Ehy2351-aspen-hysys-upstream

EHY2351 Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream Course Number EHY2351.084.01 .

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EHY2351 Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream AspenTech Customer Education Training Manual Course Number EHY2351.084.01

Copyright© 2014 by Aspen Technology, Inc. 200 Wheeler Road, Burlington, Massachusetts 01803, USA All rights reserved. This document may not be reproduced or distributed in whole or part in any form or by any means without the prior written permission of Aspen Technology, Inc. The information contained herein is subject to change without notice, and Aspen Technology assumes no responsibility for any typographical or other errors that may appear.

Aspen Technology may provide information regarding possible future product developments including new products, product features, product interfaces, integration, design, architecture, etc. that may be represented as "product roadmaps." Any such information is for discussion purposes only and does not constitute a commitment by Aspen Technology to do or deliver anything in these product roadmaps or otherwise. Any such commitment must be explicitly set forth in a written contract between the customer and Aspen Technology, executed by an authorized officer of each company.

Modeling I-Ieavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstrea111

Contents

Contents Section

Introduction to Heavy Oil Characterization Heavy Oil Characterization Workshop Oil & Gas Separation Plant Oil & Gas Separation Plant Workshop Pipeline Simulation Using Pipe Segment Oil and Gas Pipeline Simulation using HYSYS Pipe Segment Workshop Aspen Hydraulics Workshop Hydraulics in Dynamic Pigging Model Gas Oil Separation Plant (GOSP) Explore Conceptual Design Builder to swiftly build GOSP Modeling Real Separators Modeling Real Separators Workshops Tuning Viscosity Tw1ing Viscosity Workshop

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Agenda

Using Aspen HYSYS Upstream

Modeling Heavy Oil & Gas Production and facilities using Aspen HYSYS Upstream Course Number EHY2351.084.01

Disclaimer Aspen Technology may provide information regarding possible future product developments including new products, product features, product interfaces, integration, design, architecture, etc. that may be represented as "product roadmaps." Any such information is for discussion purposes only and does not constitute a commitment by Aspen Technology to do or deliver anything in these product roadmaps or otherwise. Any such commitment must be explicitly set forth in a written contract between the customer and Aspen Technology, executed by an authorized officer of each company.

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Using Aspen HYSYS Upstream

Agenda

Course Objectives At the end of this course you will be able to: Use upstream PVT information to simulate component based processes in HYSYS Model a oil and gas separation plant Simulate pipeline and piping networks using both the Pipe Segment operation and Aspen Hydraulics Simulate pipeline pigging using HYSYS Dynamics

Course Agenda Day 1

Introduction to Aspen HYSYS Upstream Heavy Oil Characterization Pipeline Simulation Using Pipe Segment I

Model Oil-Gas Separation Plant (OGSP) Pipeline Simulation Using Aspen Hydraulics

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Agenda

Using Aspen HYSYS Upstream

Course Agenda Day 2

Dynamic Pigging Using Aspen Hydraulics Conceptual Design Builder Modeling Real Separators Tuning Viscosity

Class Structure

"Hands-on" learning philosophy Brief introduction to each module, with demos as required Learning is achieved primarily by doing workshops and asking questions as problems are encountered, rather than via lecture

Tell me and I forget, Show me and I may remember, Involve me and I understand. Once each simulation model has been completed, attempt to answer the challenge questions posed at the end of the module Discussions and requests for demonstrations are welcome at any time

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Using Aspen HYSYS Upstream

Agenda

Course logistics

Morning Session - 8:30 am to 12:00 pm - Coffee break mid-morning

Lunch Break - 12:00 pm to 1:00 pm

Afternoon Session - 1:00pmto4:30pm - Coffee break mid-afternoon

Emergency exits, restrooms, etc.

AspenTech Contact Information Internet:

http://Support.AspenTech.com

Email:

[email protected] Training [email protected]

Phone:

NALA: +1 888 996 7100

EMEA: +44 (0) 118 922 6555 APAC:

+66 33 132920

Technical Support Hotline Training Customized Support Services Knowledge Base Solutions Product Patches

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Agenda

Using Aspen HYSYS Upstream

Q ues t .ions.']

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Introduction

Aspen HYSYS Upstream

Introduction to Aspen HYSYS Upstream Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objective Introduction to the Aspen HYSYS Upstream product Overview of key product features

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Introduction

Aspen HYSYS Upstream

Aspen HVSVS Upstream learning the Oil and Gas language

•Black Oil

•Mo/% • Components

•GOR

•Water Cut

• OH Characterization

•PVT

• FfowsheeUng • Equipment Sizing

• Well Modeling • Nodal Analysis

Production Engineer

Facility Engineer

forming the foundation Aspen HYSYS forms the foundation for AspenTech's oil and gas process modeling vision Oil &Gas Petroleum Upstream

AspenHYSYS Upstream

&

Downstream

Aspen HYSYS Petroleum Refining

Aspen HYsYS l.Jpstream Dynamics

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Introduction

Aspen HYSYS Upstream

Aspen HYSYS Upstrearn (1} Aspen HYSYS Upstream - Steady State: - Oil and Gas Thermodynamics and Methods ~ ~

-

Oil and Gas Feed Neotec Black Oil

Oil and Gas Flowsheeting Black Oil Translation in the case of Neotec Black Oil Component Lumping\Delumping Hydraulics Subflowsheet ~

Steady state pipeline network solver

- Production Allocation Utility - PVT Environment Infochem Multiflash Schlumberger DBR PVTPro Link with Calsep's PVTSim

Aspen HYSVS Upstream - Field Model Integration PIPESIM-Net Link -

Black Oil, Compositional, Gas Lift

Prosper/GAP Link

Aspen HYSYS Upstream - Dynamics: - Hydraulics Subflowsheet • ProFES engine inside

- OLGA 2000 Runtime Interface - Oil and Gas Feed I Black Oil Flowsheeting - Dynamics

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Aspen HYSYS Upstream

Introduction

Black Oils

Surface

-~=~""'r----1

1

·. •

Production Fluid (oil/water/gas)

•

Language of the Upstream industry - Reservoir, well, and flowline simulators use black oil models Reduces computational complexity of the problem

.1

- Petroleum/Production engineers have limited information on production fluid from well tests rv i

Complete compositional analyses rarely available

Black Oil Translation

Compositional Mode Standard ModeVntt Ops

Flow

Density

Oil and Gas Feed Translates automatically

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Introduction

Aspen HYSYS Upstream

Black Oil Translation

Compositional Mode

Neotec Black Oil Methods

Flow Density

Black Oil Translator

Cl C3 Cf

C2

N-C3 N-C4

cs

C6 C7+

PVT Environment

Resides in the basis environment Facilitates the work flow between Aspen HYSYS and third party PVT Packages Automatically generates fluid packages and component lists where appropriate Allows easy access to the created fluids from the stream level

•• I

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Aspen HYSYS Upstream

Introduction

Component lumping: lumper unit operation Methodology for "blending" and "grouping" components together Can be used to mix streams that have different component lists

Mainly used for hydrocarbons -

Can lump any components: pure, hypothetical, and other lumped components

Preserved Bulk Properties: - Molecular weight - Ideal liquid density - Molar and mass flow rates - Viscosities at two specified temperatures

Component lumping/ Del umping Cf

C2 C3 N-C3

C4

N-C4

C5

Cf

CB

C2

C7

C3

CB

N-C3

C4

N-C4

C5 CB CT>

C30-t

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Introduction

Aspen HYSYS Upstream

PnHluction Allocation Utility Tracks composition contribution in product streams from desired source streams

~ReporJ

Aspen Hydraulics Steady State Topology - Straight Run Convergent Branched - Looped/Divergent

Unit Operations - Pipe Segment (with/without Heat Transfer) - Valve, Mixer/Tee (Calculates Flow Direction and Pressure Drop) - Swage

Composition Tracking - Fully Compositional Model using Equation Of State (COM Thermo) - Black Oil

Refer to Sample files in folder "Irootl:\Prngr;un FiL~s\l\sPenie<::IJ\l\:menJ]Y5Ys\18.4\5ilmPles\l\sPenHyclrilcr1Lc:s"

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Aspen Technology, Inc.

Introduction

Aspen HYSYS Upstream

Aspen Hydraulics Transient Topology - Straight Run - Convergent Branched - Looped/Divergent

j

Solver Technology -

·-r--,,.M,-,---,,.,r-Tt"t--c-c-1

! ·~t--¥:+~+--+t-~

ProFES Two Phase Transient ProFES Three Phase Transient Two Phase Pigging Model Slug Prediction

Liquid Holdup Profile During Pigging

~

Terrain Induced • Flow Induced

Runtime interface to OLGA 2000

field Model Integration

PIPESIM-Net - Black Oil and Compositional modes supported - Gas Lilt rates

Petroleum Experts Prosper/GAP - Black Oil - Compositional

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Aspen HYSYS Upstream

Heavy Oil Characterization

lieavy Oil Characterization Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objectives Specify material streams using Oil & Gas Feed capabilities and calculate unknown heavy oil properties Select crude oil information from the built-in HYSYS library of worldwide crude samples Work with the Macro Cut table as an option for defining the Oil & Gas Feed

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Aspen HYSYS Upstream

Heavy Oil Characterization

Oil Characterization Various oil characterization options are available in Aspen HYSYS Oil & Gas Feed - With Oil & Gas Feed with Bulk Properties - Oil & Gas Feed with Assay Information

HYSYS Oil Manager/Oil Environment HYSYS Petroleum Refining (RefSYS) Assay Manager - Macro-cut table, Import CSV file, import from HYSYS Oil Manager

Few third party options also available such as: - Neotec Black Oil, PVT Infochem Multiflash and DBR PVT Pro.

Oil & Gas Feed Characterization The fundamental calculation is to mix oil fluid, gas fluid and water fluid in an appropriate ratio to match a user-specified Gas-To-Oil Ratio (GOR) and Water-to-Oil Ratio (WOR). Hypo component liquid density values are adjusted in order to match the desired stock tank density value.

Note: You can also enter the Oil Flow Target value at stock tank conditions, and have the stream calculate its total molar flow to match the oil flow target value specified.

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Aspen HYSYS Upstream

Heavy Oil Characterization

Oil & Gas feed Options

The material stream property view has three options for Oil & Gas Feed characterization: - No Oil & Gas Feed(default): Stream is a normal process stream and should be specified with composition & conditions - Oil & Gas Feed with Bulk properties: Oil fluid is characterized by bulk properties such as Watson K and bulk density - Oil & Gas Feed with Assay Info: Oil fluid is characterized using data from the HYSYS Assay Library. Mrteri.il St1tilm: ReitlVOir1 i

. 1

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Oil & Gas feed with Bulk Properties Oil & Gas Feed with Bulk Properties needs minimum data to define a heavy oil After importing/ adding the components and fluid package, Oil & Gas Feed requires the following properties at minimum: - Density of the oil, Watson K - GOR, WOR - Gas composition

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- Number of stages - Temp. & press. of stages

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Aspen Technology, Inc.

Aspen HYSYS Upstream

Heavy Oil Characterization

Oil & Gas feed with Assay Info (1) Assay information from the Assay Library - Assays are categorized by geography Once Assay is selected from library, it needs the following information to be entered to characterize the Oil & Gas feed stream: ·"1'""'"·=!0..._ ~ - Density ·I iiJ

- GOR, WOR - Gas composition

Also needed: - Number of stages - Temp & Press. of stages

Oil & Gas Feed with Assay Info (2} View Details button allows the user to edit the assay accessed from the library r Worksheet l~~~'~.~~li?r~j~!l __ I Worksheet j Oil & Gas Feed with Oil A>sav I ,,,. !,.

r

I /I

Condition~

Properties Composition Oil & Gas Feed Petroleum Assay K Value User Va1iables

Notes Cost Parameters Normalized Yields

- _ _ _ _ _ _ _ _ _ _ _ _ _, Prop_e_fti~s

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""M.

_q, Vol%

'Volume%

'Region:

· Countiy:

North America Canada

:Assay:

Bow River He.w

c :[

''''''''''''''''''' Select Assay

HJ

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Gas Composition ·'.'}Mole% (' Mass%

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Methane

!>.0<100

£tl1ane

0.0000

Propane

0:0000 0.0000

i-Butane

n-Bulane i-Pentane n-Pentane

0.0000 0.0000 0.0000

GOR Specification --

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Heavy Oil Characterization

Aspen HYSYS Upstream

Oil

Gm;

fe~~d

with Assay Info (3)

Assay data can also be manually defined Uses Macro Cut table for data entry - Specify distillation data, light ends, and any known crude properties such as density and sulfur content ... ~--- .......... 0 ~·~~

0.«wl"'-

., '''"""·~·

Heavy Oil Characterization Workshop Introduction to the basics of modeling well head fluids using Oil & Gas Feed capabilities

-+

Reservoir1

-+

Reservoir2

-+

Reservoir3

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Heavy Oil Characterization Workshop

aspen

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Heavy Oil Characterization Workshop Objective After completing this workshop, you be able to conduct the basics of modeling well head fluids using the Aspen HYSYS Oil & Gas Feed capabilities. The workshop assumes the user already has some familiarity with Aspen HYSYS. In this module you will learn different ways of modeling reservoir fluids using the Oil & Gas Feed option.

Description In order to model a produced oil and gas fluid, a computer program must faithfully

simulate the vapor-liquid equilibrium (VLE) and fluid property characteristics of the fluid. There are various methods used to characterize the VLE and fluid properties of oil in computer simulations. The choice of method depends largely on the data available to the modeller, which may be limited to simple field data or include detailed lab analyses. The four basic oil characterization methods available in Aspen HYSYS are: • User Defined Hypothetical Components • ASTM Crude Assay Characterization (part of the Crude Option which is included in the HYSYS Upstream Option) • PVT Characterization (part of the Upstream Option) • Oil & Gas Feed option (V7.3 and later versions) • Neotec Black Oil Models (a third patty software integrate with Upstream Option) A heavy oil model is made up of three bulk phases - oil, water, and gas - and with no detailed composition except the gas. Aspen HYSYS offers two options to handle heavy oil. One is Oil & Gas Feed option. The other option is developed by Neotechnology Consultants Ltd. ("Neotec"). Oil &Gas Feed: Starting from V7.3 version, Aspen HYSYS Upstream offers its own heavy oil modeling capability. It is called Oil & Gas Feed option. You can use it with or without any distillation I assay data of the oil. You can also use an assay databank to choose a library assay data. This databank is added in V7.3 version as well.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

Workshops

Resulting Calculations: Physical propetties will be calculated for each phase (for example, viscosity, surface tension, specific enthalpy). VLE related calculations are also done (for example, solution GOR), as are other related calculations of interest (for example, Oil Fonnation Volume Factor). (NOTE: literature often uses the following symbols: Rs = SGOR = solution Gas Oil Ratio, Bo= Oil FVF =Oil Fonnation Volume Factor)

Heavy Oil Considerations When Defining Your Simulation Basis: • Heavy Oils Input-Oil & Gas Feed requires various bulk properties: density of the oil, GOR, WOR, and Watson K. There is a table in the Oil & Gas Feed interface to provide gas composition. • A Component List is Required-The internal workings of Aspen HYSYS require that all fluid packages have both a component list and a property package. Moreover, the bulk data of heavy oils are translated into compositions by HYSYS. Starting with a default upstream component list, UpstreamComps.cml, is recommended. In these methods, PVT lab analysis or ASTM crude assays (i.e., boiling point curves,

property curves) of the production fluid are used to generate and characterize hypothetical oil components. Whereas Black Oil infonnation is usually used to describe upstream oil assets, PVT lab analyses are common in upstream gas and condensate production, and crude assays are common in the downstream industry. This module deals with Black Oil methods only. PVT and crude assay oil characterization methods are covered in depth in other training materials. This workshop includes the following tasks: • • • •

Task l - Define the Simulation Basis Task 2 - Oil & Gas Feed Bulk Properties Task 3 - Oil & Gas Feed with Assay Task 4- Oil & Gas Feed with Macro Cut Table

Task 1 - Define the Simulation Basis As mentioned previously, even a Black Oil property package requires a component list. You will how to import the prebuilt upstream component list, upstreamComps.cml. It consists of light end components that might be found in a typical gas analysis and hypothetical components for heavier hydrocarbons. o

Statt a new case by clicking on New in the start page or by going to File menu New or by pressing Ctrl+N.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Open ]New New

Open

In the Properties envirorunent, click the Components folder in the navigation pane. Click on Import button and open UpstreamComps.cml file from Paks folder.

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When you click on Import button, HYSYS opens the Paks folder by default. If it does not, browse to the folder [root]:\Program Files\AspenTech\Aspen HYSYS (version)\Paks and open the component list. o

Double click on Components folder to expand it. Click on Component List -1 to view the component list.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

''"•

Workshops

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Right click on the component list name, Component List-I, click on Rename and rename it to Upstream.

Component Lists:

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AU Items

.

Component List. - 1

<

Properties

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L.~ ;~~op:::;ge; .Lict_,. ~~en

Source Databqnk: HYSYS

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Click on the Fluid Packages folder and click on Add button to add a fluid package. The Fluid Package view appears. In the Property Package Selection group, select Peng-Robinson from the list of available property packages.

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PropBtieos

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Pacb19eType:

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Readiom Ce, Ccmpcnent Maps ,:-::i, U>e• P1operties

Proputy Pac~ge Selection faso Tab<1lar f!.te11ded NRTt

GCEOS GMualNRTl Glyrn1' Package Gmys<:<~ St'Eed Kobod1-Donnet

1ee·Kesier-Piocker Marg!l!f> Mfl!//R

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I Modify Tc, Pc for Hl, He llmlexcdVk;cosity

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Surface Tens1on Method

NB-SStt>om NRTL

lhermal Conductrvlty

OLl_fi<'ctrol;.-te PM9-Robi•»M PR-Twu PRSV

©2014 AspenTech. All Rights Reserved.

..............

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5

Parameters Property Pac~ EOS

Costa Id Modify Tc, Pc for H2. He

HY5Y5 Viscosify HYSYS Cubk EOS Analytical Metli<xl Default

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API 12A3.2-1 M~thod

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Modeling lleavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

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Workshops

Right click on the fluid package name, Basis- I, click on Rename and change the name to PR. Click on Simulation to go to simulation environment. _'} Properties

o o

Save your case by going to the File menu and choosing Save As. Save your case in a convenient location (i.e. the Desktop, an accessible network drive, or some local drive) and call it 01 Oil-Gas Basis.hsc.

Task 2 - Oil & Gas Feed Bulk Properties Next you will create a black oil stream to model an oil and gas reservoir. In this step, the procedure will be completed based on bulk fluid properties measured in the reservoir. You will also customize the stream property view to show various oil and gas properties of interest. Later in the workshop you will add additional Black Oil streams, all characterized in different ways. These streams will be used as feed streams for the next module. o o o

Add a stream to your simulation. Double click on the stream to open its property view. Rename the stream to Reservoirl by typing the new stream name directly in the Stream Name cell. Specify the following conditions: In this cell ...

Enter...

Name

Reservoir1

Temperature

15'C (59'F)

Pressure

7500 kPa ( 1088 psi a)

Aspen HYSYS assumes all the phases are in equilibrium and automatically assigns the same temperature and pressure to the Gas, Oil, and Water phases. o

Click on Oil & Gas Feed under Worksheet in the Stream Property view. There are two choices in the drop down list:

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

o

Workshops

Oil & Gas Feed with Bulk Oil Properties: Choose this option if you have no distillation I assay data for oil. You will use only bulk properties for the oil. Oil & Gas Feed with Oil Assay Info: Choose this option if you want to input assay information of the oil. There are two ways you can input assay information. • Choose one of the assay data sets from HYSYS assay databank. Starting from V7.3 version, HYSYS has a databank of oil assays for oil from all over the world. You will use one of the databank assays for Task 3 of the workshop. • hlput your own assay data in the Macro Cut Table. You will use this option in Task 4.

o

Material Stream: Reservoir1

m;;;~;k~h~~;r~i;;;;,~ril¥-;,~~~J . . Conditions Properties

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You will create Reservoir! stream without any assay data. Choose Oil & Gas Feed with Bulk Oil Properties from the drop down list. Specify the following black oil infonnation: In this cell ...

Enter ...

Std Liq Density

800 kg/m3 (49.94 lb/1!3)

Watson K

11. 1

Total GOR

120 STD m3/m3 (673.7 SCF/bbl)

Total WOR

0.1

Oil Flow Target

1000 m3/hr (1.51E+5 bbl/day)

Specify Number Of Stages= 2. Temperature of both stages is 15 °C (59 °F). Pressure of stage I is 7,500 kPa (1088 psia) and stage 2 is 101.3 kPa (14.7 psia). You will now enter composition of the gas under the Gas Composition menu of the Oil & Gas Feed page of the stream (not in the Composition page!). The mole fractions are given below. Enter the following composition for each component or copy and paste the composition from Reservoirs.xis file, which can be found in the same folder as your course workshop files.

©2014 AspenTech. All Rights Reserved.

7

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

a

..

Component

Mole Percent

Methane

80.0

Ethane

10.0

Propane

5.0

i-Butane

1.0

n-Butane

0.5

i-Pentane

0.5

n-Pentane

0.5

Hydrogen

0.5

H20

0.0

Nitrogen

0.5

co

0.5

C02

0.5

H2S

0.5

Workshops

The window should now look like the screen shot below:

M~\erilll Stteill'll: R~e~irt .

<

Wo~k~he~i1i~~hii!~-;:;t;T2Y~l;;;~:J ~-----------·

Worksheet

Oil & Gas Feed with Bulk Oil P1

Conditions Properties

Composition

Std Liq Density

800,0

Oil&Ga
11.10

Methane Ethane

User Variables

Propane

Notes

I-Butane

Cost Parameters

I

n-Butane

Normalized Yields1

i-Pentane

I

n-Pentane

·· GOR Specification -··-·-·--Number Of Stages Stg No

1 2

©2014 AspenTech. All Rights Reserved.

Press

[CJ

[kPa]

15.00 15.00

7500 101.3

8

•

====:::::--".:'.'.".'"'.:=::::::''

l-----------

·····-····-·-····-=·

2

·Temp

0.5000 0.5000 0.5000

Oil Flow TarQet Total GOR

1000 120.0

0

~;~~~~:_pensity ____ ~~o;~-

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

o

Workshops

Review Conditions and Composition pages on the Worksheet tab:

