetylacetate (ethyl 3-oxobutanoate) and other necessary organic reagents . c) N-benzyl-pentylamine (without impurities of secondary and tertiary amines) from benzyl alcohol (phenyl- methanol) and pentan-1-ol . d) 1,3,5-tribromobenzene from nitrobenzene (5 pts). e) 3-ethyl-oct-3-ene from two carbonyl compounds (aldehydes and/or ketones) containing 5 carbon atoms in the molecule (at one of the steps use the Wittig reaction) ). f) 2-ethyl-hex-2-enal from but-1-ene
To synthesize benzonitrile from benzene, one possible route is the Sandmeyer reaction.
Benzene can be converted to benzonitrile using sodium cyanide (NaCN) and a copper(I) catalyst, such as copper(I) chloride (CuCl). The reaction proceeds as follows: Benzene + NaCN + CuCl → Benzonitril. b) To synthesize butanone from ethyl acetylacetate, one possible method is to perform a hydrolysis reaction. Ethyl acetylacetate can be hydrolyzed using an acid or base catalyst to yield butanone. The reaction can be represented as: Ethyl acetylacetate + H2O + Acid/Base catalyst → Butanone. c) To synthesize N-benzyl-pentylamine without impurities of secondary and tertiary amines, a reductive amination reaction can be employed. Benzyl alcohol can react with pentan-1-ol using an amine catalyst, such as Raney nickel, and hydrogen gas to yield N-benzyl-pentylamine. Benzyl alcohol + Pentan-1-ol + Amine catalyst + H2 → N-benzyl-pentylamine. d) To synthesize 1,3,5-tribromobenzene from nitrobenzene, a bromination reaction can be performed. Nitrobenzene can be treated with bromine (Br2) in the presence of a Lewis acid catalyst, such as iron(III) bromide (FeBr3), to yield 1,3,5-tribromobenzene. Nitrobenzene + Br2 + Lewis acid catalyst → 1,3,5-tribromobenzene.
e) To synthesize 3-ethyl-oct-3-ene, a possible route is to use the Wittig reaction. Two carbonyl compounds containing 5 carbon atoms in the molecule, such as an aldehyde and a ketone, can react with a phosphonium ylide, such as methyltriphenylphosphonium bromide, to yield the desired product. Aldehyde + Ketone + Phosphonium ylide → 3-ethyl-oct-3-ene. f) To synthesize 2-ethyl-hex-2-enal from but-1-ene, an oxidation reaction can be performed. But-1-ene can be oxidized using an oxidizing agent, such as potassium permanganate (KMnO4), in the presence of a catalyst, such as acidic conditions, to yield 2-ethyl-hex-2-enal. But-1-ene + Oxidizing agent + Catalyst → 2-ethyl-hex-2-enal. Please note that these are general approaches, and specific reaction conditions and reagents may vary. It is always important to consult reliable references and conduct further research for detailed procedures and precautions before carrying out any chemical synthesis.
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What is the molality of p-dichlorobenzene (C6H4Cl₂, 147 g/mol) when 2.65 g is dissolved in 50.0 mL of benzene (C6H6, 78.11 g/mol, p = 0.879 g/mL)? Select one: O a. 2.44 m O b. 1.22 m O c. 0.410 m O
The molality of p-dichlorobenzene in the solution is approximately 0.410 m. The correct option is c. 0.410 m.
To calculate the molality (m) of p-dichlorobenzene in the given solution, we need to determine the moles of p-dichlorobenzene and the mass of the solvent (benzene). Molality is defined as moles of solute per kilogram of solvent.
First, let's calculate the moles of p-dichlorobenzene:
Moles of p-dichlorobenzene = mass / molar mass
Moles of p-dichlorobenzene = 2.65 g / 147 g/mol
Moles of p-dichlorobenzene ≈ 0.01803 mol
Next, we need to calculate the mass of benzene:
Mass of benzene = volume x density
Mass of benzene = 50.0 mL x 0.879 g/mL
Mass of benzene ≈ 43.95 g
Now, let's calculate the molality:
Molality = moles of solute / mass of solvent (in kg)
Molality = 0.01803 mol / (43.95 g / 1000 g/kg)
Molality ≈ 0.410 m
Therefore, the molality of p-dichlorobenzene in the solution is approximately 0.410 m. The correct option is c. 0.410 m.
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a. State the difference between reversible and irreversible reaction b. Y CS Tha PFR 6.00 1280 Pure A is fed at a volumetric flow rate of 10 ft³/h and a concentration of 5x10³ lbmol/ft to a CSTR that is connected in series to a PFR. If the volumes of the CSTR and PFR were 1200 ft' and 600 ft respectively as shown below, calculate the intermediate and final conversions (XAI and XA2) that can be achieved with existing system. Reaction kinetics is shown in the graph below. Don't can be achieved CSTR V=Y² CSxu' PfR. df-V dv CSTR=ff -Yj PFR=F₁-X dv
a. The main difference between reversible and irreversible reactions lies in the ability to reverse the reaction and restore the initial reactants.
b. To calculate the intermediate and final conversions (XAI and XA2) achievable with the existing system, we would need additional information such as the reaction kinetics or rate expression.
a. Difference between reversible and irreversible reaction:
The main difference between reversible and irreversible reactions lies in the ability to reverse the reaction and restore the initial reactants.
Reversible reaction: In a reversible reaction, the reaction can proceed in both the forward and reverse directions. This means that the products can react to form the original reactants under suitable conditions. Reversible reactions occur when the system is not at equilibrium and can shift towards the reactants or products depending on the prevailing conditions (e.g., temperature, pressure, concentration). The reaction can reach a dynamic equilibrium state where the rates of the forward and reverse reactions are equal, and the concentrations of reactants and products remain constant over time.
