Catalyst system and method of reducing nox

FIELD: chemistry.

SUBSTANCE: invention relates to a catalyst system and a method of reducing nitrogen oxide emissions. The described catalyst system for reducing NOx contains: a catalyst having a support which contains at least one compound selected from a group consisting of aluminium oxide, titanium dioxide, zirconium dioxide, cerium oxide, silicon carbide and mixtures thereof, a catalytic metal oxide containing at least one of gallium oxide or silver oxide and at least one activating metal selected from a group consisting of silver, cobalt, molybdenum, tungsten, indium or mixtures thereof; and a gas stream containing oxygen ranging from approximately 1 mol % to approximately 12 mol % and an organic reducing agent selected from a group consisting of alcohol, carbonate or combinations thereof, where the said organic reducing agent and the said NOx are present in molar ratio carbon: NOx ranging from approximately 0.5:1 to approximately 24:1. A catalyst system for reducing NOx which contains the following is described: a catalyst consisting of (i) metal oxide support which contains aluminium oxide, (ii) at least one of the following oxides: gallium oxide or silver oxide, present in amount ranging from approximately 5 mol % to approximately 31 mol %; and (iii) an activating metal or a combination of activating metals, present in amount ranging from approximately 1 mol % to approximately 22 mol % and selected from a group consisting of silver, cobalt, molybdenum, tungsten, indium and molybdenum, indium and cobalt, and indium and tungsten; and a gas stream containing (A) water in range from approximately 1 mol % to approximately 12 mol %; (B) oxygen in the range from approximately 1 mol % to approximately 15 mol %; and (C) an organic reducing agent containing oxygen and selected from a group consisting of methanol, ethanol, butyl alcohol, propyl alcohol, dimethyl carbonate or combinations thereof; where the said organic reducing agent and NOx are present in molar ratio carbon: NOx ranging from approximately 0.5:1 to 24:1. Also described are methods of reducing NOx which involve the following steps: providing a gas mixture and bringing the said gas mixture into contact with above described catalysts for reducing NOx (versions).

EFFECT: reduced ill effects of air contamination caused by by-products of incomplete high-temperature combustion of organic substances.

21 cl, 34 ex, 4 tbl

 

The technical field to which the invention relates

The present invention generally relates to a catalytic system and method of recovery of emissions of nitrogen oxides, more particularly to a catalytic system which comprises a multi-component catalyst and reducing agent.

For a long time been looking for ways to reduce the harmful effects of air pollution caused by-products resulting from incomplete high temperature combustion of organic substances. When combustion occurs in the excess air and at high temperatures, it creates harmful by-products such as nitrogen oxides, commonly known as NOx. It was assumed that the NOxand its derivatives play a major role in the formation of the ozone layer of the Earth, which is associated with asthma and other respiratory diseases. NOxalso contributing to the formation of soot, which is associated with a number of serious health effects, as well as in acid rain and deterioration of river mouths. As a result, emissions of NOxgoverned by many regulations that limit the amount of NOxthat may be present in the gas stream released into the environment.

One known method when working with NOxincludes the use of selective kataliticheski the th reductant (SCR) to restore the NO xto nitrogen gas (N2using ammonia (NH3) as a reductant. However, because the inherent ammonia dangerous consequences is well known, the use of NH3in the SCR system is more environmental and other issues that also need to pay attention. While regulators continue to reduce the limits on the emissions of NOx, other normative documents, in addition, reduce the allowable levels of NH3that can be released into the atmosphere. Due to regulatory limits on the content of ammonia is a very attractive use of hydrocarbons and their oxygenated derivatives to restore the NOxin SCR technology. With this purpose have been proposed numerous catalysts comprising zeolites, perovskites and metals on a metal oxide carrier. However, existing catalytic systems have either low activity or a narrow temperature range or low stability with respect to water, which is harmful in their practical use. U.S. patent No. 6703343 discloses a catalytic system for use in the restoration of NOx. However, these catalytic systems require specially synthesized metal oxide catalyst carrier with a very low level of impurities. P is there a need for an efficient catalytic system for the recovery of emissions of NO xwhile this system is stable and operating in a wide temperature range.

The invention

The authors of the present invention installed catalytic systems, which are surprisingly effective when using commercially available metal oxide carriers of the catalyst with the usual impurities. Thus, in one embodiment, the present invention proposes a catalytic system for recovery of NOxwhile specified catalyst system includes a catalyst containing a metal oxide carrier, the catalytic metal oxide containing at least one of the oxides of: gallium oxide or silver oxide, and at least one activator metal selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and mixtures thereof. The catalytic system further includes a gas flow formed by the organic reducing agent containing oxygen.

In another embodiment, the present invention proposed catalytic system for recovery of NOxspecified catalyst system includes a catalyst consisting of (i) metal oxide carrier containing alumina, (ii) at least one of the oxides of: gallium oxide or silver oxide is, present in a quantity in the range of from about 5 mol.% to about 31 mole%; and (iii) an activating metal or a combination of the activating metals present in the range of from about 1 mol.% to about 22 mol.%, and selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and molybdenum, indium and cobalt and indium and tungsten. The catalytic system further includes a gas stream containing (A) water in the range of from about 1 mol.% to about 12 mol.%; (B) oxygen in the range of from about 1 mol.% up to about 15 mol.%; and (C) an organic reducing agent comprising oxygen and a compound selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, dimethyl ether, dimethylcarbonate and combinations thereof. Organic reducing agent and NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1.

In yet another embodiment of the present invention, a method for recovery of NOxthat includes the stages of: providing a gas mixture containing NOxand an organic reducing agent containing oxygen, and contacting the gas mixture with the catalyst. The catalyst includes a metal oxide carrier, the catalytic metal oxide containing at least one of oxide is: gallium oxide or silver oxide, and at least one activator metal selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and mixtures thereof.