Mati!rial Stream: Rciffloirl WorhheetT ~·~t:i_,_~rn~~_[py~!-~~~i

r--·- --------·- --------------

Conditions

!~~;:~r ~~~ae1e frachon

Propert'es Compo;jtion

~~~~.=~:F:-=~.,,

Worhhed

Vapour Plia1e

liquid Phaoe

Aqueous Phase

0.0621

0.6354

0.3026

ITemperaturf [CJ Pre> sure fkPaJ

ReseEV<:>irl 00621 15.00 7500

15.00

15.00

15.00

7500

7500

IMolar Flow {kgmole/t.]

7500

1.885e+004

1170

1198:.... 004

570<

r.::

Material Stieam: R~rvcir1 Worksheet

[~!~~~~:~~ J~PJ-~i~~J

Worksheet

Mole Fractions

Conditions Properties Composition Oil & Gas Feed Petroleum Ass:ay KVa!u.e Us
co

0.0014

C02

0.0014

H2S C6-C10* c10-c1s· C15-C20'

0.0014 0.4155 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 Q,0000

c20-c2s·

I

C2S-C30' C30-C35'

(35-(40'

I

c4-0 .. •

Aque.

liq1.1id Phase

Vapoor Phase

0.0013 0.0019 0,0021 0.6539 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0098 0.0025

o.oo:o 0.0004 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000

0.0000

The Properties page of each material stream shows various physical properties /correlations at the current stream conditions. This listing of properties can be customized by the user. You will use the following procedure to customize your Properties page for the Rese1voirl stream. i~•'

o

Go to the Properties page. Click on the Remove All Correlations icon ( near the bottom. This will clear all correlations from the Properties page.

«;)( )

·Matrir Stte
!

!

'I

Reservoir!

Stream Name -~

Properties Composition Oil & Gas Feed Petroleum AS5
•

- Property Corre!at1on Controls -

[C.t_Bll • •

1!

1·

©2014 AspenTech. All Rights Reserved.

I •

9

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

o

Now you will add only a few prope11ies of interest. Click on the Append New

o

Correlation icon ( i:{1> ). Select the Oil Gas Feed category and the Oil FVF correlation. Click on the Apply button. GC

User

-------·-·---·--·-·-·-·---·--··-·-·-·-----·-----·-··---·-··---·--·-····-

Plot

YI

El [

o o

I_·_ _ _ _ _R_e_se_rv_o_ir_l_ _ _ _

~J

"----C_l.o'-s~'--'-~J ~

Apply

Do the same to add Soln GOR and Soln WOR. Now select the Standard set and add Mass Density and Viscosity.

'Mat~al St;~.

Risew6ir1 .

-w~~h~~-;tT_~~~:;,i-~n~]Pi~~~!~1

Properili!s Compnsition Oil & Gas Feed Petroleum AsSff/ I( V3lue User Varillbles

Oil FVf!OGF] [STD_m3/m3] i So!n GOR{OGf) [STO_m3/m3J So!n WOR[OGFJ ! Mass Cv !li:J/~9-CJ i MMs Density {k9/m31

!

IVi
[cP)

Phij~e

Vapour Phase

liquid Phase

1.200 27A3

<empty>

<empty>

<empty>

<empt('

<empty>

9.888e-002

<empty>

<empty>

<empty.>

2.171

1.715

1.450

3.779

623.1

63.40

734.2

1017

<empty>

1.321e-002

0.'B90

1,1:~6

Worksheet Cond;tions

Aqueous

'<empty>

Notes

Oil Formation Volume Factor (FVF)-The Oil FVF is equal to the ratio of the volume of oil and solution gas at the given process conditions to the volume of dead oil at stock tank conditions. Solution Gas Oil Ratio (GOR)-The Solution GOR is a measure.,ofthe amount of gas dissolved in the oil at current process conditions. It is calculated as the standard volume of gas (such as the volume of gas at standard conditions) contained in one volume of oil (for example, SCF/bbl or STDm3/m3). At high pressures, where all of the gas is dissolved in the oil, this ratio will be nearly equal to the Produced GOR; at low pressures, the Solution GOR will near zero. WOR- A ratio of the water volumetric flow to the oil volumetric flow. o

Save your case as 01 _Oil-Gas Feedl.hsc.

©2014 AspenTech. All Rights Reserved.

10

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Workshops

Task 3 - Oil & Gas Feed with Assay In this portion of the workshop, you will create another reservoir stream, this time by

making use of oil assay data. Your assay data will come from a built-in library within Aspen HYSYS of various assay samples worldwide. o o o

Add a new stream and name it as Reservoir2. Select Oil & Gas Feed with Oil Assay Info in Oil & Gas Feed from the drop down list. Define the stream with the following infonnation: In this cell...

Enter ...

Worksheet. Temperature

20°C (68°F)

Pressure

7000 kPa (1015 psia)

Target Oil Flow

1000 m3/h (1.51E+5 bbl/day)

Std Liq Density I Stock tank density

900 kg/m3 (56.19 lb/ft3)

GOR

180 STD_m3/m3 (1011 SCF/bbl)

WOR

0.1

Compo$ltlon (mole percent) Av<1ilable In Reservoir corrtposition.xlsx file Methane

70.0

Ethane

20.0

Propane

5.0

i-Butane

1.0

n-Butane

0.5

i-Pentane

0.5

n-Pentane

0.5

Hydrogen

0.5

H20

0.0

Nitrogen

0.5

co

0.5

C02

0.5

H2S

0.5

©2014 AspenTech. All Rights Reserved.

11

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

o o o ,_

Workshops

Specify Number Of Stages= 2. Temperature of stage I is 20 °C (68 °F) and temperature of stage 2 is 15 °C (59 °F). Pressure of stage I is 7,500 kPa (1088 psia) stage 2 is 200 kPa (29.01 psia). Click the Select Assay button. Select North America for the region and USA for the country. Select the West Texas Intermediate assay and click Import Selected Assay. The stream should be solved. Review its conditions, properties and composition pages. You may want to customize the properties page. -''"'""'"

M..terl~fl>t~eaifl: Res~nioitt

W~rksheet IAttach;;;;·::'~ts::-::'j".:~Dy::'..'::~n=.~=·,;;-=ic=·;=J==··=·=·::::···::::...:::..·::::···::::.. ·::::·:::: Worksheet

i-Oil & Gas Feed with Oil Assav I Y; ~

Conditions Properties

Gas Composition ·"··---·----------

Mole%

· ,9!1 prop,<'rties

1

:1 Mass%

Com pos.ition

Oil & Gas Feed Petroleum Assay

KValue User Var'1ables

1i:j'1

Vol%

Volume%

Region : Country : [ As5ay ;

North America USA West Texas Inte

Notes

Cost Paran1eters Normalized Yietds; Vi~Det~ils ~GO R Sp-etification

Number Of Stages Stg No 1 2

70.0000

Ethane

20.0000

Propane i-Butane

5.0000 1.0000

n-Butane i-Pentane

0.5000 0.5000

n-Pent~ne

0.5000

,

-·--·------·-- -

2

Temp

Press

[CJ

[kPa]

20.00 15.00

Methane

7500 200.0

Oil FlowTaraet Total GOR Total WOR Stock Tank Densitv

1000 180.0 0.1000 900.0

Note: The Oil Flow Target and Stock Tank Density fields may clear out after selecting the databank assay. If so just re-enter the values provided earlier and the stream should calculate. o o

From the Tools menu, choose Preferences. Click the Variables tab and select the SI unit set.

o

Save the file as 01 Oil-Gas Feed2.hsc.

©2014 AspenTech. All Rights Reserved.

12

Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Task 4 - Oil & Gas Feed with Macro Cut Table Next, you will install a Reservoir3 stream with all conditions the same as Reservoir2, except for the assay data. You will input your own assay data manually using a tool called the Macro Cut Table. The Macro Cut table is a feature that allows for greater flexibility than the standard HY SYS Oil Environment for the specification of crude oil assays. It is also used with the Aspen HYSYS Petroleum Refining functionality. You can utilize the Reservoirs.xis file included with the course workshop files as the source of your assay data. o o

Create a new stream and call it Reservoir3. Provide the following inputs for the stream (same that were used for Reservoir2): In this cell... Worl<shijijt

Enter ... .

·.

.·

..

.

Temperature

20°c (68°F)

Pressure

7000 kPa (1015 psia)

Target Oil Flow

1000 m3/h (1.51 E+5 bbl/day)

Std Liq Density I Stock tank density

900 kg/m3 (56.19 lb/ft3)

GOR

180 STD_m3/m3 (1011 SCF/bbl)

WOR

0.1 " -:--, ,, __ : ,: ' Composition (mole percent) Available in Reservoir composition.xlsx file ,,,

''

'

.

,

Methane

70.0

Ethane

20.0

Propane

5.0

i-Butane

1.0

n-Butane

0.5

i-Pentane

0.5

n-Pentane

0.5

Hydrogen

0.5

H20

0.0

Nitrogen

0.5

co

0.5

C02

0.5

H2S

0.5

©2014 AspenTech. All Rights Reserved.

'

13

,

"

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

Specify Number Of Stages= 2. Temperature of stage I is 20 °C (68 °f) and temperature of stage 2 is 15 °C (59 °f). Pressure of stage I is 7,500 kPa (1088 psia) stage 2 is 200 kPa (29.01 psia). To access the Macro Cut table input, click the View Details button on the Oil & Gas Feed page.

o

lhc:.OCuto..to1 Sin~ ·RU~

Spec•~cohon ! Settmg; j Note• I Sptt1flullon As.,,y Property

I

l•ght fod< 1·011 & Ga• Fee
Q.,t.llat o~ I 0 ,i.1;,11on Type

AnllinePaint

Import/Export

'-"'"!~_':!.~~~-

L ·--~.?.2.~~......J

}Autc-uku!ote

wher.ever

o o o

"I'"' ch•ng"'

Open the provided Reservoirs.xis file and review the data. Note that there are eight cuts listed in the table. Type 8 into the Add Dist Data field to account for eight cuts in the Macro Cut Table. Click the Add button. -

_ Oistil!ation Type

TBP

~i

Yield Basis

Cut Width

(Cl

----- -

.,

[-

--

Add

Dist1lfation Yi~!d Distil'alion Temp (\1011.>me %) (Cl <empty> <empt'/> <empty> <empty>

<::

<empty•

<empty> <empty> .:empty>

<empty> ~empty>

~./) T1a11~pose

--

Amlin
liquid Volume

<empty> <emply> <empty> <empty> <empty> <empty>

<empty>

.:empty>

<empty>

<empty>

<empty>

<

<empty>

<empty>

<empty::.

<empty>

Table

D1st11fabc11 Points Add Dist Data

0

, Import/Ellport

1m.~.~.~r~,

1 .. ·. • ~

·./C ""·····'·· "J .. \ . r

©2014 AspenTech. All Rights Reserved.

14

-J

L-----~~~~--J I

Aspen Technology, Inc.

Modeling 1-Ieavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

o o

o

Change the Yield Basis to Liquid Volume. This matches up with the data provided in the Excel spreadsheet. Select Liquid Density from the Petroleum Property drop down list (near top right corner) and click the Add button next to it. Add the remaining properties the same way. Maintain the order of the prope11ies the same as in the Excel file for convenience. The table now looks like the following figure:

·~

..

o

o o o

o

Workshops

..,,...

...

... .,...,. ..,.., . .......,..,, ,.,,

.. ..,, ,

•A•

-·· --....

·~

...

Now you can enter the data from the Excel file by copying and pasting into the table. To copy, highlight the green part of the table (Distillation temperature through Aniline Point) and press Ctrl+C. To paste, click on first cell under Distillation Temp and press Ctrl +V. Select the Light Ends fonn and uncheck the Input option. This will maintain the inputs from the Oil & Gas Feed page. The assay should be solved. Review and conditions or properties of interest. Select Tools> Workbooks and view the HYSYS Workbook. Use this to compare the conditions, properties, and compositions of the three Reservoir streams. Save your case as 01_0il-Gas Feed3.hsc.

©2014 AspenTech. All Rights Reserved.

15

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Pipe Segment

Pipeline Simulation Using Pipe Segment Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objectives

Add and connect a Pipe Segment to build a flowsheet in Aspen HYSYS Upstream Explore pipe segment results and flow assurances

Workshop: Use the Pipe Segment to simulate a pipeline

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Pipe Segment

Summary of Available Pipe Options (1) Pipe Segment - Standard feature in HYSYS - Optional add-on license to use OLGA 2-phase, or 3-phase correlations

Compressible Gas Pipe Pipe included in Valve (shortcut option for Dynamics) - Requires HYSYS Dynamics license

PIPESYS - Requires separate PIPESYS license from SPT Group

Links to Pipesim and Prosper/Gap - Requires HYSYS Upstream license and separate license from Schlumberger

Summary of Available Pipe Options (2} Aspen Hydraulics - Requires HYSYS Upstream in Steady State and Aspen Hydraulics license in Dynamics

Link to OLGA - Requires HYSYS Upstream from AspenTech and OLGA license from Neotec

©2014 AspenTech. All Rights Reserved.

2

Aspen Technology, Inc.

Aspen HYS YS Upstream

Pipeline Simulation Using Pipe Segment

HYSYS Pipe Segment PIPE-100

Production

To

Fluid

BaUery

Part of standard HYSYS Steady State & Dynamics for modeling process piping and transport pipelines Needs feed and product streams, plus an Energy stream Represents "multi-segment" single line Segments can be pipes (different lengths, elevations, diameters) or fittings

r:,

9

6

2 __ 3 ____.,, ~========::::1x1

L4

HYSYS Pipe Segment Limited network capabilities For a single pipe you can specify two out of P; 0 , Pout & Flow Rate Alternatively, give all 3 (P; 0 , Pout & Flow) and it will calculate pipe length (for single segment only) For a single branched system of 3 pipes specify, for example, Pl & the inlet flows Calculates P2 Set mixer to equalize pressures, therefore P3 = P2 Calculates P4 and then PS P1

©2014 AspenTech. All Rights Reserved.

P2

3

Aspen Technology, Inc.

Pipeline Simulation Using Pipe Segment

Aspen HYSYS Upstream

HYSYS Pipe Segnient

Limited network capabilities A typical gathering network will have well flows that depend on the back pressure of the network and a discharge pressure. Limited network models can be done with Adjust blocks to balance pressures (use Simultaneous Adjusts) A network that gathers more than five wells is usually slow to solve - Could have more wells with some flows fixed

HYSVS Pipe Segment

Can model single phase and multiphase - Wide choice of multi phase correlations (see documentation

for details) Can model heat loss in detail Can estimate heat transfer coefficient with fluid + metal + 1 layer of insulation

..,......,_ ........ '"""";'""l•~-·l,.,•"'""'''"'"'"".... ;~lc.,.;..; ...... ·-~·/

Ambient medium can be Air, Ground or Water - Alternatively enter a coefficient

for pipe, or for each segment - Or, specify heat loss (duty)

©2014 AspenTech. All Rights Reserved.

4

Aspen Technology, Inc.

Pipeline Simulation Using Pipe Segment

Aspen HYS YS Upstream

HVSYS Pipe Segment Runs in dynamics, but does not consider phase slip Option to use OLGA 2-phase or 3-phase correlations in Pipe Segment p~~ ~1'5'Hro The pipe model -"'"!-' -ru,,_"9_r...-.""'h..1_ff-..f.,,.,.~rf"',:""-..,~~ro:,....,,..,. can predict Coe::'"' l~~~j~~''°p",(o"'~'"" typical slug length ~:::.'.:: ( , •'«t·<>'f'poH;,,(c.. ... >l>O and frequency ;..:;:: •.• rn.fu\S lP Not« ..

~

i

·QlGAS lP

HVSYS Pipe Segment Improvements

Improved flexibility in assigning pipe flow correlations - Can now assign different pipe flow correlations to different segment orientations (vertical, horizontal, inclined)

(·-"~""""'

;

''"""'~'

I;;:::,:_~,

~:'.~-'~~= ··}•· d,f?]~1i~~:~"'

h

directions

,.,;.., '"'"'"'"'"""

,>ms.uo""'"~

,.,,,,.~

'.,,,:

""''° "''

©2014 AspenTech. All Rights Reserved.

5

Aspen Technology, Inc.

Pipeline Simulation Using Pipe Segment

Aspen HYSYS Upstream

Pressure Drop Correlations and Usage Model

Aziz, Govlf)r & Fogarasl

Horizontal Flow

11£MIJM&&Jl£MM&IJ&!M&

Use with Care

"'

Yo;

Baxendell & Thomas

y"

No

N•

BegQs'&.Brlll (1973)

v..

v..

Yo$

Yes

Beggs&: Brill (1979)

Yes

y"

y.,

Di,ins&ROS

No

y"

"'

No

"'

"' "'

No

Yes

y.,

"' No

HTFS Homogeneous

Yes

No

Y.s

No

OLGAS 2-Phase

y" y,.

"' y,.

No

HTFS liquid, $1ij>

y.,

Yes

Yes

OlGAS 3-Phase

v..

"'

y.,

Yes

"' v..

"' No

Yes

No No

y"

Yes

"'

Gregory, Aziz, Mandhane Hagedorn &'Bi"oWn'

Orklsewskl P0ettinali

'a ca'rpei1tet

Tulsa 99

N•

No

"'

Yes

No

New f1.111ctio11ality for Pipeline Modeling Available starting from V7.3 CP1 Flow Assurance -

C02 corrosion rate profile Erosion velocity profile Hydrate formation profile Slug flow Wax deposition

Emulsion Viscosity Models - Several options for calculating viscosity of combined oil and water phase

Tulsa Unified Model Correlation - New correlation for HYSYS pipe and Aspen Hydraulics

~aspfl!'\lech

©2014 AspenTech. All Rights Reserved.


6

I

12

~NJE.

Aspen Technology, Inc.

Pipeline Simulation Using Pipe Segment

Aspen HYSYS Upstream

flow Assurance Ensure successful and economical flow of multiphase fluids from reservoir to point of sale Often dynamic modeling techniques employed Unstable flow

Wax/Hydrate tormauon

(•lugging)

• Instability of waves at gas~Uquld

interface

caused by

hydrodynamic factors or terrain •Create significant pressure fluctuations •Disturb receiving/separation facllltres

Asphaltenes •Deposition of high

•Precipitate to block pipe •Temperature maintenance

molecular components

•Most common In

heavy olls

• Remediation often requires production stoppage so need to minimize frequency

and length

~

•

~

"

In oil/gas industry, lost production cost can dwarf Installation cost

flow Assurance New Flow Assurance tab on HYSYS pipe, Hydraulics pipe, and Hydraulics complex pipe Analysis tools available on flow assurance tab

iI'"'"

'-~:

------- -------

,'-~.: '""+---+--+'.,..""'11"'""1 t.,,..,,, P..1.,Jr>-n,,,,.,..-0

©2014 AspenTech. All Rights Reserved.

7

'I'.'

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Pipe Segment

flow Assurance Analysis Tools

Hydrates (>" \'•eW pre>~t~

j

,fy·n'"'"·'.·~::'.~~:r::~) Slug Analysis Wax Deposition '''""""'"~'""'" '"""·~"'~~""'"'

'•

ilf,fj

m•

'"

;.:90 .:90

,,, '"""

'"

Emulsion Viscosity Models Available to Properly Account for Oil-Water Mixtures User has options for how viscosity is calculated for emulsions in HYSYS Pipe Segment and Hydraulics subflowsheet

Methods Available -

Simple Volume Weighted

-

HYSYS

-

Brinkman Guth and Simha Levinton and Leighton Barnea and Mizrahi General Polynomial

©2014 AspenTech. All Rights Reserved.

~!':i~i~!!:T~~-~_!TI~~~!:-~i.ifi?i~J __ _

!

De>_Jg_n

_ :·Emul>"><>Vi>
1 • (00.necnons

~.

Ret

Vosrn5'~/=

l + H *VJ+ n 'Vf'2

~

K3 • V/'3

Vf = Ois;>Etsed f'ha<e Vol- FrgcMrt

Notes

! Kl

Iu

1~

2.~00 1.410

I

_o~ .. 1

·a_Si!Oii'

8

"'i

1

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Pipe Segment

rulsa University fluid flow Project (TU ff P) AspenTech joined the TUFFP in 2011 to gain access to the latest multiphase pipeline flow research and collaborate with leading researchers in both industry and academia Cooperative industry-university research group for 35+ years Major deliverables -

Software for different multiphase flow applications Experimental data and analyses Access to facilities for possible contract projects Platform to exchange information and Ideas on multiphase flow practices Personnel training through resident education and short courses

Member companies/organizations: -

-

AspenTech, Baker Atlas, BP Exploration, Chevron, ConocoPhillips, ExxonMobil, GE Oil & Gas, JOGMEG, Kuwait Oil Co., Marathon Oil, Petrobras, Schlumberger, Shell Global Solutions, SPT, Total Bureau of Ocean Energy Management, Regulation, and Enforcement (BOEMRE)

New Tulsa Unified Correlations in HYSYS Compared against field operational data from European company No significant differences between Tulsa and OLGAS correlations

.J

Mixing correlations for vertical and horizontal orientation is useful to match plant data Interesting tuning discovery - use wax deposition thickness to tune the pipeline pressure drop (assuming wax deposition is likely) ModelO~U

Plant Data ~Perlment

n

"

Well1

Well2

We111

WeH2

Pre,.ure

Pressure

Pres.sure

w" Pressure

'"

'"

'"

'"

w"

--

30.18 30.18 30.18 30.1 H.27 33.27 33.2 H.2

©2014 AspenTech. All Rights Reserved.

w"

W" 43.5 43.5 43.5 43.5 43.S 43.S 43.S 43.S

30.39 30.34

38.5

olruLSA 3P OloLGAS 3P

33.45 34.39

OITIJL5A for Vertical, HTFS for horizontal & In dined 4ITTJL5A for Vertical, HTFS for horizontal & Inclined OhiH5A3P OinLGAS 3P

37.81 43.42

17.S hiJL5A for Ver\l
42.05 41.6

9

Commeab

Waxlaver

mm

36.01

33.6 33.6 30.06 29.84 32.82 32.82

Pipe from Well2

1thiJL5A for Vertical, HTFS for horizontal & Inclined

Aspen Technology, Inc.

Pipeline Simulation Using Pipe Segment

Aspen HYSYS Upstream

Pipe Segment Workshop

Model a combined well flow through a pipeline using the Aspen HYSYS Pipe Segment Model Discover the new Flow Assurance capabilities in HYSYS

Reservoir1

PIPE-100

To Battery

Production Fluid MIX-100

Plpe-Q

Reservoir2

©2014 AspenTech. All Rights Reserved.

IO

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Pipeline Simulation using HYSYS Pipe Segment Workshop

aspen·

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Pipeline Simulation using HYSYS Pipe Segment Workshop Objective In this module, the Oil & Gas Feed streams produced from the first two oil and gas reservoirs are blended into one production feed stream. The blended production stream is then fed through a pipeline. You will model the pipeline using the HYSYS Pipe Segment unit operation. You will explore the various results, including flow assurance calculations.

Description The Aspen HYSYS Pipe Segment is the standard unit operation for single and multiphase flow calculations in Aspen HYSYS and HY SYS Upstream. It is best suited towards single pipe models, or small-scope networks. Larger piping networks will be better modelled by the Aspen Hydraulics sub-flowsheet - which you will leam about later in the course. The Pipe Segment consists of various multi-phase correlations that can be employed for different directions of flow (beginning with HYSYS V7.3). It allows for a multisegment construction easily facilitating the inclusion of fittings and custom piping arrangements. You can also specify heat transfer parameters in varying degrees of detail.

This workshop includes the following tasks: • • •

Task I - Install the Mixer Task 2 - Build the Pipe Segment Task 3 - Results and Flow Assurance

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Task 1 - Install the Mixer You will make use of the Oil & Gas Feed streams you built in the previous workshop for this exercise. The first two streams, Reservoir! and Reservoir2, will be combined and studied in the Pipe Segment. o

o

Open the case 01_0il-Gas Feed2.hsc. Use the Save As c01mnand from the File menu to save the case under a new name: 02_Oil-Gas Pipeline Starter.hsc.

o As with streams, there are a variety of methods to add unit operations in Aspen HYSYS: 0

o o

To Use... Menu Bar

o o

o

Workbook

o o

o

Object Palette

o o

o

PFD/Object Palette

o

Do this ... From the Flowsheet menu, select Add Operation or Press F12. The UnitOps view appears. Open the Workbook and go to the UnitOps page, then click the Add UnitOp button. The UnitOps view appears. From the Flowsheet menu, select Open Object Palette, or press F4. Double-click the icon of the unit operation you want to add. For Upstream Unit Operations use Shift+F6 Using the right mouse button, drag and drop the icon from the Object Palette to the PFD.

You will begin building the flowsheet by first adding a Mixer operation to combine the flows of Reservoir! and Reservoir2. o

Add a Mixer operation to the PFD in your preferred mode.

!

!Parnrnet~rs User Variables: 'Notes

---.D,...______. . Outlet

Inlets <:<:Str~~m rel="nofollow">>

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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Select Reservoirl and Reservoir2 as the Inlet streams. Type Production Fluid into the field for the Outlet stream. Since Aspen HYSYS recognizes that there is no existing stream with this name it will create a new stream with the name you have supplied. M'i)('er. Mix-loo

c--Cksi9tl--~ti~I\i;;rb.~~l~~-~-~J. Design

Name

MIX-100

· Connections Parameter~

User Variables: Note~

Outlet

Inlets

Production Fluid

Reservoir! Reservoir2 <<Stream>>

o o

Fluid Package

The Mixer is now completely defined. Click the Parameters page. Leave the Automatic Pressure Assignment at its default setting of Set Outlet to Lowest Inlet. In this case, lowest inlet pressure is 7000 kPa, so the outlet stream is set at 7000 kPa.

Note: The alternate approach, Equalize All, would set all streams to the same pressure. Therefore if two streams are specified with different pressures a consistency error would be generated. Only use this approach ifyou have only specified one stream pressure. o

To view the calculated outlet stream, click the Worksheet tab and select the Conditions page:

MiXer.

e~-~!~D.:I.~~!,~~-~k~h?~~f!l_ict_I Worksheet

Name

!Conditions i ' Properties !

Vapour

I

Composition PF Specs j

Res:ervoirl

Res:ervoir2 Production Fluid

0.0621

0.3410

0.1992

Temperature (Cl

15.00

20.00

19.40

Pressure {kPa]

7500

7000

7000

1.88Se+004 L011e+006

1.690e+004 1.135e+006

3.57Se+004 2.146e+006

1415 ·2.079e+005

1543

2958

-2.406e+005

-2.233e+OOS

Molar Flow [kgmole/h} Mass Flow [kg/h} Std !deal liq Vol Flow [rn3/h} Molar Enthalpy [kJ/kgmo!e]

83.71

145,l

113<9

-3.919e+009

-4.066e+009

-7.985e..i- 009

Molar Entropy (kJ/kgmole-C] Heat Flow [k.J/h]

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Task 2 - Build the Pipe Segment The Pipe Segment is used to simulate a wide variety of piping situations ranging from single/multiphase plant piping with rigorous heat transfer estimation, to large capacity long pipeline problems. You can choose from common pressure drop c01Telations including those developed by Gregory, Aziz, and Mandhane, and Beggs and Brill, as well as a large number of specialty pressure drop correlations. The OLGAS correlations (licensed separately) are also available as a gradient method. Consult the online help and the manual for more information on these methods. To solve the pipe, you must supply enough information to completely define both the material balance and energy balance. The pipe segment offers four hydraulic calculation modes: Pressure Drop, Flow, Pipe Length and Pipe Diameter; the appropriate mode will automatically be selected depending on the information supplied. There are four levels of complexity in the estimation of heat transfer, allowing you to find a solution as rigorously as required while also allowing for quick generalized solutions to well-known problems. Each pipe segment can represent a single continuous branch of pipe and may contain multiple sub-segments to represent the various elevation rises and drops that occur over the length of that pipe. CJ

Add a Pipe Segment from the Object Palette. Double click on the Pipe Segment. The Pipe Segment property view appears.

Plpec sEigmetit! PiPE-100

Desig 11 --[~~-~~J-~~X~~~~I~~~!~~-~~]!~~~~~~~5-~J--~~~-~~~J Oe!!;i9 11

Name:

l

PIPE-100

!Coonections Parameter!>

Calculation Emulsions Userl/ari

Inlet

Outlet

Notes

-~() Fluid Package

Delete

CJ

Energy

iiiiliiliillliil•llliliililllllllilllliliillllliiillllliiiliilllliiliill ;:·;

Ignored

Complete the Connections page as shown below:

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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Pip··~·"· pjp~. !00

Desig~---;-·R~-~~]~~~~~~~t "fiel!~f~~-~~:I£!.~~~~-~~~~~~J.·jiY~~i~J Name~

DMigll Connections Parameters Calculation

PIPE-100

Inlet

Emulsions i 1 User Variables I

! Notes

Outlet

Production Fluid

I

{)

I

Fluid Package

Energy

·

c•1;~~
PR

o

__::-_:]

On the Parameters page you can select the gradient method that will be used for two-phase (VL) flow calculations. For this exercise, select the Beggs and Brill (1979) correlation for all directions of flow.

Note: The pressure drop for the pipe can be supplied on the Parameters page. In this example, it will be left empty and be calculated.

o

Select the Rating tab and view the Sizing page.

Note: On the Sizing page, you construct the length-elevation profile for the Pipe Segment. Each pipe section and fitting is labeled as a segment. To fully define the pipe sections segments, you must also specifY pipe schedule, diameters, pipe material, and a number of increments.

o

o

For this pipeline, there is only one segment. Add a segment to the pipe unit operation by clicking the Append Segment button. Specify the following information for the segment: In this cell...

Enter ...

Fitting/Pipe

Pipe

Length

500 m (1640 ft)

Elevation Change

0

Nominal Diameter

508 mm (20.0 in)

Schedule

40

To access the nominal diameter and pipe schedule inputs, click the View Segment button.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

=

~ Pipe Info: Pipe Segment' PIPE-100

~

@]

Pipe Parameters -------s~;~a~1e40·1

i Pipe Schedule i Nominal Di<1meter

508.0000

!Inner Diameter

477.8248

~~l:2~~~e;

! Pipe Material

iRoughness

i Pi_pe W~JI Conduc_~-~ity

. 1

JI

45.000

Available Nominal Diameters

o o o o o

25.40

152.4

38.10 50.80

203.2 254.0

76.20

304.8

101.6

355.6

406.4 4572

~ -~~-~--1

508.0 609.6

Select Schedule 40 as the Pipe Schedule. Select the nominal pipe diameter as 508.0 mm (20 inch). Click on the Specify button. Use the default Pipe Material, Mild Steel and the default Roughness, 4.572e-5 m (0.0018 inch). Leave the Pipe Wall Conductivity as default at 45.00 W/m-K. Close the Pipe Info view. When the segment has been added and defined, the view should look like this: l?itfi! Segmehti: PIPE-l(IQ

JE~~~~:iJ-- -R~lin 9 ~~~-ksh~~~[~~i~!~~~~J.}~?_~_:':.~~,-~~~1.~~-~~~~J

I

Rating

Sizing

I

1

Segment

1

Heat Tranderi

Pipe 500.0

Fitting/Pipe length/EquNalent length

0.0000 508.0 477.8

Elevation Change

I

Outer Di
Mild Sted .J572e·005 d.5.00

Material Roughnes~

Pipe W
5

Increments

-<empty>

FlttingNc

[~=~~~~~~~~-~~~--_J

[

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r

View Se9r11ent.-

-------------~---~---

.I

··c1~~~S~~~ent

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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Workshops

Click the Append Segment button twice to add two more segments. Define them as follows: Segment 2 In this cell...

Enter ...

Fitting/Pipe

Elbow: 90 Std

Length Elevation Change

0

Outer Diameter

508 mm (20 in)

Inner Diameter

477.82 mm (18.81 in)

Segment 3 In this cell...

Enter ...

Fitting/Pipe

Pipe

Length

500 m (1640 fl)

Elevation Change

10 m (32.81 fl)

Nominal Diameter

508 mm (20 in)

Schedule

40

The Pipe Segment is not yet able to solve because we have not specified any information about the heat transfer properties of the pipe. On this page, you select the method that Aspen HYSYS will use for the heat transfer calculations. You have the option of specifying the heat transfer information by segment or overall. The following are the four available methods: Heat Loss Specified - If the Overall heat duty of the segment is known, the energy balance can be calculated inunediately. Each increment is assumed to have the same heat loss. Overall Heat Transfer Coefficient (HTC) Specified - If the overall HTC and ambient temperature are known, then rigorous heat transfer calculations are performed on each increment of the pipe. Segment HTC Specified - You specify the ambient temperature and HTC for each segment that was created on the Dimensions page. Estimate HTC - The overall HTC can be found from its component patts. o Inside Film Convection (Inner HTC) o Outside Conduction/Convection (Outer HTC) o Conduction through Pipe Wall and Insulation

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

o o

Click the Heat Transfer page. Select the Overall HTC radio button and enter an ambient temperature of 15.555°C (60°F) and an overall heat transfer coefficient of 1022 kJ/h-m2-C (50 Btu/hr-ft2-F). The pipeline is now completely defined and should solve. Save the case as 02_Oil-Gas Pipeliue.hsc.

o o

Task 3 - Results and Flow Assurance In this section of the workshop you will review some of the standard HY SYS Pipe Segment Results, such as pressure and velocity profiles. You will also look at the Flow Assurance options within the Pipe Segment, which are used to calculate items such as erosional velocity, hydrate fonnation, and slug flow. Go to the Performance tab and click on View Profile button. The table is shown partly in the following figure. Scroll to the right to view more profile results.

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Click on the Plot tab to view the profiles in plots. Select the radio button of a profile you want to view. Pressure profile is shown below.

l'!i>lil•V,..,'·P"''l't~~lOO

h~'® ""''""" -,°'P""·"'

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iqRo

\'•p'-'

''~"·'"'~',

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..................•.... ··············----·---

..

"""" "" ""'

©2014 Aspen Tech. All Rights Reserved.

................... ···-····

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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The HYSYS V7.3 CPI and newer versions contain many new improvements for the modeling of pipeline hydraulics, including substantial improvements in solution speed for steady-state flow networks, support of flexible boundary conditions, and new flexibility to model shut-in branches of a flow network. More information can be found on these improvements in solution 131579. Flow Assurance Calculations are available in the Aspen HYSYS Pipe Segment Model and the Aspen Hydraulics Pipe and Complex Pipe Models. The Pipe Segment model in HYSYS and the pipe and complex pipe models in Aspen Hydraulics can now check for a variety of potential flow assurance issues. These new features can be found on the new Flow Assurance tab within the pipe models. C02 Corrosion - The presence of C02 in a hydrocarbon pipeline can cause an undesirable deterioration of the pipe wall, and may ultimately lead to a catastrophic failure of the pipe. It is therefore necessary to predict the pipe wall corrosion rate caused by the presence of C02 in a hydrocarbon pipeline. The corrosion rate for a set of conditions can only be estimated by correlations. V7.3 CPI and newer versions include three C02 corrosion correlations: I. NORSOK Standard M-506 correlation developed with the support of the Norwegian Oil Industry Association (OLF) and the Federation of Norwegian Manufacturing hldustries (TBL). 2. de Waard Model 1995 correlation 3. de Waard Model 1991 correlation o Go to the Flow Assurance tab of the pipe segment. Select C02 Corrosion. o Check the box Do Corrosion Cale. Leave corrosion inhibitor and pH values as default.

·Hydrate<

iSlug Ana\~;<.

j

,w~~ °""°''tl
COtTosion Rate-Pipe length t::1·"

fv -

-4 lnp"t PH

!

i C~k

Cor r sion Rate

~ca I d Carros!

'

PH

PH~

·1

nRate

~

""" ' l"-e;

.

J.OO'J

"00-~

400.0

W
BOO.O

JOO
Pipe Length {m)

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Modeling Heavy Oil & Gas Production Facilities Using Aspen 1-IYSYS Upstreatn

Erosion - In multiphase flow through pipelines, the continuous impact of particles (liquids or solids) on the pipe wall surface can cause potential erosion problems. It is therefore imperative that erosion effects are considered when sizing and designing pipelines. The maximum fluid velocity in a pipeline to prevent erosion is given by: V1nax --

c * (Pm) .Q.5

Where Pm is the mixture density and C is an empirical constant based on the correlation chosen. Correlations supported in V7.3 CPI and newer versions include: 1. API-RP-14E Report- suggests a value ofC=lOO for solid free cmrnsive and continuous flow, and C= 125 for noncontinuous flow 2. Salama & Venkatesh ( 1983) - suggests a value of C=JOO The prediction of the erosion rate is suppo1ted in both the pipe models in Aspen Hydraulics and the HYSYS pipe segment model. o

Select the Erosion page and click the Do Erosion Cale checkbox. Keep the default API-14E Continuous service option. l'ipt Segmem: PlPE·100

: O_e$•Q~

i

Flow

J R_ating: I W~na~~w As•ur~,,~~mics_ !

Auur~ne
~
£ros:onol Vel"';ty Vrr""' =C/
,. Tab!e

I

fmp;rico! Con>tant

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~:

( "

100.0

fb/ft)'O.Sh

d:Dcho•ion~!E) Velocity-Pipe Loogth

I.

HN

=~~=~~--~--~-~ & Erno.lo~ Velocity

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+---1---t---+--+---

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ii i!

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;ooo ll--"'4=1F:+--'i'--l'--~-+---~---+ 0000

40CW

WU~

0000

Pipit lenqth (m)

Hydrates-The formation of hydrates in a pipeline can have a severe impact on the flow characteristics through the line, reducing the capacity of the pipeline or significantly increasing the pressure drop. V7.3 CP 1 and newer versions have the ability to predict hydrate formation throughout the pipeline, using the same capabilities that have been available within the HYSYS Hydrate

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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Formation Utility for streams. The prediction of the hydrate fonnation is supported in both the pipe models in Aspen Hydraulics and the HYSYS pipe segment model. o

:,

Go to the Hydrates page and check the Do Hydrate Profile Calculation box.

\
51S

11 Wax DepQ51tlon

Temperature-Pipe length 2-0.00

---- Tempe t"re Profile ---=-.!:b_~t

Fotmahc-n Tern >e.r11hm•

l'S<.00 _.,,__-n;;;;rp,..-~c+---1----+-----l · '1-- Type fl ----...____ ---~-- _

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I':: Low pressure, ~ 1 atm

i,''

High pressure. - 10000 atm

::-~,From

a correlation

) User input

rsoo -¥~-"'<~i-'"~--1-----l----!--===t . --:*-- !ce Fo ris F"st

;- 17.00

~

+·

---A--- Type. H

Typ<> 1 H

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0000

200.-0

&'.l(l_Q

1000

Pipe Length (m)

Slug Analysis - Pipelines transporting multiphase fluids (vapor and one or more liquid phases) can experience slugging behavior, especially when the pipeline's elevation varies significantly over its length. Under certain conditions, slugs of liquid can form in predicts slug properties for horizontal and inclined two-phase flows in each pipe segment. In V7.3 CPI and newer versions, the slug analysis functionality available under the Flow Assurance tab. The form has been redesigned to provide both the slug analysis tool options and results on a single fonn.

o

Go to the Slug Analysis page and check the Do Slug Calculations box. Once finished you can click the View Cell Plot button to view a detailed slug flow profile.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

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Pii"' S.!!"'ont l'lPOGO L>e<.gn j_ ~-"'"''I

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!),.,.,,,'<>.

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Wax Deposition - Wax deposits can form on pipeline wall surfaces, restricting the flowrate and increasing the pressure drop through the pipeline. In V7.3 CPI and newer versions, the wax deposition functionality available under the

Flow Assurance tab. The form has been redesigned to provide both the wax deposition input options and results on a single form. o

Choose Profes as designated correlation. Type 0 Int Dep Thick (Initial Deposit Thickness) for the whole pipe length. Leave everything leave everything else as default. - Pipe:Segtnent i>lP~-fl)o' -

[Ee_~ig_~L~~~J~o_r_~~h~!~__ j_P_e~~J flow AsstffillKe

Flow Asrnrnnce : OyoM11iC~ ;__ _

Deoosition Correl~tion

, limits I

C02 (om>
Vi
Prof!s

1-

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Maximum

-

~""'PIJ'>

10...erall Pressure Drop Total Deposit Volume

I

L_ _ _ _ _ _ _ _j

Wu Depositio'.!J>

!

; Simu;al1on Ti:'ne 881.0 kg/ml ·

Den~»ty

Therm.•I Cond.

0.2596 \Wm-K

[ v.eld Strength

2.C-6d kPa

576.5 kPa

<£r>1p:y>

7.246 m3

~e,,..pty>

~empty>

168.000CO

168:00.000

; Plug Presrnre Drop

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100.000

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200000 300.000

0.000000 0.000000

.100.000

0.000000

500.000 600.000

0.000000 0.000000

700.000

0.000000

Dep. Thick, {mm!

Dep. Volume

Oep. R.lte

[m3]

[kg/s·m2]

4.830321 4.774047

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3.9309&.•

0.709487

3.91567<

4.72522'}

0.702304 0.69523'>

3.90473E

.\.677190 4.629901 5.113101 5.069083

3.89366(

0.688274 0.759330

O.i52863

--~---·-~-·----------~·-

"' "' _J=========---=--=---=---=---=~ o

Save your case as 02_Oil-Gas Pipeline F A.hsc.

©2014 AspenTech. All Rights Reserved.

13

Aspen Technology, Inc.

Aspen HYSYS Upstream

Model Gas Oil Separation Plant

Model Oil-Gas Separ·ation Plant Modeling Heavy Oil & Gas Production and Facilities using Aspen HYSYS Upstream

learning Objectives Build a flowsheet based on Oil & Gas Feed inputs Review HYSYS process modeling using separators, heat transfer equipment, rotating equipment, etc. Add an HC Dewpoint calculation to a stream through the Correlation Manager Use the Adjust operation to meet a desired process specification

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Model Gas Oil Separation Plant

Process Overview

,, I

.:it-----:::..

Questions?

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Oil-Gas Separation Plant Workshop

aspen.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Oil-Gas Separation Plant Workshop Objective This module is a continuation of the Oil and Gas Feed simulation and Pipeline by Pipe Segment modules. You will model a two-stage oil-gas separation plant used to separate the gas, crnde oil, and water contained in the streams produced from the reservoirs. Each separation train consists of a 3-phase separator followed by some additional gas processing (a low temperature separator and compressor). The lean, dry gas produced must meet a pipeline hydrocarbon dew point specification before it is delivered to the gas plant for further processing. The crude oil extracted from the separation process is exported for refining. The water produced is collected for reinsertion to the wells, where it is used to pressurize the reservoir to enhance the recovery of remaining oil and gas deposits.

Description The standard Aspen HYSYS unit operations such as separators, heat transfer equipment, and rotating equipment items can also be employed in an upstream model. This Oil-Gas Separation model is a simulation of a standard-type processing unit. The model will also attempt to meet ce1iain product specifications and this is made possible by using certain logical (or mathematical) operations in HYSYS. This workshop includes the following tasks: • • •

Task I - Open Starter & Inlet Separator Task 2 - Finish the Model Task 3 - Dew Point Control

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Workshops

Task 1 - Open Starter & Inlet Separator You will use the case created in the Pipeline module as the base for building this module. o o

Open the case 02_Oil-Gas Pipeline.hsc. Save this case as 03_ OGSP Starter.hsc.

Note: The Oil-Gas separation plant will be built with only streams 'Reservoir I' and 'Reservoir2 '. The oil and gas production from reservoirs 1 and 2 enter the separation plant at a controlled pressure and proceed to a 3-phase separator. This separates the gas, crude oil, and water phases into three different streams. Overhead gas from the 3-phase separator is then passed through a cooler where heavier hydrocarbons condense. These hydrocarbon liquids are separated from the cooled gas in a Low-Temperature Separator. A compressor raises the pressure of the dry, cold gas up to the operating conditions of the pipeline. The condensed liquids from the low temperature separator are mixed with the crude oil from the 3-phase separator. The combined liquid stream then proceeds to the secondary separation train. An inlet valve is added to reduce the pressure of the pipeline before the production fluid enters the 3-phase Separator.

o

Add a Valve operation and specify the Connections page as follows: Valv<:t VLV-100

D~~i~~--TR;;ti~i[W~rk:h-~-~~-~i~ Design Name

Connections Parameters User Variables! Notes '

VLV-100

Inlet To

1

Fluid Package

o o

View the Parameters page and specify a Delta P of700 kPa (101.526 psi). Add a 3-phase Separator to the flowsheet. The 3-phase Separator view appears.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

On the Design tab, Connections page, attach To Sep 1 as the inlet to the 3-phase Separator. Create the three outlet streams as follows:

o

o

o

In this cell...

Enter ...

Vapor

Gas 10

Light Liquid

Oil 10

Heavy Liquid

Water 10

Click the Parameters page. The default inlet and outlet Delta P of zero is acceptable for this example. The Volume, Liquid Volume, and Liquid Level (which generally apply only to vessels operating in dynamic mode or with reactions attached) are also acceptable at their default values. To view the calculated outlet stream data, move to the Worksheet tab and select the Conditions page. The table appearing on this page is shown in the following figure:

o

. . . . . .•i:;;;l[ilf-,§f.

Conditions

i Properties

Compo~ition;

PF Specs

To Sep 1 0.2221 17.68

Oil 10

G11'1'10

0.0000

1.0000

17.68

17.68

5776

5776

5776

Molar Flow [kgmole/h]

3,575e+004

1.654e+004

7941

1.127e+004

Mass Flow [kg/hj

2.146e+006

1.80Se+006

1385e .. oos

2317

438.1 -7,715e+004

2.031e+OOS 20.lS -2.867e+005

149.4 -6.126e+008

51.73 -3.23le+009

V<1pour Temperature [CJ P(essure [kPaJ

Std Idea! Liq Vo! Flow {m3/hJ Molar Enthalpy (kJ/kgmolej Molar Entropy (kJ/kgmole-CJ

Heat

o

Flo~·1

{kJfhJ

2958 ·2.235e+005 114.0 -7.990e-.009

-2.507e+OOS

139A -4.147e+009

Water 10 0.0000 17.68 5776

After the inlet separator calculates, save your case as 03_ OGSP Separator.hsc. After saving, move on and build the remainder of the plant.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Workshops

Task 2 - Finish the Model This portion of the workshop is focused on building the remainder of the Oil-Gas Separation Plant model. Resume by adding another valve to reduce the pressure of the overhead gas stream from the 3-phase Separator.

o

o

Specify a new valve operation with the following information: In this cell...

Enter ...

Inlet

Gas 10

Outlet

Gas 11

Delta P

3000 kPa (435.1 psi)

The overhead gas stream is cooled with a Cooler operation. Add Cooler and connect it as follows: Cooler. .

r~too

Oesign"'[.~-t~_g_J_wcrb~eet !_ l'erfor'.1la~eJ '90i~!!ti:<:~J De.-ign

Name

E-100

Corme-ctiom P~ran1ete~

lJ•er Va~abi,.,! Not,.•

Inlet

Gas 11

fr erg)'

Chiller 1-Q

--------~ GM 12

~!

] Ignored

o o

Click the Parameters page. Specify a Delta P of 50 kPa (7.25 psi). On the Worksheet page, specify an outlet temperature of -5°C (23°F).

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Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

The next separator, the Low-Temperature Separator separates the Gas 12 stream into its vapor and liquid phases, knocking out any condensed water or hydrocarbon liquids. o

o

o o

Double-click the Separator icon on the Object Palette. The Separator view appears. Name the Separator as LTS-1 and specify the Connections page as follows: In this cell...

Enter ...

Inlet

Gas 12

Vapour Outlet

Gas 13

Liquid Outlet

Liq 1

Add a Compressor to the flowsheet and call it Comp 1. Specify the Connections page as follows: In this cell...

Enter ...

Inlet

Gas 13

Outlet

Gas 14

Energy

Comp 1-HP

At this point, the Compressor has one degree of freedom. To fix this remaining degree of freedom you can specify either the Compressor outlet pressure or the horsepower of the Compressor. In this example, we will set the pressure indirectly when we specify a Mixer in the next step. o

Add a Mixer operation with the following information: In this cell...

Enter ...

Inlets Outlet

Automatic Pressure Assignment

Equalize All

To Gas Plant, Pressure (kPa)

5500 kPa (797. 7 psia)

After you specify the pressure for the To Gas Plant stream, Aspen HYSYS can perfonn a flash calculation on the Gas 14 stream. Now, the Mixer and the Compressor operation should all be completely calculated. o

Save your file as 03 OGSP-Gas.hsc.

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

The cmde oil extracted from the first separator mixes with the condensed gas liquids collected from LTS-1. The combined stream is fed to a second 3-phase Separator to further separate the remaining gas, crude oil, and water components. The separated gas then goes through low temperature separation and compression before it combines with the gas stream from the first separation train. The combined gas stream is then fed to the pipeline (for delivery to customers or to a gas plant for further processing). The crude oil stream produced from the secondary separation train is fed to the stock tank for crude exp01t. As previously described, the water extracted from the production fluid will be reinse1ted to the production wells. o

Install a Valve with the following specifications: In this cell...

Enter ...

Con.nectioris.flage ; Inlets

Oil 10

Outlet

Oil 11

· Parameters Page Delta P

o

I

.

Unspecified

Add a Mixer with the following infonnation: In this cell...

Enter...

Inlets

Oil 11 Liq 1

Outlet

To Sep 2

Par~rrietel's F>age • • Equalize All

Automatic Pressure Assignment

o

Add a 3-phase Separator with the following infonnation: In this cell...

Enter... '""

,,,'"

Inlets

To Sep2

Vapour

Gas 20

Light Liquid

Oil 20

Heavy Liquid

Water 20

' "

"

'',, ::·, :_ -, -_::-,:

"

i

Parameters Pafile Delta P, Inlet

©2014 AspenTech. All Rights Reserved.

700 kPa (101.5 psi)

7

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

A pressure drop for a separator can be entered on the Design > Parameters page. Refer to the figure shown below:

3 PhaS~ Sejiaiator. V-101

Desi9-~---Th;~tio~~~LRati~~~[Wo~~~~l-[!?Ynami~-~

J

Design Connections

Delta P

P.,r<1meters

.•.•...•...•..•....•..

User Variable; Notes

ln!et lkPa]

[.Vapour outlet-·-·-·{kPal. ·-·····

--100.0· 1

---

. 00000..J Volume

li<:juid Votume

'''

t

50.00 %

Type

I c:-, Separator o

'§' 3 Phase Sep

()Tank

Add a Valve with the following information: In this cell...

Enter...

Gas20 Gas 21

Delta P

o

I

350 kPa (50. 76 psi)

Add a Cooler with the following inf01mation: In this cell...

Enter ...

Inlets

Gas 21

Outlet

Gas22

Energy

Chiller 2-Q

Delta P

100 kPa (14.5 psi)

Outlet temperature

-22°C (-7°F)

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrca1n

o

Workshops

Install a Separator with the following information: In this cell...

Enter ...

Connections Page

o

Name

LTS-2

Inlets

Gas22

Vapour Outlet

Gas 23

Liquid Outlet

Liq 2

Install a Compressor named Comp 2 with the following information: In this cell...

Enter ...

Connections Page '

o

"

,',

'

..

Inlet

Gas23

Outlet

Gas24

Energy

Comp 2-Q

Connect Gas 24 as one of the inlets to MIX-101 and it should calculate due to the "Equalize All" pressure assignment in MIX-I 0 I.

Now you will combine the crude oil streams collected from the two-stage separation and export it to the stock tank at atmospheric pressure. o

Add a Mixer operation with the following information: In this cell...

Enter ...

co11nectiolls ~ag~ ' Inlets

Liq 2

Oil20 Oil 21

Outlet

o

Add a Valve operation with the following information: In this cell...

Enter ...

connections Page

o

Inlet

Oil 21

Outlet

To Stock Tank

Specify a pressure of 101.3 kPa (14.70 psia) for the To Stock Tank stream.

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

a a

Workshops

Double-click the Tank icon on the Object Palette. The Tank property view appears. Click the Design tab. Type Stock Tank in the Name field and specify the Connections page as follows. Tank:Slod:Taiil:

De•'9n

[~1-~$~[Ra~i~-fW~~~;~~-i~J:i:;-~~~l Nome

Oesi9n

<:wmK!JOl\S Parnmete"

Stock Tank

Inlet< To Stock lank

u,erVariabl~<

~<

Notes

Strnam >>

\lapcu1 Outlet

j_v~-~

- - - - - - c...

I

L

~t-l~-:"-,:-~-·tl;-~:- .,- - _,._____ . _

fo~rg\I (Opfio~aQ

0

; "''"· ::;II'11"11"11'·11....ll,ll.1111111111111111111111111111111111111111111111111111111111111111111 :-,

a

lgnQiffl

Add a Mixer operation with the following information: M'oo!ri MiX-104 Desi9~-""[~~~]~~~~~~i~l~_a~-i~i1 Design

Name

MIX-104

Connections Paramet<'rs ' User Vilfiables Notes

Outlet

Inlets

!.. !.?..~~~!_~-~~~~~-

Wate
Wate..-20 <<Stream>>

Fluid Pad::age

I~---

i

Review the production from this model and answer the following questions: 1. What is the Gas flow to the Gas Pla11t a11d Oil prod11ctio11fro111 tlte Stock Tank?

1. How does this co111pare to the reservoir data that we e11teredfor the two reseri•oirs?

3. How do you account/or any differences?

a

Save your case as 03_ OGSP .hsc.

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen I-IYSYS Upstream

Workshops

Task 3 - Dew Point Control Produced gas must meet a meet a Hydrocarbon Dew Point temperature specification at the pipeline flowing pressure to ensure that no free hydrocarbon liquids accumulate in the transmission line. A typical pipeline dew point specification of-10°C, 5516 kPa (15°F at 800 psia) will be applied to the To Gas Plant stream in this case. The current dew point can be viewed by adding the HC Dew Point gas property con-elation to the To Gas Plant stream. o o o o

Double-click the To Gas Plant material stream. Select the Properties page from the Worksheet tab. Click the Append New Correlation button at the bottom of the table. From the Gas grouping select the HC Dew Point con-elation and click Apply to add it to the stream.

: BlackOil ! Electrolyte

-' Gas C02E-AR4

C02E-SAR C02E-US HC Dew Point

HHV Mass Basis HHV Molar Basis

HHV Vol. Basis LHV Mas5 Basis LHV Mo!.:ir Basis LHV Vol. Basis

I

.. .!

Mass Density (Std. Cond)

I

Water Content

j

Water Dew Point

l___,___

{)_,.~.~~-~~~e·I-~~-~~--.,--------

--,

........ A~ely.

.

Close

J

..

J

fV!tat is tlze HC Dew Point of tile To Gas Plant streani at current co11ditio11s?

Note: HC Dewpoint has been added to the bottom of the list on the Properties page; there are various ways of customizing the property list for this stream using the local property controls. Be aware that we have added HC Dew Point as a local property only; it will only be viewable from this stream. Property pages can also be customized globally so that every stream in your simulation is changed in the same way. Ask your instructor or refer to the help topic "Correlation Manager" for more details.

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

The current HC Dew Point is just a bit out of our required range. To set the HC Dew Point to a desired value, you will use the HYSYS Adjust block. This will allow you to set the HC Dew Point to a desired value by manipulating some independent variable. Which variables in the OGSP process 111ight iuj111e11ce this HC Dew Point?

The Adjust operation is a Logical Operation, meaning it is a mathematical operation rather than a physical operation. It will vary the value of one stream variable (the independent variable) to meet a required value or specification (the dependent variable) in another stream or operation. In this example, an Adjust operation is used to adjust the duty of the chiller in the first separation train until the To Gas Plant dew point is within a few degrees of the pipeline specification. In effect, this increases the heating value of the gas, while still satisfying the dew point criteria. o

Add an Adjust operation to your flowsheet and double-click the icon. The Adjust property view appears: ADJ-1

Connectlons

Adju~t

Notes

Name

AOJ-1

·Adjusted Variable : Object:

J

j Va.table:

I

Target Variable

Object: I

~~n~~~e~---

~----------~

[ ___-___S_~:-~_t_.Y~r_"'__

L ________________________________ ~~-----~~-]

~I

!

, Target Vatue

Source O' User Supplied

Specified Target Value

Another Object

CJ Ignored

""''' o

Click the Select Var button in the Adjusted Variable group. The Select Adjusted Variable view appears.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

The chiller duty, Chiller 1-Q, should be adjusted in some way to meet the required target. An adjustable variable for the Chiller 1-Q must now be selected from the Select Adjusted Variable view. As we have not directly specified the chiller duty, we need to select the variable that directly affects this duty, in this case the outlet temperature from the chiller.

o

From the Object list, select Gas 12. From the Variable list which is now visible, select Temperature.

~ Select Adjusted Variable For ADJ-1 Flowsheet Case (Milin)

Object

Chiller 1-Q f Ch:!ler 2-Q ! Comp 1 Comp 1·HP

Variable

[ ___ OK~- -

Feed ,\'o:;:!e El.:-rntion L"q Vol Flow -@:•Std Cond

:a

Comp2 Ccmp2-HP Crnde Expod E-101

FeedffB:'cck_ Reser, o

pHv'a!ue

FeederBlock_f?esero
Pressure

GaslO

Streams

,, Unil0p$

· logicals ' ·:Utilities '_!

Prodvrt No:::zle Eit:>'I Spn:

si!y Gos 1.f

! '9, AH

MacroCut lighrEnd; MMs F/o.v Mo/or Entliaipy Melo~ F1'11'1

E-100

: ; -Object Filter

Macrowl Assay Data MoucCur Data Macron.«/ Gm Cof>'positio'l

Temprro!we

Co!umnOps

'fCustom

r,

j

i-

Custom...

J

G.n20 Gos 21 Gos 22

Total WOR

Uso·r Vorioblt:'s Vapour Frortirm

Variable

o

o o

o

~scription

Temperature

Click the OK button to accept the variable and return to the Adjust property view. Click the Select Var button in the Target Variable group. The Selected Target Variable view appears. Specify the following: In this list...

Select...

Object

To Gas Plant

Variable

Calculator

Variable Specifics

HC Dew Point (Gas)

Click the OK button to close the Selected Target Variable view.

Note: Any variable that has been added to the Properties Page using property correlations such as HC Dew Point must be accessed through the "Calculator" variable when using a variable navigator. The next step is to provide a value for the target variable, which in this case is the dew point temperature. The pipeline specification to which we must adhere is to keep the HC Dew Point temperature at or below -14 °F (-25.5 °C). You will allow for a I °C safety margin in your specification, however.

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

Enter a value of-25°C (-13°F) in the Specified Target Value box. The completed Connections tab is shown below:

(011nection<

Adju~t

Connedions Nates

Name

ADJ-1

-Aclju. ste'J Varia.b!<

