The way isomerization of olefins
(57) Abstract:Isomerization of olefins with external links contained in the hydrocarbon loading, olefins with external links with a greater degree of substitution is carried out in the presence of a catalyst based on palladium and hydrogen at 20 - 300oC, 1 to 50 bar, a volumetric hourly rate of 50 to 600 h-1and a molar ratio of H2: olefins = 0,01 - 1. When this catalyst before it is loaded into the isomerization reactor is treated with at least one sulfur-containing compound diluted with a solvent so that the catalyst contains 0.05 to 10 wt.% sulfur. Addition of organic sulfur-containing compounds, inhibits the hydrogenation and improves the isomerizing activity of the catalyst. 13 C. p. F.-ly, 1 table. The present invention relates to a method of isomerization of olefins, more precisely isomerization of olefins with external bonds in olefins with internal links and / or isomerization of olefins with a low degree of substitution in the olefins with external links with a greater degree of substitution that is in a liquid hydrocarbon fractions WITH4WITH5and C6after vapor or catalytic pyrolysis or oligomerization, from which previously removed n the activity of the isomerization of olefins with external bonds in olefins with internal connections due to their use in alkylation or esterification.In particular, the known isomerization of 4-methyl-1-pentene (olefin with external connections and a low degree of substitution) in 2-methyl-1-penten (olefin with external links and a higher degree of substitution) and 2-methyl-2-penten (olefin with internal links) and the isomerization of 4-methyl-2-pentene (olefin with internal links) 2-methyl-2-penten (olefin with internal links) and 2-methyl-1-penten.Isomerization leading to catalysts on the basis of at least one metal of group VIII deposited on amorphous or crystalline substrate.If the original load entering the isomerization does not contain or contains little diolefines, additional difficulties arise because in conditions close to the state of thermodynamic equilibrium, it is difficult to carry out the isomerization of olefins with external bonds in olefins with internal links, while limiting the hydrogenation of olefins to paraffins. The method of controlled selective hydrogenation of n-olefins? for example, by adding sulfur to the mixture described in U.S. patent N 4724274.This patent describes, in particular, the method of obtaining 2-methyl-2-butene (olefin with internal links) from a fraction WITH5containing 2-methyl-1-butene (olefin with external links) and IU the sulfur (H2S thiol, thiophene), contained in a fraction in the amount of 2-50 ppm. Linear olefins selectively hydronauts and butene-1 isomerized in butene-2. In the absence of sulfur in the download is the hydrogenation of isopentanol, which reduces the yield of the final product.The aim of the present invention is the suppression of hydrogenation reactions, in order to favor isomerization using appropriately treated catalyst.More specifically, the present invention relates to a method of isomerization of olefins with external links contained in the download, olefins with external links with a greater degree of substitution and / or olefins with internal links, and the download contains practically no diolefin, in the presence of a catalyst based on palladium and in the presence of hydrogen at a temperature of 20-200oC, a pressure of 1-50 bar, volumetric hourly rate of 0.5-10 h-1, a molar ratio of H2: olefins = 0.01 to 1, the distinctive feature of which is that you load it into the isomerization reactor, the catalyst is treated with at least one sulfur compound, diluted with solvent, the treated catalyst containing 0.05-10 wt.% sulfur is loaded into the reactor isomers the me clock speed 50-600 h-1, and serves the load for contacting the activated catalyst. Unexpectedly it was found that the addition of organic compounds containing sulfur, can improve isomerizing activity of the catalyst.As sulfur compounds can be used sulfides and, in particular, organic sulfides, degradable when activated catalyst in the reactor.Activation of the catalyst are in a neutral or reducing environment at a temperature of 20-300 (preferably 60-210oC), a pressure of 1-50, preferably 3-20) bar, volumetric hourly speed 50-600 (preferably 100-200) h-1.As organic sulfides in the present invention using alkylsulfate, arylsulfonyl, alkylarylsulfonate or arylalkylamine, for example, utilityscale, diallyl sulfide, dibutyltin, dipropylacetic, thiophene, dimethylthiophene, ethylthiophen.You can also apply thiols (tosporte, mercaptans, thiophenol) of the formula R1SH, where R1organic radical, the thioethers of