A mixture of benzene, air, and hydrochlonc usid is fed to a reustor $($R$1)$ producing

munochlorobenzene $($MCB$)$ as the primary product. The reactor operates continuously with a $20\%$

wonersion per pass of berzene, $5\%$ of the berzene converled per pass combusts. The reactur

isolates isothermally at $2700C.$ All reactants enter at the reactor temperature. The hot reactor

products pass to a hoiler wherein they are used to boil water to produce dry saturated steam at

$1000$C$.$ This dry saturuled sleam is fed to a heat exchanger which preheats recycled hydructloric

acid $($HC$)$ on roate to RI$.$ The cooled reactor products exil the boiler at $1500$C and are

immediately passed to a second heal exchinger. The reactor products are further cooled bere to

fivac: and are then discharged to a vented vessel which allows gases to exit the process. The

remaining process liquid passes to a decanter. In the decanter, the organie and aquenus phases are

separated. Both phases are sent to intennediate holding sections. The holding vessel which

uccomnodates stonge of the wuter, prior to use as a hydrolysis fexd, mcorponutes un overflow

system. The overflow system ultimutely discharges to the drain. The organic liquid from the

decanter pusses to the extructor unit purposed with the recovery of phenol from hquid hydrochloric

acid arriving preconled $($at $500C)$ from the hydrolysing unit. The organic liquid exiting the

extractor passes to a distillation section which sequentially separates the constituents. The first

unit, distillarion column $(KI,$ fecovers the phenol product at $99$mol$\%$ purity. This product stream,

which may be assumed to contain no benzene, is sent for funther proessing elsewhere in the plane.

The top product from $KI$ passes to a scend distillation column, wherein the binary mixture is

separated producing two streams which are used as feedstock for the reactors. You may assume

that the benzene composition of the top and bottom product streums produced by $K2$ are $98$ mol$\%$

and $2mo{l}^0\%$ respectively. The main $MCB$ output from the distillation section is hydrolysed in a

second reactor which operates isothermally at $310C$ with a $22\%$ conversion per pass of MCB$.$

You may assume that any benzene present in the feed passes through the reactor. The reactor

products move to an ideal separator which fully recovers all unconverted MCR $($at $99\mathrm{.}9\%$ purity$).$

which is recyeled to the reactor. This recycle nperates with a small purge stream $(r=0\mathrm{.}905)$ to

prevent build$-$up of unwanted volatiles.

Additional Information:

The process operates continuously. The overall conversion of benzene within the process is

$-100\%.$

The process runs under stead state conditions.

The levels in the buffer $($holding$)$ tanks do not ctange under normal operating conditions.

All pressures are approximaly I bar absolute$.$

Berzene und hydroctlonic acid $(25$ wt$\%)$ ure availuble from sepurute storage facilities to feed

the process as required.

Process conditions are such that no HCl gas leaves the chlorination unit.

Hydrogen gas does not appeat in the process.

Discharge to the water drain must nut exceed $560$ kgh hour.

The molar feed ratio $($steam $($MCB$)$ for the hydrolysis unit is $3$:$2$

The $R1$ molar fied ratio $($air$\text{'}$benzene$)$ is $2$:$1.$

You mily assume that the temperature of the licund feed supplied to KI is $$90C.$

K$1$ opentes with a reflux ratio of $2.$

Overview of main tasks to consider:

Construct a material balance for the process.

Perform entergy balances fur specilied items within the process.