The activation method palladium catalyst
(57) Abstract:Usage: petrochemicals, isomerization of butene-1 in the butenes-2. The inventive palladium catalyst on the carrier activated by treatment with a mixture of hydrogen and from 0.5 to 7.5%. vol.% of carbon monoxide at 120-250°C. the Characteristics of the catalyst: conversion of butene - 1 82,7-95,0%; selectivity 94,7 of 97.8%. table 1. The invention relates to the field of petrochemical industry, specifically to methods of structural isomerization of butene-1 in the butenes-2 in the presence of palladium catalyst on the carrier. The invention relates to the production of olefins, in particular of receipt of butenes-2, representing a mixture of TRANS - and CIS-isomers of normal structure, used in the manufacture of butadiene, methyl ethyl ketone, and for other purposes.Known catalysts structural isomerization of butene-1 - metals of group VIII (Vi, Co, Fe, Pd, Rh) on the media, which allow for the isomerization of butene-1 in the butenes-2 at low temperatures (below 100aboutC), but with insufficient depth conversion - 70-80% and a selectivity of 80%, due to active leakage adverse reactions of hydrogenation, cracking and skeletal isomerization of butene-1.It is known that activation or reaction is e hydrogen at a temperature of 80-480aboutC.The closest in technical essence and the achieved result is the activation method palladium catalyst on activated carbon by passing hydrogen through the catalyst bed, which allows the subsequent conduct isomerization of butene-1 at 80-200aboutC and a flow rate of 500-1000 h-1with a conversion of 82% and a selectivity of 92% (the prototype).The disadvantage of this method is the low productivity of the catalyst raw materials (low activity) and the lack of selectivity of the process.The purpose of the invention to increase the activity and selectivity of palladium catalyst on a carrier.This goal is achieved by the proposed method of processing palladium catalyst on a carrier with a mixture of hydrogen and carbon monoxide content of 0.5 to 7.5% vol. of carbon monoxide at 120-250aboutC.Distinctive features of the method are the treatment of the catalyst with a mixture of hydrogen and carbon monoxide content of 0.5 to 7.5% vol. of carbon monoxide at 120-250aboutC.As a source of hydrogen using the hydrogen-containing gas, comprising at least 50 vol.% hydrogen and inert impurities (nitrogen, methane, ethane, etc.). Oxide and its content above 7.5% decrease in activity and selectivity of the process.As a carrier for the palladium used aluminum oxide or activated carbon in the form of grains or pellets.The method is as follows. The catalyst in the form of immobile layer is loaded into the reactor, representing a metal tube heated purge the system with nitrogen and serves the hydrogen-containing gas. The reactor is heated from 5 to 10aboutper hour up to the activation temperature 120-250aboutC and maintain the temperature selected within the specified limits, for 10-30 hours, then cooled in a stream of hydrogen containing gas to a predetermined operating temperature isomerization. The specified processing of the catalyst is carried out at elevated pressure, and the lower limit of the pressure is determined by the resistance of the catalyst layer, and the upper and technological needs.On activated as described palladium catalyst serves butene-1 or a hydrocarbon fraction containing butene-1 and hydrogen at a ratio of butene-1: hydrogen equal to 10-100 mol/mol.The process of structural isomerization of butene-1 is carried out at a temperature of 80-160aboutC and a pressure of not more than 10 ATM with volumetric feed rate of the hydrocarbon feedstock 1000-5000 h-1(the volumetric rate of Rotana-1 82,7-95% with a selectivity 94,7 of 97.8%.The possibility of implementation of the method is confirmed by the following examples.The results of the experiments are summarized in table, where the conditions of activation of the catalyst and results from testing of the catalyst in the isomerization process.P R I m e R 1. Charged to the reactor 10.0 cm3palladium catalyst (2.5 wt. % palladium on aluminium oxide), purge it with nitrogen, and then served bogorodskii gas of the following composition,%: Hydrogen 85 Oxide 5 carbon, Nitrogen, methane, ethane, argon Others
