The method of purification of fraction c4- olefins
(57) Abstract:Usage: in the petrochemical industry, in particular in the cleaning method C4- olefins. The inventive fraction formed during the synthesis of tert-allyl ether, cleaned ethers and alcohols by contacting with a catalyst consisting of silicon dioxide, modified by the addition of aluminum oxide in an amount of 0.1 to 0.15% by weight of silicon dioxide. The process is conducted at 200 to 250°C and space velocity fraction 4-15h-1. 2 C.p. f-crystals, 1 table. The invention relates to a method of selective catalytic decomposition alilovic ethers and alcohols formed from the synthesis of methyl tertiary amyl simple ether (TAME). In particular, the invention concerns a method of purification of fraction5-olefins formed during the synthesis of methyl tertiary amyl simple ether (TAME) to make it suitable for subsequent alkylation with isobutane. The method consists in the catalytic processing to remove the oxidized compounds which poison the catalyst for alkylation.It is known that when methanol is present, then branched unsaturated olefinic5hydrocarbons (ITAM Lewis acids, mineral and organic acids (as described, for example, in the patent of great Britain, N 1506596 the applicant). The corresponding flow of product on refining plant for the production of methyl tertiary amyl simple ether fraction is5from catalytic cracking, containing only a small amount of hydrocarbons4and C5+.The TAM is used as an additive to enhance the octane rating, and it can be left in the products of the reactions, or to separate by distillation as a residual product. In this latter case, the remaining hydrocarbon products can be effectively used in the alkylation reaction, provided that they are of high purity (in particular oxidized products must be kept at a very low concentration).In addition to methyl tertiary amyl simple ether (TAME), oxidized products, which may remain in the above-mentioned fractions are tertiary amyl simple ether formed as a side product in the synthesis of TAME, and in particular MTBE, which is formed due to the presence of isobutene in a small number of fractions WITH5and that it is difficult to separate from the faction WITHbut this is a very expensive operation. Now find the catalyst that allows you to selectively decompose the oxidized compounds present in the products, which are formed from the synthesis of TAME, so the feedstock of hydrocarbons WITH5becomes suitable for alkylation.The known method (international application WO 87/00166), which proposed to decompose the flow of raw materials, completely consisting of tert-alkyl alilovic esters, on the catalyst.The method in accordance with the invention has a high selectivity in respect of the content of oxidized components, and the formation of heavy products, which are harmful for the selectivity and unsuitable for use.The invention is characterized by two essential features:
the application of chemical methods (destructive catalytic destruction) for separating undesirable oxidized components instead of using physical methods, such as extraction or distillation. Really, if you want to remove the oxidized components to the low content, the result may not be achieved by application of the mentioned physical ways;
the use of highly selective and alkylation, is supported at a very low level parallel oligomerization reaction or the formation of compounds WITH6+, which as such will only reduce the selectivity of the reaction to a low value.The method of decomposition alilovic ethers and alcohols formed during the synthesis of TAME, in accordance with the invention consists in the reaction of this mixture in the presence of a catalyst consisting of silicon dioxide, modified by the addition of aluminum oxide in an amount of 0.1 to 1.5% by weight of silicon dioxide, which operates at a temperature between 200 and 250aboutWhen flow rate (IHSY) between 4 and 15 h-1. The decomposition is preferably carried out at an operating pressure of between 1 and 2 bar.The catalyst can be easily prepared from pre-formed silicon dioxide required purity (this product is commercially available), thus preventing the preparation of the impregnation, drying and calcination.The impregnation is performed by the solution of an aluminum salt (e.g., nitrate or isopropyl) to obtain the final desired content of aluminum oxide.However, it is desirable to use silicon dioxide of high purity, i.e., silicon dioxide with a content of Na2O The Catalysts, used in this way are non-toxic, non-corrosive, and they can work in the presence of water without the formation of acidic products.Furthermore, they are stable for many thousands of hours and can easily be regenerated.P R I m e R s. Conducted testing of the reaction mixture, reproducing the composition of the exit stream from the synthesis of methyl tertiary amyl simple ether (TAME). His following composition, wt.%: WITH40,016 Isopentane 45,933
