Method of system separation: benzol-perfluorobenzol-tertiary amyl alcohol

FIELD: chemistry.

SUBSTANCE: method includes supply of initial mixture and dimethylsulfoxide (DMSO) as separating agent, taken in ratio 7-7.5:1 to initial mixture, into extraction rectification column (1) efficiency 50 t.t., initial mixture being supplied on 30 t.t., separating agent on 10 t.t. of column (plate numeration from top of column), phlegm number in column constitutes 1.5-2, taking of benzol in distillate and mixture benzol-perfluorobenzol (PFB) - tertiary amyl alcohol (TAA)-DMSO from column (1) cube , supply of mixture PFB-TA-DMSO on 25 t.t. of column of separating agent regeneration (2) with efficiency 50 t.t., phlegm number in column being 1-3, removal separating agent from column cube and its supply to column (1), supply of column (2) distillate, representing aseotropic mixture PFB-TAA, for separation into complex of two columns (3) and (4) with efficiency 35 t.t., with removal from column cubes of TAA and PFB, respectively, aesotropic mixture being supplied on 18 t.t. of column (3), phlegm numbers of columns (3) and (4) being equal 0.5-1.5 and 1-2 respectively, re-cycle of aseotrope PFB-TAA, which is separated in distillate of column (4) into column(3) feeding, ratio of re-cycle of column (4) and feeding of column (3) being (1-1.1):0.66, pressure in columns (1)-(3) is 300 mm of mercury, pressure in column (4) - 760 mm of mercury.

EFFECT: simplification of technology, increase of ecological compatibility of process and quality of obtained products.

1 tbl, 1 dwg, 1 ex


The invention relates to the field of organic synthesis, and particularly to a method of separation bizeurope mixture of benzene-performanta-tertiary amyl alcohol.

Benzene is included in the composition of gasoline, is widely used in industry, is the raw material for the production of drugs, various plastics, synthetic rubber and dyes. Performanta used in laboratory practice for synthesis of polyfluoroaromatic compounds and as a solvent.

There is a method of separating such a mixture of the carboxylic acid fraction With5-C13and butyl esters. [Smokes. Higher fatty alcohols. M.: Chemistry, 1970]

In the process of obtaining higher fatty alcohols With7-C9by catalytic hydrogenation of fatty acids and their esters the first step is the esterification of the acids of the C5-C13. Since the esterification reaction is reversible, despite the continuous removal of water from the reaction mixture, it is not possible to obtain esters without impurity acids (butyl esters contain from 2 to 5% of unreacted acids). Therefore, the crude ester is neutralized with 25%-rastvorom alkali to remove acids, unreacted. From the neutralizer selected three layers: ether containing pure butyl esters, alkaline and intermediate (emulsion). Emulsion layer, which which contains esters and unreacted carboxylic acid, collect in a container, and again sent to the Converter. The alkaline solution of sodium salts of fatty acids (Soaps) are separated from the esters by settling and treated with sulfuric acid. Thus regenerate the free acid, which after washing with water is separated from the sodium sulfate and again return to production. Esters are washed in the neutralizer with water and dried in vacuum. When washing produce large quantities of waste water, so washing is sometimes replaced by distillation.

The disadvantages of this method include the complexity of technology, the formation of large quantities of sewage, polluting the environment, and the need to use corrosion resistant materials, since the process takes place in the presence of sulphuric acid.

Share the mixture described above, and the mixture described in this invention contain binary bizeurope component.

The technical result of the proposed method is to simplify the technology, improving the environmental friendliness of the process and quality of the products.

This technical result is achieved by using for the separation of a three component system with binary bizeurope component method of extractive distillation.

As the source of the selected triple basetsana system: benzene (B)-performanta (PFB)-Tretij the first amyl alcohol (TAS). As a separating agent (RA) selected polar solvent is dimethyl sulfoxide (DMSO), often used in the processes of extraction separation.

