Method for isomerization of paraffin hydrocarbon

FIELD: petroleum chemistry, organic chemistry, chemical technology.

SUBSTANCE: method involves contacting the parent raw flow in the flow-type reactor with oxygen-free gas flow at increased temperature with a catalyst comprising a precious metal of VII group of the periodic system of elements. The industrial isomerization platinum-containing catalyst SI-1 or industrial hydrogenation catalyst "palladium on active aluminum oxide in sulfured form" is used as a catalyst. Contact of the parent raw with catalyst is carried out by its feeding in inert gas flow, for example, nitrogen at the volume rate 1-2 h-1 at temperature 320-370°C in the presence of the additive representing a solution of hydroquinone or p-benzoquinone in isopropyl alcohol and taken in the concentration 0.01-0.5 mole/l wherein the additive is fed to the parent raw flow in the amount 5-30 vol.%. Invention provides carrying out the highly selective isomerization and cyclization of light petroleum fractions in on industrial Pt- and/or Pd-containing catalysts with the high yield of the end products no containing aromatic compounds and not requiring the presence of hydrogen or hydrogen-containing gas for its realization and regeneration of the catalyst.

EFFECT: improved method for isomerization.

4 cl, 2 tbl, 2 ex

 

The invention relates to processes of isomerization and cyclization of hydrocarbons in the presence of catalysts containing compounds of platinum and/or palladium, in particular to the process of isomerization of unbranched or malorazmernyj paraffins in more branched paraffins, which are themselves high-octane components of gasoline, or which can be used as raw material in various other processes refining (e.g., alkylation), which also receive high-octane components of gasoline.

Processes for the isomerization of normal alkanes to isoalkanes in the catalytic compositions containing a noble metal of group VIII, in particular platinum, palladium or a mixture of, on the active aluminiumoxide media, including promoted, as well as containing the oxides of other elements, as well as various additives well known (application RU # 98120706, class C 07 C 5/22, publ. 2000; US No. 5494571, CL 10 G 35/085, 1996; US No. 5120898, C 07 C 5/27, 1992; RU №2219153, class C 07 C 5/22, 1999; RU №2176233, class C 07 C 5/27, 2000; EN No. 2158723, class C 07 C 5/27, 1999; RU №2196124, class C 07 C 5/27, 2002; RU №2191627, class C 07 C 5/27, 1996).

The disadvantage of these processes is the rapid decline in catalyst activity, in particular, due to the formation and accumulation of high molecular weight hydrocarbons in the pores of the catalyst for isomerization, and on its surface, b is okoruwa its active centers, which leads respectively to the short lifetime of the catalyst and unstable yield of hydrocarbon products. In addition, the implementation of the isomerization process requires the presence of hydrogen or hydrogen-containing gas. Moreover, it should be noted that to prevent deactivation of the catalyst and thus increasing the life of the isomerization of n-alkanes is carried out in the presence of high content of hydrogen or a hydrogen-containing gas with respect to the original hydrocarbon and, as a rule, at relatively high temperatures, which significantly complicates the technological process and accordingly increases the cost of it.

The closest analogue to the claimed invention is a method for the isomerization of light gasoline fractions, described in the article "Medium-temperature isomerization of light gasoline fractions" authors Aigoual etc. W. "Chemistry and technology of fuels and oils", 2000, No. 5, S. 30-32, which are as follows.

Easy pentane-hexane fraction With5-C6Nicholas - 70°served in the flow reactor at platinum industrial zeolite catalyst C-1 (Babikov A.F., Shakun A.N., Fedorova M. and other Refining and petrochemicals, 1996, No. 10, p.17-19) with a bulk velocity of 2-3 .5 h-1when the temperature at the inlet of the reactor 270°giving the situation in the reactor 2.5 MPa and the ratio of the circulation of hydrogen gas of 1000 m3/m3.Mainegenealogy period of approximately 2 years with a total service life of the catalyst 6-8 years.

The isomerization process proceeds with high selectivity and allows for the passage to increase the octane number by 12 points.

However, this process is characterized by low stability of the catalyst regeneration which requires high temperatures, accompanied by a loss and deterioration of the catalyst, high energy consumption, and emissions of gases regeneration. In addition, as all of the above methods analogous isomerization of paraffins, this method also requires the use of expensive hydrogen or hydrogen-containing gas.