Noah in the amount of 100 nl/h at a pressure of 10 ATM. Heat the reactor from room temperature to 250aboutWith raising temperature speed 8-10about/hour. At a temperature of 250aboutTo maintain the catalyst for 10 hours, then cooled to 110aboutWith and reduce the pressure to 5 ATM.Through the catalyst passed 900 g of butene-1 (basic substance content 99% ) with a bulk velocity of 5000 h-1; simultaneously feeding hydrogen in an amount such that the molar ratio of butene-1:hydrogen was 100 mol/mol.Get 901,6 g of product containing, g: Butene-1 44,0 Amount of TRANS - and CIS-butene-2 802,0 n-butane 46,6 Impurities 9.0 Degree of conversion of butene-1 is 95,1% when the selective behaviour is on charcoal), purge it with nitrogen, and then serves the hydrogen-containing gas of the following composition,%: Hydrogen 92.0 Monoxide 0.5 Nitrogen, methane and other inert impurities Others
Noah in the amount of 50 nl/h at normal pressure. The reactor is heated to 120aboutWith heating rate of 4-5aboutC/hour. At a temperature of 120aboutTo activate the catalyst for 24 h, after which the reactor is cooled to 80aboutC. Through the reactor is passed 500 g of butylene-isobutilene fraction of the following composition, wt. % : Butene-1 40,0 n-butane 12,0 isobutylene 32,0 Isobutane 13.5 Divinyl 0,5 other hydrocarbons 2.0 isomerization Process is carried out at 80aboutC, a pressure of 1.2 ATM. with volumetric feed rate 1000 h-1and hydrogen in an amount of 0.1 mol per 1 mol of butene-1.Get 500,5 g hydrocarbon fraction of the following composition, wt.%: Butene-1 7,0 Amount of TRANS - and CIS-butene-2 32,0 n-butane 13.5 isobutylene 31,9 Isobutane 13,6 other hydrocarbons 2.0 Conversion of butene-1 in these conditions is 82,7% with selectivity to 95.5%.P R I m e R 3. Charged to the reactor 10 cm3palladium catalyst (1.6 wt. % palladium on aluminium oxide), purge it with nitrogen, and then serves the hydrogen-containing gas of the following composition,%: Hydrogen 90,0 carbon Monoxide 2,5 Ine is the temperature with a speed of 7-8aboutC/hour. At a temperature of 200aboutWith continued activation of the catalyst for 30 h, after which the reactor is cooled to 120aboutC. Through the reactor is passed 1000 g of butene-1 (basic substance content 99%) with a bulk velocity of 2500 h-1, feeding simultaneously hydrogen in an amount such that the molar ratio of butene-1:hydrogen was 50 mol/mol. Get 1000,7 g of product containing Butene-1 70,0 Amount of TRANS - and CIS-butene-2 900,0 n-butane 20,7 Impurities 10.0 Conversion of butene-1 is of 92.9% with the selectivity of the process of 97.8%.P R I m e R 4. The process is carried out analogously to example 1 with the only difference that the activation of the palladium catalyst is carried out in a current of hydrogen-containing gas of the following composition,%: Hydrogen 90,0 carbon Monoxide 7,5 Inert impurities 2.5 Degree of conversion of butene-1 is 92,5% with the selectivity of the process is 97.6%.P R I m e R 5. The process is carried out analogously to example 1 with the only difference that during activation, the catalyst is heated to 300aboutC and incubated for 10 h at this temperature.Through the reactor is passed 500 g of butene-1 (basic substance content 99%) under the same conditions as in example 1.Get 500,9 g of product containing, g: the effectiveness of the process in 94.7%, i.e. increasing the activation temperature from 250 to 300aboutWith virtually no effect on the activity and selectivity of the catalyst.P R I m e R 6. The process is carried out similarly to the conditions of example 1 with the only difference that passed through the catalyst 900 g of butene-1 with a bulk velocity of 7000 h-1.The conversion of butene-1 is of 91.3% with a selectivity of 94.5%.P R I m e R 7. The process is carried out analogously to example 1 with the only difference that the activation of the palladium catalyst is carried out in a current of hydrogen-containing gas of the following composition,%: Hydrogen 85,0 carbon Monoxide 10,0 Inert impurities 5,0
