Getting Started with Aspen HYSYS Dynamics

8/10/2019 Getting Started with Aspen HYSYS Dynamics

1/42

2012 Aspen Technology, Inc. All rights reserved

Getting Started withAspen HYSYS DynamicsSolving safety and operability challenges

Dr. Glenn Dissinger,

Product Director, Aspen Technology

Hosted by:

Ron Beck,

Product Marketing, AspenTech

Optimizing Operations Webinar

Sept 5, 2012


2/42

2012 Aspen Technology, Inc. All rights reserved | 2

Ongoing Series of Technical WebinarsEngineering Webinars for education and best practices

UPCOMING WEBINARS OF INTEREST: Sept 5, 2012: Getting Started with Aspen HYSYS Dynamics

Sept 13, 2012 (Asia/Pacific time): Improved Heat Exchanger Design withaspenONE EDR Integrated with Process Modeling (Tom Ralston)

Sept 20, 2012: Improving Olefins Plant Feedstock Flexibility andWindow of Operation Using Aspen Plus (Phil Edwards, SABIC UK)

Oct 24, 2012: Modeling Conversion of Carbon to Biomass in AlgalSystems (Dr. Eric Dunlop, Pan Pacific)

Dec 12, 2012: Solid Phase Modeling in Specialty Chemicals (AjayLakshmanan)

OTHER TOPICS TO BE ANNOUNCED

A library of additional recent webinars on many engineering topics isavailable on the AspenTech public website


3/42


Common Models & Data

aspenONE Integration

SupportManufacturing& SupplyChain

ConceptualEngineering

BasicEngineering

DetailedEngineering

aspenONE engineeringBest-in-class engineering solutions in an integrated work flow

Aspen SimulationWorkbook & Aspen OnlineDeployment

Aspen PetroleumDownstream & HYSYSUpstream

Aspen EquipmentDesign & Rating

Aspen BasicEngineering Aspen Capital

Cost Estimator

(ACCE)

Aspen PlusDynamics, ACM &

Flare System &Energy Analyzer

Aspen Plus

Aspen HYSYS

Aspen Process

EconomicAnalyzer (APEA)

DetailedEngineering


4/42


Agenda

Introduction to Dynamic Simulation What Is It?

Applications

Overview of HYSYS Dynamics

Demo Transitioning a Steady-State Model to Dynamics Q&A


5/42


Process Dynamics

Consider the simple bath tub example

Steady-state: Fi= Fo

Dynamic: dV/dt = FiFo

where V=Vinit@ t=0

V=H*A

Fo = k * H

Dynamic simulation predicts how a process and its associated controlsystem will respond to various disturbances as a function of time

Usage has been increasing

Better tools

Safety and quality demands have increased

Today, steady-state design by itself is not enough!


6/42


Applications of Dynamic Modeling & Simulation

Design / Analysis of Control Schemes Design the process and control system simultaneously

Analyze and improve basic control strategies (e.g., fractionators,compressor surge, location of sensors, etc.)

Pre-tune control loops

Evaluate, develop and test APC scenarios (DMCplus)

Operability Engineering Studies Understand dynamic plant behavior, including upset propagation (e.g.,

slugging)

Operability studies of highly-integrated processes

Design / analysis of start-up, shutdown and process transition strategies

Hazard and Safety Studies

Design / analysis of pressure relief and flare systems Safety studies

Design / analysis of emergency shutdown systems

Operator Training

DCS checkout

Graphics functionality/operability of the operator consoles


7/42 2012 Aspen Technology, Inc. All rights reserved | 7

Agenda


Applications and Success Stories


Demo Transitioning a Steady-State Model to Dynamics

Q&A



What Does HYSYS Dynamics Offer?

Seamless transition from SteadyState to Dynamic

Interactive environment

Rich choice between simple anddetailed modeling

A comprehensive library ofcontrol and logical operations

Dynamics Assistant



Steady State

Dynamic mode

Completely Integrated with HYSYS

Same program

Same GUI

Same thermodynamic models

All input data are shared

Steady state results can be used as initialization fordynamic simulation



Rich choice between simple and detailedmodeling options - Vessels

Simple Design Dynamics

A vessel with only thevolume specified

Detailed Plant Dynamics

A vessel with Vessel elevation defined

Nozzle positions defined

Heat losses defined

Entrainment modeling

Level taps

or



Rich choice between simple and detailedmodeling options - Valves

Simple Design Dynamics

A linear valve with instant action

Detailed Plant Dynamics

An equal percentage valve with

an actuator with linear rate

an actuator with a defined failmode

a holdup

an offset to simulate leaking

or



Controllers BooleanOperations

Logical Operations

Comprehensive Library of Controller andLogical Operations

Used to replicate control logic and strategiesused in the actual plant DCS system



Dynamics Assistant

Can be VERYuseful as a guideto see what changes itrecommends

However, use the MakeChanges button withcaution as its advice mayNOTbe what you want to do


14/42


Agenda


Applications and Success Stories


Demo Transitioning a Steady-State Model to Dynamics

Q&A


15/42


Additional Data Required for a Dynamic Model

Dynamic

Model

Steady-State Model

Initial Model Input:

Thermodynamics

Components

Unit Operations

Flowsheet Construction

Dynamic Model

Additional Input:Pressure-Flow Specs

Equipment Sizing

Controllers

Strip Charts


16/42


Transitioning from Steady State to Dynamics

4 Steps are Needed

1. Pressure Flow Setup and Specifications

2. Equipment Sizing

3. Set up your Control Strategy

4. Set up your Strip Charts and Run the Model


17/42

2009 AspenTech. All Rights Reserved.


Step 1: Pressure Flow Setup and Specifications


18/42


Solver Basics

Aspen HYSYS Dynamics Solver is different from the SteadyState Solver

Steady State Pressures and Flows are not related, but canbe set independently

Flow = 495 m3/sPres = 130 kPa


Flow = 440 m3/s

Pres = 120 kPa

Flow = 440 m3/s

Pres = 375 kPa

Flow = 440 m3/s

Pres = 365 kPa


No pressure drop across heat exchanger!


