Modeling of a CO2-stripper

Slides:

Advertisements

Similar presentations

Implementation of MPC in a deethanizer at the Kårstø Gas plant

Advertisements

Distillation: So simple and yet so complex... and vice versa Sigurd Skogestad Norwegian University of Science and Technology (NTNU) Trondheim, Norway.

1 Name, title of the presentation Master project: Control structure design for a sequence of distillation columns Tor Anders Marvik Supervisor: Sigurd.

Aspen Tutorial Terry A. Ring ChEN 4253.

Dynamic modeling, optimization and control of a CO 2 stripper Marie Solvik Supervisors : Sigurd Skogestad and Marius Støre Govatsmark.

CHEN 4460 – Process Synthesis, Simulation and Optimization Dr. Mario Richard Eden Department of Chemical Engineering Auburn University Lab Lecture No.

Composition of Methanol- Water Batch Distillation Prepared by: Jason Hixson Don Scott Michael Hickey September 20, 2005.

Dividing wall column application

Batch Distillation Model By: Jason Hixson Jennifer Potter Wayne Johnson.

CHEN 4460 – Process Synthesis, Simulation and Optimization Dr. Mario Richard Eden Department of Chemical Engineering Auburn University Lab Lecture No.

INTRODUCTION Air at lower temperatures (-196 o C) becomes in liquid and so can do the distillation of air to its components. Distillation of air is currently.

Multi-Comp. Distillation Design Short-Cut Method Example Problem

Energy Use in Distillation Operation: Nonlinear Economic Effects IETC 2010 Spring Meeting.

Introduction In the pharmaceutical and fine chemical industries the batch heteroazeotropic distillation (BHD) is frequently applied for the recovery of.

1 EFCE Working Party on Fluid Separations, Bergen, May 2012 New results for divided-wall columns Deeptanshu Dwivedi (PhD Candidate, NTNU) Ivar Halvorsen.

PSE and PROCESS CONTROL

Practical plantwide process control Part 1

1 Self-Optimizing Control HDA case study S. Skogestad, May 2006 Thanks to Antonio Araújo.

1 A Plantwide Control Procedure Applied to the HDA Process Antonio Araújo and Sigurd Skogestad Department of Chemical Engineering Norwegian University.

Integration of Design and Control: A Robust Control Approach by Nongluk Chawankul Peter L. Douglas Hector M. Budman University of Waterloo Waterloo, Ontario,

1 Active constraint regions for economically optimal operation of distillation columns Sigurd Skogestad and Magnus G. Jacobsen Department of Chemical Engineering.

1/31 E. S. Hori, Self-optimizing control… Self-optimizing control configurations for two-product distillation columns Eduardo Shigueo Hori, Sigurd Skogestad.

3) OBJECTIVE FUNCTION & DISTURBANCES Objective function: Assuming product prices are the same, p D = p S = p B and (p-p F ) = p’, with F given and Q =

1 Operation of Energy-Efficient Divided Wall (Petlyuk) Column Speaker : Ambari Khanam Course : Specialization Project-tkp4550 Department of Chemical Engineering.

1 Modelling of Biodiesel Production Marianne Øien Supervisors: Sigurd Skogestad and Chriss Grimholt.

ON / OFF OPERATION OF CO 2 CAPTURE By : Sepideh Ziaii Fashami Supervisors: Dr. Gary T. Rochelle Dr. Thomas F. Edgar Research Review Meeting January 11.

LOGO Plantwide Control Structure Design of Tert-Amyl Methyl Ether (TAME) Process Thitima Tapaneeyapong and Montree Wongsri Department of Chemical Engineering.

Control of Distillation Column （精馏塔控制）

Control of Distillation Column （精馏塔控制） Dai Lian-Kui Shen Guo-jiang Institute of Industrial Control, Zhejiang University.

Multi-Variable Control

Coordinator MPC with focus on maximizing throughput

Aspen Tutorial Terry A. Ring ChEN 4253.

Implementation of a MPC on a deethanizer

Unit Operations Laboratory Distillation Analysis Seminar Super Team 2005 Monday, December 5, :30 PM.