The conversion of butene-1 is 67,1 when selectivity to 78.3%, i.e. an increase in the content of carbon monoxide above stated results in decreased conversion of butene-1 and the selectivity of the process.P R I m e R 8. The process is carried out similarly to the conditions of example 1 with the only difference that the activation of the catalyst is carried out at a pressure of 15 ATM. After activation through the reactor is passed 900 g of butene-1 in the same conditions as in example 1, obtaining the same results in the conversion of butene-1 and the selectivity of the process.P R I m e R 9. The process is carried out analogously to example 2 with that is passed 500 g of butene-1 in the same conditions, as in example 4.Get 500,6 g of product containing, g: Butene-1 250,0 Amount of TRANS - and CIS-butene-2 209,0 n-butane 16,0 Impurities 15,6
The conversion of butene-1 is a 50.5%, while the selectivity of the process 85,3% , i.e., the activation at a temperature below stated, gives a catalyst having low activity and selectivity.P R I m e R 10. The process is carried out under the conditions of example 2 with the only difference that the activation of the catalyst is carried out in a current of hydrogen-containing gas of the following composition,%: Hydrogen 92.0 Monoxide 3,0 Inert impurities 5.0 and the isomerization of butene-1 is carried out with a bulk velocity of 2000 h-1the degree of conversion of butene-1 is the 87.3% with a selectivity to 95.7%.P R I m e R 11. The process is carried out under the conditions of example 3 with the only difference that the isomerization of butene-1 is carried out at flow rate of 4000 h-1. Under these conditions, the conversion of butene-1 is 91.5% at a selectivity 96,7%.P R I m e R 12. The process is carried out under the conditions of example 3 with the only difference that the activation of the catalyst is carried out in a current of hydrogen-containing gas of the following composition,%: Hydrogen 85,0 carbon Monoxide 10,0 Inert impurities 5,0
The conversion of butene-1 sostiniu conversion of butene-1 and the selectivity of the process. The ACTIVATION METHOD PALLADIUM CATALYST on a carrier for the structural isomerization of butene-1 in the butenes-2 by treating the catalyst with hydrogen at elevated temperature, characterized in that the treatment is carried out with a mixture of hydrogen and carbon monoxide content of 0.5 to 7.5% vol. carbon oxide at 120 - 250oC.
FIELD: organic chemistry, chemical technology, catalysts.
SUBSTANCE: invention relates to a method for preparing acetic acid by gas-phase oxidation of ethane and/or ethylene with oxygen using catalyst comprising molybdenum and palladium. For realization of method gaseous feeding comprising ethane, ethylene or their mixture and oxygen also are contacted at enhanced temperature with catalyst that comprises elements Mo, Pd, X and Y in combination with oxygen of the formula (I): MoaPdbXcYd wherein X and Y have the following values: X means V and one or some elements optionally taken among the following group: Ta, Te and W; Y means Nb, Ca and Sb and one or some elements optionally taken among the following group: Bi, Cu, Ag, Au, Li, K, Rb, Cs, Mg, Sr, Ba, Zr and Hf; indices a, b, c and d mean gram-atom ratios of corresponding elements wherein a = 1; b = 0.0001-0.01; c = 0.4-1, and d = 0.005-1. Niobium is added to the catalyst structure using niobium ammonium salt. Preferably, niobium ammonium salt is used as the niobium source. The continuance of contact time and composite values of the parent gaseous mixture are so that taken to provide output value by acetic acid to be above 470 kg/(m3 x h). The selectivity of oxidation reaction of ethane and/or ethylene to acetic acid is above 70 mole %. Invention provides enhancing stability and output of catalyst.