The forecast of the possible products of extractive distillation was carried out on the basis of the analysis of changes in the relative volatility in the presence of different amounts of RA in the respective phase diagrams. Using computational experiment was studied phase behavior of a mixture of B-PFB-TAS in the presence of DMSO and its separation by extractive distillation.

The analysis was performed on the phase behavior of the Quaternary system in the sections of the tetrahedron with a constant concentration of DMSO (0.2, 0.4, 0.6 and 0.8 molar fractions). For each section of the received data arrays vapor-liquid equilibrium (AHC) and using the relative shares of the original components in the liquid phase (X1, X2, X3built appropriate charts the progress of a single α-lines. According to the AHC in the triple components built single α-lines on the faces of the tetrahedron. In the end, there was obtained a General picture of the progress α-surfaces in the concentration simplex four-part system, which allowed to evaluate the possibility of separating a mixture of B-PFB-TAS extractive rectification.

In this work, the developed circuit split triple baserape mixture, the cat heaven consists of 4 columns (Technological scheme of the process of extractive distillation). First column - ER (1), in a distant part of which serves original mix B-PFB-TAS equimolar composition in an amount of 1 KMOL/h, and DMSO injected into the upper section of the column. The variation value of the first recycling (number DMSO) provides the necessary selectivity separating agent for the implementation of the extractive effect. The ratio of the quantities RA and initial mixture in column (1) was changed from 1 to 10. In distillate first column select pure benzene, and a cube is a three-component mixture PFB-TAS-DMSO, which goes in the next column regeneration separating agent (2), in the cube which comes out clean separating agent and sent back to the column (1). The distillate of the column (2) is an azeotropic mixture PFB-TAS. It is directed to the separation of the complex of the two columns (3,4), working under different pressures. Cubes columns out of pure components (TAS and PPB respectively), and the distillates - azeotrope PFB-TAS. In the diagram there are two recycling: in the first column ER returns a separating agent (DMSO), in the second azeotrope recycle PFB-TAS, which is highlighted in distillate column (4). The pressure in the columns (1)-(3) - 300 mm Hg, in column (4) is 760 mm Hg separation Process is focused on getting the products (benzene, performante and tertiary amyl alcohol) with a purity of 99.5 mol.%.

Held computer research more than 50 different modes of columns separation schemes. To select the optimal mode varied the following parameters of the pillars: the height (number of theoretical plates), size recyclo, reflux number.

The optimal ratio of the recycle column (4) and supply columns (3) is (1-1,1):0,66, which corresponds to the desired target products TAS and PFB.

The required quality of products is achieved when the following parameters columns: column (1) efficiency 50 TT, the filing of the original mixture for 30 TT separating agent 10 TT (the numbering of the plates from the top of the column), reflux the number of 1.5-2.0; a ratio of the amounts of the separating agent and the initial mixture (7-7,5):1; column (2) efficiency 50 CT, power supply 25 TT, reflux number of 1,0-3,0; columns (3), (4) efficiency 35 CT, power supply 18 TT, reflux ratio equal to 0.5-1.5 and 1.0-2.0, respectively.

Thus, the used method allows to obtain the target products (B, PFB, TAS) given quality - of 99.5%, to simplify the existing technology and improve ekologichnost process due to the absence of sewage.

td align="center" morerows="4"> 100
The material balance of the process of separating a mixture of benzene - performanta - tertiary amyl alcohol in the presence of dimethylsulfoxide.
# example Parameters columns (R - reflux number PA/F0- the ratio of the separating agent and nutrition)The initial mixtureA separating agentProduct streams
Composition, mol.%BPFBTAS
Qty, KMOL/hBPFBTASQty, KMOL/hComposition, mol.%Qty, KMOL/hComposition, mol.%Qty, KMOL/hComposition, mol.%Qty, KMOL/hComposition, mol.%

