Method for production of high oxoalcohol from olefin mixture
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 a method for producing the highest oxaspiro by hydroformylation mixtures of olefins, comprising a stage of selective hydrogenation of mixtures of products hydroformylation and recycling the unreacted olefins.
As is known, higher alcohols, especially alcohols with carbon atoms from six to twenty-five, can be obtained in the catalytic hydroformylation, also known as oxosynthesis from olefins containing one carbon atom less than the target alcohols, with subsequent catalytic hydrogenation containing aldehydes and alcohols reaction mixtures. Such alcohols is used mainly as a source of products to obtain plasticizers or surfactants.
View of the catalytic system and the optimal conditions of the reaction of hydroformylation depend on the reactivity of the starting olefin. The dependence of the reactivity of olefins from their structure is described, for example, in the book J.Falbe, New Syntheses with Carbon Monooxide, ed. Springer, Berlin, Heidelberg, new York, 1980, p.95 FF. The difference in reactivity is also known in a specific example of isomeric octanol (B.L.Haymore, A. van Hasselt, R.Beck, Annals of the New York Acad. Sci., 415 (1983), str-175).
The technical mixture of olefins, which are used as starting products for the of cosynthase, contain a mixture of isomeric olefins of various structures with different degree of spatial branching, razlichnim the position of the double bond in the molecule, and in appropriate cases and with different numbers of carbon atoms in the molecule. This is especially important to consider when using mixtures of olefins, which were formed as a result of dimerization, trimerization or deeper oligomerization of olefins with carbon atoms from two to five or other easily accessible higher olefins, or as a result of cooligomerization the above olefins. As typical examples of mixtures of isomeric olefins, which as a result catalyzed by rhodium or, more preferably catalyzed by cobalt reaction hydroformylation can turn into a mixture of the corresponding aldehydes and alcohols, should be called three - and tetrapropenyl, as well as di-, tri - and atributary.
The reaction rate of hydroformylation decreases with increasing number of carbon atoms and with increasing degree of branching. The reaction rate linear olefins can be five to ten times higher than the reaction rate their branched isomers. Reactivity is also influenced by the position of the double bond in the molecule of the olefin. Olefins with terminal double bonds react significantly more likely than isomeric olefins with the double bond in the Central part of the molecule. The consequence of differences in the reaction ability of isomeric olefins becomes necessary to increase the reaction time to achieve the highest possible degree of conversion of olefin. But it also leads to a decrease in product yield due to leakage of unwanted parallel and consecutive reactions. The same effect leads and attempt to reduce the time of reaction by increasing the temperature of the reactions. When hydroformylation mixtures of olefins becomes difficult to achieve a combination of high degree of conversion and high selectivity primarily due to the different reaction abilities isomers.
In the document JP 01-160928 A, 1989, describes a single-stage method of hydroformylation8-olefins followed by complete hydrogenation of the resulting reaction mixture. In addition, the document US 4447661 And 1984, the famous two-way hydroformylation, where the second stage of hydroformylation simultaneously carry out the hydrogenation. In the document US 4320237 And 1982, as well as document SU 847911 And 1981, which is equivalent document US 4320237 And describes a two-step method hydroformylating olefins, and in the first stage become chemically more active olefinic end connection, and the second stage is less active inside nnie olefinic connection.
The closest analogue of the present invention is a method of obtaining oxaspiro from mixtures of isomeric olefins by hydroformylation in the presence of a catalyst at elevated temperature and at elevated pressure, followed by hydrogenation to obtain saturated alcohols known from the document EP 0183547 A1, 1985
Known solutions have the above drawback, i.e. the implementation of these methods cannot be reached by an effective combination of high conversion and high selectivity or high performance on-time and on-scope.
The present invention is to develop a method of obtaining highest oxaspiro from the corresponding mixtures of olefins, which combines a high degree of conversion with high selectively and which also has a high performance on-time and on-scope.
The problem is solved by the method of obtaining the highest oxaspiro from mixtures of isomeric olefins with the number of carbon atoms of from five to twenty-four by hydroformylation in the presence of a catalyst at elevated temperature and at elevated pressure, in which hydroformylation carried out in one stage, limiting the degree of conversion of olefins in a single pass outside from 40-90%, the resulting reaction mixture, it is advisable PEFC is the separation of the catalyst, sent for selective hydrogenation, which is carried out at a temperature of 120-220°and a pressure of 5 to 30 bar, in the presence of a catalyst on a carrier containing as active ingredients copper, Nickel and chromium, the mixture of products of hydrogenation separated using distillation and return olefinic fraction on stage hydroformylation.
