Aspen Plus - Intermediate Process Modeling (3 of 3) (Slideshare)

a) Getting Results
b) Plotting Data
c) Design Spec
d) Sensitivity Analysis
e) Optimization & Constraint
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 i. Overall Results: (Summary, Block, Stream)
 ii. Adding T/P/M labels & Results Table in flowsheet
 iii. Reports

 Stream Results
 Block Results
 Results Summary

 After running the simulation:
 Streams will be calculated
 All thermodynamic property will be present
 You can access it:
 Navigation Panel  Streams  X Stream  Results
 Flowsheet  Right-click  Stream Results
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 After running the simulation:
 Block Calculations will be obtained
 Main result swill be available
 This depends on the type of Unit Operation/Block
 You can access it:
 Navigation Panel  Blocks  X Block - Results
 Flowsheet  Right-click  Results

 Total Results Will be obtained after running the simulation
 This is the result of al calculations:
 Stream
 Convergence
 Block Results
 Access it via:
 Navigation Panel  Results summary
 Home Tab  Stream Summary

 Open any simulation we have bene working with,
 WKS Sep1 and Sep 2
 Part 1) Get Stream results
 Part 2) Get Block results
 Part 3) Get Results Summary

 i. Overall Results: (Summary, Block, Stream)
 ii. Adding T/P/M labels
 iii. Results Table in flowsheet

 There is the possibility to add “labels” to the streams/blocks
 Typical Data:
 As well as Q/W flows
 Simulation must have “RESULTS”
 i.e. it has been ran already
 Other Properties can be added:
 Property Sets
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 Other Properties can be added:
 Property Sets
 Limited to 6 labels
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 PART 1:
 Add a Stream Results conditions of any previous simulation
 WKS Sep1 + Sep2
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 PART 2:
 Add Custom Properties
 Property Set 
 PS-1  Viscosity of Mixture (MUMX, Liq.)
 PS-2  Thermal Conductivity of Mixture (KMX, Liq)
 PS-3  Specific Heat Capacity of Mixture (CPMX, Liq)
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 PS-1  Viscosity of Mixture (MUMX, Liq.)
 PS-2  Thermal Conductivity of Mixture (KMX, Liq)
 PS-3  Specific Heat Capacity of Mixture (CPMX, Liq)

 Result Tables can be added to the Flowsheet:
 This is very useful when performing results
 Avoids loss of time
 Can be printed
 Can be customized
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 For any WKS simulation we have worked:
 WKS  Sep1 and Sep2
 PART 1:
 Add Results to the Flowsheet
 PART 2:
 Add  Flowsheet View to “Plant”
 Add  Flowsheet View to “Table”
 Add  Flowsheet View to “ALL”
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 PART 3:
 Customize your table:
 Add:
 Fugacity
 CP/MU
 Re, Pr Numbers
 Remove
 Solid properties
 Mass/Volume properties

 Plenty of properties can be plotted once the results are present
 Physical properties (seen in Section 2)
 Simulation environment, i.e. Results
 Common units to plot:
 Reactors
 dP, Change in concentration, Flow rate variation, Temperature profile, etc…
 Catalyst
 Columns
 dP, Change in concentration, Flow rate variation, Temperature profile, etc…
 Packing vs. Tray Design spec.
 Volatilities, K-Values
 Use the PLOTTING TOOL
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 Use the Plotting Tool from the Home tab of the ribbon to quickly generate plot results
of a simulation.
 You can use the Plotting Tool for displaying results for the following operations:
 Assay data analysis (Phys.Prop.Env.)
 Physical property analysis (Phys.Prop.Env.)
 Data regression analysis (Phys.Prop.Env.)
 Profiles for all separation models including RadFrac, MultiFrac, and PetroFrac (Sim.Env.)
 Sensitivity analysis (Sim.Env.)
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 Use the Plotting Tool to create plots of temperature, flows, and compositions
throughout the block

