Phenol is added to mixer $1$ and mixed with recycled phenol from distillation column $1.$ Into a pump $1$ then into mixer $2$ the product is then mixed with fresh H$2$ and recycled H$2.$ The product is sent to heat exchanger $1$ then a fixed bed reactor and reacted at $100$ degrees Celsius and $5$ bar. Cyclohexanol, Cyclohexanone, unreacted H$2$ and unreacted Phenol is then passed to heat exchanger $2$ then flash separator $1.$ h$2$ is removed and recycled back into the system through a compressor then back into mixer $2.$ The products from separator $1$ are passed through pump $2$ then heat exchanger $3$ then distillation column $1,$ phenol is separated and passed through heat exchanger $4$ and joins mixer $1$ from cyclohexanone and cyclohexanol which are removed as top product. This product is then passed through a reboiler and heat exchanger $5$ then Into Distillation column $2,$ cyclohexanol is removed as bottom product while cyclohexanone is removed as top product and stored. Cyclohexanol is passed through heat exchanger $7$ then reacted in reactor $2$ to dehydrate it into cyclohexanone. The product is passed through heat exchanger $8$ then into separator $2$ where hydrogen is removed as top product and cyclohexanone as bottom and sent into distillation column $1$ after passing through pump $3.$

Perform a MANUAL CALCULATION $($by hand$)$ energy balance to produce cyclohexanone and cyclohexanol from phenol.

USE specific heat capacity: Phenol$=134\mathrm{.}58$ KJ$/$molK $,$ cyclohexanone$=177\mathrm{.}20$KJ$/$molK $,$ Cyclohexanol$=214\mathrm{.}06$ KJ$/$molK$,$ H$2=28\mathrm{.}84$Kj$/$molK

Reactor $1-$ Phenol conversion rate $99\mathrm{.}9\%,$ cyclohexanone selectivity $99\mathrm{.}2\%,$ cyclohexanol selectivity $0\mathrm{.}8\%$

Reactor $2-$ temp $275$C$,$ Phenol Conversion $89\%$ Selectivity for Cyclohexanone $93\%,$Pressure $1$ atm

Mass flowrate$=$ kg$/$hr

Molar flowrate$=$kmol$/$hr

C$6$H$5$OH $+2$H$2=$C$6$H$10$O

C$6$H$10$O $+$ H$2=$ C$6$H$12$O

Reflux ratio $=0\mathrm{.}68$

Efficiency of separator $100\%$

Distillation column $1$ efficiency $90\%$

Distillation column $2$ efficiency$=80\%$

Q$17$ Heat balance around reactor $2$

Stream $38$ in stream $39$ out

stream $38$

temp $180$ C $,$ pressure $1$ bar, phenol molar flowrate in kmol$/$hr $=0\mathrm{.}000,$ phenol mass flowrate $=0\mathrm{.}000,$Mole fraction of phenol is $0\mathrm{.}000.$ Cyclohexanone molar flowrate in kmol$/$hr $=1\mathrm{.}054,$ Cyclohexanone mass flowrate $=103\mathrm{.}440,$Mole fraction of Cyclohexanone is $0\mathrm{.}310.$ Cyclohexanol molar flowrate in kmol$/$hr $=2\mathrm{.}345,$ Cyclohexanol mass flowrate $=234\mathrm{.}870,$Mole fraction of Cyclohexanol is $0\mathrm{.}690.$ All other components $0.$

stream $39$

temp $180$ C $,$ pressure $1$ bar, phenol molar flowrate in kmol$/$hr $=0\mathrm{.}000,$ phenol mass flowrate $=0\mathrm{.}000,$Mole fraction of phenol is $0\mathrm{.}000.$ Cyclohexanone molar flowrate in kmol$/$hr $=3\mathrm{.}141,$ Cyclohexanone mass flowrate $=308\mathrm{.}258,$Mole fraction of Cyclohexanone is $0\mathrm{.}464.$ Cyclohexanol molar flowrate in kmol$/$hr $=0\mathrm{.}258,$ Cyclohexanol mass flowrate $=25\mathrm{.}836,$Mole fraction of Cyclohexanol is $0\mathrm{.}038.$ hydrogen molar flowrate in kmol$/$hr $=3\mathrm{.}377,$ hydrogen mass flowrate $=6\mathrm{.}822,$Mole fraction of hydrogen is $0\mathrm{.}498$