~~~~--~----

Objut

!Vanabfe: 1

Select Vl11...

lf~;;;p.,~·~;~;;,~-;~~·--------------~---1

Target Variable

~o-Ga, Pian!

Object.

f~~~~-~~C D'.'_"':'._~_~int[C:i_~---------------------------

Vanab!e.

,-- Target V<1lue ············ ·················· ·· ·············· ·············

I

Source

;

:q- UserSuppl1ed

i

') A1'o!~er Object

) SpreadS~eetCel! Object

o o

Specified Target Value -15.0000 (

Select the Parameters tab. Replace the default Tolerance and Step Size with 0.2°C (0.5°F) and 5°C, respectively. No values will be entered in the Minimum and Maximum fields (these are optional parameters).

Parameters

- Solving Parameters ---------------·-----------

Parameters

Options

[] Simultaneous Solutinn

Method

Secant

Tolerance

0.20000 C

5.0000 C

Step Size

-

Minimum (Optional}

l~~;~_;;;~~~;.;_~-----------·- _._ ______:_u_''_·b_°"_"_d·-~-~-

[] Optimizer Controlled

o

Go to the Monitor tab; this will allow you to view the progress of the Adjust as it rnns.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Workshops

AOJ-1

1-c~~~~i~-~~]~Pa~;~~t;;-1 M~~i;~;-l-U~~-;v~;i~-bi~~--1 Monitor

-rteratlon History

Tables

Iter

o

6

Iterations

Plots

Adjusted Value

Target Value

Residual

[CJ

!CI

[CJ

1

-5.000

-18.766

6.234

2

-4.315 -4.677

-18.023

6.977

-18.415

6.585

3 4 5

-14.720

-23.788 -29.080

1.212 -4.080

6

-10.828

-25.015

-1.450e-002

-9.673

From the Monitor we can see that the To Gas Plant stream now has an HC dew point temperature of approximately -25°C (- l 3°F). This specification is within the acceptable range set forth by our tolerance.

How 11111ch was the te111perature/or strea111Gas12 adjusted?

Did this have a sig11ijica11t effect 011 your gas and oil production rates?

o

Save your file as 03_0GSP Adjnst.hsc

©2014 AspenTech. All Rights Reserved.

15

Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Pipeline Simulation Using Aspen Hydraulics Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

Lesson Ob_jectives Identify and explain the Aspen Hydraulic sub-flowsheet and unit operations Compare and contrast the HYSYS Pipe Segment calculations with Aspen Hydraulics Use Aspen Hydraulics in Steady State mode to model a pipeline network

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Aspen Hydraulics

Aspen Hydraulics Unit Operations Aspen Hydraulics unit operation models include: - Pipes, junctions, mixers, splitters, swages and valves

Aspen Hydraulics simulations can be solved in:

Piping

Steady State mode, or Dynamic mode on a single network, - with the ability to switch between the two modes and also switch between solvers

Summary of Available Pipe Options (1) Pipe segment - Standard feature in HYSYS - Optional add-on license to use OLGA 2-phase, or 3-phase correlations in the Pipe unit

Compressible Gas Pipe Pipe included in Valve (shortcut option for Dynamics) - Requires HYSYS Dynamics license

PIPE SYS - Requires separate PIPESYS license from SPT Group

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Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Summary of Available Pipe Options (2) Links to Pipesim and Prosper/Gap - Requires HYSYS Upstream license and separate licence from Schlumberger

Aspen Hydraulics - Requires HYSYS Upstream in Steady State and Aspen Hydraulics license in Dynamics

Link to OLGA - Requires HYSYS Upstream from AspenTech and OLGA license from Neotec

Capabilities

Three main capability differentiators - Steady State vs. Dynamic modeling (SS / DYN) - Single line piping vs. Network modeling (SL or NET) - Single phase vs. Multiphase modeling (SP or MP)

Assess your needs in terms of these capabilities - See table on next slide

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Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Aspen Hydraulics

Capability Overview

Operation Pipe segment Compressible Gas Pipe(') Pioe included in Valve Pioesvs Link to Pioesim, Prosper/Gap Aspen Hvdraulics Link lo OLGA (') Only gas phase calculat1ons

S~SUSP

SSIBUMP

S~NET/SP

ssmETIMP DYNIBUSP DYNISLJMP DYNINETIBP

x x x x x x x

x x x

x x x x x x x x x x x x

DY~NET/MP

x x x x x

x x

x x

Aspen Hydraulics Requires an additional license - HYSYS Upstream in Steady State and - Aspen Hydraulics license in Dynamics

Aimed at modeling pipelines and pipeline networks - Limited choice of fittings (valve, swage) in earlier version to V7.3 - Full range of fittings available in V7 .3 and newer versions.

Can model heat loss in detail - Fluid

+ metal + multiple layers of insulation

2 and 3 phase transient analysis Pipeline cool down calculation for shut in pipe

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Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Pipeline Modeling Options in HYSYS Options HYSYS Pipe Segment model - part of Aspen HYSYS Aspen Hydraulics Sub-Flowsheet - part of Aspen HYSYS Upstream -- ., --.-

,,,,.~.-T' ~ito

7-~·

TEE-1

TEE-ID! "'E-101

7---~------;-,;':,

I'

PIPE-W•

'"C' 0-102

-~-" ~--- • i"

~.O<

$··~··•00

Single Pfpeline Steady-State

Flow Network Steady-State

Solver

Solver

- - -,;:,

~ ~,

Dynamic Solver

HYSYS Pipe

Segment Aspen Hydraulics Sub-Flowsheet

Aspen Hydraulics Steady State

Topology Straight Run - Convergent Branched - Looped/Divergent

Unit Operations - Pipe Segment (with/without Heat Transfer) Valve - Mixer/Tee (Calculates Flow Direction and Pressure Drop) - Swage - Full range of fittings in V7 .3 and newer versions

Composition Tracking - Fully Compositional Model using an Equation Of State - Black Oil/Oil & Gas Feed

©2014 AspenTech. All Rights Reserved.

5

Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Aspen Hydraulics Transient Topology

...

Straight Run Convergent Branched Looped/Divergent

~" ·!,

Solver Technology ProFES Two Phase Transient ProFES Three Phase Transient Two Phase Pigging Model Slug Prediction

·-

Atio!Ois!a1>te{m)

Liquid Holdup Profile During Pigging

Terrain Induced

Flow Induced

Dynamic Solver Options ·~-~~~;;;.1.t;!frriR.j'O;i'

'. ~~,.,,.;d_~f~-i_~~?"~j

DJ"'"" 1~~"'.'~J

A""'"k">"'""'"°"Co~p-..,;o,~.c"'">''"'''''!o\,. '"'·' r.,1.i.;1.,,,~~ ' " " "

•Acto'""""'S"""'"'I•·•~••

'""

·,._,o...,.eo·

'""

!"'"""""' Au!o """'"'''l' An'-"'"

!.._,.,,..,,_,,,d.0"'~'~>¥""-'PO,·o•"'~;,,:...,.';>

l

y..,.¥<, ! 1/0!"':'!-!<~_i Tr""~''°'' j ~°".. '

,,,,.o Hrd""'k< "'"' "'""'"''°"'"'"""""'moo.I.

O.rt<•l<...,.rol<'>""

····~""""'''"''""' '"'"""

o.1000

""'°"'"'"°"II"'"'°' ;-,,,,foffi\Nop°"'""''°"'"'"'p~"G

00000

p.,.,.co..-., •.,..,_,.,,,,"'0·

A•1"tl><:k<e'l'~°"''ti»'1<><< ,,~Mtj
"'"""""'""""""'"""""""'''"'f''-'"''""

l~.00

1.;00

'"-""

:~->~·-1

:Frol"'

·,,.,<-<.,c•""'·''l"'"Tcm'"

Co-~"°""'"T'"''°"'l

·coo'D<>-.-,,,

Qff__

'._-l'Y"''"'"'c"""P""'''"at"'"

: o.;,.,,"" "'"""'"' lO.c>--c..,,.,.,,.,

'«'"'"'"'"~'""'"""'""",.,.'"'"'°""9'-'""'

·I

©2014 AspenTech. All Rights Reserved.

6

Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Building a Model in Aspen Hydraulics (1) Use Flowsheet > Upstream Operations .... To display the Upstream palette Select the Aspen Hydraulics icon ,.. Palette

=

@l '

OliflX I+ II"*" I Custom

Dynamics

Building a Model in Aspen Hydraulics (2) This creates a sub-flowsheet for the Aspen Hydraulics calculations Along with a palette of unit ops allowed in Aspen Hydraulics ;.;..'!t.....,fJ>-:.;..o.,,.;_.;. 'V•"'<•>

,-,.1;,:-~

•'Y", '-~>-.~~i o,-~ I '«~,.,,..J ,·~_.. j

,, ...;, ....!.«~<.,,

: .,... '

G3S> ,_ ) - - - - - - -

©2014 AspenTech. All Rights Reserved.

7

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Aspen Hydraulics

Building a Model in Aspen Hydraulics (3)

p

p

specified

calculated

.. '" !""'

"....,,

-~-...,

""'"

!••

'

.

;;-_,

~"""

Reference Conditions Reference Conditions must be specified by the user to define the fluid enthalpy of the stream that will be used as a feed specification The stream will be flashed at these conditions to determine the enthalpy - Note: These reference conditions will only be used if the Molar Enthalpy of the stream as shown on the Worksheet tab Conditions page is undefined - If the Aspen Hydraulics stream is not a flow specification and the enthalpy has been calculated by the container flowsheet, then the Reference Data is not required - If the stream has a known mass flow rate, then a pressure must be defined for these reference conditions; otherwise, if the stream has a known pressure, that pressure will be used

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Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Aspen Hydraulics

Ste<~dy~State

Solver in V7 .c~

• V7 .3 steady-state solver can be up to 10 times faster than V7 .2

Substantial improvement in the speed and efficiency in how pipeline models and scenarios can be developed and tested in Aspen Hydraulics V7.3 and newer versions

• Improved boundary conditions • Ignore unit operations

• Internal pipe fittings

• Improved heat transfer specifications

Steady-State Solver Boundary Conditions Pipeline Pressure-Flow

Behavior Three variables characterize flow 1. Inlet Pressure 2. Outlet Pressure 3. Mass Flow

Inlet Pressure Pipe

By specifying two variables as :1 boundary conditions, third 1'"2 unknown can be calculated with 3

Calculated

:sp~c·~fecr

Specified

mass and energy balance

•

.