In yet another embodiment of the present invention, a method for recovery of NOxthat includes the stages of: providing a gas stream containing (A) NOx; (B) water from about 1 mol.% to about 12 mol.%; (C) oxygen is from about 1 mol.% up to about 15 mol.%; and (D) an organic reducing agent containing oxygen, selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, simple dimethyl ether, dimethylcarbonate and combinations thereof; and contacting the specified gas stream with a catalyst consisting of (i) metal oxide carrier containing at least one representative selected from the group consisting of aluminum oxide, titanium dioxide, zirconium dioxide, silicon carbide and oxide series; (ii) at least one of the oxides of: gallium oxide or silver oxide in the range from about 5 mol.% to about 31 mole%; and (iii) an activating metal or a combination of the activating metals in the range of from about 1 mol.% to about 22 mol.%, and selected from the group consisting of silver; cobalt; molybdenum; tungsten; India and molybdenum; India and cobalt and indium and tungsten; where the specified organisasjonsstudier and specified NO xare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1 and in which the specified contact is carried out at a temperature in the range of from about 100°C to about 600°C and with a bulk velocity in the range of from about 5000 hours-1to about 100000 hours-1.

Various other distinctive features, aspects and advantages of the present invention will become clearer based on the following description and the accompanying claims.

Detailed description of the invention

In the following description and is shown then the claims will be made reference to a number of terms that should be defined as having the following values. The singular includes the plural, unless the context clearly indicates otherwise.

In one embodiment, the present invention includes a catalytic system for the selective reduction of NOxspecified catalyst system includes a catalyst and a reducing agent. The catalyst includes a metal oxide carrier, the catalytic metal oxide and an activating metal. The reducing agent includes oxygen-containing organic compound.

Metal oxide carrier may include aluminum oxide, titanium dioxide, zircon dioxide is I, dioxide series, silicon carbide or any mixture of these substances. Typically, metal oxide carrier comprises gamma-alumina with a high surface area containing impurities of at least about 0.2 wt.% in one embodiment, and at least about 0.3 wt.% impurities in the other. Metal oxide media can be obtained by any method known to experts in the art, such as, for example, coprecipitation, spray drying the Sol-gel method.

The catalyst includes a catalytic metal oxide. In one embodiment, the catalytic metal oxide comprises at least one of the oxides of: gallium oxide or silver oxide. In a specific embodiment, the catalyst comprises from about 5 mol.% to about 31 mole% gallium oxide. In another specific embodiment, the catalyst includes from about 12 mol.% to about 31 mole% gallium oxide. In another specific embodiment, the catalyst includes from about 18 mol.% to about 31 mole% gallium oxide, and in all cases, the molar percentage determined by dividing the number of moles of the catalytic metal on the total number of moles of the metal components in the catalyst including the catalyst carrier and any present an activating metal. Drugom specific embodiment, the catalyst comprises about 0.5 mol.% to about 31 mole% silver oxide. In another specific embodiment, the catalyst includes from about 10 mol.% up to about 25 mol.% silver oxide. In another specific embodiment, the catalyst includes from about 12 mol.% up to about 20 mol.% silver oxide, and in all cases, the molar percentage determined by dividing the number of moles of the catalytic metal on the total number of moles of the metal components in the catalyst, including metal components of the catalyst carrier and any present an activating metal. The catalyst also comprises at least one activating metal. Activating the metal may include at least one of silver, cobalt, molybdenum, tungsten or India. Additionally activating the metal may also be a combination of more than one of these metals. The catalyst generally comprises from about 1 mol.% to about 22 mol.% the activating metal. In some embodiments, the implementation of the catalyst includes from about 1 mol.% to about 12 mol.% activating metal and in some other embodiments, the implementation of from about 1 mol.% to about 7 mol.% the activating metal. In one specific embodiment, the catalyst includes from about 1 mol.% to about 5 mol.% the activating metal. Note that the term "kiviruusu metal" is intended to cover the metals in the form of simple elements, metal oxides or salts of activating metal such as, for example, Co2O3. In one specific embodiment, in which the catalytic metal oxide comprises silver oxide, the catalytic system must additionally include at least one activator metal selected from the group consisting of cobalt, molybdenum, tungsten, indium and mixtures thereof.

The catalysts can be obtained by wet technologies, including the use of a homogeneous and pre-mixed solutions of precursors for catalytic metal oxide and an activating metal in contact with the metal oxide catalyst carrier. The oxide particles of the metal catalyst carrier is usually calcined before use solution predecessor. In some embodiments, the implementation stage of the primary annealing is conducted from about 80°C to about 120°C for about 1-2 hours, after which carry out the basic process of annealing. Such annealing may be performed at a temperature in the range of from about 500°C to about 800°C. In some embodiments, the implementation of the annealing performed at a temperature in the range of from about 650°C to about 725°C. In some embodiments, the implementation of p is ukalyvanie is carried out for from about 2 hours to about 10 hours. In some other embodiments, implementation of the annealing is carried out for from about 4 hours to about 8 hours. Particles sieved to select and use those, which have a diameter of approximately from 0.1 to about 1000 microns. In one embodiment, the area size of the particles is set in the range of from about 2 microns to about 50 microns in diameter. Based on the value of the surface area and total pore volume of the catalyst carrier in the form of particles of metal oxide can then be calculated desired catalyst loading. As will be clear to experts in the field techniques, surface area and porosity may be a value that approximately 20-30% lower in the final catalytic product resulting from the catalytic filling. The content of the catalyst is determined total pore volume of the carrier, which is the volume of the metal precursors, which can be filled due to the source of the moisture. Filling predecessor pick up so that the quantity of metal was usually reduced value in comparison with the monolayer of active metal oxide on the metal oxide catalyst carrier. In some embodiments, the implementation uses double pore volume as the total volume of the precursor to the implementation of the Taco filling and the filling metal is chosen in the range from about 1 mmol to about 5 mmol of a mixture of catalytic metal oxide and an activating metal per gram of metal oxide catalyst carrier.

At the subsequent stages of preparation of the catalyst can be prepared solutions of the precursor catalytic metal oxide and one or more activating metals. The solutions of the precursor can be prepared in aqueous medium, the hydrophilic organic media or in mixtures. Hydrophilic organic medium include carboxylic acids, alcohols and their mixtures, such as without limitation, acetic acid or ethanol. The solutions are usually obtained by mixing the solvent with metal salts, such as, but not limited to these, nitrates metals, salts of citric acid, oxalates, acetylacetonates, molybdates or benzoate, in number, to create a solution corresponding polyarnosti based on the desired composition of the catalyst. In some embodiments, the implementation of the metal salt is a molybdenum heteropolyanions or ammonium molybdate. Used to prepare the catalytic system methods known to experts in the field of technology and include coating the metal oxide catalyst on a carrier having a honeycomb structure, method a thin coating or extrusion pressing suspension in the required form. The purity of the metal precursors, or the catalytic metal oxide, or an activating metal is located is in the range of from about 95 wt.% to about to 99.999 wt.%. In one embodiment, all metal precursors are mixed together and are so homogeneous as possible before adding it to the metal oxide catalyst carrier. In some other embodiments, implementation of the various metal precursors add consistently in the metal oxide catalyst carrier. In one embodiment, the required volume of solution precursor added to cover the metal oxide catalyst carrier and create a catalyst with the desired final catalyst loading. As soon as the solution or solutions of metal salt added to the metal oxide catalyst carrier, the catalyst may not necessarily be left to bear from about 6 to 10 hours in some versions of the implementation. The catalyst was then dried for a certain period of time at the required temperature. In a specific embodiment, the catalyst may be dried in a vacuum, not necessarily in a stream of nitrogen. Finally, the catalyst may be calcined at the required temperature and for the required time to create the final catalyst product.

