Preparation and hydrogen permeation studies of ultrathin ... · 10-13/07/2017 / Page 3 (Disclosure...
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Preparation and hydrogen permeation studies of ultrathin palladium and
carbon membranes
D. ALFREDO PACHECO TANAKA1, MARGOT A. LLOSA TANCO1,
JOSE MEDRANO2, JON MELENDEZ1, EKAIN FERNANDEZ1, MARIA
NORDIO2, MARTIN VAN SINT ANNALAND2 FAUSTO GALLUCCI2.
July 10-13 2017. Houston, Texas
13th International Conference onCatalysis in Membrane Reactors
1 2
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ObjectiveDeveloping of an advanced high performance, cost effective separation
technology for direct separation of hydrogen from natural gas networks
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Thin and ultra thin supported Pd/Ag membranes
D. ALFREDO PACHECO TANAKA1, JON MELENDEZ1,
EKAIN FERNANDEZ1, MARIA NORDIO2,
FAUSTO GALLUCCI2
(3-5 µm thick)
Poster ULTRA-THIN PALLADIUM-SILVER MEMBRANES FOR PURE HYDROGEN PRODUCTION AND SEPARATION: MODELLING
AND EFFECT OF SWEEP GAS
Thin Ultra thin
(≈1 µm thick)
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13th ICCMR, July 10-13, 2017 Texas,
MesoporousCeramics (nm)
Zeolites Carbon
MicroporousCeramics (Å)
PalladiumPalladium alloys
0.1
1
1000
100
10
10 100 1000 10000 ∞
Re
lati
ve H
ydro
gen
pe
rme
atio
n
H2/N2 selectivity
Membranes for hydrogen separation
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
H H
H H HH
H H
Adsorption
Splitting
DiffusionPd membrane
H2 permeation in Pd membranes
Recombination
Desorption
resistance of support
Ultra-thin membranes
-Surface interference- H2 splitting
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Ceramic supported Pd-based
(3-4 µm thick) membrane
T=400 ºC
Membraneactivation
Helmi et al., Molecules 21 (2016) 376
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
• H2 permeance 400 ºC: 0.9 x 10-6 mol m-2 s-1 Pa-1
• H2/N2 ideal selectivity 400 ºC: >150,000 for >1200 h
Long term permeation test at 400 °C
Metallic supported Pd-Ag membranes
(5 µm thick)
Medrano et al., Int. J. Hydrogen Energy 41 (2016) 8706-8718
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
• At >500 ºC and after >800 h, H2/N2 ideal selectivitydropped to from 223000 to 2650
Long term permeation test at more than 500 °C
Metallic supported Pd-Ag membranes
Medrano et al., Int. J. Hydrogen Energy 41 (2016) 8706-8718
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Ultra-thin Pd-Ag membranes ≈ 1μm
Melendez et al., Journal of Membr. Sci. 528 (2017) 12–23
Thickness vs plating time
H2/N2 selectivity and H2 permeancevs thickness
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Activation energy of Ultra-thin Pd-Ag membranes
Melendez et al., Journal of Membr. Sci. 528 (2017) 12–23
7.81 KJ mol-1
Ea vs thickness
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Membrane thickness 1.30 um
Melendez et al., Journal of Membr. Sci. 528 (2017) 12–23
H2 flux at various gas mixtures and pressures at 400°C
Effect of dilution H2 and N2
Effect of COAt H2 /N2 60/40
Replacing some N2with CO
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Melendez et al., Journal of Membr. Sci. 528 (2017) 12–23
Thickness 1.30 um3 bar total pressure, vacuum at the permeate
H2 flux at various gas mixtures and pressures at 400°C
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Long term test Pd-Ag membranes ≈ 1,3 μm
Melendez et al., Journal of Membr. Sci. 528 (2017) 12–23
H2
N2
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
DOE 2015
1 µm Pd / ceramic
3-4 µm Pd / ceramic
5 µm Pd / metallic
DOE 2015
Gallucci et al., Chem. Eng. Sci 92 (2013) 40–66
DOE 2015 target :Purity > 99.99%>100 𝑵𝒎𝟑/𝒎𝟐. 𝒉 (6.9 bar ΔP)
Pd alloy membrane properties at TECNALIA
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13th ICCMR, July 10-13, 2017 Texas, Pd membranes
Carbon Molecular Sieves Membranes (CMSM)
D. ALFREDO PACHECO TANAKA1, MARGOT A. LLOSA
TANCO, JOSE MEDRANOJON MELENDEZ1,
FAUSTO GALLUCCI2
Poster
BIOGAS UPGRADING WITH CARBON MEMBRANES: EXPERIMENTAL DEMONSTRATION AND BENEFITS
EVALUATION
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Mechanism
Pore size
0.5 – 0.7 nm
16
Porous membranes for gas separation
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Molecular sieves membranes