the formula R1SR2where R1and R2- same or different; organic disulfides of the formula R1SSR2and the disulfides of the formula HOR1SSR2OH,the organic timeslot, thioamides, thioesters, thiophenols. As an example named diamentina acid, thiocresol, 3,3-thiodipropionic acid, 2,3,6-trimethylsilanol, methylthiophenol, naphthalene-2-thiol, phenyl-ISO-thiocyanate, 2-phenylthiophene, thioacetamide, thiobenzamide, 2,6-dimethylthiophenol, 3,5-dimethylthiophenol, 2,21-dinitrodiphenylamine, 2,5-dithiodimorpholine, ethyldiglycol, 2-methoxythiophene, 3-methoxythiophene.The method can also be carried out in the presence of other types of sulfur-containing additives. For example, you can apply mercaptopurine formula:
< / BR>where m and n are integers;
R1, R2, R3and R4identical or different, denote hydrogen atoms or organic radicals, the alkyl, aryl, aralkyl and the other containing 1-20, preferably 1-6) atoms in the molecule; preferably n = 1-10 (examples 1-2) and m = 1-10 (example 1).You can use monotypical, for example, monothioglycerol, dithioglycolic, for example, dithiodipropionic, dithiobenzoate, for example, detioration, heterocyclic compounds, substituted mercapto groups, for example, mercaptopyridine, mercaptopyrimidine and so on; dioxyalkylene, for example, thiodiethanol [S(CH2CH2OH)2] tailslide, cyclic thioethers and their substituted derivatives (tylenchid, thiophene, thiazole, thiopyran, thioxanthone, Dicastery, 1,4-dioxan and so on), heterocyclic S-containing alkylamine, substituted mercaptans (2-methylthio-4,6-diaminopirimidina and so on).Among the above compounds, it is most preferable to use dimethyl sulfoxide, ethylthioethyl, thioglycolic acid, dithioglycolic and organic disulfides of the formula HOR1SSR2OH (as above) or formula ,
where R1and R2as stated above;
x, x' and x" are the same or different, denote integers.As an example, diethanolamide or 2,2-dithio-bis(ethanol) (DEODS) formula HOC2H4SSC2H4OH, soluble in water, glycols and polyglycols.You can also apply a polysulfide of the formula RSnR1,
where n is an integer of 3 to 20 (preferably 4-8, better 5-7); R and R1- same or different represent organic radicals, each containing 1-150 carbon atoms, preferably 5-40, better 7-16 C atoms, these radicals selected from saturated or unsaturated, linear or branched or naphthenic type Akilov, arrow, alkylaryl, S="ptx2">The most preferred example of the polysulfide is dicret. todatetimeoffset (n= 5), where R and R1every radical tert.- didodecyl. This product is made by the company Elf Acetan under the trademark TPS 32 (sulfur content of 32 wt.%).An example is dicret.dinonylphenol (n=5), where R and R1every radical tert.Neil.Agent pretreatment using dilute adequate amount of solvent, the choice of which depends on the nature of the sulfonation agent.The solvent may be selected from the following compounds, used separately or in a mixture: a light gasoline fraction, for example, so Kip. 60-95oC; hexane fraction with so Kip. 63-68oC; gasoline fraction F (the content of aromatic hydrocarbons 10-20%, preferably 15% by volume) so Kip. 100-160oC; white spirit (the content of aromatic hydrocarbons 14-22, preferably 17% by volume) so Kip. 150-250oC; any hydrocarbon or non-hydrocarbonaceous fraction, similar to the previous gasoline.The sulfonation agent can be used in solvents such as alcohols (methanol, ethanol, propanol), aldehydes, ketones, ethers and esters, polyalcohol, acid as solvent.After sulfur impregnation, the catalyst is subjected to heat treatment at a temperature of 100-200oC.In accordance with the invention, in the catalyst, it is advisable to enter of 0.05-10 wt.% preferably 0.02 to 1 wt.% sulfur on the catalyst inventory.The catalyst also contains 0.02 to 2 wt.% preferably, 0.05 to 1 wt.%, most preferably, 0.05 to 0.5 wt.% palladium.Pre-sulfated activate the catalyst in the isomerization reactor before the introduction of the boot.The isomerization reaction is carried out under a pressure of 1-50, preferably 5-30) bar, a temperature of 20-200, preferably 50-150)oC, at a volumetric hourly rate of 0.5-10 (preferably 1-6) h-1when the molar ratio of H2: olefins = 0.01 to 1, preferably of 0.02 to 0.2).Sulfa sulfur compound may be added in the download.The following examples illustrate the invention.Example 1 (comparative)
