Junior Design Reactor_Separations Presentation
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Transcript of Junior Design Reactor_Separations Presentation
![Page 1: Junior Design Reactor_Separations Presentation](https://reader031.fdocuments.net/reader031/viewer/2022030304/5876859b1a28ab1b158b6f8b/html5/thumbnails/1.jpg)
The Production and Optimization
of Ethylene Oxide
Roderick Ashcraft
Anika Coolbaugh
Matthew Fox
Chad Glasscock
Justin Talbott
Harry Weaver
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Introduction
Given a process and tasked with creating 99.5%wt
ethylene oxide
Produced 120,000 tonnes per year
𝐶2𝐻4 + 0.5𝑂2→ 𝐶2𝐻4𝑂 . . . . . . . .(1)
𝐶2𝐻4 + 3𝑂2 → 2𝐶𝑂2 + 2𝐻2𝑂 . . . . . .(2)
𝐶2𝐻4𝑂 + 2.5𝑂2 → 2𝐶𝑂2 + 2𝐻2𝑂 . . . . .(3)
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Base Case
Two reactors
Adiabatic
Conversion of 20% of the ethylene
Two absorbers
5 stages
30 bar and 64 °C
Water to Ethylene Oxide ratio of 100
Stripper
5 stages
11.35 bar and 52 °C
MPS to Ethylene Oxide ratio of 40
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Base Case
Distillation column
31 stages
10 bar
Reboiler uses HPS
18700 MJ/hr
Overall EAOC of base case
Loss of 222 million/yr.
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Base Case Cost Breakdowns
Ethylene62%
High Pressure Steam27%
Deionized Water2%
Electricity8%
Boiler Feed Water1%
Ethylene
High PressureSteam
Cooling Water
RefridgeratedWater
Waste WaterTreatment
Deionized Water
Electricity
Boiler Feed Water
Compressors40%
Pumps3%
Heat Exchangers
37%
Reactors9%
Catalyst11%
Compressors Pumps
Separations Heat Exchangers
Reactors Catalyst
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Separations - Results
Absorber
1 Absorber
10 Stages
Pressure: 30 bar
Temperature: 64°C
Pressure Drop: 54 kPa
Water to ethylene oxide ratio is 56
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Separations - Results
Strippers
1 stripper
Pressure: 3 bar
Pressure Drop: 49 kPa
Steam to ethylene oxide ratio is 11
Superheated steam at 3 bar and 150°C
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Separations - Results
Distillation Column
Tray column
15 stages at 12” spacing
Diameter: 2.07m
Reflux Ratio:1.18
Active Area: 2.70m
Weir Height: 3”
Pressure: 3 bar
Pressure Drop: 10 kPa
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Separations - Results
Reflux Drum:
Volume: 6.5 m3
Condenser:
Uses cooling water
-18,600 MJ/hr
Reboiler:
Uses LPS
20,000 MJ/hr
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Separations - Discussion
Absorber and Stripper
Main optimization was done on the water and
stream ratios
Removed an absorber
Dropped the pressure in the stripper and
distillation column
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$(40,000,000.00)
$(35,000,000.00)
$(30,000,000.00)
$(25,000,000.00)
$(20,000,000.00)
$(15,000,000.00)
$(10,000,000.00)
$(5,000,000.00)
$-
62/13 60/12 58/12 56/11 54/11 52/11
EAO
C
Absorber Water Ratio/ Stripper Steam Ratio
EAOC as Affected by Water and Steam Ratios
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Separations - Discussion
Distillation column
Optimized R/Rmin
Determined appropriate tray spacing
Reduced temperature and pressure
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EAOC vs R/Rmin
-$36,100,000
-$36,050,000
-$36,000,000
-$35,950,000
-$35,900,000
-$35,850,000
-$35,800,000
-$35,750,000
-$35,700,000
1 1.1 1.2 1.3 1.4 1.5 1.6 1.7EA
OC
R/Rmin
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EAOC vs Tray Spacing (Designed for Top)
$2,419,400
$2,419,600
$2,419,800
$2,420,000
$2,420,200
$2,420,400
$2,420,600
$2,420,800
$2,421,000
$2,421,200
$2,421,400
$2,421,600
9-inch: 12-inch: 18-inch: 24-inch: 36-inch:
EAO
C
Tray Spacing
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Reactions - Results
Best EAOC found with
One reactor
Adiabatic conditions
With a 99.5% conversion
Inlet at 250°C
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Reactions - Discussion
Began with 3 different reactor types
Adiabatic
Isothermal w/ boiler feed water
Isothermal w/ Dowtherm A
Optimum chosen by keeping conversion the same
and evaluating EAOC
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$(1,400,000)
$(1,200,000)
$(1,000,000)
$(800,000)
$(600,000)
$(400,000)
$(200,000)
$-
Isothermal withBFW Adiabatic
Isothermal withDowtherm A
