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UNIVERSIDAD NACIONAL DE CALLAOFACULTAD DE INGENIERA QUMICA

SIMULACIN PARA INGENIERA DE PROCESOS

Por: AGUILAR CAMPOMANES, BeatrizCASTILLO FRANCO, AnthonyCHIPA SAAVEDRA, MiguelMEDINA BURGA, Brenda

PUCHULAN CARQUN, Cesar

RAMOS BALVIN, KatherineSANCHEZ GUZMAN, MayraTORRES ANAYA, Andy

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OBJETIVOS DEL CURSO

GENERAL PURPOSE : To provide theoretical and practical basesfor the implementation of the Process Simulation (using HYSYSASPEN ) in the hydrocarbon industry .

SPECIFIC OBJECTIVES : - Strengthen knowledge of basicprinciples (mathematics, thermodynamics, mass and energybalances , etc.) Process Simulation . - Getting to Aspen Hysysenvironment and recognition of its powerful tools for processsimulation. - Simulate transfer operations of momentum , heat

and mass . - Recognize the usefulness of the logical tools ofAspen Hysys ( Adjust, Balance , Set, Recycle, etc ) . - Check withthe utility of applications in industry Aspen Hysys Refining ofPetroleum and Natural Gas Processing

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the simulation system is to recreate or imitate reality designing a model and

performing experiences with him , in order to understand the behavior of the

system or evaluate new strategies -within the limits imposed by the way ( s )

criteria ( s ) - for system operation .

In process engineering, simulation can be defined as a technique to rapidly

assess a process based on a representation of it using mathematical models , in

which the solution of these models is carried out by means of computer programs

.

Due to the complexity of real problems in the chemical process industry ( in

which the number of variables and number of equations to be solved can be on

the order of thousands ) , simulators and computer software are essential tools

.

Although in the beginning the process simulation was focused principally forindustrial oil refining , natural and petrochemical gas, its application has been

extended to other industries such as food , synthetic fuels , pulp and paper,

cement , metals , minerals , etc.

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Typical objectives of a simulation : Assess the system behavior

and predict outcomes under different conditions and situations (

ANALYSIS ) .

-Confirm Desirability of implementing new operations and / or

processes ( DESIGN ) .

-Sugerir Modifications to improve system performance and for

achieving the expected results ( OPTIMIZATION )

Simulation programs are very reliable in their

results , however , given the wide variety ofoptions , data and thermodynamic models ; isnecessary to apply a strict judgment and soundengineering judgment to evaluate the results andvalidate them.

The simulationsoftware notthink!

The softwarejust does themath , engineereverything else!

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Software and User Interface

CAPE- OPEN standards are basic rules for the development of communication

interfaces of software components for process modeling , especially developed

for the design and operation of chemical processes. These standards are basedon universally recognized software technologies , such as COM and CORBA .

The advantage of CAPE- OPEN is that they are used by many process

simulators , such as Aspen Plus , Aspen Hysys , ChemCAD , Unisim ,

ProsimPlus , ProMax Pro II , Design II , etc.

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ASPEN PLUS

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Basic steps for performing a simulation in Aspen Hysys

1. - Start program.

2. 2. - Create a new project.

3. 3 - State the chemical compounds involved in the simulation.

4. 4. - Choosing the thermodynamic model .

5. 5. - Enter the simulation environment .

6. 6 - Create the flowchart of the process. 7

7. - declare the conditions of feed streams .

8. 8. - define operating parameters for each team.

9. 9. - process specifications ( design specifications )10.10. - Generate the report and / or final report.

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1.- Start program. From Start / All Programs / Apen Tech / Process Modelling

V7.3 / Aspen HYSYS , from the desktop ( shortcut) or any other custom location .

It is recommended ( immediately after opening Aspen Hysys ) , establish the

system of units with which he goes to work . At this point , you should also set all

preferences for simulation.

To do this, follow the path: Tools / Preferences

The system of units can be chosen tab : Variables -Aspen Hysys works with the

International System (SI) by default , however , are also available metric and

English systems. -Additionally Can customize units to use by clicking Clone .

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2.- Create a new project From the menu bar , go :

File / New / Case or Ctrl -N to open the Simulation window Basis Manager.

3. declare the chemicals involved in the simulation. Therefore, in the Components leaf

Press Add and choose the compounds. You can see the basic properties of each

component by selecting it and View by pressing Component.

You can see the basic properties of each

component by selecting it and clickingView Component. ( Properties reviewsnormal boiling point, physical properties, transport , thermodynamic ,correlation coefficients for vaporpressure, enthalpy , etc.)

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4. Choosing the thermodynamic model

Fluid Pkgs allows us to choose the ( the

) model ( s ) Thermodynamic ( s ) to

used in the simulation.

If you have doubt regarding that use thermodynamic models ,Aspen Hysys includes a wizard to select it. To do this, click

Launch Wizard Properties

5.- Enter the simulation environment Todo this, press the Enter SimulationEnvironment button.

