Fuels requirements for

Od condensed from the released volatdes from the second stage is filtered and catalyticady hydrotreated at high pressure to produce a synthetic cmde od. Medium heat-content gas produced after the removal of H2S and CO2 is suitable as clean fuel. The pyrolysis gas produced, however, is insufficient to provide the fuel requirement for the total plant. Residual char, 50—60% of the feed coal, has a heating value and sulfur content about the same as feed coal, and its utilisation may thus largely dictate process utdity. 

Use of a low temperature shift converter in a PSA hydrogen plant is not needed it does, however, reduce the feed and fuel requirements for the same amount of hydrogen production. For large plants, the inclusion of a low temperature shift converter should be considered, as it increases the thermal efficiency by approximately 1% and reduces the unit cost of hydrogen production by approximately 0.70/1000 (20/1000 ft ) (140,141). 

H. Strawson and A. Lewis, Predicting Fuel Requirements for the Concorde, SAE 689734, Society of Automotive Engineers, Warrendale, Pa., Oct. 1968. 

The most logical place to begin is to size the furnaces and direct-fired heaters. Often the chemistry of the process has dictated the conditions, but frequently they can be modified in order to conserve energy usage. The burning of waste materials should also be considered as a means of both disposing of unwanted by-products and reducing fuel requirements. For each of these units, the amount of fuel needed per pound of product should be determined. 

By applying nonlinear curve fitting, we obtained the fuel requirements for the two generators explicitly in terms of MW produced. For generator 1 we have the fuel requirements for fuel oil in tons per hour (jtn)... 

The ratio of limestone to fuel required for effective desulphurisation depends upon both the mineral and sulphur content of the coal. It may be possible to burn low sulphur (<0.8%) western coal directly with 90% sulphur retention thus avoiding the necessity for flue gas desulphurisation and still meeting environmental SO2 emission regulations (18). Fluidyne (19) have indicated that a 3.65% Illinois coal with 0.3 lbs. of dolomite added per pound of coal in a fluidised bed combustor can reduce SO2 emission to less than 1.2 lbs. of SO2 per million BTU thermal output thus meeting U.S. EPA limits for large plants. 

TUo Mack-band iron ore, of the average of thirty-three per cent, of iron, will contain, fitter calcination, an average of seventy per cent, of iron. The clay-hand of thirty per cent, of metal in the ore, will, when properly calcined, contain about fifty-four per cent., so that by this meanB a great saving is effected in the amount of fuel required for the subsequent operation of smelting. 

Ayers, G.E. (1989). Fuel Required for Field Operations. Extension publication PM-709. Iowa State University, Ames, IA. 

As of the Summer of 1991, 112 cement plants were operational in the United States.2 Annual U.S. production of clinker in 1990 was approximately 81 million tons per year. Using an average of 5 MMBtu s per ton of clinker produced, some 400 x 1012 Btu s are required nationally by the industry each year. One source estimated that, theoretically, if all waste tires went to the cement industry, waste tires could provide approximately 11 percent of the fuel requirements for the cement industry.4... 

Total fuel requirements for steam generation can be assumed to be 1200 Btu, lower heating value (LHV), per pound of steam. A contingency of 20% should be applied to preliminary estimates of steam requirements. Water makeup to the boilers is usually 5 to 10% of the steam produced. 

Fuel requirements for driers are variable. They range from zero for dry cotton to as much as 450,000 Btu/bale for wet cotton. 

Table VI summarizes a typical heat balance in second stage of the above calcining system (Case A) in comparison with that of an alternative system (Case B) in which the exhaust gas from first stage kiln is not utilized for second stage calcination. The amount, composition and temperature of the exhaust gas from first stage kiln determine the auxiliary fuel requirements for second stage kiln.

Energy Saving. Reduced fuel requirements for heating the aggregate can be realized by decreasing the hot-mix temperature (estimated... 

All electrical power and fuel required for operation are calculated assuming an external supply ... 

Those constituents that release energy in the cracking process do not tippetir to obey the same rules as those that do not. Values in the published literature suggest that those compounds oxidize til i much lower fluegas enthalpy level. It should be remembered that the published flammability charts are basically a safety tool intended to,prevent explosions. Their purpose is not to define the minimum fraction of fuel required for complete combustion. 

Figure 5. Estimated annual fossil fuel requirements for electric utility generation...

Table V. Fossil Fuel Requirements for Electric Power Generation...

Fuel Requirements,— Locomotive cranes are for the most part steam operated and on account of the intermittent nature of their operation average fuel consumption is the most reliable index of power requirements. With coal of average grade, the average fuel requirements for standard sizes of locomotive cranes are ... 

The solid fuel requirement for 5 hours of operation/day is 1425 kg/vehicle/day... 

Fuel composition for 2005 is to be determined by end 1998, after Auto Oil 2. 50 ppm Sulphur level is suggested as the likely quality of fuel required for 2005 based on the current status of research development. 

External Flame Initiates Polymer Decomposition Which Produces the Fuel Required for Combustion)... 

Significant improvements in energy efficiency resulting in a 20% reduction in HP steam demand, with no support fuel requirement for the process... 

The purge gas is burned as fuel in the primary reformer furnace, reducing the total fuel requirement for the reformer. Additional hydrogen must be produced to account for the purge gas loss and this increases the feed rate and the size of the reformer furnace. Nevertheless, the overall economics of the PSA unit, due in part to more efficient heat recovery, are superior to the conventional process with the low temperature shift and methanation reactors. Also, because the PSA unit removes all of the methane and carbon oxides from the hydrogen product, the operation of the reformer is independent of hydrogen product purity and, thus, can be operated at optimum conditions [4]. 

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