 There are some “default” Plots
 Custom plots can be created as well!
 Others can be assigned by selection
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 Hydraulic Plots
AP. V10

 Open simulation:
 WKS RadFrac3 - Column Internals, Trays vs Packings
 Verify what can be plotted.
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 WKS RadFrac3 - Column Internals, Trays vs Packings

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 WKS Adiabatic vs. Isothermal PFR

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 Introduction to Manipulators
 Design Spec
 Define, Spec, Vary
 Convergence Notes

 Are used to manipulate mathematical concepts / formulas in the Flowsheet
 Stream manipulators modify or change stream variables for convenience.
 They do not represent real unit operations.
 Convenience for the user

 Allows user to set the value of a calculated flowsheet quantity to a particular value by
manipulating a specified input variable
DSNSPEC
Operatorinput Output

 Similar to a feedback controller
 Allows user to set the value of a calculated flowsheet quantity to a
particular value
 Objective is achieved by manipulating a specified input variable
 Location
 Navigation Pane  Flowsheeting Options  Design Specs
 Design specifications change the simulation results
DSNSPEC
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 Design Spec blocks (and Calculator/Transfer blocks) can be placed on the PFD using
icons on the Manipulators tab of the Model Palette
 Dashed connection lines will indicate the unit operation models and streams affected by
these blocks
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 Display can be toggled on/off from:
 File  Options  Flowsheet dialog box or Flowsheet  Modify ribbon Display Options group

 Modify Tab  Display Options
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 Forms:
 Define
 Spec
 Vary
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 Define:
 VARIABLE(S) input by user
 Category: Stream, Block, Utility, Property Parameter, Reaction
 Reference:
 Type:
 Stream:
 Substream:
 Component:
 Units:
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 Spec:
 The specification/value required
 Spec = the stated VARIABLE
 Target = the required value
 Tolerance = (value for iteration, i.e. +/- x)

 Vary:
 VARIABLE(S) manipulated by Aspen Plus (DesignSpec)
 Manipulated Variable:
 Type
 Stream
 Substream
 Component
 Units
 Manipulated var. limits:
 Min.
 Max.
 Step size/ No Steps

 Only quantities that have been input to the flowsheet should be manipulated
 The calculations performed by a design specification are iterative
 Providing a good estimate for the manipulated variable will help the design specification
converge in fewer iterations
 This is especially important for large flowsheets with several interrelated design specifications
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 Viewing results of a design specification
 Design-Spec Results form
 Results Summary | Convergence | DesignSpec Summary
 Convergence | Convergence and by choosing the Results form in the appropriate solver
block
 The final values of the manipulated and/or sampled variables can be viewed directly on the
appropriate Stream or Block Results forms

 If a design-spec does not converge:
 Check to see that the manipulated variable is not at its lower or upper bound
 Verify that a solution exists within the bounds specified for the manipulated variable,
perhaps by performing a sensitivity analysis
 Ensure that the manipulated variable does indeed affect the value of the sampled variables
 Provide a better estimate for the value of the manipulated variable
 Narrow the bounds of the manipulated variable or loosening the tolerance on the objective
function to help convergence
 Make sure that the objective function does not have a flat region within the range of the
manipulated variable
 Change the characteristics of the convergence block associated with the design-spec (step
size, number iterations, algorithm, etc.)
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 Open:
 WKS Radfrac1 C3-iC4 Separation
 Initial Purity of Propane (C3) in distillate is 98.5%
 Use Design-Spec Block to:
 Verify the Reflux Ratio (MOLE-RR) for a 99.5% purity
 Verify Number of Stages for a 99.5% purity
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 Open:
 WKS R-Gibbs Competing Reactions
 Change Temperature  Increase Yield to 18.0%
 Find T

 OPEN:
 Change:
 Diameter  48.5% of ketene (current is 44%)
 Length  increase total yield of acetone to 12 kmol/h of ketene (current is 10.8 kmol/h)
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 i. Sensitivity Analysis
 ii. Methodology
 iii. Plotting

