Method of intensification of the installation for production of nitric acid
 Method of removing nox and n2o from nitric acid production residual gas / 2259227Invention aims at reducing concentration of NOx and N2O in residual gas and provides a method wherein residual gas escaping absorption column, prior to enter turbine, is passed through two consecutive steps first reducing NOx content by catalytic reduction and then reducing N2O content by decomposing it into nitrogen and oxygen on catalyst containing one or more iron-loaded zeolites at working pressure 4-12 bar. Molar ratio NOx/N2O in residual gas before second step lies within a range of 0.001 to 0.5. |
 Method of modernization of an installation for production of nitric acid with its increased productivity / 2253614The invention is pertaining to the field of chemical industry, in particular, to the method of modernization of installations of nitric acid production. The method of modernizing of installation of production of the nitric acid providing for oxidation of ammonia with the help of air under a rarefaction, compression of the cooled nitrous gases in a nitrose supercharger, an absorption of nitric oxides in a tower absorber under pressure of 3.5-4.0 kg / cm2, expansion of the waste tail gases in the turbo-expander, consists in the fact that they increase the pressure of the nitrous gases at the inlet of the supercharger in the range from rarefaction up to the pressure of 1.02-1.05 kg / cm2, by installing a new or an additional gas blowers on the lines of the ammonia - air mixture or the nitrous gases or by decrease of hydraulic resistance of apparatuses and devices of pipelines at absorption inlet of the nitrose supercharger. At a pressure increase at the inlet of absorption of the nitrose gasses supercharger by decrease of the hydraulic resistance of the apparatuses and pipelines before absorption of the nitrose supercharger the increase of productivity of the installation will be much lower (~ up to 8 %). The method ensures an increase of productivity of the installation using the existing equipment at addition of small investments, which pay off less than for 1 year (from 0.6 up to 0.8 of a year) due to decrease of specific consumptions of raw material and power and a significant decrease of the conditionally-permanent expenses. Simultaneously the method allows to increase concentration of nitric acid and a degree of absorption, that may achieve its maximum at addition of pressure systems. |
 Method for production of nitric acid / 2248936Claimed method includes ammonia catalyst oxidation and nitrogen oxides absorption from nitrous gas with water and nitric acid, wherein nitrogen oxides absorption in absorption unit is carried out by using mass-exchange elements having several absorbing zones with different surfaces. Ratio (n) of oxidized nitrogen monoxide (NO) and absorbed nitrogen dioxide (NO2) in determined according to equation: lg n = (0.22-0.29)-0.0626 lg PNOx, wherein PNOx is partial pressure of nitrogen oxides in nitrous gas. According the invention it is made possible to increase absorption ratio and reduce nitrogen oxide content in exhaust gas up to 0.005 vol.%. |
 Method of nitric acid production and an installation for production of nitric acid / 2248322The invention is dealt with production of nitric acid with the help of oxidation of ammonia by oxygen of the air and absorption of nitrogen oxides by water in installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides. The method of production of nitric acid in the installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides provides, that compression of the air up to a uniform terminal pressure is conducted continuously within one stage without intermediate cooling and after that the compressed and so heated air is divided into two streams, one of which intended for production of nitric acid is directed to be cooled with further mixing with ammonia, and another is fed directly into a fuel combustion chamber connected with a recuperation turbine. The design embodiment of the installation for production of nitric acid provides for usage in the gas-turbine plant as an air engine for compression of air of an axial-flow compressor mounted directly on a common shaft with the recuperation turbine, at which near the outlet of the air engine the line of a compressed air stream is divided into two parts, one of which intended for production of nitric acid is first connected with a compressed air cooler and then with a mixer of ammonia with air, and the second intended for incineration of fuel is directly connected with the recuperation turbine combustion chamber. Besides in the capacity of a the compressed air cooler they use a "boiling" economizer connected to a line of a feed water for a boiler-utilizer and with a vapor collector of the boiler-utilizer by a line of steam-and-water mixture. The line of the air intended for production of nitric acid is also connected through the reheater of ammonia with a nitric acid blowing column. The technical result is simplification of the method, decreased investments and specific consumption of fuel. |
 Method and the device for supporting of the catalytic meshes in the burners for oxygenation of ammonia / 2284291The invention is pertaining to the support system for catalytic meshes in the burners for oxygenation of ammonia and to the method of reduction of movement of the particulates of the ceramic substance caused by the thermal expansion. The support system consists of the catalytic meshes (1) and possibly, of the support sieves (2) which are supported by the ceramic filling agents placed in the burner box with metallic walls and the perforated bottom. The support structure (9) is attached to the metallic wall (4) and-or the outer part of the periphery of the bottom (5). The technical result of the invention is development of the support structure, which does not cause damage of the packet from the catalyzer during operation of the burner, and the development of the system preventing movement of the of the particulates of the ceramic substance. |
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Ammonia conversion process / 2276098 Invention relates to ammonia conversion processes based on two-step catalytic system, which can be employed in production of nitric and hydrocyanic acids and in hydroxylamine sulfate production. Process according to invention comprises passing gaseous ammonia- and oxygen-containing mixture through two-step catalytic system, wherein first downstream step is embodied in a wire catalytic grate stack and second step in one or several layers of block honeycomb material, ratio of second-step hydraulic resistance value to the first-step one exceeding 4. Catalytic system steps are spaced from each other by distance equal to at most 10 and preferably 0.5 to 2 effective thickness of block channel σ calculated in terms of formula σ=2(S/(πn)1/2 (1-ε1/2), wherein S represents honeycomb block cross-section area, n number of channels in block, and ε open surface of block. Spacing between the steps is achieved by positioning between them spacing layer of gas-permeable chemically inactive material having hydraulic resistance coefficient below 100, hydraulic resistance of the second step being calculated as summary value of hydraulic resistances of honeycomb and spacing layers. |
