Aspen HYSYS - Petroleum Assays and Oil Characterization (Slideshare)

Chemical Engineering Guy
www.ChemicalEngineeringGuy.com

1. Introduction
2. Hypotheticals Manager
3. Petroleum Assays
4. Oil Manager: Step 1 – Input Data Assay
5. Oil Manager: Step 2 – Cutting & Blending
6. Oil Manager: Step 3 – Installing the Oil
7. Plotting Results: Graphs, Tables, Charts
8. Study Case – Industry Application
9. Conclusion
10. Bonus Section!
25%Theory
75% Workshop

a) Why Process Simulation?
b) What is Aspen HYSYS? Required version?
c) Why Hypos, Assays and Oil Characterization?
d) Required Background and previous knowledge

 Fractionation Column
 Given conditions
 Reboiler Duty
 Crude Oil composition (LAB)
 Inlet Temperature
 Products conditions
 Model this!
 Optimize
What will happen if we change Crude Oil Composition?

Crude Oil

 Makes us easier/faster work
 Multiple and Simultaneous Simulations
 Different Real-Life Scenarios
 Change on raw/feed materials scenario
 Pricing and Costs calculation
 Raw Materials
 Plant Cost
 Utilities
 How it would behave under different conditions
 High/Low Pressure
 Humidity Changes
 Temperature change (cool/warm days/seasons)

 Mainly:
 Petrochemical
 Oil&Gas
 Other commodities such as:
 Sulfuric acids
 Chlorine/Caustic industry
 Coatings
 Ammonia
 Hydrogen Gas

 Helps us:
 Stream flow rates
 Compositions of streams
 Physical properties such as P, T, v of streams
 Unit operation operating conditions:
 Heat duty
 T, P,
 Electricity
 Efficiency
 Power…
 Preliminary equipment sizing ideas/design
 Important operational/design concerns/issues

 As any Engineering problem, we require to set some data:
 Mass & Energy balances
 Transport phenomena:
 Momentum
 Heat
 Mass
 Separation principles
 Equilibrium relationships
 Gibbs free energy
 Entropy
 thermos’s law

 DESGIN:
 Decrease in time
 Decrease or experimental requirements
 Improves Pilot Plants and Tests
 Explore proprietary/experimental process technology
 Allows Equipment design

 OPERATION:
 Helps to improve existing processes
 Set possible set of scenarios
 Determine best operational input
 Safety Analysis (Safety Regulations)
 Emissions studies (Environmental)

 Excelent for your curriculum as an engineer
 Perfect for analytical/numerical minds
 Good for debuging and fixing
 .

From the website:
“Aspen HYSYS is the energy industry’s leading process simulation software that’s
used by top oil and gas producers, refineries and engineering companies for process
optimization in design and operations.”
http://www.aspentech.com/products/aspen-hysys/

 Petroluem Assay Manager
 Oil Manager
http://www.aspentech.com/products/aspen-hysys/
Aspen HYSYS® - Crude License
Aspen HYSYS® - Petroleum Refining
License

 My version V8.8 (May 2015)
 Most recent version V10 & 10.1 (Nov 2017)
 https://home.aspentech.com/en/v10

 “X” is not present in database
 “Y” is a required product, new in chemical world
X + Solvent
YX
Solvent
N/A

 Hypos:
 Chemicals not present in database
 92 Octane Gasoline
 Diesel
 Coal
 Natural Gas
 NEW chemical components
 Non-standardized products
 Nature of chemical compounds vs. real life compounds
 Databases not 100% reliable
 Detailed material composition/modeling
 They can be still be modeled!

 Assays & Oil Characterization
 Nature crude’s composition
 Naphtha
 Kerosene
 Diesels
 Fueloils
 Asphalt/residue
 Databases not 100% reliable
 Required input
 Viscosity, density, molar mass

 Paraffins CnH2n+2
 Gasses or liquids at room temperature
 Examples (methane, ethane, propane, butane, isobutane, pentane, hexane)
 Aromatics C6H5 - Y
 ringed structures with one or more rings rings contain six carbon atoms(single/double bond)
 benzene, napthalene
 Napthenes or Cycloalkanes CnH2n
 ringed structures with one or more rings rings contain only single bonds between the carbon atoms
 typically liquids
 cyclohexane, methyl cyclopentane
 Alkenes CnH2n liquid or gas
 ethylene, butene, isobutene
 Dienes and Alkynes CnH2n-2
 liquid or gas examples
 acetylene, butadienes
1.paraffins (15-60%)
2.naphthenes (30-60%)
3.aromatics (3-30%)
4.asphaltics (remainder)