Irreversible reaction: In contrast, an irreversible reaction proceeds only in the forward direction, and it is not possible to regenerate the original reactants once the reaction has occurred. The reactants are converted into products, and this conversion is typically favored under specific conditions, such as high temperatures or the presence of a catalyst. Irreversible reactions are often used to achieve desired chemical transformations and are commonly encountered in many industrial processes.
b. In the given system, a CSTR (continuous stirred-tank reactor) is connected in series with a PFR (plug-flow reactor). The volumes of the CSTR and PFR are provided as 1200 ft³ and 600 ft³, respectively. The feed to the system is pure A with a volumetric flow rate of 10 ft³/h and a concentration of 5x10³ lbmol/ft.
To calculate the intermediate and final conversions (XAI and XA2) achievable with the existing system, we would need additional information such as the reaction kinetics or rate expression. Unfortunately, the provided equation and symbols in the question do not give a clear representation of the reaction kinetics or rate expression. Without the necessary information, it is not possible to calculate the conversions accurately.
To determine the conversions, we would typically need the rate equation or kinetic expression for the reaction and the residence time or reaction time in each reactor (CSTR and PFR). With these details, we could solve the appropriate mass balance equations to calculate the intermediate and final conversions.
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A fuel gas containing 86% methane, 8% ethane, and 6% propane by volume flows to a furnace at a rate of 1450 m3/h at 15°C and 150 kPa (gauge), where it is burned with 8% excess air. a) Calculate the required flow rate of air in SCMH (standard cubic meters per hour). b) If the fuel is completely consumed, find the volumetric flowrate of product stream in SCMH. c) Find the partial pressure of each component of the product stream if it is at the 1 atm absolute.
To calculate the required flow rate of air, we need to consider the stoichiometry of the combustion reaction. For every 1 mole of methane (CH4), we need 2 moles of oxygen (O2) from air.
The volumetric flow rate of methane can be calculated as: Flow rate of methane = (86/100) * 1450 m3/h = 1247 m3/h. Therefore, the required flow rate of air in SCMH can be calculated as: Flow rate of air = (2 * 1247) / 0.21 = 11832 SCMH. Here, 0.21 is the mole fraction of oxygen in air. b) Since the fuel is completely consumed, the volumetric flow rate of the product stream will be equal to the volumetric flow rate of the fuel gas. Therefore, the volumetric flow rate of the product stream in SCMH is also 1450 SCMH.
c) To find the partial pressure of each component in the product stream, we can assume ideal gas behavior. The total pressure is given as 1 atm. Partial pressure of methane = (86/100) * 1 atm = 0.86 atm; Partial pressure of ethane = (8/100) * 1 atm = 0.08 atm; Partial pressure of propane = (6/100) * 1 atm = 0.06 atm. Note: The partial pressures of the components are calculated based on their respective mole fractions in the product stream.
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3.1. Mention the types of corrosion. (9) 3.2. If a metal (at room temperature) with an area of 30 cm² is penetrated at 5 mm/year and losses 900 mg of its weight, calculate the exposure time in days. The density of the metal is 8.96 g/cm³. 3.3. In the case of galvanic coupling the metal that needs to be protected is coupled with a metal that is more anodic than itself. This implies that the anodic metal gets corroded in order to protect the cathodic one. Show how this is done using a diagram.
The types of corrosion include uniform corrosion, galvanic corrosion, crevice corrosion, pitting corrosion, intergranular corrosion, stress corrosion cracking, etc.
The exposure time can be calculated by determining the length of penetration and dividing it by the penetration rate.
Galvanic coupling involves connecting a more anodic metal with a more cathodic metal, causing the anodic metal to corrode and protect the cathodic metal.
Types of corrosion:
Uniform corrosion: Occurs evenly over the entire surface of a metal.
When two distinct metals come into touch with each other when an electrolyte is present, galvanic corrosion occurs.
Crevice corrosion: Occurs in localized areas such as gaps, crevices, or tight spaces where the electrolyte becomes stagnant.
Pitting corrosion: Characterized by small pits or holes on the metal surface.
Corrosion that occurs between metal grains is referred to as intergranular corrosion.
Stress corrosion cracking: Occurs due to the combined effects of tensile stress and corrosive environment.
Erosion corrosion: Caused by the combined action of corrosion and mechanical erosion.
Fretting corrosion: Occurs at the interface of two surfaces experiencing slight relative motion and repeated contact.
Corrosion that is influenced by microorganisms on the metal surface is known as microbiologically influenced corrosion (MIC).
3.2. Calculating exposure time:
Area of metal = 30 cm²
Penetration rate = 5 mm/year
Weight loss = 900 mg
Density of metal = 8.96 g/cm³
First, convert the weight loss from milligrams to grams:
Weight loss = 900 mg * (1 g / 1000 mg)
= 0.9 g
Next, calculate the volume loss of the metal:
Volume loss = Weight loss / Density of metal
= 0.9 g / 8.96 g/cm³
Since density = mass / volume, we can rearrange the equation to solve for volume:
Volume = mass / density
Volume loss = Volume
= 0.9 g / 8.96 g/cm³
= 0.1004464 cm³
Now, calculate the length of penetration:
Length of penetration = Volume loss / Area of metal
= 0.1004464 cm³ / 30 cm²
Since the penetration rate is given in mm/year, we need to convert the length of penetration to millimeters:
Length of penetration = (Length of penetration) * 10 mm/cm
Finally, calculate the exposure time in years:
Exposure time = Length of penetration / Penetration rate = (Length of penetration) / (5 mm/year)
Converting the exposure time to days:
Exposure time (days) = Exposure time (years) * 365 days/year
3.3. Diagram of galvanic coupling:
In galvanic coupling, a more anodic metal (higher on the galvanic series) is coupled with a more cathodic metal (lower on the galvanic series). The anodic metal undergoes corrosion to protect the cathodic metal. Here's a simplified diagram illustrating this concept:
Cathodic Metal (More Cathodic) --> Galvanic Connection --> Anodic Metal (More Anodic)
^
|
Electrolyte
The galvanic connection allows the flow of electrons between the two metals, with the anodic metal serving as the sacrificial metal that corrodes to protect the cathodic metal.
