Performance of dual-reactor system for conversion of syngas to aromatic-containing hydrocarbons

Varma, R. L.; Bakhshi, Narendra N.; Mathews, J. F.; Ng, Samson

doi:10.1021/ie00062a001

Cited by 38 publications

(24 citation statements)

References 6 publications

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“…Contrarily, Freitez et al (2011) reported a decrease in cracking activity with a ZSM-5 temperature increase. In addition, the observed effect of maximum selectivity of aromatics at 573 K is in agreement with the results obtained by Varma et al (1985), Varma and Bakhshi (1987), and Karre et al (2013), who also reported an increase of aromatization reactions with a HZSM-5 temperature increase up to 573 K. A negative effect of a HZSM-5 temperature increase was also observed for the selectivity toward CH 4 and C 2 , which increased up to 10.8% and 1.1%, correspondingly. Figure 1 shows the effect of HZSM-5 temperature on the individual product selectivities of DB reaction, C 3 -C 4 paraffins ( Figure 1a) and aromatics ( Figure 1b).…”

Section: Resultssupporting

confidence: 91%

“…The number of studies investigating the combination of FTS and HP in a single reactor is fairly limited. In most, the catalysts' bed configurations evaluated include (a) physical mixture configuration (Martinez et al, 2007;Subiranas, 2009), (b) impregnation of the FT catalyst on the zeolite (Sartipi et al, 2013), (c) coating of the FT catalyst by zeolite (Sartipi et al, 2013), and (d) dual bed (DB) configuration (Varma and Bakhshi, 1987;Gormley et al, 1988;Botes and Böhringer, 2004;Subiranas, 2009;Freitez et al, 2011;Karre et al, 2012;Pabst et al, 2013). The advantages of the DB configuration are (a) operation of FT and HP catalysts at their optimal operation conditions (Asami et al, 2005); (b) no alteration in the activity of the FT catalyst (Karre et al, 2012); and (c) increase in the yield of LPG and aromatics Bakhshi, 1987, Botes andBöhringer, 2004;Cho et al, 2008;Freitez et al, 2011).…”

Section: Introductionmentioning

confidence: 99%

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Conversion of Syngas to LPG and Aromatics Over Commercial Fischer-Tropsch Catalyst and HZSM-5 in a Dual Bed Reactor

Corsaro

Wiltowski

Juchelková

et al. 2014

Petroleum Science and Technology

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The commercial Co-based Fischer-Tropsch catalyst and HZSM-5 were tested in a single reactor process. FT catalyst was evaluated at 463 K, whereas HZSM-5 was evaluated at various temperatures (523, 573, and 623 K). The effect of syngas flow rate, HZSM-5 temperature and loading on liquefied petroleum gas (LPG) and aromatics selectivities were investigated. HZSM-5 addition suppressed the formation of CO 2 and CH 4 , and remarkably enhanced the simultaneous formation of LPG and aromatics. The optimal operating conditions were identified as: T HZM-5 = 623 K, HZSM-5 loading = 2.5 g, and GHSV = 4.8 L syngas /(g cat h).

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Section: Resultssupporting

confidence: 91%

Section: Introductionmentioning

confidence: 99%

Conversion of Syngas to LPG and Aromatics Over Commercial Fischer-Tropsch Catalyst and HZSM-5 in a Dual Bed Reactor

Corsaro

Wiltowski

Juchelková

et al. 2014

Petroleum Science and Technology

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“…83,85 Therefore, the future production of large-volume products such as benzene, toluene, and xylene (BTX) should preferentially be done by further development of catalyst systems able to convert syngas into specific aromatic hydrocarbons. 89,90 Here, black liquor gasification as well as gasification using green biomass are renewable alternatives to the use of coal.…”