 Carbon - 84%
 Hydrogen - 14%
 Sulfur - 1 to 3% (hydrogen sulfide, sulfides, disulfides, elemental sulfur)
 Nitrogen - less than 1% (basic compounds with amine groups)
 Oxygen - less than 1% (found in organic compounds such as carbon dioxide, phenols, ketones,
carboxylic acids)
 Metals - less than 1% (nickel, iron, vanadium, copper, arsenic)
 Salts - less than 1% (sodium chloride, magnesium chloride, calcium chloride)

 Coal  not present
 Gasoline 92 Octanes  not present

 Basic Chemistry, petrochemistry
 Basic knowledge in Unit Operations
 Engineering Field
 Oil / Drilling / Chemical / Petrochemical / Mechanical / Process / Industrial
Need Training?

 Please feel free to take this Course!
 You will need to know the basics of Aspen HYSYS
Aspen HYSYS
Use the following coupon
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 Also, if you need even more training, please checkout:
www.ChemicalEngineeringGuy.com/Courses

 For my students!
 Get these FREE
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 Coupon = OILMNG-15

 Hypothetical Compounds (Hypos)
 Estimation of hypo compound data
 Use the UNIFAC Component Builder
 Basis conversion of existing components
 Petroleum Assays Manager
 Input crude oil data
 Model Crude oils
 Import existing Assays
 Plot relevant data/results
how to setup hypothetical compounds, oil assays, blends, and petroleum characterization
using the Assays and Oil Manager of Aspen HYSYS

 Oil Manager
 Input of Crude Assay Data
 TBP
 ASTM (D86, D1160, D86-D1160, D2887)
 Chromatography
 Light Ends
 Density, viscosity, molecular weight based (dependent/independent)
 Plot Relevant Results
 Distillation Curves
 Viscosity
 Distribution Plots (Off Gas, Light Short Run, Naphtha, Kerosene, Light Diesel, Heavy Diesel,
Gasoil, Residue)
 Property Table/Plots

 Installing the Oil
 Cutting/Blending different assays
 Using the oil in Flowsheet
 Simulation using the Oil
 Study Case
 Fractionation of crude oil

 Compounds not present in Data Bases
 Mostly modeled/theoretical
 Select desired methods to estimate unknown properties
 Hypothetical Manager

 Possible components:
 non-library
 hypothetical
 Pure
 Defined mixtures
 Undefined mixtures
 Solids (Coals)
 You can also convert/clone HYSYS library components into hypotheticals, allowing
you to modify the library values.

 Component List > Hypo Group > Hypo Compound
 One class  One group
 Classes: Alkanes, inorganics, ketones,
 1 Comp. List = 1 Fluid Package
 Hypo Manager  Settings  Group  Class

 3 Ways to model:
 Physical + Chemical properties
 Chemical Structure
 Converting/Cloning “base” component
 NEXT  Practice each one in a Workshop!

 Typically choose 2:
 Normal Boiling Point
 Molecular Weight
 Liquid Density
 Partial T/P
 Accentricity
Estimate!
I
n
p
u
t

 1) Generate Hypo Components
 Method = Create a Batch of Hypos
 Initial BP = 500°C
 Final BP = 900°C
 Interval = 50°C
 “ADD” to list

 2) Generate Hypo Components
 Method = Create&Edit Hypos
 NBP = 117.50°C
 MW = 150
 Density = 750 kg/m3
 Estimate unkown  Tc,Pc,Vc, Acc.
 “ADD” to list

 Use FP: Antoine
 Coefficients will be calculated

 Go to Sim. Environment
 Add stream
 T = °50, P = 101 kPa, F = 100 kmol/h
 Setup Composition
 You can now simulate the streams!

Check Course for:
*Video Lecture
*Spreadsheets
¨*Results
*Simulation/Cases

 Aspen HYSYS will model given the Structure
 Identify the “important” organic groups
 Chemical Structure + UNIFAC Component Builder
 Double click “Hypo#ID”  Button “Structure Builder”  State “UNIFAC
Structure”

1
2
3

 4-nonanona  Ketone
 Hypo Manager  Ketone
 Generate 1 Hypo
 UNIFAC Structure Builder
 CH3 - (sub group 1)
 CH2 - (sub group 2)
 C=O - (sub group 20)

 Converted from another existing component
 Based on its properties
 The “base” component must be stated FIRST
 Manual/edition
 Estimation/Calculation

 Model “Benzenalike” a molecule very similar to benzene, with different propeorties,
and unkown structure
 First, Add “Benzene” to the comp. list
 Choose “Convert” from Hypo Manager
 Choose Benzene  change composition

 You can now model Benzenalike!

