Platinum Based Catalysts in the Water Gas Shift Reaction: Recent Advances
Abstract
:1. Introduction
2. Comparative Studies
2.1. Monometallic Catalysts: The Supports
2.1.1. Effect of the Preparation Method of the Ceria Support
2.1.2. Effect of the Preparation Method of the Ceria-Based Solid Solutions and Mixed Oxide Support
2.1.3. Effect of Preparation Method of Supports Different from Ceria
2.1.4. Commercial Supports
2.1.5. Conclusions
Selected Catalyst (Particle/Crystallite Size) | Preparation Procedure | Operative Condition WGS | CO Conversion (XCO) (Temperature) | Ref. |
---|---|---|---|---|
1wt%Pt/CeO2 (12 nm) | Pt loading by wet impregnation; CeO2 by microwave-assisted hydrothermal synthesis | WHSV = 40,000 mL·g−1·h−1; H2O/CO = 6 | XCO ≈ 97% (T = 360 °C) | [23] |
1wt%Pt/CeO2 (not specified) | Wet impregnation + Ar plasma treatment | WHSV = 40,000 mL·g−1·h−1; CO/H2O = 6 | XCO ≈ 97% (T = 280 °C) | [24] |
1wt%Pt/CeO2 (14.0 nm) | Pt loading by wet impregnation; CeO2 by supercritical antisolvent process | GHSV = 5000 h−1; H2O/CO = 3 | XCO ≈ 99% (T = 287 °C) | [25] |
1wt%Pt/CeO2 (5.8 nm) | Pt loading by wet impregnation; CeO2 by supercritical antisolvent process | WHSV = 1.13 gCO·gcat−1·h−1; H2O/CO = 3 | XCO ≈ 98% (T = 280 °C) | [26] |
1wt%Pt/CeO2 (7.9 nm) | Incipient wetness impregnation | GHSV = 45,625 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 87% (T = 320 °C) | [27] |
1wt%Pt/CeO2 (1.4 nm) | Incipient wetness impregnation | GHSV = 45,625 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 82% (T = 320 °C) | [28] |
1wt%Pt/CeO2 nanorods (1.6 nm) | Pt loading by incipient wetness impregnation; CeO2 by hydrothermal process for 12 h | GHSV = 95,541 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 77% (T = 360 °C) | [29] |
3wt%Pt/CeO2-nanorod (<2 nm) | Pt by impregnation method | GHSV = 4.6 × 105 h−1; H2O/CO = 2.4 | XCO ≈ 92% (T = 600 °C) | [30] |
1wt%Pt/CeO2 nanofibers (4.5 nm) (dnanofibers = 80–120 nm) | Electrospinning technology | WHSV = 60,000 mL·gcat−1·h−1; H2O/CO = 5.3 | XCO ≈ 98% (T = 350 °C) | [31] |
1wt% Pt/Ce0.8Zr0.2O2 (1.69 nm) | Incipient wetness impregnation | GHSV = 45,515 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 86% (T = 320 °C) | [32] |
1Wt%Pt/CeO2/ZrO2 (7.22 nm) | Wet impregnation | GHSV = 5000 h−1; H2O/CO = 5 | Equilibrium CO conversion at 200 °C | [33] |
2wt%Pt/Ce0.8Fe0.2/Al2O3 (2.2 nm) | Wet impregnation | GHSV = 4000 h−1; H2O/CO = 6.9 | Equilibrium CO conversion at 280 °C | [34] |
1.63wt%Pt/Ce0.4Ti0.6O2 (7.25 nm) | Wet impregnation | GHSV = 3600 h−1; H2O/(CO + CO2) = 4.8 | XCO ≈ 91% (T = 400 °C) | [35] |