_Specified Specified

ca1cU1Qtec:t

.

.

Sp~~i~,d~

Calculated

.SPecmeci

Aspen Hydraulics V7.3 and up

A,Spen Hydraulics V7 .2 • Supports scenario 1

©2014 AspenTech. All Rights Reserved.

Outlet Pressure

Mass Flow

•Supports all three scenarios

9

Aspen Technology, Inc.

Aspen HYSYS Upstream

Pipeline Simulation Using Aspen Hydraulics

Ignore Hydraulic Unit Operations

Individual unit operations can be

ignored in Aspen Hydraulics subflowsheet

Useful to quickly

...

implement scenarios where

section of field is shut-in

Ignoring this pip:· ignores

th~

associated network branch

,Q:i 11 ~ 1 A:; ~

.!l

but allows the rest of the sub-flowsheet to solve

Options in Hydraulics Pipe Operation Internal_ fittings available in Hydraulics pipe segment

..________[C: ·'

- Equivalent length is calculated for pipe - Models pressure drop impact of fittings without having to add additional unit operations to sub-flowsheet ;..,,.;.-,,~;.....,.;,-~.;.;;;.;;-,

i "''"" ;!"'r~J \'f~"':';.\fR~•~!".'!f.i

New heat transfer options

1-,,,v::,. :~.,,., ,.0-,-.•-,.,,.,,..-.-,_-:::>

- Overall heat loss from pipe can be specified - Outlet temperature can be specified

©2014 AspenTech. All Rights Reserved.

I ....,,........i "'"'".''"'°"~'"~' ~= !6..,,.,1.~, ..;..;,- -

IO

-~...,,

Aspen Technology, Inc.

Pipeline Simulation Using Aspen Hydraulics

Aspen HYSYS Upstream

Aspen'Tech provides a comprehensive pipeline modeling solution Summary of HYSYS's Capabilities for Pipeline Modeling Feature

Functlonal1tv

HYSYS Pipe

Aspen Hydraulics

Pipe Correlations

Multiple options

./

New options ln V7.3

Allows different correlations for different segment orientations

./

New In V7.3

Flow Network

Can solve flow networks

Boundary Condlllons

Calculate pipe diameter

Fluid Properties

./ ./ ./

./

Options for emulsion viscosity method

New In \17.3

New In \17.3

Pumps, compressors, healers, coolers,

./ ./ ./ ./

Calculate pressures and flowrates Unit Operations Heal nanMer

fittings, etc.

Specify heat flow Specify outlet temper..ture Specify heat transfer coefficients

Flow Assurance

New In V7.3

./

C02 Corrosion

New In \17.3

New ln\17.3

Hydrate Formation

New In V7.3

New lnV7.3

./

Wax Oeposltlon

New In V7.3

Erosion Utility

New tn VJ.3 Rigorous Dynamics

Pigging

./

Slugging Analysis Dynamic Slmufatlon

New In \17.3

Support of dynamic modeUng

.fcsrmple)

.f (Rigorous)

Aspen Hydrm.1lks Workshop Model steady state gas-condensate gathering network using Aspen Hydraulics Discover how to properly specify boundary and reference conditions Review the result reporting and calculation capabilities in the Hydraulics sub-flowsheet

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Aspen Technology. Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Aspen Hydraulics Workshop

aspen.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Aspen Hydraulics Workshop Objective This module will provide a different perspective of piping calculations in Aspen HYSYS. Rather than using the standard HYSYS piping operation, the Pipe Segment, you will be using the Aspen Hydraulics sub-flowsheet option of HYSYS Upstream. Aspen Hydraulics enhances pipe and pipeline simulations by allowing for flexibility when calculating both single pipe and network-type applications. Certain boundary conditions can be specified around the sub-flowsheet, allowing for flexible calculation of unknown boundary conditions. Aspen Hydraulics supports both steady-state and dynamic calculations - while this workshop will only involve steady-state.

Description A gathering system located on varied terrain is simulated using the Aspen Hydraulics capabilities of Aspen HYSYS Upstream. The following figure shows the physical configuration of this system superimposed on a topographic map. The system consists of four wells distributed over an area of approximately 2.0 square km, connected to a gas plant by a network of pipelines. ~lmeelevation b°1>':1

point

Elevation m meters

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen I-IYSYS Upstream

Workshops

The fluid in this case is varied; both sour and sweet gases are being combined in the pipeline, as well as a gas condensate mixture. Various piping connections combine all of the incoming gas streams from the outlying wells into one common header. Flow lines extending from this central site to each of the individual wells are modeled in Aspen HYSYS Upstream using the Pipe and Complex Pipe operations available in Aspen Hydraulics. Since the plant is located in an area with mixed terrain, the elevation changes must be accounted for. Aspen Hydraulics Mixer operations are used to model mixing points where flows from remote wells are combined in common lines. Pipe Diameters for each of the branches are: Pipe Branch

Diameter

Branch 1

76.2 mm (3")

Branch 2

101.6 mm (4")

Branch 3

76.2 mm (3")

Branch 4

101.6 mm (4")

Branch 5

152 mm (6")

Branch 6

76.2 mm (3")

Branch 7

152 mm (6")

Schedule 40 steel pipe is used throughout and all branches are buried in Dry Peat at a depth of 1 m (3 ft) with an ambient temperature of 12°C. All pipes are uninsulated. Elevation data for each of the branches are provided in the following table. Branches that traverse undulating terrain have been subdivided into a number of segments with elevation points assigned at locations where there is a significant slope change. Such locations in the network are labelled on the schematic diagram with the elevation value in italics.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

1

2

Branch 2

Branch 3

GasWell3 1

648 (2125)

2

634 (2080)

3

Branch 4

205 (670)

633 (2077)

.sa1..(i!g~o>···•

.B.ranchf<'l,2 1

633 (2077)

1

625 (2050)

-7.5 (-25)

2

617 (2025)

-8 (-25)

604 (1980)

-13 (-45)

Branch 5 Branch 6

Branch 7

.Brnnc!i 5..&. 6... 1

340 (1115)

This workshop includes the following tasks: • • • • •

Task I - Define Simulation Basis Task 2 -Add Hydraulics Sub-Flowsheet Task 3 - Build the Piping Network Task 4 - Boundary Conditions and Results Task 5 -Heat Transfer Contributions

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

Workshops

Task 1 - Define Simulation Basis The gas gathering field will be modeled using the Peng-Robinson equation of state. The fluid package needs to contain the components shown below. It is important to know that Aspen Hydraulics will always use a COM Thenno fluid package for its calculations. If the fluid package of the main flowsheet is not a COM Thenno fluid package, Aspen Hydraulics will create a new COM Thenno fluid Package that uses a default PengRobinson equation of state and the component list of the main flowsheet fluid package. To maintain control over the fluid package being used, it is advisable to set up the Simulation Basis with a COM Thenno fluid package in the main flowsheet. Rather than adding the components data from scratch, you will import a provided component list file (.cml). It will contain the following components: Nitrogen H2S C02 Methane Ethane Propane i-Butane 11-B11ta11e i-Pe11ta11e

o o

11-Pe11ta11e 11-Hexa11e Cr+* H20 NBP[0/92* NBP[0/171* NBP[0/243* NBP[0/322* NBP[0/432*

Open Aspen HYSYS and begin with a New Case. From the Components tab, click the Import button. All~em<

c:::;comp<moc.tilll•

L,;iFi.,,AIJ"br'

::>

·

j

1

!

;:

C~ Mroltum Amy• tao,1M..n•9"

[
o

Browse to the folder 04_Aspen Hydraulics in the course workshop folder and select the file titled Hydraulics Comps.cm!.

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Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

o

The component list should now be available. To review it, double click on the Component Lists folder and then click on Component List-1. Click on Fluid Packages folder. Click on the drop down button by the Add button and select COMThermo.

o o

o

To define the property package, you must select a package for both the vapor and liquid phases. First, select HysysPR for the vapor phase. Choose the Liquid radio button and select HysysPR again for the liquid phase. The yellow status bar will show "Vapor: HysysPR Liquid: HysysPR"

o

..

~i> Componwt Li
Component L1>l Selection

Ci;. Component li
.. l:'t; fluid Padagp'

'.':"ii So»<-1

i'.O Potroloum A''°Y'

[ i_Ge~ri
(;:, 011 Manoger

- Mod
!~0 R
W Component Mar rel="nofollow">> (.<)Um Prop.,li.,

Component list - 1 [HYSYS Oaial>ank<J

Propffiy Pachg~ Selection

I,<"""" I :AnfO'ne I·

Mo:lel Option•

ModelPha,. 'Vapor

<>·Liquid

i : (i\Pf·0~£N I.0 ' . CAPE-OPEN 11

Cl•«>n·N"!i ; DB'
. &nrn1iNl?Tl '.Hyi5""~1,-,,,,

Method

P1op•lty Entholpy Enlrcn

Brav" 1;:10

CAPE·OPl'N U Fia
Cp Cv AU Prop

CAPf-OPtil/Fla•I> DIJf'AmiNf!CJsi-

HYCONFla>h HYS~Sfl~•h

lnfu9~c1ty(oefl

!Mulliflb
lnFu acrt

o" "c!un1~

PVTProflosh

Mol•rO•n•ity

'ld~o/Scl~ti'.Xl!!Y.

Peng-l/o/Jro5'>n EMl>olpy

Peny-PC'boM-"'1 Enlropy Ptng·llobiMOtl Cp

Peng-Robinsen (v Peng-Robin
K~bcd1·Da""u

lu-l(p,ler-Plocl-ec

/11o:guk< Mu't
lhmn~iCondu
H'rSYS il>ecma/ CMducfaily

SurfaceT~n
HYSYS S!i1c<~ fr~""" Pong·Robin•an f-l
Hefmholll

Nfln ; Neot.: Blad. OiJ PfiS\I

Gibbs

P
!PRS\l/lK ; : P\IOP«>f>t~kg ' 'Peng-flD~I"""'

Properly Pkg

o

. .:v.·-.··'·'··'··.."> ...·..·.., .· .·.· ·'· · '· ·. 1;(iUod·-i-tfiy;~f', .""-:-~.............:................ ;;,.,.t'.

In the Model Options section on the right-hand side of the view, scroll down until you see the Molar Volume and Molar Density calculation options. Change these from the default Peng-Robinson option to the Costald Molar Volume and Costald Molar Density options.

Note: When in the COM Thermo environment, use this "Model Options" section to customize any physical property calculations for the selected property package. Similar modifications can be made when using the standard HYSYS packages as well. o

Save this case as 04_Hydraulics Basis.hsc.

©2014 AspenTech. All Rights Reserved.

6

Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Task 2 - Add Hydraulics Sub-Flowsheet Aspen Hydraulics can be used to simulate a wide variety of piping situations ranging from single/multiphase plant piping with rigorous heat transfer estimation, to largecapacity, looped pipeline problems. It offers the pressure drop correlations developed by HTFS and the commonly used Beggs and Brill. The heat transfer can be estimated in detail including multiple layers of insulation both inside and outside the pipe. By default in steady-state, Aspen Hydraulics works with specified inlet flow rates and a specified back pressure. In this simulation we will be using some of the common unit operations available inside Aspen Hydraulics: Pipe, Complex Pipe, and Mixer. The standard mode of calculation used by Aspen Hydraulics means that the feed pressures will be calculated and therefore should be left unspecified. However, Aspen Hydraulics does need to know the thermodynamic state of the feed streams and there are two ways of achieving this: I. Install a unit operation between a completely specified feed stream that results in a stream with a known mass enthalpy and an unknown pressure. For example, you can add Valve, without specifying pressure drop. The valve will pass the Enthalpy, Flow and Composition infonnation from inlet to the outlet. 2. Provide a reference condition for each feed stream inside Aspen Hydraulics flowsheet. In this workshop, we will use the second method.

o

Click Simulation to view the HYSYS PFD.

o

Add four material streams to the PFD and define them as follows: GasWell 1

GasWell 2

GasWell 3

GasWell 4

Temperature 'C ('F)

40 (105)

45 (115)

45(115)

35 (95)

Pressure kPa (psia)

4000 (600)

3500 (500)

3800 (520)

4000 (600)

Flow kgmole/h (lbmole/hr)

425 (935)

375 (825)

575 (1270)

545 (1200)

©2014 AspenTech. All Rights Reserved.

7

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

o

Workshops

For the stream compositions, open the provided Excel spreadsheet (Gas Well Comps.xis) in the course workshops folder. You can copy the compositional data from the Excel spreadsheet and paste it into HYSYS. At this point all required streams should be defined. Now you can add the Aspen Hydraulics sub-flowsheet. Click on Upstream group in the object palette.

;:£! Palette

0 &.X

l+ll+I Custom

o

Click on the Aspen Hydraulics icon and then click on the PFD where you want to place the hydraulics subflowsheet.

Aspen Hydraulics operation opens automatically. If it is not open, double click on the hydraulics subflowsheet icon to open it. o

Select GasWelll under External Stream in the Connections page. Select rest of the three streams one after another.

-- Aspen H;-d~auli'cs St:ib-Fici~s'h~ H'i0R;100 Connections Name

~pe~~~i~~i]~steady staf~T-QY~~~~-~-[~~~~~~~]~~~~~-~i_~l~[T;~~~f~r_B~~~[ii~~-s~~!J:~.L~~!~J

HYDR-100

Tag

TPll

Inlet Connections to Sub-Flowsheet Internal Stream

External Stream

GasWelll GasWel!2

o o

GasWelll

GasWe113

GasWellZ GasWell3

GasWe!l4

GasWelf4

0

<empty>

New'"*

Click on the Show Flowsheet button. This is where you will construct your piping network. Press F4 to open Hydraulics object palette. Alternatively, you could go to Flowsheet/Modify ribbon and click on Models and Streams Palette.

©2014 AspenTech. All Rights Reserved.

8

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Workshops

Task 3 - Build the Piping Network Aspen Hydraulics is very strict when it comes to connecting various pieces of equipment. The following three rules that need to be respected: Inlet and outlet streams need to be connected to a pipe or complex pipe segment You cannot have two fitting type objects (Swage, Tee, Mixer) in series, there needs to be a pipe in between You cannot connect two pipe or complex pipe models with different inside diameters. You must use a swage to model the change in diameter. Pipes can be modeled using either the regular Pipe or the Complex Pipe operation. The Complex Pipe allows for multiple piping segments, much like the HYSYS Pipe Segment operation, while the regular Pipe just allows for one segment. The Complex Pipe will be used for Branches 1, 3, and 6 while the regular Pipe will be used for all other piping branches in the network. o o o

Add an Aspen Hydraulics Complex Pipe from the Hydraulics object Palette. Double click on the complex pipe. On the cotmections page, connect Gas Well! as the inlet, Bl-Out as the outlet, and also add a duty stream Bl-Q. Rename the Complex Pipe-100 to Branch 1.

Asp eh Hydiaulit!O Ci.impre( P1pe·seg1tiflnt· Bra11ch I

---·o~-~-i-~-~....Lf:!!?.'.n.l~~"~J. ~~-f!<-~i-~. t!!.~!-~~t~~~~:.l . . Design Connections ' Data Heat Tran5fer Notes

Name Branch 1

Product

Feed GasWelll

©2014 AspenTech. All Rights Reserved.

9

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

Go to the Data page and enter the following infonnation In this cell ...

Enter ...

Internal Diameter

76.2 mm (3")

Length

150 m (500 ft)

Elevation Change

6m(15ft)

o

Use the default Pipe Material, Mild Steel, and the default Roughness, 4.572E- 5 m (0.0018 inch). o Do not change the heat transfer options yet! Calculations using heat transfer are significantly slower and we will first solve this problem without accounting for the heat loss. o The number of pipe cells can be left at 5. As a rule of thumb the number of Pipe Cells needs to be such that the pressure drop over one cell is less than 10% of the inlet pressure of that cell. o Two more segments are needed to complete the branch. Click the Append Segment button twice to add them, the diameter of the first segment is automatically copied to the new segments.

o

In this cell ...

Enter ...

Enter ...

Segment

2

3

Internal Diameter

76.2 mm (3 inch)

76.2 mm (3 inch)

Length

125 m (410 ft)

100 m (325 ft)

Elevation Change

-6.5 m (-21 ft)

0.5 m (1 ft)

The Data from should like this:

A
!o~,;~~ -'._P~i~r:u~~.r.w;.;...~_1 I ~A."'"'""". I ;

lksign

; (om rel="nofollow">tttion<

! , 1-fMt T<"Mfer ! Nct0<

6.000 m

Miid Slee!

4.512e·005 m

! N<>HeatT~

ns.o m

-6.SOOm

Mil
4_571.,.()0S m

tlnHtdllr1

lOOJ}m

05000m

Mild Steel

4.sn.,-005 m

No

Lero; th

:-o,ta

76.20mm 76.20 mm 76.2(}mm

£1.._,,i:,,,..ch.!ng<:

HO.Ont

Wall Su
Roughne<>

Heat fr•n
HeJITl

i o o

o

Leave the Calculation, Friction Factor, etc. with the default settings. These are reasonable for a first-pass, conservative calculation. Continue by adding the remaining piping operations. Note that Aspen Hydraulics will not solve as you build the network. You will need to account for the system boundary conditions before the model will calculate. Add an Aspen Hydraulics Pipe with the following values:

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Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Name

Branch 2

Inlet

GasWe112

Outlet

B2-0ut

Energy

B2-Q

Oata

o o

Length

200 m (655 fl)

Elevation

23 m (75 fl)

Internal Diameter

101.6 mm (4 in)

Keep all other inputs for Branch 2 at their defaults. For the mixing of various streams, Aspen Hydraulics uses the T-Junction Mixer.

I

Piping

~§1?11v1J D!J~~)[S1J

Add a T-Junction Mixer to the PFD and define it as follows:

Name

Junction 1

Feed/Side-Arm

B1-0ut, B2-0ut

Product

J1-0ut

.Pata

o

Angles

Leave the default values (90, 0, 0)

Calculation Method

Static Pressure Balance (default) At low velocities there is little difference between the different methods.

Add a Complex Pipe with the following values:

©2014 AspenTech. All Rights Reserved.

11

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Name

Branch 3

Inlet

GasWell3

Outlet

B3-0ut

Energy

B3-Q

Workshops

Segment 1

Length

160 m (525 ft)

Elevation

12.5 m (40 ft)

Internal Diameter

76.2 mm (3 in)

Segment2

Length

100 m (325 ft)

Elevation

-14 m (-45 ft)

Internal Diameter

76.2 mm (3 in)

Segment3

o

Length

205 m (670 ft)

Elevation

-1 m (-3ft)

Internal Diameter

76.2 mm (3 in)

Add an Aspen Hydraulics Pipe to your case with the values provided below:

Name

Branch 4

Inlet

J1-0ut

Outlet

B4-0ut

Energy

B4-Q

Segment 1

Length

355 m (1165 ft)

Elevation

-4 m (-13 ft)

Internal Diameter

101.6 mm (4 in)

©2014 AspenTech. All Rights Reserved.

12

Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

o

Add a second T-Junction Mixer to your case.

Name

Junction 2

Feed/Side Arm

84-0ut, B3-0ut

Product

J2-0ut

Data

o

Angles

Leave the default values (90, 0, 0)

Calculation Method

Static Pressure Balance (default)

Add a Complex Pipe to your case with the values provided in the following table.

Name

Branch 6

Inlet

GasWell4

Outlet

86-0ut

Energy

86-Q

1>1m11.r\1110.ns Segment 1

Length

180 m (590 ft)

Elevation

-7.5 m (-25 ft)

Internal Diameter

76.2 mm (3 in)

Segment 2

o

Length

165 m (540 ft)

Elevation

-8 m (-25 ft)

Internal Diameter

76.2 mm (3 in)

Add an Aspen Hydraulics Pipe to your case, using the following data:

Name

Branch 5

Inlet

J2-0ut

Outlet

B5-0ut

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13

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

o

Length

300 m (985 ft)

Elevation

-16 m (-52 ft)

Internal Diameter

152.4 mm (6 in)

Workshops

Add the third and final T-Junction Mixer to the simulation, set up with the following specifications:

Name

Junction 3

Feed/Side Arm

B5-0ut, B6-0ut

Outlet

J3-0ut

Angles

Leave the default values (90, 0, 0)

Calculation Method

Static Pressure Balance (default)

Add one final Aspen Hydraulics Pipe to the simulation with the following values:

Name

Branch 7

Inlet

J3-0ut

Outlet

B7-0ut

Energy

B7-Q

.Pimensions..

o

Length

340m(1115ft)

Elevation

-13 m (-45 ft)

Internal Diameter

152.4 mm (6 in)

The piping network should now be fully built. Check your against the image below:

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

T

·- "',;T B
J"0"'1M1

"~

J1-0"1

'-"0

• c___ , Dra'10!15

Juoctco :I )~-::>•

Workshops

~ra11cll7

Junc!ioo1

-I "''"'-C

1!5-:l

'

s1-a

e2-6u1

,__

t.,..;~~

OiHJu1

6(;-[l

o o

Note that the network is still not calculating. You will need to define the proper boundary conditions and data transfers to the main PFD. Do this in the next task. Save your case as 04_Hydraulics Network.hsc.

Task 4 - Boundary Conditions and Results Before the model will calculate, you need to define the proper boundary conditions for the model. In this case, the inlet flow rates and outlet (87-0ut) pressure will be fixed. That will allow Aspen Hydraulics to back-calculate the required inlet pressures. o

Go to View ribbon and click on Flowsheet to go to main PFD. _.:;,i;;;•

Piping Network

Econom,:;k•'

Z). Zoom

&!jZoom to Fit

~Zoomln

•.::P1-;1;;,\'plti'

Flowsht>et

(~ Zoorn Out

Model P;ilette

Zoom

Simulation

Start Paqe

Notes Manaqet Show

Pl<1nt

View

l;~~t L.;~·;_t~~1 layout r~

i

I

Flowsheet/Modify

i'

tP1T

Window

I V-ie-w Flows.Ji.etot I

o

In the Connections tab and show B7-0ut as an outlet external stream. Just type

87-0ut under External Stream corresponding B7-0ut internal stream. B6-Q

<empty> <empty> 87-0ut

BS-Q B7-0ut 87-Q

<empty> <empty>

·~ N€'\V *~

_ _ _ _ _l_n,_0~1plete

o

Remove the defined pressures from the four Gas Well streams in the main PFD. These pressures will be calculated.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

o o

Workshops

Go to the prope1ty view for B7-0ut (either in the main PFD or sub-flowsheet) and define a pressure of 1800 kPa (261. l psia). This fixes the outlet pressure from the system. Go to the Transfer Basis tab for the Hydraulics sub-flowsheet and set the Transfer Basis for all material streams as a T-P Flash. Go to Home ribbon and tum the solver on.

~'

~Copy• ~Unit Sets

~place

~Paste·

!lect ..

i

;,;.;,,..... c•.•• Clip_board_j

'{f Process Utility Manager ~Correlation Manager

1"11M!lf!I!:;:

if; Adjust Manager Units

Simulation

1~

Solver

i-~31

Workbook

~J ~,, ~=~:::~;~

Reportsc

r.

:_]Input

Sumn1aries:

At this point the flowsheet should calculate. If it doesn't, make sure that the Gas Well streams in the sub-flowsheet are showing an "OK" status. If not, they may require some reference conditions. In our case, the reference conditions should be defined from the main PFD data. o o o o o o

To view the calculation results for the sub-flowsheet, select the Performance tab. The Boundaries page shows the calculated boundary conditions. What are the pressure ofGasWelll, 2, 3 and 4? _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ __ What is the temperature of B7-0ut? _ _ _ __ The Pipes page shows tabular data for each pipe, while the Profiles page allows you to build plots for the pipes in your network. On the Profiles page, click the Add button. Create a profile for Branch 3 by highlighting Branch 3 and clicking Add. Then click OK.

~ Profile Editor

Selected Unit Op~

Available Unit Ops

Branch 3

Branch 1

Branch 2 Branch 3 Branch 4 Branch 6 Brandi 5 Branch 7

L

Add ,,, ,,,,,,

J

.....,.... ,

j

Delete

OK

[_ _____ ~_~_e_I

o

_J

This creates a new results profile, which you can view in tabular fonnat by clicking Table, or in a graphical fonnat by clicking Plot.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Workshops

Profilei - flJot

H

I Pressure vs Axial Di.stance

Plot Variables

1J1?-m:~1 .i&hf~i,K'

7000

'-

6500 6000

~

.

5500 .

,._,, S-000

l!1

.

£.

.

~ 4500 4000

.

3500

.

'2--

'\:_

-

>-~""- · ~ -

Temperature vs Axial Distanc 0 Velocity vs Axial Distance Density vs Axial Distance Vapour fraction vs Axial Distance Liquid Holdup vs Axial Distance Mass Flow vs Axial Distance Elevation vs Horizontal Distance ····-······ -- --········-·-..;;;;::

'-....

.......... ........

3000

. .

2500 0.000

... . .. . 1000

500.0

.

1500

.......

,

.. 2500

2000

Axial Distance (m)

o

Add a new results profile showing Branches 1, 4, 5, and 7 in series. Compare your pressure profile to the one below:

Pressure vs Axial Distance

Plot Variables

Pressure vs Axial Distance 3450

........

3400 3350

.

(ti' 3300

.

'lz

3250

l!1

3200

.

"'

3150

. .

""'

£ 3100

I

........

~-i..IDistanc •1ml""3 9 Pretsure.(kP< ) ..... . .. 3 02

...... ....

......... .......... ..........

........

...... ,

3050 . 3-000

........

.

2950 0.000

. 5000

. 100.0

'

. 200.0

150J)

250.0

300.IJ

3SIJ.O

400.0

Axial Distance (m)

o

Save your case as 04_Hydraulics Profiles.hsc.

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Modeling Heavy Oil & Gas Production facilities Using Aspen HYSYS Upstrean1

Workshops

Task 5 - Heat Transfer Contributions The heat loss parameters to be used are as follows. Pipes buried in Dry Peat at a depth of 1 m with an ambient temperature of l 2°C. There is no insulation on the pipes. The pipe thickness is defined by the Pipe Schedule (Schedule 40). For simplicity we have used the nominal pipe diameters up till now, we now need to use the col1'ect inside and outside diameters. Below is a list of the required sizes for our pipes: Nominal Size

Inside Diameter

Wall Thickness

3" (76.2 mm)

77.93 mm

5.5mm

4" (101.6 mm)

102.3 mm

6.0mm

6" (152.0 mm)

154.1 mm

7.1 mm

Note: Before you start doing these modifications, click the ignore checkbox of the Aspen Hydraulics operation. This will prevent the operation for solving each time you change an input. Heat transfer calculations in Aspen Hydraulics take a bit of time to complete, so we will wait until all details are provided before calculating.

