Method for cobalt regeneration of cobalt sludge

FIELD: chemistry.

SUBSTANCE: invention refers to the field of organic synthesis, namely to the preparation of butyraldehyde from synthesis gas and propylene by the method of oxo process (called also propylene hydroformylation process), particularly to the cobalt regeneration of cobalt sludge. The described method involves the regeneration of the cobalt from cobalt-containing sludge forming in oxo process with usage of cobalt dicarbonyl as catalyst by the way of sludge treatment by the high-boiling organic acid with stirring at elevated temperatures, preferably 190-220°C at the ratio acid: sludge equal 10-20 during no less than 4 hrs.

EFFECT: simplifying of the technology of cobalt sludge regeneration and implementation of the regeneration stage directly on the hydroformylation plant.

3 cl, 3 tbl, 1 ex

 

The invention relates to the field of organic synthesis, namely the production of aldehydes by the method of oxosynthesis from synthesis gas and propylene from the reaction CO+H2+CH2CHCH3=(n, iso)C4H8O - in the process, which in this case is called the process of propylene hydroformylation.

The process is carried out at a temperature of 120-150°C and pressures up to 30 MPa in the presence of a catalyst. On most operating industrial plants using cobalt catalyst in the form of dioctahedral cobalt

[H Co(CO)4]2(simplistically - hydrocarbonyl), in which the reaction zone is at a concentration of 0.1-0.2 wt.% (in terms of metallic cobalt).

A variety of technological schemes of the process and its technical and economic performance is directly linked to the method of extraction of cobalt from the reaction mass (ECOBALTICA), to return cobalt in the process.

In industrial practice, the earliest were the technological scheme with thermal decomposition of hydrocarbonyl cobalt emitting cobalt metal media: stationary (e.g., pumice) / Patent Germany 896341, 1956/ or suspended in the reaction mass (for example, kieselguhr) /Silich M.I. Chem. science and industry 1957, vol. 2, No. 1, p 59.)/, and without the media getting the suspension of the powder is metallicheskogo cobalt /A.S. The USSR 173224/. Replaced thermal methods came the so-called salt of the schema in which hydrocarbonyl cobalt destroyed by processing the product of the mass of the acid. One of the analogues salt schemes is the process of the company Mitsubishi under which demobilization carried out in an aqueous solution of nitric acid, the resulting solution of nitrate of cobalt is separated from the reaction mass, and then carry out the exchange reaction with the sodium salt of lauric acid. Winners of cobalt float above aqueous solution of sodium nitrate and in this form is returned to the process (stage carbonylative) /Chem. Eng., 1965, v.72, N 11, p.90/.

The closest analogue of the invention is the most modern so-called "naphthenate-evaporation scheme, developed by the specialists of the USSR (Vniineftehim) and GDR (National enterprise of Leuna-Werke) /Hankin V.Y. and other Htim, 1966, No. 10, p.12/.

A distinctive feature of this scheme is that the products of propylene hydroformylation, separated from the synthesis gas, process air (oxygen) at a temperature not exceeding 50°C (to avoid thermal decomposition of hydrocarbonyl cobalt) in the presence of high molecular weight acids (e.g., naphthenic acid, 2-ethylhexanoate, 2-ethylhexanoate, and other similar acids). When this oxygen partially oxidizes aldehydes, forming hydroxypropane the si, which then interacts with hydrocarbonyl cobalt and, for example, 2-ethylhexanoic acid, to form oil-soluble salt of cobalt and of this acid. In the subsequent distillation of the reaction mass of target products (isomeric oil aldehydes, acids and a number of isomeric butyl alcohols produced by hydrogenation of aldehydes with hydrogen from the composition of the synthesis gas) oil-soluble cobalt salts remain in the VAT residue, recycled into the process at the stage of carbonylative. At this stage, cobalt, isolated from the products of propylene hydroformylation in the above schemes (metal or in the form of oil-soluble salts) is treated with carbon monoxide at a temperature of 130-180°C and pressure up to 300 MPa. The resulting diaballickall in a mixture with propylene and synthesis gas is fed into the reactor hydroformylation, which under the influence of hydrogen diaballickall becomes hydrocarbonyl cobalt, through which the synthesis of aldehydes. Losses of cobalt in this process is carried out in a reaction-distant apparatus, which serves acetate solution of cobalt (usually 5-15% aqueous solution of acetic acid and higher acid involved in the process, such as 2-ethyl-hexane. In the result of the exchange reaction in the distillation moving water and acetic acid, and oil-soluble salt of cobalt together with recirculating kubovy the remainder is fed to the stage of carbonylative.

