Hysys Course 2022.ppt

Why ASPEN HYSYS ?
 It allows you to predict the behavior of a
chemical process by using basic
engineering relationships, such as mass
and energy balances, phase and
chemical equilibrium
 You can simulate actual plant behavior
by given reliable thermodynamic data &

 It can help in design better chemical
plants, allow you to run many cases
and perform analyses in order to
optimize existing plants and design.

Where ?
 Process simulation is used in Research and
Development for:
Interpreting bench-scale and pilot plant data
Process scale-up and feasibility studies.
 Process simulation is used in Process
Design for:
Comparing alternative process designs
Developing heat and material balances
Designing process equipment
Evaluating process performance at different
conditions

 Generally, Aspen HYSYS can Design &
Simulate real process or plant.

Special Features
 Built-in Intelligence
The Hysys property packages know when enough
information is available and perform the correct
flash calculation automatically.
 On Time Calculations

Course Outline:
 Introduction
 Propane Refrigeration Loop
 Refrigerated Gas Plant
 NGL Fractionation Train
 Oil Characterization
 Gas Gathering
 Two-Stage Compression
 Acid Gas Sweetening With DEA
 Natural Gas Dehydration with TEG
 Reporting in Aspen HYSYS

to add all the raw materials involved in the process
1- Components:
Note:
N2 + 3H2 = 2NH3
In any Chemical Reaction
You have to add both the reactants and the products

When you have established a component list, you
combine the component list with a property package.
The property package is a collection of methods for
calculating the properties of the selected components.
The combination of the component list and the property
package, along with other simulation settings, is called
the fluid package.
2- Fluid Package

The built-in property packages in HYSYS provide
accurate thermodynamic, physical and transport
property predictions for hydrocarbon, non-hydrocarbon,
petrochemical and chemical fluids.
The database consists of an excess of 1500
components and over 16000 fitted binary coefficients. If
a library component cannot be found within the
database, a comprehensive selection of estimation
methods is available for creating fully defined
hypothetical components.
2- Fluid Package

Choices for HYSYS Property
Packages
A. Equations of State (EOS):
Equation of State models have proven to be very
reliable in predicting the properties of most hydrocarbon
based fluids over a wide range of operating conditions.
Their application focuses on primarily non-polar or
slightly polar components.

Choices for HYSYS Property
Packages
The GCEOS model allows you to define and implement
your own generalized cubic equation of state including
mixing rules and volume translation.
GCEOS

Kabadi Danner
 The Kabadi Danner model is a modification of the original SRK
equation of state, enhanced to improve the vapour-liquid-liquid
equilibria calculations for water-hydrocarbon systems, particularly
in dilute regions.
 The model is an improvement over previous attempts which were
limited in the region of validity. The modification is based on an
asymmetric mixing rule, whereby the interaction in the water
phase (with its strong H2 bonding) is calculated based on both the
interaction between the hydrocarbons and the H2O, and on the
perturbation by hydrocarbon on the H2O-H2O interaction (due to
its structure).
 The Kabadi Danner model uses the Kabadi Danner method to
calculate VLE and uses SRK to calculate Enthalphy and Entropy.

Lee-Kesler Plocker
 The Lee-Kesler Plocker model is the most
accurate general method for non-polar
substances and mixtures and is recommended
for Ethylene Towers. LKP uses the Lee-Kesler-
Plocker method to calculate VLE and uses the
Lee Kesler method to calculate Enthalpy and
Entropy.

Peng-Robinson
 The Peng-Robinson (PR) model is ideal for VLE calculations as well
as calculating liquid densities for hydrocarbon systems. Several
enhancements to the original PR model were made to extend its
range of applicability and to improve its predictions for some non-
ideal systems. However, in situations where highly non-ideal
systems are encountered, the use of Activity Models is
recommended.
 The PR property package rigorously solves any single-, two-, or
three-phase system with a high degree of efficiency and reliability
and is applicable over a wide range of conditions:
 Temperature Range > -271°C or -456°F
 Pressure Range < 100,000 kPa or 15,000 psia

 The PR property package also contains enhanced
binary interaction parameters for all library
hydrocarbon-hydrocarbon pairs (a combination of fitted
and generated interaction parameters), as well as for
most hydrocarbon-non-hydrocarbon binaries. For non-
library or hydrocarbon hypocomponents, HC-HC
interaction parameters are generated automatically by
HYSYS for improved VLE property predictions.