 A crude oil assay is the chemical evaluation of crude
oil feedstocks by petroleum testing laboratories.
 The results of crude oil assay testing provide extensive detailed hydrocarbon analysis
data for refiners, oil traders and producers.
 Assay data help refineries determine if a crude oil feedstock is compatible for a
particular petroleum refinery or if the crude oil could cause yield, quality, production,
environmental and other problems.

 Each crude oil has unique molecular and chemical characteristics
 No crude oil types are identical.

 In a refinery, a typical crude oil stream consists of the following
characteristics:
 Mixture of many naturally occurring hydrocarbons
 Boiling points ranging from -160°C (Methane) to more than 1500°C.
 Heavy fractions that are not mixtures of discretely identifiable components.
 Plus-fraction starting from C7+ to C12+
Specially  Heavy crudes!

 A proper description of the physical properties of the plus-fractions
is essential for reliable phase behavior calculations and
compositional modelling studies.

Aspen HYSYS® - Petroleum Refining License

 Users with the HYSYS Petroleum Refining license should use the HYSYS
Petroleum Assay to model petroleum crude.
 This is an advanced form of crude oil assay supporting extensive petroleum
properties such as gravity, sulfur, nitrogen, cloud point, carbon, metals, and more.
 You can easily import existing Oil Manager assays to HYSYS Petroleum assays
from the Petroleum Assay setup pages.
Aspen HYSYS® - Petroleum Refining License

 The Assay Manager lets you manage Petroleum Assay Data in
Aspen HYSYS Petroleum Refining.
 Assays can be added to the case from a variety of sources and
characterized.
 Properties required in the simulation can then be calculated
according to the specified Fluid Package.
A Fluid Package must be stated!

 Using the Petroleum Assays form, you can:
 Display the Assay Description
 Input Data / Import Assay / Download Assay
 Define cut properties
 Generate plots

 NEW Assays:
 Import Existing (Library/File)
 Manually Enter
 Characterize
 Download Assays

 Least Required
 More DATA

 Assay-1
 Define the Cuts (100°-500°)

 Assay-1
 Define the Cuts (100°-500°)
 Click “Characterize Assay”

 Assay-1
 Check out all results!

 Copy: Assay-1  Copy of Assay-1
 Add more data:
 %whole crude = 100%
 Density whole = 750 kg/m3
 Total Sulfur % = 2.5%
 Paraffin Vol = 40%
 Naphthene Vol = 25%
 Oleffins Vol = 10%
 Aromatic Vol = 15.0%

 Check results!
 Compare vs. less data

 Pre-existing Assays (600 approx.)
 By Region
 By Country
 Complete DATA!

 Import existing 
 West Texas Intermediate 1994
 Review Component List
 Verify FP = Peng Robinson (default)
 Checkout “Input Assay” Folder
 Go to “Conventional Results”

 West Texas Intermediate

 Typically, we are interested on the Assay Properties:
 Cuts
 Distillation Curve (BP vs. composition)
 Physical/Chemical Properties
 Viscosity of crude
 Viscosity of Cuts
 PNA (information of Paraffins, Napthenes, Aromatics)

1 Assay
2 or more…

 (y-axis)
 Weight
 Volume
 Mol
 (x-axis)
 %, ppm
 g/kg
 g/g (fract)

 Type:
 TBP
 D86
 D2887
 (y-axis)
 Mass
 Volume
 (x-axis)
 Temperature
 Flip Coordinates

 Selected Property
 Vs. T or V%

 PNA represents
 Paraffin
 Naphthene
 Aromatic

 Assay  From previous Workshop (#5) Imported  West Texas Intermediate 1994
 Get all the next:

 Select Property
 Burning Props.  FlammabilityFlash point

 Select Property
 Cold Properties  CloudPoint

 Select Property
 Contaminants Sulfur by weight %

 The same can be done for 2
Assays or even more assays
 Excellent for crude oil comparison

 From WSK4+5  Compare our “random” assay vs. TX-Intermediate
 Repeat previous Workshop
 Get all the next:

 Select Property
 Density (kg/m3)

 Users with the HYSYS Petroleum Refining license should use the HYSYS
Petroleum Assay to model petroleum crude.
 This is an advanced form of crude oil assay supporting extensive petroleum
properties such as gravity, sulfur, nitrogen, cloud point, carbon, metals, and more.
You can easily import existing Oil Manager assays to HYSYS Petroleum assays
from the Petroleum Assay setup pages.
Aspen HYSYS® - Crude License
Aspen HYSYS® - Petroleum Refining
License

 Oil characterization  Oil Manager in Properties Environment
 Converts Assay Data into a series of discrete hypothetical components
 “Portion of hydrocarbons which boil from 40°C to 50°C  “NBP[0]045”

 Three steps in Oil Characterization:
1. Input assay data
2. Cut and blend assay into hypothetical components
3. Install oil information to flowsheet

 Min info. required to characterize the oil:
 Distillation data curve (*at least 2 points)
 OR/AND
 Two bulk properties (molecular weight, density, or Watson K)
 Provided distillation curves are converted to other formats using built-in API
methods
More data  Better model
API = American Petroleum Institute

 Input 1:
 (Bulk Properties)
 MW = 365 g/mol
 Density = 750 kg/m3
 Input 2:
 (Distillation Curve)
 TBP
 Point 1 (1% v/v; 0°C)
 Point 1 (99% v/v; 500°C)

Assay Types:
 TBP (true boiling point)
 ASTM D86
 D1160 distillation
 D86–D1160
 ASTM D2887
 EFV (equilibrium flash
vaporization)
 Chromatographic analysis
 Bulk Properties:
 Molecular Weight > 16
 Mass Density = 250 ~ 2000 kg/m3
 Watson K Factor = 8 ~ 15
 Bulk Viscosity, @ 100°F and @210°F
 Physical Property Curves:
 Molecular Weight
 Density
 Viscosity

Assay Types:
 TBP (true boiling point)  BP vs. Composition
 ASTM D86  https://www.astm.org/Standards/D86.htm
 D1160 distillation
 D86–D1160
 ASTM D2887
 EFV (equilibrium flash vaporization)
 Chromatographic analysis
An ASTM designation number identifies a unique
version of an ASTM standard.
D86 - 17
D = miscellaneous materials;
86 = assigned sequential number
17 = year of original adoption (or, in the case of
revision, the year of last revision)
•D86 Test Method for Distillation of Petroleum Products at Atmospheric Pressure
•ASTM D20-03(2014) Standard Test Method for Distillation of Road Tars
•D1160 Test Method for Distillation of Petroleum Products at Reduced Pressure

 Be sure how you get the input data (specifications)
 Type (TBP, D86, etc.)…
 Are light-ends included?
 Do you have a separate light ends analysis?
TBP equipment (Crude
Oil)AUTOMATIC TBP D2892 DISTILLATION UNITSwww.ChemicalEngineeringGuy.com

 Peng Robinson
 Bulk: MW = NA D = 800 kg/m3
 Assay Data Type: ASTM D86
 Light Ends: IGNORE
• Distillation Curve (v/v% vs. T°C)
%Assay Percent T(°C)
0 165
5 175
10 183
30 195
50 205
70 210
90 225
95 230
98 235

 Peng Robinson
 NAME = Naptha
 Bulk: D = 54.3 API-60 Watson UOPK = 11.83
NOTE: We will use this in Blending
(Naphtha + Kerosene)
0 186
5 220
10 232
20 244
30 254
40 265
50 274
60 286
70 298
80 310
90 329
95 344
100 360

 Peng Robinson
 NAME: Kerosene
 Bulk: D = 37.9 API-60
 Watson UOPK = 11.71
 T1 = 100F  V1 = 2.230 cSt
 T2 = 210F  V1 = 0.95 cSt
NOTE: We will use this in Blending
(Naphtha + Kerosene)
0 379
5 402
10 412
20 432
30 450
40 467
50 486
60 502
70 520
80 540
90 562
95 574
100 586