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By doing which of the following will you decrease the number of collisions and energy of reactant molecules?
increasing the pressure of the reactant mixture
decreasing the concentration of reactants
adding a catalyst
decreasing the temperature of the reactant mixture
There are certain factors we can manipulate to change the rate of a reaction:
Temperature is a measure of average kinetic energy. An increase in temperature leads to a faster rate.Concentration. The more reactant molecules available to react, the greater the rate.Pressure. An increased pressure leads to a decreased volume, leading to more collisions and an increased rate.Adding a catalyst increases the rate by providing an alternate pathway for the reaction where the Ea is lowered.That being said, to decrease the number of collisions, we must decrease the temperature.
We apply a voltage of 220 V to Fcc an copper wire of 20 m long. number of charge carries (n.) - 22 5 -1 8.466-10 electrons/cm. electrical conductivity and o-5.89 x10 19 cm calculate the average جد �
The average drift velocity of the charge carriers in the copper wire is approximately 1.793 m/s.
To calculate the average drift velocity of the charge carriers in the copper wire, we need to use the formula:
J = σ * E
where:
J is the current density (A/m²),
σ is the electrical conductivity (S/m), and
E is the electric field strength (V/m).
Given information:
Voltage (V) = 220 V
Length of the wire (L) = 20 m
Number of charge carriers (n) = 2.25 × 10^18 electrons/cm³ = 2.25 × 10^24 electrons/m³
Electrical conductivity (σ) = 5.89 × 10^19 S/cm = 5.89 × 10^25 S/m
First, let's calculate the electric field strength:
E = V / L
= 220 V / 20 m
= 11 V/m
Next, we can calculate the current density:
J = σ * E
= (5.89 × 10^25 S/m) * (11 V/m)
= 6.479 × 10^26 A/m²
The current density is related to the charge carrier density (n) and the average drift velocity (v) by the formula:
J = n * q * v
where q is the charge of an electron (1.602 × 10^(-19) C).
Rearranging the formula, we can solve for the average drift velocity:
v = J / (n * q)
= (6.479 × 10^26 A/m²) / (2.25 × 10^24 electrons/m³ * 1.602 × 10^(-19) C)
= 1.793 m/s
Therefore, the average drift velocity of the charge carriers in the copper wire is approximately 1.793 m/s.
The average drift velocity of the charge carriers in the copper wire, under the given conditions, is approximately 1.793 m/s.
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Question 44 of 76 The activation energy Ea for a particular reaction is 50.0 kJ/mol. How much faster is the reaction at 319 K than at 310.0 K? (R = 8.314 J/mol •K)
The reaction at 319K is 1.080 times faster than the Reaction at 310K.
To determine how much faster the reaction is at 319 K compared to 310.0 K, we can use the Arrhenius equation:
k = A * exp(-Ea / (R * T))
where:
k is the rate constant
A is the pre-exponential factor or frequency factor
Ea is the activation energy
R is the ideal gas constant (8.314 J/mol·K)
T is the temperature in Kelvin
Let's calculate the rate constant (k) at both temperatures and compare the ratio.
For T1 = 310.0 K:
k1 = A * exp(-Ea / (R * T1))
For T2 = 319 K:
k2 = A * exp(-Ea / (R * T2))
To determine how much faster the reaction is, we need to calculate the ratio of the rate constants:
k2 / k1 = (A * exp(-Ea / (R * T2))) / (A * exp(-Ea / (R * T1)))
Simplifying the expression:
k2 / k1 = exp((-Ea / (R * T2)) + (Ea / (R * T1)))
k2 / k1 = exp(Ea / R * (1 / T1 - 1 / T2))
Now we can substitute the values:
T1 = 310.0 K
T2 = 319 K
Ea = 50.0 kJ/mol = 50.0 * 10^3 J/mol
R = 8.314 J/mol·K
k2 / k1 = exp(50.0 * 10^3 J/mol / (8.314 J/mol·K) * (1 / 310.0 K - 1 / 319 K))
k1/k2 = exp(6.021 - 5.944)
k1/k2 ≈ exp(0.077)
Using the exponential function, we can evaluate the expression:
k1/k2 ≈ 1.080
Therefore, the reaction is approximately 1.080 times faster at 319 K compared to 310.0 K.
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Problem 4. a. Hydrogen sulfide (H₂S) is a toxic byproduct of municipal wastewater treatment plant. H₂S has a TLV-TWA of 10 ppm. Please convert the TLV-TWA to lbm/s. Molecular weight of H₂S is 34 lbm/lb-mole. If the local ventilation rate is 2000 ft³/min. Assume 80 F is the 0.7302 ft³-atm/lb-mole-R. (5) temperature and 1 atm pressure. Ideal gas constant, Rg Conversion of Rankine, R = 460 + F. Assume, k = 0.1 b. Let's assume that local wastewater treatment plant stores H₂S in a tank at 100 psig and 80 F. If the local ventilation rate is 2000 ft³/min. Please calculate the diameter of a hole in the tank that could lead a local H₂S concentration equals TLV-TWA. Choked flow is applicable and assume y= 1.32 and Co = 1. Ideal gas constant, Rg = 1545 ft-lb/lb-mole-R, x psig = (x+14.7) psia = (x+14.7) lb/in² (10) =
a) the TLV-TWA of H₂S is equivalent to 22.322 lbm/s. b) diameter ≈ 2 * sqrt(A / π)
a. To convert the TLV-TWA (Threshold Limit Value-Time Weighted Average) of hydrogen sulfide (H₂S) from ppm (parts per million) to lbm/s (pounds-mass per second), we need to use the given information and perform the necessary calculations.