The catalysts according to the typical variants of implementation of the present invention can be created using either manual or automated methods. the AK rule, manual method used to prepare catalysts with a large weight, such as from about 1 to about 20 grams (g). The automated method is typically used when the catalysts have a lower weight, such as from about 5 milligrams (mg) to about 100 mg. Generally manual and automated methods of preparation of the catalyst is similar except that the automated method includes automated measurement and distribution solutions of metal oxide precursors on the catalyst carrier.

The reducing agent for use in the catalytic system according to the typical variants of implementation of the present invention includes oxygen-containing organic compound. These oxygen-containing organic compounds are liquid-gas mixture or in the form of liquid or gas, so they can flow through the catalyst, when introduced into the stream of exhaust gas for use in a catalytic system for recovery of NOx. Generally, oxygen-containing hydrocarbons with less than about 16 carbon atoms are liquid, while oxygen-containing hydrocarbons with a large number of carbon atoms may also be liquid, for example, depending on the chemical structure and temperature vasovasotomy. Oxygen-containing organic compounds suitable for use as reducing agents, typically include a representative selected from the group consisting of alcohol, simple ester, complex ester, carboxylic acid, aldehyde, ketone, carbonate, and combinations thereof. In some embodiments, the implementation of oxygen-containing organic compounds suitable for use as reducing agents include at least one functional group selected from the group consisting of hydroxy, alkoxy, carbonyl, carbonate, and combinations thereof. Some non-limiting examples of oxygen-containing organic compounds suitable for use as reducing agents include methanol, ethanol, 1-butanol, 2-butanol, 1-propanol, isopropanol, dimethyl ether, dimethylcarbonate and combinations thereof.

The catalytic system can be used in cooperation with any process or system in which it may be desirable to reduce the emissions of NOxsuch as gas turbine, steam turbine, boiler, locomotive or mobile exhaust system, such as, but not limited to, a diesel exhaust system. The catalytic system can also be used in interaction with systems, which includes education is the use of gases from the combustion of coal, combustion of volatile organic compounds (VOC) or by burning plastics, or on the plants to obtain a silicon dioxide, or plants for the production of nitric acid. The catalyst is usually placed inside the exhaust system, where it will be subjected to exhaust gas containing NOx. The catalyst may be located in the reactor with thickened or fluidized bed deposited on the monolith, foam, mesh or membrane structure, or be located in any other way within the exhaust so that the catalyst was in contact with the exhaust gas.

As will be understood by skilled specialists in the field of technology, despite the fact that the catalytic reaction is generally complex and involve many stages, the total primary selective catalytic reduction reaction of when restoring NOxbelieved to be as follows:

NOx+ O2+ organic reducing agent → N2+ CO2+ H2O (1)

This flue gas stream typically includes air, water, CO, CO2, NOxand may optionally contain other impurities. In addition, can also be present in the off-gas flow nevosplamenauschayasa or not completely burning the fuel. Organic reducing agent is usually in the up in the flow of exhaust gas for forming the gas mixture, which is then passed through the catalyst. A sufficient amount of oxygen to support the reduction reaction of NOxmay already be present in the off-gas flow. If present in the gas mixture of oxygen is not sufficient for the reduction reaction of NOxadditional oxygen gas may also be introduced into the stream of exhaust gas in the form of oxygen or air. In some embodiments, the implementation of the gas stream comprises from about 1 mol.% to about 21 mol.% gas oxygen. In some other embodiments, the implementation of the gas stream comprises from about 1 mol.% up to about 15 mol.% gas oxygen.

According to variants of implementation of the present invention advantage is that the reduction can take place in conditions of "depleted by the restorer." That is, the amount of reducing agent, which is added to the flue gas to recover NOxusually low. Reducing the quantity of reducing agent to convert the NOxin the nitrogen can provide a more efficient process, which will decrease the cost of raw materials. The molar ratio of reductant to NOxis usually in the range of about 0.25:1 to about 6:1. In other embodiments, implementation of the specified relationship is usually such that the ratio of carbon atoms to reset the novitel is from about 0.5 to about 24 moles per mole of NO x. In some other embodiments, the implementation of the organic reducing agent and NOxare present in a molar ratio of carbon:NOxin the range of about 0.5:1 to about 15:1. In a specific embodiment, the organic reducing agent and NOxare present in a molar ratio of carbon:NOxin the range from about 0.5:1 to about 8:1.

The reduction can take place in a wide range of temperatures. As a rule, the temperature in one embodiment, may be in the range of from about 100°C to about 600°C, in another embodiment from about 200°C to about 500°C and in another embodiment from about 350°C to about 450°C.

The reduction can take place in the conditions under which the gas mixture is prepared so as to have a space velocity in one embodiment in the range from about 5000 hours-1to about 100000 hours-1in another embodiment, in the range of from about 8000 hours-1to about 50000 hours-1in one embodiment in the range from about 8000 hours-1to about 40000 hours-1.

Typical embodiments of the catalytic system can also successfully be used in wet conditions. Specific embodiments of restore what means NO xthat brings to end the use of typical embodiments of the present invention can be effective in the exhaust gas containing water. In some embodiments, the implementation of the gas stream comprises from about 1 mol.% to about 12 mol.% water and in some other embodiments, the implementation of from about 2 mol.% up to about 10 mol.% water.

Without further elaboration, the inventors believe that any qualified specialist in the field of technology, using the steps in this job description, can utilize the present invention in its entirety. The following examples are included to provide additional explanations to the experts in this field regarding the practical implementation of the claimed invention. The proposed examples are only illustrative examples, which contribute to the explanation given in this application. Accordingly, the examples are in no way intended to limit the invention, which is defined in the attached claims.

