Coke study on MgO-promoted Ni/Al2O3 catalyst in combined H2O and CO2 reforming of methane for gas to liquid (GTL) process

Koo, Kee Young; Roh, Hyun Seog; Seo, Yutaek; Seo, Dong Joo; Yoon, Wang Lai; Park, Seung Bin

doi:10.1016/j.apcata.2008.02.009

Cited by 278 publications

(78 citation statements)

References 49 publications

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“…Besides the comparing catalyst efficiency and other economic issues related to process operating costs, H 2 to CO ratio is another important parameter to study. For cobalt-catalysts H 2 to CO ratio is suppose to be around 1.8-2.1, while for iron catalysts H 2 to CO ratio is way below 1 as a favor for water gas shift reaction (Koo, et al, 2008a;Steynberg, et al, 1999). Iron catalysts are better suited to use with coal derived synthesis gas because cobalt catalysts are more expensive and it is difficult to prevent coal derived catalyst poisons.…”

Section: Fischer-tropsch Synthesismentioning

confidence: 99%

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Simulation, integration, and economic analysis of gas-to-liquid processes

Bao

El‐Halwagi

Elbashir

2010

Fuel Processing Technology

158

103

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Simulation, Integration, and Economic Analysis of Gas-to-Liquid Processes. (December 2008) Buping Bao, B.S., Zhejiang University Chair of Advisory Committee: Dr. Mahmoud M. El-Halwagi Gas-to-liquid (GTL) process involves the chemical conversion of natural gas (or other gas sources) into synthetic crude that can be upgraded and separated into different useful hydrocarbon fractions including liquid transportation fuels. A leading GTL technology is the Fischer Tropsch process. The objective of this work is to provide a techno-economic analysis of the GTL process and to identify optimization and integration opportunities for cost saving and reduction of energy usage and environmental impact. First, a basecase flowsheet is synthesized to include the key processing steps of the plant. Then, computer-aided process simulation is carried out to determine the key mass and energy flows, performance criteria, and equipment specifications. Next, energy and mass integration studies are performed to address the following items: (a) heating and cooling utilities, (b) combined heat and power (process cogeneration), (c) management of process water, (c) optimization of tail-gas allocation, and (d) recovery of catalystsupporting hydrocarbon solvents. Finally, an economic analysis is undertaken to determine the plant capacity needed to achieve the break-even point and to estimate the return on investment for the base-case study. After integration, 884 million $/yr is saved from heat integration, 246 million $/yr from heat cogeneration, and 22 million $/yr from water management. Based on 128,000 barrels per day (BPD) of products, at least 68,000 BPD capacity is needed to keep the process profitable, with the return on investment (ROI) of 5.1%. Compared to 8 $/1000 SCF natural gas, 5 $/1000 SCF price can increase the ROI to 16.2%.

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Section: Fischer-tropsch Synthesismentioning

confidence: 99%

“…Koo (Koo, et al, 2008a;Koo, et al, 2008b) listed the criteria for choosing F-T catalyst considering the molecular adsorption and formation effect to overcome the disadvantages listed above. They also introduce an effective and stable nano sized catalyst for the F-T reaction.…”

Section: F-t Catalystsmentioning

confidence: 99%

Simulation, integration, and economic analysis of gas-to-liquid processes

Bao

El‐Halwagi

Elbashir

2010

Fuel Processing Technology

158

103

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“…Besides these peaks, there are small diffraction bands at 43.8°, 52.8°and 63.2°o bserved, which correspond to the diffraction of planes of 011, 200 and 220 of nickel crystal. Meanwhile, a small sharp diffraction peak at 27.6°is seen, which can be assigned to the deposited carbon [36,37]. This suggests that there is carbon formed during the CO hydrogenation although the catalyst is still active.…”

Section: Resultsmentioning

confidence: 81%

Highly active and selective catalyst for synthetic natural gas (SNG) production

Huang¹,

Chen²,

et al. 2014

Appl Petrochem Res

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A novel nickel-based methanation catalyst has been prepared and tested for CO and CO 2 hydrogenation to synthetic natural gas under various conditions. The catalysts before and after reaction have been characterized using XRD, Laser Raman and IR spectroscopes. It is showed that the novel catalyst can give high methane selectivity and yield at a very broad ranges of temperature and H 2 /CO ratios, although the selectivity to methane increase with the H 2 /CO ratio, which, however, increases with the temperature rising from 200 to 350°C, then gradually decrease. The characterization results showed that the there is surface carbons forming over the catalyst surface, and the nickel crystalline structure changes during the reaction. Despite this, the catalyst still gives the same performance, which suggested that the catalyst can operate in a very broad range conditions.

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“…After reaction, these Figure 7 shows the XRD diffraction patterns of all spent catalysts. The diffraction peaks at approximately 2θ = 27° in samples PG and NF/PG belong to the carbon with graphitic structure on these catalysts (Koo et al 2008;Therdthianwong et al 2008). The peaks disappeared after the addition of CeO2, which was ascribed to the interaction between CeO2 and PG, promoting the migration of oxygen ions from the interior of CeO2 to its surface, leading to the gasification of carbon deposition.…”

Section: Characterizations Of Spent Catalystsmentioning

confidence: 99%

Hydrogen Production from Steam Reforming of Acetic Acid over Ni-Fe/Palygorskite Modified with Cerium

Wang¹,

Chen²,

Yang³

et al. 2017

BioResources

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The steam reforming of acetic acid (SRA) was carried out in a fixed-bed tubular reactor with Ni-Fe/ceria-palygorskite (CPG) catalysts. The asprepared catalysts were analyzed by N2 adsorption-desorption, scanning electron microscopy coupled with energy dispersive spectroscopy (SEM-EDS), H2 temperature programmed reduction (H2-TPR), and X-ray diffraction (XRD). The results of H2-TPR and XRD showed that the addition of CeO2 increased the hydrogen consumption of catalysts and the interaction force between active component (Ni-Fe alloy) and carrier. Moreover, the Ni-Fe alloys were successfully synthesized in the Ni-Fe/CPG catalysts and their crystallite sizes were decreased by adding CeO2. In addition, these catalysts were employed to SRA at 600 °C, GHSV = 14427 h -1 and different molar ratio of S/C. The experimental results revealed that the Ni-Fe/C0.4PG0.6 catalyst can achieve the highest yield of H2 (87%) and HOAc conversion (95%), as well as the highest stability during the process of steam SRA. Additionally, the spent catalysts were characterized by XRD, SEM, and thermogravimetric analysis (TGA). The results showed that the addition of CeO2 enhanced the stability and activity of Ni-Fe/palygorskite catalyst and reduced the coke deposition rate on the catalyst surface.

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Coke study on MgO-promoted Ni/Al2O3 catalyst in combined H2O and CO2 reforming of methane for gas to liquid (GTL) process

Cited by 278 publications

References 49 publications

Simulation, integration, and economic analysis of gas-to-liquid processes

Simulation, integration, and economic analysis of gas-to-liquid processes

Highly active and selective catalyst for synthetic natural gas (SNG) production

Hydrogen Production from Steam Reforming of Acetic Acid over Ni-Fe/Palygorskite Modified with Cerium

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