100 cm3catalyst LD265 (catalyst A) firm Societe Procatalyse, containing 0.3 wt.% palladium on Al2O3placed in a steel tube with a diameter of 3 see This catalyst commonly used for selective hydrogenation of fractions, poluri 200oC hydrogen supplied for 5 h at 30 l/h, and then cooled in a stream of hydrogen and nitrogen purge.Then measure isomerizing and hydrogenating activity of the catalyst with the hydrocarbon loading composition in wt.% specified in the table.For this purpose, the load is passed in the form of a downward flow of hydrogen through the catalyst bed under conditions shown in the table.Emerging from the reactor flows analyzed by chromatography in the vapor phase in PONA capillary column 50 m height.The results of the study are presented in the column "Example 1" of the table.One advantage of the invention consists in the possibility of carrying out the sulfonation on specialized units, designed only for this reaction, and the avoidance of contamination of the isomerization reactor (and other future devices) sulfur compounds. Another advantage is that the pre-sulfated catalyst can africasat with air when it is loaded into the reactor. This fact greatly facilitates the conditioning and transport of the catalyst.Examples 2-6 (in accordance with the invention)
100 with oputyvayut dry aqueous solution of formic acid concentration of 2.2 mol/l, and deoxidised concentration of 0.15 mol/l and dried 6 hours at 120oC. the Treated catalyst (catalyst B) was placed in a steel tube with a diameter of 3 cm and subjected to activation by reduction with hydrogen at a temperature of 200oC, submitted for 5 h at 30 l/h with subsequent cooling of the catalyst in a stream of hydrogen by purging with nitrogen. Then measure isomerizing and hydrogenating activity of the catalyst with the hydrocarbon loading, the composition of which is specified in the table. To this end, skip this load in the form of a downward flow of hydrogen through the catalyst bed under the conditions listed in the table.Emerging from the reactor flows analyzed by chromatography in the vapor phase in PONA capillary column 50 m height.The results of the study are presented in columns "Examples 2-6 table of example 1. The table shows that according to the invention the quantity of olefins type 2-methyl-pentanol (most desired olefins) in examples 2-6, the most high, while the ratio of alkanes to misappropriation of olefins is reduced compared to the results of example 1. 1. The way isomerization of olefins with external links contained in the hydrocarbon loading, not containing virtually diolefines in olefins with external links with the pain of the hydrogen at a temperature of 20 200oC, a pressure of 1 to 50 bar, a volumetric hourly rate of 0.5 - 10 h-1and a molar ratio of H2: olefins = 0,01 - 1,0 characterized in that the catalyst before it is loaded into the isomerization reactor is treated with at least one sulfur-containing compound, diluted with solvent, and the treated catalyst containing 0.05 - 10 wt.% sulfur is loaded into the reactor and activated in a neutral or reducing environment at a temperature of 20 - 300oC, a pressure of 1 to 50 bar and a volumetric hourly rate of 50 to 600 h-1and the hydrocarbon loading in contact at isomerization conditions with an activated catalyst.2. The method according to p. 1, wherein the load is a fraction of C5and C6obtained in a vapor-phase catalytic pyrolysis or by oligomerization and contains practically no diolefines.3. The method according to p. 1, characterized in that the catalyst consists of palladium deposited on alumina.4. The method according to PP.1 to 3, characterized in that the sulfur-containing compound selected from organic alkylsulfides, arylsulfatase, alkylarylsulfonate or organic arylalkylamines, thiols, thiadiazole, organic timeslot, thioamides, tio is storytell choose from gasoline and hydrocarbon fractions.6. The method according to PP. 1 to 5, characterized in that the solvent used alcohols, aldehydes, ketones, ethers and esters, polyalcohol, acid, polyacid, glycols.7. The method according to p. 1, characterized in that the solvent is water.8. The method according to PP. 1 to 7, characterized in that the activation is carried out at a temperature of 60 - 210oC, a pressure of 3 to 20 bar and a volumetric hourly rate of 100 - 200 h-1.9. The method according to PP.1 to 8, characterized in that the isomerization is carried out at a temperature of 50 to 150oC, a pressure of 5 to 30 bar, an hourly volume rate of 1 to 6 h-1and a molar ratio of H2: olefins = 0,02 - 0,2.10. The method according to PP.1 to 9, characterized in that the sulfur compound injected in the download.11. The method according to PP.1 to 10, characterized in that the catalyst contains 0.2 - 1 wt.% sulphur.12. The method according to PP.1 - 11, characterized in that the catalyst contains 0.02 to 2.0 wt.% palladium.13. The method according to PP.1 - 12, characterized in that the catalyst contains 0.05 to 1.0 wt.% palladium.14. The method according to PP.1 - 13, characterized in that the catalyst contains 0.05 - 0.5 wt.% palladium.
