Hydrodesulphurization of Thiophene over Co, Mo and CoMo /g-Al2O3 Catalysts

2018 ◽  
Vol 69 (2) ◽  
pp. 396-399
Author(s):  
Rami Doukeh ◽  
Ancuta Trifoi ◽  
Mihaela Bombos ◽  
Ionut Banu ◽  
Minodora Pasare ◽  
...  
Keyword(s):  
Fixed Bed ◽  
Molar Ratio ◽  
Catalytic Reactor ◽  
Monometallic Catalysts ◽  
Thiophene Conversion ◽  
C 30 ◽  
Al2o3 Catalyst

The hydrodesulphurization (HDS) of thiophene was performed on monometallic catalysts Co/g -Al2O3, Mo/g -Al2O3 and bimetallic CoMo/g -Al2O3. Experiments were carried out on a fixed bed catalytic reactor at 175-300�C, 30-60 atm, thiophene volume hourly space velocities of 1h-1- 4h-1 and molar ratio hydrogen/thiophene of 60/1. The thiophene conversion on the bimetallic CoMo/g -Al2O3 catalyst was higher than on Co/g -Al2O3 or Mo/g -Al2O3.

Hydrodesulphurization of Thiophenes over CoMoRe/ ZSM 5gama-Al2O3 Catalyst

2018 ◽  
Vol 69 (6) ◽  
pp. 1386-1390
Author(s):  
Rami Doukeh ◽  
Mihaela Bombos ◽  
Marioara Moldovan ◽  
Ion Bolocan
Keyword(s):  
Pore Volume ◽  
Pore Diameter ◽  
Fixed Bed ◽  
Texture Features ◽  
Molar Ratio ◽  
Catalytic Reactor ◽  
Average Pore ◽  
Metallic Catalyst ◽  
C 30 ◽  
Al2o3 Catalyst

The hydrodesulphurization (HDS) of thiophenes was performed on metallic catalyst CoMoRe/ZSM5-gAl2O3. Experiments were carried out on a fixed bed catalytic reactor at 175-300�C, 30-60 atm, thiophene volume hourly space velocities of 1h-1- 4h-1 and molar ratio hydrogen/thiophene of 60/1. Texture features like specific surface area, the pore volume and the average pore diameter decrease after catalyst sulfurization. The thiophenes conversion on CoMoRe/gAl2O3-Zn-HZSM 5 catalyst differs with the nature of the studied thiophenes.

Dimethyldisulphide Hydrodesulphurization on NiCoMo / Al2O3 Catalyst

2017 ◽  
Vol 68 (7) ◽  
pp. 1496-1500
Author(s):  
Rami Doukeh ◽  
Mihaela Bombos ◽  
Ancuta Trifoi ◽  
Minodora Pasare ◽  
Ionut Banu ◽  
...  
Keyword(s):  
Good Accuracy ◽  
Fixed Bed ◽  
Continuous System ◽  
Space Velocity ◽  
Molar Ratio ◽  
Catalytic Reactor ◽  
Liquid Hourly Space Velocity ◽  
Hydrodesulfurization Process ◽  
Al2o3 Catalyst ◽  
Simplified Kinetic Model

Hydrodesulphurization of dimethyldisulphide was performed on Ni-Co-Mo /�-Al2O3 catalyst. The catalyst was characterized by determining the adsorption isotherms, the pore size distribution and the acid strength. Experiments were carried out on a laboratory echipament in continuous system using a fixed bed catalytic reactor at 50-100�C, pressure from 10 barr to 50 barr, the liquid hourly space velocity from 1h-1 to 4h-1 and the molar ratio H2 / dimethyldisulphide 60/1. A simplified kinetic model based on the Langmuir�Hinshelwood theory, for the dimethyldisulphide hydrodesulfurization process of dimethyldisulphide has been proposed. The results show the good accuracy of the model.