1 ppm of H₂S means that for every million parts of air, there is 1 part of H₂S by volume. We can convert this volume concentration to mass concentration using the molecular weight of H₂S.
Given:
TLV-TWA of H₂S = 10 ppm
Molecular weight of H₂S = 34 lbm/lb-mole
Local ventilation rate = 2000 ft³/min
To convert the TLV-TWA to lbm/s, we need to know the density of air at the given conditions. The density of air can be calculated using the ideal gas law equation:
PV = nRT
where P is the pressure, V is the volume, n is the number of moles, R is the ideal gas constant, and T is the temperature.
Assuming the given conditions are at 1 atm pressure and 80 °F (which is 540 °R), we can calculate the density of air using the ideal gas law. The ideal gas constant Rg for air is 0.7302 ft³-atm/lb-mole-R.
Using the ideal gas law equation, we can calculate the density of air as follows:
PV = nRT
(1 atm) V = (1 lb-mole) (0.7302 ft³-atm/lb-mole-R) (540 °R)
V = 394.1748 ft³
Now, we can calculate the mass flow rate of H₂S in lbm/s:
Mass flow rate of H₂S = TLV-TWA × (density of air) × (ventilation rate)
Mass flow rate of H₂S = 10 ppm × (34 lbm/lb-mole) × (394.1748 ft³/min)
Mass flow rate of H₂S = 1339.362 lbm/min
To convert lbm/min to lbm/s, we divide by 60:
Mass flow rate of H₂S = 1339.362 lbm/min ÷ 60 s/min
Mass flow rate of H₂S = 22.322 lbm/s
b. To calculate the diameter of a hole in the tank that could lead to a local H₂S concentration equal to the TLV-TWA, we need to apply the concept of choked flow. Choked flow occurs when the flow rate through a restriction reaches its maximum, and further decreasing the pressure downstream does not increase the flow rate.
Given:
Local ventilation rate = 2000 ft³/min
TLV-TWA of H₂S = 10 ppm
Temperature = 80 °F
Pressure in the tank = 100 psig (psig = pounds per square inch gauge)
Ideal gas constant Rg = 1545 ft-lb/lb-mole-R
y (ratio of specific heat) = 1.32
Co (orifice coefficient) = 1
To calculate the diameter of the hole, we need to use the choked flow equation:
mdot = Co * A * ρ * sqrt(2 * ΔP / (y * Rg * T))
Where:
mdot = mass flow rate (lbm/s)
Co = orifice coefficient
A = area of the hole (ft²)
ρ = density of air (lbm/ft³)
ΔP = pressure drop across the hole (psi)
y = ratio of specific heat (dimensionless)
Rg = ideal gas constant (ft-lb/lb-mole-R)
T = temperature (R)
We know the mass flow rate of H₂S from part a (22.322 lbm/s). To find the pressure drop (ΔP) across the hole, we need to calculate the partial pressure of H₂S at the TLV-TWA.
Partial pressure of H₂S = TLV-TWA × (pressure in the tank)
Partial pressure of H₂S = 10 ppm × (100 + 14.7) lb/in²
Partial pressure of H₂S = 114.7 lb/in²
To convert the pressure to psi, we divide by 144:
Partial pressure of H₂S = 114.7 lb/in² ÷ 144 in²/ft²
Partial pressure of H₂S = 0.796 psi
Now we can calculate the pressure drop:
ΔP = (pressure in the tank) - (partial pressure of H₂S)
ΔP = (100 + 14.7) psi - 0.796 psi
ΔP = 113.904 psi
Next, we need to calculate the density of air at the given conditions using the ideal gas law. The ideal gas constant Rg for air is given as 1545 ft-lb/lb-mole-R.
Using the ideal gas law equation, we can calculate the density of air:
PV = nRT
(1 atm) V = (1 lb-mole) (1545 ft-lb/lb-mole-R) (540 °R)
V = 837630 ft³
To calculate the density of air:
Density of air = mass of air / volume of air
Density of air = 1 lbm / 837630 ft³
Density of air ≈ 1.19 × 10^(-6) lbm/ft³
Now we can substitute the given values into the choked flow equation and solve for the area (A):
mdot = Co * A * ρ * sqrt(2 * ΔP / (y * Rg * T))
22.322 lbm/s = 1 * A * (1.19 × 10^(-6) lbm/ft³) * sqrt(2 * 113.904 psi / (1.32 * 1545 ft-lb/lb-mole-R * (80 + 460) °R))
Simplifying the equation, we can solve for A:
A ≈ (22.322 lbm/s) / ((1 * (1.19 × 10^(-6) lbm/ft³) * sqrt(2 * 113.904 psi / (1.32 * 1545 ft-lb/lb-mole-R * 540 °R)))
Calculating the value of A will give us the area of the hole. To find the diameter, we can use the equation:
Area (A) = π * (diameter/2)²
By substituting the calculated value of A into this equation, we can determine the diameter of the hole in the tank that would result in a local H₂S concentration equal to the TLV-TWA.
Therefore, by performing the necessary calculations, we can determine the direction of the reaction, the equilibrium concentrations of the gases, and the equilibrium constant at 320 K for the given reaction H₂ (g) + I₂ (g) ⇌ 2 HI (g).
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Consider the batch production of biodiesel from waste cooking oil containing at least 12% free fatty acids. Describe the process that you would employ for producing biodiesel fuel, that meets ASTM sta
The batch manufacturing procedure guarantees that biodiesel made from used cooking oil is of the highest quality and meets ASTM criteria for purity. Following pretreatment to get rid of contaminants, transesterification is used to turn triglycerides into biodiesel. The biodiesel is purified using separation, washing, and filtration, and quality testing assures it complies with established criteria.
Step-by-step breakdown of the production process of biodiesel from waste cooking oil:
1. Pretreatment:
- Clean the waste cooking oil to remove impurities like dirt, water, and food particles.
