To improve the technical and economic parameters of the two-stage isoprene from isopentane production the authors studied the features of most energyintensive the second stage of the process – methyl butenes dehydrogenation. In particular, the influence of carbon dioxide formed during the self regeneration of the iron oxide catalyst (the reaction Ccoke + 2H2O → CO2 + 2H2), on the methyl butenes conversion and isoprene selectivity. It is established that CO2 presence in the reaction batch has a significant effect on the methyl butenes conversion: when the CO2 concentration in the feed close 1,5 wt.% the methyl butenes conversion reduced by 5–6 %. It is shown that CO2 reversibly deactivates the catalyst and if terminate it flow the catalyst activity is restored (yield of isoprene is slowly returning to its original value). The regeneration rate depends on the concentration and duration of carbon dioxide exposure. Treatment of the catalyst with steam in the absence of the reaction mixture leads to rapid regeneration of the catalyst. It is concluded that the implementation of two-step methyl butenes dehydrogenation technology whose primary purpose is to increase the methyl butenes conversion up to 35–40 %, the activities for continuous monitoring of CO2 content in the contact gas of the first stage of dehydrogenation and the selection of optimal regimes for iron oxide catalyst (temperature, the ratio of pairs: raw materials, etc.) become particularly important to reduce the catalyst carbon residue.

High-molecular branched polyethers (PP) on the basis of propylene and ethylene oxides are used as an active base for oil emulsions demulsifying agent compositions. The present investigation focused on the features of the propylene oxide polymerization in the presence of double metal cyanide catalyst on the example of PP based on the mono ethylene glycol and glycerol by varying the molecular weight in the interval 6000–150000. The polymerization was carried out in a laboratory reactor at 110–120 °С, the catalyst concentration from 50 to 300 ppm. For PP samples viscosity, iodine number, molecular-mass characteristics are defined. It is shown that the PP with a molecular weight 6000–40000 are characterized by narrow molecular weight distribution (MWD), a low content of unsaturated impurities. With further increase of the PP molecular weight the broadening of the MWD is observed, the polydispersity reaches a value of 2,5–3,9, which is associated with the formation of low molecular weight unsaturated and bifunctional PP. The results can be used to create the PP technology with using double metal cyanide catalyst.

The features of the iminodiacetic acid (HIDA) synthesis by ehydrogenation of diethanolamine (DEA) on the Cu/ZrO2 catalyst in flow microchannel reactor in comparison with the synthesis in the autoclave are studied. It was found that the specific performance of reactors in terms of the reaction volume and weight of the catalyst in a microchannel reactor are 4,38 gHIDA/(cm3·h) and 0,49 gHIDA/ (g cat·h), respectively, while in an autoclave – 0,018 gHIDA/(cm3·h) and 0,46 gHIDA/(g cat·h). Analysis of kinetic data indicates that the synthesis of HIDA proceeds in two stages with the formation of an intermediate N-(2-hydroxyethyl)glycine (Bicine). A formal two-step kinetic scheme of this process and calculated apparent rate constants of stages are proposed. It was found that the apparent constants of rate of stages are magnitude greater in several orders for the microchannel reactor than the corresponding constants for the autoclave synthesis. Specific productivity, calculated for the reaction volume for the microchannel reactor, also higher in two orders of magnitude than for the autoclave, what is indicating that a substantial intensification of the process in the channels of sub-millimeter sizes due to the high efficiency of heat and mass transfer.

The work is dedicated to the development of the domestic process of catalytic dehydrogenation of ethanol to ethyl acetate – a product that is widely used as a solvent in the manufacturing of paints, drugs, printing inks for food industry. The process is an alternative to the traditional method of production of ethyl acetate - acetic acid etherification with ethanol. The only feed in the developed process is ethanol (bioethanol). Compared with the traditional process, despite the reversibility is virtually no waste of feed, there are no corrosive medium and waste water. The industrial catalysts NTK type are used for the dehydrogenation of ethanol in ethyl acetate, they differ in chemical composition (producer – JSC «Dorogobuzh»). Testing of the catalysts was carried out in flow laboratory unit in the temperature range 230–300 °C and pressures of 0,1–2,0 MPa. The best results were obtained on the catalyst NTK- : it allows to reach the ethanol conversion per pass-flow from 40 to  3 % with selectivity of 86–94 %. NTK-4 catalyst showed reliable  erformance and reproducibility of results in laboratory conditions, it is assumed sampling process in a pilot plant. The process is interesting for enterprises of small capacity (not willing to work with sulfuric acid according to the traditional method), carrying out activities in the area solvents, paint industry, the packaging material.

