scholarly journals Catalytic Steam Reforming of Glycerol Over Cerium and Palladium-Based Catalysts for Hydrogen Production

2013 ◽  
Vol 10 (2) ◽  
Author(s):  
Ali Ebshish ◽  
Zahira Yaakob ◽  
Y. H. Taufiq-Yap ◽  
Ahmed Bshish ◽  
Abdulmajid Shaibani
Keyword(s):  
Electron Microscopy ◽  
Hydrogen Production ◽  
Steam Reforming ◽  
Catalytic Reactions ◽  
Fixed Bed Reactor ◽  
Hydrogen Yield ◽  
Water Mixture ◽  
Impregnation Method ◽  
Catalytic Steam Reforming ◽  
Total Average

In this work, catalytic steam reforming of glycerol for hydrogen production was performed over Ce/Al2O3 and Pd/Al2O3 catalysts prepared via the impregnation method. The catalysts were characterized by scanning electron microscopy (SEM-EDX), transmission electron microscopy (TEM), BET surface area, and X-ray diffraction (XRD). Two sets of catalytic reactions were conducted, one comparing 1% Pd/Al2O3 to 1% Ce/Al2O3 and the second comparing 1% Ce/Al2O3 loading to 10% Ce/Al2O3 loading. All catalytic reactions were performed using a fixed-bed reactor operated at 600 °C and atmospheric pressure. Aglycerol–water mixture at a molar ratio of 1:6 was fed to the reactor at 0.05 ml/min. In the first set of experiments, Pd/Al2O3 exhibited higher hydrogen productivity than Ce/Al2O3. A maximum hydrogen yield of 56% and a maximum selectivity of 78.7% were achieved over the Pd/Al2O3 catalyst. For the second set of experiments, the results show that the reaction conversion increased as the cerium loading increased from 1% to 10%. A total average hydrogen yield of 28.0% and a selectivity of 45.5% were obtained over 1% Ce/Al2O3, while the total average hydrogen yield and selectivity were 42.2% and 52.7%, respectively, for 10% Ce/Al2O3.

Steam Reforming of Model Compounds from Bio-Oil for Hydrogen Production over Pd/HZSM-5 Catalyst

2012 ◽  
Vol 550-553 ◽  
pp. 558-562
Author(s):  
Qi Wang ◽  
Long Guo ◽  
Xin Bao Li
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Hydrogen Yield ◽  
Impregnation Method ◽  
Wet Impregnation ◽  
Product Gas ◽  
Bio Oil ◽  
H2 Yield

Ethanol was selected as a model compound of bio-oil. Pd/HZSM-5 catalyst with 5%wt Pd was prepared by wet impregnation method. The steam reforming experiment for hydrogen production was carried out on a fixed bed reactor. The carbon conversion, carbon selectivity of product gas and H2 yield was calculated according the experimental resultsl. It has been found that the best performance was obtained at T=700°C, S/C=9.2 and GC1HSV=346h-1. At this condition, the hydrogen yield and potential hydrogen yield can be as high as 58.1% and 84.3%. The results show that the addition of Pd to HZSM-5 can improve the reforming performance and increase the hydrogen yield.

Activity of Copper and Nickel Loaded on HZSM-5Zeolite Based Catalyst for Steam Reforming of Glycerol to Hydrogen

2014 ◽  
Vol 699 ◽  
pp. 504-509
Author(s):  
Hafizah Abdul Halim Yun ◽  
Ramli Mat ◽  
Tuan Amran Tuan Abdullah ◽  
Mahadhir Mohamed ◽  
Anwar Johariand Asmadi Ali
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Operating Conditions ◽  
Zeolite Catalysts ◽  
Fixed Bed Reactor ◽  
Molar Ratio ◽  
Hydrogen Yield ◽  
Impregnation Method ◽  
Glycerol Conversion

