The method of obtaining isobutylbenzene and 4 methylpentene-1
(57) Abstract:Usage: for the synthesis of the medicinal product ibuprofen and as a monomer for the heat-resistant polymer of templene and copolymers with linear polyethylene. The inventive products isobutylbenzene. BF C10H14, 4-methylpentene-1. BF C6H12. Reagent 1: toluene. Reagent 2: propylene, catalyst: sodium on potash. Conditions: 140-170°C, 9-10 MPA. The process involves the drying of toluene, after drying the toluene is divided into two streams: 50-70 wt.%, the dried toluene serves to interact with propylene. The remaining toluene is passed at 50-100°C and a space velocity of 0.5-1 h-1through the catalyst after carrying out stage of the interaction with subsequent distillation and recycling the stage of drying the toluene. The catalyst after passing toluene regenerate hydrogen. 1 Il., table 1. The invention relates to petrochemistry, in particular to a method for isobutylbenzene (IBD) and 4-methylpentene-1 (4-MP-1).IBD is used for the synthesis of drug - ibuprofen (2-(4-isobutylphenyl) propionic acid), which has anti-inflammatory and analgesic action, and 4-MP-1 is the source Monomoscoy density).A method of obtaining IBD interaction of chloride with benzene chloride propylene in the presence of metallic sodium, suspended in toluene . The disadvantage of this method is the formation of significant amounts of by-products and sludge.Closest to the invention to the technical essence and the achieved results is a method for IBD interaction of dried toluene and propylene in the presence of catalyst sodium on the potash" . In parallel with IBD in the specified method is obtained 4-MP-1.Due to the lack of data in the description of this method were performed control experiments to evaluate the performance of the catalyst, the duration of its stable operation and quality of IBD. The results of the control experiments presented in the table.The disadvantages of the described method include small period of stable operation of the catalyst, the relatively low productivity of the catalyst and lower the quality of IBD.The aim of the invention is to increase productivity by improving the performance of the catalyst, increasing the period of stable operation of the catalyst and ponovo toluene is passed through the catalyst before regeneration at elevated temperatures. Passed through the catalyst toluene is subjected to distillation and direct to the stage of drying. Then the catalyst is regenerated with hydrogen by a known method (3).Distinctive features of the method is that the toluene after drying is divided into two streams, 50-75% of dried toluene serves on the stage of interaction with propylene, the remainder of the dried toluene miss 50-100aboutWith a bulk velocity of 0.5-1 h-1through the catalyst after carrying out stage of the interaction with subsequent distillation and recycling the stage of drying the toluene and the catalyst after passing the toluene is subjected to regeneration with hydrogen.The drawing shows a schematic diagram of receipt of IBD and 4-MP-1 according to the invention.Fresh and return toluene on lines 11 and 15, respectively, are mixed and fed to the column azeotropic dehydration 1. Water Argonauts top of the column 1 in the form of an azeotropic mixture with toluene and removed from the system through line 29 through the phase shifter 2. The dried toluene (stream 26) extending from the cube column 1, is divided into two parts. One part (50-75 wt. %) in line 27 is mixed with a mixture of fresh (stream 12) and recycle (stream 14) propylene (line 28) and the SIP layer of catalyst sodium on the potash (sodium 2.0 to 2.5 wt. %). The fusion reaction IBD and 4-MP-1 is carried out at a temperature of 140-170aboutC, a pressure of 9-10 MPa, flow rate of 1-2 h-1. The mixture of reaction products after the reactor of unit 3, 4 (or 5, 6) (stream 16) is fed to the rectification unit, where sequentially allocated in the form of distillate: recycle propylene (stream 14) - column 7; commodity 4-MP-1 (stream 20) - column 8; recycle toluene (stream 15) - column 9; commodity IBD (stream 23) is on the column 10. CBM product column 10 (stream 24) is a heavy residue and sent for incineration.The second part of the toluene (25-50% of stream 27) in line 13 is passed to the block reactors 5, 6 (or 3, 4), disabled for catalyst regeneration. This stream of toluene is passed through the regenerated catalyst with a given volumetric rate at a certain temperature. The toluene, leaving the reactors 5, 6 ( or 3, 4), in line 17 is directed in column 9, where it is separated from the heavy impurities in the form of distillate in line 15 recycle on stage azeotropic dehydration. Impurities of heavy products contained in the stream of toluene and 17 remain in the distillation residues columns 9 and 10 and are displayed with a heavy residue (stream 24). After passing toluene catalyst in reactors 5, 6 (or 3, 4) regenerated moderadores conducted at the facility in accordance with the scheme shown in the drawing, only without feed and output of toluene in the reactor block on lines 13 and 17.In reactor 3, 4, 5, and 6 loaded stationary layer of catalyst sodium to potassium in the form of tablets. The volume of catalyst in each apparatus is 20 litersThe reactors operate cyclically in pairs.In order to avoid cluttering the data unnecessary for illustration of the invention, all of the examples are indicators of one pair of reactors (3 and 4).In reactors 3 and 4 on line 27 serves 15 kg/h of dried toluene, 28-8 kg/h of a mixture of fresh and recycled polypropylene. From the mixture of reaction products in the block of distillation columns 7, 8, 9 and 10 produce 4-MP-1 and IBD. The reactor switch on regeneration after reducing the catalyst activity below 50% of the original. Fresh catalyst to the first regeneration works 100 hoursThe catalyst recovered in a stream of hydrogen with a flow rate 0,018 kg/h supplied through line 25 at 200aboutWith over 20 hours of Regeneration