The method of purification of benzene and toluene from impurities nah

 

(57) Abstract:

The invention relates to the petrochemical industry and can be used to clean gasoline and toluene. Describes a method of purification of benzene and toluene from impurities of non-aromatic hydrocarbons by distillation of aromatic extract using osetroobraznykh solvents. At the same time as azeotroping solvent used oxygen-containing antiknock additive to gasoline, representing a simple ether selected from the group consisting of methyl tert-butyl ether, epic-tert-butyl ether, methyl tert-amyl ether, diisopropyl ether, or alcohol, selected from the group consisting of ethanol, 2-propanol, tert-butanol, or a mixture of these alcohols or methanol with ether, taken in a mass ratio of 8 and 28 : 1 for the non-aromatic hydrocarbons from the extract, and warded off the azeotropic mixture is sent to the gasoline without regeneration of the solvent. The technical result - the exception of recycling, reducing energy consumption and improving the quality of benzene and toluene. table 1.

The invention relates to the refining industry and can be used to improve the quality of benzene and">

At industrial installations extraction of aromatic hydrocarbons purification of the extract from the impurities of non-aromatic hydrocarbons is carried out by the method of simple rectification in prednisolnoe column. Up to 20% of the extract Argonauts and returned to the extraction column. Thus, the most difficult impurities to the arenas not are removed from the system, and recycle, worsening the results of the extraction process. Another disadvantage of the simple rectification is that impurities do not form azeotrope with benzene, remain in the extract, reducing the quality of the benzene and toluene.

To avoid recycling, reduce energy costs and improve the quality of benzene and toluene offered to clean them instead of the simple rectification to use azeotropic rectification.

Known methods for removal of benzene and toluene from impurities nah azeotropic distillation with dimethoxymethane and methanol (U.S. Pat. USA 5405505, 1995), a mixture of methanol and acetone (U.S. Pat. Czechoslovakia 135677, 1970), acetone (U.S. Pat. France 1510250, 1967).

Closest to the proposed invention is a method of separation of benzene from mixtures of paraffinic and naphthenic hydrocarbons by a combination of extraction with polar> The main disadvantage of the known methods for removal of benzene and toluene from impurities, the necessity of regeneration osetroobraznykh components of the azeotropic mixtures. In particular acetone forms a homogeneous azeotrope with impurities, of which it must be extragonadal water followed by distillation separation from aqueous solutions. The need for regeneration of the selective solvents leads to considerable complication of the technological scheme and to increase specific power consumption when cleaning aromatic hydrocarbons.

As osetroobraznykh components in the present invention it is suggested to use high-octane oxygenated gasoline additive is a mixture of ethers [tert-butyl (MTBE), ethyl tert-butyl (ETBE), tert-amylotrophic (tame), diisopropyl (DIPE)], alcohols (methanol, ethanol, 2-propanol, tert-butanol) or individual high-octane additives.

The table presents the results of simple distillation of aromatic extract, azeotropic distillation (AR) with high-octane oxygen-containing solvents of the proposed method and to compare azeotropic distillation with acetone (prototype).

Compared with a simple rectification of the advantages of the proposed method is more selective removal of non-aromatic hydrocarbons with prednisolnoe fraction, resulting in a loss of the extract reduced with 23,59 wt.% 3-5 wt.%, i.e. 4.7 - 8 times, while improving the quality of allotted aromatic hydrocarbons.

Example 1 (simple distillation)

In the reboiler of a distillation column efficiency 15 theoretical plates download 85,565 g of an extract isolated from catalyzate reforming faction 62-105oC, composition, wt.%: nonaromatic hydrocarbons - 0,38, benzene - 50,43, toluene - 44,05, arena C8+- 5,14. When reflux 12 and the temperature of the vapor in the upper column section 55-79,5oC select 20,18 g prednisolnoe fraction, at a temperature of vapors of 79.5-80,5oC -23,265 g of benzene fraction, at a temperature 109-111oC - 37,631 g toluene fraction. In the reboiler of the column remains 4,489 g VAT residue. The composition of the distilled fractions and the cubic residue is analyzed by the method of gasai is S="ptx2">

In the boiler the same distillation column load 130,18 g of extract (the same composition as in example 1) and of 3.9 g of a mixture of MTBE + tert-butanol, composition 70: 30 wt.% respectively. When reflux 12 and the temperature of the vapor in the upper section of the column 52-79,5oC select 8,61 g azeotropic mixture of high-octane solvent and prednisolnoe faction, including solvents of 45.3 wt.% and hydrocarbon - 54,7 wt.%; when the temperature of the vapor of 79.5-80,5oC distilled to 61.4 g of benzene fraction; at a temperature 109-111oC distilled 57,24 g toluene fraction. In the reboiler of the column remains 6,825 g VAT residue, consisting mainly of a mixture of arenes C8+. Output fractions in wt.% raw materials and their composition is given in the table.