With all the advantages of naphthenate-evaporation scheme, it has such a disadvantage as inlay sediments of the inner surfaces of vessels, tanks and piping from reactor processing products hydroformylation oxygen (air)to the receiver VAT residue after the distillation of target products. Deposits make it difficult working conditions of heat exchangers, occupy the volume of the containers, cover the living section of the pipeline. For this reason, the technological scheme forced to enter duplicate equipment and carried out periodic cleaning of the resettable devices from sediments. Purification precedes the washing system (5-15%) aqueous solution of acetic acid, with which it is possible to remove soluble compounds from the sediments, loosen them, which facilitates the subsequent mechanical (usually manual) cleaning equipment from the residue, the so-called "cobalt sludge", causing major losses of cobalt in the process.

In order to reduce losses cobalt cobalt sludge processed according to the following scheme (prototype).

The sludge is dissolved in sulfuric acid, in which it is highly soluble. Received dissolve the sulphate of cobalt served in the apparatus, where under the pressure of the carbon dioxide is mixed with equimolar amount of sodium bicarbonate. In the sediment falls carbonate cobalt. The precipitate is separated from the solution in settling centrifuge, washed with water and then fed into the apparatus, which is mixed with equimolar amount of acetic acid, removing the evolved carbon dioxide. The resulting solution of cobalt acetate is injected into the reaction-distant apparatus, which receives an oil-soluble salt of cobalt (as described above). Because of mnogostadiinost with relatively small material flows usually cobalt sludge is passed on specialized refineries, where a similar scheme is processed cobalt containing ore, thus obtaining (with the addition of operations: parki, crystallization and drying) of the crystalline cobalt acetate is used in the process of propylene hydroformylation. /Bolshakov K.A. "Chemistry and technology of cobalt". M, Chemistry, 1981; Chemical encyclopedia, Vol.2, 1990 str. "Cobalt acetate"/.

The disadvantages of technology regeneration of cobalt sludge, described the prototype, except mnogostadiinost is spending reagent (sulfuric acid, sodium bicarbonate) and auxiliary materials (carbon dioxide), the presence of effluents and emissions into the atmosphere, and in the processing of it on special is sirovina plant transportation costs are added, and the operation of parki, crystallization, drying of the crystals and their packing.

The aim of the present invention is to simplify and reduce the cost of recovery technologies cobalt sludge and operation of regeneration directly on the installation of propylene hydroformylation.

When solving the tasks we studied different techniques to which requirements were applied to the simplicity of the technology, its combination with the technology existing and planned facilities of propylene hydroformylation, environmental and Toxicological safety.

In the course of the investigations, it was found:

that cobalt sludge, already at room temperature, soluble in mineral acids (sulfuric, nitric, hydrochloric), practically insoluble in strong organic acids (formic, acetic) at room temperature and at long boiling;

- when exposed to cobalt sludge elevated temperature ranging from 170°C, there is a change in coloration from dark crimson to black with selection (sublimation) whitish vapor, otlichayuschihsya on cooled surfaces in the form of white crystals, Elemental analysis of these crystals showed that the composition contains (wt.%): carbon 70-75; oxygen 12-17; hydrogen 10-15, and analysis of the black residue showed that he is a her mainly of cobalt oxide (CoO).