0.9wt%Pt/CeO2@SiO2-nanotube (3.1 nm) | CeO2 by hydrothermal synthesis method SiO2 shell by modified Stober method | WHSV = 36,000 mL·gcat−1·h−1; H2O/CO = 3 | XCO ≈ 30% (T = 250 °C) | [36] |
1wt%Pt/CeO2 (3 nm) | Incipient wetness impregnation | GHSV = 45,515 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 88% (T = 320 °C) | [38] |
1wt%Pt@Al2O3-nanorods (10.4 nm) | Pt loading by NaBH4 reduction Al2O3 by polymerization | GHSV = 22,500 h−1; H2O/CO = 2 | XCO ≈ 96% (T = 450 °C) | [39] |
1Wt%Pt/sZnOspherical morphology (1.5 nm) | Incipient wetness impregnation | GHSV = 9583 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 92% (T = 240 °C) | [40] |
0.5wt%Pt/Zr0.9Y0.1O1.95 (0.5–2 nm) | Incipient wetness impregnation | GHSV = 120,220 h−1; H2O/CO = 8.7 | XCO ≈ 74% (T = 300 °C) | [41] |
1wt%Pt/TiO2/PRGO-5 (11.3 nm) | Incipient wetness impregnation | GHSV = 47,770 h−1; H2O/(CH4 + CO + CO2) = 3.3 | XCO ≈ 81% (T = 280 °C) | [42] |
1wt%Pt/ZrO2-monoclinic (10.1 nm) | Incipient wetness impregnation | WHSV = 43,200 mL·gcat−1·h−1; H2O/(CO + CO2) = 3.2 | XCO ≈ 65% (T = 300 °C) | [43] |
2.2. Monometallic Catalysts: The Active Phase
2.2.1. Effect of the Preparation Method
2.2.2. Effect of the Platinum Loading
2.2.3. Comparative Studies between Pt and Rh
2.2.4. Conclusions
Selected Catalyst (Particle/Crystallite Size) | Preparation Procedure | Operative Condition WGS | CO Conversion/Rate (XCO)/(rCO) (Temperature) | Ref. |
---|---|---|---|---|
1wt%Pt/CeO2 (1.5–2 nm) | Reactive Spray Deposition Technology | GHSV = 8622 h−1; H2O/CO = 3 | Equilibrium CO (T = 350 °C) | [44] |
3wt%Pt/CeO2 (1.7 nm) | Pt loading by photochemical method adding PVP and 4-benzyolbenzoic acid; CeO2 by co-electrospinning | WHSV = 1.2 × 105 mL·g−1·h−1; H2O/CO = 5 | XCO ≈ 95% (T = 450 °C) | [45] |
BaCe0.96Pt0.04O(3-δ) (<100 nm) | Citrate-gel method | GHSV = 5000 h−1; H2O/CO = 4.5 | XCO ≈ 86% (T = 400 °C) | [46] |
0.9wt%Pt/CeO2 (0.8 nm) | Hydrothermal method | GHSV = 5000 h−1; H2O/CO = 1 | XCO ≈ 97% (T = 140 °C) | [47] |
2wt%Pt/Ce0.75Zr0.25O2 (7.45 nm) | Yolk−shell microspheres formation by a spray pyrolysis process | GHSV = 18,193 h−1; H2O/(CH4 + CO + CO2) = 2 | XCO ≈ 89% (T = 320 °C) | [48] |
1.2wt%Pt/La2O3·SiO2 | Incipient wetness impregnation | GHSV = 2.8 × 106 h−1; H2O/CO = 3 | rCO = 350 mol·g−1·min−1 (T = 400 °C) | [49] |
Pt@TiO2 (1.0 nm) | Yolk-shell nanospheres by a reverse micelle system | WHSV = 40,000 mL·gcat−1·h−1; H2O/CO = 5 | XCO ≈ 99%, T = 260 °C) | [50] |
