The method of obtaining the fraction of aromatic hydrocarbons, c6-c9
(57) Abstract:Use: petrochemical and chemical industry. The inventive fraction of aromatic hydrocarbons, C6-C9. Raw materials: 1 - phenolic resin (FS) - waste production of phenol and acetone. 2-isopropylbenzene (cumene) or recirculate process of production of phenol and acetone. The catalyst composition, wt.%: (1-) Pd 0,75, crystalline miniserial 5, -Al2O3100, (2) NiO 5; MoO315; crystalline miniserial 10; -Al2O3to 100, (3) the zeolite ZSM-8 - 45; ZnO - 1,0, -Al2O3to 100, (4) Pt 45; Sn - 0,25; F - 0,25; zeolite ZSM-8 or ZSM - 23 and 5-Al2O3up to 100. Conditions: the process are sequential contacting of the feedstock with 4 of these catalysts in the two reactors. The mass ratio of catalyst 1:2 1:9 and 3:4 1: 9, 300 - 380°C, 2.0 To 4.0 MPa, the volumetric feed rate of 1.5-2.5 h-1the volumetric ratio FS:IPA or recirculate 1:1 hydrogen: feedstock (900 - 1600): 1. 1 C.p. f-crystals, 1 table. The invention relates to organic catalytic chemistry, in particular to the processing of hydrocarbon resins, namely phenolic resin in the fraction of aromatic hydrocarbons containing mainly benzene and isopropylbenzene (cumene), and m the FL fraction of aromatic hydrocarbons from acetophenones fraction of phenolic resin at 360-380aboutC, space velocity of the raw material 1 h-1, a pressure of 3.5 MPa, the ratio of N2raw materials (800-1000) 1 in the presence of aluminoborosilicate catalyst. The resulting hydrogenation product of the fraction of aromatic hydrocarbons containing monocyclic aromatic hydrocarbons WITH6-C9wt. 55,2, including benzene and 0.7, toluene 2; and-propylbenzoyl 0,2, -methylsterol 1,1, phenol 15,5, acetophenone 5,9, ethylbenzene 23,4, isopropylbenzene 27,8.The disadvantage of method (1) is low activity, stability and selectivity of the catalyst in hydroperiod phenolic resin and the degree of conversion in benzene and cumene.The closest in technical essence and the achieved effect is the method (2), including the hydrogenation of phenolic resin in the presence of hydrogen and aluminoborosilicate (AKM) of the catalyst composition, wt. Soo 4; NoO312, 0mm; -Al2O3else if T 350aboutC, Vc 1-1,2 h-1; P 4,9 MPa; filed hydrogen 1000 m3/m3of raw materials.The original phenolic resin composition, acetone 0,15; water 10,1 O. m 0,35; IPA 30,40; alpha methylsterol 2,18; phenol 11,93; acetophenone 18,03; DMPC 0,80; dimer of alpha-methylstyrene 9,49, complex phenol resin 14,55 becomes 80% phenol, cclu aromatic hydrocarbon composition WITH6-C9(benzene, isopropylbenzene), there remains much resin, phenol and other hydrocarbon impurities, low stability and high coking ability of the used catalyst, mainegenealogy period is 250,0 PMThe resulting hydrogenation product has a black color (CNT more than 8 units). The method does not provide complete hydrogenation of alpha-methylstyrene and acetophenone; the temperature of the end of the boiling section of hydrogenated feed compared to the raw material phenol resin + IPA remains practically unchanged.The aim of the invention is to obtain the fraction of aromatic hydrocarbons WITH6-C9with a predominant content of benzene and cumene.This goal is achieved by the fact that as a starting raw material, a mixture of phenolic resin and IPA in a volume ratio of 1 to 1, which is subjected to hydrobromide in two sequential adiabatic reactors, the first of which layers are loaded during the feed catalysts (I) and (II) at a mass ratio of 1 to 9; the catalyst (I) has a composition, by weight. Pd 0,76; crystalline miniserial 5; -Al2O3else, the catalyst (II) has a composition, by weight. Ni 0,5; MoO315; crystalline miniserial (tellago reactor catalysts at a mass ratio of 1 to 9. The