Click here

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7 - declare the conditions of feed streams . Double clicking on the arrow the

properties window to begin reporting data opens .

The entered data is displayed , Blue . Thedefault values and / or editable are Red and

the values calculated by Aspen Hysys (whichcan not be changed ) appear in Black

Aspen Hysys , unlike other simulators , twokinds of currents is used :

1 Current field (blue arrow )

2 current energy (red arrow)Flows of matter and energy can beadded in a same way as any icon onthe Object Palette , however , toavoid the time making connections ,you usually add them directly fromthe properties window of eachequipment / tool ( icon) .

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8. - define operating parameters for each team. These are generally available

data ( operating conditions ) , are entered into the computer properties window ,

which is accessed by double clicking the icon or by right clicking Wiew selecting

Properties .

9. - process specifications ( design specifications ) Is related to the results that

are desired and conditions that must be met necessarily to achieve them. This isProduct Specifications , technical specification ASTM standards equipment, etc

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9. - Generate the report and / or final report. The results of the simulation for

each current or team can be seen in the same properties window each . The

overall results of the simulation (balance of matter and energy ) can be see in

the Workbook

For all results ( in PDF format) ,such as : Specification sheet foreach team , material balances ,energy, etc. You must follow thepath: Tools / Reports / edit /insert data sheet / ...

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The choice of thermodynamic models to be used in a simulation is perhaps the

most important task to achieve optimal results .

Therefore, if you have questions about which model to use , Aspen Hysys

includes a wizard to perform this important task , which can be accessed byclicking Launch Wizard Properties tab of the setup window the fluid package .

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Previously it was necessary to stop a good time to analyze and decide that

thermodynamic model used , therefore, was a common practice to review a book

of thermodynamics and / or follow recommended by authors of scientific articles.

Today, thanks to Assistant - Property Package Selection , you can save a lot of

time and effort.

In any case , you can access the help window for a detailed description of each

of the thermodynamic models he works with this simulator

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Finally , when required , it is advisable to employ decision trees, such as

suggesting Elliott and Lira (1999) *

*Elliott and Lira (1999). Introduction to Chemical Engineering

Thermodynamics, Prentice Hall, 1999.

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We begin with applications!!!

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Example 1 : For a closed system , in which an

equimolar mixture of ethanol - water at equilibrium

at 40 C and with a vaporized fraction is 0.3 ; is to

be determined : The pressure of the system andwhat are the compositions of ethanol / water are

in liquid and vapor phases ?. Create a new case,

using NRTL as Fluid Pakgs . Create a stream and

assign the data indicated . - The pressure is

estimated immediately (automatically ) - View the

compositions in compositions .

Results: Pressure: P = 16.45 kPacompositions:

COMPONENTES FRACCIN MOLAR

F. Lquida

Etanol 0.63721 0.441196

Agua 0.36279 0.558804

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NOTE : It is known as a static equilibrium condition, where , over time , there

occurs any change in the macroscopic properties of the system, which implies a

balance of all the potential that may cause change.

THE FAMOUS RULE STAGE ( phase equilibrium ) To describe the equilibrium

state of a Various "closed system" of several phases and must know the

chemical species number of independent intensive variables defining the system

. For this number , the phase rule applies : L = F + C- 2; where L is the number ofindependent intensive variables ( degrees of freedom ), C the number of

components chemical system and F the number of phases present in the system

source: Introduction to Chemical Engineering Thermodynamics . J. M. Smith , H.

C. Van Ness , M. M. Abbott. McGraw Hill . Seventh edition, 2007 .

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GENERALIZATION OF THE PHASE RULE In general , to start solving the

mathematical models the number of independent equations must equal the

number of variables and / or unknown parameters . Since the number ofvariables and / or parameters is almost always greater than the number of

independent equations ( available ) , you need to give values to a group of

variables to the model to be solved. The number of variables and / or parameters

set is known as degrees of freedom of the system or model .

ND = NV - NE where : ND : Number of degrees of freedom NV : Number ofvariables NE : Number of independent equations Nor is it to give values to any

variable and / or parameter. In a real system variables normally have value ( are

fixed ) are those corresponding to the input currents and can be intensive

(composition , pressure, temperature , etc.) or extensive ( flows of matter , heat )

. The parameters may be : size of the equipment , number of steps , etc.

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Analysis of Current An actual current and different phases may contain

no necessarily be homogeneous , for analyzing the real or physical currents

must be broken into lines homogeneous phase currents .

In a homogeneous phase stream and C components can define following

variables: Intensive : molar fractions (X1, X2 , X3, ......., XC)

C pressure 1 Temperature

1 Extensive : Stream 1

molar Variables of a stream : NV = C + 3

The only equation is the sum of molar fractions equal to 1 : ( Xi = 1) Degrees ofFreedom : ND = C + 2 Then: For a homogeneous phase current is fully specified

(you know all about it ) will need to set ( add value ) to C + 2 variables.