The study focuses on hydrogen production via glycerol steam reforming over copper and nickel loaded on HZSM-5 zeolite based catalyst. The catalysts were prepared by using different loading amount of copper (0-10wt%) and nickel (0-10wt%) on HZSM-5 zeolite catalysts through wet impregnation method and was characterized by X-Ray Diffraction (XRD). The performances of catalysts were evaluated in terms of glycerol conversion and hydrogen production at 500°C using 6:1 of water to glycerol molar ratio (WGMR) in a tubular fixed bed reactor. All the catalysts had achieved more than 85% of glycerol conversion except that of 5%Cu loaded on HZSM-5 catalyst. The addition of nickel into 5% Cu/HZSM-5 catalyst had increased the hydrogen yield. Similar trend was observed when copper was added into Ni/HZSM-5 catalyst but using copper loaded on HZSM-5 alone was unable to produce hydrogen compared to using nickel catalyst alone. It showed that copper acted as a promoter for hydrogen production. It was established that a 5wt% of Cu with 10wt% of Ni loaded on HZSM-5 catalyst showed significant improvement in terms of hydrogen yield and gaseous product compositions at selected operating conditions.

scholarly journals Ca-Modified Co/SBA-15 Catalysts for Hydrogen Production through Ethanol Steam Reforming

2013 ◽  
Vol 24 ◽  
pp. 1-16 ◽  
Author(s):  
Chen-Bin Wang ◽  
Siao Wun Liu ◽  
Kuan Fu Ho ◽  
Hsin Hua Huang ◽  
Chih Wei Tang ◽  
...  
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Coke Deposition ◽  
Incipient Wetness Impregnation ◽  
Hydrogen Yield ◽  
Impregnation Method ◽  
Steam Reforming Of Ethanol ◽  
Incipient Wetness

Hydrogen production through steam reforming of ethanol (SRE) over the Ca-modified Co/SBA-15 catalysts was studied herein to evaluate the catalytic activity, stability and the behavior of coke deposition. The Ca-modified SBA-15 supports were prepared from the Ca(NO3)2·4H2O (10 wt%) which was incorporated to SBA-15 by incipient wetness impregnation (assigned as Ca/SBA-15) and direct hydrothermal (assigned as Ca-SBA-15) method. The active cobalt species from the Co(NO3)2·6H2O (10 wt%) was loaded to SiO2, SBA-15 and modified-SBA-15 supports with incipient wetness impregnation method to obtain the cobalt catalysts (named as Co/SiO2, Co/SBA-15, Co-Ca/SBA-15 and Co/Ca-SBA-15, respectively). The prepared catalysts were characterized by using X-ray diffraction (XRD), temperature programmed reduction (TPR), transmission electron microscopy (TEM) and BET. The catalytic performance of the SRE reaction was evaluated in a fixed-bed reactor. The results indicated that the Co/Ca-SBA-15 catalyst was preferential among these catalysts and the ethanol can be converted completely at 375 °C. The hydrogen yield (YH2) approached 4.76 at 500 °C and less coke deposited. Further, the long-term stability test of this catalyst approached 100 h at 500 °C and did not deactivate.

Hydrogen Production from Ethanol Steam Reforming over Ni-Cu/ZnO Catalyst

2011 ◽  
Vol 236-238 ◽  
pp. 1067-1072
Author(s):  
Li Ping Liu ◽  
Xiao Jian Ma ◽  
Peng Zhang ◽  
Ya Nan Liu
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Surface Characteristics ◽  
Catalytic Performance ◽  
Fixed Bed Reactor ◽  
Molar Ratio ◽  
Ethanol Steam Reforming ◽  
Hydrogen Yield ◽  
Ethanol Steam

Hydrogen production by ethanol steam reforming over Ni-Cu/ZnO catalyst in the temperatures range of 250-550°C was studied on a fixed bed reactor. The effects of reaction temperature and water/ethanol molar ratio on hydrogen production were investigated. The structure and surface characteristics of the catalyst were measured by scanning electron microscopy (SEM), X-ray diffraction (XRD) and differential thermal analyzer (TG-DSC). The results show that the Ni-Cu/ZnO catalyst has good catalytic performance with higher hydrogen yield of 4.87molH2/molEtOH reacted. A comparison of hydrogen production from ethanol steam reforming over Ni-Cu/ZnO catalyst with over a commercial catalyst was made in this paper.

