Method of initiating ammonia conversion reaction

FIELD: initiating ammonia conversion reaction.

SUBSTANCE: 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.

EFFECT: reduction of time required for reaction over entire surface of catalyst; reduction of explosion danger.

2 cl, 10 ex

 

The technical field to which the invention relates.

The present invention relates to a method of initiating the reaction of ammonia conversion to mesh the platinum catalyst by passing through the gas mixture containing ammonia and oxygen-containing gas, and can be preferably used in reactors for catalytic conversion of ammonia industrial installations for obtaining nitrogen, hydrocyanic acid and has synthesis. You should specify that in the reactor the conversion of ammonia industrial installations to produce hydrocyanic acid and also has synthesis of ammonia with oxygen-containing gas additionally served, respectively, methane and water vapor.

The level of technology.

Known methods of initiating the reaction of conversion of ammonia (EN 1476677 C1 IPC 01 J 8/04, 1987; EN 2054961 C1 IPC V J 8/04, 1996) on the mesh platinum catalyst by passing through the gas mixture containing ammonia and oxygen-containing gas, which is continuously heated localized areas of the surface of the catalyst to a temperature of initiation of the reaction with the use of a linear electric heating elements located directly on the surface mesh of the platinum catalyst.

The main disadvantage of the considered way of analog is that in some cases the industry is Noah implementation possible burning of local areas mesh platinum catalyst due to the continuous heating of these plots using linear electrical elements during the initiation of the reaction conversion of ammonia on the catalyst. Obviously, this kind of burning leads, on the one hand, the overuse mesh platinum catalyst, on the other hand, to increase the explosiveness of the process because of the "breakthrough of unreacted ammonia in the area behind the mesh platinum catalyst ("breakthrough" ammonia is not only burnt through space, but through the net sites of the platinum catalyst, where the reaction of ammonia conversion has not started yet). In the area of the screen the platinum catalyst unreacted ammonia reacts with the nitrogen oxides with the formation of nitrite-nitrate of ammonium salts. Accumulate over time in communications and pipelines, industrial plants, these ammonium salts under certain conditions can detonate the explosion, which leads to the release of system failures and even human casualties.

The closest in technical essence to the present invention prototype, which largely addressed the shortcomings of the way of analog, is a method of initiating the reaction of ammonia conversion to mesh the platinum catalyst by passing through the gas mixture containing ammonia and oxygen-containing gas, in which periodically heat localized areas of the surface of the catalyst to a temperature of iniciaron the deposits using linear electrical elements, located directly on the catalyst surface (article: Viernes, Eousa "Reduction of the platinum catalyst and the explosion process at the stage of oxidation of ammonia to nitric acid production", Catalysis in industry, 2001, No.3, pp.30-41, see the second paragraph in the left column on page 38. A photocopy of this article is attached). In the description of the prototype method presents experimentally obtained values of electrical power per unit length of linear single electric heating element depending on the composition of the alloy mesh platinum catalyst, the number of nets in the package net the platinum catalyst and the flow rate of the ammonia-air mixture (see also Fig. 7 and 8 on p.40 of the above article). The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the mesh platinum catalyst domestic industrial installation of nitric acid, UKL-7 in the method prototype is 20 - 25C for net platinum catalyst of alloys Pt - 92,5, Pd - 4.0 and Rh - 3.5 wt.%; Pt - 81, Pd - 15, Rh - 3.5 and EN - 0.5 wt.% (see page 38, first paragraph of the right column of the text, and figure 7 on p.40 of the above article).