Next, we studied the simultaneous exposure to cobalt sludge of high temperature and high molecular weight (i.e. high-boiling organic acids.

The experiments were conducted in a glass flask placed in an oil bath and equipped with a stirrer, thermometer and reflux condenser. It was found that cobalt sludge at elevated temperatures (160°C) is appreciably soluble in 2-ethylhexanoic acid. The evaluation was made by measuring the time of complete dissolution of the sample of cobalt sludge at a given temperature. The best results were achieved when the boiling point of 2-ethylhexanoic acid, which at atmospheric pressure is equal 218-220°C (depending on the degree of its purification). Decomposing 2-ethylhexanoic acid were not observed. During the experience there has been little selection of whitish vapor and deposition of white crystalline substance in the neck of the flask, but it was quickly dissolved by phlegm, flowing down from the back of the refrigerator.

In the course of the experiments has been stable (at room temperature) solution of cobalt salt 2-ethylhexanoic acid in which the concentration of cobalt (in terms of metal) reached 5-6% by weight.

In subsequent experiments in a laboratory setup, we investigated the behavior of the obtained solutions in terms of% the pas oxosynthesis (stage carbonylative, of propylene hydroformylation and distillation of target products), fully reproducing the industrial, which are described above. If this were the results obtained are identical to those which were received with use of 2-ethylhexanate cobalt, obtained as a result of metabolic reactions in the reaction-distant apparatus (see above the description of technology of the process).

Thus, the proposed method of recovery of cobalt from cobalt sludge is fully consistent with the goal and the ways of solving the task.

The essential difference of this invention from the prototype and its advantage is the simplicity of the technology, exclusion from special reagents, lack of wastewater and emissions while significantly reducing the cost of processing.

The invention is illustrated by the following examples.

Example 1. In a vessel equipped with a stirrer, a heater with automatic temperature control and a reflux condenser, placed 10 g of cobalt slurry and poured 90 g of 2-ethylhexanoic acid, preheated to a temperature of 170°C.

After that, include a stirrer and heated to a specified temperature, include the chronometer. The vessel Shine a focused light beam. The dissolution process is considered complete when the solution becomes and is absolutely transparent (without opalescence). Fixed time of dissolution. When switching to a higher temperature heat-up time from 170°C. to a predetermined temperature, is added to the total time. The results of the experiment of example 1 and other examples, are placed in tables 1-3, where the results of experiments on the solubility of the cobalt sludge in other high-boiling organic acids with the time dependence of the dissolution temperature and the weight ratio of acid (To): sludge (W). The time of dissolution was taken as the average from at least three definitions of "rounding" up to half an hour.

As seen from the above examples, focusing on the time of the dissolution of cobalt slurry is not more than 4 hours, technologically acceptable to all used in the examples of the acids should be considered as the weight ratio of the acid in the slurry is in the range from 10 to 20, and the process temperature is above 190°C, but this should take into account thermal stability of the used acid: process temperature should not be above the threshold of its thermal decomposition.

2-ethylhexanoic acid and acids corresponding to the above requirements, the process is preferably carried out at the boiling point, so as boiling provides a good mixing environment without the use of mechanical means. For example, benzoic acid this when the m is excluded because at the boiling temperature (250°C) clearly reveals its thermal decomposition.

1. Method of regeneration of cobalt from cobalt containing sludge formed in the process of oxosynthesis using as catalyst dictcursor cobalt, by processing the sludge acid, characterized in that the processing using a high-boiling organic acid, the treatment is carried out by stirring at elevated temperature, preferably 190-220°C, with a ratio of acid sludge within 10-20, for at least 4 hours

2. The method according to claim 1, characterized in that the processing of sludge use naphthenic acid or benzoic acid, or other high-boiling acid that is compatible with the technology of oxosynthesis, preferably 2-ethyl-hexanoic acid.

3. The method according to claim 2, characterized in that in the case of the application
2-ethylhexanoic acid mixing is carried out by boiling acids, i.e. at a temperature 218-220°C (atmospheric pressure).



