Catalytic purification of tarry fuel gas

Simell, Pekka; Bredenberg, Johan B-son

doi:10.1016/0016-2361(90)90280-4

Cited by 101 publications

(51 citation statements)

References 12 publications

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“…The concept applied in the test run of this paper, illustrated in Fig. 3, is based on the invented method for avoiding the well-known soot formation problems [17,19,20] of tar reforming by using a staged reformer concept as described in [21,22]. In the pre-reformer, heavy tars and C 2 -hydrocarbons are decomposed and the gas temperature is gradually increased from the filtration temperature up to 800-850°C, which is reached by the end of the pre-reformer (T 2 in Fig.…”

Section: Methodsmentioning

confidence: 99%

Steam–oxygen gasification of forest residues and bark followed by hot gas filtration and catalytic reforming of tars: Results of an extended time test

Kurkela

Hiltunen

2016

Fuel Processing Technology

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Steam-oxygen gasification in a Circulating Fluidized-bed (CFB) reactor was developed for producing transportation fuels from different wood residues. This article presents the results of a two week test campaign, in which crushed forest residues and industrial bark mixture were used as the feedstocks. The aim of the work was to carry out extended time testing of the developed gasification and hot gas cleaning process and to determine the fate of different gas contaminants and trace components of wood. In the test runs, wood fuels were gasified in the CFB reactor at a 0.2-0.25 MPa pressure using a mixture of steam and oxygen as the gasification agent. A mixture of sand and dolomite was used as the bed material in order to maintain stable fluidization and to catalyse in-situ tar decomposition before hot filtration. Raw gas was filtered at ca. 550°C and the filtered gas was then led into a two-stage catalytic tar reformer. The gasifier performance and the concentrations of different gas contaminants were determined at four different operating variable set points during a total of 215 h of operation. The results for carbon conversion efficiency, raw gas composition and the fate of fuel nitrogen, chlorine and trace metals are presented in this paper. The concentrations of gas contaminants were determined after the ceramic filter unit and after the catalytic reformer. The conversion efficiencies for hydrocarbon gases, tars and ammonia in the reformer are also presented. The test run was carried out as a continuous operation without any interruptions or operational problems.

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Section: Methodsmentioning

confidence: 99%

Steam–oxygen gasification of forest residues and bark followed by hot gas filtration and catalytic reforming of tars: Results of an extended time test

Kurkela

Hiltunen

2016

Fuel Processing Technology

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“…The catalytic activity of this material (similar to that of dolomite) is related to its complex mixture of aluminium, oxygen and hydroxyl ions that produces both acid and base sites [24]. His porous structure increases the residence time of the tars in the bed by promoting the cracking and steam reforming reactions of the tars [25,26]. As the main innovation of this work, a set of tests with alumina were carried out using not only air but also air-steam mixtures as gasifying agents.…”

Section: Introductionmentioning

confidence: 99%

Air-steam gasification of sewage sludge in a bubbling bed reactor: Effect of alumina as a primary catalyst

Andrés

Narros

Rodríguez

2011

Fuel Processing Technology

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ARTICLE INFO ABSTRACT Keywords:Sewage sludge gasification Primary catalyst Bubbling fiuidised bed Gasifying agenteNumerous references can be found in scientific literature regarding biomass gasification. However, there are few works related to sludge gasification. A study of sewage sludge gasification process in a bubbling fiuidised bed gasifier on a laboratory scale is here reported. The aim was to find the optimum conditions for reducing the production of tars and gain more information on the influx of different operating variables in the products resulting from the gasification of this waste. The variables studied were the equivalence ratio (ER), the steambiomass ratio (SB) and temperature. Specifically, the ER was varied from 0.2 to 0.4, the SB from 0 to 1 and the temperature from 750 °C (1023 K) to850 °C (1123 K). Althoughit was observed that tar production could be considerably reduced (up to 72%) by optimising the gasification conditions, the effect of using alumina (aluminium oxide, of proven efficacy in destroying the tar produced in biomass gasification) as primary catalyst in air and air-steam mixture tests was also verified. The results show that by adding small quantities of alumina to the bed (10% by weight of fed sludge) considerable reductions in tar production can be obtained (up to 42%) improving, at the same time, the lower heating valué (LHV) of the gas and carbón conversión.

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“…To minimize fuel cost, other fuels, such as coal or biomass, could also be used for the reduction of Fe 2 O 3 to Fe 3 O 4 in these conditions. The presence of CaO and Fe 2 O 3 , which are well-known catalysts for gasification and tar cracking reactions (Simell and son Bredenberg, 1990;Asami et al, 1996;Yu et al, 2006), should lead to the rapid gasification of the solid fuels and result in high char and tar conversions in the fuel reactor calciner. However, a certain amount of carbon leakage to the air reactor and a reduction in the CO 2 capture efficiency would be unavoidable when using these fuels for the reduction of Fe 2 O 3 (Leion et al, 2008;Berguerand and Lynfelt, 2008).…”

Section: Process Descriptionmentioning

confidence: 99%