The disadvantage of the prototype is that it is not developed its basic performance parameters is s, namely, the limits of the ratio of the equivalent diameter of the heated local area of the surface of the catalyst and the equivalent diameter of the individual line item (equivalent diameter d - common geometrical parameter that is determined from the ratio d = 4S/P, where S is the cross-sectional area of a physical object, P is its perimeter (on this, see, for example, in the book Agitatin "Basic processes and apparatus of chemical technology, M., ed. "Chemistry", page 38). In the context of this model under equivalent diameter of separate linear electric heating element means is equivalent to the diameter of its actual cross-section, and under the equivalent diameter of the heated local area of the surface mesh catalyst - equivalent diameter of the area of these plots, lying directly under the linear electric heating elements, as well as the duration of the period of connection of the linear electric heating elements to a power source. As shown by the industrial survey conducted by the authors of the present invention, this deficiency leads to increased period of time of initiation of the reaction of conversion of ammonia on the entire surface of the mesh platinum catalyst, maintaining the possibility of burn-out mesh is th the platinum catalyst, the result is a relatively high risk of this process (the process of initiation is explosion-proof, when the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the sieve catalyst when using linear electric heating elements shall not exceed the values defined by the technological requirements of production, determining the safe conduct of the starting period of operation of the reactor. For example, for most industrial installations to produce nitric acid, this value is 60). In addition, the use of the prototype method leads to a waste of energy for initiating the reaction of conversion of ammonia, which is determined, in particular, the duration of time period connecting linear electric heating elements to a power source.

Disclosure of the invention.

The technical problem to be solved by the present invention is directed, is to increase the explosion process of initiating the reaction of conversion of ammonia on the surface mesh of the platinum catalyst by reducing the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the mesh platinum catalyst and avoid burn-out, and to reduce the cost of electricity when initier the processes.

This technical task is implemented in the method of initiating the reaction of ammonia conversion to mesh the platinum catalyst by passing through the gas mixture containing ammonia and oxygen-containing gas, in which periodically heat localized areas of the surface of the catalyst to a temperature to initiate reaction of ammonia conversion using linear electric heating elements located directly on the surface mesh of the platinum catalyst. When this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is chosen in the range of 1-5 on the value of the external equivalent diameter of separate linear electric heating element, and a linear electric heating elements connected to a source of electricity with the duration of the connection, which take in the appropriate limits 20-1 C.

The main distinguishing features of the proposed method consist in the fact that heat localized areas of the surface of the catalyst, equivalent to the diameter of which is chosen in the range of 1-5 on the value of the external equivalent diameter of separate linear electric heating element, and a linear electric heating elements connected to a power source with a duration of connections which are in the appropriate limits 20-1 C.

An additional distinguishing feature is that as the mesh material of the platinum catalyst used alloys Pt - 81, Pd - 15, Rh - 3.5 and EN - 0.5 wt.%; Pt - 92,5, Pd - 4.0 and Rh - 3.5 wt.%; Pt - and Rh 95 to 5 wt.%; Pt - 92,5 and Rh - 7.5 wt.%.

The present invention meets the condition of patentability - novelty", as in the prior art failed to find technical solutions, the essential features which would coincide with all the features available in the independent claims of the present invention. The present invention meets the condition of patentability - "inventive step", since the prior art has failed to find technical solutions, the essential features of which was provided by performing the same technical problem on which the present invention is directed.

In the technical literature there is no information about the mutual influence of the main parameters of the process of initiating the reaction of ammonia conversion to mesh platinum catalyst when using linear electrical elements to each other - within varying the ratio of the equivalent diameter of the heated local area of the surface of the catalyst and the equivalent diameter of individual linear electric heating element, and the duration of their period on the connecting to a power source. On the basis of industrial research conducted by the authors of the present invention in the reactor ammonia conversion of various industrial plants receiving nitrogen, hydrocyanic acid and has synthesis, the first set that are specified in the independent claim of the present invention limits are operational parameters are the same for the process of conversion of ammonia in these industrial settings.

The implementation of the invention.

The present invention is illustrated below by examples.