Corresponding to the invention the method may be performed with respect to both periodic and preferred the continuous scheme. The drawing shows a block diagram of an installation in which the method can be implemented by continuous scheme. In the reactor 1 serves a mixture of olefins 2, synthesis gas (carbon monoxide and hydrogen) 3 and the catalyst 4. In a mixture of products hydroformylation 5 relieve pressure and select the escaping gas 6 (unreacted synthesis gas)after discharge pressure of the mixture of products of hydroformylation in the operations Department of the catalyst 7 is released from the catalyst 4, which, after feeding, if she needed fresh catalyst returns to the reactor 1. Freed from the catalyst, the mixture of products of hydroformylation 8 is directed to a stage of hydrogenation of 9, on which the aldehydes and such contained in a mixture of side products, such as acetals of aldehydes and esters of alcohols, mainly their formate, hydronauts with the formation of alcohol is. Of a mixture of products of the hydrogenation of 10 on stage distillation 11 emit low-boiling components 12, which are mostly unreacted isomeric olefins, and send them together with a fresh portion of the olefins 13 in the form of a mixture of olefins of 2 to the reactor 1. Part of the low-boiling components is removed from the recycling of olefins in the form of residual low-boiling components 14. The crude mixture of alcohols 15 is processed into pure alcohol at the stage of distillation, which in the diagram is not presented.
Initial products for the reaction of hydroformylation are a mixture of monoolefins with the number of carbon atoms of from five to twenty-four, in which the double bond between the carbon atoms may be in the end and in the middle of the chain, for example, 1 - or 2-penten, 2-methyl-1-butene, 1-, 2 - or 3-hexene, formed by the dimerization of propene mixture of isomeric olefins with six carbon atoms (ditropan), 1-hepten, 2 - or 3-methyl-1-hexene, 1-octene formed at the dimerization of butenes mixture of isomeric olefins with up to eight carbon atoms (debute), 1 none, 2-, 3 - or 4-methyl-1-octene formed by the trimerization of propene mixture of isomeric olefins with nine carbon atoms (tryprophan), 1-, 2 - or 3-mission 2-ethyl-1-octene, 1-dodecene formed by tetramerization of propene or the trimerization of butenes mixture of isomeric olefins with two of adatu carbon atoms (tetrapropyl or tribute), 1-tetradecene, 1 - or 2-hexadecene formed by tetramerization of butenes mixture of olefins with sixteen carbon atoms (terabyte), as well as mixtures of olefins, obtained by cooligomerization olefins with different numbers of carbon atoms (preferably from two to four), which if necessary can be separated by distillation into fractions of equal or similar numbers of carbon atoms in the molecules. The preferred source products are a mixture of olefins with eight, nine, twelve or sixteen carbon atoms.
The invention relates to a method or conditions hydroformylation. Olefins hydroformylation in General the usual ways. In accordance with this work is carried out with rhodium or, preferably, cobalt catalysts and with the addition of stabilizing complexes additives, such as organic phosphines or phosphites, or without them. Pressure and temperature depending on the catalyst and a mixture of olefins can vary within wide limits. Description hydroformylation olefin is, for example, in the book J.Falbe, New Syntheses with Carbon Monooxide, ed. Springer, Heidelberg-new York, 1980, p.99, etc., and in Kirk-Othmer, Encyclopedia of Chemical Technology, V.17,4th edition, John Wiley and sons, str-919 (1996).
A significant characteristic izobreteny what is the degree of conversion per pass is limited to the range from 40 to 90%. Preferably the reaction come from 65 to 80% of the olefins. Predpochtitelnye initial products are mixtures of olefins with eight, nine, twelve or sixteen carbon atoms, consisting of a large number of different isomers. As mentioned above, the easiest react olefins linear structure with konzum location of olefinic double bonds. In line with this, the more branched molecule and/or the further shifted double bond in the inner part of the molecule, the lower its reactivity. Corresponding to the invention limit the degree of conversion leads to more reactive olefins react in the first place, and less reactive remain in the reaction mass, and after the selective hydrogenation reaction mixture is returned to the step of hydroformylation. Limiting the degree of conversion increases the selectivity of the reaction of hydroformylation. Recycling olefins leads to an increase in total time for the less reactive olefins. A consequence of the recycling of olefins become higher total degree of conversion of olefin at a lower yield products. Thanks to that achieved higher output is s aldehydes, and after hydrogenation and higher yields of alcohols. In addition, reducing the number of products facilitates the processing of reaction mixtures. Compared with the single-stage method, which does not use recycling olefins corresponding to the invention the method is based on the selective hydrogenation and recycle olefins, improves economic performance of the production oxaspiro.
