Literature analysis was focused on the existing processes for synthesis of altax (2,2’-dibenzothiazolyldisulfide) as an important rubber vulcanization accelerator. Oxidation of mercaptobenzothiazole (captax) with various oxidants such as oxygen in the presence of catalysts, hydrogen peroxide etc., as well as electrochemical oxidation was shown to be the primary way to altax. The data from literature were the basis to develop a low-tonnage technology for synthesis of altax; the technology was developed at the Boreskov Institute of Catalysis and tested using a pilot setup at the Volgograd Department of BIC.

The influence of the cobalt-containing component (Co-Al₂O₃/SiO₂, Co-Re/A_l2O₃ and Co-Re/TiO₂) of a composite catalyst was studied in the Fischer – Tropsch combined process for synthesis and hydrotransformation of hydrocarbons. A flow fixed-bed reactor was used for characterization of the catalytic properties at 2 MPa, flow rate 1000 h^–1, 240–280 °C for 40–90 hours of continuous operation. The highest productivity and selectivity to C₅₊ hydrocarbons equal to 106 kg/(m³ cat·ч) and 67.1 %, respectively, was characteristic of the composite catalyst Co-Al₂O₃/SiO₂(35%)/ZSM-5(30%)/Al₂O₃(30%) at 240 °C. The comparable activities were observed with the catalysts Co-Re/Al₂O₃ and Co-Al₂O₃/SiO₂ but the former provided the formation of unsaturated hydrocarbons in a lower proportion in the products. The use of the Co-Re/TiO₂ catalyst at elevated temperature (up to 280 °C) allowed the molecular mass distribution of the products to be shifted towards the formation of the gasoline fraction. The rate of the catalyst deactivation was established to increase in the series Co-Al₂O₃/SiO₂ > Co-Re/Al₂O₃ > Co-Re/TiO₂.

A capillary column with functionalized poly(1-trimethylsilyl-1-propyne) (PTMSP/N₂O) was proposed to use for detecting products of catalytic pyrolysis of ethylbenzene. The capillary PTMSP/N₂O column separated selectively light C₁–C₂ (methane, ethane, ethylene, acetylene) and aromatic (benzene, toluene, ethylbenzene, styrene) hydrocarbons. A procedure for gas-phase measuring weight fractions of light C₁–C₂ and aromatic hydrocarbons was developed. The analytical measurement range was 2.9·10^–8 to 1.2·10^–1 mg/mL for light C₁–C₂ components and 3.5·10^–11 to 4.0·10^–3 mg/mL for liquid components. The analytical error margin at repetition ranged from 1.9 % to 4.7 %.

Under discussion is optimization of texture and chemical composition of alumina as the support for the catalyst for hydrotreatment of vacuum gasoil synthesized using the environmentally friendly modern technology of flash thermal treatment of gibbsite. Approaches to increasing the specific surface area by introducing inorganic admixtures (including boron or sulfur) at the stage of synthesis of pseudoboehmite were developed. The introduction of these modifiers was established to increase S_BET by 50–100 m²/g comparing to the maximal areas attaineddue to variation in the standard process parameters of the hydrothermal treatment. It was shown that the introduction of boron at the stage of pseudoboehmite synthesis resulted in no less than two times increase in the catalytic activity of CoNiMoP to hydrodesulfurization and hydrodenitrogenation against the activity of a similar catalyst with boron introduced with the impregnating solution.

Morphologies and structures of catalytic compositions and coats based thereon were studied using Pd-CeO₂/Al₂O₃ calcined at 100, 500, 1000 °C and the coats prepared by gas dynamic cold spraying onto a metal foil. It was established that the methods for preparation of the initial catalytic composition and for introduction of the active components to the coat influenced the phase composition, particle size and activity to oxidation of methane. The introduction of the active components by impregnation of the pre-deposited alumina layer was shown to provide the uniform distribution of Pd and Ce through the support profile, formation of nanosize PdO particles and of the interacting phases between the catalyst and support components. The impregnated catalyst was most active to oxidation of methane. The method for preparation of the coats has no limitations in scaling-up and, therefore, can be widely used for production of full-size catalysts on metal foils to be used for various energy devices.