Authors: Machado, R.; Marangoni, C.; Miotto, F.; Querino, M.

Name: Marius Støre Govatsmark

Natural Gas Processing I Chapter 9 Fractionation

Simulation Of Gas Sweetening Process

Chapter 17. Inferential Control Copyright © Thomas Marlin 2013

Stian Aaltvedt Supervisors: Sigurd Skogestad Johannes Jäschke

Polypropylene PGC Applications

Implementation of a MPC on a deethanizer

Aspen Separation Unit Operations

Process Equipment Design and Heuristics – Process Vessels

Separation Columns (Distillation, Absorption and Extraction)

Qin Group Research Highlights: Process Monitoring and Control

Process Equipment Design Distillation Columns

Refinery: Separation units

Example regulatory control: Distillation

SPECIALIZATION PROJECT TKP 4550

Modeling of a CO2-stripper

Stathis Skouras and Sigurd Skogestad

Outline Skogestad procedure for control structure design I Top Down

Implementation of a MPC on a deethanizer

Implementation of MPC in a deethanizer at the Kårstø Gas plant

Implementation of MPC in a deethanizer at the Kårstø Gas plant

Distillation Column – External Balance

Methodology for Complete McCabe-Thiele Solution

Modelling of the production of biodiesel by reactive distillation

Example regulatory control: Distillation

Ambari Khanam Supervisor: Sigurd Skogestad

Plant-wide Control- Part2

Implementation of a MPC on a deethanizer

Example regulatory control: Distillation

MCD – Short-Cut Methods

Example regulatory control: Distillation

Example “stabilizing” control: Distillation

Separation Columns (Distillation, Absorption and Extraction)

ADVANCED THERMODYNAMICS 8th semester

PID control of unstable chemical reactor

Presentation transcript:

Modeling of a CO2-stripper Marie Solvik Supervisors : Sigurd Skogestad and Marius Støre Govatsmark

CO2-stripper Objectives Produce pure ethane product PC PC LC Objectives Produce pure ethane product Keep the CO2 content in the sales gas within the limit. LT, XLT FC F, z, hf 75 stages including reboiler and reflux tank Bottom product – purified ethane Distillate – Offgas (CO2, ethane and some methane) QR LC There exist a dynamic model of the system in D-spice B, xB

2-component flash tank made in Matlab SRK equation of state with binary interaction parameter found by Kornberg (2007) 2 components- ethane and CO2 Compared to simulation done in ProSim z1 P[barg] T[K] x1 y1 K 0.99 34.0 288.7 0.9927 0.9873 0.9946 0.90 283.8 0.9248 0.8752 0.9463 0.80 279.0 0.8428 0.7572 0.8984 0.60 271.5 0.6503 0.5497 0.8453 0.40 267.8 0.4202 0.3798 0.9039 0.20 268.0 0.1810 0.2190 1.2099 z1 P[barg] T[K] x1 y1 K 0.99 34.0 288.7 0.9924 0.9868 0.9943 0.90 283.7 0.9231 0.8727 0.9453 0.80 278.9 0.8419 0.7561 0.8980 0.60 271.6 0.6528 0.5520 0.8455 0.40 267.8 0.4225 0.3812 0.9023 0.20 268.0 0.1780 0.2166 1.2168

3-component flash tank made in Matlab Added an extra component, methane to the model Compared with actual process data from the top of the column and a flash tank model made in D-spice Real time composition of ethane(red) and CO2 (green) from Aspen process explorer.

D-spice versus Matlab yC2 yCO2 P[barg] T[◦C] Operating point 1 (3h) yC2 yCO2 P[barg] T[◦C] Operating point 1 (3h) Aspen 0.455 0.525 34.7 -3.3 Matlab 0.528 0.458 Malab 0.443 0.527 -6.0 D-spice -3.7 Operating point 2 (15h) 0.515 0.456 34.5 -2.0 0.556 0.420 34.6 -2.7 -3.1

Column model made in Matlab SRK function of state Builds on the flash tank model 75 stages Time-consuming

Conclusion The column model needs to be improved before finding optimal operating points Flash tank model made in D-spice showed accurate results when comparing with actual plant data and with Matlab model.