scholarly journals Hydrogen Generation from Catalytic Steam Reforming Bio-Oil Model Compound—Acetic Acid Employing Ni/attapulgite Catalysts Prepared with Different Preparation Methods

2016 ◽  
Author(s):  
Yishuang Wang ◽  
Mingqiang Chen ◽  
Tian Liang ◽  
Jie Yang ◽  
Zhonglian Yang ◽  
...  
Keyword(s):  
Acetic Acid ◽  
Steam Reforming ◽  
Catalyst Deactivation ◽  
Hydrogen Generation ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Precipitation Method ◽  
Impregnation Method ◽  
Bio Oil ◽  
Catalytic Steam Reforming

In this research, catalytic steam reforming acetic acid derived from the aqueous portion of bio-oil for hydrogen production was investigated by using different Ni/ATC (Attapulgite Clay) catalysts prepared by precipitation, impregnation and mechanical blending methods. The fresh and reduced catalysts were characterized by XRD, N2 adsorption-desorption, TEM and H2-TPR. The comprehensive results demonstrated that the interaction between active metallic Ni and ATC carrier was significantly improved in Ni/ATC catalyst prepared by precipitation method, and in which the mean Ni particle size was the smallest (~13 nm) resulted in the highest metal dispersion (7.5%). The catalytic performance of the three catalysts was evaluated through the process of steam reforming of acetic acid in a fixed-bed reactor under atmospheric pressure at two different temperatures, such as 550 ℃ and 650 ℃. Results showed that the Ni/ATC (PM-N/ATC) prepared by precipitation method, achieved the highest H2 yield of ~82% and little lower acetic acid conversion efficiency of ~85% than that (~95%) of Ni/ATC (IM-NATC) prepared by impregnation method. In addition, the deactivation catalysts after reaction for 4 h were analyzed by XRD, TGA-DTG and TEM, which demonstrated that the catalyst deactivation was not caused by the amount of carbon deposition, but owed to the significant agglomeration and sintering of Ni particles in the carrier.

The Preparation Conditions of Catalyst for Steam Reforming of Fast Pyrolysis Bio-Oil

2011 ◽  
Vol 347-353 ◽  
pp. 2231-2235 ◽  
Author(s):  
Ping Lan ◽  
Li Hong Lan ◽  
Tao Xie ◽  
An Ping Liao
Keyword(s):  
Calcination Temperature ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Active Agent ◽  
Fixed Bed Reactor ◽  
Hydrogen Yield ◽  
Preparation Conditions ◽  
Bio Oil ◽  
Renewable Hydrogen ◽  
Catalytic Steam Reforming

Catalytic steam reforming of bio-oil is an economically feasible route producing renewable hydrogen. Ni/MgO-La2O3-Al2O3 catalyst was prepared with Ni as active agent, Al2O3 as support and MgO, La2O3 as promoters. The experiments were carried out in a fixed-bed reactor. The content of Ni, calcination temperature, and calcinations time, were investigated with hydrogen yield as index. The optimal preparation conditions were concluded as follows: the Ni content 18%, the calcination temperature 8500C and the calcinations time 6 h.

Hydrogen production by steam reforming of glycerol over Ni/Ce/Cu hydroxyapatite-supported catalysts

2013 ◽  
Vol 67 (7) ◽  
Author(s):  
Lukman Hakim ◽  
Zahira Yaakob ◽  
Manal Ismail ◽  
Wan Daud ◽  
Ratna Sari
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Fixed Bed ◽  
Supported Catalyst ◽  
Fixed Bed Reactor ◽  
Bet Surface Area ◽  
Precipitation Method ◽  
Molar Ratio ◽  
Hydrogen Yield ◽  
Glycerol Conversion