Examples

Catalysts were prepared and used in combination with reducing agents in accordance with exemplary embodiments implementing the present invention. The conversion of NOxanalyzed using warioware the experimental conditions, including the variation of the composition of the catalyst, the reducing agent, the temperature of the reaction and attitude of a reducing agent to

NOx.

In the following examples, the catalyst samples were prepared so that each contained a catalyst carrier of gamma-dioxide aluminum, commercially available Saint-Gobain NorPro of Stow, Ohio. The catalyst carrier of aluminum oxide had a purity from 99.5% to 99.7 per cent. The catalyst carrier of aluminum oxide was first probalily at 725°C for 6 h in the presence of an oxidant. The oxidant may be air or oxidant gas containing from about 1% to about 21% oxygen in nitrogen. The aluminium oxide particles were then sieved to select catalyst carrier, having a diameter with a particle size of from about 450 microns to about 1000 microns. Before loading the carrier of the catalyst had a surface area of approximately 240 m2/g and pore volume coefficient was 0.796 ml/year

Gallium was used as the metal catalytic metal oxide which was added to the alumina. Gallium was added in soluble form to hydrate carrier of aluminum oxide and obtained from a solution of gallium nitrate having the formula Ga(NO3)3·6H2O. the Solution was obtained by combining deionized water with gallium nitrate having a purity of 99,999% (base metals)obtained Alfa-Aesar of Ward Hill, Massachusetts. Water, subjected to ultra-filtration, having a specific resistance of 18 Mω·cm was used in all operations. For activating metal aqueous solution of the nitrate salt of the desired metal(s), with a purity of 99,999% (base metals) and obtained from Alfa-Aesar, was added to the media aluminum oxide. All metal precursors were mixed together and were so homogeneous as possible before adding to the medium aluminum oxide. The catalysts were sustained for 6 to 10 hours and then dried under dynamic vacuum in a stream of nitrogen for 4 to 5 hours at 80°C. At the final stage of the dried catalyst was heat-treated. Temperature curve when the treatment began to increase from 25°C to 110°C and 1.4°C/min, the Catalyst was kept at 110°C for 1.5 hours, then the temperature quickly linearly increased at 5°C/min to a value of 650°C. the Catalyst was kept for 6 hours at this temperature and then allowed him to cool down for approximately 4 to 6 hours.

The catalysts were tested in 32-tube microreactor with a highly efficient screening of heterogeneous catalyst. The reactor consisted of a conventional heated distribution manifold with a free space, which is evenly distributed flow of reagent through th the data capillaries in parallel tubes of the reactor. The collector was heated device that allows pre-heating of the flow of the reagent and the evaporation of liquid reagents prior to distribution. All of the heated manifold was mounted vertically on a floating table which is raised and lowered by pneumatic pressure. The tube reactor was inserted in gold-plated 10-centimeter (cm) thick insulated copper reactor block (with dimensions of 13.5 cm×25 cm), which was heated in order to vary the temperature from 200°C to 650°C.

Chemically inert KALREZ (TM) o-ring, obtained from DuPont of Wilmington, Delaware, served as viscoelastic mechanical seals at either end of each tube of the reactor. Tube reactor made of INCONEL 600 pipe (TM) with an outer diameter 0,635 cm and an inner diameter of 0,457 cm, obtained from Inco Alloys/Special Metals of Saddle Brook, New Jersey. The tube was free to slide vertically through gold-plated copper heating block. Each tube contains a glass fiber Frit, in which the catalyst samples about 0,050 g were placed in the center of each of the pipes through which the flow of the mixed reagent gas mixture containing NOxand a reducing agent, and imitated the transmitted stream of exhaust gas. Used only bypass pipe to ensure equal the flow through each of the 32 test tubes. The fitting was connected to the distribution manifold for delivery of the mixed gas mixture. Components of the mixed gas of the mixture was applied on a common manifold for mixing, using electronic mass flow controllers, and then distributed on the manifold. The pressure in the distribution manifold was maintained at about 275,8 kPa. The reactor temperature and flow control were fully automated.

After loading in the tube catalysts were thermally treated air stream, as described in this description previously, and then interacted with the mixed gas mixture. The reactor stream is sent to the heated valves sampling, which was consistently selected tube and filed a continuous stream on the chemiluminescent analyzer. Any thread that has not been sent to the analytical device, sent to a common gate.

Diverter valve for routing gases operated by computer, and they were brought into effect in accordance with a predefined synchronized sequence. Chemiluminescent analyzer is connected by a data-logging system based on the use of the computer. Data corresponding to the reactor the composition of the flow tube are assigned timestamps, and they remained in memory. Data from the bypass pipe is also kept in memory as reference information on the input composition of the tubes of a catalytic reactor. This allowed us to combine data for determining the activity and selectivity of each sample of the catalyst.

To test the recovery of NOxthe flow of the mixed reagent gas mixture consisted of a reducing agent, and about 200 ppm NOx, 12% vol. oxygen, 7% vol. water and the remainder nitrogen. The type and amount of reducing agent in the stream varied depending on the conducted experiments. The flow rate of the mixed gas mixture through each of the tubes was 33 NCM3rpm pipe.

Table 1 shows the compositions of the prepared samples of the catalyst in the form of a composition, expressed in mole percent for each activating metal and/or the catalytic metal present in the catalyst. The remainder of the composition is an aluminum oxide as catalyst carrier of aluminum oxide. The molar percentage was determined for each component by dividing the number of moles of the specified component to the total number of moles of the metal components in the catalyst, including metal components of the metal oxide catalyst carrier. Comparative example 1 consists only of a carrier of aluminum oxide.

Table 1
ExampleGa InAgCoMoW
Comparative example 1000000
Comparative example 22900000
Comparative example 3020000
Comparative example 4040000
Comparative example 5002000
Comparative example 6 005000
Comparative example 72720000
Example 12702000
Example 22504000
Example 32700200
Example 42500400
Example 5252200
Example 62230300
Example 72700020
Example 82500050
Example 92200080
Example 102230030
Example 1121600 0
Example 122700002
Example 132500004
Example 142000008
Example 152260001
Example 162130003

Was conducted the first series of experiments, in which different catalyst samples were prepared and tested with various reducing agents, using the described testing procedure at 350°C. the Data in table is e 2 show the percentage of the converted NO xfor each of the catalytic systems. Non of the examples and comparative examples in table 2 correspond to the catalytic compositions in examples and comparative examples of table 1. Although the molar ratio of reductant to NOxvaries depending on the use of the reducing agent, the molar ratio of carbon:NOxusually is approximately 2:1 for each of the experimental systems. The abbreviation "NBA" means 1-butanol.

