CASE$1$: Case $1($Extractor $+$ Distillation$)$

Water has a high latent heat $($heat of vaporization$)$ compared to many other components. For the separation of a water$-$acetone mixture $(60$ wt$-$

$\%$ and $40$ wt$\%),$ it may be more energy efficient to use extraction instead of direct distillation. In this example, we compare direct distillation to extraction using $3-$methylhexane as the solvent. please solve the all queastion and do the figur.

The feed stream enters to extraction column @ $25$ oC and $1$ bar with mass$-$ flow rate $60$ kg$/$hr for water and $40$ kg$/$hr for acetone. Solvent$(3-$ Methylhexane$)$ feed stream enters to extraction column @ $30\backslash$deg C and $1$ bar with the of $150$ kg$/$hr$.$ The temperature $30\backslash$deg C sufficient to separate because it is low enough for the extraction of acetone from the water phase to the solvent phase. The product streams of water $($Bottom$)$ and rich solution $($Top$)$ connected with extraction column. The number of stages used in the extraction column is $8$ with adiabatic conditions. Use or move the $1$st liquid phase is WATER and $2$nd liquid phase is $3-$ Methylhexane as Key components. The extraction column operates at $1$ bar and $25$ oC $($Stage $1).$ The rich solution $($Top$)$ stream is connected to distillation column?$($Rec column$)$ and the specifications of column as follows.

$1.$ Equilibrium

$2.50$ stages

$3.$ Partial vapour condenser

$4.$ Kettle type reboiler.

$5.$ Vapour$-$ liquid$-$ liquid phase

$6.$ Distillate rate: $50$ kg$/$hr

$7.$ Reflux ratio: $1\mathrm{.}5$

$8.$ Feed stage: $25$

$9.$ Stage$1/$ condenser pressure: $1$ bar

$10.$ Key component: $2$nd Liquid Phase: water

The bottom product of distillation column connects to heater block with specifications of $30$oC and $1$ bar. The valid phases in heater balock is vapour$-$ liquid$-$ liquid.

Determine whether distillation or extraction is more energy intensive and by how much for separating a $60$ wt$-\%$ acetone $40$ wt$-\%$ water stream.

Use Property Package: UNIQ$-$RK CASE$2$: Case $1$ Direct Distillation $($Single Column$-$ RadFrac$)$

The feed stream enters to redfrac column @ $25$ oC and $1$ bar with mass$-$ flow rate $60$ kg$/$hr for water and $40$ kg$/$hr for acetone. Connect the outlet streams and the specifications of column as follows.

$1.$ Equilibrium

$2.50$ stages

$3.$ Partial vapour condenser

$4.$ Kettle type reboiler.

$5.$ Vapour$-$ liquid phase

$6.$ Convergence: Strongly non ideal liquid

$7.$ Distillate rate: $50$ kg$/$hr

$8.$ Reflux ratio: $5$

$9.$ Feed stage: $48($above stage$)$

$10.$ Stage$1/$ condenser pressure: $1$ bar

Create the new design specs $1$ by clicking the design specifications under block specifications.

$1.$ Mass purity with target value of $0\mathrm{.}9951-$ stream type

$2.$ Select or move the component $$ water

$3.$ Base component $$ Both water and Acetone

Create the new design specs $2$ by clicking the design specifications under block specifications.

$1.$ Mass purity with target value of $0\mathrm{.}995088-$ stream type

$2.$ Select or move the component $$ water

$3.$ Base component $$ Both water and Acetone

Create the vary $1$ by clicking the vary folder in under block specifications.

$1.$ Adjusted variable: reflux ratio

$2.$ Lower value: $0\mathrm{.}1$ and upper value: $20$ Create the vary$2$ by clicking the vary folder in under block specifications.

$1.$ Adjusted variable: Distillate rate.

$2.$ Lower value: $0\mathrm{.}1$ and upper value: $200$

$$ Find the potential energy saving options using case$1$ and case$2.$

$$ Compare the results

$$ Tabulate the all the results of the simulation sheet for case $1$ and case $2.$

$$ Generate detailed report $.$

Please solve it all with details and do the figure

because then i want to do it in aspen plus $14$