Catalysts for deep oxidation of methane were studied using the methods of X-ray diffraction, thermal desorption of nitrogen and temperature-programmed reduction with hydrogen. These catalysts comprise oxides of 3d-metals (Mn, Co), rare earth (La) and alkaline earth (Ba, Sr) elements in a porous matrix of secondary supports (Al2O3, ZrO2, their binary composition) formed on the surface of the honeycomb structure blocks (cordierite, kaolin – aerosil ). It is shown that the activity and stability of the catalysts depends on the way of preparation, the nature of the active ingredient, and the block of secondary carriers. Suggested catalysts provide 80–100 % conversion of methane to CO2 at temperatures 650–750 °C, and can be recommended for use in the catalytic purification of gases from impurities hydrocarbons (methane and homologous С2–С4), and for burning a hydrocarbon fuel in industrial and household catalytic heat generators.

The effect of modifying the conditions of the natural aluminosilicate catalyst by 10 % HCl solution on its chemical and phase composition, porous and crystalline structure, acidity and catalyst activity in the reaction of α-pinene isomerization. When aluminosilicate are treated by 10 % HCl in an amount of 25–250 ml per 1 g of aluminosilicate (ml HCl/g) cationic exchange proceeds, the concentration of proton centers increases on its surface, there is a removal of impurities – calcite and dolomite. The specific surface area increases from 52 to 68–82 m2/g. Aluminosilicate treatment by 175,0 and 250,0 ml of HCl/g causes removal of substantial number of frame cation Al3+, Fe2+/3+, Mg2+ which leads to a partial destruction of its structure and reducing the acidity, specific surface area and hence catalytic activity compared with samples treated with 50 and 100 ml of HCl/g. Aluminosilicate treated by 50 ml of HCl/g shows the highest catalytic activity. The selectivity of camphene and dipentene (with α-pinene conversion 85 %) on original catalyst are 55 and 30 % respectively, after acid modification the camphene selectivity increases and dipentene selectivity decreases on 5–6 %. Considered catalyst has the activity advantage before commercial titanium catalyst.

Investigation of the influence of the chemical composition of support, substance and the method of nickel fixing on the physico-chemical and catalytic properties of the NiO/B2O3–Al2O3 system was conducted. Boron oxide content in the support was varied from 2 to 30 wt.% and a nickel content from 0,59 up to 3,18 wt.%. Catalyst samples were studied by X-ray phase analysis, thermoprogrammed desorption of ammonia, IR spectroscopy, including the adsorbed CO, as well as electronic diffuse reflectance spectroscopy. Tests of catalysts were carried out in the ethylene oligomerization in a flow reactor with a fixed catalyst bed at a temperature of 200 °С, pressure of 1 MPa, and a mass flow rate of ethylene of 0,5 hr–1. A gaseous mixture of ethylene-methane with ethylene content 30 wt.% was used as feed. The assumption was made that activity of NiO/B2O3–Al2O3 system in ethylene oligomerization process is associated with the formation of octahedral configuration Ni2+ cations surrounded by borate anions on the surface of the catalyst system. The most active catalysts containing 3,2 wt.% Ni and 10–20 wt.% B2O3 in the composition of the support. Method of preparation (adsorption binding or impregnation) had a little effect on the state of nickel in NiO/B2O3–Al2O3 system samples and their catalytic properties. The resulting catalysts are characterized by simplicity of preparation, low cost and availability of feed in comparison with the known ones.

Nanoparticulate catalysts M/Ce0,72Zr0,18Pr0,1O2, where M – Pt, Pd, Ru at 0,5; 1,0 and 2,0 wt.%, for diesel exhaust soot afterburning in a «weak» contact were synthesized. Structural, textural and catalytic properties of the samples were studied using EDX, X-ray synchrotron diffraction, XANES, EXAFS, TEM, low-temperature nitrogen adsorption and TG-DSC. It is shown that in the process of impregnating of platinum metals on the surface of the support Ce0,72Zr0,18Pr0,1O2, metal-support interaction occurs and increases in a line Pt → Pd → Ru. Ruthenium-ontaining catalysts are the most active in the soot afterburning, not only due to the nature of the supported component, but relatively faint metal-support interaction as compared with platinum and palladium samples. For them it is characterized the reduction of start oxidation temperature on 190 °C and lowering the temperature of complete oxidation approximately on 120 °C compared with the same parameters for the support without platinum. Due to the high activity of 0,5%Ru/Ce0,72Zr0,18Pr0,1O2 the opportunity for effective cleaning of diesel soot emissions are created by using relatively small amounts of the precious metal, which will reduce the cost of catalytic converters of diesel emissions.