EFFECT: improved preparing method.
14 cl, 1 tbl, 6 ex
FIELD: petrochemical synthesis catalysts.
SUBSTANCE: invention discloses a method for preparation of palladium catalyst comprising impregnation of alumina carrier with palladium chloride solution in presence of aqueous hydrochloric acid, treatment with reducing agent (hydrogen), washing with water, and drying, said carrier being preliminarily decoked exhausted catalyst containing alumina and group I and/or II, and/or VI, and/or VIII metals and subjected to washing with aqueous hydrochloric or nitric acid and then with water. Exhausted ethylene oxide production catalyst or methylphenylcarbinol dehydration catalysts can also be suitably used.
EFFECT: increased selectivity and activity of catalyst.
2 cl, 2 tbl, 21 ex
FIELD: supported catalysts.
SUBSTANCE: invention claims a method for preparation of catalyst using precious or group VIII metal, which comprises treatment of carrier and impregnation thereof with salt of indicated metal performed at working pressure and temperature over a period of time equal to or longer than time corresponding most loss of catalyst metal. According to invention, treated carrier is first washed with steam condensate to entirely remove ions or particles of substances constituted reaction mixture, whereupon carrier is dried at 110-130oC to residual moisture no higher than 1%.
EFFECT: achieved additional chemical activation of catalyst, reduced loss of precious metal from surface of carrier, and considerably increased lifetime.
5 cl, 9 ex
FIELD: petrochemical process catalysts.
SUBSTANCE: preparation of catalyst comprises applying palladium compound onto silica cloth and heat treatment. Palladium compound is applied by circulation of toluene or aqueous palladium acetate solution through fixed carrier bed until palladium content achieved 0.01 to 0.5%. Palladium is introduced into cloth in dozed mode at velocity preferably between 0.1 and 5.9 mg Pd/h per 1 g catalyst. Heat treatment includes drying at temperature not higher than 150oC under nitrogen or in air and calcination in air or nitrogen-hydrogen mixture flow at temperature not higher than 450oC. Original silica cloth can be modified with 0.6 to 6.5% alumina. Palladium is uniformly distributed in silica cloth and has particle size preferably no larger than 15 Å. Invention can be used in treatment of industrial gas emissions and automobile exhaust to remove hydrocarbons.
EFFECT: deepened oxidation of hydrocarbons.
5 cl, 1 tbl, 4 ex
FIELD: hydrogenation-dehydrogenation catalysts.
SUBSTANCE: palladium-containing hydrogenation catalyst, which can be used to control rate of autocatalytic hydrogenation reactions, is prepared by hydrogen-mediated reduction of bivalent palladium from starting compound into zero-valence palladium and precipitation of reduced zero-valence palladium on carbon material, wherein said starting material is tetraaqua-palladium(II) perchlorate and said carbon material is nano-cluster carbon black. Reduction of palladium from starting compound and precipitation of zero-valence palladium on carbon material are accomplished by separate portions.
EFFECT: increased catalytic activity, enabled catalyst preparation under milder conditions, and reduced preparation cost.
1 dwg, 1 tbl, 12 ex
FIELD: hydrogenation-dehydrogenation catalysts.
SUBSTANCE: preparation of catalyst comprises depositing active components on γ-alumina carrier at stirring, carrier being preliminarily treated with concentrated NaOH solution. Active components are deposited consecutively in three steps. In the first step, preliminarily prepared chitosan in acetic acid solution with KCl solution is deposited for 60-65 min; in the second step, sodium tetrachloropaladate(II) trihydrate Na2PdCl4·3H2O solution is deposited for 60-65 min; and, in the third step, hydrazine hydrate solution as reducing agent is added for 180-240 min. After each step, resulting suspension is filtered off, washed, and dried at 293-303K for 1-2 h in vacuum. Catalyst can be used in chemical industry and in processing of industrial and household wastes.