Table 2
Reductants
ExampleMeOHEtOHi-DNBA
Comparative example 112353035
Comparative example 218323331
Comparative example 329352833
Comparative example 426344332
Comparative example 56246642
Comparative example 67143621
Example 112599755
Example 22143019
Example 315343130
Example 443562546
Example 542462841
Example 6 34393339

As shown in table 2, example 1, which is characterized by a combination of gallium oxide as a catalytic metal oxide and silver as the activating metal, showed especially good results when using reducing agents, such as ethanol, isopropanol and 1-butanol. Example 4 containing gallium and cobalt showed good characteristics with methanol, ethanol and the NBA. Examples 5 and 6 containing cobalt, indium and gallium, also showed good characteristics with methanol, ethanol and 1-butanol.

Held a second series of experiments, in which different catalyst samples were prepared and tested with various reducing agents, using the described testing procedure at 400°C. the Data in table 3 show the percentage of the converted NOxfor each of the catalytic systems. Non of the examples and comparative examples in table 3 correspond to the catalytic compositions described in the examples and comparative examples of table 1. Although the molar ratio of reductant to NOxvaries depending on the use of the reducing agent, the molar ratio of carbon:NOxusually equal to about 6:1 for each of the experimental systems. The abbreviation "DMC", "IPA"and "NBA" means dimethylcarbonate, isopropyl alcohol and 1-butanol, respectively.

Table 3
The catalytic compositionThe restorer
ExampleGaInAgCoMoWMeOHDMCEtOHIPANBA
Comparative example 229000002038575557
Comparative example 30200001834 556156
Comparative example 50020002130959683
Comparative example 727200002848625457
Example 327002001779494237
Example 622303 001849404033
Example 727000202844605256
Example 825000503454767065
Example 922000805077443141
Example 1022 300303562473342
Example 1121600102525652821
Example 1227000023755192268
Example 1325000045332282421
Example 1420000086536303129
Example 1522600012458501355
Example 1621300034164602261

While all catalyst samples showed good or improved performance compared with the samples of comparative examples, in particular the sample of example 8, containing 5 mol.% molybdenum and 25 mol.% gallium, showed good results with the seven five oxidizing reducing agents. In General, the catalytic system in accordance with typical choices of implementation and this method was successful in restoring a certain amount of NOxin each instance.

Held the third series of experiments, in which the methanol was tested as a reductant at 400°C in the presence of a gas mixture containing 200 ppm NOx, 4%water and 13% O2and residual nitrogen at a nominal flow rate 28000 h-1. Catalytic compositions along with the activity of the catalyst for each experiment are given in table 4. The molar balance of the catalyst includes a metal oxide catalyst carrier. Although the molar ratio of reductant to NOxvaries depending on the use of the reducing agent, the molar ratio of carbon:NOxusually equal to about 6:1 for each of the experimental systems. The catalyst activity is expressed in moles of NOxconverted to N2per gram of catalyst per hour.

Table 4
ExampleThe catalytic compositionThe restorer
GaAg InMeOH
Example 1766195,2E-06
Example 1861313l,0E-05
Example 1961961,6E-05
Example 20136135,2E-06
Example 21019132,0E-05
Example 22013195,9E-07
Example 2329208,4E-08
Example 2401616Example 25911111,1E-05
Example 26516101,6E-5
Comparative example 831006,3E-07

Various embodiments of the present invention is described to meet the different needs that the invention meets. It should be recognized that these embodiments of are simply an illustration of the principles of various embodiments of the present invention. Numerous modifications and adaptations of the invention are obvious to experts in the field of technology without derogating from the meaning and features of the present invention. Thus, it is assumed that the present invention covers all suitable modifications and variations that fall in the scope of the claims appended claims and their equivalents.

1. Catalytic system for recovery of NOxcontaining: the catalyst containing the medium containing at least one representative selected from the group consisting of aluminum oxide, titanium dioxide, zirconium dioxide, cerium dioxide, silicon carbide and mixtures thereof, a catalytic metal oxide containing at least one of gallium oxide or silver oxide, and at least one activator metal selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and mixtures thereof; and
the gas stream containing oxygen in the range of from about 1 mol.% to about 21 mol.%, water in the range of from about 1 mol.% to about 12 mol.% and an organic reducing agent selected from the group consisting of alcohol, carbonate and combinations thereof, and
specified organic reducing agent and specified NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1.

2. The catalytic system according to claim 1, in which the specified catalytic metal oxide comprises an oxide of gallium in the range of from about 5 mol.% to about 31 mole%.

3. The catalytic system according to claim 1, in which the specified catalytic metal oxide comprises an oxide of gallium in the range of from about 18 mol.% to about 31 mole%.

4. The catalytic system according to claim 1, in which the specified catalytic metal oxide comprises silver oxide in the range of about 0.5 mol.% to about 31 mole%.

5. The catalytic system according to claim 1, in which the specified catalyst includes himself has specified an activating metal in the range of from about 1 mol.% to about 22 mol.%.

6. The catalytic system according to claim 1, in which the specified catalyst includes activating the specified metal in the range of from about 1 mol.% to about 7 mol.%.

7. The catalytic system according to claim 1, in which the catalytic metal oxide comprises an oxide of gallium and activating the metal comprises silver or a combination of indium and silver.

8. The catalytic system according to claim 1, in which the catalytic metal oxide comprises silver oxide and activating the metal includes indium.

9. The catalytic system according to claim 1, in which the specified organic reducing agent selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, dimethylcarbonate and their combinations.

10. The catalytic system according to claim 1, in which the specified organic reducing agent and specified NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 8:1.

11. The catalytic system according to claim 1, in which the NOxpresent in the stream of exhaust gas from the combustion source, this source of combustion includes at least one of the following: gas turbine, steam turbine, boiler, locomotive, mobile exhaust, coal combustion, incineration of plastics, incineration of volatile organic compounds, plant to produce silicon dioxide sludge the plant for the production of nitric acid.