2.2wt%Pt_NaA (not specified) | NaA zeolite by hydrothermal syntesis with conventional heating; Pt loading by encapsulation | GHSV = 6421 h−1; H2O/CO = 2 | XCO ≈ 96% (T = 400 °C) | [51] |
0.5wt%Pt/CeO2 (1.3 nm) | By wet impregnation | H2O/(CO + CO2) = 2.5 | XCO ≈ 45% (T = 275 °C) | [52] |
3.7wt% Pt/CeO2 (2.3 nm) | Flamespray pyrolisis method | WHSV = 5 × 104 mL·g−1·h−1; H2O/CO = 4 | XCO ≈ 97% (T = 250 °C) | [54] |
0.6wt%Pt/La2O3·SiO2 (not specified) | By Incipient wetness impregnation | WHSV = 6–24 × 103 mL·g−1·h−1; H2O/CO = 3 | XCO ≈ 95% (T = 400 °C) | [55] |
2.3. Polymetallic Catalysts and Addition of Promoters: The Active Phase
2.3.1. The Addition of Na, Re, Mo, V and Ni
2.3.2. Comparative Studies between Multiple Metals
Selected Catalyst (Particle/Crystallite Size) | Preparation Procedure | Operative Condition WGS | CO Conversion/Rate (XCO)/(r) (Temperature) | Ref. |
---|---|---|---|---|
1wt%Pt-2wt%Na/CeO2 (2.2 nm) | By incipient wetness impregnation | GHSV = 45,515 h−1; H2O/(CH4 +CO + CO2) = 2.0 | Equilibrium CO conversion (T = 310 °C) | [56] |
0.5wt%Pt–0.5wt%Re/TiO2 (not specified) | By co-impregnation | GHSV = 410,000 h−1; H2O/CO = 2.5 | XCO ≈ 90% (T = 300 °C) | [57] |
Pt0.25-Mo0.75/C (1.27 nm) | By controlled surface reaction | WHSV = 240,000 mL·gcat−1·min−1; H2O/CO = 2 | r ≈ 10 μmol/gcat·s (T = 300 °C) | [58] |
4.3wt%Pt/64.6wt%Mo2C (not specified) | By wet impregnation | GHSV = 125,000 h−1 H2O/(CO + CO2) = 1.23 | XCO = 70% (T = 250 °C) | [60] |
4.79wt%VOx-0.49wt%Pt/Al2O3 (not specified) | By wet impregnation | WHSV = 80,000 mL·gcat−1·h−1; H2O/CO = 3 | XCO ≈ 60% (T = 450 °C) | [61] |
2.5wt%Pt-2.5wt%Ni/5wt%CeO2/Al2O3 (not specified) | By wetness incipient impregnation | W/FCOin = 20.37 gcat·h/molCO; H2O/CO = 5 | XCO ≈ 80% (T = 750 °C) | [62] |
1wt%Pt-1.25wt%K-1.25wt%CeO2/Al2O3 (not specified) | By incipient wetness co-impregnation | WHSV = 24,000 mL·gcat−1·h−1; H2O/(CO + CO2) = 0.67 | XCO ≈ 60% (T = 300 °C) | [64] |
1wt%Pt/1wt%Sn/CeZrO4 (9.3 nm) | By wet impregnation | GHSV = 10,000 h−1; H2O/CO = 3.75 | Equilibrium CO conversion (T = 230 °C) | [65] |
1wt%Pt-1wt%Re/CeZrO4 (9.4 nm) | By wet impregnation | GHSV = 10,000 h−1; H2O/CO = 3.75 | Equilibrium CO conversion (T = 200 °C) | [66] |
2.1wt%Pt–2.1wt%Re/25wt%CeO2/Al2O3 (1.4–5.0 nm) | By the incipient wetness impregnation | WHSV = 400,000 mL·gcat−1·h−1 H2O/(CO + CO2)= 2.2 | XCO ≈ 74% (T = 400 °C) | [67] |
LaCo0.94Pt0.04O3-δ (75.5 nm) | By pyrolysis | GHSV = 5000 h−1; H2O/(CO + CO2) = 1.8 | XCO ≈ 90% (T = 325 °C) | [69] |
2.3.3. The Addition of Promoters to the Support