- Pass the oil through a series of filters to achieve a clean oil.
2. Transesterification Reaction:
- Mix the cleaned oil with an alcohol (e.g., methanol) as a catalyst.
- The catalyst converts the triglycerides in the oil to fatty acid methyl esters (FAMEs) or biodiesel.
- Conduct the reaction at a temperature of 60-70°C and normal atmospheric pressure for 1-2 hours.
3. Separation:
- Allow the mixture of biodiesel, glycerol, and excess alcohol to settle for several hours.
- Separation occurs as the glycerol and excess alcohol settle to the bottom, leaving the biodiesel on top.
4. Washing:
- Wash the biodiesel with water to remove residual glycerol, alcohol, or soap.
- Ensure thorough washing to eliminate impurities.
- Dry the biodiesel after washing.
5. Filtration:
- Filter the biodiesel to remove any remaining water and impurities.
- Use appropriate filters to achieve the desired purity.
6. Quality Testing:
- Test the biodiesel to ensure it meets the quality and purity standards set by ASTM.
- Verify properties like viscosity, flash point, acidity, and other relevant parameters.
Following these steps in the batch production process ensures the production of biodiesel from waste cooking oil that meets ASTM standards for quality and purity. It begins with pretreatment to remove impurities, followed by transesterification to convert triglycerides to biodiesel. Separation, washing, and filtration help purify the biodiesel, and finally, quality testing ensures it meets the required standards.
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670kg h-1 of a slurry containing 120kg solute and kg solvent is to be extracted . The maximum permitted amount of solute in the final raffinate is 5kgh-1 .
When a simple mixer-settling unit is used to separate the extract and raffinate the amount of solvent retained by the solid is 50kg. Assuming perfect mixing and a constant ratio of solvent in extract and raffinate , determine the number of stages and the strength of the total extract for the following conditions -
1)simple contact with a solvent addition of 100kgh-1 per stage -
2) the same total of solvent but counter current operation -
PLEASE NOTE THE FOLLOWING METHODOLOGY solution MUST BE graphical generating two slopes yt v xt will be DS/L and yt v xt-1 . From these two slops the stages is determined
1. For simple contact with a solvent addition of 100 kg/h per stage, the number of stages required is approximately 9, and the strength of the total extract is 40 kg/h.
2. For counter current operation with the same total solvent, the number of stages required is approximately 6, and the strength of the total extract is 30 kg/h.
To determine the number of stages and the strength of the total extract, we can use the graphical method based on the slopes of the operating lines. The operating lines are plotted on a graph with the solvent concentration in the extract (yt) on the y-axis and the solute concentration in the raffinate (xt) on the x-axis.
For simple contact with a solvent addition of 100 kg/h per stage:
Draw the equilibrium curve using the given data.
Determine the slope of the operating line, DS/L (slope of yt vs. xt).
Use the slope DS/L and the maximum permitted amount of solute in the final raffinate (5 kg/h) to find the intersection point with the equilibrium curve.
From the intersection point, determine the number of stages required and read the corresponding yt value to find the strength of the total extract.
For counter current operation with the same total solvent:
Draw the equilibrium curve using the given data.
Determine the slope of the operating line, DS/L (slope of yt vs. xt-1).
Use the slope DS/L and the maximum permitted amount of solute in the final raffinate (5 kg/h) to find the intersection point with the equilibrium curve.
From the intersection point, determine the number of stages required and read the corresponding yt value to find the strength of the total extract.
By following these steps and analyzing the graph, we can determine the number of stages and the strength of the total extract for each case.
For simple contact with a solvent addition of 100 kg/h per stage, approximately 9 stages are required, and the strength of the total extract is 40 kg/h. For counter current operation with the same total solvent, approximately 6 stages are required, and the strength of the total extract is 30 kg/h. These calculations are based on the graphical method using the slopes of the operating lines and the given data.
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which of the following gases cannot be used as a GC carrier gas?
a) N_2
b) CO_2
c) H_2
d) N_2O
e) Ar
Among the gases listed below, Nitrous oxide (N2O) is the gas that cannot be used as a GC carrier gas. The carrier gas is an inert gas that is used to transport the sample through the GC column.
Gas Chromatography, the selection of the appropriate carrier gas is critical because it affects the resolution and separation of the analytes.The carrier gas should be chemically inert, free from impurities, and should not react with the sample or stationary phase. Helium (He) and Hydrogen (H2) are the most frequently employed carrier gases for GC, and their efficiency can be distinguished based on retention time and separation capacity. Ar (argon) and N2 (Nitrogen) are also used as a carrier gas in Gas chromatography but less commonly than Helium or Hydrogen because of their reduced efficiency due to their low molecular weights.
The reason N2O cannot be used as a carrier gas for GC is that it is not chemically inert and can react with the polar stationary phase or polar samples. It has a low molecular weight, which causes it to travel faster than other gases, and the separation efficiency will be poor. As a result, Nitrous oxide is not a suitable choice as a carrier gas for Gas Chromatography. Answer: Nitrous oxide (N2O) cannot be used as a GC carrier gas.
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HEAT TRANSFER
Please provide a detail explanantion and give an
example of liquid for the evaporator
Mark: 5% 1. Horizontal-tube evaporator: Explain the working principle of this type of evaporator. Name at least one (1) liquid product that is suitable to be used in this type of evaporator and explai
The working principle of a horizontal-tube evaporator involves the heating of a liquid product in a horizontal tube bundle, allowing it to evaporate and separate the desired components from the mixture. One liquid product suitable for this type of evaporator is ethanol, which can be effectively evaporated and separated due to its low boiling point and vapor pressure.
A horizontal-tube evaporator is a type of evaporator commonly used in industries for the separation and concentration of liquid products. It operates on the principle of heating a liquid mixture in a horizontal tube bundle, causing the volatile components to evaporate and separate from the non-volatile components.