The degree of conversion of olefins limit zhelatelny value through appropriate changes in the reaction conditions of hydroformylation. The degree of conversion of olefins can be lowered by reducing the reaction temperature and/or concentration of the catalyst, and reducing the duration of interactions. The degree of conversion in a single pass of a mixture of olefins 2, consisting of a fresh mixture of olefins 13 and returned to the process, low-boiling components 12, is determined on the basis of the number and composition of the mixture of olefins 2, and the number and composition of return in the process, low-boiling components 12 with account taken of the low-boiling components 14. The total degree of conversion calculated on the basis of the number and composition of the fresh mixture of olefins 13 and the quantities of olefins, which is removed from the process with the remaining mixture of low-boiling components 14. To determine the content of olefins in the region of slichnih material flows can be used gas chromatography analysis.
The reaction mixture hydroformylation it is useful first to separate from the catalyst, and this operation is also carried out by known methods. If you have used a cobalt catalyst, for his separation, you can use the following operations: pressure relief, separation of the aqueous phase with a catalyst, oxidation with air or oxygen remaining in the mixture of products hydroformylation derivatives of CARBONYLS of cobalt and washing the resulting compounds of cobalt with water or acid solution in water. The methods of separation of cobalt is well known, for example, they are presented in the above cited papers J.Falbe, 164, 165 (BASF process), Kirk-Othmer, as well as in the application for European patent No. 0850905 A1. If the catalyst hydroformylation served as a rhodium compound, it can be separated in a thin film evaporator in the form of residue from distillation of a mixture of products hydroformylation.
Freed from catalyst reaction mass from the stage of hydroformylation contain in the General case, depending on the degree of conversion of 3 to 40 wt.%, most often from 5 to 30 wt.%, the low-boiling components with lower than aldehydes boiling point, mainly olefins along with the corresponding saturated hydrocarbons, and water, and in some cases methanol then they contain from 30 to 90 wt.% aldehydes, from 5 to 60 wt.% alcohols, up to 10 wt.% formate of these alcohols and from 5 to 15 wt.% high-boiling compounds having a boiling point higher than the boiling point of the alcohols. It should be emphasized, however, that corresponding to the invention the method can be implemented and on mixtures of products hydroformylation, which in some way does not meet these parameters.
Selective hydrogenation of mixtures of products of hydroformylation that it is expedient to separate from the catalyst hydroformylation, represents another important hallmark of the relevant invention. When this happens proceeding with the formation of the target alcohols hydrogenation of aldehydes and certain related substances, among which these acetals of aldehydes and esters of alcohols, primarily their formate. Since the degree of transformation at the stage of hydroformylation limited to the economic performance of the process is crucial hydrogenation, in which neprevyshenie olefins not hydronauts or almost not hydronauts, resulting in the possibility of separating them from the mixture of products of hydrogenation and return to the stage of hydroformylation.
Selective hydrogenation of mixtures of products of hydroformylation is the tsya object simultaneously pending patent application No. 198423705 (O.Z. 5356). In accordance with this reaction mixture products hydroformylation hydronaut hydrogen at elevated temperature and at an elevated pressure in the presence of catalyst on the carrier, as the active component contains copper, Nickel and chrome.
The preferred catalysts of this kind are the catalysts on carriers containing as active ingredients copper and Nickel in a concentration of in each case from 0.3 to 15 wt.%, chromium in a concentration of from 0.05 to 3.5 wt.%, and component-based alkali metal in a concentration of from 0.01 to 1.6 wt.%, preferably from 0.02 to 1.2 wt.%, in each case, based on the catalyst on the carrier. Another preferred catalyst on the carrier contains copper, Nickel and chromium in the above quantities, but does not contain the component based on the alkali metal. Suitable substances carriers are primarily silicon dioxide and aluminum oxide. Quantitative characteristics are to receive on the following methodology unrestored catalytic Converter.