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Method of initiating ammonia conversion reaction / 2253613 Proposed method is performed on reticular platinoid catalyst by passing the ammonia-containing gas mixture and oxygen-containing gas through it; local sections of catalyst surfaces are periodically heated to reaction initiating temperature by means of linear electric heating elements located directly on catalyst surface. Equivalent diameters of local sections of catalyst surface are selected between 1-5 of magnitude of external equivalent diameter of separate electric heating element; linear electric heating elements are connected to electric power source at duty factor from 20 to 1 s. Used as material for reticular platinoid catalyst are the following alloys: Pt-81, Pd-15, Rh-3.5 and Ru-0.5 mass-%; Pt-92,5, Pd -4.0 and Rh -3.5 mass-%; Pt-95 and Rh-5 mass-%; Pt-92.5 and Rh-7.5 mass-%. Initiating the ammonia conversion reaction by this method is performed in reactors for production of nitric and hydrocyanic acids and hydroxylamine sulfate. |
 Catalyst and a method of conversion of ammonia / 2251452The invention is pertinent to the field of chemical industry, in particular to production of a catalysts and processes of oxidation of ammonia in production of a weak nitric acid. The invention offers an ammonia conversion catalyst on the basis of the mixture of oxides of unitized structure and a method oxidation of ammonia in production of weak nitric acid. The catalyst represents a mixture of oxides of the over-all formula (AxByO3Z)k (MmOn)f, (NwPgvOv)r where: A - cation of Ca, Sr, Ba, Mg, Be, Ln or their mixtures; B - cations of Mn, Fe, Ni, Co, Cr, Cu, V, A1 or their mixtures; x=0-2, y=1-2, z=0.8-l.7; M - A1, Si, Zr, Cr, Ln, Mn, Fe, Co, Cu, V, Ca, Sr, Ba, Mg, Be or their mixtures; m=l-3, n=l-2; N - Ti, Al, Si, Zr, Ca, Mg, Ln, W, Mo or their mixtures, P - phosphorus, O - oxygen; w=0-2, g=0-2, v=l-3; k, f and r - mass %, at a ratio (k+f)/r=0-l, f/r=0-l, k/f = 0-100. The catalyst is intended for use in a composition of a two-stage catalytic system generated by different methods, also in a set with the trapping platinoid screens and-or inert nozzles. The technical result ensures activity, selectivity and stability of the catalyst to thermocycles at its use in two-stage catalytic system with a decreased loading of platinoid screens. |
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Method of nitric acid production and an installation for production of nitric acid / 2248322 The invention is dealt with production of nitric acid with the help of oxidation of ammonia by oxygen of the air and absorption of nitrogen oxides by water in installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides. The method of production of nitric acid in the installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides provides, that compression of the air up to a uniform terminal pressure is conducted continuously within one stage without intermediate cooling and after that the compressed and so heated air is divided into two streams, one of which intended for production of nitric acid is directed to be cooled with further mixing with ammonia, and another is fed directly into a fuel combustion chamber connected with a recuperation turbine. The design embodiment of the installation for production of nitric acid provides for usage in the gas-turbine plant as an air engine for compression of air of an axial-flow compressor mounted directly on a common shaft with the recuperation turbine, at which near the outlet of the air engine the line of a compressed air stream is divided into two parts, one of which intended for production of nitric acid is first connected with a compressed air cooler and then with a mixer of ammonia with air, and the second intended for incineration of fuel is directly connected with the recuperation turbine combustion chamber. Besides in the capacity of a the compressed air cooler they use a "boiling" economizer connected to a line of a feed water for a boiler-utilizer and with a vapor collector of the boiler-utilizer by a line of steam-and-water mixture. The line of the air intended for production of nitric acid is also connected through the reheater of ammonia with a nitric acid blowing column. The technical result is simplification of the method, decreased investments and specific consumption of fuel. |
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Method of nitric acid production and an installation for production of nitric acid / 2248322 The invention is dealt with production of nitric acid with the help of oxidation of ammonia by oxygen of the air and absorption of nitrogen oxides by water in installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides. The method of production of nitric acid in the installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides provides, that compression of the air up to a uniform terminal pressure is conducted continuously within one stage without intermediate cooling and after that the compressed and so heated air is divided into two streams, one of which intended for production of nitric acid is directed to be cooled with further mixing with ammonia, and another is fed directly into a fuel combustion chamber connected with a recuperation turbine. The design embodiment of the installation for production of nitric acid provides for usage in the gas-turbine plant as an air engine for compression of air of an axial-flow compressor mounted directly on a common shaft with the recuperation turbine, at which near the outlet of the air engine the line of a compressed air stream is divided into two parts, one of which intended for production of nitric acid is first connected with a compressed air cooler and then with a mixer of ammonia with air, and the second intended for incineration of fuel is directly connected with the recuperation turbine combustion chamber. Besides in the capacity of a the compressed air cooler they use a "boiling" economizer connected to a line of a feed water for a boiler-utilizer and with a vapor collector of the boiler-utilizer by a line of steam-and-water mixture. The line of the air intended for production of nitric acid is also connected through the reheater of ammonia with a nitric acid blowing column. The technical result is simplification of the method, decreased investments and specific consumption of fuel. |