Example 1. Testing is carried out in the reactor ammonia conversion installation for the production of nitric acid, working under pressure 0,716 MPa, with a capacity of 348 tons per day in terms of 100% NGO3(for a detailed description of this setup, see the book: M. Bonn, Ndeshiko, AVI and others, "the Production of nitric acid in aggregates of large capacity", Ed. by Vmelilo, Moscow: Chemistry, 1985, p.94-214). Working diameter mesh platinum catalyst 1650 mm as the mesh of the platinum catalyst used pack of 12 woven platinum catalyst grids with the number of holes 1024/cm2wire dia. 0,092 mm, made of alloy Pt - 81, Pd - 15, Rh - 3.5 and EN - 0.5 wt.% with an initial mass of ~ 24 kg Package grids installed in the reactor between the flanges. The reactor is oversee ammonia supplied with Windows for visual observation of the distribution initiated by the reaction of ammonia conversion on the entire surface of the layer grids. In the reactor there is also a thermocouple for measuring the temperature of the layer grids. As the initial mixture of reactants during start using a gas mixture containing ammonia and air with the concentration of ammonia in a mixture of 8 vol.% and the initial temperature 130° C. the Initial mixture under an absolute pressure of ~ 0,716 MPa and a flow rate of 45000 nm3/h (~70% of flow rate under steady-state operation) served in the reactor. To initiate the reaction of ammonia conversion in the reactor are mounted four linear electric heating element directly on the surface mesh of the platinum catalyst in parallel to each other at a distance of 400 mm, which are connected in-series in an electrical circuit. Each item is a piece of wire of alloy with high electrical resistance, for example HUT according to GOST 5632-72. The elements are enclosed in isolation on the basis of electrical porcelain MKR, derived from mulit-corundum mixture by sintering. The outer diameter of the insulation element is 4 mm, the Total electrical resistance of the four elements is 7 Ohms. Elements connected to a source of alternating current voltage of 220 V through a regulating transformer within the range of the voltage 20-380 Century, the Required value of the electric voltage is chosen so that the power allocated is appropriated from the surface of all elements was sufficient to achieve local surface mesh platinum catalyst temperature to initiate reaction of the ammonia conversion. Testing is carried out as follows. First, in the reactor conversion of ammonia serves only the process air flow 41400 nm3/hour. After the set pressure to the set point in the reactor serves ammonia with a flow rate of 3600 nm3/hour. At the start of the supply of ammonia elements connected to a source of electricity for the first period of the connection. When this instrument is fixed supplied electric voltage and current, as observed through the observation window and the readings of thermocouples is the moment of initiation of the reaction, the conversion of ammonia in local areas of the surface mesh of the platinum catalyst, lying directly under the elements. The duration of the connection elements to the source of electricity is 20 C. During this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equivalent to the outer diameter of the element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages defined visually by the stopwatch was 18 C.

Example 2. Everything is the same as in example 1, with the difference that the duration of the connection elements to an electrical power source is 10 C. During this heat localized areas of the surface is utilizator, the equivalent diameter of which is equal to 2.5 values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages defined visually by the stopwatch was 17 C.

Example 3. Everything is the same as in example 1, with the difference that the duration of the connection elements to an electrical power source 1 is C. this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equal to 5 the values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, amounted to 16 C.

Example 4. Everything is the same as in example 1, with the difference that the duration of the connection elements to an electrical power source is 22 C. During this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equal to 0.85 the values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, particularly what I visually stopwatch, was 22 C. it Should be noted that the initiation of reaction, the conversion of ammonia on the net platinum catalyst in this case was able to realize an average experience of five, i.e. in four experiments, the reaction of ammonia conversion is not instantiated.

Example 5. Everything is the same as in example 1, with the difference that the duration of the connection elements to an electrical power source is 0.8 C. this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equal to 6.2 values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, 15.5 C. However, for each test the proposed method in this case would inevitably have been observed or burning of local areas of the surface mesh of the platinum catalyst, or violation of the integrity of the linear electric heating elements due to the high values of electrical power.

Example 6. Everything is the same as in example 2, with the difference that as the mesh material of the platinum catalyst used alloy Pt - 92,5, Pd - 4.0 and Rh - 3.5 wt.%. The duration of the period of time of initiation of the reaction of conversion of ammonia all over the surface of the catalyst package nets after power outages, some visually stopwatch, amounted to 16 C.

Example 7. Everything is the same as in example 2, with the difference that as the mesh material of the platinum catalyst used alloy Pt - and Rh 95 to 5 wt.%. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, 15.5 C.

Example 8. Everything is the same as in example 2, with the difference that as the mesh material of the platinum catalyst used alloy Pt - 92,5 and Rh - 7.5 wt.%. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, 16.5 C.

