Simsci pro/ii free download

The equipment and refrigerant stream data are shown in Table 6. Name the inlet stream 50 and the outlet stream Even though the flowrate of this stream is going to be calculated by the controller, you must enter a flowrate here.

This not only satisfies the data requirements of the dialog box but also serves as an initial estimate. Select the Cold Product Liq- uid Fraction specification and set the value to 0. The Feedback Controller dialog box appears. Click on Parameter and choose Flowrate as the variable.

When complete, the Feedback Controller dialog box looks like Figure A portion of this table is shown below. Compare the quantity of refriger- ant required to that obtained in the previous example. Why are the results different? Use MIXER units to combine the plant liquid streams into one product and the plant vapor streams into another product. Figure Schematic of! Con- nect the streams as shown in Figure Name the units and streams.

Note that the Table 7 gives actual trays and tray efficiency. The kettle reboiler is simulated as a theoretical stage and thus is stage This column has no condenser. Step 2 Enter the Unit Data The mixers require no data. Check that the Number of Trays is cor- rect and that the default selections for Algorithm and Calculated Phases are appropriate to your simulation. Check that the default entry for the Phase of each Product is correct. Estimate the rate of the overhead product.

You can make a good guess from the results of the previous run. You could also use the Define proce- dure, assuming that the overhead stream consists of all the Nitrogen through Methane from the column feed Figure Check the Add Specifications and Variables box.

In the Specifications grid, click on Parameter, choose the bottoms stream, 15, and select Vapor Pressure and True from the lists. Return to the Specifications and Variables dialog box and enter a value of psig kPa. The completed dialog box is shown in Figure Find the reboiler duty required to meet the liquid product specification. TASK Suppose that a nearby refinery has been shut down and some columns are available at bargain prices.

Your company is exploring a joint venture with the Royal Gas Company to build a fractionation plant as shown in Figure 23 to process the liquids from your chiller plant and their plant. You have been asked to provide a quick design for such a plant. To save time, you want to perform a shortcut analysis. However, using keyword input files you can run the problem in either Run Batch or Run-Only mode.

A message will appear indicating that unsupported features were found in your keyword file. You can examine a list of these features by clicking Yes. Run the simulation and create an output file. Read the results from the output Figure For example, for the deeth- anizer column, the recommended number of theoretical trays is 24, which is twice the calculated Fenske minimum trays. For a 24 tray col- umn, the feed should be introduced at tray TASK Use the shortcut results from Part 5 to set up a rigorous simulation of the light ends fractionation plant shown in Figure Begin with the flow- sheet built in Part 4, or create a new flowsheet and provide the feed data given below.

Size each column for valve trays through the Tray Hydrau- lics dialog box. Vary the column duties to meet the specifications given in Table The over- head rate estimates from the shortcut calculation were quite good, but the duty estimates were more approximate.

Plot the liquid and vapor fractions of ethane and propane in column T-2 on a single plot. For column T-3, plot the separation factor of the light and heavy components. For column T-4, plot the overview of the temper- ature and flowrates. Solve it first with a recycle loop and then break the loop using a reference stream Figure Compare the calculation histories in both runs.

Determine the number of iterations it takes to run with the recycle in place and how many it takes to run with the broken recycle. Figure Gas Cooling Flowsheet with Recycle.

Carbon Dioxide 1. Figure 31 contains a portion of the output for the broken-recycle flowsheet. The flash drum vaporizes 40 mole percent of the feed, and the heat exchanger further heats the flash drum liquid. Both the flash drum and heat exchanger have 1 psi 6. A total of 1. Find the liquid fraction and temperature of the PROD stream and the two duties. Table 13 shows the feed composition and condition.

Since the flash duty is unknown before the run, you cannot assign a value to the heat exchanger's duty. Flash Duty 0. Cut 11 91 64 Cut 12 61 Cut 13 55 Cut 14 48 Cut 15 40 Figure 33 shows the Flash Drum Summary, which only reports the water decant flashes.

You can observe that the three solubility methods produce very similar results for this problem. This report gives the vapor and liquid mole fractions and the K-value for each component, providing you with information about the relative volatilities of the components of the prod- ucts. If you choose to lump the vapor and liquid phases into one product, you can obtain the relative compositions of the different phases in the product.

The vapor and liquid mole fractions for each component in the three product phases are at the end of the standard three-phase Flash Drum Summary. For this example the second liquid water phase contains only 0. All three solubility correlations give similar results for the total flowrate of each product.

The best method for selecting a VLLE or a VLE thermodynamic system with a water solubility correlation is to compare the simulation results of each system with actual process data. TASK Enter the assay data for the naphtha feed described below and generate a set of petroleum components.