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: organic chemistry, petroleum chemistry, chemical technology.
SUBSTANCE: method involves preparing ethylene and hexane-1 from butene-1 by the exchange reaction of butene-1 and the isomerization reaction of synthesized hexane-3 to hexane-1. The parent material represents a mixed butene flow wherein butene-1 is isomerized to butene-2 after separation of isobutylene followed by the isomerization reaction of butene-2 to butene-1. Butene-1 is a raw for the exchange reaction.
EFFECT: improved preparing method, simplified technology process.
32 cl, 4 tbl, 4 ex
SUBSTANCE: catalyst system component is obtained via mechanical activation of a solid mixture with the ratio of 2-ethyl hexanoate of group I metal:CrCl3>1:1 and heating the activated mixture to obtain the desired product. The ethylene oligomerisation catalyst system contains an organoaluminium compound of general formula AlR3, a complexing agent, a modifier, a solvent and a chromium-containing component obtained using the disclosed method. The ethylene oligomerisation method is carried out in the medium of a hydrocarbon solvent at temperature of 40-95°C and ethylene pressure of 1-5 MPa in the presence of said catalyst system.
EFFECT: simple method of producing a component of catalyst systems for oligomerising olefins, high output of the product when oligomerising ethylene to hexene-1, high selectivity of the process and purity of hexene-1, low probability of secondary reactions.
4 cl, 1 tbl, 16 ex
SUBSTANCE: invention relates to a method of producing 1-hexene from ethylene trimerisation method, involving use of the catalyst system consisting of chromium complex of general formula [CrCl3(H2O)((Ph2P(1.2-C6H4)P(Ph)(1.2-C6H4)CH=CR2)], where R is hydrogen or metal group, an activator is represented by methylaluminoxane and co-activator, is used as trimethylaluminium. System components are in the following molar ratio: chromium complex: MAO: TMA = 0.1% : 21.4% : 78.5%, in the solution methylcyclohexane at temperature 70-90°C, pressure of 30-40 bar. Invention provides selectivity of the process for trimerisation of ethylene 89-95% of fraction C6, made on 99.3-99.5 % of 1-hexene with high efficiency of process from 900 up to 1400 kg of the product/gCr·h and minimal formation of polymer - 0.3 wt% of all products.
EFFECT: selectivity process for trimerisation of ethylene 89-95% of fraction C6.
1 cl, 1 tbl, 13 ex
SUBSTANCE: present invention relates to an ethylene oligomerisation method. Method involves following steps: a) feeding ethylene, a solvent and catalyst composition containing catalyst and cocatalyst, into a reactor, b) oligomerisation of ethylene in reactor, c) discharging reactor effluent, containing linear alpha-olefins, including 1-butene, solvent, unconsumed ethylene, dissolved in output stream of reactor, and catalyst composition, from reactor, d) separation of ethylene and 1-butene together from rest of reactor effluent and e) recirculation of at least part of ethylene and 1-butene, separated at step d), into reactor. Equal amounts of 1-butene are removed from reactor with reactor effluent and recycled into reactor at step e).
EFFECT: use of disclosed method allows stable operation of reactor, improves heat removal and prevents clogging of reactor.