Pentane normal structure of the carbon chain 5,564 2-Methyl-2-butene 6,665 2-Methyl-1-butene were 1,268 1-Penten 35,640 Methyl tertiary butyl ether (MTBE) 3,634 Tertiary amyl alcohol (TAA) 0,583 Methyl tertiary amyl simple ether (TAME) 0,5476-C100,150
Catalytic tests were carried out in a solid micro-reactor for process type pulse containing 1 cm3 of the catalyst particles of the appropriate size (30-40 mesh.).P R I m e R 1. The catalyst of the silica-modified alumina was prepared as follows.10 g of high-purity silicon dioxide of the following composition, wt.%: Na2O 0,05; TO40,15; Al2O30,30; STO2the rest is up to 100, processed water the scientists of the material was slowly dried at 120aboutC for 3 h, then was progulivali at 500aboutC for 4 h1 cm3the catalyst prepared in this way contains 0.5% Al2O3on high-purity silicon dioxide), was placed in the microreactor and heated to 240aboutC. the Pressure was equal to 1.6 bar. Then the reaction mixture was applied with a volumetric hourly rate IHSY = 4, the obtained results are presented in the table.P R I m m e R 2. Without any intermediate regeneration of the catalyst from example 1 set the temperature to 230aboutC and a space velocity (IHSY) increased to 5.6 h-1. Maintained a pressure of 1.6 bar. After stabilization of the analyzed product. The results are presented in the table.P R I m e R 3. Applying constant other working conditions of the preceding examples, increased volumetric hourly rate of liquid product up to 10 h-1. After stabilization of the analyzed product. The results are presented in the table.P R I m e R 4. In other unchanged operating conditions of the previous example increased hourly space velocity of liquid product (IHSY) up to 11 h-1. The test results presented in the table.P R I m e R 5. The test was carried out at 235aboutWith and cha is taulani in the table.P R I m e R 6. The test was carried out at 240aboutWith and volumetric hourly rate of 11.6 h-1. Analysis of the product was carried out after stabilization. The results are presented in the table.P R I m e R 7 (comparative). The catalyst from example 1 was placed in the microreactor and raise the temperature to 240aboutC. Working pressure was equal to 1.6 bar. The reaction mixture was applied with a volumetric hourly rate of 0.5 h-1. The results presented in the table.P R I m e R 8 (comparative). The catalyst from example 1 was placed in the microreactor and the temperature was raised to 240aboutC. Working pressure was equal to 1.6 bar. The reaction mixture was applied with a volumetric hourly rate of 24.0 h-1. The results presented in the table.P R I m e R 9 (comparative). The catalyst from example 1 was placed in the microreactor and the temperature was raised to 350aboutC. Working pressure was equal to 1.6 bar. The reaction mixture was filed with the hour bulk velocity of 11.5 h-1. The results presented in the table.From the table we can see that a very high flow rate (IHSY, higher than 15 h-1, example 8) does not lead to a complete decomposition of methyl tertiary butyl ether (MT is p 7) or too high temperature (above 250aboutC, example 9) lead to a significant decrease in the selectivity to olefin due to the large formation of by-products from side reactions. 1. THE METHOD OF PURIFICATION OF FRACTION C5- OLEFINS formed during the synthesis of the tert-amyl ether, from the contained impurities ethers and alcohols, characterized in that the raw material is in contact with a catalyst consisting of silicon dioxide, modified by the addition of aluminum oxide in an amount of 0.1 to 1.5% by weight of silicon dioxide, at 200 - 250oC and flow rate 4 - 15 h-1.2. The method according to p. 1, wherein the process is carried out at a pressure 1 to 2 bar.3. The method according to p. 1, characterized in that the use of catalyst containing silicon dioxide containing Na2O not more than 0.12 wt.%, SO42-- not more than 0.15 wt.%, alumina - not exceed 0.30 wt.%.
SUBSTANCE: invention relates to producing a catalyst and a process of obtaining hydrocarbons via catalytic hydrodeoxygenation of products of processing plant biomass, including microalgae biomass. Described is a catalyst for hydrodeoxygenation of organooxygen products of processing plant biomass, which is a complex composite containing Ni in a reduced form and other transition metals, wherein the catalyst contains up to 15 wt % P which is in the reduced catalyst in form of phosphides with general formula where: Mi is a transition metal in phosphide form, other than nickel or boron, 2≤n≤5, with atomic ratio from 0.01-99, mainly from 7 to 99, and a stabilising additive. Described is a hydrodeoxygenation process, which is carried out in a single step at hydrogen pressure of 0.5-20 MPa, temperature of 250-320°C in the presence of the catalyst.
EFFECT: high catalyst activity.