Q$18$ Energy balance around heat exchanger $8$

Stream $39$ in stream $40$ out

stream $39$

temp $180$ C $,$ pressure $1$ bar, phenol molar flowrate in kmol$/$hr $=0\mathrm{.}000,$ phenol mass flowrate $=0\mathrm{.}000,$Mole fraction of phenol is $0\mathrm{.}000.$ Cyclohexanone molar flowrate in kmol$/$hr $=3\mathrm{.}141,$ Cyclohexanone mass flowrate $=308\mathrm{.}258,$Mole fraction of Cyclohexanone is $0\mathrm{.}464.$ Cyclohexanol molar flowrate in kmol$/$hr $=0\mathrm{.}258,$ Cyclohexanol mass flowrate $=25\mathrm{.}836,$Mole fraction of Cyclohexanol is $0\mathrm{.}038.$ hydrogen molar flowrate in kmol$/$hr $=3\mathrm{.}377,$ hydrogen mass flowrate $=6\mathrm{.}822,$Mole fraction of hydrogen is $0\mathrm{.}498$

stream $40$

temp $50$ C $,$ pressure $1$ bar, phenol molar flowrate in kmol$/$hr $=0\mathrm{.}000,$ phenol mass flowrate $=0\mathrm{.}000,$Mole fraction of phenol is $0\mathrm{.}000.$ Cyclohexanone molar flowrate in kmol$/$hr $=3\mathrm{.}141,$ Cyclohexanone mass flowrate $=308\mathrm{.}258,$Mole fraction of Cyclohexanone is $0\mathrm{.}464.$ Cyclohexanol molar flowrate in kmol$/$hr $=0\mathrm{.}258,$ Cyclohexanol mass flowrate $=25\mathrm{.}836,$Mole fraction of Cyclohexanol is $0\mathrm{.}038.$ hydrogen molar flowrate in kmol$/$hr $=3\mathrm{.}377,$ hydrogen mass flowrate $=6\mathrm{.}822,$Mole fraction of hydrogen is $0\mathrm{.}498$

Q$19$ Energy balance around heat exchanger $9$

Stream $41$ in stream $42$ out

Stream $41$

temp $50$C $,$ pressure $1$ bar, hydrogen molar flowrate in kmol$/$hr $=3\mathrm{.}377,$ hydrogen mass flowrate $=6\mathrm{.}822,$Mole fraction of hydrogen is $1\mathrm{.}000.$ All other components are $0$

Stream $42$

temp $25$ C $,$ pressure $1$ bar, hydrogen molar flowrate in kmol$/$hr $=3\mathrm{.}377,$ hydrogen mass flowrate $=6\mathrm{.}822,$Mole fraction of hydrogen is $1\mathrm{.}000.$ All other components are $0$

Q$20$ energy balance around pump $3$

Stream $47$ in stream $48$ out

Stream $47$

temp $50$ C $,$ pressure $1$ bar, phenol molar flowrate in kmol$/$hr $=0\mathrm{.}000,$ phenol mass flowrate $=0\mathrm{.}000,$Mole fraction of phenol is $0\mathrm{.}000.$ Cyclohexanone molar flowrate in kmol$/$hr $=3\mathrm{.}141,$ Cyclohexanone mass flowrate $=308\mathrm{.}258,$Mole fraction of Cyclohexanone is $0\mathrm{.}924.$ Cyclohexanol molar flowrate in kmol$/$hr $=0\mathrm{.}258,$ Cyclohexanol mass flowrate $=25\mathrm{.}836,$Mole fraction of Cyclohexanol is $0\mathrm{.}076.$ All other components are $0.$