2.3.4. Conclusions
Selected Catalyst (Particle/Crystallite Size) | Preparation Procedure | Operative Condition WGS | CO Conversion/H2 Formation Rate (XCO)/(rH2) (Temperature) | Ref. |
---|---|---|---|---|
2.5wt%Au-2.5wt%Pt/FSM16 (7 nm) | Pt and Au loading by co-impregnation; FSM by surfactant templation | H2O/CO = 0.08 | rH2 = 5 mmol·gcat−1 (T = 77 °C) | [70] |
1wt%Pt–40wt%CeO2/C (not specified) | Pt and Ce loading by impregnation under vacuum with acetone | WHSV = 60,000 mL·gcat−1·h−1 H2O/CO = 20.5 | XCO > 70% (T = 300 °C) | [72] |
20wt%CeO2/1wt%Pt/Al2O3 (5.7 nm) | By sol-gel synthesis | WHSV = 130,000 mL·gcat−1·h−1 H2O/CO = 10 | XCO ≈ 95% (T = 350 °C) | [73] |
3. Kinetics of Water-Gas Shift Reaction
3.1. Monometallic Catalysts
3.1.1. Pt/Mo2C-Based Catalysts
3.1.2. Pt/CeO2-Based Catalysts
3.1.3. Pt/MnO2-Based and Pt/strontium Hydroxy and Fluorapatite Catalysts
3.1.4. Conclusions
3.2. Polymetallic and Promoted Catalysts
3.2.1. Mo-Promoted Catalysts
3.2.2. Alkali-Promoted Catalysts
3.2.3. Rare Earth and Transition Metals-Promoted Catalysts
3.2.4. Conclusions
4. Reaction Mechanisms
4.1. Monometallic Catalysts Supported on Single and Mixed Oxides
4.1.1. CeO2- and CeO2-TiO2-Supported Platinum Catalysts
4.1.2. Ca and Si Addition to CeO2-Supported Platinum Catalysts
4.1.3. CeO2ZrO2-Supported Platinum Catalysts
4.1.4. CeO2La2O3-Supported Platinum Catalysts
4.1.5. Different-Supported Platinum Catalysts
4.1.6. Conclusions
4.2. Polymetallic and Promoted Catalysts
4.2.1. Pt-Based Bimetallic Catalysts Supported on Different Oxides
4.2.2. Alkali Metals Promotion of Pt-Based Catalysts
4.2.3. Other Metals Promotion of Pt-Based Bimetallic Catalysts
4.2.4. Conclusions
4.3. DFT and Theoretical Studies
4.3.1. Unsupported Monometallic Pt Surface Models
4.3.2. Unsupported Polymetallic Surface Models
4.3.3. TiO2-Supported Pt Models
4.3.4. CeO2-Supported Pt Models
4.3.5. MgO-Supported Pt and Bimetallic Supported Models
4.3.6. Conclusions
5. Deactivation Studies
6. Electrochemical Promotion
7. Pt-Based Catalysts for Medium Temperature Single Stage WGS Process
8. Conclusions
Author Contributions
Funding
Conflicts of Interest
Abbreviations
Acronym | Extended term |
ALD | Atomic layer deposition |
BET | Brunauer–Emmett–Teller |
CNTs | Carbon nanotubes |
DFT | Density functional theory |
DRIFTS | Diffuse reflection infrared Fourier transform spectroscopy |
EPOC | Electrochemical promotion of catalysis |
GGA | Generalized gradient approximation |
GHSV | Gas Hourly Space Velocity |
HOPG | Highly oriented pyrolytic graphite |