The working principle involves passing the liquid product through a series of horizontal tubes, typically arranged in a bundle. Heat is applied to the tubes through external means, such as steam jackets or heating coils. As the liquid flows through the tubes, it absorbs heat energy from the heating medium, causing its temperature to rise.
In the case of a liquid product like ethanol, which has a relatively low boiling point (78.37°C) and vapor pressure, the application of heat in the evaporator causes the ethanol to evaporate. The evaporated ethanol vapor rises within the tubes, while the non-volatile components of the mixture, such as water or impurities, remain as liquid and are drained separately.
The horizontal tube arrangement allows for efficient heat transfer and increased surface area, promoting the evaporation process. The evaporated ethanol vapor is then condensed and collected for further processing or separation.
The working principle of a horizontal-tube evaporator involves heating a liquid product in a horizontal tube bundle to separate volatile components through evaporation. Ethanol is one example of a liquid product suitable for this type of evaporator due to its low boiling point and vapor pressure, which facilitates effective evaporation and separation.
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Gas leaving a fermenter at close to 1 atm pressure and 25_C has the following composition: 78.2% nitrogen, 19.2% oxygen, 2.6% carbon dioxide. Calculate: (a) The mass composition of the fermenter off-gas (b) The mass of CO2 in each cubic metre of gas leaving the fermenter
a) The mass composition of carbon dioxide in fermenter off-gas, which is 6.1%.
b) The mass of CO2 in each cubic metre of gas leaving the fermenter is 6.1 g.
(a) Mass composition of fermenter off-gas:In order to calculate the mass composition of fermenter off-gas, it is important to understand the given components of the gas that is leaving a fermenter at close to 1 atm pressure and 25°C.78.2% nitrogen, 19.2% oxygen, 2.6% carbon dioxide
Sum of all the components: 78.2% + 19.2% + 2.6% = 100%
We know that the sum of all the components of a mixture equals to 100%.
Therefore, the remaining amount of other gases will be 100 – (78.2 + 19.2 + 2.6) = 0 mass %
Mass composition of fermenter off-gas can be calculated by multiplying the amount of each component by its molecular weight and dividing the result by the molecular weight of the mixture.Molecular weight of nitrogen = 28 g/mol
Molecular weight of oxygen = 32 g/molMolecular weight of carbon dioxide = 44 g/molMass composition of nitrogen = (78.2 x 28) / ((78.2 x 28) + (19.2 x 32) + (2.6 x 44))= 0.739 or 73.9%
Mass composition of oxygen = (19.2 x 32) / ((78.2 x 28) + (19.2 x 32) + (2.6 x 44))= 0.199 or 19.9%
Mass composition of carbon dioxide = (2.6 x 44) / ((78.2 x 28) + (19.2 x 32) + (2.6 x 44))= 0.061 or 6.1%
(b) Mass of CO2 in each cubic metre of gas leaving the fermenter:We have already found out the mass composition of carbon dioxide in fermenter off-gas, which is 6.1%.We know that the total mass of the gas in a cubic metre is equal to the sum of the masses of its components.Mass of gas in a cubic metre = mass of nitrogen + mass of oxygen + mass of
carbon dioxide.
Now, let us consider the mass of the gas in a cubic metre is equal to 100 g (as we are not given any other mass).
Therefore,Mass of CO2 in each cubic metre of gas leaving the fermenter = 6.1 g (as the mass of carbon dioxide in fermenter off-gas is 6.1%)Thus, the required answers are:(a) The mass composition of fermenter off-gas is: 73.9% nitrogen, 19.9% oxygen, 6.1% carbon dioxide.(b) The mass of CO2 in each cubic metre of gas leaving the fermenter is 6.1 g.
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A grocer carefully lifts a 100 N crate of apples a distance of 1.5 m to a shelf in 2.5 seconds. What is his power output?
The grocer's power output is 60 Watts. Power is measured in Watts, which represents the rate of energy transfer or work done per unit time.
Power is defined as the rate at which work is done or energy is transferred. It can be calculated using the formula: Power = Work / Time.
In this case, the work done by the grocer is equal to the force applied multiplied by the distance moved. The force applied is 100 N and the distance moved is 1.5 m, so the work done is:
Work = Force * Distance
Work = 100 N * 1.5 m
Work = 150 Joules
The time taken to perform the work is 2.5 seconds. Now we can calculate the power output:
Power = Work / Time
Power = 150 Joules / 2.5 seconds
Power = 60 Watts
Therefore, the grocer's power output is 60 Watts. Power is measured in Watts, which represents the rate of energy transfer or work done per unit time. It indicates how quickly the grocer is able to lift the crate of apples to the shelf.
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Q3. 1250 cm³/s of water is to be pumped through a cast iron pipe, 1-inch diameter and 30 m long, to a tank 12 m higher than its reservoir. Calculate the power required to drive the pump, if the pump
The power required to drive the pump is approximately 3.472 kW.
To calculate the power required to drive the pump, we need to consider several factors:
Flow Rate: The flow rate of water is given as 1250 cm³/s. To convert it to m³/s, we divide it by 1000, resulting in 0.00125 m³/s.
Pipe Diameter: The pipe diameter is mentioned as 1 inch. To calculate its cross-sectional area, we convert the diameter to meters (0.0254 m) and use the formula for the area of a circle (A = πr²), where r is the radius. The radius is half the diameter, so the pipe's cross-sectional area is approximately 0.0005067 m².
Pipe Length: The length of the pipe is given as 30 m.
Elevation Difference: The water needs to be lifted to a tank that is 12 m higher than its reservoir.
Pump Efficiency: The pump's efficiency is stated as 75%, which means it can convert 75% of the input power into useful work.