catalyst (III) has a composition, by weight. over high-silica zeolite with the module SiO2Al2O340 families pentelow (ZSM-8) 45; ZnO 1,0; -Al2O3else, the catalyst (IV) composition, wt. Pt 0,45; Sn 0,25; 0,25 F; servicecompany zeolite properties of pentelow (ZSM-23, ZSM8) (module SiO2Al2O340) 5; -Al2O3the rest of it.The process of the proposed method in the proposed catalysts is carried out at 300-380aboutC, F 2-4 MPa; Vc 1.5 to 2.5 h-1, the ratio of hydrogen feedstock 900-1600 1, that is convertible composition of the raw material 1 (phenolic resin + isopropylbenzene (cumene) by about. the ratio of 1 1), wt. isopropylbenzene (cumene) 40,84; phenol 2,03; acetophenone (ACP) 2,14; dimer of alpha-methylstyrene (d-M-CT) 11,44; complex phenol 19,27; dimethylphenylcarbinol (DMPC) 0,58; heavy resin 23,39; fractional part;aboutWITH THE TC-90; QC-390;4200,972 g/cm3: iodine number 48,3 J2/100 g or raw material 2 a mixture of phenolic resin and recirculate (risaykl section of hydrogenated feed) at a volume ratio 1 1 composition, wt. benzene 20,02; ethylbenzene 0,87; IPA 16,15; phenol 0,34; -M-ST 0,62; ACF 2,01; dimer-M styrene 10,63; compound 19, 22 the phenol before. dimer-m styrene 1,31; DMPC 0,42, heavy hydrocarbons (tar) 28,41 get catalysate with the release of 100 wt. costulae of 0.03 to 4.0 from raw materials N 2 catalysate composition, wt. benzene 59,8-6; ethylbenzene 4-4,1; toluene 0,2-0,4; IPA 26-31; phenol 1.0 to 1.5; -m-styrene 0,4-0,5; complex phenol of 0.2-0.3; heavy leave the rest of the paraffin, naphthenic.To date the literature has not described how to obtain a fraction of aromatic hydrocarbons from phenolic resin using catalysts of the specified structure, therefore it can be argued that the claimed combination of features of an object is new and, therefore, the corresponding solution has criterial feature of the "novelty."On the other hand, the distinctive features of the proposed technical solutions (way) from the famous are.The application of new catalysts (I), (II), (III), (IV).The process of hydrobromide in 2 sequential reactors at different temperatures, thus ensuring that the necessary reactions of transformation of uglevodorodov of raw materials.Layer-by-layer load reactors catalysts that provides in the first reactor in the upper layer on the catalyst (I) preliminary hydrogenation of resins, unsaturated hydrocarbons, in the lower layer on the catalyst (I) hydrocracking complex phenol, dimers, trimers-m-styrene, alkilirovanija, dealkylation, parallelomania and isomerization of aromatic hydrocarbons, preventing the catalyst (IV) from coking due to the content in the catalyst (III) zeolite Pancasila, which has anticariogenic component, and finally, in the lower layer on the catalyst (IV) of the 2nd reactor reactions proceed exhaustive hydrogenation alkylaromatics and unsaturated hydrocarbons.Made certain ratio of the catalyst in the first reactor (I) (II) as 1 9, in the second reactor (III) (IV) 1 9.At the start of the process as a diluent phenolic resin is used IPA, and then recirculating the hydrogenation product with a volumetric ratio of 1 to 1.On the basis of these signs can be argued that the essence of the proposed facility is not obvious from the well-known in the industry prior art, therefore, it has criterial element of the invention "inventive step".Technologically, the proposed method can be implemented in the chemical and petrochemical industry and allows you to receive waste from the production of phenol and acetone phenol resin fraction of aromatic hydrocarbons containing benzene 43-65 and the third criterion a symptom of the invention "industrial applicability".P R I m e R 1. Phenolic resin mixed with IPA in a volume ratio of 1 to 1, the