====------R-JI-gn-o-re_d__J

J

~~~~~~~~~~~

T

o o o o

o

Make sure the Hydraulics sub-flowsheet is Ignored as shown above. Go to the subflowsheet environment by clicking on Show Flowsheet button. Update the seven piping operations in the sub-flowsheet with the diameters Go to Data fonn to define diameter. Go to the Heat Transfer fonn of each pipe and complex pipe. Make sure Mild Steel is selected as material in each case. Define the thickness. For simple pipe, check Estimate HTC radio button to define thickness in Heat Transfer form. For each pipe and complex pipe, use the Heat Transfer fonn to enter the required heat transfer parameters. Shown below are the forms for a complex pipe and a pipe.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

G?:[email protected]

A~pen Hydrauri<:i Compkii Pipe segment: Br•ildi 1

·c;~·~;.;;~· l~.~~~·~!~~~J_\,v~~~~~t IA~.~~~-~;~1 Oe~ign

Rem°""' set

iBurled

Cou~ction; D~t~

txtem~I

: Heat Tr.i,,,fo,

Medium

Temperalur<'

i ''""

[CJ

P•pe Wall

M~d·um

Gro•.md C-o~ductivity

[~

.~".ri•_d_()_:p_!I\_[!_"] __ _

!

I

Mild Steel

Materidl

GroundTyp<'

Thi~kne•s

Type

5.500

Conduct~·:·iy_!_•V('.".-KL

45.00

C
1-'e~t C~pa<•t:l

Clensi~J

f'<J!kg·Q

[kg/m3J

Th,
Co~du
[mm]

[\'\l/m·KJ

1-'eot Copociti [kJ!kq·CJ

[kg/mJ]

{mm]

I

Thrc'
Add Layer

Inner ln
11

Oen.>t;

Add,,,.. J

1--~-

Aspen· Hydliiuf"l(s 'Pipe Segment Sr~nch 2

r. o;;·~··~·~·"[P~~~J1n[l(e 1-W~~t j fl~,,As~r.a_n~e-]

I I i

Design

1

Sprnfy By

(<>rne,t•ons

Data

'\-'eat lm>

. hlema\ Medium

E
P•pe Wall

fitting<

Note•

9.

': Out!e! Tomperature

'

· rT•mp•'
12.00 (

Medoum

Ground

GroumJT)pe

Dry Peal

: Ground Condvdi-.•ty [ Burjed Depth

0.17000W/m-K 0.1()()()()0 rn

f·M;;;;;·~·i

MildSlffi

Thi
6.00-0

-~?_r>eluctivi!!_ P.-~('1l~_KJ

45.00

I

·Outer lnsulabon Layers

I;,;

i (<>nducL.,.,ly

r<eat c~pacot)

[W/m-K]

(l<_l/k9·CJ

Demity {kg/m3}

Thickness

;conduchity

[mrr]

[W/m-K]

Helt Cap.>ci!) fk!lkg-CJ

[kgiml]

Thickness [mm]

Acid~;,.-]

I , Inner Insulation layers

~ [ :~~__

Density

~;--·-1:

o o o

o

lgnOfed

After you define the heat transfer considerations for each branch, Go to View ribbon and click on Flowsheet. Choose Yes to the solver message. Un-check the Ingored box for the Hydraulics sub-flowsheet. The model should calculate once again. Did the temperature profile change significantly? What is the new B7-0ut temperature? Save your case as 04_Hydraulics HeatTransfer.hsc.

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Aspen Technology, Inc.

Dynamic Pig Launching Using Aspen Hydraulics

Aspen HYSYS Upstream

Dynamic Pigging Using Aspen Hydraulics Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objectives Convert a steady state Aspen Hydraulics model into dynamics Setup Aspen Hydraulics pipeline operations for pig modeling Review how to merge Aspen Hydraulics sub-flowsheets with fully-defined Aspen HYSYS Dynamics files Model pigging using a Microsoft Excel interface to plot the liquid profile along the pipeline

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Dynamic Pig La1mching Using Aspen Hydraulics

Aspen liydraulks in Dynamics The Aspen Hydraulics (Dynamic) Pipeline Solver - Is a means for modeling transient multiphase hydrocarbon flows in wells, pipelines, and other process components - Solves mass, momentum and energy equations for each phase using a one-dimensional finite difference scheme

Appropriate flow pattern maps and constitutive relationships are provided for wall and interfacial friction and heat transfer, and a model for multi-component phase-change is included

Dynamic Initialization Dynamic Initialization allows you to define how the network simulation will initialize when switching to dynamics mode In order to obtain accurate results, and prevent movements in the model and pressure-flow convergence error, it is critical to properly set up the cold-start initialization configuration before switching to dynamics mode Both the two-phase and three-phase dynamic solvers can perform a "cold start" The three-phase dynamic solver must only be used from a cold start scenario. Note: Cold-start initialization refers to a scenario when the initial pressure, temperature, phase velocities, and phase fractions are all set to their cold start-up conditions.

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Dynamic Pig Launching Using Aspen Hydraulics

Aspen HYSYS Upstream

What is Multiphase Pipe Flow? Petroleum production pipelines often include multiple phases (oil, water, gas)

Downstream Pressure

- Sometimes also include solids like sand

Key characteristics/parameters of multiphase flow -

Pressure drop across pipe Flow-rate through pipe Flow geometry Flow patterns can vary Upstream Pressure

Why is Multiphase Pipe flow Important? Design - Accurate prediction of pipeline pressure drops critical to meet production targets for a new production field - Account for ~29% of CAPEX costs ($24B/year in 2012') for deepwater production fields - Bad design can cost billions of $$ in lost production over the life of a field Operations - Troubleshoot operational problems as oil/water/gas mixture changes as field ages - Extend economic life of the production field ln deepwater, pressure drop across riser can be 1OOOs of psi

' "Prospeds for Deepwater Drilling 2008-2012", E&.P, May 2008

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Aspen Technology, Inc.

Aspen HYSYS Upstream

Dynamic Pig Law1ching Using Aspen Hydraulics

Challenges of Modeling Multiphase Flow Large number of variables affect pressure drop - Thermodynamic properties - Interaction of different phases, e.g. interfacial tension - Piping material and dimensions Multiphase mixture is compressible Fluid slip - Large difference between densities of liquid and gas phases cause gas to overtake or "slip by" liquid phase Flow patterns - Fluid phases can spatially arrange in different manner

Stratified Bubble

Mist

Using Pipe flow Correlations ,•Fit experimental

Empirical

data uslng dimensionless para mete ts

'•Develop equatlohs

Mechanistic : to model particular flow pattern

•Large choice of correlations available •None perform across all conditions because developed using specific set of experimental data •Errors in measured data •Many correlations developed for two-phase flow

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Dynamic Pig Launching Using Aspen Hydraulics

Aspen HYSYS Upstream

Aspen Hydraulics Transient Topology Liquid Fraction V$ Axial Distance

Straight Run Convergent Branched Looped/Divergent

.

Solver Technology ProFES Two Phase Transient ProFES Three Phase Transient Two Phase Pigging Model Slug Prediction

·-.-

·.

.

\.

__

- ·-- ·--

•

. \ . \

. •

Liquid Holdup Profile During Pigging

Terrain Induced Flow Induced

~

Dynamic Solver Options

'""'"'"'"'fh,.-,,.,,,•. ,,,. .. ,,..,.,.,,,,., .• TI,.; .... ,"'°' ''"''"'0-~

._,,,,~,~~-o.,

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r ... ,,_.,.,.r>..~,-.,,1 .• """

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,.."'" "~""'"" "'""'"""~-,.

'"'"f'-''"''"''"'''"'"""'""""'"'"·'

,,

©2014 AspenTech. All Rights Reserved.

5

Aspen Technology, Inc.

Aspen HYSYS Upstream

Dynamic Pig Launching Using Aspen Hydraulics

launch a Pig Pig is a type of device used in pipeline operations for cleaning and info gathering Aspen Hydraulics (in dynamics) allows you to model pigging through a line or multiple lines

!0(1.0.

'"""

I

'·'"' I ,~::,I

J•u·O>-,Ntxe""""'~'

,.,,,,_'Ni"'"""''"""'''""""'

"'"'""""""'"

o;-.... ~ ..... ~,...--

.

'~"'F"~°"''

..

'"""""~'"'"'""' ,~,.._

..,,~,

'-"""'" '"""".,.._,..

.

,,,,.,.,,,k-t...,.,,.,,,,,~·~

<:~~·"-.;..-,---::::>

"""'

;_..,.,_'JI

_iGi:)_.,...,...,

Dynamic Pigging Workshop Familiarize yourself with the setup of a dynamic problem in Aspen Hydraulics Set up a pigging operation and illustrate how to integrate this information with an Aspen HYSYS model Review strategies for linking/associating an Aspen Hydraulics model with a pre-build HYSYS Dynamics simulation Utilize Microsoft Excel for enhanced reporting and review of the pigging model

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Dynamic Pigging Workshop

··aspen

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Dynamic Pigging Workshop Objective After completing this workshop, you will be able to provide sufficient information to fully configure and use the pigging operations within an Aspen Hydraulics sub-flowsheet. You will also get an opportunity to use dynamic modeling capabilities of Aspen HYSYS and review some of the basics of the HYSYS Dynamics package.

Description Aspen Hydraulics is intended for use within the Aspen HYSYS® Oil & Gas option and in particular with the Dynamic Pipeline Solver embedded within Aspen Hydraulics. The Dynamic Pipeline Solver is designed for modeling transient multiphase hydrocarbon flows in wells, pipelines, and process equipment. The Dynamic Pipeline Solver solves mass, momentum and energy equations for each phase using a one-dimensional finite difference scheme. Appropriate flow pattern maps and constitutive relationships are provided for wall and interfacial friction, heat transfer, and a model for multi-component phase-change is included. You have learned about using the Aspen Hydraulics sub-flowsheet in the previous module. The purpose of this module is to set up a pigging operation in the dynamic mode of HYSYS and illustrate how to integrate this infonnation with a piping network model. This workshop includes the following tasks: • • • • •

Task 1 Task 2 Task 3 Task 4 Task 5 -

Review the Base Hydraulics Case Transition from Steady State to Dynamics Setup Pipeline Hydraulics for Pig Modeling Merge Aspen Hydraulics with the HYSYS Dynamics Case File Use Microsoft Excel to Enhance Pigging Study

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Workshops

Task 1 - Review the Base Hydraulics Case In this section, we are going to inspect and run the Aspen Hydraulics model that is included with the course files. We will configure a pigging operation and observe how it affects the liquid holdup and other variables in the piping network. o o

Open the supplied case file 05_HydroPigging_base.hsc in Aspen HYSYS. Right click on the hydraulics operation AH-100 and click on Open Flowsheet as New Tab. to reveal the sub-flowsheet.

"~J'" ;;-==--,,. ""

"''*"'

-;--~~--~=;;;;;;- ---~~'''

r===:'-;-;; ~==>----c.:-

·~'

o

o

o

Within the hydraulics sub-flowsheet view the pressure profile across the process by using the keyboard combination Shift-P. Notice that three incoming flows (Alpha-2, Bravo-2, and Charlie-2) merge into a single downstream source (108). Press Shift-N to show the stream names once again. Inspect the elevation profile for the piping network by navigating to the Design I Data page for each pipe. Pay particular attention to Pipe-104. You should see that Pipe-102 declines 60 111 and Pipe-105 exhibits a 60 111 increase in elevation. All other pipes have no elevation change. We can review the liquid hold up for each pipe in the network. This is done by navigating to the Performance I Profiles page for each pipe and selecting the Plot button toward the lower left of the window. After clicking on the Plot button, the plot window appears. Use the pull down list at the top to select the Plot Variables as Liquid Holdup vs. Axial Distance. Compare the liquid holdup for Pipe-104 vs. Pipe-102 and Pipe-105. You should see that the liquid hold-up for Pipe-104 increases with axial distance. Close all the plot windows when you are satisfied.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

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Task 2 - Transition from Steady State to Dynamics In this part of the workshop, you will convert the steady state file into a dynamic file. Please note that this course is not intended to serve as full instrnction of HYSYS Dynamics. Separate training on HYSYS Dynamics is recommended if you wish for a full overview and introduction into that product. In this module we will learn minimum infonnation needed to convert this particular steady state file into dynamics, particularly smrnunding the pigging of a pipeline. o

HYSYS Dynamics requires a dynamic pressure or flow specification all boundary streams (i.e. inlets/outlets). Change the color scheme to Dynamic P/F Specs. To do this, go to Flowhsheet/Modify ribbon. In the Display Options group, change the Color Scheme to Dynamic P/F Scheme. This will make it easier to see which streams have a dynamic pressure or flow specification in place.

o

If the Dynamic P/F Specs is not listed in the drop down list: click on the icon before the field to add the color scheme.

.,,

Temperature

dvisor

Press>Jre

~

ecycle

L;;;il Workbook Table~ Color Scheme · Dffau!t Colour ''.";l>.>.Jy,' "'"'''JI"''· .,:;1,.-.;'

Stre~m l~b~I '~ --------·----------·----..•..

Hide Object·

'ik~Y

p_,,,rr!

'1\l"'-·1<

;

')1_~L~v1.,Ld•!;'

---------------l:f_i_e~-~-~l'. . --··· .. --·-···-_J ______________ _El!P.!!Y_~!~~!- . .-. 11ure Color Sd1eme

'.i~)!l~·~"'.''.D:~C~ra~oo'.~'S~<:h'.'''.m'.~"~....................,,,.. . .~..~--~-~-~--~=--~·~~-~....;~;...l Current Scheme

rr·~~-~~~u_.._____

Add a Scheme

J

-!

1-c~~~~~~~~----------.,.-~~~c. i!!J Sele<:t Query Vari11ble i = @.I Z3 'narnir P/F 5pea eea .• fluid Package /feat Flo.v

<1or.

Heat Of Vapourization Hea•y liqu ~n~ir_v@Std C liq Voi Flow @Std Cond liquid Fraction lower Hea/in!J Vowe Mf!cr:xW Am:iy Data

r'.

I

Can<;e<

MaaoC11t Doto

•i

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Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

o

The color of a stream indicates what type of dynamic specification it has. Green - Pressure specification Yellow - Flow specification Red - Both pressure and flow specifications (over specified). Blue - No dynamic specification. In the main PFD, double click on the Alpha-2 stream. Go to the Dynamics tab. Make sure only flow is checked. Uncheck pressure. Do the same thing for Bravo2 and Charlie-2 streams.

Spec'i Stripchart

·Pressure Specification --

Pressure

Flow Specification -~;

Mofar

<--i

Mass


Std. LiqVol

olar Flow

Active

f;i'

1.000e+004 kgmole/h

o

Make sure pressure is the dynamic specification for the outlet stream (ABCD). '"

-

"

-

-

1<=<1r a lg

MaterlalS!ream: ABCD

L~.?~-~-~~~-:1~i~~fT_e!1_ Dynamics

ISpecs IStnpchart

Pressure Specification -

Pressure

Active

P'

6500 kPa I

Flow Specification ti".);: Molar

'.-J

Mass

t) Ideal UqVo!

-~.:Std.

Molar Flow

Active

-----=2-~94~9e+004 kgmolejl:____

©2014 AspenTech. All Rights Reserved.

liqVot

5

········'·····························'

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Workshops

i'1!!J Go to Dynamics ribbon. Click on the Dynamics mode icon(~::~;" ) to move into HYSYS Dynamics. Aspen HYSYS Dynamics does not prefer flow rate specifications (it would rather use pressure specifications) - that's why you will get the following message:

o

A•pen HYSYS

...........

-A

'Qt

. r',lllWf•

.

-····

--

• -------------------~----

- - ---

The dynamics assi>tant identified i!Em• which neEd attenhon, Would you like to re
y.,

J(

No

J]

o Click on No to ignore the assistant. Note: The Dynamics Assistant is a tool that checks for any improper dynamic specifications within your model. It is intended to aid you with your transition from steady state into dynamics. o

The file is now in dynamic mode. However, the Dynamic Integrator (i.e. time) is on hold. Click the green light to tum the Integrator on.

,~,..;"

Home

i

o o

D'{namks rv1ode

I Dynamics

-

Run

,

.

Get Started

L~~ Dynan1ic Initialization ~Event Scheduler

:lli' Snapshot Manager r.; Modelin.gOption; ,:.•.•...................•...•......

Tai

Snar

- -- -- (~T @_~;!iii.

·: E~~~~J~_".'J~!!!'.?~~j

I

\1-A1,10..-..1><

! lntegr~tior1

Charlie-2

'/,
Time

iU~·i.

J;1: rel="nofollow">'

i :¢rrent T1m<

1

Stop . Re.et

Custon1ize

The Assistant will come back with the same message. Choose No again. It may take few seconds before dynamic solver starts solving. Click on Integrator (it is at the left of the run button shown above). The shortcut command to go to integrator is Ctr!+I. You can view the current time there. The current time is shown at the left hand side bottom of the HYSYS file as well.

lntegrohon Cont•ol

1·

Run

Assistant i ~namic Simulation (j I

I

i;

I

View

[> •.--· .· ·.·- 0

'I

r..t.gritot

1· G•cerai

k(b Integrator Real Tin1e

CT

'~~~~L,,,

''

r



: Ru1 \>me f0
:_stop

D D

Turn the solver off ( ). Save the file as OS_HydroPigging_Dynamic.hsc

©2014 AspenTech. All Rights Reserved.

6

Aspen Technology, Inc.

Workshops

Modeling lleavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Task 3 - Setup Pipeline Hydraulics for Pig Modeling o o o o

Double click on the Hydraulics sub-flowsheet, AH-100. Click on the Dynamics tab. Select the View Pig Options button near the middle of the window. This will open a new window for configuring dynamic pig modeling. Remove the pig already installed by clicking the Delete Pig button. Click on the Add Pig button to add a new pig. A set of default settings will appear in the first column of the Pig Modeling window.

.

""""""""'""

OynamiC.~ Pig Modemtig A1>pen Hyd~a~ik.f-~ub-~heet' AH-100 Name Pig moves with gall vel·

Mode! EntJY Pipe

Entiy lm:ation

b:.t Pipe Exit location Leakage Velocity

IStatus IIPig Position

0.0000 m 0.0000 m 0.010

O.OOOOm/s Not Specified

(tJrrent Pig Segment

'I

SJtJg Fmnt Position Tran~it

Time Position Reference

O.OOOOm O.OOOOm 000:00:0.00 seconds

Current Segment Orlgir

L__ I o o o o o o o

j __C_lo_re_~

Add''•

In the Model row, use the pull down list and select Pig moves with constant velocity. In the Entry Pipe row, use the pull down list and select Pipe-104. In the Entry Location row, enter a value of 0 m. This value implies the entrance of the pipe. In the Exit Pipe row, use the pull down list and select Pipe-104. In the Exit Location row, enter a value of 100 m (328.1 ft). This means the pig will travel a length of 100 m within Pipe-I 04. In the Leakage row, accept the default value of 0.010. In the Velocity row, enter a value of0.4 mis (1.312 ft/s) for the pig velocity.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

The pig is now configured to launch once the integrator starts. The input data window should look like the following:

f-N-~·~~

.

PJG-1 Pig moves with constar

1Model Entry Pipe

Pipe-104 0.0000 m Pipe-104 100.0 m

Entry Location

Exit Pipe Exit Location

Leakage

0.010

Q4000tn/s

Velocity Status Current Pig Segment Pig Position Stug front Position

Ready to launch

o.oooom

o.oooom

Transit Time Position Reference

000:00:0.00 seconds

Current Segment Origh

The pig is ready to launch. However, we need to add a Strip Chart to view the liquid holdup changes with respect to time. First, you need to add the variables in the strip chart. Then you can create and format the strip chart. Note that strip charts are the most common means of view model data in a dynamic simulation in HYSYS. They allow for the convenient tracking of any desired process or control variable with respect to time. o o

Click on Strip Charts folder in the navigation pane. Click on the Add button to add a strip chart. Change the name from DataLoggerl to Waves. Change the logger size(# Sample) from 300 to 3000.

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Click on Edit button to build the strip chart.

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Workshops

Click on Add button to add variables. ;!!..IW••e> . ~t-up : H,-.1~oil c~'re;><-_]

--------~

o

--

--~-----··---·--------·--·---·

Double click on Case (Main) under Flowsheet list. Select AH-100. Select Pipe104 as the object, Profile Liquid Holdup as the variable and Profile Liquid Holdup_l under Variable Specifics. If you can't find the Profile Liquid Holdup, you probably selected stream I 04 instead of Pipe- I 04.

:)] Variable Navigator flc.w
Object H1o'mu!id?efS!ocl:_S•o>o-.'' • Hjdrtw!d?e,fS!ixk_ C/1~rf•e-2 MtXer-100@TPl1 Mi.<er-l01 @TPLl Pip<>· 100 @ TPll Pipe-101 @TPLI

Pipe-102@fP1!

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Object Fi!t~r q,-AJI • 'S1reariv; • tJriitOps

: fr11g!h

Pip.,[email protected]

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i Profile Oii/ante

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i[

(llltom ...

L___

Cancel

Swage·100 ~TPU

Profile liquid H!l!dup (Profifo liquid H!l!dup_l)

o o

o

J

Click the Add button. Staying in the Variable Navigator, select the Profile Liquid Holdup_2 and click the Add button. Do the same for rest of the list. Once you are done with all six of them, close the window. Once you are done with adding the variable(s), the Variables tab should like the following.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

---

Object

---------·--·----~-------

Active

Variable

Pipe-104 Profile Liquid Hofdup (Profile Liquid Ho!dup_

PP"

Plpe-104 Profile Liquid Hofdup (Profile Liquid Holdup_

P

Pipe-104 Profile Liquid Holdup {Profile Liquid Holdup_

Pipe-104 Profile Liquid Holdup (Profile Liquid Holdup_

P:

Pipe-104 Profile liquid Holdup (Profile liquid Hotdup_

17

_ _ _ _ _ _ _Pipe-104 Profi~e li~':"_i~ __Hold~(Profi!e Liquid Holdup

l\1

Delete

o

Workshops

Edit

Click on the Display button (last button at the bottom) to view the strip chart. ~Wave~ ------------------------~

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o o

Make the window bigger or smaller, depending on your preferences. You may close the Waves (strip chart setup) window. Click on Flowsheet Main tab to view the flowsheet and the strip chart.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

:!SJ Waves

CJ CJ CJ

___

,

Start the Integrator (click the green light under Home ribbon or Run button under Dynamics ribbon) to resume the dynamic calculations. Now, go back to the Dynamic Pig Modeling window (double click on the hydraulics subflowsheet I Dynamics I View Pig Options button). Click on the Launch Pig button and observe the system behavior in the Waves window, ~I Dynamics Pig Modelling Aspen Hydraulics Sub-flowsheet: AH- HJO

PIG-1 Pig moves with conrta1 Pipe-104 O..OOOOm Pipe-104

Name Mode!

Entry Pipe Entry location Exit Pipe

lOO.Om

fx>t location Leakage

0.010

Velocity

O.COOOm/5 Ready to launch

Statu'i Current Pig Segment Pig Position Slug Front Position Transit Time Position Reference

r CJ CJ

Add Pig

O.OOOOm O.COOOm 000:00;0,00 >econd> Cuffent Segment Origh

I

<

launch Pig

)

r

Delete Pig

Close ~--

-J

As the integrator runs observe the liquid holdup curves for Pipe-104 along with the Pig Position, and try to rationalize the observed behavior. If the curves are not filling up the majority of the strip chart area, right click on anywhere in the chart area and click on AutoScale All Axes,

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

~Waves

~-I

'354.25

o'

~ 0

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The Status row in the Dynamic Pig Modeling window will indicate when the pigging operation is finished. When done, click the Reset button to reset the pig. The Reset button takes the pig to initial state and sets zero velocity. If you want to launch the pig again you must provide a new velocity. Experiment with different speeds and different spans of the pigging operation. Observe the different situations and interpret the results. You may track any other variables you wish via your Strip Charts. Tum the integrator I solver off. Save the file as 05_ HydroPigging_Dynamic Final.hsc

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Task 4 - Merge Aspen Hydraulics with the Aspen HYSYS Dynamics Case File Our next task is to merge the Aspen Hydraulics sub-flowsheet with an Aspen HYSYS Dynamics case file. o o o o o

o o

Close the strip chart and pig modeling window. With the main PFD view open, use the mouse and select all items in the flowsheet. Right click on it and click Copy. Open the case 05_ TEG.hsc Right click on the main PFD view of05_TEG.hsc and select Paste. The Aspen Hydraulics elements should appear in the lower right of the PFD window. Run the Integrator for a short time. If you get any message, choose OK or NO. Note that it may take a few seconds before the integrator starts while the PVT table processing takes place. You can monitor the messages in the lower left window, or use Integrator (Ctrl+I) to see that it is actually running. Stop the .mtegrator ( lffia~·H;;1cil ' ··). Break the ToSep stream connection with the HPSep flash. Highlight and delete all operations from the Alpha, Charlie, and Bravo feeds through the ToSep stream.

f:C-HF-S~p

.

lpta

PIPE-tO!

,

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1 ).._!_~--0-~U)'·----+...... ±"'l'ZZ-t-s'"'6' 2

ra·,·o

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MlX-lCO

0-Bravo

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Seep

•

art~

o o

Now, highlight and drag and bring the newly pasted flowsheet in place of the deleted portion. Connect the ABCD stream to HPSep as the feed.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Alpha-2

Workshops

HP\ !

Bravo-2 AH-100

ABCD

Charlie-2 o

o o o o

Note that the color of ABCD stream is green. ABCD is not a boundary stream anymore. We don't want a dynamic pressure specification in this stream. Double click the stream (ABCD). Go to the Dynamics tab and un-check the pressure spec. Now the stream color is blue. Start the integrator and the combined simulation should run. Please note that the strip chart from the other PFD is not pasted in this PFD. You need to recreate the waves strip chart if you want to run pigging in this file. Feel free to experiment with any other process variables you wish in this fully integrated model. Stop the Integrator and save the file as 05_HydroPigging Merged.hsc

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Task 5 - Launch Pig from excel to plot the liquid profile along the pipeline Aspen Simulation Workbook can be used to establish a live connection between Aspen HYSYS (including Dynamics) and Microsoft Excel. You will investigate a simple modeling case in this task where you will use a prebuilt ASW interface with a HYSYS Dynamics model for launching a pig. The case aims to show how far you can go in building a custom interface in ASW to show something complex like a pigging model in a more straightforward manner. The HYSYS file models a flow line with following details. Internal Diameter Length Complex Pipe-lCJO: 1 200.0mm

Elevation Change Wall Surface Roughness

lOOOm -20.00m

Mild Steel

4.572e-OOS m

Complex Pipe-100: 2 200.0mm

2000m O.OOOOm

Mild Steel

t.572e-005 m

Complex Pipe-100: 3 200.0mm

100.0m 25.00m

Mild Steel

.572e-005 m

Complex Pipe-100: 4 200.0mm

25.00m 25.00m

Mild Steel

4.572e-005 m

Pipe-100:

5.000m O.OOOOm

Mild Steel

.572e-005 m

200.0mm

The flow line is connected to a separator, the pressure and level are controlled. I

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©2014 AspenTech. All Rights Reserved.

r

=:Ii

LCV-100

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

In this workshop, we are going to watch the liquid profile across the plot for flow line displayed below. Sta1us

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Open Excel file 05_ ASW_Upstream_Dynamics_pig.xis. Select the Aspen ASW ribbon at the top of the Excel window. This contains many of the Aspen Simulation Workbook command buttons. In the Simulations menu of the ribbon, make sure ASW is pointing towards the PIGGING RESPONSE.hsc file. It should be in the same folder as the HYSYS files provided for the course. Click the Active button.

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'PIGGING RESPOMSE

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Run

Click the Start button on the Excel spreadsheet. After staiting the case, observe that the "Updates" cell is set at 8 seconds. If you want the case to run faster, you can increase that setting to 15 or 20 seconds and the case will nm faster, but you will see less detail. You can use that setting to make the case stabilize and after that bring it back down to observe the pigging operation. You can change the liquid valve Cv to 60 to avoid bad control on the level. The pipeline in Excel plots the liquid holdup after pressing Start. For the first pig launch you can leave everything as it is, just stait the Integrator and when the process conditions have more or less stabilized, launch the first pig.

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o o

Workshops

Click on the launch button to launch first pig and see how it affects level control and if you lift the relief valves. You should be able to create a situation where they lift by having a fairly high liquid level to start with. Observe the level and the pressure and also if there is any venting going on. Some venting should be happening. Next change the set point of the pressure controller to a lower value, for example 27.5 bar. Does that prevent venting during a pig launch?

Assuming that 27.5 bar is the lowest you can go in pressure, is there something else you could try to prevent venting? (Possible Answer: if you run the autotuner on the pressure controller and accept the results and increase the LIC proportional gain from 1 to 10, you can prevent venting.) o

Refer to the screen shot below. All the three pigs were launched.

i!'J Dynamics Pig Modelling Aspen Hydtauli~s !iill:l:'~!ll\I.

·.

.

.

Narno Mo\lel

.· ~.l)~,l'Pjp~.

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PIG·1 PiQ moves with·g.L Comple< Pipe•1 OC

PIG-2 11

Pig inoves '.'\1-ith ~ CompleK Pipe·1OC

PIG·3 Pig moves with ~ CompleK Pipe'1OC

~ ----o~ooooril ---------iioooo m --···---- ci.oooo m • . CompleK Pipe·10( Complex Pipe:1_DC · Comolox Pipe-1 OC . Ex~.l.oealion 3125m 3125m 3125m 0.010 Leokago 0.010 0.010 6.388 mis 6.'.)98 in/i Ve10citJI s:o54 mis Active Sfalus Active Aclive :s2irentfig Se!lment· Comple< P1pe-10ll 2 Complex P1pe·1oiF2 Complex Pipo-100 2 ---- -·l 756 ,;;· - - - - - -753.6 ,;;- ------ -4518m Pig Position .· §lu!lf!:'?.nl Position 2151 m 8744 ~13b&oi -- Tfansit Tirtte oOO:Oil 38 oo 00!104 28 00 000 02:48

..~ntry_Loc-tition

Exit Pipe

·· P4sJti0n Refl!!ence .

.

Current Segment I

eddPig

©2014 AspenTech. All Rights Reserved.

.

Current Segmen'tl Current Segment I .

Qelete Pig . ,

17

!;lose

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

A

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©2014 AspenTech. All Rights Reserved.

18

"·' "·'" "·" "'·"' 30.01

Aspen Technology, Inc.

Conceptual Design Builder: Gas Oil Separation Plant (GOSP)

Aspen HYSYS Upstream

Conceptual Design Builder: Gas Oil Separation Plant (GOSP) Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

Lesson Objectives

Understand the capabilities and options in the Aspen HYSYS Conceptual Design Builder Use the Conceptual Design Builder to quickly build a HYSYS model of a Gas Oil Separation Plant (GOSP) Review results in built-in report formats

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Conceptual Design Builder: Gas Oil Separation Plant (GOSP)

Gas Plant Flow Diagram

[!.".~"~

Prop,-,,; 8ul•r-;, l"en!dc·~-''

LEGEND·

Looalod al gas Wlural g>Soline or caslngh~•d guolin~ Penhnes + are penhnes plus heavier hydroc.rbons l<.Jral gasoline l\cid gasH are hydrogen sulfide and carbon d10:.ide Sw.olening processes remove mercaphns from th~ NOL prnduch PSP. is Prusure S"'1n11 /ldsorplion • HGL Is thlural G.s liquids

Appraisal of Assets Evaluate and Rank Development Scenarios

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f I I

R•w

I

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• • • • • •

""" Loc>t•d >t 11» ""II> ,.,,._, Locot•d 1n g•s proco.s;ngpl>nl R-'d lndicole> Hml >>lo> prolos opli<>n•I unH prooe»e> •Y•il•blo Condonsi>!o 1• olllod n.tural g•soline or ca0< • ate P"''hne< plus hO>l'if hydr0<arbon> •nd •llled n>lur>I ll"Olino Acid g><es oce hydrogffi ><JI!< do •nd evbon d romov• m@reopl•n< from the NOL produds PSI\ is s,.;,,g Mso.-pllon NGL<> N>lcx•I Gos Uquids

p,..,._...

©2014 AspenTech. All Rights Reserved.

2

Auto~enerate

"first pass"

HYSYS flowsheet with basic Information using Conceptual Design Builder (CDB)

Aspen Technology, Inc.

Conceptual Design Builder: Gas Oil Separation Plant (GOSP)

Aspen HYSYS Upstream

Aspen HYSYS Upstream V7.3: Oil & Gas Conceptual Design Builder

(

_______________________ _:-~:~ ~~~: ~ Simple Menu for

Options

'""'

Minutes to Evaluate Options!

Gas lift ratio?

Conceptual Design Builder - GOSP Model: Design Preferences (1)

r

-~~fine Separation Pro~-~-~~. ·:;;~~~-

~

desired operating conditions*

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©2014 AspenTech. All Rights Reserved.

3

/~;c'"•

[_1~~::.C~

Aspen Technology, Inc.

Aspen HYSYS Upstream

Conceptual Design Builder: Gas Oil Separation Plant (GOSP)

Conceptual Design Builder - GOSP Model: Design Preferences (2} Define Gas Sweetening and Gas Dehydration Process with its specifications*

C02 I H2S Rrmoval

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Goycol Type

These conditions are used to

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build the HYSYS model of the GOSP plant. The model can be optimized by the process engineer at a later stage.

_____-;_]

"

24-9712

HYSYS Models of GOSP facility

Oi!_To_M>X

Export_Oil 01l_CoOO_M11

GC_Oli_Tee

~uto-generation HYSYS models

[ minutes

©2014 AspenTech. All Rights Reserved.

of

in

4

Aspen Technology, Inc.

Aspen HYSYS Upstream

Conceptual Design Builder: Gas Oil Separation Plant (GOSP)

Introduction to Conceptual Design Builder Reference the following Knowledge Base solutions (via support.aspentech.com): Solution ID 131601 Solution ID 133226

Com::eptual Design Builder Workshop Learn how to define and run the Conceptual Design Builder Generate an Aspen HYSYS simulation via the Conceptual Design Builder Review resource and process modeling data via built-in report formats

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Aspen Teclu1ology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Conceptual Design Builder Workshop

..

aspen·

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Conceptual Design Builder: Gas-Oil Separator Plant (GOSP) Workshop

Objective After completing this workshop, you will be able to provide sufficient information to specify and build a Gas-Oil Separation Plant (GOSP) model using the Conceptual Design Builder tool in Aspen HYSYS.

Description The Conceptual Design Builder is new V7.3 feature that provides a method for entering information to specify and build an Aspen HYSYS Gas-Oil Separation Plant) GOSP simulation model. Based on inputs the user provides in the Conceptual Design Builder tool, Aspen HYSYS builds a simulation model incorporating those user inputs. The purpose of this module is to use the Conceptual Design Builder to enter the basic input requirements needed to generate a simulation model. This workshop includes the following tasks: • • • • •

Task 1 Task 2 Task 3 Task 4 Task 5 -

Project Setup Data Enter Project Specifications Enter Design Preferences Run Design Case and Review Model Build Results Create Excel Reports and Review Data

Task 1 - Project Setup Data To access the Conceptual Design Builder, you only need to open the Aspen HYSYS window. You do not need to create a new case or open an existing case. This section of the workshop will help you start off with the Conceptual Design Builder and provide some basis information for the proposed project. o

Open a new session of Aspen HYSYS, but do not start a new case or open an existing case.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

o

Click on Conceptual Design Builder in Customize ribbon. Resources:

Customize

I 11

OJ Script

Macro language MacrosEditor

~1anager

Conceptual Destgn

Register Extension

BuHder

Tools

You will begin on the first tab of the Conceptual Design Builder and work your way across throughout the workshop. The first tab, the Project Setup tab, provides a high level description of the project. To enter data for the Project Setup tab: Enter a name in the Project Name field- This will be used for information documentation purposes only. You may enter any project description you like in the Description field. This is optional. Define where you wish to save the project on your disk/computer using the Project Location on Disk field. It is suggested to save the project somewhere you'll be able to access with ease. Select North America as the Asset Location.

o o o

o

Note: Entry of an Asset Location will limit the menu choices for the types of crudes available to define the feed conditions on the Project Specification tab. ~Her-..

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Re< av. O•l l\e<et1:e fm3j

«mply>

Oistancef<>W<E>:pott[m]

<e<>1ptf>

Ro< av. G•• Re;IW~ [
<ernp~>

(<>od•c«•IE E>:!Mrt MetMd

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hi;,,., OJ Rt>••~e kn3J

<emp'.y>

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•

<empty>

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Am bent Condi I"'"

«mp~f"

Arnb•ent Temperature lC!

<emp!f•

S..a Wate
<empty•

Wat.t Deptil [ml


-,.,

The rest of the entries on this tab are only used for documentation purposes, and will not be used in this workshop.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

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Workshops

Confom and validate your selections and navigate to the Project Specification tab.

Task 2 - Enter Project Specifications The Project Specification tab defines the feed and design conditions for the project. Default values are provided for all input data, but these will usually be overridden with the actual feed conditions for the proposed asset field. The feed conditions can be defined directly on the form (From Input option) or using data from the crude assay database provided with Aspen HYSYS Upstream. o o o