Example 9. Testing is carried out in the reactor ammonia conversion installation for the production of hydrocyanic acid, working under atmospheric pressure, with a capacity of 19 tons per day in terms of 98.5% HCN (an example of one of the schemes of this installation, see the book: SBC, Skimino. "Prussic acid", Moscow: Chemistry, 1970, str-120). Working diameter mesh platinum catalyst 1150 mm as the mesh of the platinum catalyst used package of 8 woven platinum meshes with the number of holes 1024/cm2wire dia is. 0,092 mm, made of alloy Pt - 92,5 and Rh - 7.5 wt.% with an initial mass of ~ 9 kg Package grids installed in the reactor between the flanges. The reactor conversion of ammonia supplied with Windows for visual observation of the distribution initiated by the reaction of ammonia conversion on the entire surface of the layer grids. In the reactor there is also a thermocouple for measuring the temperature of the layer grids. As the initial mixture of reactants during start using a gas mixture containing ammonia, methane and air with an initial temperature of 40° C. the Initial mixture under atmospheric pressure and flow 6425 nm3/h (~75% of rate under steady-state operation) served in the reactor. To initiate the reaction of ammonia conversion in the reactor is mounted two elements directly on the surface mesh of the platinum catalyst in parallel to each other at a distance of 400 mm and connect in series in an electrical circuit. Elements similar to the elements used in example 1. The total resistance of the two elements is ~ 2 Ohms. Elements connected to an AC power source described in example 1. Testing is carried out as follows. In the reactor the conversion of ammonia serves process air flow 5025 nm3/h in a mixture of methane (flow rate of the methane - 870 nm3/h) and ammonia (flow rate of ammonia 530 nm3 /hour) at a concentration of ammonia in the mixture ~ 8,2%. At the start of the supply of ammonia elements connected to a source of electricity for the first period of the connection. The duration of the connection elements to an electrical power source is 10 C. During this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equal to 2.5 values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, 16.5 C.

Example 10. Testing is carried out in the reactor conversion of ammonia production unit has synthesis of (NH2OH)2×H2SO4working under atmospheric pressure, with a capacity of 48 tons per day (an example of one of the schemes of this installation, see the book: Assadian, VEGAKON, Viewsindian and others, "caprolactam", Ed. by Viewindicate and Wroczynski, Moscow: Chemistry, 1977, p.122-124, 129, 130). Working diameter mesh platinum catalyst 2900 mm as the mesh of the platinum catalyst used package of 3 woven platinum meshes with the number of holes 1024/cm2wire dia. 0,092 mm, made of alloy Pt - 92,5 and Rh - 7.5 wt.% with the touch mass of ~ 18 kg The service grid is installed in the reactor between the flanges. The reactor conversion of ammonia supplied with Windows for visual observation of the distribution initiated by the reaction of ammonia conversion on the entire surface of the layer grids. In the reactor there is also a thermocouple for measuring the temperature of the layer grids. As the initial mixture of reactants during start using a gas mixture containing ammonia, oxygen and steam with an initial temperature of 100° C. the Initial mixture under atmospheric pressure and flow 4995 nm3/h (~65% of flow rate under steady-state operation) served in the reactor. To initiate the reaction of ammonia conversion in the reactor is mounted six elements directly on the surface mesh of the platinum catalyst in parallel to each other at a distance of 400 mm and connected in-series in an electrical circuit. Elements similar to the elements used in example 1. The total electrical resistance of six linear electrical elements is ~ 16 Ohms. Elements connected to an AC power source described in example 1. Testing is carried out as follows. In the reactor the conversion of ammonia serves oxygen with a flow rate of 945 nm3/h in a mixture with water vapor (the flow rate of the water vapor - 3650 nm3/h) and ammonia (flow rate of ammonia 400 nm3/hour) at a concentration and Miaka in a mixture of ~ 8 vol.%. Elements connected to a source of electricity. The duration of the connection elements to an electrical power source is 10 C. During this heat localized areas of the surface of the catalyst, equivalent to the diameter of which is equal to 2.5 values of the equivalent diameter of the outer element. The duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, amounted to 16 C.

