Nitric acid (HNO 3 ) is a high-tonnage product of the chemical industry, which has come into widespread use in various processes of chemical technology, especially in the mineral-fertilizer industry. The annual world production of HNO 3 has reached 60 million tons [1, 2], and is tending to increase. The production of nitric acid in countries of the former USSR is approximately 17 million tons/year. With such a massive product yield, problems of the optimal design and operation of production and power plants are basic from the standpoint of operating costs and ecology; this is associated with the following specifics of this production process: • a large amount of the heat liberated in the process, including high-temperature heat (the heat of exothermal reactions with allowance for condensation and dilution of the acid amounts to 7,149 MJ/ton of HNO 3 ); and • a large amount of compressed air required for the production process (oxygen and ammonia are raw materials for the production of HNO 3 ) and post-production tail gas discharged to the environment (4.75 tons of air/ton of HNO 3 , and 3.73 tons of tail gas/ton of HNO 3 ). Let us examine a method of reducing operating costs, which utilizes the heat of the exothermal chemical reactions and which is more effective than that of classical systems employed for the production of HNO 3 . This is possible when the production process is combined with the steam-gas process used for the production of electric power and effective heat. In the classic scheme employed to produce nitric acid with a single pressure (Fig. 1), the machinery consists of a compressor, which supplies air for the catalytic oxidation of ammonia to nitric oxide (NO) and its conversion to nitrogen dioxide (NO 2 ) in an absorption column, where nitric acid HNO 3 is formed with the participation of water, and also a tail-gas expander (approximately 98% of nitrogen, 2% of oxygen, and from 50 to 100 ppm of NO x ) for driving the compressor. A condensing steam turbine, which is supplied with steam from a waste-heat boiler incorporated in a series of heat exchangers for the process-gas cooling system, serves as an additional drive of the air compressor. The temperature distribution of the tail gas in th is cycle (Fig. 2) depends on the design assumptions with respect to the distribution of heat output for the gas and steam cycles i n the power system of the plant producing the HNO 3 , i.e., above all, for the steam turbine and expander, as well as for the amount of heating and process steam output externally (so-called export). The method used to extract the NO x from the exhaust gas to support the requirements for environmental protection may exert a significant influence on the output distribution of these cycles. In modern HNO 3 production, two principal methods are basically used for the catalytic reduction of the NO x : selective ammonia (SCR), and also natural gas [3]. The chemical reactions in both methods are exothermic; moreover, the temperature rise of the exhaust gas (SCR method) is only 10°K (for an optimal temperature range of from 230 to 330°C). Reduction of the NO x by natural gas using catalysts with favorable metals provides for an increase of approximately from 200 to 300°K when
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