The synthesis conditions, reduction and passivation of industrial methanation catalysts are summarized. There are the requirements for the catalysts preparation for usage. The main characteristics of industrial methanation catalysts and operating conditions are considered. It is noted that the domestic catalysts NIAP-07 series (NKM) have a lifetime at least 15 years. It is shown that the developed new high-efficiently nickel catalyst for methanation has a low temperature activation and can be made in the form of rings, extrudates or tablets. Using the ring-shaped catalyst reduces the gas-dynamic resistance of methanator and thereby natural gas is saved in ammonia production units. In the «NIAP-CATALYST» by the industrial production of methanation catalysts is organized. The catalysts NIAP-07 series (NKM) can be used in various technological processes of purification of gases from carbon oxides by their hydrogenation.

It is known that cerium compounds are widely used as promoters in the iron-potassium catalysts for alkylaromatic and olefinic hydrocarbons dehydrogenation. To establish the mechanism and the role of cerium oxide in the formation of catalytically active phases (ferrite potassium) must first to determine its effect on the transformation and reactivity of the iron oxide containing in the catalyst in an amount of 50–80 %, and participating in ferrite formation. There is the studying of thermal behavior at heating in air of cerium oxalate and Fe2O3–CeO2 model system, which are the main components in the manufacture of iron-potassium catalysts, by X-ray, thermal, analysis of variance, low-temperature nitrogen adsorption and temperature-programmed reduction with hydrogen. A great lability of cerianite compared with hematite is identified. It is established that the introduction of cerium into hematite increases the reactivity of the Fe2O3–CeO2 system and its thermal heating leads to a partial reduction of Fe2O3. The results obtained will be used for development a new iron-potassium catalysts with improved catalytic activity in the dehydrogenation reaction of isoamylenes to isoprene.

The catalytic performance in n-butane dehydrogenation of bimetallic PtSn, PtGa and PtIn, and trimetallic PtSnIn and PtSnGa catalysts (with low metal contents) supported on a MgAl2O4 prepared by a novel mechanochemical synthesis was evaluated both in flow and pulse equipment. The influence of the addition of different promoters (Sn, Ga and In) to Pt on the activity, selectivity and deactivation in the n-butane dehydrogenation reaction was studied. Stability experiments through successive reaction–regeneration cycles were carried out for selected catalysts. In order to correlate the properties of the metallic phase of the catalysts with the catalytic behavior, several characterization techniques were used, such as test reactions of the metallic phase (cyclohexane dehydrogenation and cyclopentane hydrogenolysis), TPR, XPS, H2 chemisorption and TEM. Bimetallic PtSn catalyst has a better catalytic behavior than PtIn and PtGa ones. For PtSnM (M: In or Ga) catalysts, whereas Ga addition to the bimetallic catalyst does not practically modify the dehydrogenation performance, the addition of In produces an increase of the activity and the selectivity to butenes. Characterization results indicate the presence of geometric effects for the PtSn catalyst, and geometric and electronic effects for PtIn and PtGa ones. For trimetallic catalysts, the presence of a close contact between Pt, Sn and In or Ga in both trimetallic catalysts was found, mainly due to geometric effects like blocking and dilution of the active sites by the promoters. In stability experiments, the trimetallic PtSnIn/MgAl2O4 catalyst clearly displays the best catalytic performance along reaction–regeneration cycles, though  PtSnGa and PtSn catalysts also showed a very good behavior through the successive cycles. The characterization of these catalysts after cycles shows that their metallic phases are slightly modified along the cycles.

In the production of phthalic anhydride by oxidizing о-xylene, the most widely used catalysts were ball – the catalyst KS-278 in the Soviet Union and the Friedrichs (F-1) catalyst in foreign practice. The service life of the first catalyst was 1 year, the second was 3 years. By studying the conditions of gas flow catalytic surfaces Academician V.V. Struminskii concluded that the catalysts should be given a form, which reduces the resistance and the probability of vortices, i.e. a tubular shape with a length greater than that of Raschig rings. Embedded under his leadership at the Leeds Paint Factory the tubular catalyst KT-1-SN spent seven years with performance significantly exceeding the performance of catalysts KS-278 and F-1, namely: the output of phthalic anhydride by contacting step was 78 mol.% versus 68 mol.% on KS-278 catalyst, and the design capacity of the plant was exceeded by 23,5 % and energy consumption reduced by 25 % due to lower hydraulic resistance of the catalyst bed (0,18 atm versus 0,38 atm on KS-278 catalyst). Experience in operation of the tubular catalyst KT-1-SN can be used in modern production of phthalic anhydride, as well as in other industrially important processes, such as obtaining maleic anhydride, aniline, anthraquinone, and many others.