EAOC
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Reactions - Discussion
Different one and two reactor cases checked
Two reactors in series
No advantage in conversion or total volume to breaking up the reactor
Two reactors in parallel
Parallel would be required if a pressure drop were too large
Unnecessary in this case
One reactor
Chosen as the optimum
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Reactions - Discussion
Then conversion optimized
Lower conversion require large recycle
High conversion needs no recycle
Best EAOC at 99.5% conversion
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$(14,000,000.00)
$(12,000,000.00)
$(10,000,000.00)
$(8,000,000.00)
$(6,000,000.00)
$(4,000,000.00)
$(2,000,000.00)
$-
$2,000,000.00
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
Reactor Conversion
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Reactions - Discussion
Temperature was optimized
Temperature changed
Stripper steam ratio changed until the column
would converge
EAOC evaluated
Best EAOC at 250°C
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$(40,000,000.00)
$(35,000,000.00)
$(30,000,000.00)
$(25,000,000.00)
$(20,000,000.00)
$(15,000,000.00)
$(10,000,000.00)
$(5,000,000.00)
$-
236 238 240 242 244 246 248 250 252
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Reactors - Discussion
To better understand the reactor, profiles were
created
Temperature
Partial Pressure
Conversion
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Case Study - Corrected Kinetics
CHEMCAD Kinetics originally incorrect
Values were changed to negatives automatically
Correct Kinetics modeled using Matlab
Resulting Volume for one Reactor at 99.5%
Conversion was 11,000 m3, assuming a
Temperature of 250 °C
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Conversion
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Temperature
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Pressure
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Optimizations
General Optimizations
Heat Integration
Three Heat Exchangers were placed after the
reactor for the production of steam
$10.5 million/year in HPS
$826,000 /year in MPS
$728,000 /year in LPS
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Optimizations
Compression Ratios
Using the Grid Search Method the optimum Ratios
were found to be:
Compressor 1: 2.6
Compressor 2: 2.4
Compressor 3: 4.076
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Optimizations
General Optimizations
Recycle Ratio
Used to keep unreacted ethylene within the system
High conversion, no recycle
Low conversion, high recycle
Because conversion was so high, recycle was eliminated
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Optimizations
Base Case EAOC: $222 million/year
Largest utilities costs:
HPS
Ethylene
Largest equipment costs:
Compressors
Heat Exchangers
Optimized EAOC: $(36.9) million/year
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Ethylene74%
BFW1%
MPS10%
Electricity13%
Deionized Water
2%
Utilities Costs
Ethylene Boiler feed water
High pressure steam cost Medium pressure steam
Cooling Water Waste Water Treatment
Electricity Deionized Water
Compressors20%
Separations Equipment
1%
Heat Exchangers
22%
Reactor26%
Catalyst31%
Equipment Cost
Compressors Separations Equipment Pumps
Heat Exchangers Reactor Catalyst
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$(50,000,000) $- $50,000,000 $100,000,000 $150,000,000 $200,000,000 $250,000,000 $300,000,000
ethylene
HPS
MPS
Electricity
Boiler feed water
Dionized water
Equipment (per yr.)
EAOC
Optimized Base Case
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Overview
Introduction
Base Case
ChE 312 – Separations
Results and Discussions
ChE 325 – Reaction Engineering
Results and Discussions
Case study – Correct kinetics
Optimizations
Conclusion and Recommendations
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Recommendations
Recommended to build plant
Profits are expected to increase with a good
outlook on the market
Plant would be a good investment
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Conclusions
Base case
Losses of $222 million/yr.
Optimized case
Profits of $36.9 million/yr.
Change of $258.9 million/yr.
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Any Questions?