Reuse of Fried Oil to Obtain Biodiesel: Zeolites Y as a Catalyst

2007 ◽  
Vol 5 (1) ◽  
Author(s):  
A. Brito ◽  
M. E. Borges ◽  
R. Arvelo ◽  
F. Garcia ◽  
M. C. Diaz ◽  
...  
Keyword(s):  
Fixed Bed ◽  
Weight Ratio ◽  
Degree Of Conversion ◽  
Transesterification Reaction ◽  
Molar Ratio ◽  
Catalytic Reactor ◽  
Reaction Products ◽  
Waste Oil ◽  
Catalytic Effects ◽  
Fried Oil

The transesterification reaction is the most utilized process to obtain biodiesel. Fried oil transesterification reactions with methanol have been studied using several zeolites Y and interchanged with CsCl and KOH. The reaction has been carried out both in a slurry reactor and a fixed bed catalytic reactor. The catalytic effects of zeolites have been tested within a temperature range of 60-476°C, 2.5-5% catalyst/waste oil weight ratio, and 6:1 - 100:1 methanol/oil molar ratio. Cosolvents (THF, n-hexane) in the reaction feedstock effect have also been studied as well as catalyst regeneration effects. Viscosity of both the oil and the transesterification reaction products was determined as an initial guide to investigate the degree of conversion to biodiesel as well as FAME content by GC. When interchanged zeolites are used conversions are improved, getting the best yields (98% FAME) for the Y756 zeolite interchanged with KOH. Viscosities of the reaction product obtained reached values next to diesel standard ones.

scholarly journals The Influence of a Mesoporous Silica on Ru-Sn Catalyst Activity in the Hydrogenation of Methyl Oleate

2019 ◽  
Vol 70 (8) ◽  
pp. 2786-2790
Author(s):  
Cristiana Rizea ◽  
Mihaela Bombos ◽  
Traian Juganaru ◽  
Dorin Bombos
Keyword(s):  
Methyl Oleate ◽  
Volume Flow Rate ◽  
Catalyst Activity ◽  
Fixed Bed ◽  
Acid Strength ◽  
Molar Ratio ◽  
Catalytic Reactor ◽  
Saturated Hydrocarbons ◽  
Diethyl Amine ◽  
Liquid Products

The hydrogenation of methyl oleate on a Ru-Sn catalyst deposited on Al-HMS was studied in comparison to that conducted on the same catalyst deposited on a conventional support, i.e. g-Al2O3. The catalyst was prepared by sequential impregnation. The distribution of the acid strength of the prepared catalysts was determined by thermic desorption of diethyl amine in the temperature range from 20 to 600�C. Experiments were carried out on a laboratory echipament using a fixed bed catalytic reactor at a temperature of 275�C, pressure of 100 atm with a methyl oleate volume flow rate (VHSV) of 0.15h-1 and molar ratio hydrogen/ methyl oleate of 10/1. The main compounds identified were saturated and unsaturated fatty alcohols and saturated hydrocarbons. Ru-Sn/ Al-HMS + g-Al2O3 shows a higher conversion to liquid products that the Ru-Sn-Ba / g-Al2O3, probably due to a favorable distribution of the acid strength.

Exergy Analysis of Oxidative Steam Reforming of Methanol for Hydrogen Producton: Modeling Study

2013 ◽  
Vol 11 (1) ◽  
pp. 489-500 ◽  
Author(s):  
Shashi Kumar ◽  
Nisha Katiyar ◽  
Surendra Kumar ◽  
Snigdha Yadav
Keyword(s):  
Steam Reforming ◽  
Exergy Analysis ◽  
Fixed Bed ◽  
Molar Ratio ◽  
Input Energy ◽  
Exergy Destruction ◽  
Catalytic Reactor ◽  
Steam Reforming Of Methanol ◽  
Molar Ratios ◽  
Higher Temperature

Abstract Hydrogen production by oxidative steam reforming of methanol in a fixed bed catalytic reactor was modeled and simulated. The addition of O2 to feed reduced the temperature in the reformer. 99.86% conversion was obtained at 550 K and S/C molar ratio of unity in steam reforming while it is at 540 K in oxidative steam reforming. Although H2 and CO yields were decreased in oxidative steam reforming in comparison to steam reforming, the reductoin H2 yield was note significant whereas reduction in CO was appreciably high. The thermal and exergy efficiencies were favored by reforming temperature and S/C molar ratios. However, variation in S/C molar ratio showed negligibly small effect on efficiencies. The reforming temperature had a notable influence on the efficiencies. The exergy destruction was found to be lower at higher temperature and S/C molar ratio. Thus, oxidative steam reforming of methanol at 540 K and S/C molar ratio of unity utilizes sufficient amount of input energy in the form of useful work and thermodynamic irreversibilities in the reactor are quantitatively small.