 For Oil, Gas, or Petrochemical applications, the PR EOS is the
generally recommended property package. The PR property
package is generally used for the following simulations:
 TEG Dehydration
 TEG Dehydration with Aromatics
 Cryogenic Gas Processing
 Air Separation
 Atm Crude Towers
 Vacuum Towers
 High H2 Systems
 Reservoir Systems
 Hydrate Inhibition
 Crude Systems

Peng-Robinson Calculation
Methods

Enthalpy & Entropy
For the Peng-Robinson Equation of State, the enthalpy and
entropy departure calculations use the following relations:
Where:
HID = Ideal Gas Enthalpy basis used by HYSYS changes with
temperature according to the coefficients on the TDep tab for each
individual component
R = Ideal Gas constant
H = Enthalpy
S = Entropy
ID = indicates Ideal Gas
° = indicates reference state

PRSV
The PRSV model is a two-fold modification of the Peng-
Robinson equation of state that extends the application of
the original Peng-Robinson method for moderately non-
ideal systems. This EOS is shown to match vapour
pressures curves of pure components and mixtures more
accurately than the PR method, especially at low vapour
pressures. It is successfully extended to handle non-ideal
systems giving results as good as those obtained using
excess Gibbs energy functions like the Wilson, NRTL, or
UNIQUAC equations.

The advantages of the PRSV equation are:
 It has the potential to more accurately predict the
phase behaviour of hydrocarbon systems,
particularly for systems composed of dissimilar
components.
 It can be extended to handle non-ideal systems
with accuracies that rival traditional activity
coefficient models.

 The only compromise for PRSV equation of state
is the increased computational time and the
additional interaction parameter that is required
for the equation.
 The PRSV equations of state perform rigorous
three-phase flash calculations for aqueous
systems containing H2O, CH3OH or glycols, as
well as systems containing other hydrocarbons or
non-hydrocarbons in the second liquid phase.

The PRSV property package generally
used in the following simulations:
 Air Separation
 Chemical systems
 HF Alkylation

SRK
 In many cases, the Soave-Redlich-Kwong (SRK) model
provides comparable results to Peng-Robinson, but its
range of application is significantly more limited:
 Temperature Range > -143°C or -225°F
 Pressure Range < 5,000 kPa or 35,000 psia
 The SRK EOS should not be used for non-ideal chemicals
such as alcohols, acids or other components. These
chemicals are more accurately handled by the Activity
Models (highly non-ideal) or the PRSV EOS (moderately
non-ideal).

The SRK property package is generally
used for the following simulations:
 TEG Dehydration
 Sour Water
 Air Separation
 Atm Crude Towers
 Vacuum Towers
 High H2 Systems
 Reservoir Systems
 Hydrate Inhibition
 Chemical systems
 HF Alkylation
 TEG Dehydration with Aromatics

Sour PR
 The Sour PR model combines the Peng-Robinson equation of state
and Wilson's API-Sour Model for handling sour water systems and
can be applied to sour water strippers, hydrotreater loops, crude
columns, or any process containing hydrocarbons, acid gases, and
H2O.
 In the Sour PR model, the K-values for the aqueous phase are
calculated using Wilson's API-Sour method. This option uses Wilson's
model to account for the ionization of the H2S, CO2, and NH3 in the
aqueous water phase. The aqueous model employs a modification of
Van Krevelen's original model with many of the key limitations
removed. The K-value of water is calculated using an empirical
equation, which is a function of temperature only.

 The original model is applicable for temperatures
between 20°C (68°F) and 140°C (285°F), and
pressures up to 50 psi. Use of the PR equation of
state to correct vapour phase non idealities
extends this range, but due to lack of experimental
data, exact ranges cannot be specified. The
acceptable pressure ranges for the HYSYS model
vary depending upon the concentration of the acid
gases and H2O. The method performs well when
the H2O partial pressure is below 100 psi.

Sour SRK
 The Sour SRK model combines the Soave Redlich Kwong and
Wilson's API-Sour Model and can be be applied to sour water
strippers, hydrotreater loops, crude columns, or any process
containing hydrocarbons, acid gases, and H2O.
 This option uses Wilson's model to account for the ionization of
the H2S, CO2, and NH3 in the aqueous water phase. The
aqueous model employs a modification of Van Krevelen's
original model with many of the key limitations removed. The
K-value of water is calculated using an empirical equation,
which is a function of temperature only.

 The original model is applicable for temperatures
between 20°C (68°F) and 140°C (285°F), and
pressures up to 50 psi. Use of the SRK equation of
state to correct vapour phase non idealities extends this
range, but due to lack of experimental data, exact
ranges cannot be specified. The acceptable pressure
ranges for the HYSYS model vary depending upon the
concentration of the acid gases and H2O. The method
performs well when the H2O partial pressure is below
100 psi.

Zudkevitch Joffee
 The Zudkevitch Joffee model is a modification of the
Redlich Kwong equation of state. This model has been
enhanced for better prediction of vapour-liquid
equilibria for hydrocarbon systems, and systems
containing Hydrogen. The major advantage of this
model over the previous version of the RK equation is
the improved capability of predicting pure component
equilibria, and the simplification of the method for
determining the required coefficients for the equation.