The method of separating a mixture of benzene-performanta (PFB)-tertiary amyl alcohol (TAS), including the filing of the original mixture and dimethyl sulfoxide (DMSO) as a separating agent, taken in the ratio of 7-7,5:1 to the original mixture to extractive distillation column (1) efficiency 50 TT, and the initial mixture serves 30 TT separating agent 10 TT columns (the numbering of the plates from the top of the column), and reflux the number in the column is 1.5-2, the selection of benzene in distillate and mixtures PFB-TAS-DMSO from the cube columns (1)feeding a mixture PFB-TAS-DMSO at 25 TTH column regeneration separating Agay is that (2) efficiency 50 TT, and reflux the number in the column is 1-3, the output from the cube columns separating agent and filing it in column (1), the filing of distillate columns (2), which is an azeotropic mixture PFB-TAS, separation of the complex of the two columns (3) and (4) efficiency 35 TT with the removal of the cubes columns TAS and PPB, respectively, and the azeotropic mixture is served on 18 TT columns (3)and reflux ratio of columns (3) and (4) 0.5-1.5 and 1-2, respectively, recycling azeotrope PFB-TAS that is distillate column (4) in the power of the column (3), and the ratio of the recycle column (4) and supply columns (3) is (1-1,1):0,66, the pressure in the columns (1)-(3) is 300 mm Hg, and the pressure in column (4) is 760 mm Hg


Same patents:

FIELD: chemistry.

SUBSTANCE: described is the method of obtaining unrefined 1, 3-butadiene with the help of extractive distillation from C4-fractions, which contain C4-acetylenes as the secondary components, with the use of a selective solvent. The method is achieved in a column with dividing partitions, which contains in the bottom part an evaporator, in which lengthwise there is a dividing partition, which forms the first zone, the second zone and the underlying combined zone of the column, connected along the upper flow with the extractive washing column. Supply of energy to the column with the dividing partition through the lower evaporator is regulated such that from the column with the dividing partition draw off the lower stream, which contains the solvent, saturated with C4-acetylenes, in which the portion of 1, 3-butadiene is limited with the estimation that the 1, 3-butadiene lost is economically acceptable. In this case the lower stream is submitted into the decontaminator for acetylenes, from which C4-acetylenes are removed and the purified solvent is removed from it from the lower stream.

EFFECT: increase in the periods of the operation of the device between the cleaning cycles.

11 cl, 1 tbl, 1dwg, 1ex

FIELD: chemistry.

SUBSTANCE: method of separation of starting mixture (A) consisting of two or more constituents, by extractive distillation with the selective solvent (S) within dividing wall column (TKW), is proposed. The separation is performed in the dividing wall column (TKW) having a dividing wall aligned in a longitudinal direction (TW) and extending to an upper end of the column and dividing an interior of the column into first region (1), second region (2), and lower combined column region (3). The starting mixture is fed into first region (1), first top stream (B) is taken off from first region (1), and second top stream (C) is taken off from second region (2), with each of the streams having a prescribed specification. The selective solvent (S) is introduced in an upper part of first region (1) and/or in an upper part of second region (2), and flow of solvent (S1) into the first region (1) and/or flow of solvent (S2) into second region (2) are set so that each of the prescribed specifications for top streams (B, C) are met.

EFFECT: invented method of dividing mixtures is more efficient in terms of energy and solvent consumption.

6 cl, 7 dwg, 1 tbl

FIELD: petrochemical processes.

SUBSTANCE: invention relates to a method for continuously separating C4-fraction by extractive distillation using selective solvent on extractive distillation column, which method is characterized by a separation barrier disposed in extractive distillation column in longitudinal direction extending to the very top of the column to form first zone, second zone, and underlying common zone. Butanes (C4H10)-containing top stream is withdrawn from the first zone, butenes (C4H8)-containing top stream is withdrawn from the second zone, and C4H6 stream containing C4-fraction hydrocarbons, which are more soluble in selective solvent than butanes and butenes, is withdrawn from underlying common zone of column.