 Greyson Streed
 Bulk: MW = 203.4 D = 52.75 lb/ft3
 Assay Data Type: TBP
 Molecular Weight = dependent
 Density Curve = Dependent
See Spreadsheet
Data (WKS09)
Assay Basis Liquid Volume
Distillation Curve
%Assay Percent T(°F) T(°C)
0 -4.9 -20.5
2 43.9 6.6
5 96.5 35.8
10 174.3 79.1
15 224.5 106.9
20 268.4 131.3
30 345.6 174.2
40 433.8 223.2
50 529.6 276.4
60 631.4 333.0
70 750.7 399.3
80 908.3 486.8
90 1144 617.8
95 1330 721.1
98 1548 842.2
100 1575 857.2
Assay Basis Molar Weight= Dependent
Distillation Curve
%Assay Percent MW
0 27.07
2 62.72
5 72.15
10 96.77
15 111.6
20 124.4
30 150.3
40 185.8
50 227.8
60 279.6
70 350.3
80 451.8
90 602.9
95 689.4
98 779.2
10 845.8
%Assay Percent Density (lb/ft3) Density (kg/m3)
0 20.10 321.9
2 37.04 593.4
5 39.30 629.6
10 43.13 690.9
15 45.01 721.1
20 46.87 750.9
30 48.93 783.9
40 50.01 801.2
50 52.17 835.8
60 54.14 867.3
70 55.75 893.1
80 58.11 930.9
90 62.22 996.8
95 67.09 1074.8
98 70.51 1129.6
10 72.95 1168.7

 Peng Robinson
 Bulk: D = 800 kg/m3
 Fixed Temperature (standard)
 Extrapolation  Lagrange
• Distillation Curve (v/v% vs. T°C fixed)
%Assay Percent T(°F) T(°F)STD T(°C)STD2
0 95 108.1 42.3
10 176 190.3 87.9
30 289.4 305.3 151.8
50 336.2 352.8 178.2
70 363.2 380.2 193.4
90 417.2 435.0 223.9

 Light Ends are defined:
 pure components
 low boiling points
 C2 to n-C5 (propane/propylene, butanes, etc.)
 They should be replaced with discrete pure components
 This should always yield more accurate results than using hypocomponent to
represent the Light Ends portion.

 Ignore
 When the assay is prepared with the Light Ends in the sample and the Light
Ends portion is characterized using hypo components (least accurate—not
recommended)
 Also useful if it is understood there is a negligible content of lights in the assay
sample
 Input Composition:
 When the assay is prepared with Light Ends in the sample and a separate Light
Ends assay is available
 Auto Calculate
 When the assay is prepared with the Light Ends in the sample and you want to
use pure components to represent the low boiling portion of the assay

 Light Ends handling and Bulk Property fitting:
 Are Light-ends included in the input curves?
 Are Light-ends included in the bulk properties?
 Do you want to control which part of the curve is tuned to match the bulk
property?

 Peng Robinson
 Bulk: D = 879.8 kg/m3
 Light Ends: Input (v/v% vs. T°C)
• Distillation (v/v% vs T°C)
Light Ends v/v%
%Assay Percent Comp
Methane 0.0065
Ethane 0.0250
Propane 0.3200
i-Butane 0.2400
n-Butane 1.7500
i-Pentane 1.6500
n-Butane 2.2500
Water 0.0000
Distillation Curve
0 -12
4 32
9 74
14 116
20 154
30 224
40 273
50 327
60 393
70 450
76 490
80 516

 Peng Robinson
 Bulk: MW = 300 D = 48.75 API-60
 Density = dependent
 Viscosity / MW = independent

0 80 27
10 255 124
20 349 176
30 430 221
40 527 275
50 635 335
60 751 399
70 915 491
80 1095 591
90 1277 692
98 1410 766
Light Ends v/v%
%Assay Percent Comp
Propane 0
i-Butane 0.19
n-Butane 0.11
i-Pentane 0.37
n-Butane 0.46
Water 0
%Assay v/v% Molecular Weight
0 68
10 119
20 150
30 182
40 225
50 282
60 350
70 456
80 585
90 713
98 838
Density Curve INDEPENDENT
%Assay v/v% API Density
13 63.28
33 54.86
57 45.91
74 38.21
91 26.01
INDEPENDENT
Visc Curve 1 (use both) Kinetic 100F
%Assay v/v% Visc (cp)
10 0.2
30 0.75
50 4.2
70 39
90 600
INDEPENDENT
Visc Curve 2 (use both) Kinetic 210F
%Assay v/v% Visc (cp)
10 0.1
30 0.3
50 0.8
70 7.5
90 122.3