HTS | High-temperature water-gas shift |
IGCC | Integrated gasification combined cycle |
KMC | Kinetic Monte Carlo |
LDHs | Layered double hydroxides |
LTS | Low-temperature water-gas shift |
MCNTs | Multiwalled carbon nanotubes |
MOF | Metal-organic frameworks |
NEMCA | Non-Faradaic Electrochemical Modification of Catalytic Activity |
NPs | Nanoparticles |
OSC | Oxygen storage capacity |
PBE | Perdew–Burke–Ernzerhof functional |
PRGO | Partially reduced graphite oxide |
PRO | Partially reducible oxide |
QoIs | Quantities of interest |
RDS | Rate determining step |
RSDT | Reactive spray deposition technology |
SAC | Single-atom catalyst |
SSA | Specific Surface Area |
TEM | Transmission Electron Microscopy |
TMCs | Transition metal carbides |
TOF | Turnover frequency |
TPB | The three-phase boundary |
UPS | UV photoelectron spectroscopy |
UQ | Uncertainty quantification |
WGS | Water gas shift |
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Catalyst | TOF (s−1) | Ea (kJ·mol−1) | |
---|---|---|---|
240 °C | 280 °C | ||
Pt/CeO2 | 0.38 | 1.30 | 55 |
Pt/Ce0.8Zr0.2O2 | 0.19 | 0.70 | 57 |
Pt/Ce0.6Zr0.4O2 | 0.14 | 0.49 | 59 |
Pt/Ce0.4Zr0.6O2 | 0.09 | 0.36 | 65 |
Pt/Ce0.2Zr0.8O2 | 0.06 | 0.22 | 72 |
Pt/ZrO2 | 0.05 | 0.14 | 83 |
Support | Pt Content (wt%) | Reaction Orders | Ea (kJ·mol−1) | TOF at 270 °C/× 10−3 molH2·(Surface molPt)−1·s−1 | |||
---|---|---|---|---|---|---|---|
CO | H2O | CO2 | H2 | ||||
SiO2 | 4.3 | 0.1 | 0.6 | 0.0 | −0.1 | 74 | 85 |
1.2Mo/SiO2 | 1.9 | 0.1 | 0.8 | 0.1 | −0.2 | 48 | 260 |
4.2Mo/SiO2 | 1.8 | 0.5 | 0.8 | −0.1 | −0.3 | 50 | 100 |
9.0Mo/SiO2 | 1.8 | 0.8 | 0.3 | −0.4 | −0.1 | 42 | 28 |
Al2O3 | 2.6 | 0.1 | 0.6 | 0.0 | −0.4 | 82 | 17 |
0.63Mo/Al2O3 | 1.8 | 0.0 | 0.8 | 0.0 | −0.2 | 44 | 150 |
1.4Mo/Al2O3 | 2.1 | 0.0 | 0.8 | −0.1 | −0.2 | 47 | 220 |
3.4Mo/Al2O3 | 2.2 | 0.1 | 0.8 | −0.1 | −0.2 | 48 | 150 |
7.5Mo/Al2O3 | 1.7 | 0.3 | 0.5 | −0.1 | −0.3 | 58 | 54 |
10.7Mo/Al2O3 | 1.7 | 0.8 | 0.5 | −0.7 | −0.5 | 63 | 5 |
CO Path (Support) | H2O Path | CO Path (Pt Particles) |
---|---|---|
CO + * = CO* CO* + O* → CO2 + 2* * + Obulk = O* * + mCO ⟷ (CO)m* | H2O* + * → OH* + H* 2OH* → H2O + O* + * 2H* → H2 H2 + O* → OH* + H* | PtO + CO ⟷ CO2 + Pt Pt + O* ⟷ PtO + * |
Mechanism | Reaction Temperature (°C) | Catalysts (Pt Particles Size) | Ref. |
---|---|---|---|
Associative | 200–450 | Pt/HfO2 (~2 nm) | [109] |
Redox | 200–350 | Pt/CeO2-TiO2 (1.1–2.0 nm) | [111] |
Associative | 150–450 | Pt/CeO2 (sol-gel method) (~0.5–2 nm) | [114] |
Redox | 200–400 | Pt/Ce0.6Y0.4O2 (~2.3–3.4 nm) | [115] |