 Tool used to change a “sensitive” property  changes a specific results
 Allows user to study the effect of changes in input variables on process outputs
 Plot results to easily visualize relationships between different variables

 Applications
 Studying the effect of changes in input variables on process (model) outputs
 Graphically representing the effects of input variables
 Verifying that a solution to a design specification is feasible
 Rudimentary optimization
 Studying time varying variables using a quasi-steady-state approach
 Doing case studies
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 Location:
 Home Tab  Analysis  Sensitivty
 Sim. Env.  Naviation Panel  Model Analyisis Tools  Sensitivity
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 Typically:
 Select (input) variable (VARY) and Range
 Select (output) variable (DEFINE)
 Select Tabulation requirements (default is automatic)
 Run Sensitivity Analysis

 Step 1A: Fill up the VARY tab
 Input variable to vary
 Type of Variable
 Stream, Block, etc…
 Select vary range
 Start – Finish Points
 Increment/No. points
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 Step 1B: Fill up the VARY tab
 If only CASES are required…
 Select “CASES” and a new tab will appear
 For this option, each row in the grid on this sheet
represents the specifications for one case to be run.
 If any values are unspecified, the base case values for
those variables are used.
 The total number of runs will be the number of rows in
this grid, plus one if the base case is specified to be run
on the Optional sheet.
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 Step 2: Fill up the DEFINE tab
 OUTPUT variable
 Type of Variable
 Stream, Block, etc…
 Specify Reference
Variable
Category
Type of Variable
Blocks Block variables and vectors
Streams Stream state variables, component
flows and composition variables
Model Utility Parameters, balance block and
pressure relief variables
Property Property parameters
Reactions Reactions and chemistry variables
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 Step 3: Fill up the TABULATE tab
 Autofill
 Or… Select custom data

 Sensitivity blocks provide information in addition to the base-case results but have no
effect on the base-case simulation itself.
 Only streams that are feeds to the flowsheet should be varied or modified directly
 If duty is specified for a block, that duty can be read and written using the variable
DUTY for that block
 if the duty for a block is calculated during simulation, it should be read using the variable
QCALC
 PRES is the specified pressure (input) or pressure drop
 PDROP is pressure drop used in calculating pressure profile in heating or cooling
curves (calculated)
 Flowsheet result variables
 (calculated quantities) should not be overwritten or varied

 Plots can be generated of Sensitivity Analysis Cases
 For a second Vary
select Parametric Variable
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 STATEMENT:
 A Hydrocarbon mixture is to be flashed and analyzed. (0.35, 0.25. 0.20, 0.15. 0.05).
 There is a compressor, 0.87 isentropic efficiency
 There is an exchanger, no pressure drop
 Setup is initially at P = 20 bar, T = 50°C
 Use Peng-Robinson Model
 S.A.1:
 Change P compressor vs. composition
 S.A.2:
 Change T exchanger vs. comp

 STATEMENT:
 A Hydrocarbon mixture is to be flashed and analyzed. (0.35, 0.25. 0.20, 0.15. 0.05).
 There is a compressor, 0.87 isentropic efficiency
 There is an exchanger, no pressure drop
 Setup is initially at P = 20 bar, T = 50°C
 Use Peng-Robinson Model
 S.A.1:
 Change P compressor vs. composition
 S.A.2:
 Change T exchanger vs. comp
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 Open WKS - RadFrac3 Column Internals, Trays vs Packings
 Prepare Sensitivity Analysis for:
 S-1 : Vary Feed Stage (1-9); verify Purity of Distillate
 S-2 : Vary Reflux Ratio (1.5-5); verify Purity of distillate
 S-3 : Vary Operating Pressure (Stage 1 – Condenser P = (18.4-184); verify Purity of distillate
 Graph each result
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 Defined variable is the same for all (Purity of Distillate)

