a$)$ Data on the process

Feed:

$-T=80F$

$-P=37$ psia

Flash:

$-T_m=270F$

$-P=35$ psia

Absorber:

number of theoretical stages $=3$

number of real stages $=15$

pressure at the top and at the bottom $=32$ psia

Distillation column:

number of theoretical trays $=20$

number of real trays $=30$

$-P_{\text{c}\text{o}\text{n}\text{d}\text{a}\text{n}\text{s}\text{e}\text{r}}=23$ psia

monochlorobenzene from the top $<mn\; id="EditorElement\_20881197">0</mn><mn\; id="EditorElement\_20881198">.</mn><mn\; id="EditorElement\_20881199">1</mn>$lbmo$\frac{l}{h}r$

Cooler:

$-T_{\text{o}\text{u}\text{t}}=120F$

Products:

$-$ monochlorobenzene $=50$lbmo$\frac{l}{h}r$

Thermodynamic model: Wilson $+$ Virial b$)$ Data for the economic evaluation

Calculation of the grass roots cost of the plant

Purchase cost of equipment in base conditions

$lo{g}_{10}(c_P^0)=K_1+K_{2}lo{g}_{10}(-1)+K_3[lo{g}_{10}(-1){]}^2,C_P^0[S],$ A:characteristic variable of the equipment

The coefficients provided in the table refer to year $2001(M$&$S=1110).$ For the calculation of costs

related to nowadays please use M&S equal to $1245\mathrm{.}2.$

For the calculation of the exchange areas the following assumptions should be considered:

$-U_{H1}=750W{m}^{-2}{K}^{-1}$;

$-U_{\text{c}\text{o}\text{n}\text{d}\text{e}\text{n}\text{s}\text{e}\text{r}}=650W{m}^{-2}{K}^{-1}$;

$-U_{\text{K}\text{e}\text{m}\text{t}\text{l}\text{e}}=1100W{m}^{-2}{K}^{-1}$;

$-U_{H2}=280W{m}^{-2}{K}^{-1}$;

service fluid for the condenser and for the heat exchanger $H2$ : cooling water entering at $20C$ and

exiting at $40C.$ Both the heat exchangers are countercurrent;

service fluid for the heat exchanger $H1$ : saturated steam at $3\mathrm{.}5$atm$(139\mathrm{.}34C)$; service fluid for the Kettle reboiler: saturated steam at $7\mathrm{.}5$atm$(168\mathrm{.}30C).$

For the calculation of the volumes of the columns the following assumptions should be considered:

vapor speed along the column: $0\mathrm{.}3\frac{m}{s}$;

$-H[m]=0\mathrm{.}6096*(n{?}_{\text{s}\text{u}\text{y}\text{s}}-1)+4\mathrm{.}6.$

Assume as purchase costs for the flash chamber $+$ other vessels, for accumulation and storage and for

the pumps $90000$ $ and $15000$ S$,$ respectively.

Installation costs

Perforated trays

$C_{AM}=C_{}^{0}N{F}_{RM}^{\text{'}}{F}_q$

$N=$ mumber $of$ trays; $F_{BM}^{\text{'}}{?}^{\text{'}}=1$;

$F_q$:$\{\begin{array}{cc}lo{g}_{10}(F_q)=0\mathrm{.}4771+0\mathrm{.}08516*lo{g}_{10}(N)-0\mathrm{.}3473*[lo{g}_{10}(N){]}^2,& N<mn\; id="EditorElement\_20878746">2</mn><mn\; id="EditorElement\_20878747">0</mn>\end{array}$

$F_q=1,N20$

Other units:

$C_{BM}=C_P^0{F}_{SM},F_{RM}=B_1+B_2{F}_M{F}_P$

For all the units $($except for the pumps and the Kettle reboiler$)$: $F_M=F_P=1.$ For the pumps: $F_P=1$

and $F_M=1\mathrm{.}5.$ For the Kettle reboiler: $F_M=1$ and

$lo{g}_{10}(F_P)=0\mathrm{.}03881-0\mathrm{.}11272lo{g}_{10}(P)+0\mathrm{.}08183[lo{g}_{10}(P){]}^2$ with $P($between $5$ and $140$Process for the separation of monochlorobenzene: design and economic evaluation

Design

A mixture of hydrochloric acid, benzene and monochlorobenzene is separated in a plant to obtain product

streams rich in one single component. After heating and expansion, the feed is separated in a flash unit;

the vapor phase exiting the top of the equipment is fed to an absorber from which hydrochloric acid is

obtained from the top and a liquid stream from the bottom. This stream is mixed with the liquid stream

exiting the flash unit and is fed to a distillation column equipped with a partial condenser; hydrochloric

acid and benzene exit from the top and monochlorobenzene exits from the bottom of the distillation

column. The stream rich in monochlorobenzene is cooled in a heat exchanger and recycled $(2/3)$ at the

top of the absorber$,$ to which is sent by a pump.

The products of the overall plant are $\frac{1}{3}$ of the stream rich in monochlorobenzene exiting the distillation

column, and streams rich in benzene $($from the top of the distillation column$)$ and in hydrochloric acid

$($from the top of the absorber and from the top of the distillation column$).$

It is asked to simulate the separation plant in ASPEN HYSYS ${?}^8$ process simulator, to draw the Block

Flow Diagram and the Process Flow Diagram, to calculate the "non$-$discounted cash flow" and the

"discounted cash flow" and to draw the related cumulative plots.