4 cl, 39 ex, 5 tbl
FIELD: industrial organic synthesis.
SUBSTANCE: embodiments of invention are accomplished via liquid-phase dehydration of methyl phenyl carbinol-containing feedstock in presence of acid-type catalyst in column-type reactor-rectifier comprising still portion, built-in heat-exchanger, and rectification portion, volume of still portion constituting 80% of built-in heat-exchanger volume. Temperature of till portion of reactor-rectifier is 140-205°C and temperature in rectification portion 130-180°C. Advantageously, methyl phenyl carbinol-containing feedstock is supplied to and/or under built-in heat-exchanger and catalyst or mixture of catalyst with feedstock and/or still product is supplied to still portion at mixing. Linear velocity of reaction mass vapors within free cross-section of reactor is 0.05 to 0.9 m/s, residence time of styrene in reaction zone 0.05 to 50 sec, and residence time of still product in reactor 5 to 500 h.
EFFECT: increased conversion of feedstock and final product formation selectivity.
5 cl, 14 ex
FIELD: industrial organic synthesis.
SUBSTANCE: invention relates to production of alkylaryl hydroperoxides useful as starting material in production of propylene oxide and alkenylaryl. Process of invention comprises following stages: oxidation of alkylaryl compound to form reaction product containing alkylaryl hydroperoxide; contacting at least part of reaction product with basic aqueous solution; separation of hydrocarbon phase containing alkylaryl hydroperoxide from aqueous phase; containing at least part of above hydrocarbon phase with aqueous solution containing waste water, said aqueous solution containing less than 0.2% alkali metal and/or salt (determined as ratio of metal component to total amount of solution); and separation of hydrocarbon phase from aqueous phase. By bringing at least part of above hydrocarbon phase containing alkylaryl hydroperoxide into interaction with propylene and catalyst, alkylaryl hydroxide and propylene oxide are obtained. At least part of propylene oxide is then separated from alkylaryl hydroxide. Dehydration of at least part of alkylaryl hydroxide results in formation of alkenylaryl.
EFFECT: reduced amount of contaminating by-products in alkylaryl hydroperoxide preparation stage.
8 cl, 4 ex
FIELD: industrial organic synthesis and catalysts.
SUBSTANCE: invention provides a method for processing methanol into dimethyl ether and liquid hydrocarbons, the latter being used as high-octane components of gasolines Ai-92, 95. Processing comprises contacting of raw material, in at least one step, in at least one reactor containing catalyst: Pentasil-type zeolite and binder, followed by cooling resulting products, condensation and separation thereof to isolate methanol conversion hydrocarbon gases, water, and desired products, after which cooled hydrocarbon gases are recycled to methanol conversion stage in at least one reactor. Catalyst is characterized by SiO2/Al2O3 molar ratio 20-100, content of sodium oxide not higher than 0.2%, and additionally contained silicon dioxide and zirconium dioxide at following proportions of components: 1.0-15.0% silicon dioxide, 1.0-5.0% zirconium dioxide, 20-70% zeolite, and binder - the balance.
EFFECT: increased yield of desired products and improved performance characteristics of catalyst.
4 cl, 5 tbl, 18 ex
FIELD: organic chemistry, chemical technology.
SUBSTANCE: invention relates to a method for synthesis of styrene. At the first step the method involves interaction of ethylbenzene hydroperoxide with propene in the presence of catalyst to yield propylene oxide and 1-phenylethanol followed by separate treatment of reaction flow and removing propylene oxide. At the second step the method involves interaction of 1-phenylethanol-containing distillate with a heterogenous dehydration catalyst at temperature 150-320°C to obtain styrene. Distillate contains 0.30 wt.-%, not above, compounds of molecular mass at least 195 Da. Invention provides decreasing the content of by-side compounds in styrene and to enhance it's the conversion degree.
EFFECT: improved method of synthesis.
3 cl, 3 tbl
FIELD: chemical industry; methods of production of the pure isobutene out of the isobutene-containing mixture.
