As a process engineer you are hired to design a

chemical plant to produce $80,00$ metric tons per annum of ethylbenzene from

benzene and ethylene. Benzene $($assumed pure$)$ and Ethylene $($containing mole

fraction of $0\mathrm{.}93$ ethylene, $0\mathrm{.}07$ ethane$)$ feed are available at $\frac{20}{b}ar$ and $298K.$

Ethane is inert.

It may be assumed that the only reactions occurring are:

$)+)+$

The molar ratio of benzene to ethylene are approximated at $8$:$1,$ in order to minimize

yielding tri$-$ and higher ethyl benzene.

The plant should operate for $330$ days in a year, to allow for shutdown and

maintenance. Executive summary

Table of Contents

Design Basis

Literature review

Process Simulation

$$ Include process flow diagram from COCO $($in GREEN colour to show

you have run it$)$

Process Description

Process Flow Diagram

$$ Include process flow diagram with all equipment $($labelled$,$ tag

name$/$number$)$ and stream names$/$numbers and table of mass and

energy balance. Please use Microschs Visio or other software to draw

the process flow diagram. Not COCO process flow diagram.

Equipment list

Conclusions

References

Appendices $($if any$)$ The economics information:

Useful information:

$\begin{array}{cc}\text{C}\text{h}\text{e}\text{m}\text{i}\text{c}\text{a}\text{l}cost& US\text{D}\text{o}\text{l}\text{l}\text{a}\text{r}\text{s}\\ \text{e}\text{t}\text{h}\text{y}\text{l}\text{e}\text{n}\text{e}& \text{\$}\frac{0\mathrm{.}77}{k}g\\ \text{b}\text{e}\text{n}\text{z}\text{e}\text{n}\text{e}& \text{\$}\frac{1\mathrm{.}22}{k}g\\ \text{E}\text{t}\text{h}\text{y}\text{l}\text{e}\text{n}\text{e}\text{b}\text{e}\text{n}\text{z}\text{e}\text{n}\text{e}& \text{\$}\frac{1\mathrm{.}54}{k}g\\ \text{D}\text{i}\text{e}\text{t}\text{h}\text{y}\text{l}\text{e}\text{b}\text{e}\text{n}\text{z}\text{e}\text{n}\text{e}& \text{\$}\frac{0\mathrm{.}76}{k}g\\ \text{F}\text{u}\text{e}\text{l}\text{g}\text{a}\text{s}\text{v}\text{a}\text{l}\text{u}\text{e}& \text{\$}\frac{0\mathrm{.}54}{k}g\end{array}$

$\backslash$table$[[$Utility costs.,US Dollars$],[$Low Pressure Steam $(618$kPa saturated$),$$$7\mathrm{.}78/$GJ$],[$Medium Pressure Steam $(1135$kPa saturated$),$$$8\mathrm{.}22/$GJ$],[$High Pressure Steam $(4237$kPa saturated$),$$$9\mathrm{.}83/$G$],[$Natural Gas $(446$kPa,$25\backslash$deg C$),$$$6\mathrm{.}00/$GJ$],[$Electricity$,$$$0\mathrm{.}06/$kWh$],[$Boiler Feed Water $($at $\{$:$549$kPa,$90\backslash$deg C$),$$$2\mathrm{.}45/1000$kg$],[$Cooling Water $(516$kPa:$\}$ and $\{$:$30\backslash$deg C$),],[$Return pressure $>=308$kPa,$],[$Return temperature is no more than $15\backslash$deg C above the inlet,$],[$temperature$,$$$0\mathrm{.}354/$GJ$],[$Refrigerated Water $($available at $516$kPa and $\{$:$5\backslash$deg C$),],[$Return pressure $>=308$kPa,$],[$Return temperature in no higher than $15\backslash$deg C$,$$$4\mathrm{.}43/$GJ$],[$Low$-$temperature Refrigerant, available at $-20\backslash$deg C$,$$$7\mathrm{.}89/$GJ$],[$Very$-$low$-$temperature Refrigerant, available at $-50\backslash$deg C$,$$$13\mathrm{.}11/$GJ$]]1\mathrm{.}1.$Design basis.

$1\mathrm{.}2.$Literature Survey.

Please remember to properly use referencing in your report. Use Harvard

referencing.

$1\mathrm{.}3.$Process Simulation $($COCO$).$ Include the green PFD from COCO.

Remember, the purpose of the simulator is to assist you in doing your work, not

to do the work for you. Remember to include a discussion of the manual

calculations you performed in addition to a description of your simulation and

thermodynamic property method and models used. The simulation report

generated by the simulation package can be included in the appendix.

$1\mathrm{.}4.$Process Description.

$1\mathrm{.}5.$Process Flow diagram with a table containing mass and energy balances: the

flowrates, compositions, temperature, and pressures of all the process streams

$($not needed for the utilities like steam and cooling water$).$ All the process

equipment should be indicated on this flow diagram.

$1\mathrm{.}6.$Equipment list please DONT USE GPTCHAT $,$ ND PLEASE IT IN WORD FORM SHOW ALL THE CALCULATIONS AND GRAPHS $.$ I ALSO INCLUDE THE PICTURE WHERE YOU GET ALL THE INFORMATIONS THANKS As a process engineer you are hired to design a

chemical plant to produce $80,00$ metric tons per annum of ethylbenzene from

benzene and ethylene. Benzene $($assumed pure$)$ and Ethylene $($containing mole

fraction of $0\mathrm{.}93$ ethylene, $0\mathrm{.}07$ ethane$)$ feed are available at $\frac{20}{b}ar$ and $298K.$

Ethane is inert.

It may be assumed that the only reactions occurring are:

$)+)+$

The molar ratio of benzene to ethylene are approximated at $8$:$1,$ in order to minimize

yielding tri$-$ and higher ethyl benzene.

The plant should operate for $330$ days in a year, to allow for shutdown and

maintenance.