HYDROGEN R&D AT INEEL

Transcription

1 HYDROGEN R&D AT INEEL Overview Joseph C. Perkowski, Ph.D April 27,

2 Long-Term Vision: The Hydrogen Model Community A Hydrogen City or Hydrogen Corridor INEEL, SE Idaho or other venue Emphasis on engineering validation Variations Treasure Valley Clean Air Non-Attainment Support Hydrogen Yellow Bus for Greater Yellowstone Ecosystem GHG-free Southern Idaho Corridor Primary Energy Sources Hydrogen Production Transport Storage Distribution Use Photo Conversion Electrolysis or Compression 2

3 INEEL Hydrogen Initiative Objectives Achieve a leading position in RD&D of key hydrogen technologies. Focus areas: 1. Hydrogen production - nuclear energy, 2. Hydrogen production - fossil and/or renewable energy, 3. Hydrogen infrastructure - bulk hydrogen handling, vehicle fueling infrastructure, vehicle testing, fuel cell fabrication/testing. Gain increased stature as a multipurpose laboratory. Contribute to the nation s energy security and an improved environment. 3

4 Nuclear Hydrogen Production Development Plan Research and Development Thermochemical (TC) High Temperature Electrolysis (HTE) Heat Exchangers and BOP Membrane and Other Engineering Demonstration 50 MW TC 5 MW HTE Pilot Scale 5 MW TC 0.5 MW HTE Lab Scale Integrated Lab Scale Demonstration

5 Hydrogen Production Using Nuclear Energy, INEEL Role Thermochemical Cycle High Temperature Electrolysis Program integration and management (w/ Sandia) Integrated laboratory scale tests Pilot scale tests Engineering demonstration Enabling technology research kinetics/catalysis, materials, separations, electrolysis 5

6 Hydrogen Production Using Fossil or Renewable Energy, INEEL Role Technology Development and Demonstration Reformer processes Modeling Gasification technology demonstration Gas cleanup 6

7 Hydrogen Infrastructure/Utilization, INEEL Role Fueling infrastructure, vehicle testing Distributed hydrogen generation Electrolysis, liquid fuel reforming/cleanup Bulk hydrogen separation, delivery, storage Fuel cell fabrication/demonstrations 7

8 Absorption of CO 2 by Aqueous Diethanolamine Solutions in a Vortex Tube Gas-Liquid Contactor and Separator Participants: INEEL: Daniel S. Wendt, ( , wendds@inel.gov) Michael G. Mc Kellar ( , mgq@inel.gov) Anna K. Podgorney Douglas E. Stacey Terry D. Turner ConocoPhillips Canada: Kevin T. Raterman May 6, 2003 Supported by U.S. DOE (DE-AC07 AC07-99ID13727) 8

9 Project Objectives: Low capital cost due to compact, simple design High CO 2 capture efficiency high efficiency mass transfer reduced solvent regeneration requirements Operationally flexible turn-down & scale-up with parallel design easily accommodates variable flow rates and gas compositions low maintenance/portable configuration Works equally well for physical / chemical absorbents 9

10 Jet type absorbers highly efficient High Shear Jet Absorber highly turbulent... large interfacial area for mass transfer Reactor Type k l a ( s-1 x 100) Packed tower 7 Sieve plate 40 Venturi reactor 25 Bubble column 24 Impinging jet 122 (Herskowits et. al.) multiple jets impingement zone creates secondary drop breakup / greater area for mass transfer 10

11 High Efficiency Absorption. acid gas separation Co-inject chemical or physical absorbent CO 2 + 2R 2 NH R 2 NCOO - + R 2 NH + 2 R 2 NCOO - + H 2 O R 2 NH + HCO - 3 R designates C 2 H 4 -OH Mass transfer rate ~ f(interfacial area, film thickness) Vortex tube high differential gas-liquid acceleration - small drops high turbulence - small film thickness GOAL achieve near equilibrium acid gas loading 11

12 Vortex Tube with Liquid Separator Gas Inlet 12.6 atm 9 C Joule-Thomson expansion near sonic to supersonic velocity Hot Gas Outlet 8.6 atm 7 C J-T Temperature = 5 C Cool Gas Outlet 8 atm 2 C Lorey, et. al., 1998 Liquid Outlet 12

