Annual operating costs for the

Operating Costs Annual operating costs for the example in Table 22-18 are shown in Table 22-19. For this 0.25 mVs plant, a service factor of 90 percent is assumed. 

Calculate the annual operating costs for the existing process that needs waste treatment, and estimate how these costs would be altered by the introduction of waste-reduction options. Tabulate and compare the process and waste-treatment operating costs for both the existing and proposed waste-management options. If there are any monetary benefits (such as recycled or reused materials or wastes), then these should be subtracted from the total process or waste-treatment costs as appropriate. The expanded cost-analysis scheme discussed in Chapter 8 is appropriate to include at this point in the process. 

Table III presents a detailed summary of investment and annual operating costs for the different processes. These are Mbase cases from which the sensitivity analysis of various factors has been derived. These can be considered as representative of current costs for the purpose of process comparison.

Typical material balances and process economics are developed in this section of the paper and related to the annual operating costs for the process. A consistent set of data was used in developing the following information. 

Table V. Estimated Annual Operating Costs for the RC/Bahco CTB-100 Module (High Sulfur Flue Gas)...

The estimated annual operating cost for the 800 MW plant, assuming capital charges of 14% per year, is 1.0 mills/kW hr without any credit being taken for the by-product sulfur produced. A return of 20/long ton for the sulfur is equivalent to a credit of 0.18 mills/kW hr, reducing the operation costs to about 0.8 mills/kW hr. This compares quite well with present estimates of 0.7-1.4 mills/kW hr for low sulfur or desulfurized fuels. 

Each chlorination method provides the same disinfecting power on a pound for pound basis of available chlorine at the same pH. The choice of method depends primarily on the availability of each chemical and the construction and annual operating costs for the different systems. 

Air stripping is used to remove 90% of the toluene (molecular weight = 92) dissolved in a 10 kg/s (159 gpm) wastewater stream. The inlet composition of toluene in the wastewater is 500 ppm. Air (essentially free of toluene) is compressed to 202.6 kPa (2 atm) and bubbled through a stripper which contains sieve trays. In order to avoid fire hazards, the concentration of toluene in the air leaving the stripper is taken as 50% of the lower flammability limit (LFL) of toluene in air. The toluene-laden air exiting the stripper is fed to a condenser which recovers almost all the toluene. A schematic representation of the process is shown in Fig. 2.11. Calculate the annual operating cost and the fixed capital investment for the system. The following physical and economic data are available ... 

Since activated carbon lies to the left of the extractant and has a lower c, it will be used to remove the remaining load (0.0003 kg toluene/s, as shown by Fig. 3.19b). The flowrate of activated carbon is 0.015 kg/s. For 8000 operating hours per year, the annual operating cost of the system is 96,700/year. The annualized fixed cost can be calculated after equipment sizing (as shown in Example 2.1). 

In order to synthesize an optimal MEN for intercepting the off-gas condensate, we constnict the pinch diagram as shown in Fig. 4.9. Since the three MSA s lie completely to the left of the rich stream, they are all thermodynamically feasible. Hence, we choose the one with the least cost ( /kg NH3 removed) namely the resin. The annual operating cost for removing ammonia using the resin is ... 

In Equation (e) an average value for the heat transfer coefficient U is assumed, ignoring the effect of pressure drop. U depends on the working fluid and the operating temperature.) Let the cost per unit area of the exchanger be CA and the annualization factor for capital investment be denoted by r. Then the annualized capital cost for the boiler is... 

With respect to the objective function for a filter, the total annual cost of filtration / is assumed to be the sum of the annualized capital costs fc and the annual operating costs/0. The annualized capital cost is related to the cross-sectional area of the filter by the relation... 

We next summarize the annual operating costs of the filter because they are equal to the energy costs for pumping... 

The annual operating cost for a tin mill plant with a new waste treatment plant is more than 1,450,000, with more than 700,000 in sludge disposal costs. Lewis asserts that, in comparison, the ENVIRO-CLEAN process treatment cost includes chromium recovery valued at more than 190,000 and water savings valued at more than 50,000 per year. According to Lewis, a large-scale ENVIRO-CLEAN system complete with electrolytic recovery has an annual operating cost of less than 800,000 a year (D135035, p. 1). 

TABLE 1 Construction and Annual Operating Cost for Sites Using the ISSZT Technology"... 

The objective function represents the total annual cost which consists of (i) the investment cost for the distillation columns and heat exchangers and (ii) the operating cost for the hot and cold utilities. 

A solvent-extraction operation is carried out continuously in a plate column with gravity flow. The unit is operated 24 h/day. A feed rate of 1500 ft3/day must be handled 300 days per year. The allowable velocity per square foot of cross-sectional tower area is 40 ft3 of combined solvent and charge per hour. The annual fixed costs for the installation can be predicted from the following equation ... 

Capital Labor costs buildings, machinery and equipment, labor as per respective activity. The cost of establishing a jatropha plantation has been estimated at US 723 per ha for the first three years. Table 2 shows the estimated capital costs, and operational costs for the production of 1800 tonnes, 5400 tonnes, and 7200 tonnes of jatropha biodiesel annually. The following cost heads have been considered in the analysis that gave the figixres in the table ... 

Chapter 17 and given by Eq. (17.10). This requires estimates of the total capital cost and the annual operating cost of the columns, trays, condensers, reboilers, and reflux accumulators. To estimate these costs, equipment sizes must be determined. In this example, calculations of the height and diameter are jJlustrated for one cdiumn in one of the segnences. 

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