Object of the invention is the creation of highly selective method for the isomerization and cyclization of light oil fractions industrial Pt and/or Pd-containing catalysts with a high yield of the final products do not contain aromatic compounds, and does not require for its implementation of hydrogen or hydrogen-containing gas and catalyst regeneration.

The problem is solved in that in the method of isomerization of light oil fractions or, at least, one of the original hydrocarbon selected from the group of paraffins containing 5 to 6 at the MOU carbon in the molecule, includes contact in flow reactor flow of the feedstock at elevated temperature in a current of oxygen-free gas with a catalyst containing a noble metal of group VIII, according to the invention the contact of the feedstock with the catalyst is carried out at a temperature of 320-370°With the current of inert gas in the presence of the additive solution of hydroquinone or p-benzoquinone in isopropyl alcohol with a concentration of 0.01-0.5 mol/l, and the additive is served in the flow of raw materials in the amount of 5-30 vol.%.

The problem is solved also by the fact that as the inert gas using nitrogen at a molar ratio of raw materials: nitrogen =1:1;

and also the fact that as the isomerization catalyst used industrial platinochloride isomerization catalyst C-1 or industrial hydrogenation catalyst palladium on active aluminum oxide in sulfurated form";

and the fact that the material in the reactor is carried out with a volume rate of about 1-2 h-1.

The invention consists in the following.

The flow of raw materials, containing in its structure at least one light (C5-C6) n-alkane and an additive, hydroquinone or p-benzoquinone in the form of a solution in isopropyl alcohol with a concentration of 0.01-0.5 mol/l, served in a flow reactor, a catalyst containing platinum or palladium on a carrier (active formaxima aluminum or zeolite), on the active centers which the isomerization process. According to this invention preferably use industrial isomerization catalysts, such as SI-1 (Babikov A.F., Shakun A.N., Fedorova M. and others - Refining and petrochemicals, 1996, No. 10, p.17-19), and hydrogenation, such as palladium on active aluminum oxide in sulfurated form"containing, wt.%: Pd-0,45÷0,55; S-0,10÷0,20; Fe-0,02; Na-0,03 having a bulk density of 0.64 g/cm3(THE 38.10249-92).

To activate the freshly prepared catalyst it is heated in a current of air to 450-550°With speeds of 10-15°/min at this temperature, incubated for 2-2,5 hours, after which the air flow is replaced with inert gas, for example nitrogen, at a speed of submission of 30-35 ml/min, the molar ratio of raw materials : inert gas =1:1, when reaching the operating temperature in the reactor 320-370°To carry out the supply of raw materials with a bulk velocity of 1-2 h-1.

This method allows to carry out the isomerization process of hydrocarbon light oil fraction at atmospheric pressure in a stream of inert gas in the absence of hydrogen or hydrogen-containing gas and to operate the catalyst without loss of its activity, allowing respectively to avoid a stage of regeneration, accompanied, as a rule, emissions of regeneration, and loss and wear the catalyst.

Tests show that the lifetime of the catalyst is not less than 8 years. The selectivity of the method according to isoalkanes is 80%, the selectivity for naphthenic - 20%.

The resulting transformations were estimated by gas chromatography using the software complex ECHOGRAM (patent RU 2418826), consisting of a chromatograph "Cambridge GC 95" with a flame ionization detector and a computer database. This database contains indexes holding in Kovacs. Column quartz length of 80 m with an inner diameter of 0.2-0.3 mm, stationary phase SE - 30, the volume of the sample is 0.1-0.2 mm.

The following examples of the method only to illustrate the invention without limiting it.

Example 1 (invention). A portion of 10 g of freshly prepared catalyst is a zeolite of structural type beta (Na7Al7Si57About128, SiO2/Al2O3=40) with 0.1 wt.% Pt (industrial catalyst C-1) were placed in a quartz flow type reactor with an inner diameter of 20 mm and a length of 250 mm and activated by heating it in a stream of air up to 500°With a speed of 10°C/min followed by holding at that temperature for 2 hours, after which the flow of air was replaced with nitrogen (30 ml/min) at a molar ratio of raw materials : nitrogen =1:1, the temperature was lowered to 350 working°and carried out the supply of raw materials, p is establisheda a mixture of n-hexane and a solution of hydroquinone in isopropyl alcohol (0.3 mol/l) at a volume ratio of hexane : a solution of 95:5, with a bulk velocity 1 h-1. Output dimethylsiloxane amounted to 62.7 percent; naphthenes with 20.4%, methylseleninic to 15.7%. The results in table 1.