19/42


Pressure Flow Solver in HYSYS Dynamics

Pressures and Flows are related, and can NOT be setindependently



Flow = 440 m3/sPres = 120 kPa Flow = 440 m3/s

Pres = 375 kPa



There must be a pressure drop to get a flowrate!!


20/42


Pressure-Flow Relationship Concepts

All unit operation models are categorized in one of thefollowing categories

Pressure Node Operations contain significant volume andcalculate a pressurebased on the holdup of vapor in the unitoperation

Resistance Equation Operationscalculate a pressure dropbased on a resistance equation

P/F specifications MUST be set on all boundary streams


21/42


Guidelines for Transitioning to Dynamics

1. Add a resistance unit operation (e.g., valve, pump,compressor) between all pressure nodes in the flowsheet

Internal flow rates will be calculated by the pressure gradientsthroughout the flowsheet

2. One P/F specification should be made on each boundarystream (feeds and products)

Make pressure specifications on boundary streams attached toprocess equipment that use a resistance equation to calculateflow rates (e.g., valves, pumps, compressor, heat exchangers

Recommendation Add valves to all boundary streams (You will use them for flow controllers anyway once you add the control

strategy to the dynamic model!)


22/42


Ensuring Pressure Gradient in ModelGuideline #1 Add valves between pressure nodes

Valve added betweentwo vessels


23/42


Ensuring Pressure Gradient in ModelGuideline #2 Add valves on boundary streams


24/42


25/42


Best Practice - PFD Display of Dynamic P/F Specifications

Available from drop-down menu on PFD

Color Code Green Pressure specified Yellow Flow specified Red Pressure and Flow specified Blue None specified


26/42



Step 2: Equipment Sizing


27/42


Size Matters in Dynamics!!

Consider the level control of a tank..

Noisy feed flow

What impacts thestability of theoutlet flow?


28/42


Size Matters in Dynamics!!

Large tanks can mitigate disturbances

E i t i i d t b t d th


29/42


Equipment sizing data can be entered on theRating or Dynamics tab


30/42



Step 3: Setting Up Your Control Strategy


31/42


Basics of Control Theory

A control system is designed to maintain stable processoperations by compensating for disturbances

Key terms used by control engineers

Process Variable (PV): Process variable that you want tomaintain at a given operating point or set point

Manipulated Variable (MV): Process variable that is changed bythe controller

Disturbance Variable (DV):A process variable which upsets aprocess and causes the control variables to move from the

desired set-points

Controls do what the process engineers can not


32/42


Controller Library

PID Controller


33/42


34/42


Key Input for the PID Controller Model

Controller Action

Controller TuningParameters


35/42


Controller Tuning - Recommendations

The values below are recommended starting points fortuning control loops

System Kc i(minutes) d(minutes)

Flow 0.1 0.2 0

Level 2 10 0

Pressure 2 2 0

Temperature 1 20 0


36/42



Step 4: Running Your Model

Three Things To Consider Before Running


37/42


Three Things To Consider Before RunningYour Model

1.Set up strip charts

2. Integration step sizes and speed

3. Event Scheduler


38/42



4 Steps are Needed

1. Pressure Flow Setup and Specifications

2. Equipment Sizing

3. Set up your Control Strategy

4. Set up your Strip Charts and Run the Model


39/42


For more Aspen HYSYS Dynamics information

Aspen HYSYS Dynamics web page

http://www.aspentech.com/products/aspen-hysys-dynamics.aspx

White papers, case studies, tutorials, resources

Library of webinars-on-demand

www.aspentech.com > events > webinar-on-demand Coming soon (will be sent to all webinar participants):

HYSYS Dynamics written getting-started-guide

HYSYS Dynamics computer-based-training (CBT) module

AspenTech Support site

Rich knowledge base of information, tips, technical support Training videos, viewlets and CBTs

Technical bulletins

Aspen HYSYS LinkedIn group

2900 members; many discussions

OPTIMIZE 2013
http://www.aspentech.com/products/aspen-hysys-dynamics.aspxhttp://www.aspentech.com/http://www.aspentech.com/http://www.aspentech.com/products/aspen-hysys-dynamics.aspxhttp://www.aspentech.com/products/aspen-hysys-dynamics.aspxhttp://www.aspentech.com/products/aspen-hysys-dynamics.aspxhttp://www.aspentech.com/products/aspen-hysys-dynamics.aspxhttp://www.aspentech.com/products/aspen-hysys-dynamics.aspx


40/42


OPTIMIZE 2013Global Conference

Join us in Boston for theindustrys must-attend event!

OPTIMIZE 2013

6 8 May 2013The Westin Waterfront HotelBoston, MA USA

For more information, visitwww.aspentech.com/agc
http://www.aspentech.com/agchttp://www.aspentech.com/agc


41/42


Questions?


42/42

Documents

Getting Started with Aspen HYSYS Dynamics