15 cl, 1 ex, 1 tbl, 3 dwg
SUBSTANCE: invention relates to a process of separating hexene-1 from the mixture obtained in the reaction of section of the ethylene trimerization process, wherein mentioned mixture comprises ethylene, solvent, catalyst and ethylene trimerization products derived, including hexene-1. The method includes at least the following steps: a) separation in the first distillation column a mixture formed by the reaction of ethylene trimerization on top fraction containing ethylene and a bottoms fraction, b) separation of at least one other distillation column at least part of the stream bottoms fraction obtained in step a) for the top fraction containing hexene-1 and butene-1, and a bottoms fraction, c) separation in the final distillation column, at least part of the fraction containing hexene-1 and butene-1, get constant in step b), at the top fraction containing mainly 1-butene and a bottoms fraction containing mainly 1-hexene, wherein in said method: at least one portion of the stream bottoms fraction obtained in step b), is recycled to the a reaction section and at least one other portion of mentioned bottom fraction obtained in step b) is used in at least one recirculation loop, connecting the reaction section and the column of mentioned step b), mentioned recirculation loop allows to cool the reaction section and provide repeated of partial evaporation in mentioned column from step b).
EFFECT: process is more energy efficient.
18 cl, 8 ex, 2 dwg
FIELD: basic organic synthesis, chemical technology.
SUBSTANCE: invention relates to the improved method for isomerization reaction of pentane-hexane fraction with aim for preparing high-octane additive for gasoline. Pentane-hexane fraction is subjected for isomerization reaction in reaction-rectifying process using a low-temperature platinum-alumina catalyst. The parent raw is subjected for preliminary separation for pentane and hexane fractions. These fractions are subjected for separate isomerization that is carried out in vapor phase in reaction zone in bottom of reaction-rectifying column. Catalyst is placed under plates of zone and pressure in reaction zone in maintained in the range from 0.6 to 3.6 MPa, temperature - from 110.0oC to 200.0oC in the mole ratio hydrogen : hydrocarbons at inlet into column from 0.03:1 to 4:1. Method provides enhancing conversion of n-pentane, n-hexane and methylpentanes to high-octane isomers, elevating octane number of isomerizate and constructive simplifying the process.
EFFECT: improved preparing method.
1 dwg, 1 ex
FIELD: petrochemical processes catalysts.
SUBSTANCE: catalyst based on crystalline element-alumino-phosphates and having structure A1PO-31 (SATO) is prepared by providing first reaction mixture containing aluminum source, phosphoric acid, and one or more sources of substituting element as well as organic structure-forming compound followed by crystallization of above mixture under hydrothermal conditions required to form crystals with structure A1PO-31 and isolation of solid crystallization product, to which further modifying group VIII metal is added. Structure-forming compound mentioned above is selected from di-n-pentylamine and mixture thereof with other di-n-alkylamines and substituting element is selected from magnesium, zinc, silicon, cobalt, manganese, nickel, and cadmium. Method of isomerization of n-paraffins at elevated temperature and hydrogen pressure in presence of above-described catalyst is also disclosed.
EFFECT: increased activity and selectivity of catalyst.
4 cl, 1 dwg, 3 tbl, 17 ex
FIELD: petrochemical processes.
SUBSTANCE: feedstock is brought into contact with preliminarily activated zeolite-containing catalyst, namely mordenite-supported Pt, at 250-300°C, pressure 1.5-3.5 MPa, hydrogen-containing gas-to-feedstock ratio 300-1000 nm3/m3, and feed flow rate 1.0-4.0 h-1. Preliminary activation of zeolite-containing isomerization catalyst is conducted in two successive steps: drying catalyst in inert gas flow; reducing catalyst in hydrogen-containing gas flow; and supplying feedstock and setting steady-state isomerization process. Drying of zeolite-containing catalyst in inert gas flow is effected under conditions of gradually raised temperature from 120°C at temperature raise rate 10-15°C/h and ageing for 2-5 h at 120°C to 350°C followed by ageing at this temperature, whereupon temperature is lowered to 130°C. Reduction of zeolite-containing catalyst in hydrogen-containing gas flow is effected at gradually raised temperature to 220-350°C at temperature rise rate 15-25°C/h and ageing for 2-6 h at 220-350°C, whereupon temperature is lowered to 180°C. Initial feedstock is supplied at 180°C in circulating hydrogen-containing gas flow, aged for 4 h at 180°C and then gradually heated to 250°C at heating rate 5°C/h, after which further heated at heating rate 5°C a day to achieve process characteristics meeting product quality requirements.