12. Catalytic system for recovery of NOxcontaining:
a catalyst consisting of (i) metal oxide carrier containing alumina, (ii) at least one of the oxides of: gallium oxide or silver oxide present in amounts in the range of from about 5 mol.% to about 31 mole%; and (iii) an activating metal or a combination of the activating metals present in amounts in the range of from about 1 mol.% to about 22 mol.%, and selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and molybdenum, indium and cobalt, and indium and tungsten; and
the gas stream containing (A) water in the range of from about 1 mol.% to about 12 mol.%; (C) oxygen in the range of from about 1 mol.% up to about 15 mol.%; and (C) an organic reducing agent comprising oxygen and selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, dimethylcarbonate and their combinations;
where specified organic reducing agent and NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1.

13. Method of recovering NOxthat includes stage:
providing a gas mixture containing NOx, water in the range of from about 1 mol.% to about 12 mol.%, the oxygen in the range of from about 1 mol.% to about 21 mol.% and the body is static reducing agent, selected from the group consisting of alcohol, carbonate and combinations thereof, and specified organic reducing agent and specified NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1; and contacting the specified gas mixture with the catalyst, where the specified catalyst includes a carrier containing at least one representative selected from the group consisting of aluminum oxide, titanium dioxide, zirconium dioxide, cerium dioxide, silicon carbide and mixtures thereof, a catalytic metal oxide containing at least one of gallium oxide or silver oxide, and at least one activator metal selected from the group consisting of silver, cobalt, molybdenum, tungsten, India and mixtures thereof.

14. The method according to item 13, wherein said contact is carried out at a temperature in the range of from about 100°C. to about 600°C.

15. The method according to item 13, wherein said contact is carried out at a temperature in the range of from about 200°to about 500°C.

16. The method according to item 13, wherein said contact is carried out with a bulk velocity in the range of from about 5000 h-1to about 100000 h-1.

17. The method according to item 13, wherein said catalytic metal oxide comprises an oxide of gallium in the range of from about 5 mol.% to about 31 mole%.

18. The method according to item 13, in which the ohms specified catalyst includes activating the specified metal is from about 1 mol.% to about 22 mol.%.

19. The method according to item 13, wherein said organic reducing agent selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, dimethyl ether, dimethylcarbonate and their combinations.

20. The method according to item 13, in which the NOxis present in the exhaust gas stream from the combustion source, this source of combustion includes at least one of the following: gas turbine, boiler, locomotive, mobile exhaust, coal combustion, incineration of plastics, incineration of volatile organic compounds, plant to obtain a silicon dioxide or a plant for the production of nitric acid.

21. Method of recovering NOxthat includes stage:
providing a gas stream containing (A) NOx; (C) water, from about 1 mol.% to about 12 mol.%; (C) oxygen is from about 1 mol.% up to about 15 mol.%; and (D) an organic reducing agent containing oxygen, selected from the group consisting of methanol, ethyl alcohol, butyl alcohol, propyl alcohol, dimethylcarbonate and combinations thereof; and
the contacting of the specified gas stream with a catalyst consisting of (i) - catalyst carrier containing at least one member selected from the group consisting of aluminum oxide, titanium dioxide, zirconium dioxide, carb is Yes silicon dioxide and cerium;
(ii) at least one of the oxides of: gallium oxide or silver oxide in the range of from about 5 mol.% to about 31 mole%; and (iii) an activating metal or a combination of the activating metals in the range of from about 1 mol.% to about 22 mol.%, and selected from the group consisting of silver, cobalt, molybdenum, tungsten, indium and molybdenum, indium and cobalt, and indium and tungsten,
where specified organic reducing agent and specified NOxare present in a molar ratio of carbon:NOxfrom about 0.5:1 to about 24:1; and in which the specified contact is carried out at a temperature in the range of from about 100°C. to about 600°C and with a bulk velocity in the range of from about 5000 h-1to about 100000 h-1.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to organic chemistry and petrochemistry, particularly to designing and using catalysts. Described is a catalyst for dehydrogenation of isopentane and isopentane-isoamylene fractions based on platinum and tin, deposited on a carrier - zincalume spinel. The catalyst is distinguished by that, the carrier is in form of nanocrystalline particles with average crystal size of 22-35 nm with components in the following ratio, wt %: platinum - 0.05-2.0, tin - 0.1-6.0, zincalume spinel - the rest. Also described is a method of preparing said catalyst, involving grinding and mixing oxygen-containing zinc and aluminium compounds, gradual addition of water until obtaining a homogeneous pasty mass, stirring and moulding, drying the granules at room temperature and calcination, subsequent saturation of the formed carrier with an aqueous solution of platinum and tin compounds, final drying of the catalyst mass in air; the method is distinguished by that, the carrier is calcined while gradually raising temperature to 800-900°C at a rate of 10-200°C/hour, and then for 5-40 hours at 850-1000°C, while constantly controlling size of the formed crystals until formation of nanocrystalline particles with average crystal size of 22-35 nm.

EFFECT: increased efficiency of dehydrogenation process due to increased output of isoprene, with high selectivity on dehydrogenation products, as well as due to longer inter-regeneration period of the catalyst.

3 cl, 1 tbl, 14 ex

FIELD: chemistry.

SUBSTANCE: present invention refers to naphtha reforming catalyst. There is disclosed a catalyst effective in naphtha reforming involving particles of heat-resistant inorganic oxide carrier containing dispersed bivalent tin, platinum group metal and rhenium and optionally halogen, characterised that tin uniformly coats the catalyst, and platinum group metal uniformly coats the catalyst; tin is impregnated into the carrier with using tin chelate resulted from reaction of chelating agent representing amino acid and bivalent tin salts. There is also disclosed catalytic reforming of naphtha as feed stock, wherein feed stock contacts with said catalyst in reforming environment involving temperature 315°C-600°C, pressure 100 KPa - 7 MPa (abs.), liquid hourly space velocity 0.1-20 h-1, and molar ratio of hydrogen to naphtha feed stock 1-20.

EFFECT: new naphtha reforming catalyst and new catalytic reforming of naphtha.