 S-1 : Vary Feed Stage (1-9); verify Purity of Distillate
ERROR  Stage 1 is the condenser (can’t feed there)

 S-2 : Vary Reflux Ratio (1.5-5); verify Purity of distillate

 S-3 : Vary Operating Pressure (Stage 1 – Condenser P = (18.4-184); verify Purity of distillate

 Open:
 WKS Adiabatic vs. Isothermal CSTR
 Use Sensitivity Analysis for:
 S.A.1  Effect of Temperature in isothermal design  PROPA-01 purity
 S.A.2  Effect of Feed Temperature in Adiabatic Design  PROPA-01 purity

 Optimization
 Constraint

 Use optimization to maximize or minimize a user-specified objective function by
manipulating decision variables
 feed stream
 block input
 other input variables
 The objective function can be any valid Fortran expression involving one or more
flowsheet quantities.
 The tolerance of the objective function is the tolerance of the convergence block
associated with the optimization problem.
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 Forms:
 Define
 Objectives & Constraints
 Vary
 Fortran (optional)

 Forms:
 Define
 Objectives & Constraints
 Vary
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 Flash Optimization
 Open WKS – Sensitivity 1
 Objetive:
 Optimize Temperature/P  Increase % purity
 NOTE: Do not add any constraint
www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=1KMfHHz2H4A

 You have the option of imposing equality or inequality
constraints on the optimization.
 Equality constraints within an optimization are similar
to design specifications.
 The constraints can be any function of flowsheet
variables computed using Fortran expressions or in-
line Fortran statements.
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 You must specify the tolerance of the
constraint.
 Tear streams and the optimization problem
can be converged simultaneously or
separately.
 If they are converged simultaneously, the
tear stream is treated as an additional
constraint.

 Forms:
 Define
 Spec
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 Forms:
 Define
 Spec

 An equimolar BTX mixture is to be separated.
 The separation is to be maximized according to market prices
 BTX = Benzene, Toluene, O-Xylene
 Method  PR
 Price List:
 Liquid phase:
 Benzene = $5.00
 Toluene = $7.00
 Xylene = $10.00
 Vapor phase:
 Benzene = $10.00
 Toluene = $5.00
 Xylene = $9.00
BP:
B < T << X

 Recommended Operation
 T = 110°C, P = 1 bar
 (A) Use Optimization to maximize the products
 Tip  Get to know min and max boiling point of mixture
 Find Profit
 (B) If the heating system can only provide:
 2163768.77 cal/s
 Find Actual Profit
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a) Hydrodealkilation of Toluene
b) Nitric Oxide Plant
c) Isobuthene Production
1. Problem Statement
2. Flowsheet Building
3. Getting Results
4. Analysis and Optimization

1. Problem Statement
2. Flowsheet Building
3. Getting Results
4. Analysis and Optimization

 Tutorial17
https://www.youtube.com/watch?v=ZHviZ41DEpI

 Toluene will be hydrodealkylated in order to produce benzene, which is later converted to
diphenyl for further processing
 The feed is initially pre-heated, then goes into an Isothermal Reactor.
 The products are cooled and separated.
 The Gas stream is further separated into H2 and CH4
 The liquid stream is of interest (benzene-toluene-diphenyl mix)
 The liquid stream is pumped in order to separate the B-T-DP mix
 Benzene product is obtained in distillate
 Bottom mixture (Toluene-Diphenyl)
 The liquid stream is then flashed
 Vapor product is mostly diphenyl
 Liquid product is mostly Toluene…

