Current trends in the use of renewable energy plant are in the review. The biomass of microalgae is considered as the most promising renewable raw materials due to the high growth rate and productivity, superior to other cultures. Although large-scale production technology of high-biomass to produce biofuels are in the initial stage of development, the progress made in recent years, suggest the creation of the industrial processes of production in the near future. Developed modern catalytic methods (transesterification, hydrocracking) allow efficient processing of the biomass of algaein biofuels. At the same time to obtain high-quality hydrocarbon lipids of microalgae exposed to several changes: hydrolysis to remove the phosphorus-containing compounds, transesterification with methanol on heterogeneous catalysts, hydro deoxygenation (hydrocracking) and isomerization. The growing number of studies and a variety of ways of algae processing can talk about their great potential as a feedstock for bioenergy.

Method of gas chromatographic analysis of the reaction components of the catalytic oxidative carbonylation of benzene to benzoic acid is improved. Conditions of chromatographic separation are defined, which allows make a complete analysis of the reaction mixture: ethanol, benzene, toluene, phenol, benzoic acid, using a flame ionization detector (FID) on a non-polar polymeric sorbent Porapake Q column at a constant temperature for 8 min input volumes (0,2–3,5 μl) analytes were determined at which the signal of the detector response varies within the range of linearity. The detection limits vary from 0,14 for benzaldehyde to 1,44 ppm for benzoic acid. The method of analysis used in the BIC in the study of the catalytic reaction of oxidative carbonylation of benzene to benzoic acid and can be recommended for quality control of benzoic acid in its production in the chemical industry, in determining the mass fraction in the processed products of vegetable and fruit crops.

Deposited platinum catalysts based on zeolite type Ferrier containing Pt 1,3–2,8 % by weight is cooked. For the first time the localization of Pt in the zeolite channels is studied. It is shown that platinum localized in them, improves the yield of the products of selective hydrocracking of n-hexane. Platinum on the external surface of zeolite crystals is involved in the conversion of n-hexane in the direction of the formation of hydrocarbons isomeric structure. The catalysts can be used to improve the octane of gasoline-reforming characteristics by selective removal of low-octane n-paraffins, and increasing the proportion of high-octane gasolines isoparaffin hydrocarbons in catalytic reforming.

The method of decomposition of organochlorine waste catalysts, which are a massive metallic nickel (99,99 %) and its alloys with chromium (nichrome: Ni – 80 %, Cr – 20 % and Chromel: Ni – 90 %, Cr – 10 %) is offered. The decomposition process is accompanied by the formation of useful waste product - carbon nanofibers (CNF), «feathery» morphology. Feature of the process of catalytic decomposition of 1,2-dich oroethane on massive nickel catalysts is a long induction period (~ 3 h), during which the spontaneous activation of the alloy surface. A preliminary activation of the catalyst acid or sequential treatment in oxidizing and reducing atmosphere reduces the induction period on the order. Surface condition before and after activation studied by SEM, TEM, EDS. The activity of catalysts in the decomposition 1,2-dichloroethane at temperatures 550–700 °C is determined. The greatest activity (yield 400 of CNFs g/g catalyst) showed nichrome N80H20; yield CNFs on catalysts prepared by coprecipitation method and mechanochemical activation was several times lower. The novelty of this approach is to combine the process of disposal of organochlorine wastes to produce useful products (CNF). The use of solid metal catalysts promising, because the technology makes it easy to prepare, and the absence of a catalyst support makes it easy to clean impurities from the fragments of CNF catalyst.

Modern three-route catalysts operate at high temperature exhaust gas as high as 1000 °C, so the development of thermostable formulations relevant. In this paper the method of direct deposition of a number of composite Al2O3–Ce0,75Zr0,25O2 synthesized Al2O3 content 0, 10, 25, 50 wt.%. Composites are freshly prepared and after calcination in air at 1000 and 1100 °C were studied by BET, XRD, TEM, TPR. Next, using composites, aged at 1050 °C in an atmosphere of 2 % O2 + 10 % H2O + 88 % N2. Block prepared catalysts, oxygen capacity (OSC) and the activity is studied in the gas analytical stand. With the increase in the proportion of Al2O3 composites increases the uniformity of mixing and dispersion of particles CexZr1–xO2–δ, their chemical composition is homogeneous, the amount of cerium involved in oxidation-reduction, increases. The composite containing 50 wt.% Al2O3, is made up of individually mixed crystallites CexZr1–xO2–δ, and Al2O3, whose dimensions are virtually unchanged during calcination. The catalyst (Pt/Al2O3 + Al2O3–Ce0,75Zr0,25O2) on the basis of the composite is characterized by the OSC and the highest activity, it can be recommended composite for industrial testing.