Zeolite membranes▪ Difficult to obtain crack-free
▪ Intercrystallite voids affecting selectivity
Carbon Molecular sieves membranesCarbonization of a polymer precursor under inert atmosphere or vacuum
Presence of micropores and ultramicropores
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
0.2
9 0.3
3 0.3
8
Kinetic diameter of various gases
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
T/ °C t/h
Dry
calcination
450-1000 °C t/h 1°C/min inert
vacuum
Dip coating
Preparation of composite-Alumina-CMSM
19
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
SEM and TEM of the Al-CMSM
Composite phenolic resin CMSM, exeira, Campo, Tanaka, Llosa, Magen, Mendes, Carbon 49 (2011) 4348
20
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Effect of carbonization temperature
Fresh membrane
Llosa , Pacheco et.al Int J.hydrogen energy 40 (2015) 5653 40 (2015) 3485
After one day
O2 and N2 very low flux
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
CMSM-500 after 14 days
N2 permeation of c-CMSM-500 in functionof the temperature at 400 kpa
0
5
10
15
20
25
50 100 150 200 250 300 350 400
N2
Pe
rmea
tio
n
[ m
lmin
-1]
Temperature [ °C ]
N2 permeation of fresh membrane 66.8 ml min-1
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
N2 permeation at 400 kPa for CMSM-500 in function of the time of water adsorption
0
5
10
15
20
25
30
0 50 100 150 200 250 300 350 400
N2
Per
mea
tio
n
[ m
lmin
-1]
Time [ min ]
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Just aftercarbonization
Active placesreact with water(water chemisorption)
Water physisorption
-OH
-OH
-OH
=O
-OH
-OH
-OH
=O
N2 66 ml/min
N2 20 ml/min
water
Modification on the porous
24
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
0.000
0.005
0.010
0.015
0.020
0.025
0.030
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
F [
cm3
g-1n
m]
Pore width [nm ]
750 °C 550 °C
Pore size distribution at various carbonization temperatures
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Gas permeance as a function of temperatureAl-CMSM carbonized at 500 °C
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13th ICCMR, July 10-13, 2017 Texas,
Ea
Activation Energy (Ea) at various activation heat treatments
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Activation energy of c-CMSM-500 membraneat various temperatures of pemeation, for various gases
The values correspond to the average of permeation dataperformed at different temperatures from 40°C to 100°C
28
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Single H2 and CH4 gas flow as a functionof temperature and pressure
H2 CH4
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
H2 and CH4 gas ideal perm-selectivity as a functionof temperature
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Testing
temp
(°C)
H2 in
feed mixture
(%)
H2 purity in the permeate
(%)
Measured Calculated
40
5 93.3 95.7
10 96.6 98.0
20 96.7 99.0
80
5 65.2 65.7
10 76.4 80.2
20 84.8 90.1
H2 purity (%) at various H2 contents in the mixturePressure: out 7.5, in 0.01 bara, inlet 2 L min-1
H2, CH4 mix gas permeation
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
Testing
temp
(°C)
H2 in
feed mixture
(%)
H2 purity in the permeate
(%)
Measured Calculated
40
5 93.3 95.7
10 96.6 98.0
20 96.7 99.0
80
5 65.2 65.7
10 76.4 80.2
20 84.8 90.1
Total flow H2- CH4 mixed gas Pressure: out 7.5, in 0.01 bara, inlet 2 L min-1
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13th ICCMR, July 10-13, 2017 Texas, Carbon membranes
H2-CH4 mixed gas tests (10% of H2)(Pressureout: 7.5 bara; Pressurein: 0.01 bara, inlet 2 L min-1)
Testing
temperature
(°C)
H2 purity in the
permeate (%)
80 76.4
60 85.4
40 96.6
30 99.4
Exceeds the H2 purity
requirement of Grade A (98.0 %)
and is close to Category 3
(99.9%).
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Acknowledgements
This project has received funding from the Fuel Cells and
Hydrogen 2 Joint Undertaking under grant agreement No
700355. This Joint Undertaking receives support from
the European Union’s Horizon 2020 research and
innovation programme and Hydrogen Europe and
N.ERGHY.
The present publication reflects only the author’s view and the FCH JU and the Union
are not liable for any use that may be made of the information contained herein.