Example 2 (invention). A portion of 5 g of freshly prepared catalyst is palladium on active aluminum oxide in sulfurated form was placed in a quartz reactor flow type with internal diameter 10 mm, length 250 mm, was heated in a stream of air up to 450°With a speed of 10°C/min at this temperature in an atmosphere of air was kept for 2 hours, after which the flow of air was replaced with nitrogen (30 ml/min) at a molar ratio of raw materials : nitrogen =1:1, lowered the temperature to 350 working°With, then carried out the supply of raw materials with a bulk velocity of 1.5 h-1. Isomerization of n-hexane were carried out in the presence of a solution of hydroquinone in isopropyl alcohol with a concentration of 0.01 mol/l, was fed into the stream of hexane. The volume ratio of hexane : a solution of 70:30. The results are presented in table 2.

Table 1

The products of transformation of the initial mixture on the catalyst C-1 (example 1)
No.Substancemole%
1isopentane13,9
22.2-dimethylbutan30,5
32,3-d is methylpentan 0,4
42,3-dimethylbutan21,1
52,2-dimethylpentan8,9
6Methylcyclopentane1,9
72,4-dimethylpentan1,8
8cyclohexane7,8
92-methylhexan1,8
101,2,4-trimethylcyclopentanone7,9
113,3,5-trimethylhexane1,2
12CIS-1,2-dimethylcyclohexane0,6
13TRANS-1,2-dimethylcyclohexane2,2
The octane number for MM - 90

Table 2

The products of transformation of the initial mixture on the catalyst Palladium on active aluminum oxide in sulfurated form" (example 2).
No.Substancemole%
1ether11,3
22-methylhexan4,1
3trimethylcyclohexane75,9
42.2-dimethylbutan 1,3
52,3-dimethylbutan1,4
62,2-dimethylpentan1,2
72,3-dimethylpentan0,6
8cyclohexane4,2
The octane number for MM - 83

1. Method of isomerization of at least one source of a hydrocarbon selected from the group of paraffins containing 5 to 6 carbon atoms in the molecule, including the contact of the flow of raw materials in a flow reactor in a stream of oxygen-free gas at an elevated temperature with a catalyst containing a noble metal of group VIII, characterized in that the contact of the feedstock with the catalyst is carried out in a current of inert gas at a temperature of 320-370°in the presence of the additive solution of hydroquinone or p-benzoquinone in isopropyl alcohol with a concentration of 0.01-0.5 mol/l, and the additive is served in the flow of raw materials in the amount of about 5-30.%.

2. The method according to claim 1, characterized in that as the inert gas using nitrogen at a molar ratio of raw materials: nitrogen =1:1.

3. The method according to claim 1, characterized in that the isomerization catalyst used industrial platinochloride isomerization catalyst C-1 or industrial hydrogenation catalyst palladium n the active aluminum oxide in sulfurated form".

4. The method according to claim 1, characterized in that the volumetric feed rate to the reactor is 1-2 h-1.



 

Same patents:

FIELD: chemistry of aromatic compounds, chemical technology.

SUBSTANCE: process involves the following stages: feeding (C2-C5)-alkane, for example, ethane and (C2-C5)-alkyl-substituted aromatic compound, for example, ethylbenzene into dehydrogenation reactor for the simultaneous dehydrogenation to (C2-C5)-alkene, for example, to ethylene, and (C2-C5)-alkenyl-substituted aromatic compound, for example, styrene; separation of the outlet dehydrogenation flow for extraction of gaseous flow containing alkene, hydrogen and alkane, and for extraction of aromatic compounds with the high effectiveness by cooling and compression; feeding a gaseous flow and (C6-C12)-aromatic compound into the alkylation reactor for preparing the corresponding (C2-C5)-alkyl-substituted aromatic compound that is recirculated into the dehydrogenation reactor; feeding the blowing flow from the alkylation unit containing alkane and hydrogen for the separation stage by using cryogenic separator for extraction of alkane that is recirculated into the dehydrogenation reactor, and hydrogen that is extracted with the purity value 99%. Invention provides the development of economic and highly effective process for preparing alkenyl-substituted aromatic compounds.

EFFECT: improved preparing method.