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Catalyst and a method of conversion of ammonia / 2251452 The invention is pertinent to the field of chemical industry, in particular to production of a catalysts and processes of oxidation of ammonia in production of a weak nitric acid. The invention offers an ammonia conversion catalyst on the basis of the mixture of oxides of unitized structure and a method oxidation of ammonia in production of weak nitric acid. The catalyst represents a mixture of oxides of the over-all formula (AxByO3Z)k (MmOn)f, (NwPgvOv)r where: A - cation of Ca, Sr, Ba, Mg, Be, Ln or their mixtures; B - cations of Mn, Fe, Ni, Co, Cr, Cu, V, A1 or their mixtures; x=0-2, y=1-2, z=0.8-l.7; M - A1, Si, Zr, Cr, Ln, Mn, Fe, Co, Cu, V, Ca, Sr, Ba, Mg, Be or their mixtures; m=l-3, n=l-2; N - Ti, Al, Si, Zr, Ca, Mg, Ln, W, Mo or their mixtures, P - phosphorus, O - oxygen; w=0-2, g=0-2, v=l-3; k, f and r - mass %, at a ratio (k+f)/r=0-l, f/r=0-l, k/f = 0-100. The catalyst is intended for use in a composition of a two-stage catalytic system generated by different methods, also in a set with the trapping platinoid screens and-or inert nozzles. The technical result ensures activity, selectivity and stability of the catalyst to thermocycles at its use in two-stage catalytic system with a decreased loading of platinoid screens. |
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Method of initiating ammonia conversion reaction / 2253613 Proposed method is performed on reticular platinoid catalyst by passing the ammonia-containing gas mixture and oxygen-containing gas through it; local sections of catalyst surfaces are periodically heated to reaction initiating temperature by means of linear electric heating elements located directly on catalyst surface. Equivalent diameters of local sections of catalyst surface are selected between 1-5 of magnitude of external equivalent diameter of separate electric heating element; linear electric heating elements are connected to electric power source at duty factor from 20 to 1 s. Used as material for reticular platinoid catalyst are the following alloys: Pt-81, Pd-15, Rh-3.5 and Ru-0.5 mass-%; Pt-92,5, Pd -4.0 and Rh -3.5 mass-%; Pt-95 and Rh-5 mass-%; Pt-92.5 and Rh-7.5 mass-%. Initiating the ammonia conversion reaction by this method is performed in reactors for production of nitric and hydrocyanic acids and hydroxylamine sulfate. |
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Ammonia conversion process / 2276098 Invention relates to ammonia conversion processes based on two-step catalytic system, which can be employed in production of nitric and hydrocyanic acids and in hydroxylamine sulfate production. Process according to invention comprises passing gaseous ammonia- and oxygen-containing mixture through two-step catalytic system, wherein first downstream step is embodied in a wire catalytic grate stack and second step in one or several layers of block honeycomb material, ratio of second-step hydraulic resistance value to the first-step one exceeding 4. Catalytic system steps are spaced from each other by distance equal to at most 10 and preferably 0.5 to 2 effective thickness of block channel σ calculated in terms of formula σ=2(S/(πn)1/2 (1-ε1/2), wherein S represents honeycomb block cross-section area, n number of channels in block, and ε open surface of block. Spacing between the steps is achieved by positioning between them spacing layer of gas-permeable chemically inactive material having hydraulic resistance coefficient below 100, hydraulic resistance of the second step being calculated as summary value of hydraulic resistances of honeycomb and spacing layers. |
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Method and the device for supporting of the catalytic meshes in the burners for oxygenation of ammonia / 2284291 The invention is pertaining to the support system for catalytic meshes in the burners for oxygenation of ammonia and to the method of reduction of movement of the particulates of the ceramic substance caused by the thermal expansion. The support system consists of the catalytic meshes (1) and possibly, of the support sieves (2) which are supported by the ceramic filling agents placed in the burner box with metallic walls and the perforated bottom. The support structure (9) is attached to the metallic wall (4) and-or the outer part of the periphery of the bottom (5). The technical result of the invention is development of the support structure, which does not cause damage of the packet from the catalyzer during operation of the burner, and the development of the system preventing movement of the of the particulates of the ceramic substance. |
 Method of intensification of the installation for production of nitric acid / 2286943The invention is pertaining to the method of intensification of the installations for production of the non-concentrated nitric acid and may be used for raising productivity of the installations for production of the non-concentrated nitric acid under pressure. The invention provides for creation of the excess pressure on the inlet of the air compressor by preliminary compression of the atmospheric air in the high-pressure fan. At that the heat of the compression process in the warm season of the year is withdrawn by the direct contact with the water at the inlet of the fan, and in the cold season the heat is used for heating, at that in full or partially excluding heating of the air in the preheater mounted to prevent the icing up of the guiding apparatuses of the air compressor. At the enterprises with the high degree of the air dusting or chemical pollution for the contact cooling of the air by water it is possible to use scrubbers-washers, which combine the functions of the air cooler and the purification device. The method is effective for the operating installations, in which as a result of the wear-out of the flow-through section of the air compressors and the gas turbines decreases not only productivity, but also the pressure in the system, and as the result of it the concentration of the nitric acid. The method allows to realize the intensification of the installations using already existed equipment due to the increased pressure in the system. Concentration of the nitric acid is not lowered, the degree of purification of the tailing gases is preserved, production cost and the specific consumption of the steam and the natural gas are reduced. |