composition of the raw material 1 (see table), subject to hydrobromide in two sequential reactors with layers loaded catalysts during feed (top to bottom): R-1 CT I composition, wt. Pd 0,75; miniserial 5; -Al2O394,25, CT II composition, wt. NiO 5, MoO315; miniserial 10; -Al2O370 (the ratio of the catalysts 1 to 9), R-2, CT III composition, wt. CRS-zeolite 45; ZnO 1; -Al2O354, CT IV composition, wt. Pt 0,45; Sn 0,25; 0,25 F; CRS-5 zeolite; -Al2O394,05. The process is conducted at P 3 MPa, V 1.5 h-1N2raw 900 1; the temperature in the R-1 300aboutWith that in R-2 350aboutC. the Results of example 1 and for the subsequent in the table.P R I m m e R 2. The process is carried out on raw materials in example 1, the catalyst composition of example 1 at a ratio of 1 to 9; P = 4 MPa; Vc 2.5 h-1; N2raw 1600 1; the temperature in the R-1 320aboutIn R-2 at 380aboutC.P R I m e R 3 (for comparison). The process is carried out on raw materials in example 1, the catalyst of example 1 at a ratio of 2 8 P2,5 MPa; V 1,2 h-1; H2raw 800 1 at a temperature in the region of 1 280aboutWith that in R-2 at 340aboutC.P R I m e R 4 (for comparison). The process is carried out on raw materials in example 1, the temperature value P-1,2 390aboutC. the Catalysts samakovlis, the product is a black, viscous, the process is not.P R I m e R 5. The process is carried out on raw materials in Prime 1, the catalyst composition of example 1, the ratio of 1 9 P = 3.5 MPa, Vc 2 h-1; N2raw materials 1200 1, at a temperature in the R-1 320aboutWith that in R-2 at 350aboutC.P R I m e R 6. The process is performed on the phenol resin in a mixture with a hydrogenation product (risaykl) (raw material 2) with a volumetric ratio of 1: 1 on the catalyst composition of example 1, at P 3 MPa; Vc 1,5; N2raw 900 1, at a temperature in the R-1 320aboutWith that in R-2 at 350aboutC.P R I m e R 7. Spend on raw materials N 2, the catalyst composition of example 1, at mass ratio of 1 9, P = 4 MPa; Vc 2.5 h-1; N2raw 1600 1, at a temperature in the region of 1 300aboutWith that in R-2 at 380aboutC.P R I m e R 8 (for comparison). The process is performed on the raw material 2, the catalyst composition of example 1 at a mass ratio of 1 9, P = 4.5 MPa, Vc 8 h-1; H2raw 2000 1, at a temperature in the region OF 1.2 390aboutC.P R I m e R 9 (for comparison). The process is performed on the raw material 2, the catalyst composition of example 1, at a mass ratio of 2 to 8; P = 2.5 MPa; Vc 1,0 h-1; H2raw 800 1; the temperature in P-1,2 290aboutC.P R I m e R 10 O395,3; (II) NiO 4; MoO313, the magnesium-silicate 7; -Al2O376; (CT III) CRS-zeolite 40; -Al2O360; (IV) Pt 0,4; SVK-zeolite 3; -Al2O396,6 when the parameters in example 6. 1. THE METHOD OF OBTAINING THE FRACTION OF AROMATIC HYDROCARBONS, C6-C9by catalytic hydrogenation of phenolic resins-waste production of phenol and acetone Kukolnik way at elevated temperature and pressure, wherein the phenolic resin is used in a mixture with cumene or recycled from the process of hydrogenation of the obtained hydrogenation product at their volumetric ratio of 1 to 1 and the process of hydrogenation lead by successive contact of the feedstock with four catalysts, having in the course materials the following composition, wt.I. Palladium 0,75
Crystalline magnesium silicate 5
The aluminum oxide To 100
II. Nickel oxide (II) 5
Molybdenum oxide 15
Crystalline magnesium silicate 10
g-alumina To 100
III. High-silica zeolite type ZS M-8 45
Zinc oxide 10
g-alumina To 100
IV. Platinum 0,45
High-silica zeolite type ZS M-8 or ZS M-23 5
g-alumina To 100
taken in the mass is 380oC, pressure of 2.0 to 4.0 MPa, the space velocity of the raw material 1,5 2,5 h-1, the volumetric ratio of hydrogen: feedstock 900 1600 1.