61 cl, 2 tbl, 2 dwg, 2 ex

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: invention relates to dehydrogenation of isoamylenes to isoprene on iron oxide self-regenerating catalysts. Method involves addition of piperylenes in the concentration up to 4 wt.-% representing a by-side product in manufacturing process of isoprene by the indicated method to the parent isoamylenes before their dehydrogenation. Method provides enhancing selectivity of method for isoamylenes dehydrogenation to isoprene in the presence of iron oxide self-regenerating catalysts.

EFFECT: improved preparing method.

1 tbl, 6 ex

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention concerns catalysts for dehydrogenation of C2-C5-alkanes into corresponding olefin hydrocarbons. Alumina-supported catalyst of invention contains 10-20% chromium oxide, 1-2% alkali metal compound, 0.5-2% zirconium oxide, and 0.03-2% promoter oxide selected from zinc, copper, and iron. Precursor of alumina support is aluminum oxide hydrate of formula Al2O3·nH2O, where n varies from 0.3 to 1.5.

EFFECT: increased mechanical strength and stability in paraffin dehydrogenation process.

9 cl, 1 dwg, 3 tbl, 7 ex

FIELD: petrochemical processes.

SUBSTANCE: 1,3-butadiene is obtained via catalytic dehydrogenation of n-butylenes at 580-640°C and essentially atmospheric pressure while diluting butylenes with water steam at molar ratio 1:(10-12) and supplying butylenes at space velocity 500-750 h-1. Catalyst is composed of, wt %: K2O 10-20, rare-earth elements (on conversion to CeO2) 2-6, CaO and/or MgO 5-10. MoO3 0.5-5, Co2O3 0.01-0.1, V2O5 0.01-0.1, and F2O3 the balance. Once steady condition is attained, dehydrogenation is carried out continuously during all service period of catalyst.

EFFECT: increased yield of 1,3-butadiene and process efficiency.

2 ex

FIELD: petrochemical processes.

SUBSTANCE: simultaneous dehydrogenation of mixture containing alkyl and alkylaromatic hydrocarbons is followed by separating thus obtained dehydrogenated alkyl hydrocarbon and recycling it to alkylation unit. Dehydrogenation reactor-regenerator employs C2-C5-alkyl hydrocarbon as catalyst-transportation carrying medium.

EFFECT: increased process flexibility and extended choice of catalysts.

36 cl

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention relates to production of olefin or diolefin hydrocarbons via dehydrogenation of corresponding paraffinic C3-C5-hydrocarbons carried out in presence of catalyst comprising chromium oxide and alkali metal deposited on composite material including alumina and aluminum wherein percentage of pores larger than 0.1 μm is 10.0-88.5% based on the total volume of open pores equal to 0.10-0.88 cm3/g. Preparation of catalyst involves treatment of carrier with chromium compound solution and solution of modifying metal, preferably sodium or sodium and cerium. Carrier is prepared by from product resulting from thermochemical activation of amorphous hydrargillite depicted by formula Al2O3·nH2O, where 0.25<n<2.0, added to homogenous mass in amount 1.0 to 99.0% using, as additional material, powdered aluminum metal, which is partly oxidized in hydrothermal treatment and calcination stages. Hydrocarbon dehydrogenation process in presence of the above-defined catalyst is also described.

EFFECT: increased activity and selectivity of catalyst.

3 cl, 2 dwg, 4 tbl, 7 ex

The invention relates to catalysts used in the dehydrogenation of hydrocarbons, and to methods of using catalysts

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention relates to production of olefin or diolefin hydrocarbons via dehydrogenation of corresponding paraffinic C3-C5-hydrocarbons carried out in presence of catalyst comprising chromium oxide and alkali metal deposited on composite material including alumina and aluminum wherein percentage of pores larger than 0.1 μm is 10.0-88.5% based on the total volume of open pores equal to 0.10-0.88 cm3/g. Preparation of catalyst involves treatment of carrier with chromium compound solution and solution of modifying metal, preferably sodium or sodium and cerium. Carrier is prepared by from product resulting from thermochemical activation of amorphous hydrargillite depicted by formula Al2O3·nH2O, where 0.25<n<2.0, added to homogenous mass in amount 1.0 to 99.0% using, as additional material, powdered aluminum metal, which is partly oxidized in hydrothermal treatment and calcination stages. Hydrocarbon dehydrogenation process in presence of the above-defined catalyst is also described.

EFFECT: increased activity and selectivity of catalyst.