13 Scaled Contactor Process -wellhead (~Mscfd) to full gas plant (~MMscfd) -distributed engine (~Mscfd) to centralized power plant (~MMscfd) CO 2 Clean Gas Absorbent Stripper Feed CO 2 Mix Parallel Vortex Contactors Flash CO 2 Simple Process Schematic (Heat Regeneration if needed) 13

14 Vortex Contactor Separator Tube Nozzle Liquid inlet Gas Exit Boroscope / Throttle Liquid Exit Vortex Contactor Gas Inlet 14

15 Contactor Prototype psia inlet 15

16 Gas - Liquid Loading Tests Achieve >95% gas-liquid separation for stoichiometric loading of a 15% volume CO 2 mixture Design parameters vortex inlet tube design tapered & slotted stepped with holes tube length 16

17 Stepped tube design exceeds gas/liquid separation target Gas/Liquid Separation Efficiency (%) Separation Efficiency Liquid/Gas Ratio Inlet Liquid Flow Rate (cm 3 /minute) Liquid/Gas Ratio (mass basis) Inlet 100 psia 17

18 Stepped tube design exceeds gas/liquid separation target Liquid Outlet Flow (cm 3 /min) liquid side gas side L/G Liquid/Gas Ratio (mass basis) Inlet Liquid Flow Rate (cm 3 /minute) Inlet 100 psia 18

19 CO 2 /DEA Baseline Test Apparatus P Air Inlet Press. CO2 Flow Controller N2 Flow Controller Tescom T Air Inlet Temp. Check Valve Reg Reg CO2 supply N2 supply Vortex Tube Hot Air Outlet Temp. T P Hot Exit Press. T Liquid Outlet Temp P Liquid Inlet Press. Gas Chromatograph Liquid Collection Vessel Atmosphere Liquid Coalescer Atmosphere P Exit Press. Vacuum Pump Tescom Flow meter Exit Low Flow Exit High Flow Hood Liquid Pump Liquid 19

20 CO 2 /DEA Baseline Testing Operation Operating Parameters cm 3 /min liquid flow rate wt% liquid DEA composition psig inlet gas pressure 5-15 mol% inlet gas CO 2 composition slpm inlet gas flow rate (dependent variable) Solvent loading and CO 2 capture efficiency unsatisfactory in baseline testing Diagnostic testing indicated increased residence time required process modifications necessary 20

21 Process Modifications Modifications to process hardware increase gas-liquid contact time capacity to adjust the gas-liquid contactor geometric configuration maintain ability to control the inlet gas pressure and CO 2 : DEA feed stream mole ratio Modifications to process operating parameters cm 3 /min liquid flow rate 30 wt% liquid DEA composition 70 slpm inlet gas flow rate 10 mol% inlet gas CO 2 composition psig inlet gas pressure (dependent variable) 21

22 Baseline and Modified Process Configurations P Air Inlet Press. P Air Inlet Press. CO2 Flow Controller N2 Flow Controller Tescom T Air Inlet Temp. Check Valve CO2 Flow Controller N2 Flow Controller Tescom Back Press. Regulator Contactor T Air Inlet Temp. Check Valve Reg Reg Reg Reg CO2 supply N2 supply Vortex Tube Hot Air Outlet Temp. T P Hot Exit Press. CO2 supply N2 supply Modified Contactor/ Separator Hot Air Outlet Temp. T P Hot Exit Press. T Liquid Outlet Temp P Liquid Inlet Press. T Liquid Outlet Temp P Liquid Inlet Press. Gas Chromatograph Liquid Collection Vessel Atmosphere Liquid Coalescer Gas Chromatograph Liquid Collection Vessel Atmosphere Liquid Coalescer Atmosphere P Exit Press. Atmosphere P Exit Press. Vacuum Pump Exit Low Flow Exit High Flow Tescom Flow meter Hood Vacuum Pump Exit Low Flow Exit High Flow Tescom Back Press. Regulator Flow meter Hood Liquid Pump Liquid Pump Liquid Liquid Supply 22

23 Inlet gas pressure as a function of liquid flow rate Fouling is caused by deposits accumulating in the vortex tube nozzles Inlet Gas Pressure (psia) Inlet Gas Pressure (psia) Inlet Liquid Flow Rate (cm 3 /minute) Inlet Liquid Flow Rate (cm 3 /minute) No Nozzle Fouling Nozzle Fouling Present 23