Azeotropic mixture of solvent and prednisolnoe fraction is sent to gasoline to increase its octane number without regeneration of MTBE and tert-butanol.

Example 3.

In the boiler the same distillation column load 64,35 g of extract (the same composition as in example 1), and 4,39 g of tert-butanol. When reflux 12 and the temperature of the vapor 71-79,5oC select 11,16 g azeotropic mixture of tert-butanol (4,39 g) and prednisolnoe fraction (6,77 g). When the temperature of the steam is tion. In the reboiler of the column remains 3,367 g VAT residue (arena C8+). Output fractions in wt.% raw materials and their composition is given in the table.

Azeotropic mixture of tert-butanol and prednisolnoe fraction is sent to gasoline to increase its octane number without regeneration tert-butanol.

The method of purification of benzene and toluene from impurities of non-aromatic hydrocarbons by distillation of aromatic extract using osetroobraznykh solvents, characterized in that as azeotroping solvent used oxygen-containing antiknock additive to gasoline, representing a simple ether selected from the group consisting of methyl tert-butyl ether, ethyl tert-butyl ether, methyl tert-amyl ether, diisopropyl ether, or alcohol, selected from the group consisting of ethanol, 2-propanol, tert-butanol, or a mixture of these alcohols or methanol with esters, taken in a mass ratio of 8 and 28 : 1 for the non-aromatic hydrocarbons from the extract, and warded off the azeotropic mixture is sent to the gasoline without regeneration of the solvent.

 

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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: organic synthesis catalysts.

SUBSTANCE: invention relates to catalyst for aromatization of alkanes, to a method of preparation thereof, and to aromatization of alkanes having from two to six carbon atoms in the molecule. Hydrocarbon aromatization method consists in that (a) C2-C6-alkane is brought into contact with at least one catalyst containing platinum supported by aluminum/silicon/germanium zeolite; and (b) aromatization product is isolated. Synthesis of above catalyst comprises following steps: (a) providing aluminum/silicon/germanium zeolite; (b) depositing platinum onto zeolite; (c) calcining zeolite. Hydrocarbon aromatization catalyst contains microporous aluminum/silicon/germanium zeolite and platinum deposited thereon. Invention further describes a method for preliminary treatment of hydrocarbon aromatization catalyst comprising following steps: (a) providing aluminum/silicon/germanium zeolite whereon platinum is deposited; (b) treating zeolite with hydrogen; (c) treating zeolite with sulfur compound; and (d) retreating zeolite with hydrogen.

EFFECT: increased and stabilized catalyst activity.

26 cl, 1 dwg, 5 tbl, 4 cl

FIELD: CHEMISTRY.

SUBSTANCE: zeolite catalyst for process of conversion of straight-run gasoline to high-octane number component is described. The said catalyst contains high-silica zeolite with SiO2/Al2O3=60 and residual content of Na2О of 0.02 wt.% maximum, metal-modified, Pt, Ni, Zn or Fe metals being in nanopowder form. Content of the said metals in the catalyst is 1.5 wt.% maximum. Method to manufacture zeolite catalyst for conversion of straight-run gasoline to high-octane number component is described. The said method implies metal modification of zeolite, Pt, Ni, Zn or Fe metals being added to zeolite as nanopowders, produced by electric explosion of metal wire in argon, by dry pebble mixing in air at room temperature. Method to convert straight-run gasoline using the said catalyst is also described.

EFFECT: increase in catalyst activity and gasoline octane number, accompanied by increase in yield.

4 cl, 3 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: method involves hydrocarbon transformation in a reactor in the presence of modified catalyst containing, mass %: 53.0-60.0 of ZSM-5 high-silica zeolite with the ratio of SiO2/Al2O3=39, 34.0-38.0 of Al2O3, 2.0-5.0 of B2O3, 1.0-5.0 of Zn, 0.0-5.0 of W, 0.0-3.0 of La, 0.0-3.0 of Ti at 300÷700°C, including separation of liquid and solid transformation products, followed by burning oxidation of gaseous products and addition of the obtained mix of carbon dioxide and water vapour to the source hydrocarbons at the rate of 2.0÷20.0 mass %. Before the raw material intake the reaction system is flushed by an inert gas (nitrogen), starting from 300°C and to the transformation temperature. Hydrocarbons used are alkanes, olefins or alkane olefin mixes C2-C15 without preliminary separation into fractions. Gaseous transformation products undergo burning and complete oxidation in the presence of an oxidation catalyst of vanadium/molybdenum contact piece, V2O5/MoO3. To sustain continuous process two identical reactors are used, where the catalyst is transformed and recovered in turns.

EFFECT: longer working transformation cycle due to the continuous process scheme; higher yearly output of aromatic hydrocarbons; reduced energy capacity and improved ecology of the process.

2 ex

FIELD: chemistry.