EFFECT: reduced power consumption and expenses.

15 cl, 2 dwg, 2 ex

FIELD: petrochemical processes.

SUBSTANCE: hydrocarbon mixture obtained by extractive distillation of C4-fraction using selective solvent, which mixture contains those C4-hydrocarbons, which are better soluble in selective solvent than butanes and butenes, is subjected to continuous separation. Mixture is supplied to first distillation column, wherein it is separated into top stream, containing 1,3-butadiene, propine, and, if necessary, other low-boiling components and, if necessary, water, and bottom stream containing 1,3-butadiene, 1,2-butadiene, acetylenes, and, if necessary, other high-boiling components. Proportion of 1,3-butadiene in bottom stream of the first distillation column is controlled in such a way as to be high enough to dilute acetylenes beyond the range wherein acetylenes can spontaneously decompose. Top stream from the first distillation column is passed to second distillation column, wherein it is separated into top stream, containing propine, and, if necessary, other low-boiling components and, if necessary, water, and bottom stream containing pure 1,3-butadiene.

EFFECT: simplified process and reduced power consumption.

4 cl

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: in particular, invention aims at producing extraction dearomatized component from reformat of gasoline fraction, which component may be used in production of petroleum solvents such as hexane solvents. Process comprising countercurrent extraction of aromatic hydrocarbons with liquid selective extractant to separate dearomatized component (raffinate) and subsequent extractive rectification of resulting extract phase by distilling off aromatic hydrocarbons is characterized by that liquid selective extractant is diethylene glycol or triethylene glycol, countercurrent extraction is carried out at 125-140°C, extractive rectification is carried out using process steam in presence of saturated selective extractant wherein evaporation of water is performed with the aid of energetic steam, unsaturated selective extractant after extractive rectification and recycled gasoline are sent to extraction stage preliminarily using unsaturated selective extractant as heat carrier to generate process steam, and energetic steam condensate is used to heat recycled gasoline to 80-130°C.

EFFECT: enhanced process efficiency.

3 cl, 1 dwg, 1 tbl, 3 ex

FIELD: petroleum processing.

SUBSTANCE: separation of crude C4-fraction comprises rectification of C4-fraction containing butanes, butenes, 1,3-butadiene, and small amounts of other hydrocarbons, including C4-acetylenes, 1,2-butadiene, and C5-hydrocarbons, via extractive distillation using selective solvent. Crude C4-fraction is fed to middle part of first extractive distillation column and selective solvent is added to column above crude C4-fraction introduction point. Vaporous side stream containing C4-acetylenes together with 1,3-butadiene1,2-butadiene, C5-hydrocarbons, and selective solvent, wherein concentration of C4-acetylenes is below self-decomposition threshold, is withdrawn from the first distillation column from the point below crude C4-fraction introduction point. Top stream containing crude C4-fraction components, which are less soluble in selective solvent than C4-acetylenes, are withdrawn from upper part of the first extractive distillation column.

EFFECT: optimized order of process operations.

21 cl, 1 dwg

FIELD: industrial organic synthesis.

SUBSTANCE: crude 1,3-butadiene is recovered from C4-fraction by extractive distillation using selective solvent on column separated by a partition installed along longitudinal direction of the column to form first and second subzones and underlying common column zone. The column is connected to preswitched flush column. Distillation column operation is controlled by energy supply with the aid of lower evaporator and distribution of a series of theoretical plates within underlying common zone to create bottom stream therefrom consisting of purified solvent.

EFFECT: simplified process technology.

23 cl

FIELD: petrochemical processes.

