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Reactor design for petrochemical Lab and assignment using polymath
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REACTOR FOR PETROCHEMICAL
CCB4433
ASSIGNMENT & LAB
Mohamed Asyraf Bin Mohamed Lias 15564
Muhammad Farid BinShahman 15566
Khairil Amri Bin Romli 15387
Mohd Eshar Bin Abdul Halim 15638
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2
OBJECTIVES
In this assignment, there are several objective to be achieved:
1. To solve using two method which are manually and using polymath software
2. To investigate the effect of varying the parameter chosen
3. To compare the weight of catalyst using different reactor Packed bed and fluidized
bed (CSTR).
RESULT AND DISSCUSSION.
1.0 Simulation on hydrogenation of ethylene to ethane (10.4).
The hydrogenation of ethelene to Ethane is carried out over a cobalt molybdenum catalyst.
The simulation is carried out based on the data given:
Run No. Reaction rate PE PEA PH
1 1.04 1 1 1
2 3.13 1 1 3
3 5.21 1 1 5
4 3.82 3 1 3
5 4.19 5 1 3
6 2.391 0.5 1 3
7 3.867 0.5 0.5 5
8 2.199 0.5 3 3
9 0.75 0.5 5 1
Table 1 : Diffrential Reactor Data
The simulation tested the data given through 4 different model equation which have
shown different result and values. The result of simulation will only cover the variance
value which indicate the best model of equation for the system.
3
Figure 1: Model 1 simulation result
Model 1 equation show the unrealistic result when the value of KEA can reach to
negative value since the value is 0.019 +-(0.03). This result shows that the model equation
cannot be used for the hydrogenation process. As Conclusion model 1 equation is not
suitable for the hydrogenation system.
Figure 2: Model 2 simulation result
Model 2 equation show good result because its shows very low value of variance
which is 0.0060534. Therefore Model 2 equation is suitable for the hydrogenation system
calculation.
4
Figure 3: Model 3 simulation result
Model 3 equation show good result because its shows very low value of variance which is
0.0623031. However the variance is higher than the model 2.
Figure 4: Model 4 simulation result
Model 4 equation show good result because its shows very low value of variance which is
0.0495372. However the variance is higher than the model 2.
5
2.0 Catalyst Decay in a Fluidized Bed Modeled as a CSTR(10.6).
The feed stream contains 80% crude and 20% inert. The crude oil contains sulphur
compounds, which poison the catalyst. The rate of catalyst is first order in the crude oil
concentration. The rate of catalyst decay is first order in the present of activity, and the
first order in the reactant concentration. The volumetric feed rate is 5000 m3/h. there are
50,000 kg of catalyst in the reactor and the bulk density is 500 kg/ m3.
Figure 5: Variation of C, a, and X with time in a CSTR.
The graph show the variation of concentration, activity and conversion of the
particular component with the function of time. The X- axis indicates the time of decay
which is 0.5. The concentration show the two direction which is decreasing and increasing.
The concentration decrease until time 0.05 and the increase until t=0.5. While the activity
show the decreasing order which ended at value of 0.2 at t=0.5. The conversion also show
two type of direction which are increasing and decreasing. The conversion increase until =
0.05 and the slightly decrease until t=0.5 with value of 0.35.
7
3.0 Decay in Straight-Through Transport Reactor(10.8).
.Figure 7: Catalyst Decay in a Fluidized Bed Modeled as a CSTR simulation result
The graph show the variation of conversion of the particular component with the function
of height of reactor. The X- axis indicates the height of reactor which is 10m high. The
concentration show the two direction which is decreasing and increasing. The conversion
also increasing order which give value of 0.55 at height of 10 m.
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