RU2607902C1 - Method of increasing stability of oxygen-containing components of motor fuel and controlling oxygen content therein - Google Patents

Abstract

FIELD: fuel.

SUBSTANCE: invention describes a method of controlling content of oxygen in high-octane component of motor fuel based on carbonyl compounds of general formula, where R¹ is H, or alkoxide -O-C_nH_2n+1, or a hydrocarbon radical of general formula -C_nH_2n+1; R² is a hydrocarbon radical of general formula -C_nH_2n+1; n is a number from 1 to 5 or mixture thereof, and controlling chemical stability of this component consists in that, carbonyl compounds of said general formula or mixture thereof in gaseous phase in excess hydrogen are passed over a layer of composite material, consisting of a mechanical mixture of a hydrogenation catalyst and a dehydration catalyst, at temperature of 100–400 °C and pressure of 1–100 atm.

EFFECT: technical result consists in increasing activity, selectivity and stability of operation of catalysts for hydrogenation of branched ketones to corresponding branched alkanes, and/or alcohols and/or their mixtures.

8 cl, 1 tbl, 28 ex

Description

The invention relates to a method for increasing the chemical stability of motor fuel components and controlling the oxygen content therein in order to improve the quality of the resulting fuel compositions.

Recently, the range of proposed oxygen-containing high-octane additives is expanding. This is partly due to the ban on the use of methyl tert-butyl ether in the United States and the restriction on its use in Western Europe. Bioethanol and components of fuel of plant origin are playing an increasingly important role in the quality of fuel [EP 2298851, US 20060199970, CA 2530219]. As new high-octane gasoline components, carbonyl compounds are also offered [Tarabanko V.E. et al. New high-octane gasoline components from plant materials. // Journal of Siberian Federal University. Chemistry. - 2014 .-- Vol. 1. - No 7. - p. 31-35]. The branched carbonyl compounds of the branched structure are characterized by high antiknock properties. Most carbonyl compounds with carbon numbers from 3 to 9 have an octane rating above 100 IOIs. However, the disadvantage of carbonyl compounds is their relatively high reactivity. Thus, a number of carbonyl compounds, primarily aldehydes, are highly active in aldol condensation reactions, contributing to the formation of resins. The conversion of carbonyl compounds to more stable alcohols should help increase the chemical stability of gasolines.

On the other hand, it should be noted that the oxygen content in the fuel is regulated. According to the technical regulations of the customs union, the oxygen content in gasoline should not exceed 2.7 wt. % However, it is far from always the addition of an oxygen-containing high-octane component to the fuel within the indicated limits that makes it possible to obtain the necessary antiknock effect. In this regard, the problem arises of reducing the oxygen content in the high-octane component while maintaining its antiknock properties. The oxygen content can be reduced by converting methyl substituted carbonyl compounds into the corresponding branched hydrocarbons.

The present invention provides a smooth control of the oxygen content in the components of motor fuel, as well as increasing their chemical stability by hydrogenation of carbonyl compounds.

A number of catalysts are known that carry out the process of hydrogenation of carbonyl compounds mainly into alcohols. However, these catalysts have a number of serious disadvantages. Thus, the Ni / Al ₂ O ₃ and Ni-Cu / Al ₂ O ₃ catalyst (Tetrahedron Lett., 22, 4227 (1981), Journal of Catalysis 85, 25-30 (1984)) has reduced activity with respect to branched and spatially difficult ketones for hydrogenation. Other commonly used supported metal sulfide-based catalysts require stringent reaction conditions (T≥300 ° C, P≥100 atm) (Journal of Catalysis 90, 147-149 (1984)).

In the work [Jenck J., Germain J.-E. High-pressure competitive hydrogenation of ketones on copper chromite catalyst // J. Catal. - 1980. - Vol. 65, N1. - P 133-140] studied the hydrogenation of a wide range of carbonyl compounds into the corresponding alcohols. It was shown that during hydrogenation of carbonyl compounds in the gas phase in the temperature range of 150-220 ° C at a pressure of 20-100 atm on the copper-chromium catalyst, no side reactions (for example, aldol condensation) are observed. The relative activity of ketones in binary and ternary mixtures was investigated. Both cyclic and acyclic ketones, in particular diisopropyl ketone, were used. It was shown that diisopropyl ketone is one of the least active ketones in the series of 19 investigated substrates. For hydrogenation of diisopropyl ketone to the corresponding alcohol, EP 0227250 proposes a highly selective Ru catalyst that effectively conducts the reaction only in the liquid phase. A large number of patents are devoted to the synthesis of highly active catalysts based on copper chromite and copper oxide on various supports (RU 2050198, RU 2050197, RU 2050195, RU 2052446, RU 2183210, WO 2006053735, US 2008103333, US 2008064883, US 2004082821, US 6448457), modified transitional and alkaline earth metals from a wide range of these compounds. The disadvantages of such catalysts are their complex composition, which makes their synthesis and operation a low-tech method, the difficulty in controlling the ratio of alcohol and alkane, the main products of hydrogenation of carbonyl compounds.

GB 2142010 A, C07C 29/14, 1985 describes a two-stage process for the hydrogenation of aldehydes containing from 6 to 20 carbon atoms. The first reactor contained a MoS ₂ / C catalyst, and the second Ni / Al ₂ O ₃ . The reaction temperature was 180-260 ° C, the partial pressure was 150-210 atm. The aim of this invention was to obtain alcohols, therefore, water was added to the reaction mixture to suppress the formation of alkanes.

