Alternative Stripper Configurations for CO 2 Capture by Aqueous Amines Babatunde A. Oyenekan 1 and Gary T. Rochelle Department of Chemical Engineering.

Slides:



Advertisements
Similar presentations
Some Projected Add-On Control Options for CO 2 Reductions at a Coal-Fired Generating Unit Kevin Johnson URS Corporation Raleigh-Durham, North Carolina.
Advertisements

Absorption and Stripping
EGR 334 Thermodynamics Chapter 4: Section 10-12
CO2 Capture Status & Issues
1 Energy consumption of alternative process technologies for CO 2 capture Magnus Glosli Jacobsen Trial Lecture November 18th, 2011.
Integrated Gasification Combined Cycle (IGCC) IGCC is basically the combination of the gasification unit and the combined cycle. It has high efficiency.
Project Motivation & Description Accomplished Work Future Work.
Carbon Management Research in UKy-CAER Supported by Carbon Management Research Group Kentucky EEC - DEDI ARPA-E US DOE International Collaboration US Department.
Combustion Calculations
Solubility of K 2 SO 4 in CO 2 Loaded MEA/PZ Solution Jan 10th, 2008 Qing Xu Rochelle group Department of Chemical Engineering University of Texas at Austin.
Entropy balance for Open Systems
Prof. Dr. Marco Mazzotti - Institut für Verfahrenstechnik Schemes for absorbent recovery.
CO 2 Capture by Aqueous Absorption/Stripping Presented at MIT Carbon Sequestration Forum VII By Gary T. Rochelle Department of Chemical Engineering The.
Dr Saad Al-ShahraniChE 334: Separation Processes Absorption and Stripping of Dilute Mixtures  In absorption (also called gas absorption, gas scrubbing,
Chapter 1 VAPOR AND COMBINED POWER CYCLES
State and Equilibrium Process and Cycles
Richard Reed Kansas State University
17th Annual Meeting of the Consortium for Processes in Porous Media
EXERCISE 1 CHAPTER 12.
Capturing Carbon dioxide Capturing and removing CO 2 from mobile sources is difficult. But CO 2 capture might be feasible for large stationary power plants.
Y. Riachi, D.Clodic 9 th Annual CCS Conference Pittsburgh Pennsylvania May CTSC Chaire Paris, 01/12/2010.
Production of Synthesis from Natural Gas by Steam Reforming Hysys Simulation Presented By : Presented By :  Beshayer Al-Dihani  Hessa Al-Sahlawi  Latifa.
Chris, Stephanie, Kyle, Mariam
PM3125 Content of Lectures 1 to 6: Heat transfer: Source of heat
CO 2 Flue Gas Scrubber Technology Michael Ng University of Texas Department of Chemical Engineering.
USE OF HEAT INTEGRATED DISTILLATION TECHNOLOGY IN CRUDE FRACTIONATION Su Zhu, Stephanie N. English, Miguel J. Bagajewicz The University of Oklahoma Department.
Alexander Voice 24 November  Motivation for the development of CCS technology  Climate change  Energy profile and outlook  Public perception.
Evaluation of performance of various alkanolamines for CO 2 capture from a pulverized coal-fired power plant Sumedh Warudkar PhD Candidate Chemical and.
KHABAROVSK REFINERY HYDROPROCESSING PROJECT BASIS OF DESIGN APRIL 29th – MAY 3rd 2013, MADRID, SPAIN TRAINING COURSE.
GHGT-8 Self-Optimizing and Control Structure Design for a CO 2 Capturing Plant Mehdi Panahi, Mehdi Karimi, Sigurd Skogestad, Magne Hillestad, Hallvard.
1 MHI's Commercial Post Combustion CO2 Capture Experiences in a Carbon Constrained World Ronald Mitchell Mitsubishi Heavy Industries, Ltd. International.
Overview of CO 2 Capture Processes John Davison IEA Greenhouse Gas R&D Programme Workshop on CCS, KEPRI, 19 th October 2007.
CO 2 Capture from Flue Gas using Amino Acid Salt Solutions Benedicte Mai Lerche Kaj Thomsen & Erling H. Stenby.
Amine Thermal Degradation By: Jason Davis. Overview Carbamate Polymerization of MEA Background Chemistry Model PZ and MEA/PZ Blends Amine Screening.
1 Research Review Meeting, Austin, 10-11/I-2008 Thermal measurements: Heat of absorption of CO 2 and Vapour-Liquid Equilibria in alkanolamine-water solutions.
Ansaldo Ricerche S.p.A. Carbon Dioxide capture Berlin, March 2008.
 CO 2 Capture Using Ionic liquid Prepared by Ahmad T. Malki Ahmad K. AL-Askar Supervised by Prof. Emadadeen M. Ali Prof. Mohammad Asif.
Introduction to Separation
CO 2 Capture by Aqueous Absorption/Stripping Research Review Meeting The University of Texas at Austin with contributions from The University of Regina,
Stephanie Freeman January 10 th, 2007 Rochelle Group University of Texas at Austin – Dept. of Chemical Engineering.
Kinetics of CO2 Absorption into MEA-AMP Blended Solution
AGUS HARYANTO 01 March  Examine the moving boundary work or P.dV work.  Identify the first law of thermodynamics for closed (fixed mass) systems.
David Van Wagener The University of Texas at Austin Research Review Meeting January 11, 2008.
Jorge M. Plaza The University of Texas at Austin January 10-11, 2008.
Two-Phase Gas-Liquid Systems (Saturation, Condensation, Vaporization) Saturation  When any noncondensable gas (or a gaseous mixture) comes in contact.
Power Plant Engineering
Prof. Gary T. Rochelle CPE 5.462, 2 MS, 8 PhD Projects/funding for MS or PhD Technology Area CO 2 Capture from Flue Gas ( to address Global Climate Change)
Kinetic and Thermodynamic Data for MEA and MEA/PZ By: Ross Dugas January 11, 2008.
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.
By Marcus Hilliard Gary T. Rochelle The University of Texas at Austin
Aspen RateSep Absorber Model for CO 2 Capture CASTOR Pilot Plant IFP – Lyon, France by: Ross Dugas January 11, 2008
Novel Post Combustion CO2 Capture (PCC) Process - MU Static Spiral Perforated Wings (MU-SSPW) Mixing Element - December 11, 2015 Mu Company Ltd. & K-Coal.
Determination of Amine Volatility for CO 2 Capture Thu Nguyen January 10, 2008 The University of Texas at Austin Professor Gary Rochelle.
“THERMODYNAMIC AND HEAT TRANSFER” University of Rome – Tor Vergata Faculty of Engineering – Department of Industrial Engineering Accademic Year
Overview of Oxycombustion Technology ASME PTC 4.5 Kick-off Meeting Orlando, Florida December 16, D.K. McDonald, Technical Fellow, Babcock & Wilcox.
Chemical Engineering Department Government Engineering College Bhuj Prepared By: ( to ) B.E. Sem-III(Chemical) Guided By:
HOSTED BY: SUPPORTED BY:.
John Edwards, P&I Design Ltd
Natural Gas Production Chapter 6 Misc. Gas Conditioning
by Lars Erik Øi and Vladyslav Shchuchenko
Projects/funding for 1 or 2 Funded by consortium of 24 companies
prepared by Laxmi institute tech. Mechanical eng. Department.
ES 211: Thermodynamics Tutorial 5 & 6
A Review of Separation Topics
carbon capture and storage (CCS)
Chapter 5 Energy Balances with reaction.
Mass and Energy Analysis of Control Volumes (Open Systems)
Adiabatic Process for an Ideal Gas
Absorption and Stripping
Dept. of Chem. and Biomol. Eng., Sogang Univ., Seoul, Korea
Presentation transcript:

Alternative Stripper Configurations for CO 2 Capture by Aqueous Amines Babatunde A. Oyenekan 1 and Gary T. Rochelle Department of Chemical Engineering The University of Texas at Austin 1 Current Affiliation: Chevron Energy Technology Company, Richmond, California Sixth Annual Conference on Carbon Capture and Sequestration Pittsburgh, PA May 7–10, This presentation was prepared with the support of the U.S. Department of Energy under Award No. DE-FC26- 02NT41440 and other industrial sponsors. However, any opinions,findings,conclusions and recommendations expressed herein are those of the authors and do not reflect the views of the DOE or the industrial sponsors.

Outline  Introduction  Practical Problems and Solutions - Improved Solvents - Matrix Stripper  Equilibrium Model Description and Results  Conclusions

System for CO 2 Capture and Sequestration Coal ESP FGD Abs/Str Comp Disposal Well 30 psia Steam FlyashCaSO 4 Boiler Power Net Power CaCO 3 Air

Flue Gas P CO2 = 12 kPa Treated Gas P CO2 = 1.2 kPa Absorber 40–60 o C 1 atm Reboiler Concentrated CO 2 Rich SolventLean Solvent Simple Stripper (160 kPa) 100–120 o C Vacuum Stripper (30 kPa) 60 – 80 o C P CO2 * ~ o C P CO2 * ~ 5 40 o C  H des = kJ/mol CO 2 Modified Baseline Absorber/Stripper Configuration  T = 5 o C

 Industrial state-of-the-art,Demonstrated Tech  Economic  Good mass transfer rates Practical Problems  High Energy Requirement - Reboiler duty (80% of operating cost)  Amine degradation and corrosion - Make-up costs  High Capital Cost - Large Absorption and Stripping Columns 7m (30-wt%) monoethanolamine (MEA)