 Peng Robinson
 Bulk: MW = 79.60 D = 0.6659 SG-60/60 api
 Assay Data Type: Chromatograph (by mol)
 Lists
 Light Ends = N2, H2S, CO2, H2O, methane to pentane
 Paraffinic = Hexane to Triconane Plus
 Aromatic = (Benzene to TMB)
 Napthenic = Cyclos

Column1 Column2 Column3
Light Ends mol%
N2 0.48
H2S 0.00
CO2 0.87
C1 41.83
C2 8.87
C3 7.11
i-C4 1.47
n-C4 3.75
i-C5 1.25
n-C5 1.63
C6 0.00
H2O 0.00
Total Light Ends % in Assay 67.26
Column1 Column2 Column3
Aromatic Components mol frac.
Benzene (C6H6) 0.0004
Toluene (C7H8) 0.0015
EBZ, p+m-Xylene (C8H10) 0.0070
o-Xylene (C8H10) 0.0028
1,2,4 TMbenzene (C9H12) 0.0028
Naphthenic Components Mol Frac
Cyclopentane (C5H10) 0.0002
Mclyclopentane (C6H12) 0.0106
Cyclohexane (C6H12) 0.0050
Mcyclohexane (C7H14) 0.0156
Paraffinic C# Mol Frac
Hexane (C6) 6 0.0268
Heptane (C7) 7 0.0371
Octane (C8) 8 0.0348
Nonane (C9) 9 0.0231
Decane (C10) 10 0.024
Undecane (C11) 11 0.0183
Dodecane (C12) 12 0.0142
Tridecane (C13) 13 0.0141
Tetradecane (C14) 14 0.0113
Pentadecane (C15) 15 0.0099
Hexadecane (C16) 16 0.0074
Heptadecane (C17) 17 0.0082
Octadecane (C18) 18 0.0062
Nonadecane (C19) 19 0.0049
Eicosane (C20) 20 0.0046
Heneicosane (C21) 21 0.0039
Docosane (C22) 22 0.0036
Tricosane (C23) 23 0.0032
Tetracosane (C24) 24 0.0027
Pentacosane (C25) 25 0.0024
Hexacosane (C26) 26 0.0021
Heptacosane (C27) 27 0.002
Octacosane (C28) 28 0.0018
Nonacosane (C29) 29 0.0016
Triconane Plus 30 0.0133

 Peng Robinson
 Bulk: MW = 277 D = 848.1 kg/m3
• Distillation (v/v% vs T°C)
Light Ends v/v%
%Assay Percent Comp
Methane 0.0000
Ethane 0.0150
Propane 0.2780
i-Butane 0.2080
n-Butane 1.6790
i-Pentane 1.7340
n-Butane 1.7930
Water 0.0000
TOTAL 5.7070
Distillation Curve
0 -20.5
2 6.6
5 35.8
10 79.1
15 106.9
20 131.3
30 174.3
40 223.2
50 276.4
60 333.0
70 399.3
80 486.8
90 617.6
95 721.3
98 842.1
100 857.2
Molecular WeightDEPENDENT
%Assay Percent MW
0 27.1
2 62.7
5 72.2
10 96.8
15 111.6
20 124.4
30 150.3
40 185.8
50 227.8
60 279.6
70 350.3
80 451.8
90 602.9
95 689.4
98 779.2
100 845.8
Density DEPENDENT
%Assay Percent Density kg/m3
0 321.9
2 593.4
5 629.5
10 690.8
15 720.9
20 750.8
30 783.8
40 801.0
50 835.7
60 867.3
70 893.0
80 930.9
90 996.7
95 1075.0
98 1131.0
100 1169.0

 Fluid Package = Peng Robinson
 MW = NA
 Density = 29.32 API-60
 Assay Data Type = TBP
0.0 15.0 -9.4
4.5 90.0 32.2
9.0 165.0 73.9
14.5 240.0 115.6
20.0 310.0 154.4
30.0 435.0 223.9
40.0 524.0 273.3
50.0 620.0 326.7
60.0 740.0 393.3
70.0 885.0 473.9
76.0 969.0 520.6
80.0 1015.0 546.1
85.0 1050.0 565.6
Light Ends v/v%
%Assay Percent Comp
Methane 0.0065
Ethane 0.0225
Propane 0.3200
i-Butane 0.2400
n-Butane 0.8200
Water 0.0000
TOTAL 1.4090
IMPORTANT  USED
IN FINAL WORKSHOP

 Cutting generates the hypothetical components and
determines their compositions in the installed oil
 Types:
 Auto-cut
 User Ranges
 User Points