View the Project Specification tab. For the Feed conditions, select the From Crude radio button option. The choices displayed are limited based on the Asset Location chosen on the Project Setup tab in Step 1. For this workshop, select United States of America, West Texas Intermediate, Cushing, Oklahoma crude.

o o o

Define a Production Rate of 665 m3/h (100,000 barrels per day). For the GOR, specify 150 STD_m3/m3, and for the WOR enter 0.1. Enter Molar Gas Composition as required. In this workshop, we will use the default values.

Basic Design Conditions, such as the inlet pressure for the first gas-oil separator, design and quality specifications for the gas and oil export pipelines, and gas lift and reinjection requirements are also defined on this Project Specification tab. In this workshop, we will use the default values for all design conditions and specifications.

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4

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Ii I

l'~l~t_;~~'!<~CJ!"! E•~fi~;

Workshops

f:'rpt;lf!stiqi Pr?!_>l!!J?i)~il!!!_'lL, ~~ILD~,_'.,Cffi'!igt)_P_!ef~~~

food Cond,ttam From lo!>'"! Q From Crude

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r_~·~;'ii_
lnlo! Pre>wre ikPagJ lnl>: h!>'pefOt\Jra (CJ

Pro
4~98

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011

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SJ~d

4E98.'Yl

5695.68

Ool hportTemper>tu'~ IC]

"

53

"

100000

Des.gn M•'S'" [%]

EOR ISTO_mJ/1nJJ

h! Sepa<Mor -~''"''"'" l~P•gl 01! &port Pressuie [tPag)

N1lr<>gen'.%] CO.If%!

H2S 1%1

''° '·' 633

Ccn!ent l%J

;;;.

8598.68

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ro1;J

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n·Butane (%]

" " "' 82 '·' "'

0]

Ga• lifl P1ew,,., [kPag)

Ga; L!t RequHment

:>898.63

l~"'3ihJ

Gas !nJechon Pre«ute {kPag)

2~89B.7

G~s Jnj«fon Requirement [Nm3/hj

Produced WMerPre«titO [l:P.-g]

-0.02~

Gas QuaMy for Export

C02 rro:.,_ pe«e-"t {%]

°'

Task 3 - Enter Design Preferences Tab Data The Design Preferences tab defines the unit operation preferences for the proposed gasoil separation process. The choices made will be used to build a specific Aspen HYSYS model based on these user-defined design preferences. o o o o o o o o o o o o o

Select the Design Preferences tab. Select 3 Stages for the number of separation stages. For the MultiTrain Setup, keep the default of 1 Train@ 100%. Only the HP Separator should be three phase, so uncheck the 3 Phase options for both the LP and MP Separators. You will not include a Stabilizer Column so keep the default, un-checked option there. Jn the Export Gas Compression section, keep the defaults everywhere. Use a Rigorous Contactor, in a Packed setup, for C02/H2S Removal. Similarly include a packed Regenerator. Keep the defaults for the remaining C02/H2S Removal settings. For the Gas Dehydration, use both Packed Rigorous Contactor and Regenerator. Keep the defaults for Glycol Type and settings. Maintain the default settings for the Gas Lift Compression and Gas Injection Compression sections. When finished, the Design Preferences should look like this:

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Unit OF'"'"
Workshops

Pr~ereCr<e•

"''••mo"<

Sep;irafrJn

Nurnbe• of St"'9•<

gorcos(o~ta
lude Re;ier•e•tor

MultiTraonSet~p

Model foch GOSP Tro'~

GM Lft Comorerno.-.

©

·, 1 Stoge

Trayed O'Pac<e
Ma>omum CcfT'p'""'on Rato

Trayed ,0 P•clc«d

~nterrool
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a_,,,;~. Type

S~plr•le!y

U<e HP hcha<>ger@ Temperoture {CJ

Atrnc,e Ma., Perce~tage

35

., ., . e:

AAw·.e Loading

18.&75

Ac~•at-;ir

, U<e MP E~ch•ngor@Temp<"<'l~te [CJ

i' 3 Pha<e HP Sep•ratc(j)Phooe LI' Sep•'•l@haoe ~P '>epacolor

clAe

GJyoo:

Tempe<~l\Jte

!C lS

Compre«Ol on .... r Type

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00

goroc" ( ontu1or

35

>S

hit

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• TrorM 'l Pock.,d 'T<0yed Q

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MIDtimum Co"'P'""icn Rato

Interceder Exit Temper Mure {C

3~

!nter<0<>lu Pr~;our., Drop {kPa~ -S'

Typ~

Compce"or DrWecType

Gl)«OI Ma» Percentage

I~

NumberOIStage>

fop Pre,.ure jkPagl

E

18675

Pre.,ur~

drop fof e;;portO:l {kl'a/m]

D.1

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l~terOI...-

Ei..t Ten1pera!Ure ICJ

hterrnolet Pre,..ure Drop {kPa9)

Com pr.,«>< Onvet Type M:xle! Each Trai" S..porat~:y

35 -8132~

'J

©2014 AspenTech, All Rights Reserved.

6

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

o

Workshops

You can save your Conceptual Design Builder case if you like. Click the Aspen Leaf button in the top left comer and choose Save As.

'

~-/ Open

I n

o

I :sa..e

Save your case as 06_ GOSP Concept.cdb.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Task 4 - Run Design Case and Review Model Build Results Once you are pleased with your settings and preferences in the Conceptual Design Builder, you can nm the case. This step will create the Aspen HYSYS model representing your preferences from the Design Builder file. o

Click the Run Design Case button in the top left comer of the Design Builder window.

I

-J Production Rate(fud) ;;- Ene .:/ Export f'u-ds Rotl~5,;; GH•

I::,;

./ GORIWOR.CGPJWGR

·..t Gas

, 'J Reveflue _R_eo_o~

I: o

Proflte P101

Unit Operation Preferences

Maximize the HYSYS interface. Watch as the tool builds the flowsheet automatically. This should take 1-3 minutes, depending on the specifications. 01l_To_M1x

GC_Cond Pump

Export_ Oil Oil_Cond_MiK

c 1 - GC_Corid_Pump_Duly

GC_Cond_To_MIX

Produced_Water

GC_Out_Tee

Sw

Inlet

Gas

oo

So cc TEG Dehydration Gas

Swee!enmg

F-6

o

Different sections of the process are built in different subflowsheet. Right click on each subflowsheet and select Open Flowsheet as New Tab. Change Jeon ...

Draw Wire Frame

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

o

Go to the Flowsheet TPLl tab (GOSP_1 sub-flowsheet) to view the details of the Separation section. Note that three-stage separation process model that is built, with water being removed from the first high-pressure stage only.

o

Go to the Flowsheet TPL2 tab (Gas_Compression sub-flowsheet) to view the details of the Gas compression section. Note that four compressors are needed to meet the gas pressure specifications.

o

Go to the Flowsheet TPL3 tab (Gas Sweetening subflowsheet) to view the details of the Gas sweetening section. Note that full rigorous HYSYS column models are used for the absorber and regenerator units. The recycling of the amine solution is also accounted for.

F-301

[

:ET r-F"iF-1l1___,.,.~ •

__

F-101

• Amine

MDEA_IN

Absorber

Ctrl

0-101

X-100

SET-2

Q-100

SET-1

F-13

G0>

R

Sweetening Tnlel

·2

F·9

Regenerntor

F·7

'----------,-!--------..... :J--Crn§ F-4 HExchanger F-8

Pump

Q-201

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

Workshops

o

Go to the Flowsheet TPL4 (TEG Dehydration subflowsheet) to view details of the gas dehydration section. As in the gas sweetening section, rigorous column models are used for regeneration and absorption, and the solvent (in this case TEG) is recycled back to the absorber.

o

You now have a fully integrated GOSP model that can be further manipulated to your requirements.

o

Save the HYSYS file with the default name (06_ GOSP Concept_DesignCase.hsc ).

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Task 5 - Create Excel Reports and Review Data The Conceptual Design Builder can generate detailed Excel reports of both the input parameters and selected outputs from the HYSYS model. Let's take a brief look at some of these reports. o

From the Conceptual Design Builder main window, select the Excel Report button to create rep01ts.

.

v

~

.,_. Run Design Case Run Se'eded Profi'e Cases

Excel

Report ..

HY5YS Model Design

-.

Energy

.J Reverive

Engir.eerfng Reports -. '·-· -·- --.. - ---··

--

"'

v

Production Rate(feed}

Export f1u.ds Rates GHG E1 •../ GOM'VOR,CGRAVGR " Gas :-../ lift Report Profi'e Plots

r·

----

-~P[YJ~§~~~~-!~j~"rPJ~sf~R~U{~P~cLL~.YS!!5~ri~'9fl~~ !>f9f!~~~tj2il:~i?~ifi_1 !1 Jj

Unit Operation Preferences

:· ii

Separation Number of Stages

II

MultiTrain Setup

'··I

ii

\ 1 Stage

· 2 Stages

-PJ 3 Stage>

[lfui~3-·-·- . -··-·-~)

i•

o

Select the Design Case Reports option from the drop down to generate the reports. Two Excel files will be generated. The first, shown below, contains an input summary from the Design Builder as well as some overall design results.

o

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;;

_J --U. p~,te

B

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_____,,_______ , ______ --------------- '---···-····-·· ...... a

.]"'lm~1t

•

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8r~1mat •

§1 1:3

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So•t& fold& -..£ • FEiier • 'iel«t •

~•I::

-------------

c

Design Case Results

1

2.: 3

': I

Production Rate Oil Production Rate[m3/d] 2.1890.94115

Gas Production Rate{m3/d_{gas)J 2895436.76

Conden: rel="nofollow">ate Flow Ra

Water Productlon Rate{m3/d_(gas)J 2568330.29

0.010927957

'Energy Consumption

1 7 Total Compressor Energy Consumption[kW]

Total Pump Energy Con5l.lmpt1on[kWJ

Heating Energy Comumption{kW!

Cool mg Energy Cons

.U40.469443

28070.9776

0

Total C02E-SAR ProducUon[kg/hJ

Total C02£-AR4 Productlon{kg/h) 1854913.296

Utility Name

1558472.164

True VP at 37.8 C of Uport OH[kPag] 11.8&$41386

C02 Mole fraction of E~port Gas 0.070243477

0.01748102

16 ;Amines In Sweet Gas[m3/d_{gas)J

Glyrnls in Ory Gas[m3/d_{gas)]

17 ·4.904575129

76.99342182

Amines In Regenerator Gas Prnduct{m3/d_{gas)] 0.000509095

Glycols in Regenern! 0.021802436

I:

8591.355635

: GHG Emission

10 :rotal C02£-US Production{kg/hJ 11 1558472.164

Power

12 ;Export Product 13 -Reid VP at 37.8 C of Export Oi![kPagj 14 :-92.6244S632.

HlS Mole Fraction o

is. losses of Amines and Glycols

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

o

Save this repmt file as Design Report.xlsx

o

The other spreadsheet is a dump of the Workbook data from the generated HYSYS file. It contains infonnation such as stream conditions and compositions.

o

Save this second report file as Detail Report.xlsx

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Aspen Technology, Inc.

Modeling Real Separators

Aspen HYSYS Upstream

Modeling Real Separators Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objectives Model separators to include carryover so that your simulation better matches real process data Predict the effect of exit devices on mitigating carryover

©2014 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Aspen HYSYS Upstream

Modeling Real Separators

Real Separators (N<>n-Ideal Separation}

In real separators, liquid droplets can be entrained in the gas exiting the separator water can be entrained in oil phase, oil can be entrained in water phase, etc. This has some practical consequences: - Rotating equipment (compressors/expanders) can be damaged by liquid droplets - Contaminants can be carried over - Mass balance around a separator may not match your simulation

The amount that is entrained can depend on process conditions (i.e. increasing the flow through a separator may increase carry-over as it reduces the settling time available for liquid droplets)

Modeling Non-Ideal Separation

Aspen HYSYS "Ideal" Separator - By default the separator unit ops are an ideal, equilibrium separation

Accounting for Carry Over - Aspen HYSYS separators now have two fixed specification options and a third that allows correlations to be used in order to calculate carry over Carry over is calculated in the separator only (streams can not "remember" carryover droplet distributions) Carry over shows up in the separator product streams as a separate phase; for example, resulting vapor product stream

will have some free liquid (vapor fraction will be < 1.0) and the liquid flow rate in the vapor stream will be equal to the calculated carry over

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Aspen Technology, Inc.

Modeling Real Separators

Aspen HYSYS Upstream

Cal'ry Over Options

Specify how much is carried over into each phase -

Feed-Based Specifications Product-Based Specifications

Calculate the carry over based on appropriate correlations -

Generic Correlations Horizontal Correlations Profes ProSeparator Correlations

Correlation Based Carry Over

Steps for setting up correlation-based carry over in Aspen HYSYS: Define carry over option (correlation-based) Enter vessel internals (separator dimensions) Specify nozzle calculations (nozzle locations)

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Aspen Technology, Inc.

Aspen HYSYS Upstream

Modeling Real Separators

Correlation Calculation Method 1. Calculate initial phase dispersion based on feed: Rossin Rammler distribution

2. Calculate phase carryover after primary (gravity) separation Light Liq -7 Gas Heavy Liq -7 Gas Etc ...

3. Include effect of any secondary separation device (i.e., vane pack, demister pad)

Inlet Dispersion Inlet Dispersion is based on: User-specified Rossin-Rammler parameters for Generic and Horizontal correlations Rossin-Rammler parameters calculated from inlet conditions (i.e., flow, nozzle diameter) for Profes ProSeparator correlation Rossin-Rammler Distribution: - F =exp ((-d/dm)')

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Aspen Technology, Inc.

Aspen HYSYS Upstream

Modeling Real Separators

Primary Separation Primary Separation is based on: Critical Droplet Size (Generic) - User specified Settling Velocities and Residence Time (Horizontal) Critical Droplet Size (ProSeparator) - Calculated from inlet velocities - Valid only for entrainment in the gas phase

Secondary Separation Exit Device calculations based on: User-specified Critical Drop Size (Horizontal Vessel) Device specific correlations (ProSeparator) Internals are used to mitigate carry-over - Exit Devices slow down the exiting vapor and provide a surface for droplets to coalesce; i.e., mesh pads, vanes

- Weirs are used to increase settling time for the liquid phases

I For Aspen HYSYS "exit device"::::: gas exit only I

©2014 Aspen Tech. All Rights Reserved.

5

Aspen Technology, Inc.

Aspen HYSYS Upstream

Modeling Real Separators

Real Separators Workshop

""'"""'°1"'""' l•~""'~--Hn

'•~'""'"'

><~-"'""d

'

....·~-''"""""-'

..

..,_,,.,,,,,_0~>

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• -t-.··r1A .,.... ., '~

.. , .. '

-..

;,,~--·~'·~-"

Real Separator Workshop Open the Real Separator Starter.hsc file to begin workshop Follow the Real Separators workshop instructions Begin from an ideal separator and progress through by specifying and then calculating carryover

©2014 AspenTech. All Rights Reserved.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Modeling Real Separators Workshop

aspen

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Modeling Real Separators Workshop Objective The Aspen HYSYS Separator nnit operation nonnally assumes perfect phase separation, but it can also be configured to model imperfect separation by using the Real Separator capabilities. The real separator offers the user a number of advantages, including carryover definition so that your model matches your process mass balance or separator design specifications as well as implementation of exit devices for mitigation of carryover. The workshop will focus on using the Aspen HYSYS Real Separator capabilities to model imperfect separation in a 3-phase oil-water-gas separator. This workshop also includes an exercise where a demister pad is added to the model as a secondary separation device to reduce liquid carryover into the gas product.

Description In real world separators, separation is not perfect: liquid can become entrained in the gas phase and each liquid phase may include entrained gas or entrained droplets of the other liquid phase. Recent years have seen increasing use of vessel internals (for example, mesh pads, vane packs, weirs) to reduce the carryover of entrained liquids or gases. This workshop will cover some of the following applications of real separators in Aspen HYSYS.

Carryover Optio11 As with many other unit operations, Aspen HYSYS allows you to increase the fidelity of your separator model to account for non-ideal effects. Aspen HYSYS has introduced Real Separator capabilities like the carryover option. This option can be used to model imperfect separation in both steady state and dynamic simulation. Gas and liquid carryover can be specified or calculated (three different correlations are available for this purpose).

Vessel /11ter11a/s Internals used to reduce carryover can be included in your separator model with some of the provided carryover correlations. Internals used to reduce liquid carryover in the gas product are termed "exit devices." Weirs are used to improve heavy liquid - light liquid separation in horizontal vessels.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Nozzle Calculations Included with the carryover correlations are calculation methods for inlet and outlet nozzle pressure drop. Inlet and outlet devices can be included in these calculations. The user can also specify pressure drop if the carryover option is not in use.

Dynamic Models of Real Separators The dynamic model of a separator must account for changing pressure and flow due to liquid levels, nozzle pressure drop, and heat effects. As such, vessel geometry, including internals and nozzle geometry and heat loss parameters need to be specified. Modeling imperfect separation with the carryover option and a specifiable PV work term are also available. Level taps can also be set for monitoring the relative levels of the different liquid phases. All of these items can be set up using the Rating tab.

Limitations oftlte carryover option As droplet distribution is not a stream property, this information is not passed onto the product streams. While droplet disttibution is not passed on, product streams containing carryover will contain multiple phases with the phase flow rates equal to that predicted by the carryover calculations.

SpeciJYing Carryover The Aspen HYSYS separator allows the user to directly specify what fraction of each of the feed phases is entrained in the other phases. Product-based specifications are also allowed. This gives you a simple method to match your material balance to your design assumptions or your real world separator.

Calculating Carryover There are three sets of correlations available to calculate phase dispersion and carryover. A detailed description of each method is given below. All three follow the same basic calculation sequence: I. Calculate the initial phase dispersion based on the inlet feed. All three methods assume the dispersion follows a Rossin Rammler distribution. 2. Calculate the ca1Tyover after the primary separation (gravity settling) of each phase in every other phase; specifically: • Light Liquid entrained in Gas • Heavy Liquid entrained in Gas • Gas entrained in Light Liquid • Gas entrained in Heavy Liquid • Light Liquid entrained in Heavy Liquid • Heavy Liquid entrained in Light Liquid

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

3.

Workshops

Based on the exit dispersion from step 2, calculate the effect of any installed secondary separation device (for example, demister pad or vanes) on the liquid carryover into the vapor product. (This is not applicable to the Generic correlations.)

Correlation Details Three different correlation models are provided: Generic, Horizontal Vessel, and ProSeparator™.

Generic Correlation The generic correlation should be used when your only criterion for separation is specifying a critical droplet size. Inlet phase dispersion is calculated using a generic method that ignores vessel geometry- the user specifies inlet splits and Rossin Rammler parameters and these are used to calculate the inlet dispersion. Carryover is calculated by assuming that all droplets smaller than a user-specified critical droplet size are carried over.

Horizontal Vessel Correlation The Horizontal Vessel correlation is designed with the horizontal 3-phase Separator in mind. Inlet phase dispersion is calculated using inlet device efficiency (rather than specified splits) and user-supplied Rossin Rammler parameters. Primary separation is calculated based on settling velocities rather than critical drop size. Each phase has a residence time in the vessel. A droplet will be carried over if it does not travel far enough (back to its parent bulk phase) in the time allowed.

ProSeparator Correlation The ProSeparator correlations are rigorous but are limited to calculating liquid carryover into gas. Both light liquid and heavy liquid entraimnent is calculated, so 3-phase separators are also suppo1ted, but no carryover calculations are done for the liquid phases. Inlet phase dispersion is calculated based on inlet flow conditions and inlet pipe size. (ProSeparator calculates its own Rossin Rammler parameters using this infonnation.) Primary separation is based on critical droplet size; however, the critical droplet size is not user-specified, rather calculated using gas velocity through the vessel. Secondary separations accomplished by exit devices (for example, a demisting pad) can be calculated by specifying a critical drop size (Horizontal Vessel) or through the use of device specific correlations (ProSeparator). Inlet flow regime, Nozzle Pressure Drop, and Exit Device Sizing can also be calculated using one of the various Horizontal Vessel correlations.

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Aspen 'fechnology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstreatn

Workshops

Rossin Ramm/er Parameters Rossin Rammler distributions are defined by: F = exp(-d/dm)z) where: F = fraction of droplets larger than d dm is related to d95 x=RRindex d95 = 95% of droplets are smaller than this diameter for the specified dispersion RR Index = exponent used in the RR equation (also known as the "spread parameter") Real Separators i11 Aspell HYS YS Using S11b-calculatio11s If desired, the user can use a different correlation for each of the calculation steps. In this case, a correlation is specified for each sub-calculation, rather than specifying an overall correlation. Only those parts of the correlation that apply to the particular sub-calculation will be used. Sub-calculations will not be used in this workshop.

For example, ifthe Generic correlation is used for the Inlet device and ProSeparator is used for primary L-L and G-L separation calculations, then the user-supplied data for the generic inlet calculations (that is, inlet split and Rossin Rammler parameters) will be used to generate the inlet droplet dispersion. The ProSeparator primary separation calculations will then be perfonned using this inlet dispersion. As ProSeparator correlations will not be used to calculate the inlet conditions, any ProSeparator inlet seh1p data is ignored. Likewise, any critical droplet sizes entered in the Generic correlation will be ignored as the ProSeparator is being used for the primary separation calculations. This workshop includes the following tasks: • • •

Task I - Build an Ideal Separator Task 2 - Specify Carryover Task 3 - Use Carryover Correlations

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Task 1 - Build an Ideal Separator You will use a pre-defined HYSYS case as a basis for your separator calculations. Open the case 07_Real Separator Starter.hsc.

o

The starter case is a model of a two stage compression train. The feed hydrocarbon stream is mixed with the recycle of the first compression stage and sent to a low pressure separator. It is this low pressure separator that you will model using the real separator capabilities of Aspen HYSYS. o o o

Create a material stream and call it To LP Sep Clone. Double-click the To LP Sep Clone stream. The stream property view appears. Click the Define from Other Stream button at the bottom of the window.

Y'::t'••

!·.rv1~.r1~lsi1.,;lrrl:folil~geµ·tk>~e

[M.;_s!lrni~!'_J_Di_Y!'_:~~~L=======-=~·=:::c::::c=:==· -==~-======·==========

Worksheet . Worksheet Conditions

·-·1

Properties Composition Oil &Gas Feed Petroleum Assay K Value User Variables: Notes Cost Parameters Norn1alized Yields:

To lP Sep Clone

Stream Name Vapour I Phase Fraction Temperature fF]

<empty> <empty>

Pressure [psia]

<empty>

Molar Flow [lbmole/hr]

<empty>

Mass Flow [lb/hrj

<empty>

Std Ideal Liq Vol Flow [barrel/day]

<empty>

Molar Enthalpy [Btu/lbmole]

<empty>

Molar Entropy [Btu/lbmole-Fl

<empty>

Heat Flow {Btu/hr]

<empty>

Liq Vol Flow @Std Cond [barrel/day] fluid Package

<empty> Basis~l

Utility Type

...~---------------------~ L-------------------..-.-_-_-__-____-_-_-::_-::_-::_..-.. ------==----------_-__-::_-_-_-_-_-_·_.•-·.::::··---------

o o

Jn the Available Streams list, select To LP Sep. In the Copy Stream Conditions group, keep the default conditions and click OK.

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Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

=

~ Spec Stream As

. -Available Streams

ni

@]

-Chosen S-tre.am Conditions

[~:~:~=~~;·;;;;~

, 'RCY-1 Out

; ! RCY-2 Out Stage 1 Out

. .. . ----- . .

o;~:~

Pressure

19765 6.2885e+005 9.936e+004

J

!Mas'> Flow 1. Std Ideal Liq Vol Flow

Copy Stream Conditions

-4.386e+004

Molar Enthalpy

'Vapour Fraction

1--~~~:_~~!!.:iEt._____

Mclar Er.tha!py

i

435.11

IMolar Flow

34.331

Mol;u fnlropy

[./]Temperature

- -----------------

Mole Fractions

Fll

Pressure

f:l]

Composition

[_;/] Correlations

C02

[;II

Flow

Fil Cost Parameters

Ethane

Nitrogen

Methane Propane

Flow Basis '!.))Molar

I-Butane n-Butane

:·Mass

0.176629 0.075154 0.050819 0.050831

n-Pentane

0.044065 0.033891

n-Hexane

0.030450

i-Pentane ' ) Liquid Volume

0.008318 0.010738 0.519104

I

i"I

1i

11 t_ _'.

'

i

-- 'i

( 0.-2 o

o

Create a new stream called Water and specify the following conditions: In this cell...

Enter ...

Temperature

Same as To LP Sep Clone

Pressure

Same as To LP Sep Clone

Mass Flow

4000 kg/hr (8818 lb/hr)

Composition

100% Water

a

Add- Mixer and provide the following information: Enter...

In this cell ... Connections Name

MIX-100

Inlet streams

To LP Sep Clone Water

Outlet stream

Feed

Parameters Set Outlet to Lowest Inlet

Automatic Pressure Assignment

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Aspen Technology. Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

Add a 3-phase Separator and specify it with the following information: In this cell ...

Enter ...

Connections Name

V-101

Inlet stream

Feed

Vapor stream

Vapor

Light Liquid stream

LLiquid

Heavy Liquid stream

HLiquid

o

The separator should calculate. Open the separator unit operation and select the Worksheet tab.

o

What is the vapor fraction of the vapor product stream? What is its molar low rate?

o

What is the molar flow rate of the LLiquid stream? HLiquid?

o

Save your case as 07_Ideal Separator.hsc.

Task 2 - Specify Carryover As a hypothetical exercise, say that we know (from a plant mass balance or as a design assumption) that approximately 800 kg/hr of liquid is entrained in the vapor product of our separator. How do we specify this in our model and ensure an accurate mass balance? o o o o o

Select and open the V-101 separator you just created. Select the Rating tab. Click the C.Over Setup page to bring up the carryover models, and choose Product Basis as the active model. Select Specification By: Flow and set the Basis = Mass. Enter 800 kg/h (1764 lb/hr) for Light liquid in gas.

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Aspen Technology, Inc.

Workshops

Modeling lleavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Sizing Nozzles Peat loss ; Level Taps

c) None

! Feed Basis

Specificat10n By

'O C.Over Setup

· · · :,;:;0o~hp;~;· ~-----___

f

i

C::

I light liquid m gas i Heavy liquid m gas I Gas in fight liqufd . 1

soo.o:)

6.&w I O.COGO

Heavy hquid in light liquid

0.0000

Gas in heavy liquid

0.0000

[. ~ig_ht liq~id in heav_y _liqu_id

0.0000

fi] Use 0.0 as product spec if phase feed flow is zero

l~! Carry over to zero f!ow streams

[C] Use PH fla~h for product streams

• • • • • • • • • • • • • • • • • • • • • • • • • • • • l~l Ignored

o

Examine the product streams and the C.Over Results page and compare to the ideal separation case.

o

What is the vapor fraction of the Vapor product stream?

o

What is the liquid flow rate in the vapor product stream?

o

Save your case as 07_ Carryover-Spec.hsc.

Task 3 - Use Carryover Correlations As an alternative to specifying the carryover, we can use correlations to predict the carryover: o o

Return to the C.Over Setup page and change the model selection to Correlation Based. For the next few steps, select the appropriate radio button. Using the Correlation Setup radio button, go to the Overall Correlation menu and select the Profes ProSeparator correlation.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Phas,'Separator:·\f.1{Jf

J···o~~;g·~·--r·R~.~·~t.!~~~JR;;ii~~ l-~P-~-~~~~1-Prrl_~_f11_,_,_s Rating

1

C<1rry Over Mode!

<> Product Basis

-::··Feed Basis

·J None

Sizing

·-Q; Correlation Based

Nozzles

Heat loss level Taps Options C.Over Setup COver Results

o o o

ix' Correlation

Setup

-:-· i DP I Ncnzlf': Setup

' Dimensions Setup

Correlation Setup Correlation Calculation Type

·CJ' Overall Correlation

Sub Calculations

Click the View Correlation button to enter inlet and separation parameters. In this case, the Inlet setup page can be left as is. The ProSeparator correlations will calculate the inlet dispersion without the need for further information. On the Yap. Exit Device page, we could define some secondary separation device for the vapour outlet. Since we do not have an exit device in the current calculation, we will set this accordingly for the Pro Separator correlation. Select Mesh Pad; enter thickness = 0.0.

PrQfes 'cafiY.OV'er Corhr~l~ri <.. V.,f&,i

s~~~---r~~i~'i't<_l Setup

: Select Vapour Exit Device ·

Vane Pack

C'§r Mesh Paj)

ap. Exit Device Mesh Pad Method

c~ Loffter/Muh!)

Pad thickness[~~]·-·-·-·--·-···-··"- ....-..... Wire diameter Imm] Pad voldage Specific

~urface

;;·) Carpenter/Othmer/Stairmand

"C:""''"o"'."'oo"'o..... "'O> 1.000 0.9COO

area [m2/m3J

0.1000

~ffler/~_u_hc_b_e_to_ _ _ _ _ _ _ _ _ _ _ _ _1~

o o o

Close the View Correlation window. Choose the Dimensions Setup radio button. Enter the vessel dimensions as length 8.0 m, diameter 3.0 m, light liquid level 1.5 m.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Carry Over Model

Rating

iSizing

'.None

(_-~ Product Basis

Feed Basis

,j;, Correlation Based

· Nozzles

··> Correlation Setup

Heat Loss

Level Taps Options

,. ~' DP I Nozzle Setup

- Dimensions Setup

C.Over Setup

Vess-el Orientation

COv,;,r Results!

[J

[Vessel length [m] Vessel diameter [ml Weir height [m]

I I

~PrJ"'!"

IWeir distance from feed [m]

[{] Has Boot

<:empty>

iBoot diameter [m]

1.000

iBoot height jm]

...

I Light liquid level [m]

[_r::.~-~.:Y.~.'~-~-i~. .~.::".:_t_ J_rl_1 l

f"] Carry over to zefo flow streams

o o

Has Weir

f'""J

t~.a~;zi I

Use PH flash for product streams

Choose the DP I Nozzle Setup radio button. Enter the following values for nozzle location (this is the horizontal or radial distance from the feed location): Feed 0.0 m, Vapor 6.0 m. Keep the default values for nozzle diameter and height.

L_D-~~~~~1~~~~~-~~] Rating

Rating T_~O!~~e_e~_J-~~~~~:;--1 ______ _ I Carry Over Model

I

I1 Sizing

None

·, Feed Basis

Nozzles Heat LOH Level Taps

Ci Correlation Setup

Options

Pressure Drop I Nozzle Setup

Correlation Based

'~J DP I Nozzle Setup

( ' Dimensions Setup

C.Over Setup C.Over Results

-~!

'Product Basis

Active

i --r "1 _ _ _ _ _ _ _ J ,~I_j

~

i:.:.J Cany over to zeto flow streams

[_J

Distance from feed end or side of vessel

U~e PH flash for product streams

[]Ignored

o

There are several pages where useful results are displayed. First, open the Worksheet tab.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrean1

Workshops

o

What is the vapor fraction of the Vapor product stream?

o

Open the Rating tab and select the C.Over Results page. To view the carryover details, click the View Dispersion Results button. Select the Gas Product radio button on the left and you should see results similar to this:

o

M.assflow Droplet Diam.

Internal F!ow

JkglhJ

Imm]

"·, Ga5 Feed :• Light liquid Feed · : ' Heavy liquid Feed ev1ce

'Q.• Gas Pfoduct ·· light liquid Product Heavy liquid Product

4.5&ie-003

6.620e-002

L252e-002

1.920e-003

9A25e-003

0.8187

2.530e-002

2374e-002

L478e-002

7.366

3.967e-002

0.2136

2.080e-002

38.15

5.584e-002

0.6657

O.DOOO

2,758e-002

157.3

7.403e-002

3.520e-002

440.8

9.450e-002

OJJOOO

4378e-002

984.7

0-1175

0,0000

;ci

I

5.343e-002

2038

0.1434

0.0000

I I

6A28e-002

3810

0.1726

0.0000

i

7.650e-002

6420

0.2053

0.0000

9.024e-002

792.6 O.OC(JO

02422

0.0000

0.2837

0.0000

0,1231

0.0000

0.3304

0.1426 0.1646

0.0000

03829

0.0000 0.0000

-0.0000

0.4420

0,0000

_0,_1~94

0.0000

0.5084

0.1057

I Total Carr; Over

1A69e+004 kg/h

Q.<JOOO

Total Carry Over

0.9050 kg/h

Dispersion Plol

' lgtln Gas Feed

CJ

Hvy.Jn Gos feed

[

Gas Jn lgt.Liq.feed

t r lgt In Gas To Exit -

'"" scoo

[J Hvy.ln Lgtliq.Feed

I [.-: Hvy In Gas lo Exit

i:--:f

I

Lgt.!n Gas Product

lWO

CJ KV';.ln Gas Product I J Gas In Lgtliq Product

moo

Gas In Hvy.tiq.Pre
I

~

;i

Hv>;.In Lgtliq Product

..

CL COO

Lgt In Hvyliq.Product

MOO

S_QC0..-002

-

0.1000

.

~

0.1500

-

~

~

02000

Oiameter(mm}

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

o

We need to eliminate all droplets larger than 50 microns (0.05 mm) in the Gas Product. Do we need an exit device to do secondary separation?

o o

Open the Rating tab and select the C.Over Setup page. Select the Correlation Setup radio button. Click the View Correlatiou button and make sure the Setup tab is showing. Select the Yap. Exit Device page; select Mesh Pad and enter a thickness of 100.0 mm.

o o

Setup

Results

.Select Vapour Exit Device l.i.!.ljlj;l.--...o1.._ I ' ' Vane Pack ' Setup

~

Mesh Pad Method

:0;~

Mesh Pad

.9: Loffler/Muhr

(~J

Carpenter/Othmer/Stairmand

Pad thickness {mmI Wire dia;n1eter [mm]

0,%00

Pad vaidage Specific suriace area [m2!m3]

0,101)0 1

Loffler/Muhr beta

o o

Return to the C.Over Results page and view the Dispersion Results. How efficient is this mesh pad at removing droplets larger than 50 microns?

o

Save your case as 07_ Carryover-Calc.hsc.

It is expected that the inlet hydrocarbon flow to the separator may vary by up to 25%. Anticipating that the separator may not be able to handle this increased flow, the detailed design engineer decides to model the new conditions in the separator and design a demister pad to remove the larger droplets.

o o o

Increase the flow rate of the To LP Sep Clone stream by 25%. Select the C.Over Results page, and then click the View Dispersion Results button. What is the Total Carryover with no mesh pad?

o

What is the Total Carryover with a 100 mm thick mesh pad? Is this sufficient for removing droplets larger than 50 microns?

o

Can you think of a way to detennine the mesh pad thickness such that the flow of droplets larger than 50 microns is sufficiently small? Are there any tools in HYSYS that will help you make this detennination?

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Aspen Technology, Inc.

Tuning Viscosity

Aspen HYSYS Upstream

Tuning Viscosity Modeling Heavy Oil & Gas Production and Facilities Using Aspen HYSYS Upstream

lesson Objectives Introduce the basics of modeling fluid properties for different oil-type fluids using the capabilities of Aspen HYSYS Upstream Use Aspen HYSYS to model fluid properties using various features built inside Aspen HYSYS Tune viscosity calculations to match measured or desired viscosities

©2012 AspenTech. All Rights Reserved.

Aspen Technology, Inc.

Tlming Viscosity

Aspen HYSYS Upstream

Tuning Viscosity Viscosity calculations are tuned based on the following: Library and Hypothetical components - Directly editing the viscosity index - Using Tabular properties

Assay data entered through Oil Manager - Providing viscosity curve

Assay data entered through RefSYS Assay Manager - Providing viscosity curve on Macro Cut table

Indexed Blended liquid Viscosity The Indexed Viscosity option enables you to toggle between two methods/rules used to calculate the blended liquid viscosity Aspen HYSYS Viscosity: Provides an estimate of the apparent liquid viscosity of an immiscible hydrocarbon liquid-aqueous mixture using only the viscosity and the volume fraction of the hydrocarbon phase Indexed Viscosity: Uses a linearized viscosity equation from Twu and Bulls

- Note: The viscosity index option is only available for the following property packages: Peng-Robinson, PR-Twu, Sour PR, Sour SRK, SRK, SRK-Twu, and Twu-Sim-Tassone

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Aspen Technology, Inc.

Tuning Viscosity

Aspen HYSYS Upstream

Pure Component Viscosity Aspen HYSYS calculates the viscosity of a pure compound based on the - component class designation - the phase in which the component is present - temperature range

HYSYS selects the appropriate model using the following criteria: Liquid

Vapor

Sy'!item

Light HCs (NBP
Non-Ideal Chemicals

Modified Ely and Hanley Twu Modified El v and Han I ev Modified Letsou-Stiel

liquid-Aqueous Apparent Viscosity Aspen HYSYS Viscosity provides an estimate of the apparent liquid viscosity of - an immiscible hydrocarbon liquid-aqueous mixture using only the viscosity and - the volume fraction of the hydrocarbon phase.