From the comparison of the results in examples 1-3, 6-10 with similar results on the prototype method it is possible to conclude that the use of the present invention can reduce the duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the mesh platinum catalyst with 20-25 C (method-prototype) to 18-15,5, 10%-22,5% and thus significantly improve the security of the process of initiating the reaction of conversion of ammonia on the surface mesh of the platinum catalyst when using linear electrical elements.

From a comparison of the results from examples 1-3 with similar results for example 4 shows that the duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package smokable off supply of electric power, some visually stopwatch, amounted to 22 C, which exceeds the value for the prototype method. It should be noted that the initiation of reaction, the conversion of ammonia on the net platinum catalyst in this case was able to realize an average experience of five, i.e. in four experiments, the reaction of ammonia conversion is not instantiated.

From a comparison of the results from examples 1-3 with similar results to example 5 shows that the duration of the period of time of initiation of the reaction of conversion of ammonia on the entire surface of the catalyst package nets after power outages, some visually stopwatch, 15.5 C. However, for each test the proposed method in this case would inevitably have been observed or burning of local areas of the surface mesh of the platinum catalyst, or violation of the integrity of the linear electric heating elements due to the high values of electric power, which is unacceptable in industrial use.

1. The method of initiating the reaction of ammonia conversion to mesh the platinum catalyst by passing through the gas mixture containing ammonia and oxygen-containing gas, in which periodically heat localized areas of the surface of the catalyst to a temperature of initiation of the reaction is the use of a linear electrical elements, located directly on the catalyst surface, characterized in that the heat localized areas of the surface of the catalyst, equivalent to the diameter of which is chosen in the range from 1 to 5 values equivalent diameter of the outer element, and the elements connected to a source of electricity with the duration of the connection, which take in the appropriate range from 20 to 1 C.

2. The method according to claim 1, characterized in that as the mesh material of the platinum catalyst used alloys Pt - 81, Pd - 15, Rh - 3.5 and EN - 0.5 wt.%; Pt - 92,5, Pd - 4.0 and Rh - 3.5 wt.%; Pt - and Rh 95 to 5 wt.%, Pt - 92,5 and Rh - 7.5 wt.%.



 

Same patents:

FIELD: chemical industry.

SUBSTANCE: 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.

EFFECT: the invention ensures high activity, selectivity and stability of the catalyst to thermocycles at its use in two-stage catalytic system with a decreased loading of platinoid screens.

8 cl, 1 tbl, 5 ex

FIELD: chemical industry; production of nitric acid.

SUBSTANCE: 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.

EFFECT: the invention ensures simplification of the method, decreased investments and specific consumption of fuel.

4 cl, 1 dwg

The invention relates to a device and method of removal of N2About during the manufacture of nitric acid

The invention relates to a catalyst and process for the oxidation of ammonia in the production of weak nitric acid

The invention relates to the production of nitrous oxide by oxidation of ammonia with oxygen or oxygen-containing gas

The invention relates to processes of high-temperature catalytic conversion of ammonia in a two-stage catalytic system in the production of nitric acid

The invention relates to a method of heat recovery nitrous and tail gas emissions in installations for the production of nitric acid

The invention relates to catalysts and methods of producing nitrous oxide (N2O) by oxidation of ammonia with oxygen or oxygen-containing gas

The invention relates to catalysts and methods of producing nitrous oxide (N2O) by oxidation of ammonia with oxygen or oxygen-containing gas

The invention relates to catalysts and methods of producing nitrous oxide (N2O) by oxidation of ammonia with oxygen or oxygen-containing gas

Reactor // 2246345

FIELD: chemical industry, catalytic processes.

SUBSTANCE: the invention presents a reactor for catalytic processes and is dealt with the field of chemical industry and may be used for catalytic processes. The reactor contains: a body; units of input and output for a reaction mixture and products of reactions; units of loading and unloading of a catalyst; a catalyst layer with the groups of the parallel hollow gas-permeable chambers located on it in height in one or several horizontal planes and each of the chambers has a perforated gas-distributing pipe with impenetrable butt connected to the group collector and used for input of additional amount of the reaction mixture. Each of perforated gas-permeable chambers is supplied with the second gas-distributing pipe with impenetrable butt. At that the impenetrable butts of the pipes are located on the opposite sides. The given engineering solution provides uniformity and entirety of agitation of the reaction mixtures.