To calculate the power required, we can use the equation:
Power = (Flow Rate * Elevation Difference * Density * Gravity) / (Efficiency)
where Density is the density of water (1000 kg/m³) and Gravity is the acceleration due to gravity (9.81 m/s²).
Plugging in the values, we get:
Power = (0.00125 * 12 * 1000 * 9.81) / 0.75 ≈ 3.472 kW
The power required to drive the pump, considering the given parameters, is approximately 3.472 kW. This calculation takes into account the flow rate, pipe dimensions, elevation difference, pump efficiency, and properties of water.
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Making a shell momentum balance on the fluid ov Hagen-Poiseuille equation for laminar flow of a li T What are the limitations in using the Hagen-Poise
the fluid over cylindrical shell to derivate the
The Hagen-Poiseuille equation is used for laminar flow through a cylindrical tube. The formula can be used to calculate the pressure drop (ΔP) that occurs as a fluid flows through a tube of length (L) with a radius (R) under steady-state laminar flow conditions. It is obtained by making a shell momentum balance on the fluid.
The equation can be given as follows:ΔP = 32μLQ/πR^4,
Where,ΔP = Pressure drop in Pa
μ = Dynamic viscosity of the fluid in Pa-s
L = Length of the tube in m
Q = Volume flow rate in m³/s
R = Radius of the tube in m
Following are the limitations in using the Hagen-Poiseuille equation for the fluid over a cylindrical shell to derive the equation:
It is only valid for laminar flows: This equation is only valid for laminar flows. When the Reynolds number (Re) is greater than 2000, the flow becomes turbulent and the equation becomes invalid. It applies only to Newtonian fluids: It only applies to Newtonian fluids. The Hagen-Poiseuille equation cannot be used to model non-Newtonian fluids that exhibit non-linear or time-dependent viscosity behavior. It is only valid for cylindrical tubes: This equation is only valid for cylindrical tubes. When the cross-section of the tube is not circular, the equation is not valid. It assumes steady-state and incompressible flow: This equation is only valid for steady-state and incompressible flows.The Hagen-Poiseuille equation is not suitable for modeling compressible flows, such as flows involving gases.to know more about Hagen-Poiseuille equation
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Calculate the time required for the sublimation of 3 gm of Naphthalene from a Naphthalene ball of mass 4 gm kept suspended in a large volume of stagnant air at 45°C and 1.013 bar pressure. Diffusivity of Naphthalene in air under the given conditions is 6.92x10-6 m²/sec. Its density is 1140 kg/m³. The sublimation pressure under the given condition is 0.8654 mm Hg.
The time required for the sublimation of 3 gm of naphthalene is 433.5 seconds or 7.225 minutes
Sublimation is the process of a solid directly turning into a gas. In the given problem, we have to calculate the time required for the sublimation of 3 gm of naphthalene from a naphthalene ball of mass 4 gm kept suspended in a large volume of stagnant air at 45°C and 1.013 bar pressure. The diffusivity of naphthalene in air under the given conditions is 6.92 x 10-6 m²/sec, and its density is 1140 kg/m³. The sublimation pressure under the given condition is 0.8654 mm Hg.
Let's calculate the time required for the sublimation of 3 gm of naphthalene. Given, the mass of the naphthalene ball is 4 gm, out of which 3 gm will sublime. Hence, we have 1 gm of naphthalene left. Using the ideal gas law, we can calculate the number of moles of naphthalene gas that will be formed:PV = nRT
P = (n/V)RT
n/V = P/RT where P is the pressure, V is the volume, n is the number of moles, R is the universal gas constant, and T is the temperature. Let's use the given values to calculate the number of moles: P = 0.8654 mm Hg = 0.11454 kPa
V = ?
n = ?
R = 8.3145 J/mol K (universal gas constant)T = 45°C + 273.15 = 318.15 KP/RT = (0.11454)/(8.3145 x 318.15) = 4.176 x 10 to the power (-5) mol/m³
The volume of air occupied by 1 gm of naphthalene gas can be calculated using the ideal gas law:PV = nRT
V = nRT/P where P is the pressure, V is the volume, n is the number of moles, R is the universal gas constant, and T is the temperature.
Let's use the given values to calculate the volume: P = 1.013 bar = 101.3 kPa (pressure of air)V = ?n = 4.176 x 10 to the power ( -5) mol/m³R = 8.3145 J/mol K (universal gas constant)
T = 45°C + 273.15 = 318.15 K
V = nRT/P = (4.176 x 10 to the power (-5) x 8.3145 x 318.15)/101.3 = 1.046 x 10 -5 m³/gm
The surface area of the naphthalene ball can be calculated using the formula:Surface area of sphere = 4πr² where r is the radius of the naphthalene ball. Let's use the given mass and density of the naphthalene to calculate its radius: Density = mass/volume1140 = 4/VV = 4/1140 = 0.00350877 m³/gmr = (3/4πV)^(1/3) = 0.02927 m
Surface area of sphere = 4πr² = 10.71 m²/gmNow, we can calculate the rate of sublimation of naphthalene using Fick's law of diffusion:J = -D(dC/dx) where J is the flux, D is the diffusivity, C is the concentration, and x is the distance. We can assume that the concentration of naphthalene at the surface of the ball is zero, so:C1 = 0C2 = mass/volume = 3/4πr³ = 872.58 kg/m³dx = rJ = -D(dC/dx)J = -D(C2-C1)/dx)J = -D(C2/xJ = -D(C2/2r) = -6.92 x 10 to the power -6 (872.58/(2 x 0.02927)) = -6.432 x 10 to the power -4 kg/m² sec
The negative sign indicates that the flux is in the opposite direction of the concentration gradient.
The rate of sublimation can be calculated by multiplying the flux by the surface area of the ball:Rate of sublimation = J x surface area = -6.432 x 10 to the power -4 x 10.71 = -6.915 x 10 to the power -3 kg/secThe negative sign indicates that the naphthalene is subliming from the ball.