This hydrogenation of aldehydes from the reaction mixtures hydroformylation subjected to hydrogenation into the corresponding alcohols with degrees of transformation in each case, more than 98% and a selectivity of more than 99% for a single stage hydrogenation. Esters and acetal is also becoming the target alcohol. It was unexpectedly found that contained in the mixture of the original olefins remain almost completely unchanged, although these preferred catalysts on carriers in comparable conditions hydronaut with practically quantitative yield of olefinic double bond in 2-ethylhex-2-anale (application for European patent No. 0326674 A2). The hydrogenation can be conducted in the area of low pressure (not higher than 30 bar) and high performance over time and volume.
The named components of the catalyst can be a homogeneous distributed in the pores of the material of the carrier or they can be enriched in the outer zone. In the first case, take a water solution that contains components in the form of metal salts, which represent precursors of catalysts, and the amount which is suitable from about 0.8 pore volume of material media. Of the salts of copper, Nickel and chromium are preferably chosen such that when heat is transferred into the oxide, for example, nitrates and acetates. If the catalyst composition should include a component based on the alkali metal, it can be entered together with chromium as chromate or bichromate of an alkali metal, especially in the form of chromate or bichromate of sodium. The concentration of metal salts in solution depends on the desired concentration of the corresponding component in the finished catalyst. Then the races is the thief metal salt sprayed in the drum for drazhirovanija material of the carrier, without exposing his preliminary heat. The solution penetrates into its pores. The preparation of the catalyst to complete the drying operation.
In cases where it is desirable receipt of the catalyst, the components of which are concentrated on the outer sphere porous or more or less devoid of pores of the material of the carrier with a solution of metal salt sprinkle preheated material of the carrier and continue heating of the material of the carrier during spraying so that the water evaporates so that the components of the catalyst were recorded mainly on the surface of the material medium.
After application of the catalyst components both above-mentioned types of conduct calcination, that is, depending on the nature of the precursors of catalysts heated up to temperatures from 200 to 400°that translates predecessors catalyst in oxide form. Thereafter, the catalyst is reactivated by hydrogen. The recovery may be carried out immediately after preparation of the catalyst or, more appropriately, in the hydrogenation reactor.
It is preferable to use the catalyst in a form which provides a low flow resistance, for example, in the form of pellets, lumps, or in the form of tablets, cylinders, Blockoban extrudates or rings. It is advisable to activate them before the COI is whether the heating in a current of hydrogen, for example, when the above temperature hydrogenation of from 150 to 250°if they were not recovered in the reactor.
The hydrogenation can be carried out both in liquid and in the gas phase with the design process both periodic and continuous scheme. Hydrogenation prefer to spend in the liquid phase, since the process in the gas phase requires high energy costs due to the necessity of the organization of recycling large volumes of gas. In addition, the evaporation of aldehydes with increasing number of carbon atoms requires more and more energy, and the content of the original product in the incoming reaction gas is reduced, and the implementation of gas-phase variant of the process of the aldehydes with the number of carbon atoms of more than approximately eight becomes problematic from an economic point of view.
For the hydrogenation in the liquid phase can be chosen in different technological options process. It can be done in adiabatic mode or in a mode close to isothermal, i.e. with a temperature increase of no more than 10°With, in one or in two stages. In the latter case, both the reactor (preferably a shell-and-tube reactors were) can work as in the adiabatic regime, and the regime close to isothermal, or one of the reactors can operate in adiabaticheskogo, while the other mode that is close to isothermal. You can also carry out the hydrogenation of mixtures of products hydroformylation in flow mode or to return the product recovery for recycling. The reactors can be operated in a stationary mode with irrigation catalyst layer or, preferably, with high loadings on the amount of liquid. In the interests of improving performance over time and volume prefer to use reactors with high loads on the fluid in the range of 5 to 100 m3most often from 15 to 50 m3per square meter of the cross-section of the empty reactor per hour. If the reactor is operated in isothermal mode for running the scheme, the unit load on the catalyst may be in the range from 0.1 to 10 h-1preferably from 0.5 to 5 h1.
The hydrogenation in the liquid phase is conducted usually at a total pressure of from 5 to 30 bar, more often in the range from 15 to 25 bar. Hydrogenation in the gas phase can be carried out at lower pressures with a corresponding increase in the volumes of gases. The reaction temperature in the hydrogenation in the liquid or in the gas phase are usually in the range from 120 to 220°With, usually from 140 to 180°C.
