Fuel autothermal gasoline

For a methane steam reforming fuel processor, more than 15% higher fuel processor efficiency was determined experimentally by Mathiak et al. [433] when utilising fuel cell anode off-gas compared with combustion of additional methane. Doss et al. analysed an autothermal gasoline fuel processor and found improved efficiency by utilisation of anode off-gas [434]. 

Figure 5.59 Dynamic simulation of the start-up fuel processor (33 kWth) S/C = 0 O/C = 0.94 behaviour of an autothermal gasoline reformer 60 Lmin air addition to the water-gas shift coupled to a heat-exchanger for feed pre-heating reactor. Right gas composition downstream of and a water-gas shift reactor both reactors were the autothermal reformer (ATR) and the high pre-heated for 5 s with 2.5-kWei energy. Left temperature water-gas shift reactor (HTS)...

Present formula gasolines contain approximately 300 ppm. No. 2 fuel oil contains 2,200 to 2,600 ppm by weight of sulfur. Even pipeline gas contains sulfur-containing odorants (mercaptans, disulfides, or commercial odorants) for leak detection. Metal catalysts in the fuel reformer can be susceptible to sulfur poisoning and it is very important that sulfur in the fuel reformate be removed. Some researchers have advised limiting the sulfur content of the fuel in a stream reformer to less than 0.1 ppm, but noted the limit may be higher in an autothermal... 

A compact design for a gasoline fuel processor for auxiliary power unit (APU) applications, including an autothermal reformer followed by WGS and selective oxidation stages, was reported by Severin et al. [83]. The overall fuel processor efficiency was about 77% with a start-up time of 30 min. 

A stand-alone IkW integrated fuel processor for gasoline, incorporating an autothermal reformer followed by high- and low-temperature WGS reactors, was reported by Qi et al. [85]. The start-up of the ATR reformer lasted less than 5 min and stabilized in around 50 min for the whole system. 

Table 6) indicate that the fuel-processing efficiencies decrease in the order of steam reforming > autothermal reforming > partial oxidation for both gasoline and diesel fuels. 

Schwank, )., Tadd, A., Gould, B., Autothermal reforming of simulated gasoline in compact fuel processor,... 

Autothermal reformers and CPO are being developed by a number of groups, mostly for fuel processors of gasoline, diesel, and JP-8 fuels and for natural gas-fueled proton exchange membrane fuel cell (PEMFC) cogeneration systems. A few examples are the following ... 

Autothermal Reforming of New Gasoline for Fuel Cell Applieations, J. P. Kopasz, M.A. Pacheco, S. Ahmed, X. Wang, M.A. Marquez, presented at the... 

Figure 1 shows the system schematic for a gasoline reformer/fuel cell system. The drawing applies to both the 0.7 V/cell and 0.6 V/cell systems, which only differ dimensionally. In these systems, California reformulated gasoline is pumped from the fuel tank and injected into the integrated autothermal... 

Kaila RK, Krause AOI (2006) Autothermal refraining of simulated gasoline and diesel fuels. 

It is under development for various fuels such as methanol, ethanol, LPG and gasoline. The complete fuel processor was composed of a catalytic autothermal reformer reactor, a heat exchanger for cooling the reformate downstream of the CAR,... 

A design study for a gasoline fuel processor/fuel cell system was presented by King and O day [616]. It consisted of an autothermal reformer, sulfur removal, water-gas shift and two stage preferential oxidation. The system pressure was close to ambient to reduce parasitic power losses of the compressor (Figure 9.39). 

Qi et al. presented a 1-kW breadboard gasoline fuel processor [451]. The device consisted of a concentric reactor arrangement, similar to the design developed by Ahmed et al. [448], see Section 5.4.5. The overall dimensions were very low, a diameter of 150 mm and length 150 mm were reported by these workers [451]. The preferential oxidation reactor was a separate device, but the autothermal fixed bed reformer was positioned in the centre of the fuel processor and surrounded by annular high and low temperature water-gas shift fixed bed reactors, as shown in Figure 9.40. The feed... 

The start-up time demand was demonstrated to be kept below 4 min, which was impressive, for the second generation fuel processor, as shown in Figure 9.51 [620]. The start-up procedure was described. Gasoline was fed to the autothermal reformer at 7 kWth for 1.5 min. Then the gasoline flow was increased to 30kWth- The carbon... 

Meyer et cd. described the development of a multi-fuel processor by International Fuel Cells, LLC [627]. Methanol and gasohne (quality California reformulated gasoline grade II) were the major fuel alternatives. The technology chosen consisted of feed desulfurisation, autothermal reforming and catalytic carbon monoxide removal by two water-gas shift stages and two preferential oxidation reactors. The system had a power equivalent of 50 kW. However, performance data were only provided with respect to the autothermal reformer Desulfurisation proved to increase the reformer conversion up to 98%. No residual heavy hydrocarbons then remained in the product. The hot spot of the autothermal reformer approached 1000 °C. 

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