SUBSTANCE: invention provides a process flow rate comprising at least (i) zone of extractive rectification in presence of polar extractant to produce distillate mainly containing butanes and butane(s); (ii) desorption zone wherein desorption of extractant gives stream containing mainly 1,3-butadiene and. as impurities, at least 2-butene(s) and acetylene hydrocarbons; and (iii) optionally rectification zone for mainly 1,3-butadiene-containing stream. In the latter, α-acetylene hydrocarbons are subjected to liquid-phase selective hydrogenation with hydrogen or hydrogen-containing mixture in presence of solid catalyst containing metal(s) exhibiting high activity in hydrogenation process, preferably non-precious metal(s) on solid support. Temperature is maintained within a range 5 to 75°C at contact time ensuring hydrogenation of no more then 6%, preferably no more than 2% of butadiene present. After hydrogenation, 1,3-butadiene is optionally additionally separated from impurities via rectification.

EFFECT: simplified process.

13 cl, 3 dwg, 2 tbl, 10 ex

FIELD: petrochemical processes.

SUBSTANCE: process involves extractive rectification in presence of extractant mainly containing aliphatic N-alkylamide, while toluene is introduced into rectification column point disposed between extractant inlet and the top of column.

EFFECT: reduced loss of extractant with distillate.

6 cl, 3 dwg, 6 tbl, 6 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalysate of reforming of long gasoline fractions containing more than 2% benzene is separated by rectification into three fractions: light-boiling fraction containing mainly nonaromatic C4-C6-hydrocarbons and no more than 1%, preferably no more than 0.5%, benzene; high-boiling fraction containing mainly aromatic and nonaromatic hydrocarbons C7 or higher and no more than 1%, preferably no more than 0.5%, benzene; and benzene fraction boiling within a range of 70-95°C and containing no more than 0.1%, preferably no more than 0.02%, toluene and no more than 0.02% nonaromatic hydrocarbons with boiling temperature above 110°C. Benzene fraction is routed into benzene isolation process involving extractive rectification with polar aprotic solvent having ratio of dipole moment to square root of molar volume above 0.3 db/(cm3/g-mole)1/2, preferably above 0.4 db/(cm3/g-mole)1/2, and boiling temperature 150 to 250°C.

EFFECT: improved quality of benzene.

4 dwg, 2 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to method of hydrophormylation of unsaturated olefine compounds with number of carbon atoms from three to sixteen in presence of catalyst in form of rhodium, modified with ligands, selected from group including phosphonites, phosphites, phosphinoxides, phosphines, phosphinites, phosphinines and/or phosphinanes, and is characterized by carrying out hydrophormylation in presence of not less than 0,1-106 mol% per unsaturated olefine compound of not less than one cyclic ether of carbonic acid, selected from group, which includes ethylcarbonate, propylene carbonate, buthylene carbonate and their mixtures.

EFFECT: increasing catalyst stability and output on more preferable terminal aldehydes.

9 cl, 4 ex, 1 tbl, 3 dwg

FIELD: chemistry.

SUBSTANCE: hydrophormylation is carried out in presence of cyclic ether of carbonic acid, selected from group, which includes ethylene carbonate, propylene carbonate or butylene carbonate or their mixtures, content of carbonic acid ether constituting from 1 wt % to 98 wt % from reaction mixture.

EFFECT: simplicity of catalyst regeneration and low degree of catalyst deactivation.

9 cl, 3 ex, 3 tbl, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention pertains to the method of oxidation of hydrocarbons using oxygen in trifluoroacetic acid and can be used particularly for oxidation of alkanes, cycloalkanes, alkylaromatic hydrocarbons, alkenes, cycloalkenes. The method involves saturation of trifluoroacetic acid with oxygen, after which, the initial hydrocarbon is added to the obtained reaction medium and is kept until depletion of bound oxygen with obtaining the corresponding oxygen containing compound.

EFFECT: invention allows carrying out a process of selective partial catalytic oxidation of hydrocarbons with obtaining different oxygen containing organic compounds without use of high temperature and traditional catalyst systems based on transition metals.