10 cl, 2 dwg, 1 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: present invention refers to catalytic system and to the method of reduction of nitrogen oxides emissions using the said system. The described catalytic system for NOx reduction contains: the catalyst containing the metal oxide substrate, catalytic metal oxide which is gallium oxide or silver oxide or both of them and initiating metal chosen from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth and their mixtures, gas flow containing the organic reducing agent and sulfur-containing substance. The described catalytic system for NOx reduction contains: the catalyst consisting of (i) the metal oxide substrate, containing aluminium oxide, (ii) catalytic metal oxide which is gallium oxide or silver oxide or both of them in quantity 1-31 mole %; and (iii) initiating metal or their combination selected from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth, indium and wolfram, silver and cobalt, indium and molybdenum, indium and silver, bismuth and silver, bismuth and indium and molybdenum and indium in quantity 1-31 mole %, gas flow containing (A) water in quantity 1-15 mole %; (B) gaseous oxygen in quantity 1-15 mole %; and (C) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations; and sulfur oxide; where at the specified organic reducing agent and NOx are present in approximate molar ratio carbon to NOx from 0.5:1 to 24:1. The described method of NOx reducing includes the stages of gaseous mixture containing NOx, organic reducing agent and sulfur-containing substance inflow and of said gaseous mixture contact with specified catalyst. The described method of NOx reduction includes: inflow of gaseous mixture containing (A) NOx, (B) water in quantity 1-15 mole %; (C) oxygen in approximate quantity 1-15 mole %; (D) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations and (E) sulfur oxide; and contact of said gaseous mixture with catalyst described above and containing the specified components in the defined molar ratio.

EFFECT: improved action of the catalyst.

35 cl, 10 tbl, 84 ex

FIELD: chemistry.

SUBSTANCE: description is given of a method of obtaining olefins. The method involves passing a mixture of a hydrocarbon and oxygen containing gas through a catalyst zone, which is capable of maintaining burning over the upper limit the inflammability of the fuel, with obtaining of the above mentioned olefin. The catalyst zone consists of at least, a first layer of catalyst and a second layer of catalyst, where the second catalyst layer is put in the process line after the first catalyst layer, has different content from the first layer and has general formula: M1aM2bM3cOz, where M1 is chosen from IIA, IIB, IIIB, IVB, VB, VIB, VIIB groups of lanthanides and actinoides, M2 is chosen from IIA, IB, IIB, IIIB, IVB, VB, VIB groups, and M3 is chosen from IIA, IB, IIB, IIIB, IVB, VB, VIB and VIIIB groups, a, b, c and z represent atomic ratios of the M1, M2, M3 and O components respectively. The value of a lies in the interval from 0.1 to 1.0, the value of b lies in the interval from 0.1 to 2.0, the value of c lies in the interval from 0.1 to 3.0, and the value of z lies in the interval from 0.1 to 9.0. The catalyst zone has a perovskite type structure.

EFFECT: perfection of the method of obtaining olefins.

9 cl, 4 tbl, 1 dwg, 4 ex

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention provides isodewaxing catalyst for petroleum fractions containing supported platinum and modifiers wherein supporting carrier is fine powdered high-purity alumina mixed with zeolite ZSM 5 in H form having SiO2/Al2O3 molar ratio 25-80 or with zeolite BETA in H form having SiO2/Al2O3 molar ratio 25-40 at following proportions of components, wt %: platinum 0.15-0.60, alumina 58.61-89.43, zeolite 5-40, tungsten oxide (modifier) 1-4, and indium oxide (modifier) 0.24-0.97. Preparation of catalyst comprises preparing carrier using method of competitive impregnation from common solution of platinum-hydrochloric, acetic, and hydrochloric acids followed by drying and calcinations, wherein carrier is prepared by gelation of fine powdered high-purity alumina with the aid of 3-15% nitric acid solution followed by consecutive addition of silicotungstenic acid solution and indium chloride solution, and then zeolite ZSM 5 in H form having SiO2/Al2O3 molar ratio 25-80 or with zeolite BETA in H form having SiO2/Al2O3 molar ratio 25-40.

EFFECT: increased yield of isoparaffin hydrocarbons.

7 cl, 2 tbl, 7 ex

The invention relates to the refining and petrochemical industries

The invention relates to the field of catalysis selective hydrogenation

The invention relates to the refining sector, namely the catalytic reforming of the original naphtha

The invention relates to a catalyst for purification of gases from nitrogen oxides mainly in the presence of methane and oxygen, the conversion of natural gas and the method of its production

FIELD: chemistry.

SUBSTANCE: invention relates to catalysts for pyrazinamide synthesis during reaction of oxidative ammonolysis methylpyrazine. Alkyl-substituted pyrazines and their derivatives have high biological activity, which enables their wide use as medicinal agents for different purposes. Described is a catalyst for synthesis of oxidative ammonolysis methylpyrazine containing vanadium pentoxide and titanium dioxide and modifying additives from a group of elements of oxidative nature such as tungsten W or molybden Mo, with the following content of components, wt %: V2O5 10-29, TiO2 70-79, WoO3 or MoO3 1-10. Also described is a method of producing pyrazinamide through oxidative ammonolysis methylpyrazine in the presence the catalyst described above.

EFFECT: proposed catalysts enable production of pyrazinamide in a single step and increase total output of pyrazinamide and pyrazinonitrile.

2 cl, 8 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: present invention refers to catalytic system and to the method of reduction of nitrogen oxides emissions using the said system. The described catalytic system for NOx reduction contains: the catalyst containing the metal oxide substrate, catalytic metal oxide which is gallium oxide or silver oxide or both of them and initiating metal chosen from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth and their mixtures, gas flow containing the organic reducing agent and sulfur-containing substance. The described catalytic system for NOx reduction contains: the catalyst consisting of (i) the metal oxide substrate, containing aluminium oxide, (ii) catalytic metal oxide which is gallium oxide or silver oxide or both of them in quantity 1-31 mole %; and (iii) initiating metal or their combination selected from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth, indium and wolfram, silver and cobalt, indium and molybdenum, indium and silver, bismuth and silver, bismuth and indium and molybdenum and indium in quantity 1-31 mole %, gas flow containing (A) water in quantity 1-15 mole %; (B) gaseous oxygen in quantity 1-15 mole %; and (C) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations; and sulfur oxide; where at the specified organic reducing agent and NOx are present in approximate molar ratio carbon to NOx from 0.5:1 to 24:1. The described method of NOx reducing includes the stages of gaseous mixture containing NOx, organic reducing agent and sulfur-containing substance inflow and of said gaseous mixture contact with specified catalyst. The described method of NOx reduction includes: inflow of gaseous mixture containing (A) NOx, (B) water in quantity 1-15 mole %; (C) oxygen in approximate quantity 1-15 mole %; (D) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations and (E) sulfur oxide; and contact of said gaseous mixture with catalyst described above and containing the specified components in the defined molar ratio.