 Auto Cut
 Aspen HYSYS performs cuts automatically using built-in cutpoint
ranges
 HYSYS performs the cutting automatically upon selection
Cutpoint Range Boiling Point Width
IBP to 800 F 25 F per cut
800 F to 1200 F 50 F per cut
1200 F to 1650 F 100 F per cut

 User Points
 User defines the number of desired cuts for the oil
 Specified cut points are proportioned based on internal weighting scheme
Cutpoint Range Internal Weighting
IBP – 800 F 4 per 100 F
800 F – 1200 F 2 per 100 F
1200 F - FBP 1 per 100 F

 User Range
 Specify boiling point ranges and the number of cuts per range
 Grants more control over how many hypothetical components are generated
 Specifies the boiling point ranges they cover

 Choose Workshop # 13 and cut via:
 “Auto-Cut”
 “User points”
 “User Ranges”

Oil 1 Oil 2 Unblended Blended
NBP(20) NBP(25) NBP(20) NBP(22)
NBP(30) NBP(35) NBP(25) NBP(32)
NBP(40) NBP(45) NBP(30) NBP(42)
NBP(50) NBP(55) NBP(35) NBP(52)
NBP(60) NBP(65) NBP(40) NBP(62)
NBP(70) NBP(75) NBP(45) NBP(72)
NBP(80) NBP(85) NBP(50) NBP(82)
NBP(90) NBP(95) etc NBP(92)
8 8 16 8
 Blending is used to combine a number of assays and provides a general
presentation of the whole crude

 Blend Assays from:
 Workshop 10 “Naptha”
 Workshop 11 “Kerosene”

 Easiest Part!
 Click the Install Oil button after creating
the blend
 Provide the name of the target stream in
the Install Oil form and the Oil Manager
will:
 Add the hypo components to the fluid package
 Create a stream in the selected flowsheet with the
calculated composition

 Install Workshops:
 Workshop #16
 Workshop #18
 Workshop #20

 Convert Oil from Workshop #21A 
 Convert Oil from Workshop #21C 

 Table Type
 Property Plot
 Distribution Plot
 Composite Plot
 Summary Plot

 Comp Prop.
 Comp. Breakdown
 Molar Comp.
 Oil Prop.
 Oil Distrb

 Comparison between types of Assays

• Saved plots

 Now, let us USE our “installed oil”
 Did you notice that w only worked on the “Physical Properties Environment”
 THIS IS EXTRA!
 Not actually part of the course!
 Check out more material in
 Aspen HYSYS: Oil & Gas Industry

This workshop includes the following tasks:
 Goal 1 – Input Assay Data
 Goal 2 – Cut & Blend
 Goal 3 – Install the Oil
 Goal 4 – Build the Flowsheet
 Goal 5 – Get Results
From Workshop #18
Oil & Gas Application

 Fluid Package = Peng Robinson
 Input Assay
 Density = 29.32 API-60
 Assay Data Type = TBP
 ENSURE v/v%
 Cutting
 User Points = 30 units
 Blending
 Installing Oil (Raw Crude)
0.0 15.0 -9.4
4.5 90.0 32.2
9.0 165.0 73.9
14.5 240.0 115.6
20.0 310.0 154.4
30.0 435.0 223.9
40.0 524.0 273.3
50.0 620.0 326.7
60.0 740.0 393.3
70.0 885.0 473.9
76.0 969.0 520.6
80.0 1015.0 546.1
85.0 1050.0 565.6
Light Ends v/v%
%Assay Percent Comp
Methane 0.0065
Ethane 0.0225
Propane 0.3200
i-Butane 0.2400
n-Butane 0.8200
Water 0.0000
TOTAL 1.4090

 Raw Oil (Material)
 T = 450 F; P = 75 psia; Liq Flow (STD) = 1E05 Barrels/day
 PreFlash (UNIT)
 Flash Separator
 Adiabatic, Vap1 vs. Liq1
 Crude Heater (UNIT)
 Heater; Inlet = Liq1, Outelt: Hot Crude; Q = Heat Duty 1
 dP = 10 psi; T= 650F
 Mixer (UNIT)
 Inlet = Hot Crude + Vap1

 Main Steam (Material)
 T = 375 F; P = 150 psia; F = 7500 lb/h; 100% Water
 Diesel Steam (Material)
 T = 300 F; P = 50 psia; F= 3000 lb/h; 100% water
 AGO Steam (Material)
 T = 300 F; P = 50 psia; F= 2500 lb/h; 100% water
 Q-Tower in (Energy)
 N/A