Also create a plot of the calculated TBP curve and component cuts. The process data is given in Table Average API gravity Leave the default data for the second and third intervals as they are.

Figure 35 shows these entries. Figure 36 shows these entries. Click OK to return to the flowsheet. You will be asked whether you want to generate the pseudocomponents now or at a later time. Answer No. Step 3 Generate the Pseudocomponents You can generate the pseudocomponents at any time by selecting Gener- ate Assay Components from the Input menu.

Do this now. The second flash drum predicts the quantity of liquid that drops out when a temperature drop is imposed on that vapor. Express the recovery specification in Flash F1 as the ratio of one stream's flowrate to that of another. You can define a recovery on the basis of one component or a range of components or, as here, on the total stream. Set the specification so that it matches the figure shown below. You can, however, enter a relative value, as shown below.

Verify that they accu- rately reflect the specifications you entered. Figure 41 shows the completed dialog box. Under certain conditions, however, it is possible for a vapor stream to undergo partial condensation as its pressure is reduced at a fixed temperature or as its temperature is increased at a fixed pressure.

This counter-intuitive phenomenon, called retrograde condensation, is particularly important in the production of petroleum from deep gas wells. Typically, as a gas is brought to the surface its pressure decreases until it matches that of the receiving vessel, which is at ambient temperature. The pressure of the vessel is set to lie in the two-phase region at that tem- perature so that partial condensation of the gas occurs.

The condensed liquid, enriched in the more-valuable heavy components, is recovered. The remaining vapor is repressurized and injected back into the well. Generate a phase envelope plot for the feed stream. Add a Phase Envelope to the flowsheet. In the Phase Envelope dialog box, select the feed stream in the first row of the grid. In the second row, select the feed stream and enter a Liquid Mole Fraction of 0.

In the same way, enter the other liquid mole frac- tions in rows three and four. Plot five graphs: one for each of the plots and one showing all the plots together. Run the simulation. The resulting phase envelope for this exercise is shown below.

TASK Set up a simulation of part of a refrigeration loop. The flowsheet, stream and process data are shown below. Ethane 1. Hint: You can reduce the number of units by combining the cooler and separator. You cannot feed streams 4 and 6 directly into the compressor because the surge mixer has an outlet pressure specification.

Name the units and streams so that the flowsheet looks like Figure Figure Modified Flowsheet 8. The Naphtha feed has been changed and you must ensure that the column can still meet the process requirements such as product recoveries and column duties.

All the data required for this simulation are summarized in the tables below. What are the duties on the condenser and reboiler? What is the reflux ratio? Part B Suppose we are using an existing column for this new separation. Not only is it cheaper to modify an existing column, it is usually quicker to do minor modifications than to wait for a new column.

The problem is that equipment limitations make it unable to meet the desired C5 product purity specification in the overhead stream. Part A As the column has converged with the required recovery specifications, it can clearly cope with the new service. Reflux Ratio 6. You want to increase the throughput of the exchanger and need to calculate the shellside outlet temperature under the new conditions.

Set up the simulation of the exchanger. This exercise is in two parts:. Part A Determine the fouling of the heat exchanger under present operating conditions. Part B Using the fouling results from Part A, rate the existing fouled exchanger for the increased throughput.

Figure Schematic of a Rigorous Heat Exchanger. Part A Determine the fouling of the heat exchanger under current operating conditions. Build the flowsheet and enter the UOM, components, and thermody- namic data, as usual. Enter stream data. Step 1 Enter Unit Data In this example, the shellside outlet temperature is given and we want to determine the fouling resistance. Select Shell Outlet Temperature from the list and enter the value in the Temperature field.

Make a note of the required shellside fouling resistance. Getting Started Workbook FT2 Part B Using the fouling results you have just calculated, rate the existing fouled exchanger for the increased throughput. Note the tubeside and shell- side exit temperatures.

TASK A natural gas stream is compressed before entering a pipeline. The stream is first compressed to 12 bar and then to 26 bar. Liquid condenses in the compressor aftercoolers and is recycled back to the previous stage. The liquid product is removed from the feed flash. Figure Two Stage Compressor Flowshee t. Part A Answer the following questions: 1. What are the amounts of liquid and vapor leaving the process? What compressor work is required for each stage? What are the stream temperatures entering the aftercoolers?

What are the aftercooler duties? Part B If you have time, answer the following questions: 1. Can the same information still be obtained with fewer units in the flowsheet? If so, simulate it and check that the data are available and that the values are the same as in the original calculation.

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