EFFECT: improved action of the catalyst.

35 cl, 10 tbl, 84 ex

FIELD: chemistry.

SUBSTANCE: claimed invention relates to catalyst of olefin monomers trimerisation. Described is catalytic composition for olefin monomers trimerisation, which contains a) source of chrome, molybdenum or tungsten; b) ligand if general formula (I), in which X stands for bivalent organic group, selected from substituted or non-substituted alkylene groups, in case of substituted groups, substituents represent hydrocarbon groups; R1 and R3 represent cycloaromatic groups, which do not contain polar substituents in none of orto-positions; R2 and R4 are independently selected from obligatory substituted cycloaromatic groups, each of R2 and R4 having polar substituent in at least one orto-position; and c) cocatalyst. Also described is method of olefin monomers trimerisation, including interaction of at least one olefin monomer in conditions of trimerisation reaction with said above catalytic composition.

EFFECT: selective obtaining 1-hexagen from ethylene, reducing level of formation of by-products, especially C10.

10 cl, 2 tbl, 12 ex

The invention relates to the production of odorants for natural gas, in particular waste-free way to obtain mercaptan, as well as to a method for producing a catalyst, providing a higher degree of interaction between methyl alcohol and hydrogen sulfide and the use of such a method of producing hydrogen sulfide, which provides waste reduction production in General

FIELD: chemistry.

SUBSTANCE: present invention refers to catalytic system and to the method of reduction of nitrogen oxides emissions using the said system. The described catalytic system for NOx reduction contains: the catalyst containing the metal oxide substrate, catalytic metal oxide which is gallium oxide or silver oxide or both of them and initiating metal chosen from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth and their mixtures, gas flow containing the organic reducing agent and sulfur-containing substance. The described catalytic system for NOx reduction contains: the catalyst consisting of (i) the metal oxide substrate, containing aluminium oxide, (ii) catalytic metal oxide which is gallium oxide or silver oxide or both of them in quantity 1-31 mole %; and (iii) initiating metal or their combination selected from the group consisting of silver, cobalt, molybdenum, wolfram, indium, bismuth, indium and wolfram, silver and cobalt, indium and molybdenum, indium and silver, bismuth and silver, bismuth and indium and molybdenum and indium in quantity 1-31 mole %, gas flow containing (A) water in quantity 1-15 mole %; (B) gaseous oxygen in quantity 1-15 mole %; and (C) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations; and sulfur oxide; where at the specified organic reducing agent and NOx are present in approximate molar ratio carbon to NOx from 0.5:1 to 24:1. The described method of NOx reducing includes the stages of gaseous mixture containing NOx, organic reducing agent and sulfur-containing substance inflow and of said gaseous mixture contact with specified catalyst. The described method of NOx reduction includes: inflow of gaseous mixture containing (A) NOx, (B) water in quantity 1-15 mole %; (C) oxygen in approximate quantity 1-15 mole %; (D) organic reducing agent selected from the group consisting of alcanes, alkenes, alcohols, ethers, esters, carboxylic acids, aldehydes, ketones, carbonates and their combinations and (E) sulfur oxide; and contact of said gaseous mixture with catalyst described above and containing the specified components in the defined molar ratio.

EFFECT: improved action of the catalyst.

35 cl, 10 tbl, 84 ex

FIELD: chemistry.

SUBSTANCE: catalytic composition contains compounds of formula: Mo1VaSbbNbcMdOx, in which Mo represents molybdenum, V stands for vanadium, Sb stands for antimony, Nb stands for niobium, M represents gallium, a constitutes from 0.01 to 1, b constitutes from 0.01 to 1, c constitutes from 0.01 to 1, d constitutes from 0.01 to 1, and x is determined by requirements of valency of other present elements.

EFFECT: increase of alkane conversion degree, increase of selectivity of catalytic composition in one stage process of alkane transformation into unsaturated carbonic acid.

9 cl, 1 tbl, 12 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to chemistry of heterogeneous catalysts and is directed to production of high-octane gasoline component via alkylation of isobutane with butane-butylene fraction on heterogeneous catalysts. Solid catalyst represents porous superacid based on zirconium and/or hafnium metallosilicates promoted with salts of double- or triple-charged metal cations with double-charged anions and depicted by general formula (EO2·aSiO2)·b(McXd) wherein E = Zr and/or Hf, a=17-34; b=0.5 when c=1 and d=1, M= Ni2+, Zn2+, or ZrO2+, X=SO42- or ZrF62-; or b=0.1666 when c=2 and d=3, M=Sc3+, Y3+, or Ga3+ and X= SO42-, parameter "a" being allowed to deviate from indicated value to larger or lesser side by 20% and parameter "b" by 5%. High-octane gasoline component is produced as indicated above at temperature 348 to 375 K, pressure 1.7 to 2.5 MPa, isobutane-to-butenes molar ratio 10-15, and volume feed supply velocity between 6.4 and 8.5 g/mL catalyst/h. Catalyst can optionally be regenerated.

EFFECT: enhanced conversion, yield of alkylate, productivity, and prolonged catalyst lifetime.

7 cl, 4 tbl, 11 ex

FIELD: oxidation catalysts.

SUBSTANCE: invention relates to carbon monoxide oxidation catalysts suitable to remove carbon monoxide from emission gases. Catalyst according to invention contains cadmium telluride and indium antimonide at weight ratio 95:5.

EFFECT: increased activity and selectivity of catalyst.

1 tbl

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention relates to processes for hydrocarbon feedstock conversion into aromatic hydrocarbons, in particular to light hydrocarbon aromatization process catalysts, to catalyst preparation processes, and aromatic hydrocarbon production processes. A composite light hydrocarbon aromatization process catalyst is described, which contains acidic microporous component with pore size at least 5 Å and oxide component exhibiting dehydrogenation activity and selected from aluminum hydroxide and/or oxide having transportation pore size at least 20 nm, said oxide component having been treated with promoter element compounds. Described are this catalyst preparation method and aromatic compound production process in presence of above-described catalyst.

EFFECT: increased activity and selectivity regarding formation of aromatic hydrocarbons and stabilized functioning of catalyst.

11 cl, 1 tbl, 23 ex

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