AbstractHydroxyapatite-supported Ni-Ce-Cu catalysts were synthesised and tested to study their potential for use in the steam reforming of glycerol to produce hydrogen. The catalysts were prepared by the deposition-precipitation method with variable nickel, cerium, and copper loadings. The performance of the catalysts was evaluated in terms of hydrogen yield at 600°C in a tubular fixed-bed microreactor. All catalysts were characterised by the BET surface area, XRD, TPR, TEM, and FE-SEM techniques. The reaction time was 240 min in a fixed-bed reactor at 600°C and atmospheric pressure with a water-to-glycerol feed molar ratio of 8: 1. It was found that the Ni-Ce-Cu (3 mass %-7.5 mass %-7.5 mass %) hydroxyapatite-supported catalyst afforded the highest hydrogen yield (57.5 %), with a glycerol conversion rate of 97.3 %. The results indicate that Ni/Ce/Cu/hydroxyapatite has great potential as a catalyst for hydrogen production by steam reforming of glycerol.

Hydrogen Production by Catalytic Steam Reforming of Model Compounds of Biomass Fast Pyrolysis Oil

2010 ◽  
Vol 1279 ◽  
Author(s):  
P. Lan ◽  
Q. L. Xu ◽  
L. H. Lan ◽  
Y. J. Yan ◽  
J. A. Wang
Keyword(s):  
Hydrogen Production ◽  
Steam Reforming ◽  
Space Velocity ◽  
Molar Ratio ◽  
Hydrogen Yield ◽  
Pyrolysis Oil ◽  
Model Compounds ◽  
Liquid Hourly Space Velocity ◽  
Bio Oil ◽  
Catalytic Steam Reforming

AbstractA Ni/MgO-La2O3-Al2O3 catalyst with Ni as active component, Al2O3 as support, MgO and La2O3 as additives was prepared and its catalytic activity was evaluated in the process of hydrogen production from catalytic steam reforming of bio-oil. In the catalytic evaluation, some typical components present in bio-oil such as acetic acid, butanol, furfural, cyclopentanone and m-cresol were mixed following a certain proportion as model compounds. Reaction parameters like temperature, steam to carbon molar ratio and liquid hourly space velocity were studied with hydrogen yield as index. The optimal reaction conditions were obtained as follows: temperature 750-850 °C, steam to carbon molar ratio 5-9, liquid hourly space velocity 1.5-2.5 h-1. The maximum hydrogen yield was 88.14%. The carbon deposits were formed on the catalyst surface but its content decreased as reaction temperature increased in the bio-oil steam reforming process.

Hydrogen Production from Acetic Acid Steam Reforming over Bimetallic Ni-Co on La2O3 Catalyst-Effect of the Catalyst Dilution

2014 ◽  
Vol 493 ◽  
pp. 39-44 ◽  
Author(s):  
Tuan Amran Tuan Abdullah ◽  
Walid Nabgan ◽  
Mohd Johari Kamaruddin ◽  
Ramli Mat ◽  
Anwar Johari ◽  
...  
Keyword(s):  
Acetic Acid ◽  
Hydrogen Production ◽  
Steam Reforming ◽  
Atmospheric Pressure ◽  
Bimetallic Catalysts ◽  
Fixed Bed ◽  
Fixed Bed Reactor ◽  
Product Gas ◽  
Catalyst Effect ◽  
Catalytic Steam Reforming

Catalytic steam reforming of acetic acid using bimetallic catalysts of 5 wt.% nickel and 5 wt.% cobalt supported on Lanthanum (III) oxide (La2O3) for hydrogen production was investigated in a micro fixed bed reactor. The reactor was of quartz tube with a 10 mm inside diameter. The effect of catalyst dilution on the reaction was studied. Silicon carbide was used as the dilution material. The experiments were conducted at atmospheric pressure and temperatures ranging from 500 to 700°C. The complete conversion of acetic acid to product gases has been observed at 550°C and 700°C for diluted and non-diluted catalysts respectively. It shows that catalyst dilution had a profound effect on the conversion of acetic acid at low temperature (550°C) whilst high temperature of 700°C was required for the non-diluted catalyst. The product gas distributions are similar when using both diluted and non-diluted catalysts.

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