 

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FIELD: chemistry.

SUBSTANCE: invention refers to method of aldehydes C3-C21production, consisting that olefins are hydroformylated with the catalyst system added as containing rhodium, polyphosphide ligand of general formula: where k+m≥2, and optionally k=0 or m=0; X is hydrocarbon radical including 1 to 50 carbon atoms; Z is hydrocarbon radicals identical or different in fragments m including 2 to 30 carbon atoms; Y is hydrocarbon radicals identical or different including 1 to 30 carbon atoms, and phosphoprous-containing promoting ligand chosen of monodentate organophosphine, bidentate organodiphosphine and organophosphite. Then product aldehydes are separated from the dissolved catalyst by distillation. The mole ratio of promoting ligand/Rh is 1-50. The disclosed method allows for radioselective production of linear aldehydes C3-C21.

EFFECT: reduced initial charge of polyphosphite ligand with lowered deactivation.

8 cl, 8 tbl, 25 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to synthesis of C7+-aldehydes from C6+-olefins, carbon monoxide, and hydrogen via hydroformylation reaction and to preparation of catalyst used in this reaction. Olefin hydroformylation catalyst contains complex compound of rhodium with polymeric nitrogen-containing ligand including phosphorus-containing fragments. Each of these fragments contains organic radicals, at least one of which is linked to nitrogen atom of polymeric nitrogen-containing ligand and phosphorus atom is in the form of Ph(III). Catalyst preparation consists in that nitrogen-containing polymer is subjected to reaction in organic solvent with Ph(III) compound including organic radicals, of which at least one radical includes group -C(O)OH. Thus obtained product is then subjected to reaction with rhodium compound and organic solvent is removed.

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11 cl, 1 tbl, 8 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for isolating n-butyric aldehyde from the aldehyde distillate of a propylene hydroformylation product containing, n-butyric aldehyde, isobutyric aldehyde and water, butyl alcohols, methanol, butylformate, acids, hydrocarbons, saturated and unsaturated butyl esters, propylketones, butylbutyrates, C8-aldehydes, C12-acetals and unidentified oxygen-containing components as impurities. Method is carried out into two fractionating devices wherein isobutyric aldehyde, water and some amount of n-butyric aldehyde and other impurities are isolated by upper part of the first device, and the end n-butyric aldehyde is isolated by upper part of the second device from vat product of the first device. Isolation of n-butyric aldehyde is carried out in heat-mass-exchange devices equipped by heat-mass-exchange packages made of metallic sheet or net and prepared as Z-shaped crimps, and special equipments for uniform distribution of phlegm by device section and wherein the specific surface of these packages is 100-800 m2/m3 and with corresponding height of crimps and their slope by vertical providing the pressure drop value between upper part and bottom of the first device in the range 0.01-0.10 atm., and that of the second device in the range 0.01-0.07 atm. Isolation of head fraction in the first device is carried out with consumption wherein amount of n-butyric aldehyde in its is 2-2 wt.-% of potential content in rectification raw. Separation in the second device is carried out at the spraying temperature on upper package of the device in the range 20-30oC. Method provides simplifying of technology in isolation of n-butyric aldehyde, enhancing potential removal of n-butyric aldehyde and decreasing consumption of heating steam per 1 t of the end product.

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11 ex

FIELD: organic chemistry, chemical technology.

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3 cl, 2 tbl, 10 ex

FIELD: industrial organic synthesis.

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2 cl, 14 ex

FIELD: organic chemistry, chemical technology.

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11 cl, 3 tbl, 3 dwg, 2 ex

FIELD: organic chemistry, in particular production of carbonyl compounds such as aldehydes and ketones.

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5 cl, 1 tbl, 14 ex

FIELD: chemical technology.