Modelling of methane dry reforming over Ni/Al2O3 catalyst in a fixed-bed catalytic reactor

2014 ◽  
Vol 114 (1) ◽  
pp. 109-119 ◽  
Author(s):  
Yacine Benguerba ◽  
Lila Dehimi ◽  
Mirella Virginie ◽  
Christine Dumas ◽  
Barbara Ernst
Keyword(s):  
Fixed Bed ◽  
Dry Reforming ◽  
Catalytic Reactor ◽  
Methane Dry Reforming ◽  
Al2o3 Catalyst

CO2 valorization into synthetic natural gas (SNG) using a Co–Ni bimetallic Y2O3 based catalysts

2021 ◽  
Vol 0 (0) ◽  
Author(s):  
Radwa A. El-Salamony ◽  
Sara A. El-Sharaky ◽  
Seham A. Al-Temtamy ◽  
Ahmed M. Al-Sabagh ◽  
Hamada M. Killa
Keyword(s):  
Reaction Mechanism ◽  
Natural Gas ◽  
Fixed Bed ◽  
Catalytic Performance ◽  
Fixed Bed Reactor ◽  
Molar Ratio ◽  
Impregnation Method ◽  
Synthetic Natural Gas ◽  
Methanation Reaction ◽  
Co2 Valorization

Abstract Recently, because of the increasing demand for natural gas and the reduction of greenhouse gases, interests have focused on producing synthetic natural gas (SNG), which is suggested as an important future energy carrier. Hydrogenation of CO2, the so-called methanation reaction, is a suitable technique for the fixation of CO2. Nickel supported on yttrium oxide and promoted with cobalt were prepared by the wet-impregnation method respectively and characterized using SBET, XRD, FTIR, XPS, TPR, and HRTEM/EDX. CO2 hydrogenation over the Ni/Y2O3 catalyst was examined and compared with Co–Ni/Y2O3 catalysts, Co% = 10 and 15 wt/wt. The catalytic test was conducted with the use of a fixed-bed reactor under atmospheric pressure. The catalytic performance temperature was 350 °C with a supply of H2:CO2 molar ratio of 4 and a total flow rate of 200 mL/min. The CH4 yield was reached 67%, and CO2 conversion extended 48.5% with CO traces over 10Co–Ni/Y2O3 catalyst. This encourages the direct methanation reaction mechanism. However, the reaction mechanism over Ni/Y2O3 catalyst shows different behaviors rather than that over bi-metal catalysts, whereas the steam reforming of methane reaction was arisen associated with methane consumption besides increase in H2 and CO formation; at the same temperature reaction.

Vapor-phase oxidation of propylene glycol-methanol mixture to methyl lactate on CeO2/Al2O3 catalyst

2021 ◽  
pp. 92-97
Author(s):  
M.E. Sharanda ◽  
◽  
A.M. Mylin ◽  
O.Yu. Zinchenko ◽  
V.V. Brei ◽  
...  
Keyword(s):  
Propylene Glycol ◽  
Vapor Phase ◽  
Flow Reactor ◽  
Aldol Condensation ◽  
Ethyl Lactate ◽  
Molar Ratio ◽  
Methyl Lactate ◽  
Reactor Inlet ◽  
Phase Oxidation ◽  
Al2o3 Catalyst

