Optimization of operating parameters for gas-phase photocatalytic splitting of H2S by novel vermiculate packed tubular reactor

2016 ◽  
Vol 181 ◽  
pp. 674-680 ◽  
Author(s):  
V. Preethi ◽  
S. Kanmani
Keyword(s):  
Gas Phase ◽  
Tubular Reactor ◽  
Operating Parameters

scholarly journals Development of a tubular continuous flow reactor for the investigation of improved gas–solid interaction in photocatalytic CO2 reduction on TiO2

2019 ◽  
Vol 18 (2) ◽  
pp. 314-318 ◽  
Author(s):  
Martin Dilla ◽  
Ahmet E. Becerikli ◽  
Alina Jakubowski ◽  
Robert Schlögl ◽  
Simon Ristig
Keyword(s):  
Gas Phase ◽  
Continuous Flow ◽  
Flow Reactor ◽  
Tubular Reactor ◽  
Co2 Reduction ◽  
Continuous Flow Reactor ◽  
Reactor Geometry

Newly developed tubular reactor geometry allows intensive gas–solid interaction in photocatalytic gas-phase CO2 reduction.

scholarly journals Gas-Phase Photocatalytic Oxidation of Dimethylamine: The Reaction Pathway and Kinetics

2007 ◽  
Vol 2007 ◽  
pp. 1-4
Author(s):  
Anna Kachina ◽  
Sergei Preis ◽  
Juha Kallas
Keyword(s):  
Carbon Dioxide ◽  
Gas Phase ◽  
Continuous Flow ◽  
Kinetic Data ◽  
Photocatalytic Oxidation ◽  
Reaction Pathway ◽  
Tubular Reactor ◽  
Order Process ◽  
First Order ◽  
Long Run

Gas-phase photocatalytic oxidation (PCO) and thermal catalytic oxidation (TCO) of dimethylamine (DMA) on titanium dioxide was studied in a continuous flow simple tubular reactor. Volatile PCO products of DMA included ammonia, formamide, carbon dioxide, and water. Ammonia was further oxidized in minor amounts to nitrous oxide and nitrogen dioxide. Effective at 573 K, TCO resulted in the formation of ammonia, hydrogen cyanide, carbon monoxide, carbon dioxide, and water. The PCO kinetic data fit well to the monomolecular Langmuir-Hinshelwood model, whereas TCO kinetic behaviour matched the first-order process. No deactivation of the photocatalyst during the multiple long-run experiments was observed.

scholarly journals Influence of Particle Size, Reactor Temperature and Gas Phase Reactions on Fast Pyrolysis of Beech Wood

2010 ◽  
Vol 8 (1) ◽  
Author(s):  
Li Chen ◽  
Capucine Dupont ◽  
Sylvain Salvador ◽  
Guillaume Boissonnet ◽  
Daniel Schweich
Keyword(s):  
Particle Size ◽  
Gas Phase ◽  
Residence Time ◽  
Beech Wood ◽  
Tubular Reactor ◽  
Gaseous Product ◽  
Drop Tube ◽  
Gas Phase Reactions ◽  
Molar Ratios ◽  
Reactor Temperature

In the present work, a drop tube reactor (DTR) and a horizontal tubular reactor (HTR) were used to study the pyrolysis behaviour of beech wood particles of different sizes under the conditions encountered in industrial fluidized bed gasifiers, namely high external heat flux (105 – 106 W.m-2) and high temperature (800 – 1000°C). The influence of the reactor temperature (800 and 950°C), of particle size (from 350 µm to 6 mm), and of gas residence time (from 1 to 10 s) were examined. Under the explored conditions, when pyrolysis is finished, more than 80 wt.% of virgin wood is converted into gas and less than 13 wt.% remains in solid. In the gas phase, CO is the main gaseous product (50 wt.% of virgin wood), followed by H2 (molar ratios of H2/CO are between 0.35 to 0.55), H2O, CO2 and CH4. Species C2H2, C2H4, C2H6 and C6H6 are present in much lower amounts. The increase of temperature increases the rate of solid devolatilization and favours the cracking reactions of hydrocarbons. The increase of particle size increases the required time for completing pyrolysis. Meanwhile, the results obtained at 950°C show that the final products distribution at the end of pyrolysis is almost the same for the particles between 350 and 800 µm. The increase of the particle size from 800 µm to 6 mm seems to have some influence on the final products distribution. The gas phase reactions mainly change the yields of light hydrocarbons and H2: the increase of gas residence time favours the cracking reactions of hydrocarbons and thus leads to a higher H2 yield.

scholarly journals Advances in Mathematical Modeling of Gas-Phase Olefin Polymerization

Processes ◽  
2019 ◽  
Vol 7 (2) ◽  
pp. 67 ◽  
Author(s):  
Mohd Atan ◽  
Mohd Hussain ◽  
Mohammad Abbasi ◽  
Mohammad Khan ◽  
Muhamad Fazly Abdul Patah
Keyword(s):  
Mathematical Modeling ◽  
Mathematical Models ◽  
Gas Phase ◽  
Olefin Polymerization ◽  
Tubular Reactor ◽  
Fluidized Bed Reactor ◽  
Catalyst Characterization ◽  
End Products ◽  
Different Types ◽  
Plant Data

Mathematical modeling of olefin polymerization processes has advanced significantly, driven by factors such as the need for higher-quality end products and more environmentally-friendly processes. The modeling studies have had a wide scope, from reactant and catalyst characterization and polymer synthesis to model validation with plant data. This article reviews mathematical models developed for olefin polymerization processes. Coordination and free-radical mechanisms occurring in different types of reactors, such as fluidized bed reactor (FBR), horizontal-stirred-bed reactor (HSBR), vertical-stirred-bed reactor (VSBR), and tubular reactor are reviewed. A guideline for the development of mathematical models of gas-phase olefin polymerization processes is presented.

Simulation and Experimental Study on Methanol Recovery in Continuous Production of Biodiesel via Supercritical Transesterification

2012 ◽  
Vol 550-553 ◽  
pp. 452-457
Author(s):  
Wen Chen ◽  
Ya Li Jin ◽  
Shao Wen Liu ◽  
Zhou Hua Zeng
Keyword(s):  
Gas Phase ◽  
Reaction Temperature ◽  
Continuous Production ◽  
Tubular Reactor ◽  
Molar Ratio ◽  
Supercritical Methanol ◽  
Flash Evaporation ◽  
Reaction Pressure ◽  
One Stage ◽  
Operation Cost

Recycling excessive methanol is simulated and experimentalized by adiabatic flash evaporation. The simulated results show that: methanol recovery and methanol purity in gas phase for one-stage flash process are almost same with two-stage flash process and one-stage flash process is more beneficial by thinking of equipment and operation cost. The experimental results show that flash pressure has a significant influence on methanol recovery and methanol purity in gas phase which can be effectively improved when flashing pressure is reduced. Meanwhile, reaction temperature and reaction pressure also have important effects on methanol recovery and methanol purity in gas phase. For continuous producing biodiesel in supercritical methanol, when the reaction temperature, the reaction pressure and the molar ratio of methanol/oil are kept at 300°C, 15 MPa and 25:1, respectively, methanol recovery and methanol purity in gas phase can reach 90% and 98.8% respectively if the flashing pressure is kept at 0.2MPa. Therefore, the flash evaporation device coupled with tubular reactor for high purity separation of methanol is very effective which can realize comprehensive utilization of heat energy and separation and recycle of methanol.

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