SUBSTANCE: invention describes a method for realization of the multiphase reaction of hydroformylation of olefins in tube reactor wherein a catalyst is in the continuum liquid phase and at least one the parent product is in the dispersed phase. The hydroformylation reaction is carried out at the loading coefficient B 0.8 or above that is calculated as a quotient from the pressure fall PD length value and the static pressure PS value wherein PD = Cw x g/2 x w2/D and PS = (M/V) x g wherein Cw means a tube reactor resistance coefficient; D means diameter of tube reactor; W means a flow rate moving; S means a density value of flowing phase; M means a weight flow of all components in reactor; V means a volume flow; g = 9.81 m/c2.

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11 cl, 1 dwg, 9 ex

FIELD: organic chemistry, chemical technology.

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1 tbl, 4 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: technology for separation of hydroformylation products by naphthenate-evaporating schedule of oxo-synthesis. Separation of propylene hydroformylation products after its decolbatization is carried out by a single evaporation under atmosphere pressure with separation of distillate - fraction of butyric aldehydes from the vat residue - cobalt salts solution in high-boiling by-side products. Indicated evaporation with separation of vapor phase from liquid phase is carried out in separator device under atmosphere pressure, at temperature of liquid phase 90-115°C or 130-170°C with reinforced circulation of liquid phase through boiler at the circulation ratio = (3-30):1. Then the successive additional extraction aldehydes and alcohols from the vat residue are carried out by a single evaporation under vacuum. Method provides reducing loss of cobalt catalyst at the stage for separating products of oxidative decolbatization, and improved economic indices.

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9 ex

FIELD: chemistry.

SUBSTANCE: invention refers to method of aldehydes C3-C21production, consisting that olefins are hydroformylated with the catalyst system added as containing rhodium, polyphosphide ligand of general formula: where k+m≥2, and optionally k=0 or m=0; X is hydrocarbon radical including 1 to 50 carbon atoms; Z is hydrocarbon radicals identical or different in fragments m including 2 to 30 carbon atoms; Y is hydrocarbon radicals identical or different including 1 to 30 carbon atoms, and phosphoprous-containing promoting ligand chosen of monodentate organophosphine, bidentate organodiphosphine and organophosphite. Then product aldehydes are separated from the dissolved catalyst by distillation. The mole ratio of promoting ligand/Rh is 1-50. The disclosed method allows for radioselective production of linear aldehydes C3-C21.

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8 cl, 8 tbl, 25 ex

FIELD: chemistry.

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6 cl, 6 ex, 2 tbl

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.

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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.

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9 cl, 3 ex, 3 tbl, 2 dwg

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to synthesis of C7+-aldehydes from C6+-olefins, carbon monoxide, and hydrogen via hydroformylation reaction and to preparation of catalyst used in this reaction. Olefin hydroformylation catalyst contains complex compound of rhodium with polymeric nitrogen-containing ligand including phosphorus-containing fragments. Each of these fragments contains organic radicals, at least one of which is linked to nitrogen atom of polymeric nitrogen-containing ligand and phosphorus atom is in the form of Ph(III). Catalyst preparation consists in that nitrogen-containing polymer is subjected to reaction in organic solvent with Ph(III) compound including organic radicals, of which at least one radical includes group -C(O)OH. Thus obtained product is then subjected to reaction with rhodium compound and organic solvent is removed.

EFFECT: increased and preserved specific activity and regioselectivity of recycled catalyst and reduced pressure in aldehyde production process.

11 cl, 1 tbl, 8 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 the hydroformylation process of olefins with using rhodium catalyst for preparing aldehydes comprising 3-21 carbon atoms. Reaction products from the hydroformylation reactor are separated for: (a) gaseous and liquid phase; (b) liquid phase is fractionated for a head fraction containing unreacted olefins and aldehydes and a vat fraction containing by-side products and rhodium catalyst, and (c) the vat fraction is cooled to temperature lower than the hydroformylation point into reactor, preferably, to 10-120°C. Then the vat fraction is saturated with carbon monoxide-containing gas under partial pressure of carbon monoxide 0.1-300 bars. The vat fraction containing catalyst and carbon monoxide are recovered completely or partially into the hydroformylation reactor. Invention provides prolonged working life of catalyst due to prevention of its inactivation in stages for isolation of the end product.