Separation of the mixture of products of hydrogenation using distillation
The resulting hydrogenation of reactions is by a mixture of share in General known distillatively ways. This operation is expediently carried out at reduced pressure, for example at an absolute pressure of 400-900 mbar. When this occurs, the allocation of unreacted olefins, which represents the major part of the low-boiling fractions of the components. It is advisable that a large portion of low-boiling fractions of the components, typically from 60 to 98%, acted as recycle to the stage of hydroformylation. The remaining fraction of the low-boiling components, i.e. from 2 to 40%, can be derived from the recycling of olefins to the concentration of the inert formed during the hydrogenation of olefins under hydroformylation saturated hydrocarbons did not exceed 70%, preferably to maintain it at the level of less than 60%.
In the high pressure autoclave with a volume of 5 l equipped with a stirrer and a system of electric heating, conduct hydroformylation 2000 g of di-n-butene (olefin with the number of carbon atoms equal to eight, obtained in the production process of octol on the firm OXENO) in the presence of a cobalt catalyst at a temperature of 180°at constant pressure syngas equal to 280 bar. Synthesis gas consists of 50 % by volume of carbon monoxide and 50 % by volume of hydrogen.
To obtain gidrocarbonata cobalt, serving as the utilizator, used as a catalyst precursor aqueous solution of cobalt acetate containing of 0.95 wt.% cobalt. A solution of cobalt acetate is treated with sintezator under stirring for 7 hours at a temperature of 170°and a pressure of 280 bar. After cooling to room temperature and pressure relief formed peridocially cobalt transferred to the organic phase by extraction with di-n-butene, which is used as the source of the product. After separation of the aqueous phase di-n-butene with dissolved in it hydridoborate cobalt and containing cobalt, equal to 0.025 wt.% (based on cobalt metal), hydroformylation for three hours at the above conditions.
After cooling to room temperature, and discharge pressure unload the reaction mixture from the autoclave and deliver her from the cobalt catalyst by treatment with 5%acetic acid and air at a temperature of 80°C. Receive 2488 g of a mixture of products hydroformylation, whose composition is analyzed by gas chromatography. The results of the analysis are shown in table 1. In accordance with these data, the achieved degree of transformation of di-n-butene is 89,3% with a selectivity of target product, equal to 90.7 percent, which corresponds to a yield of target products 81,0 % based on introduced in the reaction of di-buten. The concept of target products refers to aldehydes with nine carbon atoms, alcohols containing nine carbon atoms and (from)noninformation.
An example of implementation of the invention of the method
Hydroformylation di-n-butene recycle of olefin with up to eight carbon atoms
Conduct selective hydrogenation 2488 g of a mixture of products hydroformylation obtained in example comparison, and get the target product alcohol with nine carbon atoms while maintaining the olefins in an unmodified form. The hydrogenation is carried out in the liquid phase on intermittent autoclave with a volume of 5 liters at a temperature of 180°and at hydrogen pressure of 20 bar in the presence of catalyst on the carrier, representing deposited on the aluminum oxide to 12.1 wt.% copper, 3.0 wt.% Nickel and 2.5 wt.% chromium. In conclusion, laboratory distillation column carry out the distillation of the mixture of products of hydrogenation for separating the low-boiling components, representing unreacted olefins from the target products and high-boiling components.
Receive 250 g of low-boiling fractions of the components, which according to gas chromatographic analysis, along with 98,7 wt.% hydrocarbon with eight carbon atoms, which is 78.4 wt.% are olefins with up to eight carbon atoms, contains about 1.3 wt.% methanol is, resulting from the hydrogenation of (doing)noninformative.
In an autoclave with a capacity of 5 liters at a pressure of syngas 280 bar and temperatures up to 180°conduct hydroformylation this mixture of low-boiling fraction with 2000 g of di-n-butene, i.e. in total, 2250 g of the raw product containing 2193 g of olefins with up to eight carbon atoms. The reaction is carried out in the presence of cobalt catalyst by analogy with the example of comparison. And in this case, use a synthesis gas containing 50 vol % of carbon monoxide and 50 % by volume of hydrogen. When the content of cobalt 0,024 wt.% based on a mixture of olefins with up to eight carbon atoms, the mixture hydroformylation for three hours.
