To develop effective catalysts based on metal meshy supports for the reaction of the methane partial oxidation to synthesis gas there were the comparative tests of metal catalysts (Pd, Ni, Co, Cu, supported on a metal grid and fechral foil) obtained two ways: thermochemical and electrochemical deposition of metals. Tests were carried out in the temperature range 680–1000 °C in a flow reactor (internal diameter 10 mm) with integrated catalyst in the form of a twisted roll of wire mesh or fechral foil. It is shown that the metal supports (grid or foil) with metals (palladium, nickel) putted on them are promising for use as catalysts in the production of synthesis gas by the reaction of partial oxidation of methane in a narrow range of the molar ratio oxygen/methane (O2/СН4 = = 0,45÷0,55). In the study of catalyst surfaces by SEM there was revealed that the thermochemical deposition of VIII group metal more extensive area of active metals is formed, providing even at 900 °C almost 100 % conversion of methane with selectivity for CO over 90 %.

Based on a complex mathematical model of the Fischer–Tropsch process the high-perfimance cobalt catalyst for synthetic oil production is developed and tested. The catalyst is granular thermally conductive composite material with a well-developed system of transport pores, which provides an effective mass and heat transfer in the granules. The influence of nature of the heat-conducting aluminum- containing additives on the physical properties of the support and catalytic properties of Fischer–Tropsch catalyst is shows. Found that increasing of catalysts granules thermal conductivity is one of the factors that increase the performance of the catalyst. In the presence of developed catalyst the performance for hydrocarbons С5+ achieved 600 g/(kg·h) or 480 g/(l·h) at 0,8 g/cm3 packing density. A pilot plant to obtain up to 20 liters of synthetic oil per day from natural gas using the catalyst is established and put into operation. Catalyst testing in this plant has confirmed receipt in the laboratory performance of granular bed.

A process for producing of β-hydroxyalkyl mercaptans and β-ydroxyalkyl sulfides based on the interaction of liquid hydrogen sulfide with alkylene oxides is proposed. This method provides the highest possible concentration of hydrogen sulfide in the reaction mixture, allows to run the process in a wide range of temperatures, allows the use of catalytic additives, does not require a solvent. The kinetic patterns of interaction of hydrogen sulfide with one of alkylene oxides (propylene oxide) under conditions effective to stay the components of the reaction mixture in the liquid phase. With an excess of propylene oxide in reaction a two consecutive macro stages are occurring: formation of 2-hydroxypropane-1-thiol and the subsequent formation of 1,1’-di(2-hydroxypropane) sulfide. Staged in the formation of sulfide and mercaptan allows to manage the process to obtain quantitatively or mercaptan or sulfide in certain conditions. So, basically 2-hydroxypropane-1-thiol is formed with an excess of hydrogen sulfide. The activity of 14 homogeneous and heterogeneous catalysts (activated carbon, ion exchange resins, metal oxides, water, triethylamine, etc.) are studied. On the basis of the developed mathematical model the principle of determining of the catalytic additives effectiveness is proposed. The most effective catalyst of all tested was the triethylamine which increases the reaction rate more than 100 times: without catalyst the reaction is completed in about 50 hours, in the presence of small amounts of triethylamine – a few minutes.

We have investigated the catalytic cracking of heavy vacuum distillate on industrial catalyst RD-DMS-PM («BASF» company) with the addition of zeolite CVM (JSC «AZKiOS» Angarsk, Russia) and special additives MOA («BASF» company) to increase the yield of olefins for growing interest to the catalytic cracking with high yield of light olefins and, above all, propylene. Additive content varied (wt.%): 10, 20, 30 and 40 for the MOA and 3, 8, 12 and 16 for CVM. Catalytic cracking was conducted on laboratory unit in flow reactor with a fixed bed reactor at 500 °С. The dependences of product composition from the number of introduced into the catalyst additives are derived It is shown that the highest yield of propylene (11,5 wt.%) is achieved with the 40 % MOA addition or 8 % zeolite CVM. Results to increase the yield of light olefins were obtained at corresponding operating conditions existing catalytic cracking unit.