EFFECT: enhanced nitrate hydrogenation efficiency.
6 cl, 1 dwg, 6 ex
FIELD: textile, paper and chemical industries; protection of environment in production of bleachers, biocides and components of oxidizing processes.
SUBSTANCE: proposed catalyst contains one or more metals of platinum group used as active component, one or more polyolefines and activated carbon carrier. It is preferably, that polyolefines have molecular mass above 400 and are selected from ethylene homopolymers and ethylene copolymers with alpha-olefines, propylene homopolymers and propylene copolymers with alpha olefines, butadiene homopolymers and copolymers with styrene and other olefines, isoprene homopolymers and copolymers with other olefines, ethylene-propylene copolymers, ethylene-propylene diolefine three-component copolymers, thermoplastic elastomers obtained from butadiene and/or isoprene and styrene block-copolymers, both hydrogenized and non-hydrogenized. Hydrogen peroxide is produced in presence of said catalyst from hydrogen and oxygen in reaction solvent containing halogenated and/or acid promoter. Proposed catalyst makes it possible to increase degree of conversion and selectivity of process, to obtain aqueous H2O2 solutions at content of acids and/or salts at level of trace amount.
EFFECT: enhanced efficiency.
48 cl, 1 tbl,18 ex
FIELD: industrial organic synthesis and catalysts.
SUBSTANCE: invention relates to a methyl ethyl ketone production process via catalytic oxidation of n-butenes with oxygen and/or oxygen-containing gas. Catalyst is based on (i) palladium stabilized with complexing ligand and (ii) heteropolyacid and/or its acid salts, in particular molybdo-vanado-phosphoric heteropolyacid having following composition: H11P4Mo18V7O87 and/or acid salt Na1.2H9.3Mo18V7O87, said complexing ligand being notably phthalocyanine ligand. Catalyst is regenerated by making it interact with oxygen and/or oxygen-containing gas at 140-190°C and oxygen pressure 1 to 10 excessive atmospheres. Oxidation of n-butenes is conducted continuously in two-stage mode at 15 to 90°C in presence of above-defined catalyst.
EFFECT: enhanced process efficiency due to increased stability of catalyst resulting in considerably increased productivity and selectivity.
7 cl, 1 dwg, 3 tbl, 8 ex
FIELD: organic synthesis catalysts.
SUBSTANCE: catalyst for modifying colophony contains, as carrier, high-porosity cellular α-alumina-based block material and, as active catalyst fraction, sulfated group IV metal oxide and metallic palladium.
EFFECT: increased modification rate due to developed catalyst surface and eliminated disintegration and carry-over of catalyst.
FIELD: reduction-oxidation catalysts.
SUBSTANCE: invention relates to catalytic chemistry and, in particular, to preparation of deep-oxidation supported palladium catalysts, suitable, for example, in afterburning of motor car exhaust. Preparation involves depositing palladium from aqueous solution of palladium precursors followed by drying and calcination. Precursors are selected from nitrite anionic or cationic palladium complexes [Pd(NO2 -)(H2O)3]Anx or [Pd(NO2 -)n(H2O)m](Kat)y, wherein An are anions of acids containing no chloride ions, Kat is proton or alkali metal cation, n=3-4, m=0-1, x=1-2, and y=1-2. Nitrite ions are introduced into impregnating solution in the form of nitrous acid salts or are created in situ by reducing nitrate ions or passing air containing nitrogen oxides through impregnating solution. Ratio [Pd]/[NO2 -] in impregnating solution is selected within a range 1:1 to 1:4.
EFFECT: eliminated chlorine-containing emissions, increased stability of chlorine-free impregnating solutions, reduced their acidity and corrosiveness, and increased catalytic activity in deep oxidation reactions.
2 cl, 1 tbl, 16 ex
FIELD: petroleum processing catalysts.
