LAB 2 ICON

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1.0 Procedure

1.1 The experiment was using iCON software.

1.2 The New Project button was selected to start a new iCON case.1.3 When iCON was activated an initialization, the property package window as shown

in Figure A was prompted.

1) To activate the property package (Referring to Figure 1):i. Al l Property Package was selected from the Chemical System Categories to

enable all possible property packages.ii. The desired Thermodynamic Model was selected. For this problem, Advance

Peng-Robinson was chosen from the Thermodynamic Model drop-down list.iii. Hit the Apply button to acknowledge the selection.

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Adding Components:

1) The Components tab was clicked on to add the components. On the Pur e Compoun dSearch tab, the Ammonia and Water was added to the system.

2) To add the necessary components:

i. Type the component’s name or formula (Methanol and Water) in the Compound box.

ii. From the given list of available components of similar name, double click therequired components.

iii. This will automatically send the selected components to the Selected Compounds box.

3) The Apply button was clicked to acknowledge the selection without leaving thethermodynamics property package environment.

4) Leaved the thermodynamics property package environment by clicked the OK button.

Building the Simulation:

The VisioPFD method was chosen in order to develop the model by creating andconnecting by using the unit operations icons from the stencil palette.

STEP 1: Draw the S 1 (Referring Figure 2). Double click on the stream to rename it to S1and fill the information in the Material Box with the temperature 25°C, pressure520.00kPa with the mole composition of Ammonia is 0.5 and Water with 0.5 (equimolar). Key in also the flow rate of the mixtures which is 2700kgmole/hr. Click enters togo to the next step.

Figure 2

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STEP 2: The splitter was chosen to connect with the Stream 1 in order to split up themixtures of Methanol and Water. At the SP-1, the outlets streams from the SP-1 werenamed as S2 and S3.

Figure 3

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STEP 3: No information was added at the Stream 2.

Figure 4

STEP 4: No information was added at the Stream 3.

Figure 5

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STEP 5: Total Distillation Column was selected to connect it with the Stream 2. At the material box for configuration, change the condenser type to Total rather than Partial as requested in thequestions. Click on the Add/Removes Stages in order to add or delete the stages. For this, 13stages have been added because at the beginning, there are 3 stages already following therequested question to be 16 stages. At the Draw section, the pressure was set up at 520 kPa.

Figure 6

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Figure 7

By referring to Figure 7, the Spec/Estimates button was clicked to fill in the values for the refluxand Draw to Feed Ratio Mole. This was selected by removing the Mole fraction by clicking onthe Delete button and Add button to add the Draw to Feed Ratio Mole. The values inserted forreflux ratio is 1.26 and 0.96 for Draw to Feed Ratio Mole. After that, Click solve button.

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STEP 6: The output for Distillation Column 1 was S4 and S5. No data input was added.

Figure 8

Figure 9

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STEP 7: The valve was selected, V1 to get connected to the S3. The pressure was set at 419.00kPa and the outlet stream was S6.

Figure 10

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Step 8: Next to V1, the output stream was S6. No information added

at this point.

Figure 11

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STEP 9: After S6, the distillation column was connected with it. The distillation columnwas named as Distillation Column 2. At the Configuration button, the total stages to beare 13. Add and removes the stages by hit on the Add/Removes Stages button.101kPawas set up as the pressure.

Figure 12

By referring to Figure 12, the Spec/Estimates button was clicked to fill in the values for thereflux and Draw to Feed Ratio Mole. This was selected by removing the Mole fraction byclicking on the Delete button and Add button to add the Draw to Feed Ratio Mole. The valuesinserted for reflux ratio is 0.834 and 0.96 for Draw to Feed Ratio Mole. After that, Click solve

button.

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STEP 10: The output stream from Distillation 2 was named as S7 and S8 8. No information wasadded in this stream both.

Figure 13

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Figure 14

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2.0 PROCESS FLOW DIAGRAM

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4.0 QUESTIONS AND DISCUSSION

What is the molar flow before entering DC1and DC2?

The molar flow before entering DC1 by look at Stream 2 is 1350 kgmole/h while the molar flow

before entering DC2 by look at Stream 4 is 1350kgmole/h. Both molar flow before entering theDistillation Column 1 and 2 are same.

How to reduce pressure in DC2?

In order to reduce the pressure in DC2 the valve is used. It is proven which we can see from theS3, the pressure is 520.00kPa and after passing through the Valve 1, the pressure reduced to101kPa.

What is the temperature at the bottom of DC1 and DC2?

The temperature at the bottom of DC1 by referring at the Stream 5 is 153.0554°C and thetemperature at the bottom of DC2 by referring at the Stream 8 is 99.918°C.

Did the process achieve a methanol that free from water? What is the purify of themethanol? How to increase the purify?

From the result of the experiment showed that methanol did not fully free from water either fromfirst distillation or second distillation. By referring stream 5, S5 showed that composition ofmethanol and water were 0.00005 and 0.99995 respectively. From second distillation showedthat the composition of methanol and water were 0.00001 and 0.9999 respectively. It is

recommended to do recycle to get more purity of methanol at stream 5 and 8. The experimentwas involved a valve. The purpose we inserted valve was to reduce the pressure. We found that

by inserted the valve the temperature also effected. From the result of the experiment we foundthat the temperature and pressure decrease. The composition of methanol may increase. To

purify the methanol use more valve and distillation column.

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The objective of this experiment is to understand the usage of valve and distillation specification.The process involves the methanol that contains a water composition with it. In order to get the

pure methanol need to undergo process purification. The process was at, the temperature 25°C, pressure 520kPa and flow rate of 2700kmol/hr. This mixture then passes through the Splitter 1.The mixtures then were splatted into 2 streams. At stream S2 and S3 the mass flow rate was33788.57kg/hr. The splitter is used to increase the flow rate that pass through. Second stream was

connected directly the distillation column 1. The temperature at the product stream 8 was increasedto 99.918°C. The mole fraction for the ammonia for Distillation Column 1 is 0.00005 and themole fraction for water is 0.99995. From the composition showed that methanol was not fullyfree from water. The distillation 2 also methanol was not fully free from water. As the mixture

passed through a valve from stream 3 to stream 6 the pressure decrease to 101 kPa. The decreaseof pressure does not give an advanced conversion of methanol. The methanol still has highercomposition of water which is 0.99999. The methanol for both distillation column still have ahigher composition of water.

Recommendation

1) Recycle the product again to get the pure methanol.2) Increase the number of valve and distillation column.

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LAB 2 ICON