EFFECT: increased catalyst activity, selectivity, and working stability.
2 cl, 2 tbl, 17 ex
FIELD: petrochemical process catalysts.
SUBSTANCE: group of inventions relates to conversion of hydrocarbons using micro-mesoporous-structure catalysts. A hydrocarbon conversion process is provided involving bringing hydrocarbon raw material, under hydrocarbon conversion conditions, into contact with micro-mesoporous-structure catalyst containing microporous crystalline zeolite-structure silicates composed of T2O3(10-1000)SiO2, wherein T represents elements selected from group III p-elements and group IV-VIII d-elements, and mixture thereof, micro-mesoporous structure being characterized by micropore fraction between 0.03 and 0.40 and mesopore fraction between 0.60 and 0.97. Catalyst is prepared by suspending microporous zeolite-structure crystalline silicates having above composition in alkali solution with hydroxide ion concentration 0.2-1.5 mole/L until residual content of zeolite phase in suspension 3 to 40% is achieved. Thereafter, cationic surfactant in the form of quaternary alkylammonium of general formula CnH2n+1(CH3)3NAn (where n=12-18, An is Cl, Br, HSO4 -) is added to resulting silicate solution suspension and then acid is added formation of gel with pH 7.5-9.0. Gel is then subjected to hydrothermal treatment at 100-150°C at atmospheric pressure or in autoclave during 10 to 72 h to produce finished product.
EFFECT: enlarged assortment of hydrocarbons and increased selectivity of formation thereof.
16 cl, 2 dwg, 2 tbl
FIELD: organic synthesis.
SUBSTANCE: invention pertains to obtaining branched alkanes with general formula CnH2n+2, where n = 4-10. CCI4 is gradually added to a mixture of hexane, triethylaluminium - Et3Al and a catalyst - PdCl2, in an argon atmosphere at atmospheric pressure and temperature of 10-60°C for a period of 0.5-2 hours. The molar ratio of hexane: Et3Al : CCl4 : PdCl2 is 75:10:20:0.1.
EFFECT: obtaining of a mixture of branched alkanes with high output.
1 tbl, 1 ex
SUBSTANCE: invention pertains to a catalyst and a method for selective increase in quality of paraffin raw material, with the aim of obtaining concentrated isoparaffin product as a benzine component. Description is given of the catalyst, which consists of a carrier from a sulphated oxide or hydroxide of group IVB (IUPAC 4) metals. The first component is, at least, from one lanthanide element or an yttric component, which is mainly ytterbium, and at least, one metal of the platinum group, which is mainly platinum, and a fireproof oxide binding substance, on which is dispersed at least, one metal of the platinum group. Description is given of the method of making the above mentioned catalyst, including a sulphated oxide or hydroxide of a group 1VB metal, depositing of the first component, mixing the sulphated carrier with the fireproof inorganic oxide of the oxide carrier, burning, depositing of the second component and subsequent burning. Description is given of the method of converting hydrocarbons through contacting with raw materials with the catalyst described above.
EFFECT: selective increase in quality of paraffin raw materials.
12 cl, 2 tbl, 2 dwg, 7 ex
SUBSTANCE: catalyst includes carrier, which contains tungsten oxide or hydroxide of at least one element from grope IVB ("ИЮПАК 4"), first component from at least one element from lanthanide line, yttrium and their mixture, and second component, which contains at least one component of metal from platinum group or their mixture. Also described is method of hydrocarbons transformation by contacting of raw material with solid acid catalyst, described above, with transformed product formation. Described is method of paraffin raw material isomerisation by its contacting with said catalyst at temperature from 25 to 300°C, pressure from 100 kPa to 10 MPa and volumetrical speed of liquid feeding from 0.2 to 15 hour-1 , with further product release, enriched by isoparaffins.
EFFECT: stability in hydrocarbons transformation process, increase of isoparaffins content.
10 cl, 1 tbl, 2 ex, 8 dwg