24 CO 2 capture efficiency as function of liquid flow rate 100% 90% CO 2 Capture Efficiency (%) 80% 70% 60% 50% 40% 30% 20% 10% Mo dified Config uration 1 Mo dified Config uration 2 Mo dified Config uration 3 Mo dified Config uration 4 Mo dified Config uration 5 Mo dified Config uration 6 Mo dified Config uration 7 Mo dified Config uration 8 Mo dified Config uration 9 Mo dified Config uration 10 Mo dified Config uration 11 Mo dified Config uration 12 30wt% DEA, 10% CO2, 90 psig 15wt% DEA, 10% CO2, 90 psig 30wt% DEA, 10% CO2, MAX psig 50wt% DEA, 10% CO2, 100 psig 0% Inlet Liquid Flow Rate (cm 3 /minute) 24

25 CO 2 capture efficiency as function of liquid flow rate (no fouling) 100% 90% 80% CO 2 Capture Efficiency (%) 70% 60% 50% 40% 30% 20% Modified Configuration 1 Modified Configuration 2 Modified Configuration 9 Modified Configuration 10 Modified Configuration 11 Modified Configuration 12 10% 0% Inlet Liquid Flow Rate (cm 3 /minute) 25

26 CO 2 capture efficiency as function of liquid flow rate (fouling present) 100% 90% 80% CO 2 Capture Efficiency (%) 70% 60% 50% 40% 30% 20% Modified Co nfig uration 3 Modified Co nfig uration 4 Modified Co nfig uration 5 Modified Co nfig uration 6 Modified Co nfig uration 7 Modified Co nfig uration 8 10% 0% Inlet Liquid Flow Rate (cm 3 /minute) 26

27 Solvent loading as function of liquid flow rate 0.50 Solvent Loading [mole CO 2 /mole DEA] Modified Configuration 1 Modified Configuration 2 Modified Configuration 3 Modified Configuration 4 Modified Configuration 5 Modified Configuration 6 Modified Configuration 7 Modified Configuration 8 Modified Configuration 9 Modified Configuration 10 Modified Configuration 11 Modified Configuration 12 30wt% DEA, 10% CO2, 90 psig 15wt % DEA, 10% CO2, 90 psig 30wt% DEA, 10% CO2, MAX psig 50wt% DEA, 10% CO2, 100 psig Inlet Liquid Flow Rate (cm 3 /minute) 27

28 Solvent loading as function of liquid flow rate (no fouling) Solvent Loading [mole CO 2 /mole DEA] Modified Co nfiguration 1 Modified Co nfiguration 2 Modified Co nfiguration 9 Modified Co nfiguration 10 Modified Co nfiguration 11 Modified Co nfiguration Inlet Liquid Flow Rate (cm 3 /minute) 28

29 Solvent loading as function of liquid flow rate (fouling present) Solvent Loading [mole CO 2 /mole DEA] Mo dified Config uratio n 3 Mo dified Config uratio n 4 Mo dified Config uratio n 5 Mo dified Config uratio n 6 Mo dified Config uratio n 7 Mo dified Config uratio n Inlet Liquid Flow Rate (cm 3 /minute) 29

30 Conclusions Gas/Liquid separation efficiencies in excess of 95% Non-optimized vortex tube testing has resulted in carbon dioxide capture efficiencies of up to 86% Solvent loading as high as 0.49 moles CO 2 /mole DEA 30

31 Future Research/Applications Process hardware optimization Scaled contactor and separator Additional solvents Additional CO 2 applications H 2 S 31

32 References Herskowits,D.; Herskowits,V.; Stephan, K.; Tamir. A.: Characterization of a two-phase impinging jet absorber. II. Absorption with chemical reaction of CO2 in NaOH solutions. Chem. Eng. Science 45 (1990) Lorey, M., Steinle, J., Thomas, K Industrial Application of Vortex Tube Separation Technology Utilizing the Ranque-Hilsch Effect, presented at the 1998 SPE European Petroleum Conference, The Hague, Netherlands, October Chakma, A., Chornet, E., Overend, R. P., and Dawson, W. H., Absorption of CO 2 by Aqueous Diethanolamine (DEA) Solutions in a High Shear Jet Absorber, The Canadian Journal of Chemical Engineering, Volume 68, August Lee, J. I., Otto, F. D., and Mather, A. E., Solubility of Carbon Dioxide in Aqueous Diethanolamine Solutions at High Pressures, Journal of Chemical and Engineering Data, Vol. 17, No. 4,