Capital costs for plants

Single-factor methods collect the various items of expenditure into one factor, which is usually used to multiply the total cost of delivered equipment X (Ce( )del lo give the fixed-capital cost for plant within the battery limits ... 

Direct fixed-capital cost for plant (batteiy-limit capital), Cfc)bl... 

Table 9-63 uses the data of Fig. 9-44 to compare the relative fixed-capital costs for plant constnic tion in other countries with those for the United States. The relative cost ratios were developed from data similar to those in Table 9-62. Labor ratios were corrected for the different local rates and hours per working week, job duration, and degree of mechanization available in other countries. Some of these factors are difficult to estimate, and the final total ratios give a reasonable order-of-magnitiide value for relative construction costs for equivalent plants in the countries indicated.

Application The ICIAMV process produces ammonia from hydrocarbon feedstocks. The AMV process concept offers excellent energy efficiency together with simplicity and reduced capital cost for plant capacities between 1,000 tpd and 1,750 tpd. Key features include reduced primary reformer duty, low-pressure synthesis loop and hydrogen recovery at synthesis loop pressure. 

Capital costs for plants, 186-187 Capital gains taxes, 156-157 Capital investments, 157-158 cost factors in, 166-179 estimation of 158-163, 179-193, 210 types of 157-158 Capital ratio, 191 Capital-iecovery factor, 228 Capital sink, 150-152 Capitahzed costs apphcation of 231-232 definition of 230-231 equations for, 231... 

Biodiesel Plant size (tonnes of biodiesel per annum) Jatropha plantation required (hectare) Cost of plantation establishment (USS for fust 3 years) Capital costs for Plant establishment (USS) Operational costs (USS per annum)... 

Low capital costs for plant construction could be ensured by the serial production of plant equipment fully under shop conditions, including equipment assembly and testing. Next, the pre-assembled units of limited mass will be transported to the site. 

Table 26. Plant Capital Costs for 500 Ton per Day Chlorine Production, Millions of Dollars...

In an economic comparison of these three common abatement systems, a 1991 EPA study (58) indicates extended absorption to be the most cost-effective method for NO removal, with selective reduction only matching its performance for small-capacity plants of about 200—250 t/d. Nonselective abatement systems were indicated to be the least cost-effective method of abatement. The results of any comparison depend on the cost of capital versus variable operating costs. A low capital cost for SCR is offset by the ammonia required to remove the NO. Higher tail gas NO... 

The key elements of the cost of production of phenol are feedstock cost and capital cost. For phenol produced on the U.S. Gulf Coast in a 200,000 t/yr phenol plant built in 1994, the cumene feedstock cost represents 70% of the net cost of production, after allowance for acetone coproduct value. Depreciation of equipment represents 14% of the net cost and utilities approximately 7.6%. The remaining 8.4% covers all other expenses, including plant labor, maintenance, insurance, adininistration, sales, etc. 

Because of large equipment and land requirements, capital costs for wastewater-treatment plants are high. A collection system that conveys both sanitary and storm flows must be designed to deal with high peak flows at the treatment plant detention basins are usually provided in order to smooth the flow into the plant and reduce the sudden peak flow. In the absence of such precautions, it may be necessary to by-pass a portion of the flow. 

Equipment and Economics A veiy large electrodialysis plant would produce 500 /s of desalted water. A rather typical plant was built in 1993 to process 4700 mVday (54.4 /s). Capital costs for this plant, running on low-salinity brackish feed were 1,210,000 for all the process equipment, including pumps, membranes, instrumentation, and so on. Building and site preparation cost an additional 600,000. The building footprint is 300 itt. For plants above a threshold level of about 40 m Vday, process-equipment costs usually scale at around the 0.7 power, not too different from other process eqiiip-ment. On this basis, process equipment (excluding the ouilding) for a 2000 mVday plant would have a 1993 predicted cost of 665,000. 

During 1990-1995, capital costs for large UF/MF plants broke down into the ranges shown in Table 22-21. 

While comparison of the absolute capital costs and costs of electricity among different power systems is difficult and uncertain, the structure of these costs is rather typical, and the costs of component units are usually within known ranges. For an oxygen-blown IGCC power system, the breakdown of the capital cost for the four component units is air separation plant (11 to 17 percent), fuel gas plant (33 to 42 percent), combined-cycle unit (32 to 39 percent), and balance of plant (2 to 21 percent). The breakdown of the cost of elec tricity is capital charge (52 to 56 percent), operating and maintenance (14 to 17 percent), and fuel (28 to 32 percent). 

It is most economical when high-grade ores are used, becoming less economical with poorer feed materials containing iron, because of the production of chloride wastes from which the chlorine cannot be recovered. By contrast the sulfate process cannot make use of rutile which does not dissolve in sulfuric acid, but is able to operate on lower grade ores. However, the capital cost of plant for the sulfate process is higher, and disposal of waste has proved environmentally more difficult, so that most new plant is designed for the chloride process. 

Thermal power plant is more commonly associated with very large central power stations. The capital cost for thermal power plant, in terms of cost per installed kilowatt of electrical generating capacity, rises sharply for outputs of less than some 15 MW. It is for this reason that thermal power plant is not usually considered for industrial applications unless it is the combined cycle or combined heat and power modes. However, for cases where the fuel is of very low cost (for example, a waste product from a process such as wood waste), then the thermal power plant, depending on output, can offer an excellent choice, as its higher initial capital cost can be offset against lower running costs. This section introduces the thermal power cycle for electrical generation only. 

Dr. Blum Our office in New York has done several economic analyses. The distinct advantage of liquid-phase methanation, other than the fact it does not have recycle cost, is that it requires only about 60% of the capital cost. For a commercial plant of 250 billion Btu per day, the capital cost is projected at about 18,000,000. Since the operating costs depend very substantially on the capital costs, there is a very big reduction in operating costs. We project at the moment an advantage in the order of four to six cents per million Btu over cold gas and hot gas recycle. 

It is well established that sulfur compounds even in low parts per million concentrations in fuel gas are detrimental to MCFCs. The principal sulfur compound that has an adverse effect on cell performance is H2S. A nickel anode at anodic potentials reacts with H2S to form nickel sulfide. Chemisorption on Ni surfaces occurs, which can block active electrochemical sites. The tolerance of MCFCs to sulfur compounds is strongly dependent on temperature, pressure, gas composition, cell components, and system operation (i.e., recycle, venting, and gas cleanup). Nickel anode at anodic potentials reacts with H2S to form nickel sulfide. Moreover, oxidation of H2S in a combustion reaction, when recycling system is used, causes subsequent reaction with carbonate ions in the electrolyte [1]. Some researchers have tried to overcome this problem with additional device such as sulfur removal reactor. If the anode itself has a high tolerance to sulfur, the additional device is not required, hence, cutting the capital cost for MCFC plant. To enhance the anode performance on sulfur tolerance, ceria coating on anode is proposed. The main reason is that ceria can react with H2S [2,3] to protect Ni anode. 

Estimate the capital cost for the nitric acid plant shown in Figure 4.2, Chapter 4. 

Table 9-4 gives the capital costs for six ammonia plants that were built between 1959 and 1969. When plant no. 5 is compared with the three other plants that have a capacity of 1,000 tons/day, it appears that its reported cost is in error. This could be a misprint, or the plant might be producing urea, nitric acid, and/or ammonium nitrate as well as ammonia. The reader must always be careful, since errors occur frequently in printed material. This is why care should be used when the cost of a plant is estimated from only one piece of information. 

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