After cooling to room temperature, discharge pressure, unload the reaction mixture from the autoclave and deliver her from the cobalt catalyst by treatment with 5 %acetic acid and air at a temperature of 80°C. Receive 2731 g of a mixture of products hydroformylation, which according to gas chromatographic analysis are shown in table 1. In accordance with this achieved the degree of conversion of olefins with up to eight carbon atoms is 88.2 %, with selectivity for the target products is equal to 90,9%, which corresponds to the output of the target product, equal to 80.2 per cent, based on introduced in the reaction of the olefin with eight atoms ug is erode. The concept of target products and in this case refers to the aldehydes with nine carbon atoms, alcohols containing nine carbon atoms and (from)noninformation.
In order to assess the impact of the corresponding present invention is the recycling of olefins on the yield of target products, compare output olefin with up to eight carbon atoms (di-n-butene and reverse olefin with up to eight carbon atoms) with the yield, calculated on the quantity used fresh di-n-butene (2000). The output is based on di-n-butene is equal to 88%.
Compared with hydroformylation without recycle olefin (example for comparison) due to the recycling of olefins is achieved by increasing the yield of the target products by approximately 8%. In practice paraffins with eight carbon atoms and a portion of the olefins with up to eight carbon atoms removed from being implemented on a continuous process at the stage of selection.
The composition of mixtures of products hydroformylation
|The composition according to gas chromatography||An example of comparison, wt.%||Example, wt.% (without paraffin with the first stage of hydroformylation)|
In accordance with the implementation of the one-stage method, the yield of the target products can not be significantly increased by increasing the degree of conversion of di-n-butene, because increasing the degree of conversion leads to a decrease in selectivity due to the occurrence of successive transformations.
In contrast, corresponding to the invention makes it possible to work at high degrees of conversion of di-n-butene without reducing the selectivity of the target product.
1. The method of obtaining the highest oxaspiro from mixtures of isomeric olefins with the number of carbon atoms of from five to twenty-four by hydroformylation in the presence of a catalyst at elevated temperature and at elevated pressure, characterized in that hydroformylation carried out in one stage, limiting the degree of conversion of olefins in a single pass outside from 40-90%, the resulting reaction mixture, it is advisable after separation of the catalyst, is directed to selective hydrogenation, which is carried out at a temperature of 120-220°and pressure the Sri 5-30 bar, in the presence of a catalyst on a carrier containing as active ingredients copper, Nickel and chromium, the mixture of products of hydrogenation separated using distillation and return olefinic fraction on stage hydroformylation.
2. The method according to claim 1, characterized in that as starting products for hydroformylating a mixture of olefins with eight, nine, twelve or sixteen carbon atoms.
3. The method according to claim 1 or 2, characterized in that the use of catalyst on the carrier, containing as active ingredients copper and Nickel in a concentration of in each case from 0.3 to 15 wt.%, chromium in a concentration of from 0.05 to 3.5 wt.% and a component part of the alkali metal in a concentration of from 0.01 to 1.6 wt.% based in each case on the catalyst on the carrier.
4. The method according to claim 3, characterized in that the concentration of the component with the participation of the alkali metal is from 0.2 to 1.2 wt.%.
5. The method according to claim 3, characterized in that the catalyst on the carrier does not contain a component part of the alkali metal.
6. The method according to one of claims 1 to 5, characterized in that as the carrier for catalyst use silicon oxide or aluminum oxide.
7. The method according to one of claims 1 to 6, characterized in that the active components of the catalyst is homogeneous distributed in the pores of the material medium.
8. The method according to one of claims 1 to 6, trichosis fact, that the above-mentioned components of the catalyst is homogeneous distributed on the outer areas of the material medium.
9. The method according to one of claims 1 to 8, characterized in that the hydrogenation is carried out in liquid phase in a continuous or intermittent.
10. The method according to one of claims 1 to 9, characterized in that the total pressure is 15-25 bar.
11. The method according to one of claims 1 to 10, characterized in that the temperature is between 140-180°C.
12. The method according to one of claims 1 to 11, characterized in that the hydrogenation is carried out in the liquid phase with loads of liquid component from 5-100 m3per square meter of the cross-section of the empty reactor per hour.
13. The method according to item 12, characterized in that the load on the liquid phase ranges from 15-50 m3per square meter of the cross-section of the empty reactor per hour.
14. The method according to one of claims 1 to 13, characterized in that the mixture of products of hydrogenation separated using distillation and return olefins on stage hydroformylation.
15. The method according to 14, wherein the low-boiling components in the amount of 2-40% is removed from the recycle olefins.