Section: Other Aromaticsmentioning

confidence: 99%

Lignin Recovery and Lignin-Based Products

Gellerstedt¹,

Tomani²,

Axegård³

et al. 2012

Integrated Forest Biorefineries

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Lignin is present in the tissue of vascular plants where it adds to the mechanical strength and structural integrity of the cell wall. Furthermore, its structure, being much more hydrophobic than that of polysaccharides, provides the necessary balance in water transport and swelling ability of the cell. In wood species, only small differences in the lignin content between stem, roots, branches, and tops can be observed. Softwoods such as spruce, pine or hemlock have a lignin content of the order of 25-30% by weight whereas hardwoods usually have lower amounts; 20-25%. 1 In Table 8.1, the chemical composition of some wood species is given.Various annual plants have even lower amounts and e.g. flax only contains around 3% of lignin as an average amount albeit with large differences between different parts of the plant. 2 Although annual plants can contain higher amounts of lignin (up to ca 15%), the normally encountered large differences in RSC Green Chemistry No. 18 Integrated Forest Biorefineries Edited by Lew Christopher

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“…This approach has been studied for the conversion of wax-containing LTFT products by a number of groups. [74][75][76][77] In these investigations, FTS and co-conversion are not fully segregated. Depending on the level of integration between the two steps (similar operating window or not), it can arguably no longer be considered as co-catalysis during FTS.…”

Section: Co-catalysts For Wax Conversion During Ftsmentioning

confidence: 96%

Upgrading of Fischer–Tropsch Waxes

2010

Catalysis in the Refining of Fischer-Tropsch Syncrude

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The distributions of hydrocarbon fractions from low-temperature FischerTropsch (LTFT) synthesis and high-temperature Fischer-Tropsch (HTFT) synthesis are shown in Table 1.1. The significantly higher yield of 4360 1C boiling (C 22 and heavier) products from LTFT synthesis is evident. In LTFT syncrude, this fraction is called the wax product and it contains mainly alkanes (95%), smaller amounts of alkenes and oxygenates and neither sulfur nor much aromatics. 1 The equivalent 4360 1C boiling fraction found in HTFT syncrude is termed a residue. The HTFT residue is in fact very aromatic (425%) and cannot be classified as a paraffin wax, although it is sometimes referred to as a waxy oil. 2 Wax upgrading therefore deals only with primary hydrocarbons from LTFT synthesis.The average ratio of condensates to wax from the iron-based slurry bed LTFT synthesis is 38:62. The n-alkanes in the condensates and the n-alkanerich waxes can be used as feed for the production of fuels, lubricants and chemicals. 3 In each instance, the objective and upgrading methodology are determined by the specifications of the commercial products being produced. Figure 6.1 shows the carbon number distribution of the condensate and wax from iron-based slurry LTFT synthesis. 4 The wax fraction includes alkanes with carbon numbers exceeding C 100 , peaking around C 30 . It is evident from Figure 6.1 that for LTFT condensates, the carbon number distribution peaked at about C 20 and that there is considerable overlap of the C 15 -C 35 fraction between condensate and wax. This is a consequence of the separation strategy after FTS (Section 4.2.1) and better separation can be achieved by appropriate design.Generally, iron-based tubular fixed bed reactor products contain less alkenes than iron-based slurry bubble column reactor products. The products from fixed bed conversion are also more linear and contain less oxygenates, specifically alcohols and carbonyls. This can be understood from reactor engineering RSC Catalysis Series No. 4 Catalysis in the Refining of Fischer-Tropsch Syncrude

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Performance of dual-reactor system for conversion of syngas to aromatic-containing hydrocarbons

Cited by 38 publications

References 6 publications

Conversion of Syngas to LPG and Aromatics Over Commercial Fischer-Tropsch Catalyst and HZSM-5 in a Dual Bed Reactor

Conversion of Syngas to LPG and Aromatics Over Commercial Fischer-Tropsch Catalyst and HZSM-5 in a Dual Bed Reactor

Lignin Recovery and Lignin-Based Products

Upgrading of Fischer–Tropsch Waxes

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