On an industrial scale the formic acid is produced from methyl formate by multi-stage liquid-phase methods characterized a high capital intensity and high energy costs. In Institute of Catalysis the gas-phase method was developed for the synthesis of formic acid by catalytic oxidation of formaldehyde by air oxygen. A pilot plant with the capacity up  and design of apparatus fully reproduce the future industrial process. It includes two catalytic stages: oxidation of methanol to formaldehyde and the oxidation of formaldehyde to formic acid. Methanol is oxidized on the commercial iron oxide-molybdenum catalyst in a traditional conditions. The formaldehyde
is oxidized to the acid on oxide vanadium-titanium catalyst at
temperatures of 120-140 °C. Due to the narrow temperature range on the second step it is used a two-reactor scheme and the partial dilution of the bed with inert packing in the first reactor. Tests were performed at a 6–7 %vol. concentration of methanol in the mixture. and temperature variations in the formaldehyde oxidation reactor. In optimal conditions the acid yield is 87-88% per converted formaldehyde and 79–81 % – for methanol conversion. This is achieved at full methanol conversion, and conversion of formaldehyde 96,5–98,5 %. The technology meets the requirements of «green» chemistry.

Preparation of 2-methyl-1,4-naphthoquinone (vitamin K3) by oxidation of 2-methylnaphthalene and 2-methyl-1-naphthol using the nanostructured gold catalysts supported on hypercrosslinked polystyrene (5 % Au/SPS) was investigated. The effect of temperature on the oxidation process was studied; the attempt was made for replacement of the standard solvent – acetic acid to an environmentally friendly supercritical carbon dioxide. It is found that the use of supercritical CO2 is high (near 100 %), selectivity of the oxidation of 2-methyl-1- naphthol to the desired product is stored, wherein the conversion is increased on 10–15 %. Oxidation of 2-methylnaphthalene using supercritical CO2 leads to a drastic reduction of conversion and selectivity to the desired product, resulting from the fact that under these conditions peracetic acid (main oxidant) is formed. The possibility of using gold nanostructured catalysts for selective oxidation of 2-methyl-1-naphthol and 2-methylnaphthalene in 2-methyl-1,4-naphthoquinone (99 and 58% respectively).

Influence of the nature and content of the promoter and catalyst activity and stability of Pd-Со/δ-Al2O3 и Pd-Zn/δ-Al2O3 bimetallic catalysts in the hydrogenation of diene and vinylaromatic hydrocarbon to BTX fractions was studied by IR spectroscopy and thermoprogrammed recovery. The molar ratio of Pd : Co (Zn) in the prepared samples – 1,0 : 0,5; 1,0 : 1,0; 1,0 : 1,5 the content of Pd – 0,5 wt.%. The support is δ-Al2O3 modified by sodium (0,5 wt.%). It is shown that promotion of cobalt and zinc leads to the disappearance of palladium cation forms, which reduces oligomerization capacity of the active component, and as it was confirmed by the 100-hour catalyst test the stability of the catalyst increases. The results showed that for the hydrogenation process of BTX fraction in industrial conditions it is Pd-Cо/δ-Al2O3(Na) catalyst with a molar ratio of Pd : Co = 1,0: 1,0, for which the expected service cycle operation is 16 months.

The aim of this study was to investigate the possibility to produce the effective catalysts based on new carbon support obtained from the soot and petroleum pitch . Samples of support using a soot marks P 234 , P 514 , P 701 , T 900 are prepared. The palladium containing catalysts (1 wt.% Pd) were prepared on the basis of the obtained samples of supports, also well known carbon supports were taken for comparison – an active carbon AH-3 and Sibunit . All catalyst samples were tested in a model reaction of dehydrogenation of cyclohexane in the temperature range 250-400 °C by pulse method. It is established that catalysts on the new carbon support possess the greater catalytic activity than the catalysts, based on AH-3 and Sibunit. This fact, as well as characteristics of the proposed support, namely large values f specific surface area (up to 200 m2/g) and pore volume (0,4– 1,0 cm3/g), high mechanical strength (up to 8 MPa), low ash (less than 1 wt.%) show that this support is possible to produce an effective metal catalysts for various processes refining, chemical and petrochemical industries.