SUBSTANCE: invention provides reforming catalyst containing Pt and Re on oxide carrier, in particular Al2O3, wherein content of Na, Fe, and Ti oxides are limited to 5 (Na2O), 20 (Fe2O3), and 2000 ppm (TiO2) and Pt is present in catalyst in reduced metallic state and in the form of platinum chloride at Pt/PtCl2 molar ratio between 9:1 and 1:1. Contents of components, wt %: Pt 0.13-0.29, PtCl2 0.18-0.04, Re 0.26-0.56, and Al2O3 99.43-99.11. Preparation of catalyst comprises impregnation of alumina with common solution containing H2PtCl6, NH4ReO4, AcOH, and HCl followed by drying and calcination involving simultaneous reduction of 50-90% platinum within the temperature range 150-550оС, while temperature was raised from 160 to 280оС during 30-60 min, these calcination conditions resulting in creation of reductive atmosphere owing to fast decomposition of ammonium acetate formed during preparation of indicated common solution.
EFFECT: increased catalytic activity.
2 cl, 1 tbl, 3 ex
FIELD: petrochemical process catalysts.
SUBSTANCE: cobalt-based catalyst precursor is prepared by impregnation of porous catalyst carrier particles with cobalt salt followed by partial drying and subsequent calcination of impregnated carrier, after which calcined product is partially reduced, impregnated with cobalt salt, partially dried and finally calcined. Preparation of Fischer-Tropsch catalyst comprises similar preparation of precursor thereof and reduction of the latter.
EFFECT: increased catalytic activity.
12 cl, 3 dwg, 1 tbl, 2 ex
FIELD: organic synthesis catalysts.
SUBSTANCE: invention relates to a method of preparing hydrocyanation catalyst, which is complex of nickel with bidentate phosphorus-containing compound. Method comprises interaction of at least one bidentate phosphorus-containing ligand, selected from group including bidentate phosphites, bidentate phosphinites, and bidentate phosphines, with nickel chloride in presence of nitrile solvent and reducing metal. The latter is more electropositive than nickel and can be selected form group consisting of Na, Li, K, Mg, Ca, Ba, Sr, Ti, V, Fe, Co, Cu, Zn, Cd, Al, Ga, In, and Sn. Nickel chloride is present in molar excess over reducing metal. Catalyst is prepared preferably at temperature between 30 and 100°C and pressure between 34 and 340 kPa.
EFFECT: lowered reaction temperature and reduced formation of by-products.
16 cl, 22 ex
FIELD: gas treatment catalysts.
SUBSTANCE: invention relates to a method for preparing catalyst and to catalyst supported by block ceramic and metallic carrier having honeycomb structure for treating internal combustion engine exhaust gases. Preparation of catalyst comprises preliminary calcination of inert honeycomb block carrier followed by simultaneously depositing at 550-800°C, on its surface, intermediate coating of modified alumina and active phase consisting of one or several platinum group metals from water-alcohol suspension including aluminum hydroxide (boehmite, AlOOH), cerium nitrate, and one or several inorganic salts of platinum group metals. Coated material is then dried and subjected to heat treatment and reduction. According to invention, aforesaid suspension contains boehmite and cerium nitrate at 1:2 ratio and further contains reducing disaccharide so that suspension has following composition, wt %: AlOOH 18-20, Ce(NO3)3·6H2O 36-40, one or several platinum group metal salts (e.g., H2PtCl6, PdCl3, or RhCl3 calculated as metals) 1.5-1.8, reducing disaccharide 5-6, and water/alcohol (between 5:1 and 10:1) the rest. Thus obtained catalyst for treating internal combustion engine exhaust gases is characterized by: specific surface area of coating 80-100 m2/g, Al2O3 content 2.5-6.5%, CeO2 content 2.5-6.5%, active phase (calculated for platinum group metals) 0.2-0.4%, and block carrier to 100%.
