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United Arab Emirates University College of Engineering Industrial Training & Graduation Projects Unit. PRODUCTION OF ACETON FROM ISO-PROPANOL. Presented By Eida AlMansouri 980724217 Rehab Alkaabi 199904156 Halima Abdullah 199902518. Summary. Primary objectives .
College of Engineering
Industrial Training & Graduation Projects Unit
PRODUCTION OF ACETON FROM ISO-PROPANOL
Eida AlMansouri 980724217
Rehab Alkaabi 199904156
Halima Abdullah 199902518
Design a chemical plant that uses isopropyl alcohol (IPA)
as the raw material for the production of a food-grade
Acetone and to asses the design from economical,
environmental and safety perspectives.
The purpose of our project is to select the
most suitable process or method
Industrial Production Methods of Acetone
2-propanol dehydrogenation process
The chemical reaction in this process is: OOH
Oxygen | C6H5CH(CH3)2 ---------> C6H5C(CH3)2 -----> C6H5OH + CH3COCH3
Cumene peroxidation process block flow diagram
Iso-propanol dehydrogenation process block flow diagram.
CH3CHOHCH3 -----> CH3COCH3 + H2
What is the catalysts?
It is a substance, usually used in small amounts relative to the reactants, that modifies and increases the rate of a reaction without being consumed in the process.
Catalysts and the required heating
The reactor conversion about 80%
Overall conversion is about 99.5%
Production rate=10000Kg/hr of 99.9wt% acetone
The pump increases the pressure of the feed from 1.01 bar to 2.8 bar.
Heat Exchanger (E-001):
This unit heats, vaporizes, and superheats the feed to 240 oC at 2.8 bar.
In this Reactor only the following reaction occurs in the presence of the catalyst:
This unit heats the molten salt that provides the heat to the reactor.
Heat Exchanger (E-002):
This unit cools and partially condenses the reactor effluent. The exit pressure and temperature are 2.4 bar and 45oC respectively.
Heat Exchanger (E-003):
This unit cools and partially condenses the reactor effluent. The exit pressure and temperature are 2.4 bar and 20oC respectively.
This unit disengages the vapor and liquid effluent from E-003. In this separator, all the hydrogen in the feed enters the vapor phase. All other components distribute according to Raoult’s Law at the temperature of E-003.
Acetone is recovered by absorption into pure process water.
In this distillation column, the acetone, IPA-water, and water in stream 15 are separated. The column operates at 1.4 bar. The acetone must be 99.9% pure and 99.5 mol% of the acetone in the feed must be recovered in stream 16. Stream 17 contains most of the water and IPA-water from stream 15.
In this exchanger, the contents of stream16 are condensed from saturated vapor to saturated liquid.
Heat Exchanger (E-005):
In this exchanger, the flow of stream17 is vaporized from saturated liquid to saturated vapor at 1.4 bar.
This additional distillation column is to process stream 17 further. This column can recover a near azeotropic mixture of IPA-water (88 wt% IPA -with all the acetone remaining in stream 17) out from the top, with residual water and IPA out from the bottom. The top product will be recycled to the feed of the process. The bottom product will go to wastewater treatment. This column operates at 1.2 bar.
In this exchanger, the contents of stream18 are condensed from saturated vapor to saturated liquid.
Heat Exchanger (E-007):
In this exchanger, the flow of stream19 is vaporized from saturated liquid to saturated vapor at 1.2 bar.
Material Balance on the Process
Material Balance on the Reactor
Microscopic equilibrium between gas and liquid. Note that the rate of evaporation of the liquid is equal to the rate of condensation of the gas.
Material Balance on tow phase separator
Material Balance on absorber
IPA-water + Water
Material Balance on the 1st Distillation Column
IPA-water + Water
Material Balance on the 2ndDistillation Column
Table (1): IPA-water flow rates inlet and outlet the feed pump (P-001)
Table (2): Power requirement for feed pump (P-001).
Table (3): IPA-water inlet and outlet flow rates to the evaporator (E-001)
Table (4): Duty and amount of stream used in the evaporator (E-001).
Table (5): IPA-water inlet and outlet flow rates to the reactor (R-001).
Table (6): Duty and amount of fuel used in the reactor (R-001).
Table (7): Products inlet and outlet flow rates to the condenser (E-002).
Table (8): Duty and amount of cooling water needed in the condenser (E-002).
Table (9): Products inlet and outlet flow rates to the 2nd condenser (E-003).
Table (10): Duty and amount of refrigerated water for condenser (E-003)
Table (11): Products and feed flow rates of the acetone distillation column.
Rop =1.5* Rmin
Table (12): Heat duties and amount of utilities needed in the acetone column.
Table (13): Products and feed inlet and outlet flow rates for the IPA-water distillation column.
Table (14): Duties and amount of utilities needed in the IPA column.
C’= 13000 N Q0.615
Where C’ = capital cost in US dollars
N = number of functional units = 8
Q = plant capacity = 10,000 kg/h = 75,600 ton/year