In the production of chlorohydrocarbons (chloromethanes, perchlorethylene, etc.) a carbon tetrachloride formed as a by-product. The Montreal Protocol refer it to ozone depleting substances. The process of liquid-phase catalytic hydrodechlorination of CCl4 in the presence of aqueous sodium hydroxide to form useful products: sodium formate, hexachloroethane and perchlorethylene,
was investigated to develop a rational (another then burning) method of disposal of CCl4. Experiments were performed in a 300 ml autoclave at pressures up to 1,5 MPa in the temperature range 80–120 °C, the catalyst - Pd on sibunit (5 fractions from 0,1 to 1,6 mm). The dependence of CCl4 conversion and main products selectivity from the initial CCl4 and NaOH concentration, temperature, hydrogen partial pressure, size of catalyst particles and palladium content were studied. Based on these results, scheme of the process is proposed, recommendations on the conditions of the process depending on the specific composition of the products are given, optimal parameters of the catalyst are determined: 1,5 wt.% Pd on sibunit with grains 0,315–0,63 mm. The proposed process will not only solve the problem of waste disposal containing CCl4, but also ensured the production of three commercially popular products.

The results of the pilot testing of two-stage catalytic systems for ammonia oxidation equipped by catalyst platinoid gauzes as catchers of palladium-wolfram alloy and block catalyst IC-42-1. The concentration of ammonia in the mixture is about 10,3–10,7 vol.%. If the residual ammonia concentration above 0,6 vol.% at the out from platinoid bed the reduction of the nitric oxide yield after the catalytic system is observed (from 0,6 up to 4,7 % depending on the number of platinum gauzes), due to increased homogeneous reduction reaction of nitrogen oxide with ammonia in the free volume of the block catalyst. When the residual ammonia concentration at the out of platinoid bed decreases less than 0,06 vol.% the reduction of the nitric oxide yield after the system is not observed. In the two-stage system consisting of nine platinoid knitted mesh with a wire diameter 0,076 mm, 4 catching gauzes and block catalyst, the nitric oxide yield remains stable at 95,4 %. According to test results there is decision to upgrade the catalytic system with block catalyst justified replace block catalyst by more technologically sophisticated inert honeycomb packing.

Comparative studies of 2-stage systems formed from the full and «light» platinoid packages and catalyst IC-42 or inert packing were performed in a pilot plant in the reaction conditions corresponding operating conditions of the commercial unit AK-72. There are effect of the blocks setting on the temperature profile in the platinoid packages and therefore on the NO yield depending of the geometry and material of the blocks, which should be considered when designing the optimal two-stage systems. Based on the results of comparative tests, there is proposal of a new bifunctional catalyst IC-42-9, which usage instead of catalyst IC-42-1 into two-stage systems will increase NO yield in industrial units UKL-7 and, in addition, reduce the N2O content.

Properties of model systems Fe2O3–K2O and Fe2O3–K2O–CeO2 with a weight ratio 80:20 and 50:20:30, respectively, were studied by methods of thermal, magnetic, and X-ray analysis of variance, and the low-temperature nitrogen adsorption. There is revealed that then interaction of iron oxide with potassium carbonate take place the successive formation of the mono-and poly ferritic phase is going. It is suggested that the activity of iron-potassium catalyst is proportional to content of the surface mono ferritic phase. Found that the introduction of cerium into iron-potassium system leads to a redistribution of mono- and poly ferrits of potassium in the ferrite phase, namely to increasing of the mono ferritic phase share. Consequently, the introduction of cerium promotes the activity of the catalyst system. The results of this study will be used to develop a new iron-potassium catalysts with enhanced catalytic activity in the dehydrogenation of isoamylenes to isoprene.

There is comparative study of the effectiveness of six commercial biocatalysts based on enzyme preparations derived from fungus of the genus Trichoderma as a producer (Cellic CTec1, Cellic CTec2, Accelerase 1000, Accelerase 1500, Accelerase XY, Accelerase DUET), and laboratory biocatalysts based on enzyme preparations derived from the fungus Penicillium verruculosum, for the hydrolysis of four types of plant cellulose material (steam pretreated corn stalks and bagasse, crushed timber pine and aspen), also microcrystalline cellulose. The activity of biocatalysts relative to various substrates and the dependence of the depth of exhaustive hydrolysis of plant material from the dosage of these biocatalysts were determined. It is shown that biocatalysts derived from P. verruculosum strains are competitive with the widely used commercial biocatalyst based on Trichoderma strains when they scale biotechnological processes bioconversion of renewable resources.