The estimates of the apparent liquid phase viscosity of immiscible Hydrocarbon Liquid - Aqueous mixtures are calculated using the following "mixing rules": Volume fraction of HC phase >=

05 Volums frad1on of HC phase < 0.33

O 33< Volume fraction of HC phase <05

©2012 AspenTech. All Rights Reserved.

3_6\ l ~1~11 =

~'cf/=

~Lo;1e

[

v.,, 1J

Ol] ~ln,o

(Pot/+ OA~tH I + 2.5v oili 1 \ ~ 1 otl + ~ 1 H2 0 ·

-

The effed•'{{! viscosity for combined l1qurd phase is calculated using a weighted average be1W1len ab()lla two

e uation

3

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Tuning Viscosity

Aspen HYSYS Upstream

Hypothetical Component Viscosity (1)

The viscosity coefficients of A and Bare first estimated, based on the initial specifications from the Hypo Group property view If you want to calculate these coefficients, you can override the estimation by clicking the Edit Vise Curve button - This allows you to enter a set of data points of temperature versus dynamic viscosity

Hypothetical Component Viscosity (2) Aspen HYSYS will recalculate the values of the viscosity coefficients based on the data points you entered - Note: The values of the viscosity coefficients A and B will then change from blue to black indicating that they are calculated values

~,..,,'.~--~~-------

'

I ,...,,....... ii

I'

"·'·~-~--~,

•~·,

'--""'""d .•.,,.,, ..

r"" "'"'~.: :;, . ";'.~,..

1-·*-···

©2012 AspenTech. All Rights Reserved.

···"·~''"

-""''c'"""

. -·;.·a·· ,....,..

-. ~

I

~--8: 4

H,_,

®c_,,._.;.;:;··c...:.;-

Aspen Technology, Inc.

Tuning Viscosity

Aspen HYSYS Upstream

Editing Viscosity Using Tabular Properties ( 1) Tabular Package calculations are based on mathematical expressions that represent the pure component property as a function of temperature The values of the property for each component at the process temperature are then combined, using the stream composition and mixing rule that you specify The Tabular Package can regress the experimental data for select thermophysical properties such that a fit is obtained for a chosen mathematical expression

Editing Viscosity Using Tabular Properties (2) ~ PropCUNe: LiqVisccv;tty~NBptlJ229'

Wt FiKlor

20.0000 40.0000 50.00W

110.8001) 40.7900 28.3700 <empty>

Pe~ding

©2012 AspenTech. All Rights Reserved.

101.3150

101.315(} 101.3250

LOOO 1.000 LOOO <~mpty>

Tabu'ar [nput

5

Aspen Technology, Inc.

Tuning Viscosity

Aspen HYSYS Upstream

Tune Macro Cut Viscosity Data In the Settings tab of the Macro Cut table you can edit the viscosity index parameters

Tuning Viscosity Workshop Begin by adjusting calculated viscosity by tuning the Viscosity Index and Viscosity Coefficients for a component View how to tune calculated viscosity by utilizing Tabular Properties Modify crude oil assay data to tune viscosity by working with the Macro Cut table options

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream Tuning Viscosity Workshop

'aspen

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Tuning Viscosity Workshop Objective In order to model pressure drop or to calculate heat transfer area, the transport fluid properties must faithfully be calculated. There are various methods used to calculate transport properties of oil in flowsheet simulators. The choice of method depends largely on the data available to the modeller, which may be limited to simple field data or include detailed lab analyses. In this workshop you will explore possible procedures for modeling fluid transport properties, namely for process streams defined using the built-in Aspen HYSYS Upstream Oil & Gas Feed option. Note that other 3'a party applications can be associated with Aspen HYSYS for the purpose of modelling oil & gas fluids properties. As an option, these approaches may be covered as pa11 of separate training on Aspen HYSYS Upstream.

Description This workshop will introduce the user to the basics of modeling fluid properties for different oil-type fluids using the capabilities of Aspen HYSYS Upstream. It assumes that the user already has familiarity with the Aspen HYSYS user interface. In this module, you will use Aspen HYSYS to model fluid properties using various features built inside Aspen HYSYS. In Aspen HYSYS Upstream V7.3 you will be able to select different methods to calculate

the fluid properties for the reservoir fluid on a process stream. The fundamental calculation is to mix oil, gas and water in an appropriate ratio to match user-specified transport properties. Hypo component liquid viscosity values are adjusted in order to match the desired viscosity value.

Transport Properties (Viscosity) Details In Aspen HYSYS, bulk viscosity can be calculated in two separate ways. The Viscosity option appears on the Parameters tab when the Peng-Robinson package is selected Note: The viscosity index option is only available for the following property packages: Peng-Robinson, PR-Twu, Sour PR, Sour SRK, SRK, SRK-Twu, and Twu-Sim-Tassone

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Package Type!

Con1ponent List Selection

HYSYS

Property Package Selection

Options. _ _ _ _ _ _ _ _ _ _ _ _ _ __ Property Padc;g-; EOS ----] Enthalpy

Antoine ASMESteam

Densit>;

Braun K10

Costald

Modify Tc, Pc for Hl, He

BWRS

ChaoSeader

Indexed Viscosity

Chien Null

Peng-Robinson Options

Clean Fuel.s Pkg Essa Tabular Extended NRTL GCEOS Genera/ NRTL Glycol Package Gray5ofl Streed Kabadi-Danner Lee-Kes!er-Plocker Margules MBl/IR NBS Stearn NRTL

Parameters

i i

'1

HYSYS Vi5cosity

EOS Solution Methods

- · I [·--~~exed Viscosity---~-~-------I ifil"ill'k~::,~~

De-fault

Phase Identification Surface Tens.ion Method Thermal Conductivity

HYSVS Method API 12A3.2-1 Method

PRSV <:;"'u<::R!(

The Indexed Viscosity option enables you to toggle between two methods/rules used to calculate the blended liquid viscosity. Description Provides an estimate of the apparent liquid viscosity of an immiscible hydrocarbon liquid-aqueous mixture using only the viscosity and the volume fraction of the hydrocarbon phase Uses a linearized viscosity equation from Twu and Bulls

Aspen HYSYS Viscosity

Indexed Viscosity

Pure Component Viscosity Aspen HYSYS calculates the viscosity of a pure compound based on the component class designation as well as the phase in which the component is present as well as a temperature range. HYSYS automatically selects the model best suited for predicting the phase viscosities of the system under study. The model selected is from one of the three available in HYSYS: a modification of the NBS method (Ely and Hanley), Twu's model, or a modification of the Letsou-Stiel correlation. HYSYS selects the appropriate model using the following criteria: System

Vapor

Liquid

Modified Ely and Hanley

Ely and Hanely

Light HCs (NBP<155F)

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Workshops

Heavy HCs

Modified Ely and Hanley

Twu

Non-Ideal Chemicals

Modified Ely and Hanley

Modified Letsou-Stiel

Note: Twu method is known to do a better job of predicting the viscosity of heavy hydrocarbon liquids. The Twu model is also based on the corresponding states principle and uses a viscosity correlation for n-alkanes as its reference fluid instead of methane. Liquid-Aqueous apparent Viscosity Aspen HYSYS Viscosity provides an estimate of the apparent liquid viscosity of an immiscible hydrocarbon liquid-aqueous mixture using only the viscosity and the volume fraction of the hydrocarbon phase. The apparent liquid viscosity calculation in Aspen HYSYS for an innniscible oil-water mixture assumes an oil-water emulsion to be present. 1 This is important to note. Emulsions usually result in higher viscosity and more conservative (i.e., larger) pressure drop calculations; in many cases it is appropriate to take this conservative approach. In scenarios where greater accuracy is required, it is advisable to use lab analysis to confirm if an emulsion is present or not. The estimates of the apparent liquid phase viscosity of immiscible Hydrocarbon Liquid Aqueous mixtures are calculated using the following "mixing rules": System

Effective Viscosity

Volume fraction of HG phase>= 0.5

Volume fraction of HG phase < 0.33

0.33< Volume fraction of HG phase< 0.5

The effective viscosity for combined liquid phase is calculated using a weighted average between above two e uation

Where: µeff

= apparent viscosity;

µH2 0

=viscosity of Aqueous phase;

µ 0 i1 =viscosity of Hydrocarbon phase VoiJ

=volume fraction of Hydrocarbon phase

Liquid emulsion viscosity options in the HYSYS pipe segment model 1 An adaptation of Woelflin method (for oil-like emulsions) and Gambill (for water-like emulsions) is detailed in Appendix A.5.4 of the Simulation Basis manual.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

In Aspen HYSYS V7.3 CPI, the Levinton/Leighton, Guth/Simha, Bamea/Mizrahi, and Brinkman models have been added as emulsion viscosity options in the HYSYS pipe segment model. These models are extensions of Einstein's and Taylor's models for higher concentrations. Pipe Segment PIPE'100

D~-~"i~~[j~~j~h~~[~~~-~~~~~~~~I~~~rf?!.~-~-~~~-~l~Y-~~~~±~E:~~~~
··Emulsion Viscosity Method -

i Connections i Parameters

i Notes

Brinkman

Guth and Simha levinton and Leighton Barnea and Mizrahi Gen. Exponential General Polynomial

Hypothetical Component Viscosity Coefficient Estimations for viscosity can be further improved over internal estimation routines by supplying the experimental viscosity for a hypothetical component. Experimental viscosity curves can be supplied via hypothetical properties or user data in Aspen HYSYS directly by mapping the library component as a hypothetical. The Thermodynamic & Physical Properties property view displays the Thennodynamic and Physical properties for the Hypo. Aspen HYSYS estimates these values, based on the base property data entered and the selected estimation methods.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

~ C6-Clo•

ro L~!!c_a1 _[~~il-~±~~-U~~p~~p 1-TyJXl J_ ________ 1-Component Ide11tific.,tion

i Component Name

(6.(10"

i Family I Class

Hydrocarbon

, ; Chem Formu!3 i !10 Number

21)(.'()0

I I

-Visc~sityType

I1 ,_; -~1nemahc

i ...... I

1 i Group Name

l-fypoGroup2

! [£~~~~".1-~~-~ -

=

~ Edit Viscosity Curve

---·

'9' Dynamic

Temperature

..t:<-c

I

ICJ

, · UNIFAC Structure

No 5tnietureAvai!ob/e

>->~

User ID Tags

Dynamic

. -·

I Vise

50.00 80.00 100.0

0.7000

150.0

0.4000

e~~tt:_

.

@]

0.9000 0.6000

----- ------ -- __ :_~~E!r>__

...................

Tag Number

1

<empty>

Tag Te)(t

Not Spec'd

.......
J)

f"---- Oe!eti::

The viscosity coefficients of A and B are first estimated by Aspen HYSYS based on the initial specifications from the Hypo Group property view. If you want to calculate these coefficients, you can ovetTide the estimation by clicking the Edit Vise Curve button. This allows you to enter a set of data points of temperature versus dynamic viscosity. Aspen HYSYS will recalculate the values of the viscosity coefficients based on the data points you just entered. The values of the viscosity coefficients A and B will then change from red to black indicating that they are calculated values.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Workshops

Indexed Viscosity Indexed Viscosity used to calculate the blended liquid viscosity. Indexed Viscosity uses a linearized viscosity equation from Twu and Bulls. In the Viscosity Index Parameters group, you specify the value for each of the three parameters used in the linearized viscosity calculation. The equation below displays how each parameter is used in the Twu and Bulls (1981) calculation. loglO [(loglO)(v+0.7)] = mloglOT+b Where: T = absolute temperature 0 R and v =kinematic viscosity in cSt The above equation can be simplified to obtain the following expression for the viscosity index: A log!O [(log!O)( v +c)] + b Where: a = constant at a fixed temperature;

v = kinematic viscosity in cSt

c =adjustable parameter;

b =constant

The mixture kinematic viscosity is calculated from the equation below:

loglO(loglO(v + c)) = L:-')loglO(log:lO(v;+ c))) i

Where: v = kinematic viscosity of the mixture in cSt; v; =the kinematic viscosity of pure component i ;

c =adjustable parameter

You can specify the values of the parameters (Parameter A, Parameter B, and Parameter C cells) used to calculate the blended liquid viscosity.

This workshop includes the following tasks: • • •

Task 1 - Tune the Viscosity Index Task 2 - Utilize Tabular Properties Task 3 - Tune Macro Cut Viscosity Data

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Task 1 - Tune the Viscosity Index In this workshop, you will leam how to tune the viscosity index parameters to achieve desired viscosity value for the process stream. A hypothetical component is created to mimic the behavior of polystyrene both as a pure component and solution. The objective is to get the polystyrene solution viscosity and mass density closer to actual measured values. You will tune various constants to meet these values.

o

Open Aspen HYSYS and load the file: 08_Polystyrene Starter. '----~S~tyre"n,•,_ _ __,

Viscosity

I . 0.1295 I cP

Mass Flow

I

13607.?-'!.. J.~~.'.~-

Styrene

E-Benz.ene

Mixer-Outlet

MIXER

Mixer-Outlet

viscosity

Polystyrene

3-446

cP

Polystyrene Viscosity Mass Flow

o o o

3.774e+006 29483.81

cP kg/h

Click the Properties environment. Go to the Components folder and view Component List - 1. Double click on Polystyrene* hypothetical component. ~ Polystyrene•

11o·r<:;;;;~~ 1 l~iit~iii.~il'J]Jii~!~l'liYI'~] _ Base Propertl es

Molecular Weight Normal Boiling Pt

2.000e+OOS

[CJ

704.4

1121

Ideal Liq Density [kg/m3] ,-Critical Properties

I

[CJ I, ~-;,;~p~rature Pressure [kPa]

865.2

I

199.8

[

792.9

Volume [m3/kgmole]

i Acentricity I_

1.371

-------------------~

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l

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Click the Critical tab. Check the properties of Polystyrene*. Do the same for the library component Styrene. Compare the two using the following table:

o

Click the Point tab for the Polystyrene* component. Note the values for the Viscosity Coeff A and Viscosity Coeff B. l ~l ~ -~

~ Polystyrene*

ID.I Critical I Point I TDep I UserProp I Type I - Additional Point Properties @ Thermodynamic and Physica l Props

0

Property Package Molecular Props

O.OoOoO 179.65451

Dipole Moment [Debye] Radius of Gyration [Angstrom]

1.25000 845.84448

COSTALD (SRK) Acentricity COSTALD Volume [rn3/kgmole] Viscosity Coeff A Viscosity Coeff B Cavett Heat of Vap Coeff A Cavett Heat of \lap Coeff B Heat of Form (25 C) [lcJ/kgmole]

2.00000 0.30000 0.22806 0.00000 -l .<J00e+007

Heat of Comb (25 C) (kJ/kgmole]

<empty>

Enthalpy Basis Offset (lcJ/kgmole)

-3.B96e+ 007 0.26000

Rackett Parameter Zra

o

Using the following table, track the calculated stream viscosities as you alter the A and B coefficients for the polystyrene hypothetical component. Use the A and B values shown in the left-side column and note the calculated viscosities for each set. Coefficients

Stream: Polystyrene Viscosity, cP

A= 0.5,

B=0.3

A=1 .0,

B=0.3

A= 1.5,

B=0.3

A= 2,

B=0.3

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Stream: Mixer-outlet Viscosity, cP

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

Workshops

Make sure the A and B parameters for polystyrene are back at their defaults of A 2.0 and B = 0.3.

CJ

=

Now we will try working with the Indexed Viscosity option to tune the flowsheet mixture viscosity. CJ CJ

Select the Fluid Packages folder. View the existing fluid package. Click the Parameters tab. Change option hldexed Viscosity from HYSYS Viscosity to Indexed Viscosity. 51_...1 P•9~ ,

Pt<>pertie>

+

PR

~"'C'"~··:;;•;;;;;;;;;c;;; ·--I I S.t lip [B.~.,,-~?.•_•~9!1., [T•_knl!a• f N~1~_]

._.....,,.

~ -:.jP•trnl•umA"•~•

' :-JOilMonog"'

Po
lflSVS

Prop•.ty P•d•9< S•lcchon

Option<

P"""'''l i>~
'!nl~OIFf

A""'1!P!g

'.:}Compon

Anto;,,e AS/1£5/fa,,-,

~~ Uw Prope1tie>

H<0u" KW H~IRS

OaoSeod
CiiiMNv!i Clrn~ Fu Pl:-j : EH~ Tcbula' Exl~-~JN Nll:'ll.

;GCE05

Modlylc,Pclorl-l2,He

·1

\lisrn<~y!nd&Por•mdm

jP;,~,;,-rl~;:-'A·

-

p,,,mrt ... ·a·

;lndu•dVi«o<;t.J

lp_.,_•md_or·c:

ihn9-P.ob1n
:rns >otut1on M
-i1Af-~

~

A• 1oglO(l<>gl0(1;1n>»<(i) + C)) + O o ..i.ufl

·Ph•" ld
Surioa Ten•ion Method

HY5YS MetOOd

Tfi«mol Conduc\O/;cy

:.:;,,,~,,_,;11:in

! Glr«15t>-e"1 K~bajt-D<moer

l•e-Ke
'"'"'P'" /.18;.'il;' NliS~t~am

•r.wn

'Oll_El«l
"Pf!-T""

CJ

Try adjusting the Index Parameter "C" and note the effect on the Mixer-Outlet stream viscosity in the main flowsheet. Use the following table in your analysis: Parameter "C''

Stream: Mixer-Outlet; Viscosity, cP

C=0.8 (default) C=1.4 C=2.0 C=2.6 C=3.2 C=3.8 C=4.4 CJ CJ

We would ideally like to get the Mixer-Outlet stream viscosity to equal 1000 cP. Which parameter gets us closest to the desired viscosity? Save this case as 08_ Polystyrene.hsc.

Note: The Oil-Gas separation plant will be built with only streams 'Reservoir 1 'and 'Reservoir 2 '.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

The oil and gas production from reservoirs I and 2 enter the separation plant at a controlled pressure and proceed to a 3-phase separator. This separates the gas, crude oil, and water phases

Task 2: Utilize Tabular Properties The Tabular Package can regress from experimental data for select thermophysical prope1ties such that a fit is obtained for a chosen mathematical expression. The Tabular Package is utilized in conjunction with one of the Aspen HYSYS property methods. Your targeted properties are then calculated as replacements for whatever procedure the associated property method would have used. Although the Tabular Package can be used for calculating every property for all components in the case, it is best used for matching a specific aspect of your process. A typical example would be in the calculation of viscosities for chemical systems, where the Tabular Package will often provide better results. Tabular Package calculations are based on mathematical expressions that represent the pure component property as a function of temperature. The values of the property for each component at the process temperature are then combined, using the stream composition and mixing rule that you specify. The Tabular Package provides access to a comprehensive regression package. This allows you to supply experimental data for your components and have Aspen HYSYS regress the data to a selected expression. Essentially, an unlimited number of expressions are available to represent your property data. There are 32 basic equation shapes, 32 Y tenn shapes, and 29 X term shapes, as well as Y and X power functions. The Tabular Package provides plotting capabilities to examine how well the selected expression predicts the property. You are not restricted to the use of a single expression for each property. Each component can be represented using the best expression. You may not need to supply experimental data to use the Tabular Package. If you have access to a mathematical representation for a component/property pair, you can simply select the correct equation shape and supply the coefficients directly. In this portion of the workshop, you will be asked to convert your heavy black oil stream to an Oil & Gas Feed stream. The main purpose is to get the same viscosity between two methods. You will provide the assay viscosity data to a light oil to correct the overall viscosity. For the heavy oil, tabular method for black oil will be employed to achieve the desired behavior.

o o

Open Aspen HYSYS and load the file: 08_BO Starter.hsc. Double click on the streams: Bow River Heavy Well A and Bow River Heavy Well B to view their data.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

IWor:h:,:·l-:;~-~~n~L:~:7I: 1,'

1'

eam1t10tn Propert,e<

Temperatu1e

g~,~~::7;: " I

0

Petroleun> A«ay K Value U<erVatiable. Not..s Co;t Paf3me1"r< NorrMhed y,eldo:

Bow River Heavy Well,

Ga<

o.,

40.00

40.CO

40.00

<000

0.0000

C.IJOOO

o.ooco

o.ro;o

!C!

: PEe«.Ufe [kPdg]

«:mpt/>

Volu'Ylelric Flo# IJl
() 7642

Water

SG_re•_to_~ir

21.98API_60

6.171APJ_60

3345e+OOS rn3/d lA24e•005

1311e+005 SlD_rn3/d 1289e•004

J400m31d

0.0000 m3/d

114 7

5:'.4.4

129Se•OOS 74.IJ.1

<emptj>

Spe«fic G, 0-,;ty(Std. D•w»ty {@
Mo-. Ent~alpy [k!ikg)

Fluid

Workshops

ilad~ge

oro;o

e~,is-I

Bulk Properties

: Produced GOR:

97.38

Water(ut

~

0

: Oil Phase Spe<:ifa Propertie•

ISurface Ten•ion;

19.62

Watso~

K:

12.09

M~teml Slrii~-tii; ~ !Uvtr f{f;aiy Wtu a·

! Worhhet _~~~~~~~~l~-~T_ic!J__ Wofk""""t Corn:Hion< Properties Ga< Ccmpo
01l&Gasfe..d Petroleum Ass.ay

"'""'Nome Temperatu•e [Cl

90.00

90.00

840.0

8400

840.0 6.111 APl_60

[Pro rel="nofollow">sure[l<.Pag] Spe<.v [@stc)

K Value User '/~liable•

Mass Flow (@:s1c) !kgfh]

Note•

Fluid Pa•kage

o,,

Bow Rlv~r Heavy Well I 90.00

m3fd

1370e•006 STO_m3/d

l9.85Af'l_60 6788 m3/d

3.78Ee+OOS

5.J31e+004

2.657e+OOS

5984e+004

277.3

6221

173.5

434.7

<empty> 137Se~006

Ma.< Enthalpy {k!/kg]

0.7642 SG_reU<>_aEr

1401 m3/d

Bo•~·l

Cmt Param'"t'"r<

Noimal1zed Yield•

Blolk

Prnperi~•

Produced GOR;

101.8

IWater Cot

17.l

Wat'°n K:

12.08

Ot! Phase Specific Properties

Surface Tension

CJ

22.M

Review the data for the two streams and verify it with the table below:

840 22.98

18.85

6.271

6.271

97.38

201.8

Water Cut

0

17. 1

Watson K

12.08

12.09

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea111

C02 Nitroaen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane n-Heptane n-Octane

o o o o o o o

0.0028 0.0053 0.7875 0.0825 0.068 0.0099 0.023 0.0055 0.0074 0.0049 0.0019 0.0012

0.0028 0.0053 0.7875 0.0825 0.068 0.0099 0.023 0.0055 0.0074 0.0049 0.0019 0.0012

Return to the Components folder and Copy the existing Component List twice. Name the first copied list Well A and the second copied list Well B. Navigate to the Fluid Packages folder. Create two new fluid packages, one titled PR-Well A and another called PR-Well B. PR-Well A should be using the Peng Robinson property package with component list Well A. PR-Well B should be using the Peng Robinson property package with component list Well B. Check yours versus the images below: ~·~. ~~ge

set

• '-::?.;Componm!L1si; CJ Component l•>I · l

l'K·Wri1' • • "'!"

Up : ~;,,oryco"u1; J St;b_T~t"} P~!~.~-Ofd~l-T_.b~1~.J.N?1«.,

; ; Pachg•

~;P·"' - - - ~SYS

(ompon•nl Ld Selection

C:Su~ !.~~~ ..Oa,i~_w..Ja:>- ----------- ---

[~$WellA Op~~n<

C
I

Enthalpy

Par>mrters -- -

_!ii Ba>i•-1
;1,-,-,MPirg

Oe11>1fy

A~IG-i?e

ASMESt<~m

ModifyT<, p, for HI, Ho

Ci>PrtroleumAm1y>

s,a.,~

•

.

I:.~ Reacticns

1-4 Component Map> 1:4 U1er Properli«

~;:.;a~:~. I

---~--P
Mod
KJ(I

8Wl1'5 ChooSnC<• CIHM llvi! Ci"Mfoti>HJ fs
-

. Pmg-Robinrnn Op!ioo•

!EDS Solution Methods

HY5V5 Cuhk ms Allalytkal Method Oef.... lt

I

Me!hod

i

AP! UAl.1-1 M~thod

!

: Pha•• kfontdicol
Conductivrty

Hv<;Y~

Gruy'~~st1ed

K"ba:li·Oo~rt' !ee-1'.~s!<>-Piocker

M.c
I, NBS S~•~"" NI/TL

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

All Roms ~h

sg Component li>I l

Workshops

uP- :~~:~_o_df~ l s_t_•-~I!>!_[~~-"1~~·:.!J j~~d!!~~_]

Pdck•ge T~P"'

____·i

HVSVS

~.ii Well A ~~'Nell B

Prop My Package S..l&tion

(lp_tion<_

Ami•>ePlg

Oomi!y

Antoi~<

Modify Tc, Pc for Hl, He

"

C,~ Petroleum As
CQ 011 Manager • CJ Roacticms [,~

Ccmpcnen! Map<

1:ci U rel="nofollow">or Prctperttes

·p;~;:typ;-~-[05

fothalpy

,;:; flutd Package•

'; i

(O
A5Mf51
lndox•d V1>eo.,ty

ChaoSeader Chi•~ /\/uli Ci.an Fu< Ptg

EOS Solu~ion fl.M~ods

Modlfy Tc. Pc for H2, He

HYSYSVis<:osity

HVSYS

Pong-Robimon Option>

Cubk EO.S Anatytlcal Method Defa!,lft

E"oT~bu~ar

HYSYS Method

Surface Ten<100 Mtlhcd

I Cxl:cndtdNRrL 'GCWS

~e;ma1_:_~-~~~~'.::~:~.-.----- --~,.----- APl~~!_:_~-~M_•<_""" __

'Gi:vco1 " " 'P~ckagc '"'" Groy>M Slr.< MIJWll NBSSlram Nl?Tt

PllSV

o o o

Go to the Home ribbon while you are in Properties environment and any folder but Oil Manager. Click on Associate Fluid Package available in oil group. Select PR-Well A from the Associated Fluid Package drop down list. Check the box under Associate to associate it with Case (Main).

er 1-typothe!icol "-1.n•qer "«j, Ccnv~rt

l\ o"

Monoq.,-

Conv~fllo

,;;,1

tJDetimhom•

A!pM P
'.1 Option• o"

Rdininq A"•V

Chpbcrnl Properties Alllt•m•

~--~

1i<J:.N1un<'.

J!1 Fluid Package A.>ooaled with 011 Manager

11.

[;'&Fluid Padagn L~Ea.si<·l Ce;PR·W~llA i~i$PR-Well

f'low>heet

Mu;d Pack•ge !n U;e

Ca>e(M01n)

To

Enl~!

1he Oil envi«>ru-nen~ There m,,;t

b~

a

Ba•is-1

B

fluid Pack<>ge and the a••ociatN Property Pad:.oge

"'""Y"

(':.Petroleum LJ 0;1 Monager

must N able to

h~ndle

Hypo Comp~en\s

[QReaLtlOM

o o o o o

I

.1

ii

Close the Fluid Package Associated with Oil Manager window. Double click on the Oil Manager folder in the navigation pane to expand the folder. Double click on Input Assay and then click on Well A assay. Review the Bulk Properties data to ensure the standard density is 22.98 API_60 and the Watson K is 12.09. Click the Calculate button to ensure the oil is calculated.

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Aspen Technology, Inc.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstrea1n

Ar.~']

Input D.aW

Def;nition

r~::~:~~:~;:~:~~t

Bull: Properfes None

Ass.ay Datil Type

----~-- 22.9:~7i~~ ··1

Watson UOPK

12.09

Viscosity Tjrpe

Dynamic

V;scosity 1 Temp Viscosity 1

<empty>

IV'.>cosity2Temp

so.ooc

l_~-~~~~itr_~------

20.00 c

---------~~e!!~

I I

I.

Mo!e
o o

Expand Output Blend folder. Select User Points cut option and set the number of cuts to 5. Cut Ranges Cut Option Selection

5

Number of Cuts:

o o o A<
Add a new Blend and select Well A to be added to the blend. Rename it as Blend-Well A by doing right click on the Blend-1 on the Navigation Pane. Click on the Install Oil button.

Solection •nd 01llnform•M~ Odflo..,lnfom rel="nofollow">•t·o~

flow Un;!• W•U A

tiqu1J V
flow Rate

Nurn~r~f(u"

~emi>ty>

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Aspen Technology, Inc.

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Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o o o

Type the stream name for the blend as PR Well A. Set the Flowsheet to Case (Main). Click on Install button.

I =l@l

tt;.:,~ B!end-1; Install Oil -

cancel

Install

o o o

Go back to the Simulation environment and click Yes on the message to replace the property package. Open the stream PR Well A and review that there is composition data. In the Oil & Gas Feed form, select Oil & Gas Feed with Bulk Oil Properties. Input the following values: Std Liq Density, 22.98 API; Watson K,12.09; Total GOR, 97.38; Total WOR, 0. Number of stages is I. Temperature and pressure of stage number 1 are 15 C and 0 kPag respectively. rWarksheet 1

l~!t~~h~~rn,.,ts,.,..,,,.,Dy<,,n,,•,,.m,,i_c,,s,i,,,====='1

Worksheet Conditions Properties Composit_ion I Oil & Gas Feed ' Petroleun1 Assay \ K Value

Oil & Gas Fe~ with Bulk Oif P1 • · Oil Properties ······· ············· · · · ··· · ·

I~~.~~: ~.~,~-~---,.---~~~~-_!

User Variables

Notes Cost Parameters ' Normalized Yields;

o

Click on the small grey arrow on top of the Gas composition section as seen on the image below: ·Gas Composition --------------~] Mote 0/o :~J Mass% Vol% Mole%

C02

0.0000

Nitrogen

0.0000

Methane

0.0000

Ethane

0.0000

Propane

0.0000

i-Butane

0.0000

n-Butane

0.0000

©2014 AspenTech. All Rights Reserved.

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-1 SJ

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o

Workshops

Introduce the composition for the Gas as the same of the stream Bow River Heavy Well A: Bow River Heavy Well A Gas component

Mole%

0 28 0.53 78.75 8.25 6.80 0.99 2.30 0.55 0.74 0.49 0.19 0.12

Nitroaen Methane Ethane Prooane i-Butane n-Butane i-Pentane n-Pentane n-Hexane

n-Heotane n-Octane

o o

o

On the Conditions page, specify the Temperature, Pressure and total Mass Flow as 40 C, 0 kPag and 142389.54 kg/h. Add a three phase separator to the flowsheet and feed the PR Well A stream into it. Connect new streams for the vapor, light liquid, and heavy liquid products as well. Record the stream mixture viscosity values for both PR Well A and Bow River Heavy Well A. _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ __

o

Save your case as 08_PR Well A.hsc.

o

Go to Condition page in Bow River Heavy Well A and click Viscosity Mtd button. The resulting window shows the viscosity data used by the Black Oil definition.

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Workshops

~ Black Oil Viscosity Method Selection ASTM Equation -~~--

------~

l_~!'cifv two or more visc~_sitv ~oints

Method Options:

Viscosity

•

Temperature

110.8

20.00

40.79

40.00

28.37

50.00

-- ---~-~ITil'_~'.'. ________________________________________________<_~~!'-~:>____ _

Next, we will put this data into the Tabular option in the Properties environment to improve the prediction of viscosity. Return to the Properties environment and go to PR-Well A in the Fluid Packages folder. Select the Tabular tab in the fluid package view. Check the option Enable Tabular Properties.

o o o

-<

Properties

~~--lte_m_:___~-----~-"-'!. Cci Component Lists

A

Tabular P.Kkage

Ca Fluid Packages

------~-----.----

r

~ Basis-1 ;[{/,PR-Well A Wi) PR-Well B

i,

Configµration ,,. Options: All Properties

!~Petroleum Assays

II

L~ Oil Manager I~ Reactions

o o

Basis For Tab. Enthalpy (ideal gas) «Q: H = 0 at 0 K (HYSIM Basis)

) H = Heat of Formation at 25C

ii

User Propertieo;

H

Expand the Options at the left, and select the Physical menu item. Check Viscosity (L) in the Use HYSYS column. For the Comp. Basis, choose Volume instead of Mole.

All Items

C& Component Li,U _,, LO Fluid Packages

f.2; Basl~-1

{:s_~_ 'Jp J_ ~i-~JY.f ?~_f!~ .l.§t.,.P!~~--LP.~-~-~~.9~~~-r_fTu~I~;- L~~-t-~ ·,---2:~~ra~:9e 1 !-_. Pro~ertyT;;~-~-,--:"u;;HvsYS

l

C~PR-Wel!A

!

Cl! PR-Well B

j

C;,1 Petroleum Assays

C& Oil Manager r~-~

I

i

Cd, Component Maps C~

Physical Thermodynamic Information Notes

-Global Tabular Calculation Options 1 : F;t:J Enable Cate. On Active Property [.~] Enable Tabular Prop-ertie!>

O--->=---

,. Options

j

ii

iI " I.

-

i

Viscosrty(V)

All Propertie~

;

Viscosrty(l)

Physkal Thermodyn.,mic Information

,

Thermal Cond(V)

Viscos1ty(l)

©2014 AspenTech. All Rights Reserved.

The<mal Cond(L) Surface Tension

18

r

f;T

r

r r

Use PPOS

r r r

- Comp. Basis Volume

Mixing Param.

033

r r

Aspen Technology, Inc.

Workshops

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

In the Information menu item, select the Viscosity (L) form. Scroll over to the first hypothetical component, and select any cell in its column. Then click the Comp. Prop. Detail button.

o o

f..t li,"f i,.,~ [»
O-q;_,o;

'"''''9"''°'"1 Of""'' I ;'""'"'"'"'"' ,,.,,._.,.

.::~~;,[;I i;~~~,:~:,,

,,

1.=

IC:~;

~,y

!Ct."¥>

J<»J

"'"Xl

>{oo:r~""'

;.:>;<J

H'<'~

''""' .w;o ,,,,,t

•15'

"•;· ,.,,,;

.;..,,;

,,€J5

,0/)

10~0

,!<"''"'"

[""'"" c.r~

._,.,

CoC"Y

JI;)!!

.. •Q

hW

;.('00

Ht'~

1.w

'"'-~ u;.,

S0.'9 l'BS

'"'"' ><'a>

131'1

UY

iP.J

~~,.,

'iiA.1

;;n

-$~~~

-a•e

.:;;:

;o;,;

..... ···········------~~":'°:""'~·~·_11111111111111111111111111__- - - - - -

o o

,~,,)

JO~;

-!!5'

;i\O

-~------------

J.4

,.,,, ;c;,; _,,,J

.•......•.••.••..•..•..•.•....

In PropCurve view, select the Table tab. Clear the existing data by clicking Clear Data button. Change the temperature units from K to C. Input the data you found in the Black Oil stream (Bow River Heavy Well A) into the table. Set a pressure of 101.325 kPa for all three data points.

o

·;lJ PropCurve: UqViscosity_N8P{l]229~

1.-~~;~~i~~:-i-c;~~T 1ab1e P~:~~L~?~~~:i_

,:m'"''"'~]

I

20.0000 40.0000 50.0000 <empty>

Wt Factor

Q

v 110.8000 40.7900

101.3250

1.000

101.3250

1.000

28.370-0

101.3250

1.000

<empty>

<empty>

<empty>

Press Regress button to update the equation cQeff:cienl:s after table i11put

[

o o o

Regress

____ _

Click the Regress button. Repeat this procedure of entering the viscosity data for each hypothetical component associated with the PR-Well A fluid package. Reh1m to the flowsheet and compare the calculated viscosity values at the following temperatures for the two oil streams mentioned.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Temperature, C

Viscosity in Bow River Heavy Well A, cP

Workshops

Viscosity in Well A, cP

20.0 30.0 40.0 50.0

Through this approach, all oil hypo components should have the same viscosity data. The stream viscosity will only change with temperature and pressure. o

Save your case as OS_Tabular Viscosity Well A.hsc.

For the stream Bow River Heavy Well B, we have the viscosity data as follow

I=

'1 Black Oil Viscosity Me.thod Sel<0
?:s

§I

ASTM Equation

Metho
Specifv two or more viscositv points

Viscosity

Temperature

1134 29.44

20.00 90.00

_ _ _".':fll!'ty_:____________<efllp_~>__

o

Repeat the same procedure as used with the Well A stream to create a new stream Well B, and enter the above viscosities as tabular properties for the PR-Well B fluid package.

o

Save your case as OS_Tabular Viscosity Well B.hsc.

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

Task 3: Tune Macro Cut Viscosity Data Starting from HYSYS V7 .3, the user can input viscosity at four different temperatures for each hypothetical component (38, 50, 60 and 100 °C). When using HYSYS-based viscosity calculations, two parameters, ThetaA and ThetaB, will be calculated internally based upon input viscosity at the four different temperatures. In earlier versions, if the hypo boiling point was less than 300 °C (the cut off temperature) then only the viscosity values at 38, 50 and 60 °C was used, whereas for higher boiling hypos, viscosity at values 50, 60 and 100 °C were used. With V7.3 and later versions, these viscosity settings can be configured in the Petroleum Assay Manager Settings page. You can specify the cut off temperature as well as whether all viscosity data for each hypo is used without any cut-off temperature. MauoCutOata: Str'eam •Siad( OffStream

Spec_ific_~_ti~-?~~] .......................

-

Pro~uct

-Input Datil ~,

Bulk Pro~rties Afld Distillation

'- !

Cut Distil!ation

9.•

Available

Not Available

I

Only Bulk Properties

I

Input Viscosity Settings ~r

Dynamic

Assay Source Info

' · Kinematic

Viscosity Temp A

19(

Viscosity Temp B

BOC

Viscosity Temp C

60(

Viscosity Temp D

100(

Region

North America

Country

Canada

Assay Name

Cold Lake blend [Edmonton]

Assay ID

COLOF008

Dislil!ation fitting Fa.dor

-Viscosity Cakulation Method

·9' Refutas

Fitting Factor

J

· HYSYS

Refutas A

lJ.47

Refutas B

23.10

Refutas C

0.8

You can use the Macro Cut view, Settings tab to set the Input Viscosity Settings to your preference. Enter viscosity data in Kinematic or Dynamic form. This data can be entered at four temperahires; Viscosity Temp A, B, C and D (enter the temperatures in ascending order). Viscosity Calculation method:

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Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

•

Refutas based method (Indexed viscosity)

•

HYSYS Viscosity (uses EOS mixing).

Workshops

If Refutas Viscosity Method is selected, enter index parameters Refutas A, Refutas B, Refutas C.

The material stream bulk Viscosity is calculated using an indexing method and there are two methods available. One method uses 0.8 as the parameter constant and the second method uses 0.08 as the parameter constant.

&'mix=

L,x1 xlog(log[\lj+C]}

Ythere: Ub = viscosity of blend U/ = viscosity of component I

XI

= composition fraction

of component I

C = parameter constant

In this workshop, we will take advantage of the Macro Cut table options. We adjust viscosity in the Oil and Gas Feed option using the Macro Cut table. In this workshop, a black oil stream has been converted into Oil & Gas Feed. Instead of using bulk properties in the Oil & Gas Feed, a predefined oil assay has been selected. o o

Open Aspen HYSYS and load the file: 08_MacroCnt Starter.hsc. Double-click the Black Oil Stream and select Oil & Gas Feed. Choose the Oil & Gas Feed with Oil Assay Info option.

Ethane

0.0000

Prq:a1"~

0.01100 0.(10(10 O.(IU(JO

i-Bulane

Co•I Patamet•" Normaliied Y;eld•

n-Butane

; i n-Pentane

0.0000

0.0000

., ;

i_L-------~----..i

GOR Spedic3lion N'1mber Of Stage> , 519 No

. Temp

i

[CJ

Pres. {kPagj

Q,I fle>w Tarqet

TotalGOR Total WOR l Stock Tank Oernitv

©2014 AspenTech. All Rights Reserved.

22

<emply> i <emptv> i tv:>

i

<.emptv>

i

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

o o o

Workshops

Click the Select Assay button. Select North America as the region, Canada as the country, and choose the Cold Lake blend assay. Click the Import Selected Assay button. ~

~

@]

! r:·:i

Sel&tffisaylolm,port:______________________________________________________ •____________________

_

~ -

-

_I

Se led A!. say To Import

l.J.e I

'f4tt4!.buta

'f

Cold lake, Albert•

i red&d!EJ t!g/lfond Medium, Alberto Gvlf Alberto, L&f{ A!Derto Rainbow light .:ind Medwm, Alberta

Ron9e/a11d-South l&M, Alberto Wointm"ght·Kin£e11o. Alberta Uoyd1T'if'ster, A!bi!rta and Soskofchewa11

H1bemio, Cot'oda

[' ] Show All ru~ys

C o

ImPQrt

:J>

Seled~ Ass.ay

I

~an1:d

Use the following screenshot to set up the remaining data for the Oil & Gas Feed input: Materlal strea~l B~c'k 6i1' siieiiih

G]t§:il!tiJ

---r Worksheet

--r-~-----~t:til<:~~~~ts. .9¥~1:i,:ii~~-.J-

Worksheet Co11ditions Properhes Compcsltion

011' & Gas Feerl Petroreum Assay KValue

[~n & Gas Fe~-~~~_oji'A~:~-! _=-: Oil Properties

I Region Country : I ""'Y •

User Variables Notes Cost Pararneler5 I Normalized Yields

North America

Canada Cold l~< Alb<

Gas Composition 0 Mo!e% Mass%

Mole% Methane Ethane

Propane

i i-Butane

II

I i-Pentane n-Botoo•

I

Vol%

n-Pentane

( GOR Specification

94.0000

2.0000 1.0000 1.0000 1.0000 1.0000

:i

I;5•