Modified carbon materials were synthesized by impregnating activated carbons with an aqueous solution of sodium hydroxide followed by thermal treatment in air at moderate temperature (60–200 °C). The samples were tested for sorption-catalytic cleaning of air from hydrogen sulfide. Particular attention was paid to the influence of temperature of thermal treatment (activation) on sorption capacity of the modified carbons to H₂S. The modifying of activated carbons by impregnation with aqueous NaOH followed by their thermal treatment in air at 200 °C was shown to allow the dynamic sorption capacity to H₂S to be more than 8 times increased. The results obtained can be used to synthesize new materials based on commercial activated carbons for removal of hydrogen sulfide from air.

Results of the studies of catalytic combustion of peat, anthracite, as well as the mixture at the peat to anthracite weight percent ratio 40/60 are discussed. The degree of the mixture burning-off was shown to increase when peat evolving large quantity of volatile substances is added to anthracite. The burn-up degrees of the solid fuel particles less than 1.25 mm in size were 98.2 % of peat, 50.9 % of anthracite, 74.2 % of the peat and anthracite mixture at 700–750 °C and 1 m height bed of the industrial aluminum-copper-chromium oxide catalyst IC-12-70. In combusting coarse particles (equivalent diameter 11.6–18.6 mm) of molded peat and anthracite mixture, the burn-up degree was 80.5 % at the top of the fluidized catalyst bed. The burn-up degree of the coarse particles fed to the bottom of the fluidized bed was estimated with allowance for the burn-up degree of fine particles moving through the bed. With the coarse molded particles of the peat and anthracite mixture fed to 1 m height catalyst bed, the burn-up degree was shown to reach no less than 95 %. When the catalyst used is 2 mm in size, the peat and anthracite particles comprised in the molded fuel must be no more than 1–1.5 mm in size in order to prevent from ash accumulation in the fluidized catalyst bed.

Sulfur resistance of nickel, platinum and palladium metals on acid supports was studied depending on the support nature. Catalysts comprising nickel, platinum, palladium metals and sulfides as hydro-dehydrogenating components were examined for hydrocracking of n-octane. HY, ZSM-5, ZSM-23, ZSM-12, as well as silicoaluminophosphates SAPO-11 and SAPO-31 were used as the supports. The sulfur resistance of the supported metals in the catalysts was shown different and independent of the properties of the acidic support under the reaction conditions. Hydrocracking follows two different pathways depending on the activity and nature of the hydro-, dehydrogenating component (a metal or the sulfide), as well as on the ratio of activities of the acidic and hydrogenating components. The first pathway is preferable cracking of the initial paraffin at the early stage, and the second is dehydrogenation of the initial paraffin.

Two series of bifunctional hydroisodeparaffinization catalysts containing palladium supported on SAPO-11 and SAPO-31 were prepared and characterized. These were catalysts: 1) With different activities of the acidic component at the constant activity of the hydro-dehydrogenating component; 2) With different activities of the hydro-dehydrogenating components at the constant activity of the acidic component. With the catalysts with identical hydro-dehydrogenating activities, the temperature of eaching 90 % conversion of n-decane was shown to depend linearly on a total of the activity of the acidic component of the catalyst. Similar profiles of the dependencies were characteristic of both SAPO-11 and SAPO-31. The bifunctional catalysts based on SAPO-31 were much more active than the catalysts on SAPO-11. At identical total activities of the acidic components, the temperature of reaching 90 % conversion of n-decane was 50 °C lower over Pd/SAPO-31 than over Pd/SAPO-11. Ways to controlling the total activity and selectivity of the hydroisodeparaffinization catalyst by varying the activity of the acidic and/or hydro-dehydrogenating components of the bifunctional catalyst were demonstrated. An increase in the hydro-dehydrogenating activity led to an increase in the hydroisomerization activity of the bifunctional catalyst but practically not to changes in the selectivity to isomers. An increase in the toital activity of the acidic component also led to an increase in the hydroisomerization activity of the bifunctional catalyst, while the selectivity to isomers changed considerably.