 Platinoid mesh catalytic agent / 2294239The invention is pertaining to the field of the chemical industry, in particular, to production of the nitric acid, nitric fertilizers, the cyanhydric acid, the nitrites and nitrates and to other productions of chemical products, where the flow sheet of production provides for the catalytic conversion of ammonia up to the nitrogen oxides with usage of the platinoid mesh catalytic agents. The platinoid mesh catalytic agent formed in the form of the catalytic package produced out of the layer-by-layer stacked wire catalytic meshes and weaved out of the wires with the diameter of 0.06-0.1 mm consisting of the alloys of platinum with rhodium, palladium, ruthenium and other metals of the platinum group differs that the catalytic package consists of two different in the geometry of the braiding types of the meshes sequentially alternating in the height of the package. At that the geometry of the braiding of the first type of the catalytic meshes is characterized by the number of the wires interlacing per 1 cm2 in the interval of 1024-450, and the geometry of the braiding of the second type of the catalytic meshes is characterized by the number of the wires interlacing per 1 cm2 in the interval of 400-200. The technical result of the invention is the increased conversion of ammonia and the decreased share of the platinoids included in the mesh catalytic agent production processes providing for the catalytic conversion of ammonia in the flow sheet of the chemical goods production. |
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N2o decomposition catalyst in ostwald process / 2304465 Decomposition if N2O under Ostwald process conditions at 750-1000°C and pressure 0.9-15 bar is conducted on catalyst, which comprises (A) support composed of α-Al2O3, ZrO2, SeO2, or mixture thereof and (B) supported coating composed of rhodium or rhodium oxide, or mixed Pd-Rh catalyst. Apparatus wherein N2O is decomposed under Ostwald process conditions on the above-defined catalyst is also described. Catalyst is disposed successively downstream of catalyst grids in direction of stream of NH3 to be oxidized. |
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Catalytic element for heterogeneous high-temperature reactions / 2318596 Invention relates to catalytic elements including ceramic contact of regular honeycomb structure for heterogeneous high-temperature reactions, e.g. ammonia conversion, and can be used in production of nitric acid, hydrocyanic acid, and hydroxylamine sulfate. Described is catalytic element for heterogeneous high-temperature reactions comprising two-step catalytic system consisting of ceramic contact of regular honeycomb structure made in the form of at least one bed constituted by (i) separate prisms with honeycomb canals connected by side faces with gap and (ii) platinoid grids, ratio of diameter of unit honeycomb canal to diameter of wire, from which platinoid grids are made, being below 20. |
 Method of obtaining oxide catalysts on a substrate / 2329100Invention pertains to the method of obtaining porous substances on a substrate for catalytic applications, to the method of obtaining porous catalysts for decomposition of N2O and their use in decomposing N2O, oxidising ammonia and reforming methane with water vapour. Description is given of the method of obtaining porous substances on a substrate for catalytic applications, in which one or more soluble precursor(s) metal of the active phase is added to a suspension, consisting of an insoluble phase of a substrate in water or an organic solvent. The suspension undergoes wet grinding so as to reduce the size of the particles of the substrate phase to less than 50 mcm. The additive is added, which promotes treatment before or after grinding. A pore-forming substance is added and the suspension, viscosity of which is maintained at 100-5000 cP, undergoes spray drying, is pressed and undergoes thermal treatment so as to remove the pore-forming substance, and is then baked. Description is also given of the method of obtaining porous catalysts on a substrate for decomposing N2O, in which a soluble cobalt precursor is added to a suspension of cerium oxide and an additive, promoting treatment, in water. The suspension is ground to particle size of less than 10 mcm. A pore-forming substance, viscosity of which is regulated to approximately 1000 cP, is added before the suspension undergoes spray drying with subsequent pressing. The pore-forming substance is removed and the product is baked. Description is given of the use of the substances obtained above as catalysts for decomposition of N2O, oxidation of ammonia and reforming of methane with water vapour. |
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Method of nitric acid production and an installation for production of nitric acid / 2248322 The invention is dealt with production of nitric acid with the help of oxidation of ammonia by oxygen of the air and absorption of nitrogen oxides by water in installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides. The method of production of nitric acid in the installations with uniform pressure at the stages of oxidation of ammonia and absorption of nitrogen oxides provides, that compression of the air up to a uniform terminal pressure is conducted continuously within one stage without intermediate cooling and after that the compressed and so heated air is divided into two streams, one of which intended for production of nitric acid is directed to be cooled with further mixing with ammonia, and another is fed directly into a fuel combustion chamber connected with a recuperation turbine. The design embodiment of the installation for production of nitric acid provides for usage in the gas-turbine plant as an air engine for compression of air of an axial-flow compressor mounted directly on a common shaft with the recuperation turbine, at which near the outlet of the air engine the line of a compressed air stream is divided into two parts, one of which intended for production of nitric acid is first connected with a compressed air cooler and then with a mixer of ammonia with air, and the second intended for incineration of fuel is directly connected with the recuperation turbine combustion chamber. Besides in the capacity of a the compressed air cooler they use a "boiling" economizer connected to a line of a feed water for a boiler-utilizer and with a vapor collector of the boiler-utilizer by a line of steam-and-water mixture. The line of the air intended for production of nitric acid is also connected through the reheater of ammonia with a nitric acid blowing column. The technical result is simplification of the method, decreased investments and specific consumption of fuel. |
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Method for production of nitric acid / 2248936 Claimed method includes ammonia catalyst oxidation and nitrogen oxides absorption from nitrous gas with water and nitric acid, wherein nitrogen oxides absorption in absorption unit is carried out by using mass-exchange elements having several absorbing zones with different surfaces. Ratio (n) of oxidized nitrogen monoxide (NO) and absorbed nitrogen dioxide (NO2) in determined according to equation: lg n = (0.22-0.29)-0.0626 lg PNOx, wherein PNOx is partial pressure of nitrogen oxides in nitrous gas. According the invention it is made possible to increase absorption ratio and reduce nitrogen oxide content in exhaust gas up to 0.005 vol.%. |
FIELD: chemical industry; method of intensification of the installations for production of the non-concentrated nitric acid.