1 tbl, 5 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of 2-ethylhexanol that is used in manufacturing plasticizing agents of high quality, solvents and lubricating materials. Method involves the hydrogenation reaction of 2-ethylhexenal at increased temperature and pressure in regiment of incomplete conversion of 2-ethylhexenal and recycle of nonconverted 2-ethylhexenal to the hydrogenation step and isolation of the end 2-ethylhexanol by rectification and hydropurification on nickel-containing catalyst at increased temperature and pressure. Concentrate of 2-ethylhexenal is used a raw for hydrogenation prepared by condensation of n-butyric aldehyde, and the hydrogenation process is carried out in liquid phase under pressure 200-300 atm, temperature 100-2200C and using nickel-containing catalyst. Isolation of crude 2-ethylhexanol from hydrogenizate containing, except for 2-ethylhexanol, also C8-aldehydes, C8-unsaturated alcohols, C12-acetals, C12-ethers and esters and other oxygen-containing impurities with boiling point near that of 2-ethylhexanol is carried out by rectification under vacuum in four columns: in the first column light impurities are isolated, in the second column unreacted C8-aldehydes are isolated, in the third column crude 2-ethylhexanol is isolated, and in the fourth column 2-ethylhexanol is extracted additionally from the third column vat residue. As a recycle to the hydrogenation mixture of fraction of unreacted C8-aldehydes from upper part of column and 2-ethylhexanol taken in the mass ratio of sum of C8-aldehydes to 2-ethylhexanol in the range = (0.03-0.5):1, and in the mass ratio fresh raw : recycle = (0.3-3):1 is fed to the hydrogenation step. Isolation of recycle fraction of C8-aldehydes in the second column is carried out at the pressure value on upper part of column 50-200 mm of mercury column, temperature difference between 12-th theoretic plate from upper and upper part of column 15-350C with consumption wherein potential removal of 2-ethylhexanol in column distillate is 1-5 wt.-%. Method provides synthesis of 2-ethylhexanol of high quality and high yield and to prolong working life of the hydrogenation catalyst.

EFFECT: improved method of synthesis.

16 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to technology of production of higher aldehydes and alcohols via hydrofomylation of olefins. C6-C24-olefins are subjected to hydrofomylation on cobalt or rhodium catalyst to achieve degree of conversion 20 to 98%, whereupon catalyst is removed from the product, regenerated and returned to hydrofomylation reactor. Resulting liquid mixture is separated by distillation into low-boiling olefins- and paraffins-containing fraction and bottom fraction containing aldehydes or aldehydes/alcohols mixture. In the case of alcohols being desired product, product fraction is subjected to hydrogenation on hydrogenation catalyst including copper, nickel, chromium, zinc, molybdenum, or mixture thereof, after which hydrogenate is routed to distillation. Olefins contained in low-boiling fraction are subjected to hydrofomylation comprising above-indicated stages. Bottom fractions obtained in all process stages are processed together in common reaction product separation stage.

EFFECT: increased yield of desired product due to improved technology.

19 cl, 3 dwg, 2 tbl, 6 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for oxidizing liquid hydrocarbons in barrier discharge carried out in the bubble reactor with mixtures of oxygen with helium, argon or nitrogen. Method involves using helium, argon and nitrogen taken in the amount 20-80%. The oxidation process is carried out in the presence of solid additives wherein aluminum, nickel, molybdenum, copper oxides or zeolite catalyst ZSM-5 comprising 1.2% of Fe is used. Method provides reducing energy consumptions for oxidation of the parent hydrocarbon in the barrier discharge.

EFFECT: improved oxidizing method.

3 cl, 2 tbl, 10 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of alcohol comprising synthesis of olefins by the Fischer-Tropsch process followed by the hydroformylation reaction and isolation of mixture of alcohols. Hydrocarbon fraction with the content of linear olefins 10-45 wt-% is separated from products reaction synthesized by the Fischer-Tropsch process with using cobalt catalyst by distillation followed by its hydroformylation with carbon monoxide and hydrogen taken in the molar ratio hydrogen to carbon monoxide = 1.0-5.0. The reaction of synthesis is carried out in the presence of cobalt-base catalyst and a substituted or unsubstituted monophosphocycloalkane ligand followed by steps of hydrogenation and distillation. Invention provides preparing a composition with the content of linear (C7-C12)-alcohols 60 wt.-%, not less, high rate of reaction and high selectivity of the process.