 Design Spec.
 Will be used in order to increase yield/purity of products
 Components:
 Toluene, H2, Benzene, C1 (methane), Diphenyl
 Property Method
 Peng Robinson
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 Units
 Reactor – Converts Toluene to diphenyl and benzene
 Presep  Separates volatile vs. gases
 Flash Drum  Separates Hydrogen gas from methane Gas
 Distil-1  Separates Benzene
 Flash separates Diphenyl from Toluene
 Heater, Pumps are used in order to set P/T in process
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 FEED  30ºC, 1 bar, 1000 kmol/h (60%T,40%H2;mol frac.)
 HEATER  (HEATER) 34bar, T= 895K
 Reactor 
 (R/GIBBS)  Reactor with specified T, T=700ºC
 Cooler  (HEATER) T = 40ºC, P = 33 bar
 PreSep (SEP) Split Vapor  1.0 H2, 1.0 CH4
 SepGas (SEP) Split Liq  1.0 CH4
 Pump  (PUMP) Discharge P = 2 bar
 DISTL  (DISTIL)
 No Stages = 27, Feed = 14, Ref. Ratio = 0.904, D:F ratio=0.5249, Cond = Total, P = 2 bar
cond/boil
 FLASH  T = 200C, P = 2bar
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 Run#1:
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 Run#2:
 Try to get this layout:

 Sep1 (De-gaser)
 H2 and Methane must go as vapors (stream 6  vapor)
 Sep1 (dehydrogenation)
 H2 must go as vapor (stream 8  vapor)
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 Pump  2 bar (discharge P)
 Distil
 N = 27, F = 14, RR = 0.904; D:F = 0.5249
 Total Condenser, Pcond = 2bar, Pboil = 2bar
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 Run#3
 Lets Add DesignSpec
 DS-1
 Var=A
 Ref
 Type: Mole-Flow, Stream: BENZENE, Component: BENZENE, Units: Kmol/hr
 Spec= A
 Spec: BENZ, Target = 165, Tolerance =0.1
 Vary
 Type: Block-Var
 Block: DISTIL
 Variable: D:F ratio
 Manipulated limits  Min -1, Max 1, Step = 1
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 Use Design Spec  Fix Distil column
 Benzene Content in Vapor Stream (S=16)
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 D:F Ratio goes form 0.409  0.432Enjoying the slideshow?
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 Flash  T = 260°C, P = 2bar

 Run#4  Try to change Flash T  Sensitivity Analysis purity
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 Run#4  Try to change Flash T 
 Sensitivity Analysis purity
 At least 95%  T = 264°C
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 Rate & Purity of Benzene Product?
 Rate & Purity of Diphenyl Product?
 Heat duties
 Heaters/coolers
 Column  Reboiler/condenser
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 Now… Try to recover / recycle gases from Hydrogen gas / Toluene  Raw Materials
 Fsplits:
 70% for Hydrogen gas recovery, 90% for Toluene Recovery
 HEATERS = 895K, P = 34 bar
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 Rate & Purity of Benzene Product?
 Rate & Purity of Diphenyl Product?
 Heat duties
 Heaters/coolers
 Column  Reboiler/condenser

www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=xSKRdquNvEI

 Nitric Oxide is to be produced from ammonia and air via oxidation.
 There are several side reactions / reversible reactions present
 Components: NH3, O2, NO, H2O, N2
 Method: NRTL-RK
 FEED1: 150C, P = 8 bar, 30 kmol/h, 100% NH3
 FEED2: 150C, P = 8 bar, 970 kmol/h, 79% N2, 21%O2

 (a) Build flowsheet
 Add Heating system
 Add Recycle Streams
 (b) Use design specification / sensitivity analysis in order to set up required conditions
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 RXN1
 Config Tab:
 Class: Equilibrium
 4NH3+5O2 4NO+6H2O
 Equilibrium Tab
 K1= 10^10  ln(10^10)=A = 23.03
 Vapor, T = 900C, Compute Keq from built-in expression, A = 23.03
 RXN2:
 Config Tab:
 Class: Equilibrium
 2NH3+3/2O2  N2+3H2O
 Equilibrium Tab
 K2 = 10^15  ln(1015)=A = 34.54
 Vapor, T = 900C, Compute Keq from built-in expression, A = 34.54
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 Heater: (HEATER) T = 900C, P = 8bar
 Reactor; (R-CSTR) T = 900C, P = 8bar, Vap-Only
 Residence Time= 30s
 Cooler (HEATER) T = 40C, P = 8bar
 Flash (FLASH2) T= 40,P = 8bar
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 Run#1:
 Reactor & Flashing