SUBSTANCE: the invention is pertaining to the method of intensification of the installations for production of the non-concentrated nitric acid and may be used for raising productivity of the installations for production of the non-concentrated nitric acid under pressure. The invention provides for creation of the excess pressure on the inlet of the air compressor by preliminary compression of the atmospheric air in the high-pressure fan. At that the heat of the compression process in the warm season of the year is withdrawn by the direct contact with the water at the inlet of the fan, and in the cold season the heat is used for heating, at that in full or partially excluding heating of the air in the preheater mounted to prevent the icing up of the guiding apparatuses of the air compressor. At the enterprises with the high degree of the air dusting or chemical pollution for the contact cooling of the air by water it is possible to use scrubbers-washers, which combine the functions of the air cooler and the purification device. The method is effective for the operating installations, in which as a result of the wear-out of the flow-through section of the air compressors and the gas turbines decreases not only productivity, but also the pressure in the system, and as the result of it the concentration of the nitric acid. The method allows to realize the intensification of the installations using already existed equipment due to the increased pressure in the system. Concentration of the nitric acid is not lowered, the degree of purification of the tailing gases is preserved, production cost and the specific consumption of the steam and the natural gas are reduced.
EFFECT: the invention allows to realize the intensification of the installations using already existed equipment, to reduce production cost and the specific consumption of the steam and the natural gas.
4 cl, 2 ex, 2 tbl, 2 dwg
The invention relates to the field of industrial production of non-concentrated nitric acid and can be used for intensification of existing facilities, in which nitric acid with a concentration of 55-65% HNO3produced by the method of oxidation of ammonia by oxygen under pressure and absorption of nitrogen oxides under the same or higher pressure.
The composition of these plants include native plant including an air compressor for compressing ambient air, nitrous supercharger to compress nitrous gases (in installations with higher pressure at the stage of absorption) and drive these compressors. Drive in modern installations include gas turbine for energy recovery of the compressed tail gas after absorption in combination with an electric motor or steam turbine.
In Russia and CIS countries the production of nitric acid is almost completely carried out on the units for energy-technological scheme, in which the engine unit is a gas turbine installation. In units of average power under uniform pressure (units of type UKL-7) gas turbine unit type GTT-3 includes an air compressor and a gas turbine with an estimated temperature of the tail gas 700°C. In large aggregates with two pressure type AK-72 gas turbine unit type GTT-12 VC is uchet air compressor, nitrous supercharger and a gas turbine with an estimated temperature of the tail gas 760°C. Heating the tail gas is the burning of natural gas. The motor in GTT-3 (10% of the total capacity of the drive), steam turbine (8%) GTT-12 project designed to run machine units, but in fact are constantly exploited as an additional drive.
The source of information
1. "The production of nitric acid in aggregates of large capacity". / Edited Olevsky V.M., M.: Chemistry, 1985, p.94-306.
2. Directory of apothica, M.: Chemistry, 1987, p.66-92.
Widely known for the installation of Western firms built on the basis of the schemes without the use of energy natural gas combustion. Accordingly, the drive machine units includes a gas turbine for energy recovery tail gas, heated to 300-500°With the warmth of nitrous gases by oxidation of ammonia, and the trailing engine - steam turbine or electric motor.
Performance installations for the production of nitric acid can be reduced during operation due to wear of machine units, and for technical reasons (for example, by reducing the degree of conversion of ammonia, wear heat-exchange equipment).
But the main reason for the poor performance of plants is always reduced the s air flow air compressor due to wear, pollution flowing part, reducing the number of turns. This refers to the machine units of any type, but in different degrees. Machine units, which ensures the constancy of the speed of the compressors (air and nitrous) at the expense of the electric motor great power more stable. Less stable machine with a steam turbine as the closing of the engine due to the lower speed when worn. The greatest instability different machine units with gas turbine drive, for example GTT-3 and GTT-12, in which the wear of the air compressor is added relatively fast, with the loss of efficiency, wear high-temperature gas turbines. It is particularly sensitive to the loss of efficiency of gas turbines gas turbine machine type GTT-12 in Assembly AK-72 with a low-powered steam turbine due to the fall speed of the air and nitrous compressor, which in addition to reducing the air flow, i.e. the plant productivity leads to a significant reduction of pressure in the absorption of nitrogen oxides and, consequently, reduce the effectiveness of the absorption column.
In installations of the type UKL-7 with the machine GTT-3, which supports a constant speed by an electric motor, wear an air compressor and gas turbine leads to decreased production HNO3not only because of the direct reduction of the feed in the spirit, but because of the need to increase the proportion of compressed air directed past the technology of the gas turbine.
The technical problem to be solved by the present invention is directed, is to achieve a substantial increase in productivity plants nitric acid is not less than 8-15% (depending on the type of units) without expensive upgrades or replacement of engine units on existing process equipment by simultaneously increase the air flow and pressure. The invention can be used in the construction of new plants, but its main purpose is to intensify existing units type UKL-7 and AK-72 gas turbine engine assemblies.
The essence of the invention is to provide a positive air pressure at the inlet of the air compressor machine unit (instead of vacuum) by pre-compression of air in the high-pressure fan and cooling by direct contact with water.
The novelty of the method according to the invention lies in the creation of excess pressure at the inlet of the air compressor and the air temperature decreases after the preliminary compression in the high-pressure fan direct contact of air with the water.