EFFECT: improved method of synthesis.

8 cl, 3 tbl, 4 ex

FIELD: industrial organic synthesis.

SUBSTANCE: process involves aldol condensation of n-butyric aldehyde in presence of 1-3% aqueous NaOH solution to form 2-ethyl-2-hexenal, which is washed out to remove alkali residues and distilled on steam stripping rectification column to separate high-boiling products, after which it is hydrogenised on copper-chromium catalyst to produce 2-ethylhexanol. 2-Ethyl-2-hexenal distillation bottom residue is treated for 15-60 min with aqueous NaOH solution at 100-120°C and aqueous NaOH solution-to-bottom residue volume ratio 1:(4-10). Alakali effluent produced in n-butyric aldehyde aldol condensation stage is evaporated to NaOH concentration 15-30% and then utilized to treat 2-ethyl-2-hexenal distillation bottom residue, while water steam obtained from evaporation is used as vaporizing agent in stripping rectification column.

EFFECT: reduced (by a factor of 20-50) volume of alkali effluent in aldol condensation stage.

2 tbl, 10 ex

FIELD: petrochemical processes.

SUBSTANCE: alcohols such as tert-pentanol or tert-butanol are obtained via liquid-phase hydration of alkenes contained in hydrocarbon feedstock in presence of solid high-acidity catalyst at elevated temperature in two consecutive stages followed by separation of unreacted hydrocarbons from reaction mixture withdrawn, preferably via rectification, from the second stage and containing synthesized alcohols. In the first reaction stage carried out at higher temperature, reaction zone(s) comprises two liquid phases, of which phase containing basically water, is in essential weight excess and phase mainly containing hydrocarbon(s) is in dispersed state. Withdrawn is only or mostly (i) liquid stream containing mainly hydrocarbon(s), synthesized alcohol(s), and dissolved water and optionally (ii) liquid stream containing basically water and alcohol(s). The latter, in the second stage, is fed through distribution device(s) into one or several in series arranged reaction zones, water being introduced into one or several reaction zones separately, and liquid in the second-step reaction zones, operated at lower temperature, is maintained in homogenous or heterogeneous state wherein one phase containing basically water and alcohol(s) is in dispersed state and its weight does not exceed 25% of the weight of phase basically containing hydrocarbons and alcohol(s).

EFFECT: increased conversion of feedstock and accelerated reaction.

12 cl, 1 dwg, 3 tbl, 6 ex

FIELD: organic chemistry, in particular production of high oxoalcohols.

SUBSTANCE: invention relates to method for production of high oxoalcohol from isomeric olefin mixture containing from 5 to 24 of carbon atoms. Claimed method includes hydroformylation in presence of catalyst at elevated temperature and elevated pressure. Hydroformylation in carried out in one step, and ones-through olefin conversion is limited in range of 40-90 %. Obtained reaction mixture after catalyst separation is preferably transferred to selective hydration carrying out at 120-220°C and pressure of 5-30 bar in presence of supported catalyst containing copper, nickel and chromium as active ingredients. Hydration product mixture is separated by distillation, and olefin fraction is recycled into hydroformylation step. As starting materials for hydroformylation mixtures of C8-, C9-, C12- or C16-olefins are used.

EFFECT: high olefin conversion ratio, selectivity, and capability.

15 cl, 1 dwg, 1 tbl, 2 ex

The invention relates to the synthesis of polyhydric alcohols, in particular to the allocation method neopentyl glycol, obtained by condensation samalanga aldehyde with formaldehyde in the presence of sodium hydroxide and used in the synthesis of polyesters and resins for the paint industry, synthetic lubricating oils and plasticizers