Catalytic steam reforming of tar for enhancing hydrogen production from biomass gasification: a review

doi:10.1007/s11708-020-0800-2

Front. Energy

2020, Vol. 14

Issue (3) : 545-569 https://doi.org/10.1007/s11708-020-0800-2

REVIEW ARTICLE

Catalytic steam reforming of tar for enhancing hydrogen production from biomass gasification: a review

Ru Shien TAN¹, Tuan Amran TUAN ABDULLAH¹(

), Anwar JOHARI¹, Khairuddin MD ISA²

¹. Centre of Hydrogen Energy, Institute of Future Energy; School of Chemical and Energy Engineering, Faculty of Engineering, Universiti Teknologi Malaysia, 81310 Skudai, Johor, Malaysia
². School of Environmental Engineering, Universiti Malaysia Perlis, Kompleks Pusat Pengajian Jejawi 3, 02600 Arau, Perlis, Malaysia

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Abstract

Presently, the global search for alternative renewable energy sources is rising due to the depletion of fossil fuel and rising greenhouse gas (GHG) emissions. Among alternatives, hydrogen (H₂) produced from biomass gasification is considered a green energy sector, due to its environmentally friendly, sustainable, and renewable characteristics. However, tar formation along with syngas is a severe impediment to biomass conversion efficiency, which results in process-related problems. Typically, tar consists of various hydrocarbons (HCs), which are also sources for syngas. Hence, catalytic steam reforming is an effective technique to address tar formation and improve H₂ production from biomass gasification. Of the various classes in existence, supported metal catalysts are considered the most promising. This paper focuses on the current researching status, prospects, and challenges of steam reforming of gasified biomass tar. Besides, it includes recent developments in tar compositional analysis, supported metal catalysts, along with the reactions and process conditions for catalytic steam reforming. Moreover, it discusses alternatives such as dry and autothermal reforming of tar.

Keywords hydrogen biomass gasification tar steam reforming catalyst

Corresponding Author(s): Tuan Amran TUAN ABDULLAH

Online First Date: 24 March 2020 Issue Date: 14 September 2020

Cite this article:

Ru Shien TAN,Tuan Amran TUAN ABDULLAH,Anwar JOHARI, et al. Catalytic steam reforming of tar for enhancing hydrogen production from biomass gasification: a review[J]. Front. Energy, 2020, 14(3): 545-569.

URL:

https://academic.hep.com.cn/fie/EN/10.1007/s11708-020-0800-2
https://academic.hep.com.cn/fie/EN/Y2020/V14/I3/545

Fig.1 Comparison between (a) fuel cell vehicle and (b) conventional vehicle.

Fig.2 A possible route of biomass gasification and proposed technique for improvement of syngas production.

Fig.3 Composition of gasified biomass tar derived from various biomass feedstock.

Tab.1 Tar classification based on molecular weight [⁵³]

Reaction	$Δ H 2980$ /(kJ·mol⁻¹)	Refs.
Steam reforming of hydrocarbon (1) $C x H y + x H 2 O \hscale 50%? (x + 12 y) H 2 + CO$ Steam reforming of oxygenated hydrocarbon (2) $C x H y O z + (x − z) H 2 O \hscale 50%? (x + 12 y − z) H 2 + x CO$	>0 >0	[²⁴,⁶⁹] [²⁴,⁶⁹]
Water-gas shift (3) $CO + H 2 O \hscale 50%? CO 2 + H 2$	−41	[⁷²,⁷³]
Dry reforming (4) $C x O y + x CO 2 \hscale 50%? 12 y H 2 + 2 x CO$	>0	[⁴⁸,⁷⁴]
Hydrodealkylation (5) $C x H y + H 2 → C x − 1 H y − 2 + CH 4$	<0	[⁷⁴,⁷⁵]
Methane steam reforming (6) $CH 4 + H 2 O ? (g) \hscale 50%? CO + 3 H 2$	206.9	[⁷⁴,⁷⁵]
Carbon formation (7) $C x H y → x C + 12 y H 2$	<0	[⁷⁰,⁷¹]
Boudouard reaction (8) $C + CO 2 \hscale 50%? 2 CO$	172	[⁷⁰,⁷²]
Carbon gasification (9) $C + H 2 O \hscale 50%? CO + H 2$	131	[⁷⁰,⁷¹]

Tab.2 Possible reactions involved in gasified biomass tar steam reforming process

Fig.4 Possible reaction pathways for steam reforming of tar.

Active metals	Supports	Preparation methods	Tar model compound	Operating conditions	Catalytic performance/%	Remarks	Ref.
Ni (10% (wt.))	Activated char	Impregnation	Toluene, naphthalene	T = 800°C, S/C= 2, GHSV= 8000 h⁻¹	Tar conv. = 92–100, H₂ comp. = 66–67	Structural damage and surface area deterioration were observed on spent catalyst	[⁴¹]
Ni (10% (wt.))	Al₂O₃, MgO, CaO	–	Toluene, phenol, naphthalene, pyrene	T = 450°C, S/C= 5, GHSV= 1900 h⁻¹	Tar conv. = 80–100, H₂ yield= 2–13	Ni/Al₂O₃ and Ni/CaO had an unstable behavior in H₂ yield	[⁷⁹]
Ni (20% (wt.))	Al₂O₃	Impregnation	Phenol, toluene, Furfural, methyl naphthalene, ndene, anisole	T = 750°C, S/C= 3	C conv. = 90, H₂ yield= 14.3	H₂ yield is much lower than the potential H₂ yield (63%) calculated from stoichiometry; O₂ contributed the largest constitute of reformate followed by CO and H₂	[²⁴]
Cu (1% (wt.))	Calcined scallop shell	Incipient wetness impregnation	Tar derived from cedar wood gasification	T = 700°C, Catalyst= 2 g, Water= 0.09 mL/min	H₂ yield= 60 mmol/g_carbon	Existence of Ca(OH)₂ on catalyst improved the basicity of catalyst and anti-coking ability	[⁸⁴]
Ru (1% (wt.))	12SrO-7Al₂O₃	Physical mixing, impregnation	Toluene	T = 600°C, S/C= 2, W/F = 7 g h/mol	Tar conv. = 80	Ru(PPh₃)₃Cl₂ recognized as a better Ru precursor for a high catalytic activity as compared with RuCl₃nH₂O	[⁸⁷]
Pt (1.5% (wt.))	Al₂O₃, CeO₂/Al₂O₃	Incipient wetness impregnation	Toluene	T = 700°C, Steam/toluene= 40	Tar conv. = 80–95, H₂ comp. = 65–68, H₂/CO= 6.5–8.5	Doping of CeO₂ decreased the selectivity to CO but increased the selectivity to CO₂; Pt/CeO₂/Al₂O₃ produced a higher H₂/CO	[⁴⁴]
Ba/Ni, Sr/Ni, Ca/Ni (2.28+ 5% (wt.))	LaAlO₃	Pechini method /Impregnation	Toluene	T = 600°C, S/C= 2, WHSV= 27.1 h⁻¹	C conv. = 28–44, H₂ yield= 26–41	Toluene conversion and H₂ yields increased drastically by the addition of alkaline-earth metals	[⁹⁷]
Ni/Ru-Mn (16+ 0.6+ 2.6% (wt.))	α-Al₂O₃	Incipient wetness impregnation	Toluene	T = 600°C, S/C= 25, GHSV= 10000 h⁻¹	C conv. = 100, H₂ comp. = 68.1	Formation of filamentous carbon which leads to reactor clogging and pressure drop was observed on spent catalyst surface	[⁴⁵]
Fe (10 wt.%) Fe-Ni (5+ 5 wt.%)	Olivine	Thermal fusion	Toluene	T = 850°C, S/C= 0.93, WHSV= 0.88 h⁻¹	Tar conv. = 98, H₂ yield= 88-98	Tendency of carbon formation of Fe/olivine was slightly higher than Fe-Ni/olivine	[⁴²]
Pt/Ni (0.85+ 5 wt.%)	La_0.7Sr_0.3AlO_3−δ	Pechini method/Impregnation	Toluene	T = 600°C, S/C= 8.9, GHSV= 12000 h⁻¹	C conv. = 59.1, H₂ yield= 52.7	Pt/Ni was the best impregnation order lead to a high H₂ yield and a high tolerance to coking	[¹¹¹]
Ni, Co (10 wt.%) Ni/Co (5+ 5 wt.%)	ZrO₂	Impregnation	Phenol	T = 600°C, S/C= 9, WHSV= 115.56 h⁻¹	Tar conv. = 33–53, H₂ yield= 24–51	Bimetallic catalyst exhibited better catalytic activity than monometallic catalysts	[¹¹⁷]
Ni (20 wt.%)	Lignite char, Al₂O₃	Ion exchange	Toluene	T = 650°C, S/C= 2	H₂ yield= 512–1125 mmol/g-Ni	Lignite char is readily gasified and not suitable service as catalyst support for steam reforming	[¹²⁰]
Ni (10 wt.%)	Activated carbon, olivine, Al₂O₃	Incipient wetness impregnation	Toluene	T = 600°C, S/C= 2, LHSV= 0.87 h⁻¹	C conv. = 18–100	The large surface area and microporous structure of activated carbon support contributed to a fine Ni particle distribution and consequently lead to a high catalytic activity	[¹²²]
LaNi_0.5Mn_0.5O₃		Pechini method	Toluene	T = 700°C, S/C= 3, HSV= 20000 h⁻¹	Tar conv. = 100, H₂ comp. = 42	Catalyst required high reduction temperature (up to 1000°C)	[¹³³]
V (3 wt.%)	Mg/Al	Co-precipitation /Impregnation	Toluene	T = 500°C, S/C= 2, WHSV= 16.6 h⁻¹	C conv. = 77.5, H₂ comp. = 57	A higher V content presented a better activity in toluene conversion while a lower V content produced a higher H₂ composition of reformate	[¹³⁸]

Tab.3 Summary of catalytic gasified biomass tar steam reforming processes

Tab.4 Comparison of perovskite and hydrotalcite catalysts with conventional supported catalysts

Tab.5 Favored temperature for H₂ production in steam reforming of gasified biomass tar

Tab.6 Favored S/C ratio for H₂ production in the steam reforming of gasified biomass tar

Tab.7 Favored space velocity or space time for H₂ production in steam reforming of gasified biomass tar

Fig.5 Mechanism of coke suppression by CeO₂ support.

Fig.6 SEM images of (a) fresh NiO/ceramic catalyst (adapted with permission from Ref. ¹⁵⁷]); (b) amorphous coked NiO/ceramic catalyst (adapted with permission from Ref.[¹⁵⁷]); (c) filamentous coked Ni/α-Al₂O₃ catalyst (adapted with permission from Ref. [¹²¹]).

Fig.7 TPO profiles of spent Ni/Al₂O₃ and Fe-Ni/Al₂O₃ catalysts after steam reforming of toluene (adapted with permission from Ref. [¹⁰²]).

Fig.8 Activity of LaNiO₃ catalyst. Reaction condition: S/C 3.9; catalyst 0.03 g; temperature 650°C; He 120 mL/min (adpated with permission from Ref. [¹³⁵]).

Fig.9 Schematic diagram.

Fig.10 Steam reforming of toluene in BBCN hollow fiber membrane reactor (adapted with permission from Ref. [²⁰²]).

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