3 cl, 2 dwg, 4 tbl, 7 ex

FIELD: petrochemical processes.

SUBSTANCE: simultaneous dehydrogenation of mixture containing alkyl and alkylaromatic hydrocarbons is followed by separating thus obtained dehydrogenated alkyl hydrocarbon and recycling it to alkylation unit. Dehydrogenation reactor-regenerator employs C2-C5-alkyl hydrocarbon as catalyst-transportation carrying medium.

EFFECT: increased process flexibility and extended choice of catalysts.

36 cl

FIELD: petrochemical processes.

SUBSTANCE: 1,3-butadiene is obtained via catalytic dehydrogenation of n-butylenes at 580-640°C and essentially atmospheric pressure while diluting butylenes with water steam at molar ratio 1:(10-12) and supplying butylenes at space velocity 500-750 h-1. Catalyst is composed of, wt %: K2O 10-20, rare-earth elements (on conversion to CeO2) 2-6, CaO and/or MgO 5-10. MoO3 0.5-5, Co2O3 0.01-0.1, V2O5 0.01-0.1, and F2O3 the balance. Once steady condition is attained, dehydrogenation is carried out continuously during all service period of catalyst.

EFFECT: increased yield of 1,3-butadiene and process efficiency.

2 ex

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention concerns catalysts for dehydrogenation of C2-C5-alkanes into corresponding olefin hydrocarbons. Alumina-supported catalyst of invention contains 10-20% chromium oxide, 1-2% alkali metal compound, 0.5-2% zirconium oxide, and 0.03-2% promoter oxide selected from zinc, copper, and iron. Precursor of alumina support is aluminum oxide hydrate of formula Al2O3·nH2O, where n varies from 0.3 to 1.5.

EFFECT: increased mechanical strength and stability in paraffin dehydrogenation process.

9 cl, 1 dwg, 3 tbl, 7 ex

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: invention relates to dehydrogenation of isoamylenes to isoprene on iron oxide self-regenerating catalysts. Method involves addition of piperylenes in the concentration up to 4 wt.-% representing a by-side product in manufacturing process of isoprene by the indicated method to the parent isoamylenes before their dehydrogenation. Method provides enhancing selectivity of method for isoamylenes dehydrogenation to isoprene in the presence of iron oxide self-regenerating catalysts.

EFFECT: improved preparing method.

1 tbl, 6 ex

FIELD: chemistry of aromatic compounds, chemical technology.

SUBSTANCE: process involves the following stages: feeding (C2-C5)-alkane, for example, ethane and (C2-C5)-alkyl-substituted aromatic compound, for example, ethylbenzene into dehydrogenation reactor for the simultaneous dehydrogenation to (C2-C5)-alkene, for example, to ethylene, and (C2-C5)-alkenyl-substituted aromatic compound, for example, styrene; separation of the outlet dehydrogenation flow for extraction of gaseous flow containing alkene, hydrogen and alkane, and for extraction of aromatic compounds with the high effectiveness by cooling and compression; feeding a gaseous flow and (C6-C12)-aromatic compound into the alkylation reactor for preparing the corresponding (C2-C5)-alkyl-substituted aromatic compound that is recirculated into the dehydrogenation reactor; feeding the blowing flow from the alkylation unit containing alkane and hydrogen for the separation stage by using cryogenic separator for extraction of alkane that is recirculated into the dehydrogenation reactor, and hydrogen that is extracted with the purity value 99%. Invention provides the development of economic and highly effective process for preparing alkenyl-substituted aromatic compounds.

EFFECT: improved preparing method.

61 cl, 2 tbl, 2 dwg, 2 ex

FIELD: petroleum chemistry, organic chemistry, chemical technology.

SUBSTANCE: method involves contacting the parent raw flow in the flow-type reactor with oxygen-free gas flow at increased temperature with a catalyst comprising a precious metal of VII group of the periodic system of elements. The industrial isomerization platinum-containing catalyst SI-1 or industrial hydrogenation catalyst "palladium on active aluminum oxide in sulfured form" is used as a catalyst. Contact of the parent raw with catalyst is carried out by its feeding in inert gas flow, for example, nitrogen at the volume rate 1-2 h-1 at temperature 320-370°C in the presence of the additive representing a solution of hydroquinone or p-benzoquinone in isopropyl alcohol and taken in the concentration 0.01-0.5 mole/l wherein the additive is fed to the parent raw flow in the amount 5-30 vol.%. Invention provides carrying out the highly selective isomerization and cyclization of light petroleum fractions in on industrial Pt- and/or Pd-containing catalysts with the high yield of the end products no containing aromatic compounds and not requiring the presence of hydrogen or hydrogen-containing gas for its realization and regeneration of the catalyst.