According to the present invention the pressure on the inlet air is tion of the compressor is limited by admissible pressure in the apparatus installation nitric acid, which intensifies. Ceteris paribus (the speed of the shaft of the compressor, the air temperature at the inlet, polytropic efficiency, etc.) air pressure after compression is approximately directly proportional to the density of air at the inlet. Technological equipment is usually calculated on the maximum air pressure that can be achieved in air compressor in the cold season, when the density of air at the inlet of the maximum.
The standard conditions for the calculation of machine units type GTT-3 and GTT-12 in terms of suction air compressor:
- nominal temperature +20°C
- in winter - 5°C (including heating at a lower temperature to prevent icing of the guide vane),
- barometric pressure of 745 mm Hg (99,3 kPa),
the vacuum in the suction pipe 500 mm VST (0,49 kPa), i.e. the absolute pressure at the inlet 98,81 kPa.
This means that in winter the maximum air density, and hence the maximum rated air pressure (273+20)/(273-5)=1,0932 times higher than the nominal. Accordingly, the allowable absolute pressure in the suction pipe at a nominal temperature of +20°will be 98,81×1,0932=108,02 kPa, which is achieved by pre-compression of air at 11-11,5 kPa. Accordingly, the performance of an air compressor due to the factor air density Mack the distribution panel is minimal can be increased by (108,02-98.81)× 100/98,81=9.3 per cent. For machine units with gas turbine drive type GTT-12, the speed of which depends on the wear of the drive, the performance of the air compressor increases to a greater extent. This is because the compression of air and the specific energy consumption in air compressor does not depend on the air density, while the energy output in a gas turbine is increased by increasing the degree of expansion, which leads to an increase in the number of revolutions. Table 1 presents the results of computational studies of the current machine GTT-12 in one of the installations AK-72 after many years of operation with the use of actual indicators of air flow, the number of revolutions of the shaft of the air compressor and nitrous supercharger, the pressure and temperature of gases in the system path.
When installing the high pressure fan pressure 11-11,5 kPa at the inlet of the air compressor creates overpressure 0.09 kgf/cm2above the original.
On the basis of such excess pressure, the calculations (table 1) different modes of increasing the air supply of the existing GTT-12. The original mode, option 0, reflects the actual performance to intensify. They served as baseline data for the program computational study of the effect of the pressure at the inlet of the air compressor. Var is the ants 1-5 apply to the GTT-12 to repair nitrous supercharger, 6-7 - after repair.
As can be seen from the calculation results, after increasing the pressure on the suction intensification (air supply) is 12% without changing the power consumption from steam drive (option # 3), and after repair No. 4 (with reduction of steam consumption in back-pressure steam turbine from 41 to 24 t/h (option # 6), the pressure at the stage of oxidation of ammonia increased from 3.9 to 4,51-4.47 kgf/cm2at the stage of absorption from 9.2 to 10,42 and 10,38 kgf/cm2i.e. on - 1,2 bar; shaft rpm OK > > > 4860 up to 4960 rpm.
The pressure increase at the stage of oxidation of ammonia by 15%at the stage of absorption by 13% allows intensification on the same manufacturing equipment.
In mode No. 8 with no reduction in load of the steam turbine can be obtained increases the production of nitric acid ˜19%.
Abbreviations in table 1:
OK - axial air compressor;
NN - nitrous supercharger;
TVD - high pressure turbine.
For installations UKL-7 gas turbine engine Assembly type GTT-3 the ratio between the increase in air pressure at the inlet of the air compressor and increase production of nitric acid retains its disproportionate, but to a lesser extent due to the constancy of the speed provided by the motor.
Table 2 shows the results of calculation of the s research machines GTT-3 in the installation of nitric acid UKL-7 under uniform pressure on the stages of the oxidation of ammonia and absorption.
The original mode, version 0.1, reflects the actual performance to the intensification of the machine GTT-3M working in the installation of UKL-7 in the region with a temperate climate and a barometric pressure of 745 mm Hg
Version 1.1 - mode after intensification with the installation of the fan to pre-compress the air to 11-11,5 kPa and a load of the motor (motorgenerator PHASE-800) with low power consumption.
Options 0.2, 1.2 job related GTT-3M in the region with a hot climate in summer (up to 35°C) and low barometric pressure (Central Asia, Caucasus).
Computational studies were conducted on the basis of the performance of existing machines in the installations.
Baseline to install 1 in temperate climates correspond to develop 14 t/h MNG. HNO3for installation 2 in the Central Asia development 12 t/h MNG. HNO3.
After the intensification under other equal conditions for the installation of 1 production is increased to 15.3 t/h (˜9,0%), in units of 2 to 13.8 t/h (˜15,0%).
Abbreviations in table 2:
OS - axial compressor;
TSN - centrifugal supercharger air compressor;
GT - gas turbine;
PHASE-800 - reversible motor comprising GTT-3M (M - upgraded).
Pre-compression of air to 11-11,5 kPa in the fan increases its temperature at 10-12�B0; With that somewhat offsets the increase in its density. The air must be cooled to a reference temperature +20°C. the known method of cooling through the wall will need a refrigerant with a temperature of +5°C.
To remove the heating of the air during compression is required to take 12500-18700 kcal per 1 t HNO3that is equivalent to the evaporation 42-60 kg of liquid ammonia.
The power consumption for the refrigeration potential of +5°in modern ammonia-refrigerating machines will be at least 5-6 kWh per 1 ton of HNO3.
Significant capital costs for construction of the ammonia refrigeration plant and air cooler, while cooling air is required 5-8 months of the year.