Focus of research Reduce energy consumption (reboiler duty) Approach to reducing energy consumption  Alternative solvents to 7m (30-wt%) MEA - Heat of absorption - Capacity - Rates of reaction with CO 2  Innovative process flow schemes - Understand stripper operation - Energy Integration

Improved Solvents  Lower energy consumption/better mass transfer/less degradation and corrosion than MEA - promoted K 2 CO 3 (K 2 CO 3 /PZ) - promoted MEA (MEA/PZ) - promoted tertiary amines (MDEA/PZ) - mildly hindered amines (KS-1)  Greater capacity (4m K + /4m PZ, MDEA/PZ, KS-1) - less sensible heat requirement  Enhanced mass transfer (PZ/K 2 CO 3, MEA/PZ) - less capital cost, closer approach to saturation  Less degradation and corrosion (PZ/K 2 CO 3,KS-1,KS-2,KS-3) - reduced make-up costs

Matrix Stripper ldg = kPa 160 kPa 1 gmol CO 2 91 C 96 C 91 C 96 C L= 0.38 kg solv. ldg =0.504 Lean ldg Semi - lean ldg Q = 51 kJ Q = 54 kJ 79C L= 1.50 kg solv. Some CO 2 recovered at high P Use Q instead of W for compression Less comp. downstream

Evaluation in Aspen Custom Modeler (ACM) Features - Flash section, 10 sections, Equilibrium reboiler - Compression to 330 kPa VLE Model Assumptions - Well-mixed L & V phases - 40%,100%,100% Murphree Eff. for CO 2, T & H 2 O - Negligible vaporization of solvent

Performance of Strippers Concept of Equivalent Work (W eq ) Why W eq ? Compare stripper configurations on same basis. Compare Q and W.

Generic Solvent Characteristics Solvent6.4m K + / 1.6m PZ 5m K + / 2.5m PZ 4m K + / 4m PZ 7m MEA MEA/ PZ MDEA/ PZ KS-1  H abs (kJ/gmol) Rich P CO2 * 40 o C Capacity VLE Sources Cullinane (2005)Freguia (2002) Posey (1996) MHI

Predicted Performance of Different Solvents and Flow Schemes (90% removal,P reb = 160 kPa,  T  5 o C, P final = 330 kPa) 4m K + / 4m PZ 7m MEAMEA/PZMDEA/PZ Equivalent Work (kJ/gmol CO 2 ) Baseline (10 o C) Modified Baseline (5 o C) Matrix

Effect of  H abs on energy requirement (90% removal,  T  5 o C, P final = 330 kPa) 6.4m K + / 1.6m PZ 5m K + / 2.5m PZ Capacity  H abs (kJ/gmol) 5063 Equivalent Work (kJ/gmol CO 2 ) Modified Baseline Vacuum

Effect of capacity on energy requirement (90% removal, P reb = 160 kPa,  T = 5 o C, P final = 330 kPa) 5m K + / 2.5m PZ MDEA/PZ  H abs (kJ/gmol) 6362 Capacity Equivalent Work (kJ/gmol CO 2 ) Modified baseline Matrix

Solvent performance for simple strippers (90% removal,  T = 5 o C, P final = 330 kPa) 6.4m K + / 1.6m PZ MDEA/PZ7m MEA  H abs (kJ/gmol) P (kPa)Equivalent Work (kJ/gmol CO 2 )

Energy requirement for separation and compression to 10 MPa Separation MethodW sep W comp Total W eq kJ/gmol CO 2 Ideal Sep., (40 o C,100 kPa) Isothermal Comp Ideal Sep., (40 o C,100 kPa) 75% Adiabatic Comp. In 5 stages Ideal Membrane (40 o C) (75% adiabatic comp. eff. in 5 stages) m MEA, 10 o C, 160 kPa m MEA, 5 o C, 160 kPa Matrix (MDEA/PZ)

Conclusions  MEA/PZ and MDEA/PZ are solvent alternatives to 7m MEA.  The matrix configuration is an attractive stripper configuration.  At a fixed capacity, solvents with high  H abs require less energy for stripping (temperature swing effect).  Less energy is required by high capacity solvents with equivalent  H abs.  Matrix using MDEA/PZ offers 22% and 15% energy savings over the baseline and the modified baseline with stripping and compression to 10 MPa.  Typical predicted energy requirement for stripping and compression to 10 MPa (30 kJ/gmol CO 2 ) is about 20% of the output from a 500 MW power plant with 90% CO 2 removal.

Contact Information Babatunde Oyenekan, Ph.D. Chevron Energy Technology Company 100 Chevron Way Richmond, CA Tel: Prof. Gary T. Rochelle Department of Chemical Engineering The University of Texas at Austin Austin, TX Tel: