System Configurations and Costs

In the United States, in the commercial sector, the most attractive application for near-term fuel cell technology is onsite cogeneration. In this application, the fuel cell power plant is located at the site of the end user, providing both electric and thermal energy. On-site applications in the commercial 

Carbon Monoxide. Carbon monoxide, a fuel in high-temperature cells (MCFC and SOFC), is preferentially absorbed on noble metal catalysts that are used in low-temperature cells (PAFC and PEFC) in proportion to the hydrogen-to-CO partial pressure ratio. A particular level of carbon monoxide yields a stable performance loss. The coverage percentage is a function of temperature, and that is the sole difference between PEFC and PAFC. PEFC cell limits are 50 ppm into the anode major U.S. PAFC manufacturers set tolerant limits as 1.0% into the anode MCFC cell limits for CO and H20 shift to H2 and C02 in the cell as the H2 is consumed by the cell reaction due to a favorable temperature level and catalyst. 

Carbon Deposition. The processing of hydrocarbons always has the potential to form coke (soot). If the fuel processor is not properly designed or operated, coking is likely to occur. Carbon deposition not only represents a loss of carbon for the reaction but more importantly also results in deactivation of catalysts in the processor and the fuel cell, due to deposition at the active sites. 

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In addition to high-profile fuel cell applications such as automotive propulsion and distributed power generation, the use of fuel cells as auxiliary power units (APUs) for vehicles has received considerable attention (see Figure 1-9). APU applications may be an attractive market because it offers a true mass-market opportunity that does not require the challenging performance and low cost required for propulsion systems for vehicles. In this section, a discussion of the technical performance requirements for such fuel cell APUs, as well as the current status of the technology and the implications for fuel cell system configuration and cost is given. 

In the first two years, develop a baseline system configuration and cost estimate based on best available and projected technology and manufacturing practices, and assess the impact of potential technology developments on system cost reduction... 

FIGURE 19.1. Base steam system configuration and costs. 

The in-line configuration consists of deposition chambers that are separated by isolation chambers [153]. The layer sequence of a solar cell structure prescribes the actual sequence of deposition chambers. The flexibility is much less than with a cluster configuration, and costs are generally much higher, but the throughput can also be much larger. In an in-line system the substrates can move while deposition takes place, which leads to very uniformly deposited layers, as uniformity of deposition is required only in one dimension (perpendicular to the moving direction). 

In this chapter, we will introduce fundamental concepts of the membrane and membrane-separation processes, such as membrane definition, membrane classification, membrane formation, module configuration, transport mechanism, system design, and cost evaluation. Four widely used membrane separation processes in water and wastewater treatment, namely, microfiltration (MF), ultrafiltration (UF), nanofiltrafion (NF), and reverse osmosis (RO), will be discussed in detail. The issue of membrane foufing together with its solutions will be addressed. Several examples will be given to illustrate the processes. 

Selected a baseline system configuration, and initiated a detailed system cost and performance analysis... 

This section focuses in the comparison of results obtained when methods presented in section 2 are implemented to analyse uncertainty propagation in the problem of optimizing maintenance intervals of a motor-operated valve in safety equipments of a nuclear power plant. These equipments consist in two main components, actuator and valve, in serial configuration and working independently. So, the problem considers how the uncertainty associated to some initial parameters in the input vector affect on system leUability and cost (R-fC) as decision criteria. 

To achieve this goal, two existing deep mining operations were considered for the application of aramid ropes. Management at these operations has provided the project team with the actual cost and production data as well as hoisting system configurations and parameters. Based on a mix of simulations and estimates, three case studies have been completed. The first two cases refer to mine A and the third case to mine B. This paper summarizes the results obtained from these case studies. 

A modular scanner system for NDE has been developed. It consists of a selection of individual electronics and motor module components, supported by scanner configuration and control software. The modules are used as standard building blocks for construction of job specific, dedicated scanners as well and general purpose scanners. The use of modular scanner components significantly reduce the work, time and cost not only for the design and manufacture but also for establishing documentation and ensure compliance with the relevant EU-directive requirements. 

The two liter carbon canister does not exhibit the HC release during the run loss portion of the test, nor does it release more than the allowable level of HC during the three day diumals. Thus, for the given vehicle configuration and the level of purge volume obtained by the vehicle, it is clear that a two liter carbon canister is required for this vehicle to pass the EPA certification requirement. This conclusion has an effect on the cost of the evaporative control system, in that the additional activated carbon volume and canister size will have an added cost, as will any additional hardware required to mount the larger canister on the vehicle. 

The choice of whether to purchase or generate electricity and decisions on generator or cable configuration and sparing are often not obvious. An economic study evaluating capital and operating costs and system reliability of several alternatives may be required. 

This chapter has therefore shown that cost minimisation of the treatment of hypochlorite effluent streams is achieved only through consideration of a wide range of process alternatives. The optimal solution for a given plant is dependent on a number of aspects, which include not only the rate and concentration of the stream as well as its required exit concentration, but also the configuration and operational mode of the caustic scrubber and any existing treatment system. 

Treatment systems should be demonstrated to be effective, and expandable (or reducible), in a stepwise modular fashion to ensure efficient design and operation. At many sites, it is cost-effective to install several temporary treatment systems in parallel configuration, and remove them as the need is diminished until the stable rate is achieved where a single unit can handle the load. After careful analysis, it may be determined that the best procedure is to install and operate the system at the projected long-term rate from the onset. Although this plan may extend the longterm remediation time, cost savings on equipment purchase (or lease) or initial operation labor may be justified. 

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