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
FIELD: organic chemistry, medicine, pharmacy.
SUBSTANCE: invention relates to new derivatives of glucopyranosyloxybenzylbenzene represented by the formula (I): wherein R1 represents hydrogen atom or hydroxy(lower)alkyl; R2 represents lower alkyl group, lower alkoxy-group and lower alkylthio-group being each group is substituted optionally with hydroxy- or (lower)alkoxy-group, or to its pharmaceutically acceptable salts. Also, invention relates to pharmaceutical composition eliciting hypoglycemic activity and to a method for treatment and prophylaxis of hyperglycemia-associated diseases, such as diabetes mellitus, obesity and others, and to their intermediate compounds. Invention provides preparing new derivatives of glucopyranosyloxybenzylbenzene that elicit the excellent inhibitory activity with respect to human SGLT2.
EFFECT: valuable medicinal properties of compounds.
13 cl, 2 tbl, 2 ex
FIELD: industrial organic synthesis.
SUBSTANCE: invention relates to production of phenol via acid catalytic decomposition of cumene hydroperoxide followed by isolation of phenol from decomposition products and purification of phenol to remove trace impurities including acetol. Purification of phenol is accomplished through hetero-azeotropic rectification with water. Acetol is isolated as a part of liquid-phase side stream from semiblind plate located within exhausting section of hetero-azeotropic rectification column. Side stream is supplemented by cumene and used to supply stripping column, from which fraction of acetol/cumene azeotropic mixture is taken as distillate and residue is returned under semiblind plate of hetero-azeotropic rectification column to be further exhausted. From the bottom of the latter, crude phenol is withdrawn and passed to final purification from the rest of reactive trace impurities. Acetol/cumene azeotropic mixture is subjected to heat treatment at 310-350°C, which may be performed in mixtures with high-boiling production waste or in mixtures with bottom product of rectification column for thermal degradation of high-boiling synthesis by-products, which bottom product is recycled via tubular furnace. Above-mentioned semiblind plate, from which side stream is tapped, is disposed in column zone, wherein content of water is minimal and below which contact devices are positioned with efficiency at least 7.5 theoretical plates. Side stream with cumene added to it is passed to the vat of stripping column with efficiency at least 15 theoretical plates.
EFFECT: minimized content of acetol in purified phenol and reduced power consumption.
5 cl, 3 dwg, 6 tbl, 4 ex
FIELD: industrial organic synthesis.
SUBSTANCE: invention relates to joint phenol-acetone production via selective decomposition of cumene hydroperoxide. Process is conducted in several in series connected reactors constructed in the form of shell-and-tube heat-exchangers, wherein part of decomposition product is recycled into reaction zone and mixed with feed stream to be decomposed, weight ratio of recycled stream to feed stream being less than 10. Reactors with tubular hydrodynamic characteristic have volumetric heat-exchange surface equal to or larger than 500 m2/m3. Preferably, residual concentration of cumene hydroperoxide is 0.1-0.3 wt % and its residence time in decomposition zone ranges from 0.5 to 10 min.
EFFECT: increased selectivity of decomposition at lesser recycle apparatus volume and reduced investment expenses.
11 cl, 1 dwg, 9 ex