When operating the reforming units with continuous catalyst regeneration there is the problem of optimizing the multiplicity of the catalyst circulation in the reactor-regenerator. This problem can be solved with a combination of natural and computer simulation through a study of the formation of coke on the catalyst surface. Based on the results of TGA of the industrial catalyst Pt-Sn/γ-Al2O3 concluded that amorphous coke is formed on the catalyst surface in reforming process, the whose number of coke at the outlet of the reactor block is 4–6 % depending on the composition of need materials and process parameters. The specific surface area of samples (m2/g): for the original – 152, after regeneration – 140, at the outlet of the reactor – 118, which correlates with the amount of coke on the surface of the samples. Mathematical analysis of processes of coke formation in the reforming reactor, a moving granular bed showed that the multiplicity of the catalyst circulation should be maintained in the range 0,008–0,010 m3/m3 to improve the efficiency of industrial plant. Maintaining the optimum conditions in the reactor and regenerator unit will allow to control the coke formation and to maintain the coke concentration on the minimum possible, and specific surface area of the catalyst at the highest possible level.

To develop technologies for carbon adsorbents, promising as catalyst supports, the use of synthetic monomer – furfural – for highstrength ash-free activated carbons with a spheroidal shape of the particles is justified. One-step process of resinification of furfural, forming a spherical product and its cure was developed, reducing production cycle times and reduce hardware costs. Derivatografic, X-ray diffraction, mercury porosimetry and adsorption studies of carbonization molded spherical product is made, it described the development of primary and porous structures of carbon residues. In combined-cycle activation of carbonized product a ashless active carbons are obtained with particles spheroidal shape, also well-developed capacity (up to 1,50 cm3/g) of sorbent microand mesopores and unique high mechanical strength– speed on the abrasion in 3 times smaller than that of commercial brands of activated carbons. The resulting activated carbons on the performance characteristics superior to all known brands of foreign and domestic counterparts, and are promising catalysts for working under harsh operating conditions – in the moving and fluidized beds.

The method of synthesis of catalysts CeO2–ZrO2/Al2O3 and CuO/CeO2–ZrO2/Al2O3 using sol – stable dispersions of nanoparticles was proposed. The effect of sols viscosity and concentration of the dispersed phase at the time of impregnation and the amount of the supported active component is investigated. The samples are prepared by hydrosol CeO2–ZrO2 and CuO impregnation of catalysts support (α-Al2O3). The samples varied molar ratio CeO2/ZrO2 (in the final catalyst, it was 9/1 4/1, 1/1 1/4) and the content of the active component on a support (0,7–3,0 wt.%). CuO is impregnated in an amount of 0,25 wt.%. The study of samples is performed by elemental analysis, XRD, TGA, SEM, low-temperature nitrogen adsorption. There is testing of the synthesized catalysts in the oxidation of CO on the laboratory unit flow type in the temperature range 20–450 °C at atmospheric pressure and space velocity 7200 h–1 with the gas mixture composition (vol.%).: CO – 4,1, O2 – 9,6 ; N2 – 86,3. It is shown that the samples exhibit catalytic activity in the temperature range 150–400 °C, complete oxidation of CO in the reaction conditions is achieved when the content of active ingredient is 1 wt.%. The introduction of copper oxide in the catalyst lowers the temperature of complete oxidation at 200 °C. Multi-component catalyst CuO/CeO2–ZrO2/Al2O3, obtained by solgel method, shows activity comparable to the activity of catalysts based on platinum group metals. The results of this work can serve as a basis for technology supported catalysts with different metal oxide sols.

The methods of X-ray diffraction, mercury porosimetry, and electron probe microanalysis the nature of phase transitions and the porous structure of the low-temperature modifications of aluminum oxide, depending on the amount of injected calcium oxide in the system CaO–Al2O3 is studied. Samples of γ-, χ-Al2O3, containing CaO in an amount 1,0; 4,0–5,0 and 7,0–8,0 wt.%, calcined at temperatures of 880–900, 1000 and 1200 °C are studied. It is shown that the introduction of CaO in the samples of the γ-, χ-Al2O3 (model ShN-2) slows down the process of phase transformations of alumina, which is explained by the competing process of interaction with the Al2O3 CaO, leading to the formation of calcium aluminate CaO·2Al2O3. With increasing calcination temperature up to 1000–1200 °C and increasing the duration of calcination, the end product of γ-, χ-Al2O3 phase transformations, occurring through a stage of education æ-Al2O3, is the formation of α-Al2O3. The γ-, χ-Al2O3 support modified by calcium oxide in an amount of 4,0–5,0 wt.% (model  ShN-2M) has a much higher strength and has a wide range of working pore volume (100–2000 Å), than the unmodified. On the base of ShN-2M support a number of catalysts – Mn-Pd (MPK-1), Pd (NPK Series) and Pt (PLK 1, PLK-2) – with low (from 0,05 to 0,20 wt .%) content of precious metal (Pt, Pd) has developed and tested their activity in reactions of deep oxidation of butane oxidation and CO. Experimental designs catalyst NPK-2 (TU 6-02-7-192–85) have been introduced in some plants, chemical and automotive industry (Moscow, Riga, Tbilisi, Rustavi). Experience in industrial use of catalysts based on ShN-2M showed that the duration of effective work in the processes of post-combustion exhaust gases of internal combustion engines, they can compete with well-known brands of industrial catalysts.