Redox + associative | 200–330 | Pt/CeO2, Pt/CeO2-TiO2 (1.8–2 nm) | [116] |
Redox | 200–330 | Pt/TiO2 (1.9 nm) | [116] |
Redox | 100–400 | Pt/CeO2-TiO2 | [117] |
Associative | 200–300 | CexCa1−xOy (~1.5 nm) | [119] |
Associative | 270 | Pt/S5C95 (not specified) | [121] |
Associative | 250 | Pt/CeO2, Pt/CeO2-ZrO2, Pt/ZrO2 (not specified) | [122] |
Redox (different carbonate species) | 200–300 | Pt/CeO2-ZrO2 (1.9–2.4 nm) | [123] |
Proposed mechanism (Table 7) | - | Pt/CeO2–ZrO2(−La2O3) (not specified) | [124] |
Associative | 250–350 | Pt/Ce0.5La0.5O2−∂ (1.2–1.5 nm) | [125] |
Redox (La-rich) + associative (Ce-rich) | 200–350 | Pt/Ce1−xLaxO2−∂ (1.0–1.4 nm) | [126] |
Redox + associative | 300 | Pt/(100−x)wt%Ce0.8La0.2O2−∂-xwt%CNT (5.6–14.4 nm) | [127] |
Associative | 200–300 | Pt/CexMe1−xO2 (Me = Ba, La, Y, Hf, Zn) (not specified) | [128] |
Redox + associative | 250–300 | Pt/Ce0.8Ti0.2O2−δ (Pt ~ 1.7 nm) | [129] |
Redox + associative | 250–300 | Pt/Ce1−xLaxO2−∂ (1.0–1.2 nm) | [130] |
CO preferential oxidation onto Ptn+ sites in Al2O3 defects | 227–400 | Pt/Al2O3 (not specified) | [131] |
CO activation on Pt-NP H2O activation on Mo2C | 110–140 | Pt/Mo2C (not specified) | [132] |
Associative | 250–450 | Pt/HAP (0.8–1.9 nm) | [133] |
CO preferential oxidation onto Pt-NPs sites | 100–400 | Pt/HZSM-5 (Pt-NPs (not-specified) and SAC) | [134] |
CO activation through the mechanism proposed in Figure 20 | 50–150 | Pt/MOF (SAC) | [135] |
Redox (Pt-SAC) + associative (Pt-NPs) | 150–300 | Pt/FeOx (2.1 nm and SAC) | [136] |
Associative (OCOH intermediate) | 252–402 | Pt(111) single crystal (SAC) | [137] |
Mechanism | Reaction Temperature (°C) | Catalysts (Metal Particles Size) | Ref. |
---|---|---|---|
Associative | 350 | Fe-Pt/SiO2 (not specified) | [140] |
Associative (HCOO-) formates | 100–350 | Pt/CeO2 (Pt ~2.5 nm) Ru/CeO2 (Ru ~1.5 nm) Pt-Ru/CeO2 (Pt-Ru alloy of ~2 nm) | [141] |
Redox | 20–220 | Pt substituted Mn3O4 (12–22 nm) | [142] |
Associative | 250–400 | Na doped Pt/YSZ (Pt ~1.5 nm) | [146] |
Associative | 200–350 | 2%Pt/2.5%Na/SiO2 (Pt ~1–4 nm) | [147] |
Associative | 260–300 | 2.6wt%K-Pt/ZrO2 (Pt ~3.6 nm) | [148] |
Associative | 150–350 | KOH-coated Pt/Al2O3 (Pt ~5 nm) | [149] |
Associative with red-ox regeneration | 300 | Pt/Ti[20]/ZrO2 (not specified) | [150] |
Reaction | Elementary Reactions | Mechanism |
---|---|---|
1 | CO* + O* → CO2(g) | Redox |
2 | CO* + OH* → COOH* → CO2(g) + H* | Carboxyl |
3 | CO* + H* + O* → CHO* + O* → HCOO** → CO2(g) + H* | Formate |
Elementary Reaction | Ea (eV) | ΔE (eV) |