EFFECT: improved method for isomerization.

4 cl, 2 tbl, 2 ex

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention provides catalytic composition for dehydration of alkylaromatic hydrocarbons optionally combined with ethane comprising: carrier consisting of alumina in δ phase or in θ phase, or in mixed δ+θ or θ+α, or δ+θ+α phase, modified with silicon oxide and having surface area less than 150 m2/g as measured by BET method; 0.1-35% gallium in the form of Ca2O3; 0.01-5% manganese in the form of Mn2O3; 0-100 ppm platinum; and 0.05-4% alkali or alkali-earth metal oxide, all percentages being based on the total weight of composition. Other variants of composition are also covered by invention. Methods of preparing such catalytic composition (options) envisage use of alumina-based carrier in the form of particles corresponding to group A of the Geldart Classification. Process of dehydration of alkylaromatic hydrocarbons optionally combined with ethane comprises: (i) dehydration of hydrocarbon stream optionally mixed with inert gas in fluidized-bed reactor in presence of catalytic composition consisted of alumina-supported and silica-modified gallium and manganese at temperature within a range of 400 to 700°C, total pressure within a range of 0.1 to 3 atmospheres, and gas hourly space velocity from 50 to 10000 h-1; and (ii) regeneration and heating of catalyst caused by catalytic oxidation of fuel in fluidized-bed reactor at temperature above 400°C.

EFFECT: increased activity of catalytic composition and prolonged lifetime thereof.

22 cl, 2 tbl, 16 ex

FIELD: organic chemistry, chemical technology, catalysts.

SUBSTANCE: invention describes a catalyst for dehydrogenation of (C2-C5)-hydrocarbons that comprises aluminum, chrome oxides, compound of modifying metal, alkaline and/or alkaline-earth metal. Catalyst comprises additionally silicon and/or boron compounds and as a modifying agent the proposed catalyst comprises at least one compound chosen from the following group: zirconium, titanium, iron, gallium, cobalt, molybdenum, manganese, tin. The catalyst is formed in the process of thermal treatment of aluminum compound of the formula Al2O3. n H2O wherein n = 0.3-1.5 and in common with compounds of abovementioned elements and shows the following composition, wt.-% (as measure for oxide): chrome oxide as measured for Cr2O3, 12-23; compound of a modifying metal from the group: Zr, Ti, Ga, Co, Sn, Mo and Mn, 0.1-1.5; silicon and/or boron compound, 0.1-10.0; alkaline and/or alkaline-earth metal compound, 0.5-3.5, and aluminum oxide, the balance. Catalyst shows the specific surface value 50-150 m2/g, the pore volume value 0.15-0.4 cm3/g and particles size 40-200 mcm. Also, invention describes a method for preparing this catalyst. Invention provides preparing the catalyst showing the enhanced strength and catalytic activity.

EFFECT: improved and valuable properties of catalyst.

12 cl, 2 tbl

FIELD: petrochemical industry; methods of production of styrene.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of production of styrene. The invention provides for dehydrogenation of the ethylbenzene charge gained after mixing of the fresh ethylbenzene with the recycled ethylbenzene on the ferrioxide catalytic agent at presence of the steam at the mass ratio of the raw to the steam of no less than 1:2, at the temperature of 580-640°С and the volumetric speed of feeding of the ethylbenzene charge of 0.23-0.45 m3/h. The hydrocarbon condensate (the product of the dehydrogenation) containing styrene, the unreacted ethylbenzene, the by-products including the phenyl acetylene impurity before the stage of the rectification is hydrogenated using the palladium-containing catalytic agents at the temperature of 20-30°С, the volumetric speed of 4.5-5.0 m3/h-1 and at the volumetric ratio of the hydrogen : raw - 35-45. The technical result of the invention is the increased purity of the produced styrene without reduction of productivity of the whole process of the marketable styrene.

EFFECT: the invention ensures the increased purity of the produced styrene without reduction of productivity of the whole process of the marketable styrene.

1 tbl, 8 ex

Up!