EFFECT: simplified technology due to reduced number of technological stages and shortened process time, and enabled preparation of high-activity catalyst.
6 cl, 1 tbl, 8 ex
SUBSTANCE: invention is referred to the area of hydrocarbons preparation by catalytical hydrodeoxygenation of products of fast pyrolysis of a biomass and working out of the catalyst for this process. The catalyst of oxygen-organic products hydrodeoxygenation of fast pyrolysis of lignocellulose biomasses, containing either precious metal in amount of no more 5.0 wt % or containing nickel, or copper; either iron, or their combination in a non-sulphide restored shape in amount of not more than 40 wt % and transitive metals in a non-sulphide shape in amount of not more than 40 wt %, carrying agent - the rest, is described. Three variants of the catalyst preparation method, providing application of transition metals on the carrying agent by a method of impregnation of the carrying agent solutions of metal compounds are described, or simultaneous sedimentation of hydroxides or carbonates of transition metals in the presence of the stabilising carrier, or the catalyst is formed by joint alloying/decomposition of crystalline hydrate nitrates of transition metals together with stabilising components of zirconium nitrate type. The process of oxygen-organic products hydrodeoxygenation of a biomass fast pyrolysis is performed using the above described catalyst in one stage at pressure of hydrogen less than 3.0 MPa, temperature 250-320°C.
EFFECT: increase stability in processing processes of oxygen-containing organic raw materials with the low content of sulphur, and also soft conditions of process realisation.
10 cl, 12 ex, 2 tbl
SUBSTANCE: invention relates to composition based on gold and reducible oxide, method of its production and its application as catalyst, in particular in carbon monoxide oxidation. Described is composition based on gold on carrier based on reducible oxide, as such composition contains titanium or iron (III) oxide, content of halogen in composition, expressed by molar ratio halogen/gold, constitutes not more than 0.05, content of gold in it constitutes not more than 1%, gold is in form of particles with size not more than 10nm, and composition is subjected to reducing processing. Described is method of composition production, which contains following stages: bringing in contact compound based on reducible titanium or iron (III) oxide and compound based on gold halogenated and, in case of necessity, compound based on silver, with formation of suspension of said compounds, pH of obtained medium being set not lower than 8; separation of solid substance from reaction medium; washing solid substance with alkaline solution; in addition method includes reducing processing after mentioned above washing stage. Described is method of carbon monoxide oxidation, method of air purification and method of cigarette smoke purification using described above composition as catalyst.
EFFECT: elaboration of catalysts, efficient at low temperatures and/or high hour volume rates.
16 cl, 12 tbl, 15 ex
SUBSTANCE: invention relates to production of catalysts and can be used in chemical industry and in production of medications. Described is method of preparing modified platinum catalyst for enantioselective hydration of esters of alfa-ketacarboxylic acids which includes impregnation of hexachloroplatinic acid from solution into pores of prepared carrier, as such supersewn polystyrene is used, by water-absorbing capacity from solution tetrahydrofurane : methanol : water with ratio 4:1:1, mixture of hexachlorplatinic acid and carrier is kept during 10-15 minutes mixed, after which it is dried at 70-75°C, washed with Na2CO3 solution with further reduction of hexachlorplatinic acid, filtering, washing and drying of catalyst and modification with cinchonidine solution.
EFFECT: reduction of time of catalyst preparation, increase of catalyst activity, enentioselectivity and stability.
4 cl, 1 tbl, 3 ex
SUBSTANCE: catalyst for selective hydrogenation of organic compounds contains mesoporous carbon carrier and active part - nanodispersed particles of the VIII group metals with content on the carrier in the range from 1 to 10%. The method for catalyst preparation includes the thermochemical treatment of the carrier, its impregnation with the solution containing active part, and then the metals of VIII group are reduced at first in the alkaline media at ultrasonic action with frequency 35 kHz, then with formaldehyde solution.
EFFECT: enhancing of catalyst activity.
6 cl, 5 dwg, 7 ex