 Feed
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 Heater
Cooler

 CSTR
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 Flash

 Run simulation:

 Sensitivity Analysis  Verify best TEMP for Flash
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 Add sensitivity analysis
 S-1
 Vary Tab
 Active; Variable = 1; Type: Block-Var; Block: FLASH; Variable: Temp; Unit C... Limits: low=0, upper=100,
points 100
 Define Tab:
 Tabulate Tab:
 FLAH20, FLANO

 Sensitivity Analysis  Verify best TEMP for Flash
www.ChemicalEngineeringGuy.com T-flash = 58°C
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 Run simulation:
T= 58°C
T= 58°C

 Run#2 
 Recycle & Heating System
 Objectives:
 Decrease Heat duty
 Recycle NH3 for CSTR

 Verify:
 Recycle Ratio
 Heating data of system
 Separator efficeincy
 What is next?
  separate No from S9

 Run3:
 NO-Purifier
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 Isobutene is to be produced from Isobutane (double bond)
 It is reacted with methanol and ethanol in the manufacture of the gasoline oxygenates
methyl tert-butyl ether (MTBE) and ethyl tert-butyl ether (ETBE), respectively
 Components
 Isobutane, Isobutene, H2
 Method
 Peng-Robinson
 RXN:
 Isobutane <=> Isobutene + H2

 FEED1: T= 35C, P = 4bar, 100kmol/h, 100%isobutane
 Heater (HEATER) T = 550C, P = 4bar
 Cooler (HEATER) 90C, 2bar
 Separator (FLASH)  Adiabatic, Q = 0; P = 2 bar

 The available reactor has the following operations:
 Reactor (R-PLUG):
 Config Tab: Reactor with specified T, T = 550C
 Multitubular Reator  N = 10 tubes
 Dimensions:
 L = 500cm, D = 24 cm;
 Vap-Liquid phases
 P = 2 abr
 Catalyst DATA:
 catalyst loading = 1 kg
 Bed void = 0.58
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 RXN1
 Config. Tab
 Class: LHHW; Reversible Reaction
 C4H10  C4H8 + H2
 Kinetic Tab:
 Reacting phase: Vapor
 [Ci] = Partial Pressure
 [Ci] =bar Rate basis = Cat(wt)
Langmuir-Hinshelwood –Hougen-Watson(LHHW) model
𝑟 =
𝑘 𝑝 𝐴 −
𝑝 𝐸 𝑝 𝐻
𝐾
1 + 𝑘 𝐸𝐻 𝑝 𝐸 𝑝 𝐻 + 𝑘 𝐸 𝑝 𝐸
𝑘 = 8.90𝑥105
e−
112
𝑅𝑇
𝐾 = 1.4𝑥106
𝑒
−117
𝑅𝑇
𝑘 𝐸 = 2.5𝑥105 𝑒
−87
𝑅𝑇
𝑘 𝐸𝐻 = 1.2𝑥106 𝑒
−79
𝑅𝑇
𝑅 = 8.314𝑥10−5
𝑚3 ⋅ 𝑏𝑎𝑟
𝐾 ⋅ 𝑚𝑜𝑙
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 RXN
 Kinetic:
𝑟 =
𝑘 𝑝 𝐴 −
𝑝 𝐸 𝑝 𝐻
𝐾
𝑘 = 8.90𝑥105e−
112
𝑅𝑇
𝐾 = 1.4𝑥106 𝑒
−117
𝑅𝑇
𝑘 𝐸 = 2.5𝑥105 𝑒
−87
𝑅𝑇
𝑘 𝐸𝐻 = 1.2𝑥106
𝑒
−79
𝑅𝑇
𝑅 = 8.314𝑥10−5
𝑚3
⋅ 𝑏𝑎𝑟
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 Adsorption Tab:
 Term 1:
 Term 2:
 Term 3:
𝑟 =
𝑘 𝑝 𝐴 −
𝑝 𝐸 𝑝 𝐻
𝐾
𝑘 = 8.90𝑥105e−
112
𝑅𝑇
𝐾 = 1.4𝑥106 𝑒
−117
𝑅𝑇
𝑘 𝐸 = 2.5𝑥105 𝑒
−87
𝑅𝑇
𝑘 𝐸𝐻 = 1.2𝑥106
𝑒
−79
𝑅𝑇
𝑅 = 8.314𝑥10−5
𝑚3
⋅ 𝑏𝑎𝑟
ln(𝑘 𝐸𝐻) = ln(1.2𝑥106
) + ln exp
−117
𝑅𝑇
𝐴 = 13.9978, 𝐵 = −950151, 𝐶 = 0, 𝐷 = 0
ln(1) = 0
𝐴 = 0, 𝐵 = 0, 𝐶 = 0, 𝐷 = 0
ln(𝑘 𝐸) = ln(2.5𝑥105
) − ln exp
−87
𝑅𝑇
𝐴 = 12.4292, 𝐵 = −1046368.308, 𝐶 = 0, 𝐷 = 0
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 Adsorption Tab:
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 Driving Force Tab