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EFFECT: reduced number of components and synthesis stages of zeolite-containing catalyst; increased transformation degree of raw material; improved quality and yield of target products with the said catalyst.

4 cl, 8 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: alkylbenzol with structure R1R2CH(Ph) is obtained from alkylphenyl alcohol with structure R1R2C(Ph)OH. Method includes following stages: (a) supply of initial flow, containing alkylphenyl alcohol with structure R1R2C(Ph)OH, into reactor with catalytic distillation zone; (b) simultaneously in reactor: (i) contacting of initial flow, containing R1R2C(Ph)OH, with hydrogen in catalytic distillation zone in order to convert R1R2C(Ph)OH into R1R2CH(Ph) and to form reaction mixture and (ii) separation of R1R2CH(Ph) from reaction mixture by fraction distillation in order to obtain higher than catalytic distillation zone, flow, which contains R1R2CH(Ph) with lower concentration of R1R2C(Ph)OH in comparison to initial reactor flow in position higher than catalytic reaction zone; R1 and R2 each represent hydrogen or hydrocarbon group with 1-10 carbon atoms and one of R1 and R2 is not hydrogen.

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6 cl, 5 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention refers to the method for preparation of aromatic hydrocarbons accompanied with simultaneous obtaining of hydrogen, methanol, motor oils and fresh water from the unstable hydrocarbon gas condensate obtained from gas condensate and oil fields including if necessary its desulphurisation, following obtaining of synthesis gas by one-stage oxidising with air oxygen, its conversion to methanol, following catalytic conversion of methanol to motor oils, separation of the water formed on all process stages, evaporation of the hydrocarbons residues including methanol and fatty hydrocarbons from the water (united and formed on all process stages), water bioremediation and mineralisation. The initial hydrocarbon gas is unstable hydrocarbon gas condensate without preliminary separation of methane and ethane from propane and butane, the said initial gas before its conversion to synthesis gas undergoes the catalytic aromatisation during heating. Then the obtained aromatic hydrocarbon and hydrogen are separated, hydrogen is at least partially used for synthesis gas obtaining in order to change the ratio H2:CO 1.8-2.3:1), and if necessary it is partially used on the stage of desulphurisation with synthesis gas obtaining from hydrocarbon gases (unreacted and formed on the aromatisation stage). The invention refers also to the device for implementation of the method described above.

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2 cl, 5 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: method of hydrocarbon aromatisation includes: a) contacting of alkane containing from 2 to 6 carbon atom in molecule with at least one catalyst consisting virtually of platinum applied to zeolite MFI which lattice consists virtually from gallium, silicon and oxygen and b) separation of aromatic products. The preparation method for platinum-gallium zeolite catalyst used for hydrocarbon aromatisation is described, it includes: preparation of gallium zeolite containing silicon and gallium; precipitation of the platinum to said zeolite; and c) zeolite calcination. In the said method the said gallium zeolite catalyst consists virtually of platinum applied to zeolite MFI which lattice consists virtually from gallium, silicon and oxygen. The platinum- gallium zeolite catalyst for hydrocarbon aromatisation containing: a) gallium-silicon zeolite and b) platinum precipitated to gallium-silicon zeolite is also described. In the said method the said platinum-gallium zeolite catalyst consists virtually of platinum applied to zeolite MFI which lattice consists virtually from gallium, silicon and oxygen.

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30 cl, 3 dwg, 4 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing aromatic hyhrocarbons and lower olefins, involving catalytic dehydrocyclisation of hydrocarbon material in the presence of a zinc-containing zeolite catalyst, at high temperature and pressure, separation of dehydrocyclisation products into product A - aromatic hydrocarbons C6+, and product B - mixture of non-aromatic hydrocarbons with hydrogen, subsequent hydrodealkylation of product A, obtaining commercial-grade benzol, and pyrolysis of product B, obtaining lower olefins, and characterised by that, the dehydrocyclisation material used is C2-C6 paraffins, the process is carried out at 0.9-1.3 MPa pressure, after separating the C10+ fraction, product A is subjected to hydrodealkylation, commercial-grade benzol, methane and ethane fractions, ethane fraction and product B are separated from hydrodealkylation products, or after separating over 50 vol % methane-hydrogen fraction from product B, product B is taken for pyrolysis, commercial-grade ethylene and propylene are separated from gaseous products of pyrolysis, liquid products of pyrolysis - pyrolysis condensate, containing aromatic hydrocarbons, is subjected to catalytic hydrogenation and hydrodesulphurisation, and subsequent hydrodealkylation, obtaining commercial-grade benzol, methane and ethane fractions, the latter is returned for pyrolysis.

EFFECT: increased output of lower olefins, significant improvement of economic parametres of the process due to increase of inter-regeneration period of dehydrocyclisation catalyst.

1 cl, 5 ex, 5 tbl

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