~~~,__:J 1

Number Of Stages StgNo

Temp

[CJ 15.00

Press {kPag]

0.0000

iro,J Flow Taraet ii Total GOil

TotalWOR

ii ~~O:Cl.:_!il_n_~_P:~r.s_;tv_

-~--___::_--_

I

~]

c=·-..---p~~--r~~~--~~;-s~~~~-::· ··-~=--~

©2014 AspenTech. All Rights Reserved.

"'

23

100.0 -,.m_p_.., ___ '_ 0.0100

·1;

I

981~0

___J_I r ·+;1.+1

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

~ if

o

What is the viscosity of the stream: Oil l?

o

Two viscosity data points are known form a laboratory analysis. They are as follows: Temperature, C

o o

;I.ft

Viscosity, cP

19.0

2099.00

80.0

39.66

JJ.JJ) tit~

l

Click the View Details button on the Oil & Gas Feed form to enter the MacroCut Data View. In the Settings tab of MacroCut table, change the temperatures to 19 °C and 80 °C for viscosity Temp A and Temp B. Change the viscosity type to Dynamic instead of Kinematic.

MacroCUt Oata: Stream •;81~ck Oil Stfeam

-Sp~itJcaJion I Settings ,_.r:i ~·,_ct_ te~s~.- - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - - -

J

... Product Cut Distillation ...._ ....................__ ....... ..........................._.

! Input Data I

ID Available

(0\ Bulk Properties And Distillation

@ Not Available

{:) Only Bulk, Properties

lln:~:::i:y Setti:sK :~::t;: -·

1

I! Viscosity Temp A

I Viscosity Temp B I i Viscosity Temp c Viscosity Temp D

·

--- -----1

19 C 80 C

.

I I

North America

Country

Canada

Assay Name

Cold lake blend [Edmonton]

As~y lQ

COLOF008

!

100 C

L-------------------------------------··----------------------J

- Distillation Fitting Factor ~ ...........................................................

..-----·-1

I

@ Refutas

Region

.

-60-c -- ·······~ --··---·-····-· -· ---·· --·· -

r Viscosity Calculation Method ................................._

.. Assay Source Info ----------·------------..---·---!

\{) HYSYS

I

Fitting Factor

'~·-----------------------·

o

Refu tas A

33.47

Refutas B

23..10

l

3

I

l

I

Go back to the Specifications tab and select the Petroleum Property pulldown menu in the top-right. Select Dyn Vise@ 19.00 C and click Add.

l.

l © 20 14 AspenTech. Al l Rights Reserved.

24

Aspen Teclrno logy, Inc.

t

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Workshops

LSJfi~E1!.Qiil,

~1~utDm; St~...,-BloctOi!Sbum

!

- s?ec,•K., ..>o i _S<«lflotlon ~ogh!

Ecd•

0.13. (;as

~<''<;l
D'UC1M•<>'!

As..-1 Prore-t,·

tl"dl•'-""

fe<j

Tyf'~

~

TBP

y,.,ld Sa"

1

C~tl'ldth

D"t.•h~ooT•mn

~ul~

'I•'+< C~

1(,,t;j ISP

1!~

\C)

<e<11p\)'•

<ee1µ!J>

,..,,r!>"

11~0

120-11

J05(CI

51 ~7

iCut>l .105 fo

UO {Cl S6'i(C/ S6'i To SI~ (CI

55<}()

1 g5_0 J4l.J 405.0 4711.0

~JOTo

0>00

565.0

·~·

815.6

(Cvt2J 115 '" j(ut1) 29'i To

29'; (C) 143 (()

48

((u!J) 3•3fo

>3

~

c~udP~k.t

!::. Poo•rPo!·"'..

:Cl

(C)

P1ope!fy

(ovnv!~®oo.~ill r-M;-j -OM~j ~-'.''_:~]

~

lfoujd Volume

. .

.

iquidCen>ily

fteeze Po!nt Sm
f><etel

SutfurCooteot ("' '?.)

;K~'!!e·1f':t:-:FNtBlF?Jl I °>'"Vise o ao.o~ c"l.}. °'<"VI« @160.0~ c I l}yn Yh< @ l 00.00 C

!.O.ddlty

'·~

~.700.,.-001

:Jl.l9 231!6 «tnply>

1.010

<empty> «mptp:

z.~oo

<empty>

<emply> l.HO «rnply>

6G.OO

15.0 <empty> 0.4000

l Hydrogen

i luminorn~« Numb•r

<emplp

amply~

i /\nmn< Point

i C !oHl!.otfo

Co~!<M

ippm"•)

22.60

;•

·~

i ~::~~~- ~-· '""'-' Rdra
OM•"

I

OVol

"-J. fr•n•po
o;,1,1i.h>• Pc"'t>

IMt1!

"-ddD,
o

......

Ce!et.c::·O.!o!~Ali.j

5<>n_]

---~-~la!.!.~.·~.:.. __ bp~
ln>p<>YI

'''"~-"''""'"•

Dyn Vise @ 19.00 will show up in Assay property table. Specify the bulk value as 2099 cP. Inf~

MWo<:'vlD.1>'5trutri-tOi!Sf>o"" ~

~···~·

"''>Y"'°"""J l.,t.!fnd. C"&G"""'

"'"'"~'''"'

Po•rnb."'?'"P'"t-1

fl>•U>tao T;•e•

'l•"'

'IBP

!JQeiolYoT""•

'"'°"''"'("'"""'' (f>P""") .mp!y>

SP fo

:i\ !o ;~>;

Jo

i;,; •CJ El {CJ 3"3 tC)

i4l 'o '~l Jo 'i~ fo 5iilio

_i-(<>C>fG..

o~-;;-V;-:@ac.ooc

•

~ i ~:I

10 O.ll«lO

"'

Otloto.o..I:

"'"'"Po

''"""0"''

Pacd\m>

""'P1P ""'P1P

•

A,.!ooF,··O

~o)



«

<empty>

<<me•Y>



""'P'P

-•QA4

~-l6

11.MQ~

omptp om ply>

«mpty> «mptp

-J!!.JJ -7HJ

-79.44

'""P'"

i cI ;c I

0.0000

00000

O.~H

«mp!y>

1'5~

rn.oo

Ol!iiC)

99.00

134.Q

tSlo

""'PIP

..,

4'!'i (() ~;~ :;,;~

<""'P'f>

'°'"""' «mptp

"'

,'""""' .....,,

49.\D >l.)O <empty> «mp!y>

'''""'" "'"P1''

"""pty> «mp!y>

};flV•><:;, 1'l0C

r:;.,,,;,,ill

'''I

(<<j

w•;c

'""

'""'P'P

<mply>

"mply>

<>mply> «mply>

<emply>

«mply>

«mply>

«mply>

'"'"ply> «mply>

«mpty> «mpty>

r.tJ.

,,,,;,,.,,,,,,.,,,, A-Jd~·>!Co:o

~nJxHof'p"I

Ada:

C~-'.:.~;_;i:~....;~-~ r~

l"po"h~

\~~

-~~"-~~] Ac:e-
""""''" .,oct ·:Oonq<•

o

Repeat the above procedure to add Dyn Vise@ 80.00 C. Specify the bulk value for that one as 39.66 cP.

o

Return to the main PFD. What is the viscosity of the stream Oil I now? g(,g ,!

o

To adjust the calculated Oil! viscosity, you will tune the Dyn Vise@ 19.00 C by continually making adjustments in the Macro Cut table input. The goal to match the Oil I calculated viscosity to 2099 cP. Use the table below entering different values for the Dyn Vise@ 19.00 C and recording the subsequent calculated viscosities for stream Oil I .

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25

Aspen Technology, Inc.

Modeling Heavy Oil & Gas Production Facilities Using Aspen HYSYS Upstream

Dyn Vise@ 19.00

Workshops

Viscosity in stream Oil1 , cP

2099.0 2500.0

AA-~

2800.0

Af{j

3000.0

;\~l

3010.0

;ti~,G

3020.0

)J;fO

l

o

Save your case as 08_MacroCut Visc.hsc.

I I [

I l (

l l. l

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26

Aspen Technology, Inc.

l l l l