 Run #1
 Preheat  PFR  Cooler  Flash Sep.
 Verify Results

 Run #1
 Preheat  PFR  Cooler  Flash Sep.
 Verify Results
PFR

 Run #2
• Add Recycling system
• Change Flash  Membrane
• Membrane (SEP1)
• 1.0 of H2 in of-gas
• Fsplit
• 80% recycle, 20% waste
• Compressor
• Isentropic, 4bar
• Heater Recycle: (HEATER)
• T = 564C, P = 4bar
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 Run #3
 Add Heating System (Heat-X)
 Optimize Process

 Run #3
 Add Heating System (Heat-X)
 Optimize Process
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 Run #4
 Add Purification Steps
 Try
 Flash (Flash2)
 Distillation column (RadFrac)
 Use Sensitivity analysis

 Run #4
 Try
 Flash (Flash2)
 Distillation column (RadFrac)
 Use Sensitivity analysis
 Change:
 Reflux
 Distillate Rate
 No. Stages
 Pressure
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 Run #5
 Use Membrane:
 99.5% can be separated purity can be achieved for C4H8
 0.5% of C4H10 remains in product
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 Run #5
 Use Membrane:
 99.5% can be separated purity can be achieved for C4H8
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 You learn!
 Important to use all tools!
 Simulation, Environments, Analysis Tools, etc…

 Finally! You made it!
 Congrats!
 Let’s see what you have learnt

1. Introduction
2. Flowsheet Manipulation
3. Physical Property Environment
4. More Unit Operations
5. Model Analysis Tools
6. Case Studies
7. Conclusion

a) Flowsheet Modification
b) Templates, Sub-flowsheets & Hierarchy Blocks

a) Property Methods
b) Property Sets
c) NIST TDE
d) Analysis Tools – Physical Property Environment

a) Separators
 Flash 2,3, Decanter, Sep, Sep2
b) Heat Exchangers
 Heater, HeatX
c) Columns
 RadFrac, Extract, Absorber
d) Reactors
 Rigurous Design (R-Equil, R-Gibbs)
 R-CSTR, R-Plug
e) Pressure Changers
 Pump, Compressors, Valves, Pipes

a) Getting Results
b) Plotting Data
c) Design Specification
d) Sensitivity Analysis
e) Optimization & Constraint

a) Wrap-up
b) Continue your training
c) Bonus

Aspen Plus - Intermediate Process Modeling (3 of 3) (Slideshare)

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Aspen Plus - Intermediate Process Modeling (3 of 3) (Slideshare)