---|---|---|
H2O + * = H* + OH* | 0.11 | −0.14 |
CO* + OH* = COOH* + * | 0.34 | −0.17 |
COOH* + OH* = H2O* + CO2* | 6.03 | −1.09 |
2H* = H2* + 2* | 0.87 | 0.43 |
Reaction | RDS | Mechanism | Ea (eV) | ΔE (eV) | k (cm3/mol·s) |
---|---|---|---|---|---|
1 | CO* + O* = CO2* + * | Redox | 4.84 | −0.05 | 8.30 × 1012 |
2 | CO* + OH* = COOH* + * | Carboxyl | 3.15 | 0.48 | 1.99 × 1011 |
3 | HCOO* + * = CO2* + H* | Formate | 3.09 | −0.24 | 7.03 × 1012 |
Catalyst | Temperature | Sour Conditions | Stability Test | Ref. |
---|---|---|---|---|
BaCe0.98Pt0.2O3−∂ | 300–400 °C | - | 5 h | [191] |
Pt/CeO2 | 400 °C | 20 ppm H2S | 300 h | [193] |
Pt@CeO2; Pt@CeO0.67Zr0.33O2 | 450 °C | 20 ppm H2S | 130 h | [194] |
Pt-based commercial catalyst | 330 °C | 1 ppm H2S | 100 h | [195] |
Pt on γ-Al2O3, ZrO2, CeO2, Ce0.75Zr0.25O2, Ce0.25Zr0.75O2 | 300 °C | 50 ppm H2S | 20 h | [196] |
Pt/Nb2O5 | 300 °C | 50 ppm H2S | 2.5 h | [197] |
Pt/Nb2O5 | 300 °C | 50–1000 ppm H2S | 4 h | [198] |
Pt(0.6)/La2O3(27)SiO2 | 400 °C | - | 155 h | [199] |
Selected Catalyst | Preparation Procedure | Operative Condition WGS | CO Conversion (XCO)/Current Density (Temperature) | Ref. |
---|---|---|---|---|
Pt/8mol%Y2O3-stabilized-ZrO2 metal loading = 0.83 mg Pt/cm2 | Pt loading by calcination of organometallic paste on the inner and on the outer side of a closed-end tube of Y2O3-stabilized-ZrO2 | GHSV = 1500 h−1; PH2O = 3.1 kPa; PCO = 0.1 kPa η = −1.5 V | XCO ≈ 95% (T = 350 °C) | [203] |
1 wt%Pt/10 mol%La–ZrO2 | La–ZrO2By polymerized complex method Pt loading by impregnation | WHSV = 117,000 ml·gcat−1·h−1 H2O/CO = 1 I = 11 mA | XCO ≈ 70% (T = 500 °C) | [204] |
Pt2.7Cu@CNTs | By impregnation method | WHSV = 333,333 mlCO·gcat−1·h−1 P = 1 bar η = 0.6 V | Current density = 70 mA/cm2 (T = 25 °C) | [205] |
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Palma, V.; Ruocco, C.; Cortese, M.; Renda, S.; Meloni, E.; Festa, G.; Martino, M. Platinum Based Catalysts in the Water Gas Shift Reaction: Recent Advances. Metals 2020, 10, 866. https://doi.org/10.3390/met10070866
Palma V, Ruocco C, Cortese M, Renda S, Meloni E, Festa G, Martino M. Platinum Based Catalysts in the Water Gas Shift Reaction: Recent Advances. Metals. 2020; 10(7):866. https://doi.org/10.3390/met10070866
Chicago/Turabian StylePalma, Vincenzo, Concetta Ruocco, Marta Cortese, Simona Renda, Eugenio Meloni, Giovanni Festa, and Marco Martino. 2020. "Platinum Based Catalysts in the Water Gas Shift Reaction: Recent Advances" Metals 10, no. 7: 866. https://doi.org/10.3390/met10070866