 Enthalpy calculations for this model are
performed using the Lee-Kesler model.
 The Zudkevitch Joffee property package
is generally used for High H2 Systems.

B. Activity Models
 The Activity Models handle highly non-ideal systems and are
much more empirical in nature when compared to the property
predictions in the hydrocarbon industry. Polar or non-ideal
chemical systems are traditionally handled using dual model
approaches. In this type of approach, an equation of state is
used for predicting the vapour fugacity coefficients and an
activity coefficient model is used for the liquid phase. Since the
experimental data for activity model parameters are fitted for a
specific range, these property methods cannot be used as
reliably for generalized application.

B. Activity Models
 Chien Null
 Extended NRTL
 General NRTL
 Margules
 NRTL
 UNIQUAC
 Van Laar
 Wilson

C. Chao Seader & Grayson
Streed Models
 The Chao Seader and Grayson Streed methods
are older, semi-empirical methods. The Grayson
Streed correlation is an extension of the Chao
Seader method with special emphasis on
hydrogen. Only the equilibrium data produced by
these correlations is used by HYSYS. The Lee-
Kesler method is used for liquid and vapour
enthalpies and entropies.
 Chao Seader
 Grayson Streed

D. Vapour Pressure Models
 Vapour Pressure K-value models may be used for ideal mixtures
at low pressures. Ideal mixtures include hydrocarbon systems
and mixtures such as ketones and alcohols, where the liquid
phase behaviour is approximately ideal. These equations are
traditionally applied for heavier hydrocarbon fractionation systems
and consequently provide a good means of comparison against
rigorous models. The models may also be used as first
approximations for non-ideal systems. They should not be
considered for VLE (VAPOUR LIQUID EQUILIBRIUM) predictions
for systems operating at high pressures or systems with
significant quantities of light hydrocarbons.

D. Vapour Pressure Models
 Antoine
 Braun K10
 Esso Tabular

E. Miscellaneous Types
 The Miscellaneous group contains Property Packages that
are unique and do not fit into the groups previously
mentioned.
 Amine Pkg
 DBR Amine Package
 ASME Stream
 Glycol PPkg
 NBS Stream
 MBWR
 OLI_Electrolyte

3- Hypothetical
This tab enables you to create non-library or hypothetical
components.
Hypothetical components can be any of the following:
• Pure components
• Defined mixtures
• Undefined mixtures
• Solids
You can also clone library components into hypothetical
components, which allows you to modify the library values.

4- Oil Manager
The Oil Characterization environment is where the characteristics
of a petroleum fluid can be represented by using discrete
hypothetical components. Physical, critical, thermodynamic and
transport properties are determined for each hypothetical
component using correlations that you select. The fully defined
hypocomponent can then be installed in a stream and used in
any flowsheet.
To use the Oil Characterization environment, at least one fluid
package must exist in the case. Any hypothetical components
must be compatible with the property method used by the fluid
package.

5. Reactions
 The Reactions Tab in the Simulation Basis Manager
allows you to define reactions within HYSYS. You can
define an unlimited number of reactions and group
these reactions in reaction sets. The reaction sets are
then attached to unit operations in the flowsheet.

5. Component Maps
 The Component Maps tab allows you to map fluid
component composition across fluid package
boundaries. Composition values for individual
components from one fluid package can be mapped to
a different component in an alternate fluid package.
This is useful when dealing with hypothetical oil
components.

6. User Property
 User properties are any property that can be
defined and calculated on the basis of composition.
You supply a user property value for each
component in a fluid package, then select the
mixing basis and mixing equation to calculate the
total user property.

Simulation Environment
 The Simulation environment contains the main flowsheet
where you do the majority of your work (installing and
defining streams, unit operations, columns and sub-
flowsheets).
 To enter the Simulation environment, click either the Enter
Simulation Environment button.

•Energy Stream (red)
•Material Stream (blue)

Example 1:
For a stream (Feed) 100 lbmole/h which consists of:
N2 0.25% , CO2 0.48%, H2S 2.37%, H2O 0.0%, C1 68.00%, C2
19.2%, C3 7.1%, N-C4 0.85%, I-C4 1.15%, N-C5 0.21%, I-C5 0.36%
& N-C6 0.03%.
Fluid PKg : PR
* Calculate the vapor fraction at P =7500 kPa & T =10oC.
* Calculate the dew point at P =7500 kPa.
* Calculate the bubble point at P =7500 kPa
Use Peng-Robinson FPkg

Add the Components
Select the suitable fluid pkg (in this case select Peng-
Robinson)
Enter Simulation Environment

Gas Refrigeration
A Refrigeration cycle utilizes propane as the
working fluid is used in the liquefaction of the NG

Hysys Course 2022.ppt

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