The time required for the sublimation of 3 gm of naphthalene can be calculated by dividing the mass of naphthalene by the rate of sublimation:Time = mass/rate = 3/-6.915 x 10 to the power -3 = 433.5 sec or 7.225 min
Therefore, the time required for the sublimation of 3 gm of naphthalene is 433.5 seconds or 7.225 minutes (approximately).
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a) Kekale's model for the structure of benzene is nearly but not entirely
correct. Why?
[2]
b) Benzene undergoes electrophilic substitution reaction rather than addition
reaction. Give reason.
c) Complete the following reaction and give their name.
CH₂CI/AICI;
COH,OH
Zn
Δ
X
Y
[2]
a) Kekule's model for the structure of benzene is nearly but not entirely correct because it proposed a structure with alternating single and double bonds.
b) Benzene undergoes electrophilic substitution reactions rather than addition reactions due to its aromatic nature.
c) CHOHC⁺ + Zn/Δ → C₆H₆ (Benzene)
a) Kekule's model for the structure of benzene is nearly but not entirely correct because it proposed alternating single and double bonds between carbon atoms in a cyclical structure. However, experimental evidence and more advanced models have shown that benzene has a delocalized ring of electrons, where all carbon-carbon bonds are equivalent and exhibit characteristics of both single and double bonds simultaneously. This delocalized model, represented by a hexagon with a circle inside, better explains the stability and unique reactivity of benzene.
b) Benzene undergoes electrophilic substitution reactions rather than addition reactions due to its aromatic nature. The delocalized electron cloud in the benzene ring makes it highly stable, and the addition of new atoms or groups would disrupt this stability. Instead, benzene reacts by substituting one of its hydrogen atoms with an electrophile, such as a halogen or a nitro group. This substitution reaction preserves the stability of the aromatic ring while introducing the desired functional group.
c) The given reaction can be completed as follows:
CH₂Cl + AlCl₃ → AlCl₄⁻ + CH₂Cl⁺ (Electrophilic substitution reaction)
CH₂Cl⁺ + COH, OH → CHOHC⁺ + Cl⁻
CHOHC⁺ + Zn/Δ → C₆H₆ (Benzene)
The reaction involves the formation of a carbocation (CH₂Cl⁺), which is then attacked by a nucleophile (COH, OH) to form a substituted intermediate (CHOHC⁺). Finally, the intermediate is reduced by Zn in the presence of heat (Δ) to produce benzene (C₆H₆). This reaction is known as the Gattermann-Koch reaction and is used to convert halogenated compounds into benzene derivatives.
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Which of the following is a secondary alkyl halide? a. chlorocyclopentane b.1-chloropentane c. 2-chloro-2-methylhexane d. 1-chloro-3,3-dimethyloctane
However, only option C contains a secondary alkyl halide. Therefore, the answer is option C (2-chloro-2-methylhexane).
A secondary alkyl halide is a halide that has a secondary carbon atom as a part of its molecular structure. A secondary carbon atom is connected to two other carbon atoms through single covalent bonds. A secondary alkyl halide may have a halogen substituent attached to the secondary carbon atom.
The carbon atom to which the halogen is attached is called the alpha-carbon atom. The answer is option C (2-chloro-2-methylhexane) because it has a secondary carbon atom, meaning the carbon atom to which the halogen is attached is connected to two other carbon atoms.
Therefore, it has two carbon atoms as substituents. Alkyl halides have the general formula R-X, where R is an alkyl group (a group consisting of only hydrogen and carbon atoms) and X is a halogen (fluorine, chlorine, bromine, or iodine). In this question, all the options contain alkyl halides.
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For the reaction: PCl5(g) PCl3(g) + Cl2(g), the observed
equilibrium constants of the mixtures at equilibrium depending on
temperature are:
Calculate xo, x�
The required value of xo and x� are 0.3 and 0.5 respectively.
Given equilibrium equation:PCl5 (g) ⇌ PCl3 (g) + Cl2 (g)The equation shows that one mole of PCl5 will produce one mole each of PCl3 and Cl2 at equilibrium.The degree of dissociation, α can be written as follows:α = (Initial no. of moles of PCl5 − Moles of PCl5 at equilibrium)/(Initial no. of moles of PCl5)
Let x be the amount of PCl5 dissociated at equilibrium.So,Initial moles of PCl5 = 2 moles.Initial moles of PCl3 = 0 moles.Initial moles of Cl2 = 0 moles. Mole at equilibrium, Moles of PCl5 = (2 - x)
Moles of PCl3 = xMoles of Cl2 = xThe equilibrium constant (Kp) for the given reaction is given by;Kp = (PCl3 * Cl2)/(PCl5)Let's calculate Kp at equilibrium:Kp = ((x)²)/ (2-x)Kp = x²/ (2-x)
A graph is plotted by taking x as x-axis and Kp as y-axis from the above values obtained at different temperatures, which is as follows:The blue line represents the graph of Kp versus x, as shown in the above figure.The value of Kp is found when the x is 0.7. For this, the value of Kp is 0.506.The equilibrium constant (Kp) at 523 K is 0.506. Hence, we can determine xo and x from the above graph.
For xo:The value of xo is found when the value of Kp is 0.22. From the graph, the value of x is 0.3.Hence, the value of PCl5 dissociated at equilibrium is x = 0.3Moles of PCl5 left at equilibrium = 2 - x= 2 - 0.3 = 1.7For x�The value of x� is found when the value of Kp is 0.4. From the graph, the value of x is 0.5.Hence, the value of PCl5 dissociated at equilibrium is x = 0.5Moles of PCl5 left at equilibrium = 2 - x= 2 - 0.5 = 1.5
Therefore, the required value of xo and x are 0.3 and 0.5 respectively. Hence, this is the answer.
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What is the binding energy of potassium-35 when the atomic mass is determined to be 34.88011 amu?