Therefore, according to the present invention, the cooling air produced by direct contact with water, i.e. evaporative cooling.
For removal 12500-18700 kcal required to vaporize 21,7-26 kg of water per 1 ton of HNO3(for installations AK-72 at the intensification of 12% - ˜1215 kg/h, for UKL-7 at the intensification of 9% - ˜420 kg/h).
When evaporative cooling is the degree of cooling affects the relative humidity of the atmospheric air.
As the calculations show, for air with an initial temperature of +20°and when the initial relative humidity <65% evaporative cooling can cool the air before initial replication of the th temperature +20° C, at a relative humidity of 70% to 21°C, at a relative humidity of 90% to 23°C.
But in those days than cooling through the wall of the contact cooling is not lost. Niedokladnie air 1-3°With contact cooling is compensated by a lower hydraulic losses due to the exclusion of the heat exchanger.
Contact cooling water is especially effective from the point of view of energy consumption, if it is carried out by injection of water through the nozzle with a fine spray on the suction side of the fan, when the compression process in the fan approaching isothermal.
In certain cases, for example when operating plants in hot and dry climates (a significant part of Russia, Central Asia), can be used for pre-cooling the air in the scrubber, as in these areas during the hot season, the air has a low relative humidity, but are often contaminated with dust from dust storms. When you install a scrubber to fan air temperature decreases at the inlet, the water spray drift and evaporation in fan during compression of the air contributes to a decrease in air temperature at the inlet of the air compressor, and reduces the energy consumption for air compression.
Contact cooling slightly increases the water vapor content in the air, but the e is more of 0.4-0.5% by volume.
Consequently, compared with the cooling of the compressed air through the wall of the reduced performance of the air compressor by 0.45%, and the heat load of the condenser on nitrous gases is increased by 2%.
These negative side contact of the cooling air is negligible compared with the benefits in relation to cooling through the wall, especially since the cooling air is required only in the warmer months (when the air temperature is +10°it may not be).
The implementation of the invention may be illustrated by examples 1 and 2.
Example 1, figure 1. Intensification of units of type AK-72 and UKL-7.
The newly installed fan 1 performance 230-240 thousand nm3/h - 15-20% above nominal performance air compressor GTT-12; pressure fan 11-11,5 kPa.
On the suction side of the fan through a nozzle 2 is supplied 1-1,25 m3/h steam condensate or demineralized water.
At ambient temperature +20°C, relative humidity of 60-65% and the heat of compression evaporation of water temperature on the discharge of the fan is maintained at +20°C and the relative humidity increases to 90-95%.
At a relative humidity of atmospheric air 90% of the water injection is maintained approximately at the same level, temperature satoh the air after evaporation of the water until full saturation is stabilized at the level of ˜ 23°C.
When ambient temperature is below 10°With modulated water in the fan may be terminated.
In the cold season air is heated by compression in the fan allows for a long period, don't waste steam to heat the air in the heater installed at the entrance to the filter 3 before the air compressor installation.
Periodically, the injection of demineralized water for a short time for washing is increased to prevent salt deposits in the flowing part of the fan with the diversion of water from a fan in the drainage.
With the intensification of plants UKL-7 principal differences from the invention in comparison with described there. Accordingly, a set of high-pressure fan performance 88-90 nm3/h of air and the pressure of 11-12 kPa.
Example 2, figure 2.
In regions with hot climates and/or high dust air on the suction side of the fan 1 is set to the coarse filter air 3 and the washing scrubber 2 circulation of demineralized water by means of a pump 4.
When the contact of air with the water mass transfer nozzle scrubber 2 is the saturation of air with water vapor. The saturation process occurs with varying degrees of cooling air, depending on the relative humidity.
At a relative humidity of 40-50% and so is the ambient air temperature value +30° Since the air is cooled to a temperature close to the temperature of the wet thermometer", in this case up to 22°C.
When the compression of the air with regard to cooling by evaporation is carried out with air drops and additionally injected water at the outlet of the fan 1 temperature ˜25°and will have a moisture content close to full saturation. Through the scrubber 2 to install the AK-72 passes ˜220 thousand nm3/h air, in the installation of UKL-7 - 90 thousand nm3/h, in the scrubber enter fresh water in a quantity equal to the amount of evaporated water and bred in the form of drainage of collected dust.
In the scrubber should not be britholite; if the ash water spray is insufficient to remove the heat of compression air their evaporation, the fan is supplied through nozzles additional water.
The examples and drawings to them illustrate the application of the method how to install AK-72 and UKL-7 that does not exhaust the scope of the invention. It can be used for any plants nitric acid production.
Among the most important advantages, providing significant economic benefits in the process, include:
- low capital gains power;
- short time-to-market, and without stopping the current installation;
- by intensification increases the pressure in the system is IU, that allows it to implement in existing process equipment without lowering the concentration of nitric acid and deterioration of discharge of harmful substances into the atmosphere from the tail gases;
- reduced the cost of production.