SUBSTANCE: the invention is pertaining to the method of production of the pure isobutene out of the isobutene-containing mixture predominantly - out of hydrocarbon С4 with usage of the catalysis by the strong-acid cationite(s) including the liquid-phase interaction of the isobutene with the water at the temperature of from 60 up to 130°С in one or several sections at the stage of hydration, delamination of the being withdrawn from it stream(s), distillation of the unreacted hydrocarbons С4 from the hydrocarbon layer, decomposing of the tret-butanol in the section(s) at the stage of dehydration, separation of the formed isobutene from the water and its) purification and characterized by that isobutene and the total amount of the returned from the stage of dehydration fresh water is fed in the section of hydration in the total molar ratio from 1:0.4 up to 1:20, and it is preferential from 1:1 up to 1:5, in the straight-flow or bubbling mode in the absence of the emulsifier hydrate from 30 up to 97 % of isobutene. From the stage of the hydration in the stage of the dehydration at least one-third of the produced tret-butanol is fed in the stream, separated by the rectification from the layer of the unreacted hydrocarbons and containing from 5 up to 30 mass % of the water, and, possibly, the rest amount - in the stream of the water layer, at the total content of the different, than the isobutene, the hydrocarbons not exceeding their admissible quantity in the target isobutene, and from the stage of the dehydration the water at least partially is returned into the stage of the hydration. The presented method requires the low power input and the low metal input.
EFFECT: the invention ensures the low power input and the low metal input.
14 cl, 2 dwg, 4 ex
FIELD: one-stage production of isoprene.
SUBSTANCE: proposed one-stage production method includes continuous or cyclic delivery of isobutylene and/or tert-butanol, formaldehyde and water to aqueous acid solution and interaction of reaction mixture at distillation of mixture containing isoprene to be produced, water, unreacted starting materials and other low-boiling components from reaction mixture beyond reaction system where said reaction is conducted at regulation of concentration of high-boiling byproducts which are accumulated in said reaction mixture at interval of from 0.5 to 40 mass-%.
EFFECT: enhanced efficiency.
10 cl, 2 dwg, 1 tbl, 13 ex
FIELD: industrial organic synthesis.
SUBSTANCE: production of styrene is effected via gas-phase dehydration of 1-phenylethanol at elevated temperature in presence of dehydration catalyst including molded particles of alumina-based catalyst having BET surface area 80 to 140 m2/g and pore volume (Hg) above 0.65 ml/g.
EFFECT: reduced amount of by-products and prolonged service cycle of catalyst.
3 cl, 1 tbl, 5 ex
SUBSTANCE: invention pertains to the method of obtaining 2-methyl-2-butene from isopentane, including gas phase dehydrogenation of isopentane in the dehydrogenation zone, extraction of the C5-fraction from contact gas, mainly consisting of isopentane, tert pentanes, isoprene impurities and other hydrocarbons and obtaining a stream from it, mainly consisting of 2-methyl-2-butene, with use of a liquid phase isomerisation catalyst in a C5-fraction 2-methyl-1-butene in 2-methyl-2-butene and distillation. The method is characterised by that, the above mentioned C5-fraction, possibly containing extra piperylene and 2-pentene, directly or after distillation from the larger part of 2-methyl-2-butene, undergoes liquid phase hydroisomerisation in the presence of a solid catalyst, containing group VIII metal(s), capable of simultaneous catalysing hydrogenation of pentadienes, isoprene and possibly, piperylenes, and positional isomerisation of tert pentenes, preferably with subsequent additional isomerisation of 2-methyl-1-butene in 2-methyl-2-butene on a sulfocationite catalyst, and distillation with output of a distillate stream of mainly isopentane, containing not more than 1.0% mass, preferably not more than 0.2% mass of pentadiene(s), which are mainly recirculated in the hydrogenation zone, and output from the lower part of the recirculation stream of mainly 2-methyl-2-butene with impurities of n.pentane and possibly 2-pentenes. The invention also pertains to the method of obtaining isoprene from isopentane, which involves reaction of 2-methyl-2-butene, obtained from gas phase dehydrogenation of isopentane, with hydroperoxide with further conversion of the oxide or products of hydroxylation in isoprene.
EFFECT: obtaining 2-methyl-2-butene and isoprene from isopentane.