gases via line 18.The second and third mezhregionalnye runs approximately 100 hours After the first regeneration, the catalyst activity is restored to 70% of the initial and after the second 50%. Pveh, are given in the table.P R I m e R s 2 - 6. The process is carried out analogously to example 1, only include threads 13 and 17 of the feed and output of toluene in the reactor block before regeneration with hydrogen. In the process, before each regeneration cycle range of flow conditions toluene.Analogously to example 1 a catalyst to the first regeneration works 100 hours Only in connection with the application of the proposed method the activity of the catalyst after regeneration is restored to 80-90%. Therefore, the overload of the catalyst is carried out through a larger number of regeneration cycles.The indicators characterizing the process runs according to example 2-6 shown in the table.Thus, the application of this method can improve the performance of the catalyst at 12-30%, the duration of the stable of his work in 2-3 times and improve the quality of IBD by reducing levels of education are difficult to separate hydrocarbons, wikipaedia near IBD. The METHOD of OBTAINING ISOBUTYLBENZENE AND 4 METHYLPENTENE-1 by reacting toluene and propylene at 140 - 170oC and a pressure of 9 to 10 MPa in the presence of a catalyst containing sodium on the potash, including the dewatering of toluene, characterized in that the goal is esta isobutylbenzene, after drying the toluene is divided into two streams, 50 to 75 wt. % of dried toluene serves on the stage of interaction with propylene, the remainder of the dried toluene pass at 50 - 100oC and a space velocity of 0.5 - 1 h-1through the catalyst after carrying out stage of the interaction with subsequent distillation and recycling the stage of drying the toluene and the catalyst after passing the toluene is subjected to regeneration with hydrogen.
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.
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
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
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.
SUBSTANCE: invention describes zeolite-containing catalyst for transformation of aliphatic hydrocarbons C2-C12 to a mix of aromatic hydrocarbons or high-octane gasoline component containing zeolite ZSM-5 with silicate module SiO2/Al2O3=60-80 mol/mol and 0.02-0.05 wt % of residual sodium oxide content, zeolite structural element, promoter and binding component, with zirconium or zirconium and nickel oxides as zeolite structural component, and zinc oxide as promoter, at the following component ratio (wt %): zeolite 65.00-80.00; ZrO2 1.59-4.00; NiO 0-1.00; ZnO 0-5.00; Na2O 0.02-0.05, the rest being binding component. Also, a method for obtaining zeolite-containing catalyst is described, which involves mixing reagents, hydrothermal synthesis, flushing, drying and calcinations of sediment. The reaction mix of water solutions of aluminum, zirconium and nickel salts, sodium hydroxide, silicagel and/or aqueous silicate acid, inoculating zeolite crystals with ZSM-5 structure in Na or H-form, and structure-former, such as n-butanol, is placed in an autoclave, where hydrothermal synthesis is performed at 160-190°C for 10-20 hours with continuous stirring; the hydrothermal synthesis over, Na-form pulp of the zeolite is filtered; the obtained sediment is flushed with domestic water and transferred to salt ion exchange by processing by water ammonium chloride solution with heating and stirring of the pulp; the pulp obtained from salt ion exchange is filtered and flushed with demineralised water with residual sodium oxide content of 0.02-0.05 wt % on the basis of dried and calcinated product; flushed sediment of ammonium zeolite form proceeds to zinc promoter introduction and preparation of catalyst mass by mixing of ammonium zeolite form modified by zinc and active aluminum hydroxide; obtained catalyst mass is extruded and granulated; the granules are dried at 100-110°C and calcinated at 550-650°C; calcinated granules of zeolite-containing catalyst are sorted, ready fraction of zeolite-containing catalyst is separated, while the granule fraction under 2.5 mm is milled into homogenous powder and returned to the stage of catalyst mass preparation. The invention also describes method of transformation of aliphatic hydrocarbons to high-octane gasoline component or a mix of aromatic hydrocarbons (variants), involving heating and passing raw material (gasoline oil fraction direct sublimation vapours or gas mix of saturated C2-C4 hydrocarbons) through stationary layer of the aforesaid catalyst.
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
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.
EFFECT: more pure alkylbenzol with smaller amount of undesirable by-products and using smaller number of stages.
6 cl, 5 tbl, 1 dwg
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.
EFFECT: increasing of the processing of the efficiency of unstable hydrocarbon gas condensate with enhanced obtaining of target products, to make the process more environmentally safe, to increase the quantity and quality of the obtained fresh water.
2 cl, 5 ex, 1 dwg
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.
EFFECT: enhancing of the catalyst selectivity in transforming of lower alkanes to aromatic hydrocarbons.
30 cl, 3 dwg, 4 tbl, 2 ex
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
SUBSTANCE: invention relates to a method of aromatising alkanes and involves bringing alkanes, which contain from one to four carbon atoms, into contact with a Pt/ZSM-5 catalyst which is deposited on MFI zeolite, the lattice of which consists of aluminium, silicon and oxygen. Use of the given catalyst during aromatisation of alkanes prevents formation of methane and increases BTX selectivity.
EFFECT: higher content of ethane than methane in the light gas fraction enables use of exhaust gas as raw material for cracking apparatus.
15 cl, 2 tbl, 5 ex