Vehicle emissions are the major contributor of one of the most poisonous gas, CO. It not only affects human beings and vegetation but also affect environment. It indirectly contributes to global warming. Cold-start phase aggravates its emission to about 60–80 % even if the vehicle is equipped with a TWC. Thus, the target of the emission regulation bodies is to reduce CO emissions below 1,0 g/km from petrol-driven car. In this paper, the CO oxidation activity
and durability of Au-CuCe/γ-Al2O3 catalyst were tested. The catalyst was prepared by wet impregnation method and calcined at 600 °C. Characterization of the catalyst by N2 adsorption showed a BET surface area 103,48 m2/g, pore size 28,664 nm and pore volume 0,07 cm3/g. The XRD pattern of the catalyst confirmed the dominance of fluorite structure of CeO2 crystals in amorphous state and also exhibited the presence of CuO crystals of tenorite phase. Very small peak of nanosize Au was also observed in amorphous state. XPS studies showed the coexistence of Ce3+/Ce4+ in the catalyst. Copper in the form of Cu(I), Cu(II) in octahedral sites and Cu(II) in tetrahedral sites respectively was observed along with the existence of Cu+ and Ce3+. A typical peak of Au was also found. Total CO conversion was found around 80 °C. For durability test catalyst was calcined at 800 °C and CO conversion was measured for the 50 hour continuous run during which catalyst did not showed deactivation. Low cost and easy availability of Au-CuCe/γ-Al2O3 might advocate for its use as a catalyst for CO oxidation in vehicular exhaust at cold-start temperature.

Causes of alumina catalyst deactivation in a process of skeletal n-butene isomerization, which leads to decreasing of the conversion from 31 to 26 % were examined. It is shown that contamination of Fe, Mg metal combination microimpurities reduces the conversion of n-butenes of about 2,5 %. The catalyst activity can be restored by cleaning from metallic impurities. Steam piping and feed are the source of metallic impurities. The accumulation of δ-modification of aluminum oxide in the catalyst occurs during the operation that leads to a decrease in the conversion of n-butenes of about 3 abs.%; this kind of deactivation is irreversible. Probable cause of the partial phase transition at a temperature below 600 °C is the reducing of the phase transition temperature under the influence of trace Fe and Mg. It is shown that the accumulation of trace and δ-phase alumina decreases the amount of acid sites of alumina catalyst and the resulting decrease in conversion. Recommendation to extend the life of the catalyst is to capture metal impurities from steam feed flow by installing a protective layer the inert to butene fraction macroporous material with a developed surface in front of the catalyst bed.

Start of the first Soviet industrial plant production of anthraquinone
(600 tons/year) by anthracene oxidation by atmospheric oxygen in a fixed catalyst bed was successfully implemented in 1965 at Rubezhansky chemical plant. USSR Ministry of Chemical Industry leaders decided to establish an industrial plant anthraquinone production (600 tons/year) by anthracene oxidation in a fluidized catalyst bed, based on the experience of production realized in Czechoslovakia to choose the most effective method for the industrial production of anthraquinone . This plant started to produce in 1972. Description of the preparation of the catalyst of the Czechoslovak method, the procedure and results of the new installation are given in this article. Comparative analysis of the two methods of production of  anthraquinone (fluidized and fixed bed ) showed that the degree of feed conversion by both methods are very similar, but the stability of the installation systems with fixed bed catalyst is more preferable. Process with a fixed catalyst bed to be used when creating a subsequent production of anthraquinone in the USSR. Unfortunately , these projects could not be implemented.

Test industrial copper- zinc catalyst MEGAMAX® 700 was held in the gas-phase methanol synthesis reaction under conditions similar liquid phase process, the variation of pressure (0,5–7,0 MPa) and a flow rate of the gas mixture (40–400 ml/min). The catalyst showed a high activity and selectivity in methanol formation. The best result –730 g (methanol)/kg(cat)·h–1 and the selectivity 99,2 % was obtained under the conditions: 2,0 MPa, 240 °C, H2 : : CO : CO2 : N2 = 70,5 : 17,9 : 6,5 : 5,1 , reaction time – 3 hours. The concentration of byproduct methane increases at gas mixture pressures greater than 3,0 MPa, which leads to lower selectivity to methanol. Besides methane, only trace amounts of ethane and water were fixed. Typical byproduct of the synthesis of methanol – dimethyl ether absent in the entire range of pressures in the gas mixture. The results indicate the possibility of using the catalyst MEGAMAX® 700 liquid-phase methanol synthesis.

The original unit (fermenter) is designed and manufactured for research of biocatalytic transformations processing of products from renewable cellulosic feed. The unit was tested in the enzymatic hydrolysis of russian miscanthus pulp. The results (dependence of reducing substances concentration in the hydrolyzate from the duration of the enzymatic hydrolysis) are completely reproduced the results obtained earlier on the laboratory equipment. Fermentation of the obtained hydrolyzate are conducted in parallel in the laboratory and in the fermenter also showed the identical results. Thus, the unit proved a promising for the preparation of enzymatic hydrolysates suitable for use as substrates in the production of bioethanol technology and bacterial cellulose. The possibilityfor scalability by volume of biocatalytic transformation processes are demonstrated.