EFFECT: the invention provides uniformity and entirety of agitation of the reaction mixtures.

5 cl, 4 dwg

The invention relates to a method for producing ammonia from a synthesis gas containing nitrogen and hydrogen, at a granular catalyst in at least one reactor under a pressure in the range from 50 to 300 bar and at a temperature in the range from 100 to 600°C; and from the reactor the mixture of products containing pairs of NH3divert, cooled, and the ammonia condenses and is separated with the formation of the recirculation gas, which is mixed with fresh synthesis gas and return the recirculated gas as synthesis gas in the reactor

The invention relates to the chemical industry and for the distribution system is a collection of fluid for a device designed to bring into contact fluid and solids, where the device contains a camera, at least one conduit for introducing a primary fluid and at least one pipeline to drain the primary fluid and multiple distribution plates, each of the distribution plates contains multiple panels for mixing, distribution or extraction of fluid (RSA)

The invention relates to a reactor for heterogeneous synthesis and upgrade in-situ such a reactor, in particular for the exothermic synthesis, for example, synthesis of ammonia or methanol, and for the conversion of carbon monoxide, which has at least one layer of catalyst radial or axial to radial type using type with opposite cylindrical perforated walls for entry and exit of gases

The invention relates to the production of TETRAFLUOROMETHANE used as a solvent, a foaming agent, in the manufacture of foams, as dry provide the Etchant electronic circuits

The invention relates to chemical technology, namely reactors for processing hydrocarbon gases and can be used in devices for production of synthesis gas for further use in methanol synthesis, Fischer-Tropsch, fuel cells, heating and hot water systems for generating heat

The invention relates to methods for carrying out heterogeneous catalytic reactions

FIELD: chemical industry; methods of production of sulfuric acid.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the method of oxidation of sulfur dioxide and may be used in oxidation of sulfur dioxide into trioxide in production of sulfuric acid both from elemental sulfur and sulfur-containing minerals (pyrite), and at purification of sulfur-containing industrial gases outbursts. The method of oxidation of sulfur dioxide provides for a gating through of the gaseous reaction mixture containing even sulfur dioxide and oxygen through a catalyst layer providing oxidation of sulfur dioxide into sulfur trioxide. At that use the catalyst representing a geometrically structured system made out of microfilaments of a 5-20 microns diameter and having the active centers, which are characterized in IR spectrums of adsorbed ammonia by availability of an absorption band with the wave numbers in the range of v = 1410-1440 cm-1 containing an active component and a highly siliceous fibrous carrying agent defined characterized by availability in a spectrum of nuclear magnetic resonance (NMR)29 Si lines with chemical shifts - 100±3 m.d. (line Q3) and - 110±3 m.d. (line Q4) at a ratio of the integrated intensities of the lines Q3/Q4 0.7-1.2, in the IR spectrum of an absorption band of the hydroxyl groups with a wave number ν = 3620-3650 cm-1 and a half-width of 65-75 cm-1 having a specific surface measured by method BET by a thermal desorption of an argon, SAr = 0.5-30 m2 / g, the value of the surface, measured by a method alkaline titrating SNa= l0-250 m2 / g at the ratio of SNa/SAr = 5-30. An active component of the catalyst is one of the platinum group metals, mainly platinum. The invention allows to increase a conversion in one adiabatic layer of the catalyst up to 80-85 %, to increase a maximum permissible concentration of sulfur dioxide in the initial blend. At that a mechanical stability of a catalyst layer is also ensured making it possible to create different types of catalyst layers.

EFFECT: the invention ensures a significant increase of a conversion in one adiabatic layer of the catalyst, an increase of a maximum permissible concentration of sulfur dioxide in the initial blend and creation of different types of the catalyst layers.

4 cl, 2 ex

Up!