- Methanol Feed: Methanol is fed into the FBR, where it's mixed with air.
- Catalytic material: The methanol-air mixture passes over catalytic pellets, typically silver or iron oxide.
- Oxidation Reaction: The metal oxide facilitates the oxidation reaction, converting methanol into HCHO.
- Formaldehyde Production: The resulting CH2O gas is then collected and processed for use in various applications.
1. Type: Fixed Bed Reactor (FBR)2. Process: Catalytic oxidation of methanol to formaldehyde3. Capacity: 10,000 kg/h formaldehyde
1. Diameter: 2.5 meters2. Length: 10 meters3. Bed Height: 5 meters4. Bed Volume: 25 cubic meters5. Void Fraction: 0.4
1. Temperature: 250-300°C2. Pressure: 2-3 bar3. Inlet Gas Flowrate: 50,000 Nm³/h4. Methanol Concentration: 30% (vol.)5. Air/Methanol Ratio: 10:1
1. Type: Silver or iron oxide2. Particle Size: 3-5 mm3. Density: 0.5-0.7 g/cm³4. Surface Area: 100-200 m²/g
1. Shell: Stainless steel (SS 316L)2. Metal Oxide Support: Ceramic or stainless steel3. Insulation: Refractory ceramic blanket
1. Pressure Relief Valve: Set at 3.5 bar2. Temperature Control: Thermocouples and temperature controllers3. Emergency Shutdown: Automated shutdown system4. Fire Suppression: Water spray system
1. Temperature Indicators: Thermocouples and temperature indicators2. Pressure Indicators: Pressure gauges and transmitters3. Flow Indicators: Flow meters and indicators4. Control System: Distributed control system (DCS) with programmable logic controller (PLC)
1. Regular Maintenance: Every 6 months2. Catalytic Substance Replacement: Every 2-3 years3. Inspection: Every 5 years
-rA = k1pA/1+k2pA
where p represents the partial pressure in atm and A refers to methanol.
CH3OH + ½ O2 → HCHO + H2O.
- Methanol feed rate (kmol/h)
- Air feed rate (kmol/h)
- Operation temperature (°C)
- Operation pressure (atm)
- Catalyst activity (k1, h⁻¹)
- Catalyst inhibition constant (k2, atm⁻¹)
- Formaldehyde production rate (kmol/h):
- Methanol conversion (%):
- Reaction vessel volume (m³):
Please note that this is a simplified calculator and does not take into account many factors that can affect the actual performance of a reaction chamber.
A mathematical model for the fixed bed reactor:
Assumptions:
- The process equipment is a plug flow reactor (PFR) with a constant cross-sectional area.
- The reaction is a first-order reaction with respect to methanol concentration.
- The reaction is catalyzed by a silver-based agent.
- The substance is uniformly distributed throughout the model.
- The reaction temperature is constant throughout the model.
Model Equations:
- Mass Balance Equation:
∂C_A/∂t + v * ∂C_A/∂z = -r_A
where C_A is the concentration of methanol (A), v is the superficial velocity, z is the axial coordinate, and r_A is the reaction rate.
Reaction Rate Equation:
r_A = k * C_A
where k is the reaction rate constant.
Metal oxide Activity Equation:
k = k_0 * exp(-E_a/RT)
where k_0 is the pre-exponential factor, E_a is the activation energy, R is the gas constant, and T is the reaction temperature.
Boundary Conditions:
C_A(z=0) = C_A0 (inlet concentration)
C_A(z=L) = 0 (outlet concentration)
where L is the length of the FBR.
Dimensionless Variables:
- Damköhler Number (Da):
Da = k * L / v
- Thiele Modulus (φ):
φ = L * sqrt(k/D_A)
where D_A is the diffusivity of methanol.
Model Solution:
The model equations can be solved using numerical methods such as the finite element method or the method of lines.
Here's a sample solution using MATLAB:
k_0 = 1.23e6; % pre-exponential factorE_a = 50000; % activation energyR = 8.314; % gas constantT = 250; % reaction temperatureL = 10; % reactor lengthv = 0.1; % superficial velocityC_A0 = 1; % inlet concentration
k = k_0 * exp(-E_a/(R*T));
Da = k * L / v;
phi = L * sqrt(k/0.1);
[t, C_A] = ode45(@(t, C_A) -k * C_A, [0 10], C_A0);
plot(t, C_A);
ylabel('Methanol Concentration');
So, let's break down the MATLAB code that solves the mathematical model of the fixed bed reactor! The code starts by defining the parameters of the reaction, such as the pre-exponential factor (k_0), activation energy (E_a), gas constant (R), and reaction temperature (T). It also defines the length of the reaction unit (L), superficial velocity (v), and inlet concentration of methanol (C_A0). Then, it calculates the reaction rate constant (k) using the catalyst activity equation. The Damköhler number (Da) and Thiele modulus (phi) are also calculated to characterize the reaction. Finally, the code uses the ode45 function to solve the differential equation that describes the reaction and plots the methanol concentration as a function of time. This code helps us visualize how the reaction proceeds over time and how the different parameters affect the outcome. Give it a try!
Note that this is a simplified model and does not take into account many factors that can affect the actual conversion unit performance.
log10k1 = 11.43-3810/Tlog10k2 = 10.79-7040/T
But we know that,
CA = PA/RT , PA = CART
Finally, the rate expression is
1/-rA = [(1+εAXA)/k1RTCAO(1-XA)] + k2/k1
Where εA is the fractional change in volume
εA = (moles of products - moles of reactants)/ moles of reactants
= 0.147
Substituting the values εA and CAo in the final rate expression and plotting the graph between 1/-rA Vs XA.
XA |
1/-rA |
0 |
81632.7 |
0.1 |
92036.3 |
0.2 |
105041 |
0.3 |
121761 |
0.4 |
144054 |
0.5 |
175265 |
0.6 |
222082 |
0.7 |
300109 |
0.8 |
456163 |
0.9 |
924327 |
From the graph the area under the curve for XA = 0.9 = 205000 Kg-sec / K-mole
The design Equation for a fixed-bed vessel is
W / FAO = dXA / -rA
W / FAO = 205000 Kg-sec / K-mole
FAO = molar feed rate of methanol
= 201.80 K-mol/hr= 0.0506 K-mol/sec
But from the bulk density of silver oxide = 100lb/ft3
= 100 X 0.453 Kg/0.3048m3= 1599 kg/m3
= 11,491.38 Kg/1599 Kg/m3
Ag2O volume = 7.186 m3
Assume the Volume of the reaction vessel to be three times the Ag2O volume since gas flows into it (Vr = 3Vc)
Vr = Volume of the reaction container
Vc = Ag2O bed volume
As,
Volume of the cylindrical type reactor unit = 21m3
π d2L/4 = 21
Assume the L/D ratio is 2
The diameter of the cylindrical reaction vessel = 2.4m
Its Length = 5m
Total Heat evolved in the reaction processing unit Q = 896043 Kcal/hr
U = Overall Heat Transfer Coefficient = 900 W/m2 oK
Tln = (149.6-60)-(343-100)/ln{(149.6-60)/(343-100)}= 153.35 oC
Heat Transfer Area AH = Q / U X Tln = 35.33 m2
Number of Tubes present in the reaction chamber Nt = AH /πdl
Assume the diameter of the tube = 0.1m
Assume the length of the tube = 4m
Therefore Number of Tubes Nt = 25