13 cl, 8 ex, 2 tbl, 3 dwg
SUBSTANCE: claimed invention relates to method of selective isolation of recycling flow, which contains dimethyl ester (DME), from flow, which leaves zone of methanol conversion into olefins (MTO), where said leaving flow contains water, methanol, DME, ethylene, propylene, C4-C6-olefins. Claimed method includes stages: (a) cooling and separation of at least part of leaving flow into liquid flow, which contains methanol and DME, liquid hydrocarbon flow, which contains methanol, DME and C2-C6-olefins, and vaporous hydrocarbon flow, which contains DME, methanol, ethylene and propylene; (b) distillation of DME from at least part of liquid hydrocarbon flow, separated at stage (a) in zone of DME distillation, functioning in conditions of distillation, efficient for formation of vaporous main flow, which contains DME, methanol, ethylene and propylene, and liquid hydrocarbon bottom flow, which contains C4-C6-olefins; (c) mixing of at least part of vaporous hydrocarbon flow, separated at stage (a), with at least part of main vaporous flow, produced at stage (b), with formation of enriched DME vaporous flow of light hydrocarbons; (d) supply of formed enriched with DME vaporous flow of light hydrocarbons into zone of primary absorption of DME, where said vaporous flow is brought in contact with methanol-containing selective with respect to DME solvent in conditions of wet purification, which allows to form (1) liquid bottom solvent flow, containing methanol, DME, water and substantial and undesirable amount of ethylene and propylene, and (2) main vaporous flow of product, enriched with light olefins and depleted of DME; (e) directing of at least part of liquid bottom flow, separated at stage (d), into zone of light olefins distillation, functioning in conditions of distillation, efficient for distillation of at least considerable part of ethylene and propylene, contained in liquid bottom flow, without distilling from there any considerable part of methanol, which results in formation of main flow of distillation section, containing DME, ethylene and propylene, and liquid bottom flow, containing DME, methanol, water and light olefins in amount reduced in comparison with amount of light olefins in liquid bottom solvent flow, supplied to this stage, and (f) recycling of at least part of liquid bottom flow, separated at stage (e) into zone of conversion MTO, thus selectively introducing to it additional oxygenated reactants.
EFFECT: reduction of undesirable increase of C2 and C3-olefins in recycling DME flow.
10 cl, 4 tbl, 2 dwg, 2 ex
SUBSTANCE: invention relates to a method of extracting isobutylene from an isobutylene containing fraction through hydration of the isobutylene containing fraction, obtaining a tert-butanol containing fraction and its subsequent dehydration. The method is characterised by that, dehydration is done in two stages. At the first stage, temperature is kept at 90-120°C and pressure at 1-3 kgf/cm2 and concentrated isobutylene and an aqueous solution of tert-butyl and sec-butyl alcohol are extracted, from which concentrated sec-butyl alcohol and an isobutylene containing fraction, which is taken for hydration, are extracted at the second stage. Process at the second stage is carried out at temperature 100-130°C and pressure 2-6 kgf/cm2.
EFFECT: use of the given method allows for extracting isobutylene without butene or butadiene impurities, and reduction of tert-butyl alcohol loss.
1 cl, 1 tbl, 8 ex, 1 dwg
FIELD: petroleum chemistry, chemical technology.
SUBSTANCE: crude alpha-olefin is heated, raw vinylidene olefins are isomerized in the presence of catalyst and alpha-olefin is separated from isomerized vinylidene olefin by rectification. Separation of alpha-olefin is carried out for at least two successive steps at similar temperatures on top of vat and reducing pressure of rectifying column at each following step. Condensed phase removing from top of the rectifying column at previous step is fed to feeding zone of the following step and the rectifying column at top and vat section is sprayed. For spraying the top section of column the condensed phase removing from the top of rectifying column at the same step is used and for spraying the vat section of column the vat liquid of rectifying column at the same step is used. Separated alpha-olefin is purified additionally from oxygen-containing impurities by adsorption up to polymerization degree of purity. Raw heating, isomerization, separation and adsorption are carried out in atmosphere in inert gas. The unit used for treatment of alpha-olefin includes reactor for isomerization of vinylidene olefins in raw, rectifying column wherein feeding zone is joined with reactor outlet and wherein alpha-olefin of high purity degree is removed from the column top. The unit includes also at least one rectifying column for additional treatment of alpha-olefin of high purity from isomerized vinylidene olefins and adsorption column for separation of oxygen-containing impurities in alpha-olefin of high purity wherein the column inlet is joined with the top outlet of the last rectifying column used for additional treatment of alpha-olefin of high purity and outlet is used for removing alpha-olefin of the polymerization purity degree. Invention provides enhancing quality of the end product.
EFFECT: improved method for treatment.
8 cl, 1 dwg, 1 ex
FIELD: petrochemical processes.