EFFECT: improved preparing method.

11 cl, 3 tbl, 3 dwg, 2 ex

FIELD: chemical technology.

SUBSTANCE: invention describes a method for realization of the multiphase reaction of hydroformylation of olefins in tube reactor wherein a catalyst is in the continuum liquid phase and at least one the parent product is in the dispersed phase. The hydroformylation reaction is carried out at the loading coefficient B 0.8 or above that is calculated as a quotient from the pressure fall PD length value and the static pressure PS value wherein PD = Cw x g/2 x w2/D and PS = (M/V) x g wherein Cw means a tube reactor resistance coefficient; D means diameter of tube reactor; W means a flow rate moving; S means a density value of flowing phase; M means a weight flow of all components in reactor; V means a volume flow; g = 9.81 m/c2.

EFFECT: improved method, enhanced output of process.

11 cl, 1 dwg, 9 ex

FIELD: processes catalyzed by metal-phosphoro-organic ligand complexes when target product may be selectively extracted and separated from liquid product.

SUBSTANCE: Specification gives description of methods of separation of one or several products of decomposition of phosphoro-organic ligand, one or several reaction byproducts and one or several products from liquid reaction product synthesized continuously and containing one or several non-consumed reagents, catalyst in form of complex of metal-phosphoro-organic ligands, not obligatory free phosphoro-organic ligand, one or several said decomposition products of phosphoro-organic ligand, one or several said reaction byproducts, one or several said products, one or several non-polar solvents and one or several polar solvents by separation of phases where (i) is selectivity of non-polar phase for phosphoro-organic ligand relative to one or several products expressed by ratio of distribution coefficient Ef1 whose magnitudes exceeds about 2.5; (ii)is selectivity of non-polar phase for phosphoro-organic ligand relative to one or several decomposition products expressed by ratio of distribution coefficients Ef2 whose magnitude exceeds proximately 2.5; and (iii) is selectivity of non-polar phase for phosphoro-organic ligand relative to one or several reaction byproducts expressed by ratio of distribution coefficients Ef3 whose magnitude exceeds approximately 2.5 (versions). Description is also given of continuous methods of obtaining one or several products (versions) and reaction mixture containing one or several aldehyde products.

EFFECT: increased conversion of initial materials and selectivity by product; avoidance or exclusion of deactivation of catalyst.

20 cl, 2 tbl

FIELD: methods of production of 1.3 alkandiol.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to production of 1.3 alkandiol by hydrogenation of the raw material, containing 3-hydroxyaldehyde at presence of a catalyst and a source of hydrogen, where as a source of hydrogen use a synthesis gas, and the catalyst represents a heterogeneous catalyst containing copper on the carrier; and also to the method of production of 1.3-alkandiol by conversion of an oxide in the process including a hydroformylation and hydrogenation. At that it is not obligatory to realize the indicated phases simultaneously in one reaction vessel. The reached technical result consists in essential reduction of the fixed value of equipment and in bringing to a "single-phase" production of 1.3-propandiol (or a similar 3-alcandil) from ethylene oxide (or a corresponding oxide).

EFFECT: the invention ensures essential reduction of the fixed value of equipment and reduction to a "single-phase" process of the propandiol or alkandiol production.

9 cl, 2 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention concerns method of hydrotreating catalyst activation containing metal oxide of group VIB and metal oxide of group VIII containing contacting catalyst, acid and organic additive with boiling point within 80-500°C and water solubility, at least, 5 gram per litre (20°C, atmospheric pressure), optionally with following drying in the environment providing at least, 50% of the additive remains in the catalyst. There are disclosed hydrotreating catalyst produced by the method described above, and method of hydrotreating raw hydrocarbons there after applied.

EFFECT: higher activity of both raw hydrotreating catalyst, and utilized hydrotreating catalyst being regenerated.

20 cl, 8 ex

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