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  • This screencast demonstrates the use of reactor models RStoic, RGibbs, RPlug, and RCSTR through

  • an example problem on the production of ethyl acetate. Open your Aspen simulation and begin

  • a new flow sheet using metric units. To start, enter your process components, ethanol, acetic

  • acid, ethyl acetate, and water. Choose NRTL HOC as your method. Watch the related method

  • video to learn more about choosing a property method. When all information is entered, run

  • the property analysis and then go to the simulation environment. To run all four reactors in one

  • simulation, create a duplicator block, which duplicates an inlet stream and can send it

  • to multiple locations. Create a RStoic, RGibbs, RPlug, and RCSTR reactor, renaming each as

  • such. Add a feed stream into your duplicator, and connect the duplicator outlets to each

  • reactor, naming the streams F-Reactor Type. Create product streams from each reactor,

  • naming them P-Reactor Type. When you're done, your flow sheet should look like this. Click

  • the green next arrow to specify the feed conditions. The stream enters at 70 degrees Celsius and

  • 1 atmosphere. Input the following parameters in kilomoles per hour. 8.892 water, 186.59

  • ethanol, and 192.6 acetic acid. Click the green next arrow to go to the duplicator block.

  • There is no information to enter here, so click the green arrow again. For the sake

  • of comparison, all reactors will be specified at 1 atmosphere and 70 degrees Celsius. Make

  • sure all reactors have vapor-liquid selected as the valid phases. For the CSTR, specify

  • a volume of 0.14 cubic meters. You can see that the RCSTR model requires a reaction to

  • be entered before you can proceed in the simulation. At this point, scroll down on the menu tree

  • and click on the reactions folder. Click new, leave the label as R1, and select a POWERLAW

  • reaction type. Click new again, and enter the forward reaction: ethanol and acetic acid

  • goes to ethyl acetate and water. Assume the reaction is first order with respect to each

  • of the reactants, and zeroth order with respect to each of the products. Enter -1 and 1 for

  • the coefficients, and 1 and 0 for the exponents of your reactants and products, respectively.

  • Now we'll enter the reverse reaction: ethyl acetate plus water goes to ethanol and acetic

  • acid. Enter -1 and 1 for the coefficients, and 1 and 0 for the exponents of your reactants

  • and products, respectively. Press the green arrow to input the reaction's kinetic information.

  • For both reactions, the reacting phase will be liquid, and the concentration basis will

  • be molarity. For the forward reaction, specify a k value as 1.9 * 10^8, and an E value as

  • 5.95*10^7 J/kmol. Make sure the units are correct before proceeding. Repeat the procedure

  • for the reverse reaction by selecting it from the dropdown menu. The k value for the reverse

  • reaction is 5.0*10^7, and the E value is 5.95*10^7 J/kmol. Press the green arrow to go back to

  • the CSTR reaction tab. You can now move the R1 reaction to your selected reaction set.

  • Pressing the green arrow brings you to RGibbs. Remember the reactor is operating at 1 atmosphere

  • and 70 degrees Celsius. Press the green next arrow to move on to RPlug. Choose reactor

  • with specified temperature as the operating type, and choose the operating condition "Constant

  • at specified reactor temperature." Enter 70 degrees Celsius. Pressing the green arrow

  • brings you to the configuration tab. Input a length of 2 meters and a diameter of 0.3

  • meters. Insure the process stream valid phases are vapor-liquid. Go the reactions tab and

  • select R1 and your reaction set. Pressing the green arrow again brings you to RStoic.

  • Input your reactor temperature and pressure. On the reactions tab, click new and input

  • the forward reaction with the appropriate coefficients. Enter 0.7 as the fractional

  • conversion of ethanol. Press the green arrow and run the simulation. Open the stream summary

  • to view the results. You can compare the production rate of ethyl acetate of the four reactors.

  • You can see that RGibbs actually produces the most ethyl acetate, while RCSTR produces

  • the least. Additionally, if you click on the CSTR Results block on the menu tree, you can

  • see the heat duty required for this equipment. Watch the following video in the YouTube playlist

  • to see an application of the reactors chapter on a chlorobenzene production plant.

This screencast demonstrates the use of reactor models RStoic, RGibbs, RPlug, and RCSTR through

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B1 中級

アスペンプラスリアクターの例題 (Aspen Plus: Reactor Example Problem)

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    蔡育德 に公開 2021 年 01 月 14 日
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