The vapor-phase oxidation of mixtures of propylene glycol with methanol and ethanol to methyl and ethyl lactate, respectively, on supported CeO2/Al2O3 catalyst with 10 wt.% CeO2 content was studied. The steel flow reactor with a fixed catalyst bed (4 cm3) was used. 20 wt.% solution of propylene glycol in alcohol was fed to the reactor inlet by Waters 950 pump at LHSV= 0.5-0.8 h-1. Reaction temperature and pressure were varied in the interval of 190-250 0C and 1.3-1.8 bars respectively. Compressed air was given to the reactor inlet at the molar ratio of propylene glycol/O2 = 1. The reaction products were analyzed using gas chromatography (Agilent 7820A) and 3C NMR (Bruker Avance 400) methods. Studied oxidation of propylene glycol in the presence of methanol describes by total reaction CH3CHOHCH2OH +O2 + СН3OH = CH3CHOHCOOСН3 +2H2O At first, hydroxyacetone is formed that is further oxidized to pyruvic aldehyde, which attaches alcohol to form hemiacetal. Then, hemiacetal of methyl glyoxal rearranges into methyl lactate by Cannizzaro. At 220 0C and load on a catalyst of < 2 mmol PG/gcat/h, the selectivity towards methyl lactate reaches 70 wt.% at 100 % propylene glycol conversion. The main by-products are formed as the result of acetaldehyde transformation. Acetaldehyde could be formed at hydroxyacetone aldol decondensation. In the presence of ethanol, the formation of a significant amount of acetaldehyde and its aldol condensation products as well as the formation of diethoxyethane are observed. Therefore, ethyl lactate selectivity at 100 % propylene glycol conversion does not exceed 45 %. Supported CeO2/SiO2 contact was tested in this oxidation reaction also. However, CeO2/SiO2 provides the low, up to 25%, selectivity towards methyl lactate at full propylene glycol conversion. It was shown that at the same conditions methyl lactate is formed with higher selectivity then ethyl lactate. The high methyl lactate yield up to 70 wt.% could be obtained via vapor-phase oxidation of 20% mixture of propylene glycol with methanol by air oxygen on supported CeO2/Al2O3 catalyst at 210 - 220°С and at time contact of 3-4 seconds.

Influence Factors of Denitration Study on Catalyst Mn-Ce/TiO2

2013 ◽  
Vol 634-638 ◽  
pp. 526-530
Author(s):  
Chun Xiang Geng ◽  
Qian Qian Chai ◽  
Wei Yao ◽  
Chen Long Wang
Keyword(s):  
Reaction Temperature ◽  
Catalytic Reduction ◽  
Removal Rate ◽  
Load Capacity ◽  
Fixed Bed ◽  
Influence Factors ◽  
Space Velocity ◽  
Molar Ratio ◽  
Impregnation Method ◽  
Ammonia Gas

Selective Catalytic Reduction (SCR) processes have been one of the most widely used denitration methods at present and the property of low tempreture catalyst becomes a hot research. The Mn-Ce/TiO2 catalyst was prepared by incipient impregnation method. The influence of load capacity, reaction temperature, O2 content, etc. on denitration were studied by a fixed bed catalyst reactor with ammonia gas. Results showed that catalyst with load capacity 18% performed high NO removal rate of 90% at conditions of reaction temperature 160°C, low space velocity, NH3/NO molar ratio 1: 1, O2 concentration 6%.

scholarly journals Effect of CO2 partial pressure on dry reforming of ethanol for hydrogen production

2018 ◽  
Vol 1 (1) ◽  
pp. 6-10
Author(s):  
Fahim Fayaz ◽  
Ahmad Ziad Sulaiman ◽  
Sharanjit Singh ◽  
Sweeta Akbari
Keyword(s):  
Partial Pressure ◽  
Fixed Bed ◽  
Dry Reforming ◽  
Fixed Bed Reactor ◽  
Bet Surface Area ◽  
Impregnation Method ◽  
X Ray Diffraction ◽  
Co2 Partial Pressure ◽  
Temperature Programmed ◽  
Al2o3 Catalyst

The effect of CO2 partial pressure on ethanol dry reforming was evaluated over 5%Ce-10%Co/Al2O3 catalyst at = PCO2 = 20-50 kPa, PC2H5OH = 20 kPa, reaction temperature of 973 K under atmospheric pressure. The catalyst was prepared by using impregnation method and tested in a fixed-bed reactor. X-ray diffraction measurements studied the formation of Co3O4, spinel CoAl2O4 and CeO2, phases on surface of 5%Ce-10%Co/Al2O3 catalyst. CeO2, CoO and Co3O4 oxides were obtained during temperature–programmed calcination. Ce-promoted 10%Co/Al2O3 catalyst possessed high BET surface area of 137.35 m2 g-1. C2H5OH and CO2 conversions was improved with increasing CO2 partial pressure from 20-50 kPa whilst the optimal selectivity of H2 and CO was achieved at 50 kPa.

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