 Step 1
 Add Abosrber Column
 Atm Tower (UNIT)
 No Trays = 29
 Partial Condenser Heat duty = Q-condenser;
 Off Gas = Condenser gas
 Ovhead = Naptha
 WasteWater = (check Water Draw)
 ATM Feed = stage 28
 Q-Trim = stage 28
 Main Stream = Bottom Stage Inlet
 Bottom Liquid Outlet = Residue

 Step 2
 Condenser:
 P = 19.70 psia;
 dP = 9 psi
 Bottoms
 P = 32.70 psia

 Step 3
 Optional Condenser T = 100F
 Optional Top Stage T= 250
 Optional Bottom Stage T = 600

 Step 4
 Volume Basis
 No fill
 “Done”

 Kerosene= 9300 Ba/day
 #stages= 3; Return Stage = 8; Draw Stage = 9
 STD Ideal Vol.; Config = Reboiled
 Boilup ratio = 0.75
 Draw Spec = 9300 Ba/day  INSTALL

 Diesel= 19250 Ba/day
 STD Ideal Vol.;
 Config = Steam Stripped
 Steam Feed = Diesel Stream

 AGO (Automotive Gas Oil)= 4500 Ba/day
 STD Ideal Vol.;
 Config = Steam Stripped
 Steam Feed = AGO Stream
4500 Ba/day

 Pump1
 Return stage = 1; Draw stage = 2
 1st Spec: Rate =5*10^4 Ba/d
 2nd Spec: Duty = -5.5*10^-7 Btu/h

 Pump2

 Pump3

 FracTower  Design  Specs
 Column Liquid Flow
 Name = Overflash spec
 Stage = 27
 Flow Basis = Std. Ideal Vol
 Spec Val = 3500 Ba/day
 Column Duty
 Name = Kerosene Reboiler Duty
 Energy Stream = Kerosene_Energy@Column
 Spec Val = 7.5E06 Btu/h
 Column Vapor Flow
 Name = Vap Prod Flow
 Stage = Condenser
 Flow Basis = Molar
 Spec Value = 0

 Monitor:
 Reflux Ratio
 uncheck Active; Value = 1.0
 Distillate Ratio
 ReName  Naphta Prod Rate
 Draw = Naptha @Col1
 Basis = Std. Ideal Vap
 Spec Val = 2.3*104 Ba/day
 Delete
 Reflux Rate; Vap Prod Rate; Btms Prod Rate ; Kerosene_BoilupRatio (0.75)
 Activate
 Kero Reb Duty = 7.5x10^6 Btu/h; Vap Prod Flow = 0

 Check out
 Flow rates
 Compositions
 Heat Duties
 Distillation Curve Profile
 T,P,Flow vs. Stages

 What you learnt
 What can you do now
 What’s next?

 Hypothetical Compounds (Hypos)
 Estimation of hypo compound data
 Models via Chemical Structure UNIFAC Component Builder
 Basis conversion/cloning of existing components

 Input of Petroleum Assay and Crude Oils
 Using the Petroleum Assay Manager or the Oil Manager
 Importing Assays: Existing Database
 Creating Assays: Manually / Model

 Oil Characterization
 Input:
 Typical Bulk Properties (Molar Weight, Density, Viscosity)
 Distillation curves such as TBP (Total Boiling Point)
 ASTM (D86, D1160, D86-D1160, D2887)
 Chromatography
 Light End
 Cutting: Pseudocomponent generation
 Blending of crude oils
 Installing oils into Aspen HYSYS flowsheets

 Getting Results (Plots, Graphs, Tables)
 Property and Composition Tables
 Distribution Plot
 Off Gas, Light Short Run, Naphtha, Kerosene…
 …Light Diesel, Heavy Diesel, Gasoil, Residue
 Oil Properties
 Proper
 Boiling Point Curves
 Viscosity, Density, Molecular Weight Curves

 Modeling Crude oils
 Study Case:
 Flash
 Heating
 Mixing
 Fractionation Column
 Side Strippers
Crude Oil

 Checkout more FREE and PREMIUM material at
www.ChemicalEngineeringGuy.com/Courses

 Get these FREE
 Use coupon = FREE-OILMNG

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Aspen HYSYS - Petroleum Assays and Oil Characterization (Slideshare)

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