The ability to prepare bimetallic Au-Cu catalysts by double decomposition of the complex [Au(en)2]2[Cu(C2O4)2]3·8H2O is considered. It is shown that this preparation method allows to selectively receive the nanoparticles of solid solution Au0,4Cu0,6 on the surface of the support. The composition corresponds of the stoichiometry of dual complex salt. Properties of bimetallic Au-Cu/CeO2 and monometallic Au/CeO2 and Cu/CeO2 catalysts were tested in the selective oxidation of CO in a mixture of CO2 and H2O. Experiments were carried out in flow catalytic unit in the temperature range 50–250 °C in a mixture of the following composition vol.%: CO – 1; O2 – 0,6; H2O – 10; CO2 – 20; H2 – 60 and He-balance, with the volume flow rate (WHSV) 276 000 sm3·g–1·h–1. The bimetallic catalyst allowed to oxidize significantly greater amount of CO at a higher selectivity in the presence of CO2 and H2O in a mixture over then the monometallic catalysts. The selective oxidation of carbon monoxide in the presence of hydrogen is a promising method of deep cleaning hydrogen from gaseous mixtures of carbon monoxide. The purified hydrogen gas may be used to power portable power plants based on low temperature proton exchange membrane fuel cell, also for synthesis of ammonia and for hydrogenation processes in thin organic synthesis.

Catalysts based on transition metal oxides are the most promising
for the efficient combustion of fuel in a fluidized bed. Afterburning
coke is a limiting stage of fuel combustion, characterized by the
release of carbon monoxide (CO) and its reacting with oxygen on the catalyst surface. Determination of the observed kinetic parameters of this process will further evaluate the efficiency of the catalyst, and optimize the performance of fluidized bed reactor. The study of the kinetics of CO oxidation on the industrial catalyst SCHKZ-1 (oxide aluminum-copper-chromium), currently used in the fluidized bed reactor when burning fuels. The studies carried out in conditions when the internal diffusion does not affect on the reaction rate. Kinetic parameters of the reaction were evaluated by a first order equation for CO and O2; the obtained values of activation energy and pre-exponential rate constants were respectively ko = 5,23·107 s–1, E = 32,8 kJ/mol. A comparison with published data showed their good correlation .

Operation start of the first commercial plant production of contact anthraquinone by oxidation of anthracene in a fixed catalyst bed capacity 600 tonnes/year have been successfully implemented in the Soviet Union 2 July 1965. Yield of anthraquinone from contacting step was up to 86 mol.%, feed rate 113 kg/h and a weight ratio of air : anthracene equal 60 : 1. Details of industrial development of contact anthraquinone production, as well as the results of laboratory studies related to the development of large-capacity reactor output 5,000 t per year are set out in the article. It has been shown that the industrial catalyst KC-14 at a temperature more then 370 °C changes its phase composition and vanadium valence state, and therefore the kinetics of the oxidation of anthracene above and below that temperature varies. The resulting kinetic equations were used in the Boreskov Institute of Catalysis, Siberian Branch of the USSR in the simulation of large-capacity reactor production of anthraquinone by oxidation of anthracene in a fixed bed catalyst. Comparative tests of both methods of industrial production of anthraquinone: stationary and fluidized catalyst beds were conducted in order to select the most effective method for industrial production of anthraquinone at RPO «Krasitel». The choice was made in favor of a fixed bed unit. After the collapse of the Soviet Union all works were stopted , and in 2007 the production of anthraquinone (600 tonnes ) with a fixed bed catalyst RPO «Krasitel» was eliminated. Currently, in CIS there is no production of anthraquinone by contact method. About the production of anthraquinone in a fluidized bed of catalyst will be discussed in the second part of the article.

Hydrolysis of cellulose biomass under the action of biocatalysts (enzyme preparations) is one of the most advanced and environmentally friendly methods of obtaining a number of useful products. In this paper, a new approach is used to create a recombinant enzyme preparations with the desired properties by using fusion-constructs for gene cloning of target enzymes. A number of enzyme preparations is based on the strain of the fungus Penicillium verruculosum using fusionconstruct. The properties of these enzyme preparations are interest primarily as an additive to increase the capacity of the base hydrolytic cellulolytic complex P.verruculosum. Sharing new enzyme preparations and basic P.verruculosum allowed to increase its biocatalytic (hydrolytic) efficiency for the vegetable cellulose feed materials. By adding 20 % of the new enzyme preparation to the base without altering the total dosage of enzyme preparations in a reaction mixture the increasing of efficiency of hydrolysis of cellulose substrates (ground aspen wood and shredded pine wood deresined ) up to 70 %.

Kinetics of hydroforming of fatty acid triglyceride of rapeseed oil was investigated in the temperature range 300–380 °C with contact times 0,38–0,10 h and hydrogen pressure 1,0 MPa in the flow reactor with a fixed catalyst bed in order to establish the basic patterns of the process. The process was carried out on unsulfided nickel catalysts, which have a great practical interest to produce green diesel. Kinetic scheme of the process considering the target (alkanes) and all byproducts oxygen-containing products is offered. Quantitative assessment of the main routes hydroforming TGZHK rapeseed oil is obtained, which allows to predict the composition of the products and other process conditions.