SUBSTANCE: invention relates to treatment of C5-hydrocarbons in order to remove cyclopentadiene impurities, which process may be, in particular, used in rubber production industry when producing hydrocarbon monomers applicable in stereospecific polymerization processes. Treatment of hydrocarbons is accomplished with cyclohexane in presence of organic solvent and alkali catalyst, after which C5-hydrocarbons are separated from reaction products via rectification. Organic solvent is selected from alkylene glycol monoalkyl ethers including their mixtures taken in amounts 0.5 to 5.0 wt % based on C5-hydrocarbons.
EFFECT: increased degree of cyclopentadiene extraction at lower reagent consumption.
8 cl, 1 tbl, 23 ex
FIELD: organic chemistry.
SUBSTANCE: invention refers to enhanced method of propane and/or butanes flow separation from original hydrocarbons containing alkylmercaptan impurities by means of fractional distillation resulted in liquid phase and separated flow from column head at pressure providing that separated flow from column head containing propane and/or butanes has temperature within 50 to 100°C, including (i) addition to specified origin hydrocarbons an amount of oxygen sufficient for mercaptan oxidation, (ii) fractional distillation of produced mixture containing at least one catalyst layer oxidising mercaptans to sulphur compounds with higher boiling temperatures and (iii) separation of sulphur compounds with higher boiling temperatures as portion of distillation liquid phase.
EFFECT: improved method of propane and/or butanes flow separation from of original hydrocarbons by means of fractional distillation resulted in liquid phase and separated flow.
8 cl, 2 tbl, 1 dwg, 1 ex
SUBSTANCE: invention relates to method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids. The method includes the following stages: (a) contact in the oxidation reaction zone of the alkane, which contains molecular oxygen gas, not necessarily corresponding to the alkene and not necessarily water in the presence of at least one catalyst, effective with the oxidation of the alkane to the corresponding alkene and carboxylic acid, alkane, oxygen and water; (b) separation in the first separating agent at least part of the first stream of products in a gaseous stream, which includes alkene, alkane and oxygen, and a liquid stream, which includes carboxylic acid; (c) contact of the mentioned gaseous stream with the solution of a salt of metal, capable of selectively chemically absorbing alkene, with the formation of a liquid stream rich in chemically absorbed alkene; (d) isolation from the flow of the solution of salt of the metal. The invention also relates to combined methods of obtaining alkyl-carboxylate or alkenyl-carboxylate (for example vinyl acetate), moreover these methods include oxidising of alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acid, isolation of alkene from the mixture of alkene, alkane and oxygen by absorption using the solution of the salt of metal and extraction of the stream rich in alkene from the solution of the salt from metal for using when obtaining alkyl-carboxylate and alkenyl-carboxylate.
EFFECT: improved method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids.
46 cl, 1 dwg
SUBSTANCE: invention is referred to the area of hydrocarbons preparation by catalytical hydrodeoxygenation of products of fast pyrolysis of a biomass and working out of the catalyst for this process. The catalyst of oxygen-organic products hydrodeoxygenation of fast pyrolysis of lignocellulose biomasses, containing either precious metal in amount of no more 5.0 wt % or containing nickel, or copper; either iron, or their combination in a non-sulphide restored shape in amount of not more than 40 wt % and transitive metals in a non-sulphide shape in amount of not more than 40 wt %, carrying agent - the rest, is described. Three variants of the catalyst preparation method, providing application of transition metals on the carrying agent by a method of impregnation of the carrying agent solutions of metal compounds are described, or simultaneous sedimentation of hydroxides or carbonates of transition metals in the presence of the stabilising carrier, or the catalyst is formed by joint alloying/decomposition of crystalline hydrate nitrates of transition metals together with stabilising components of zirconium nitrate type. The process of oxygen-organic products hydrodeoxygenation of a biomass fast pyrolysis is performed using the above described catalyst in one stage at pressure of hydrogen less than 3.0 MPa, temperature 250-320°C.
EFFECT: increase stability in processing processes of oxygen-containing organic raw materials with the low content of sulphur, and also soft conditions of process realisation.
10 cl, 12 ex, 2 tbl
SUBSTANCE: invention refers to the method of purification of paraffin hydrocarbons from methanol admixtures. The said purification is carried out in the presence of hydrogen on the catalyst containing one of the metal selected from Ni and Pd applied on the inert carrier at temperature 30-100°C, mole excess hydrogen : methanol in the range (5-50): 1 and volume hydrocarbons feed rate 1-6 hrs.-1.
EFFECT: simplifying and cheapening of the process.
1 cl, 9 ex, 1 tbl