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Example 2: Estimate the highest pressure and

temperature that may be vapor-liquid equilibrium of

the mixture of 60 % C1 , 20 % C2 , 10% C3 , 5 % n -

C4 and 5 % n - C5 . [ Hougen et al. "

Thermodynamics " , p.420 ] In addition . Developequilibrium diagram P -T Create a new case, using

the model of Lee- Kessler- Plocker as Fluid

Package. Create a stream and assign the indicated

composition and molar flow either .

This causes no problem, since the properties are intensive compute

In Tools / Utilities / Envelope utilities select currentand click ok See P , T maxims : Design / CriticalValues / Maxima See graph : Performance / Plots :

Envelope Type PT

Resultados:Pmax= 121.1 bar, Tmax= 70.04 C

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Example 3: For the data of the previous problem , develop a profile of density,

heat capacity , etc. depending on the temperature .

Since the current to estimate the properties is alreadydefined ( above problem ) . From Tools / Utilities ,select Property Table List utilities available ( AvailableUtilities) and click the Add Utility button. 'InConections set the current for which are to estimatethe properties ( stream Select button) and specify the

independent variables (Vapour Fracc. , Temperature ) -In Dep.Prop specify the dependent variables.

Finally click on Calculate and see the results inPerformance.

Results: Density profile

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Example 4: A hydrocarbon distillate ( = 43.7 lb / ft3 , MW = 120 ) is carried at

70 F and 200 psig . For purposes of design of piping and equipment , you want

to know the transport properties (Cp , thermal conductivity , viscosity, etc.) of said

mixture.

Create a new case , create pseudo -component and add it to the Components list.Using the equation of PR as Fluid Pkgs . Enterthe simulation environment , create anddeclare their current conditions (P , T). The

properties are calculated in the Propertiessheet.

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NOTE : Creating Pseudocomponetes When you have a mixture of chemical

compounds, of which the exact composition is not known , but if you are also

provided values such as density, viscosity, apparent molecular weight, etc.

Declaring that information , Aspen Hysys can " establish" a layer

pseudocomponent it adequately represent the thermodynamic behavior,transport , etc. of said mixture. The software uses correlations according to the

type declared ( solid, hydrocarbon, alcohol, etc. ) to estimate how all other

"properties" precisely as possible compound.

In the Components tab of the Basis ManagerSimuation window , and click the Add button. Selectedtab in the popup window ( HYSYS Component ListView) , select Hypothetical list below and click the AddComponent Manger Hypo button. In the popup

window, click the Add button to open the saleHypoGroup . In HypoGroup window , click Add Hypo,then click the View tab to open and declareHypo20000 available information. Finally Click theEstimate Unknown Props button.

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Example 5 : Create a stream of matter containing only water with the following

conditions: Flowrate : 100 kgmole / h Pressure : 1 atm Steam / Phase Fraction :

1.00

1.- What is the temperature of the system ? Repeat the above procedure byreplacing the pressure at 150 C

2.- What is the pressure of the system? For P = 4 atm ,

3.- At what temperature should the water to have a quality of 40 %. ?

CASO PROPIEDAD

Valor Unidad

1 211.9 F

2 0.252 atm

3 291.3 F

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MIXER (MIXER )

The mixer combines multiple streams of feed material (at different

thermodynamic conditions ) to produce a single output stream , which pair

rigorously calculates the temperature , enthalpy , pressure , composition of the

output current, or of any of the currents entrance .

Example 6 The line of light distillates two primary columns operating in parallel

are joined before entering the storage tank. Obviously , their compositions and

properties are not equal. Additionally, because of the different paths , the

pressures and temperatures at the time of joining , are different. Determining the

properties of the current resulting from the mixture . Use the following

information: Components n - C5 n -C6 n - C7 n - C8 n - C9 -C10 n P ( psi ) T ( F) GPM Current 1 ( % mass ) 5.0 10.0 25.0 30.0 20.0 10.0 30.0 100 20 Current 2

(mass% ) 6.0 11.0 24.0 31.0 20.0 8.0 24.0 90 22

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Create a new case , declare components , using the SRK equation as Fluid Pkgs

. Enter the simulation environment to set the PFD .

Assign the composition , pressure , flow and temperature at the inlet streams .Sign mixer properties window and make connections in the Design tab ,

Conections sheet.

View results on the Worksheet.

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FLASH DISTILLATION ( INSTANT ) These units can also be used to simulate

chemical reactors .

Example 7 1 kmol / hr of a stream containing benzene ( 40 % mol) , toluene (30%mol) and o- xylene (30% mol) at 373 K and 1 atm is subjected to adiabatic flash

distillation . Determining the flow and composition of the fluid current andgenerated steam . Disparaging pressure drop in the reservoir.

Create a new case , declare components , using theSRK equation as Fluid Pkgs . Enter the simulation

environment to set the PFD . Assign the composition ,pressure , flow and temperature at the inlet stream .

Resultados:

COMPONENTES Mole fraction

F.LQUIDA F.VAPORBenzene 0.2117 0.4956

Toluene 0.2925 0.3038

O-Xylene 0.4958 0.2006

Flujo (kgmol/H) 0.3368 0.6632

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