Literature
1. The production of nitric acid in the units of large capacity, edited by V.M. Olevsky. M.: Chemistry, 1985, p.94-306.
2. Directory of apothica, vol. 2. M.: Chemistry, 1987, p.66-92.
| Table 1 Table of results of computational studies of the modes of operation of the existing GTT-12 |
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| Options | 0 | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | |
| Atmospheric pressure | kg/cm2 | 1.00 | 1.00 | 1.00 | 1.00 | 1.00 | 1.00 | 1.00 | 1.00 | 1.00 |
| The pressure behind the fan | kg/cm2 | 1.00 | 1.09 | 1.09 | 1.09 | 1.09 | 1.09 | 1.09 | 1.09 | 1.09 |
| Press OK | kg/cm2 | 3.90 | 4.23 | 4.32 | 4.51 | 4.55 | 4.60 | 4.47 | 4.52 | 4.57 |
| Pressure before LV | kg/cm2 | 3.40 | 3.69 | 3.73 | 3.95 | 3.97 | 3.98 | 3.92 | 3.94 | 3.95 |
| The pressure for low-voltage | kg/cm2 | 9.20 | 9.89 | 10.38 | 10.42 | 10.70 | 11.07 | 10.38 | 10.66 | 11.04 |
| The gas pressure before TVD | kg/cm2 | 8.40 | 8.95 | 9.38 | 9.43 | 9.68 | 10.01 | 9.40 | 9.65 | 9.99 |
| The rotor speed OK | rpm | 4860 | 4930 | 5050 | 4960 | 5035 | 5 130 | 4960 | 5040 | 5 130 |
| The rotor speed NN | rpm | 4880 | 4840 | 5000 | 4830 | 4900 | 5000 | 4800 | 4870 | 4970 |
| Stability margin OK | % | 18.8 | 18.4 | 23.9 | 17.8 | 20.9 | 25.2 | 18.6 | 21.8 | 26.2 |
| Stability margin NN | % | 44.7 | 42.5 | 46.2 | 42.3 | 43.7 | 46.0 | 43.3 | 44.8 | 47.2 |
| Temperature atmospheres. air | ° | 20 | 20 | 20 | 20 | 20 | 20 | 20 | 20 | 20 |
| The temperature of the air before OK | ° | 20 | 30 | 30 | 20 | 20 | 20 | 20 | 20 | 20 |
| The air temperature at the exit OK | ° | 187 | 201 | 205 | 196 | 198 | 200 | 195 | 197 | 200 |
| The temperature of the air before LV | ° | 65 | 65 | 70 | 70 | 70 | 70 | 70 | 70 | 70 |
| The air temperature at the outlet LV | ° | 215 | 213 | 226 | 217 | 221 | 227 | 207 | 210 | 216 |
| The temperature of the gas before the turbine | ° | 745 | 745 | 745 | 745 | 745 | 745 | 745 | 745 | 745 |
| The temperature of the gas turbine | ° | 391 | 385 | 380 | 380 | 377 | 374 | 380 | 377 | 373 |
| The steam flow to the turbine | t/h | 1.0 | 1.0 | 1.0 | 1.5 | 1.5 | 1.5 | 1.0 | 1.0 | 1.0 |
| The power of the steam turbine | kW | 1700 | 1700 | 2400 | 1700 | 2050 | 2550 | 950 | 1250 | 1700 |
| The total steam consumption | t/h | 41 | 41 | 57 | 42 | 49 | 61 | 24 | 30 | 41 |
| The air flow before OK | t/h | 254.0 | 270.7 | 283.7 | 284.5 | Compared with RUB 292.1 | 302.1 | 284.5 | 292.2 | 302.5 |
| Performance | % | - | 6.6 | 11.7 | 12.0 | 15.0 | 18.9 | 12.0 | 15.1 | 19.1 |
| Table 2 Table of results of computational studies of the modes of operation of the existing GTT-3 in UKL-7 |
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| № p/p | Indicators | Unit. | Options | |||
| 0.1 | 1.1 | 0.2 | 1.2 | |||
| 1 | Barometric air pressure | kPa | 99,3 | 99,3 | 96,6 | 96,6 |
| 2 | Air pressure | kPa | ||||
| 2.1 | for inflatable fan | - | 110,0 | - | to 106.0 | |
| 2.2 | - suction OK | 95 | 105 | 92 | 102 | |
| 2.3 | - discharge TSN | 716 | 780 | 680 | 745 | |
| 2.4 | before GT | 560 | 609 | 540 | 580 | |
| 3 | Temperature | ° | ||||
| 3.1 | - air suction OK | 20 | 20 | 30 | 25 | |
| 3.2 | - the tail gas before GT | 680 | 680 | 690 | 690 | |
| 4 | The rotor speed | rpm | 5100 | 5100 | 5100 | 5100 |
| 5 | Air consumption | t/h | ||||
| 5.1 | before OK | 100 | 108,4 | 85,3 | 97,2 | |
| 5.2 | - technology | 72 | 78,5 | 61,57 | 70,8 | |
| 6 | The natural gas consumption | metro3/h | 1680 | 1800 | 1500 | 1725 |
| 7 | Power consumption | kWh | ||||
| 7.1 | - fan | - | 400 | - | 370 | |
| 7.2 | - PHASE-800 | 350 | 150 | 400 | 200 | |
| 8 | The increase in production HNO3 | % | - | 9 | - | 15 |
1. Method of intensification of installations for the production of nitric acid, including compressed air in the air compressor, the stage of oxidation of ammonia by oxygen and absorption of oxides of nitrogen under pressure, the recovery of energy from the hot tail gas in a gas turbine, wherein the inlet of the air compressor creates excessive pressure pre-compression of atmospheric air in the high-pressure fan, and in the warm season warm compression assign direct contact of air with the water.
2. The method according to claim 1, characterized in that the air is cooled during the compression process by the injection of water through a nozzle at the inlet of the fan.
3. The method according to claim 1, characterized in that the air is cooled in the scrubber when in contact with water, mixing the cooling air with the preliminary cleaning of dust and chemical contaminants.
4. The method according to claim 1, characterized in that the absorption of oxides of nitrogen is carried out under the same pressure as the oxidation of ammonia, or a higher pressure.