In the last decade, processes have been developed using biomass as a raw material for the production of motor fuels. The products of primary biomass processing contain carbonyl compounds, in particular acetone. The latter, by aldol condensation, is converted to methyl isobutyl ketone (MIBK), which, in turn, can be converted to 2-methylpentane by hydrogenation with hydrogen. To date, an approach has been proposed to increase the selectivity for the corresponding hydrocarbon using bifunctional catalysts containing metals with a hydrogenating function introduced into a carrier having a dehydrating effect.

Examples of the use of platinum catalysts are known, the basis of which are modified heteropoly acids or zeolites with the structure of MFI, BEA and Y [M.A. Alotaibi, EF Kozhevnikova, IV Kozhevnikova Hydrogenation of methyl isobutyl ketone over bifunctional Pt-zeolite catalyst // J. Catal, 2012, v. 293, p. 141; K. Alharbi, EF Kozhevnikova, IV Kozhevnikov. Hydrogenation of ketones over bifunctional Pt-heteropoly acid acid catalyst in the gas phase. Stabilization of Ni / Al ₂ O ₃ catalyst by Cu addition for CO ₂ reforming of methane. // Applied Catalysis A: Gen. - 2014, https://dx.doi.org/10.1016/j.apcata.2014.10.032]. It was shown that high selectivity for hydrocarbons (99%) is achieved by gas-phase reaction at 200 ° C and atmospheric pressure on a zeolite of 0.3% Pt / ZSM-5. The need to maintain the dehydrating function of the carrier, especially zeolites, requires the introduction of a small amount of metal. It is known that only noble metals can provide high activity of the hydrogenation catalyst when their content is at the level of 0.5-2 wt. % Patent RU 2050190 proposes a method for the synthesis of a low-percentage nickel catalyst modified with heteropoly compounds of various compositions for hydrogenation processes, including carbonyl compounds. The activity of such a catalyst can be flexibly controlled by changing the nature of the heteropoly compound or the metal / GPS ratio. The disadvantages of the catalyst include the complexity of the synthesis of GPS and the low stability of their salts.

The present invention proposes to use to control the chemical stability of the high-octane component and the oxygen content in it, a composite, which is a mechanical mixture of a hydrogenation catalyst for a carbonyl compound and a dehydration catalyst for the resulting alcohol. This approach allows us to separate the hydrogenating and dehydrating functions of the branched ketone hydrogenation catalyst and to use relatively cheap copper and nickel-based hydrogenation catalysts. When trying to combine these two functions in one catalyst (fixing the corresponding catalytically active metals on one carrier), it can be expected that a high concentration of the hydrogenating active component will inevitably negatively affect its dehydrating function of the catalyst and vice versa. In this invention, we propose the use of copper and nickel-containing catalysts with a nickel content of from 10 to 50 wt. % As a carrier, a number of known catalyst support oxides can be used. Thus, it is proposed to use, including, and any industrial hydrogenation catalyst. As a dehydrating component of the composite, it is proposed to use any heterogeneous acidic catalyst, preferably zeolites. The best result is achieved when using zeolite in the H-form of any structure selected from the series: MFI, Y, BEA, FER, MTT, TON. The use of zeolites unmodified by hydrogenating metal makes it easy to control the ratio between the hydrogenating and dehydrating functions of the composite both by changing the zeolite content in the composite and varying the concentration and strength of its acid centers due to the use of zeolites of different chemical composition and structure. In the end, this allows you to adjust the ratio of alcohol and hydrocarbon in the final reaction mixture, directing the process either in the direction of the predominant formation of alcohol, or the predominant formation of a saturated hydrocarbon.

Closest to our invention can be considered the content of Pat. US No. 8048290, C10G 69/04, 01/01/2011, dedicated to the process of obtaining base oil from non-oil raw materials. One of the stages of this process is the hydro-functionalization reaction with the simultaneous isomerization of oxygen-containing raw materials in order to obtain branched hydrocarbons. The reaction is carried out on bifunctional catalysts, the basis of which is a molecular sieve selected from zeolites or silicoaluminophosphates, with an introduced metal with a hydrogenating function selected from metals of groups 8-10 of the Periodic system. The authors specifically note that, along with the hydrogenation of carbonyl compounds, this catalyst conducts the processes of isomerization and cracking of the resulting hydrocarbons, while the formation of light hydrocarbons C ₁ -C ₄ in significant quantities - from 4 to 30 wt. % The fact of a significant decrease in the yield of higher branched hydrocarbons greatly reduces the practical value of this patent. The disadvantage of such bifunctional catalysts is the fact that it is difficult to predict the relationship between the hydrogenating and isomerizing functions in the catalysts in advance, therefore, any change in the properties of the molecular sieve used entails a special selection of the nature of the hydrogenating component, the transition metal, and also its amount in the catalyst.

The main difference of our approach is the possibility of minimizing the processes of isomerization and cracking of methyl substituted branched alkanes by varying the simple ratio of the loadings of the hydrogenation catalyst with the known catalytic properties and unmodified zeolite in the H form, the dehydrating activity of which is also fixed.

The invention solves the problem of increasing the efficiency of the process of selective hydrogenation of branched ketones to the corresponding hydrocarbons or mixtures thereof with alcohols.

EFFECT: increased activity, selectivity and stability of operation of branched ketone hydrogenation catalysts to corresponding branched alkanes and / or alcohols and / or mixtures thereof.

The problem is solved by controlling the oxygen content in a high-octane component of motor fuel based on carbonyl compounds and controlling the chemical stability of this fuel component, in which the conversion of carbonyl compounds is carried out in the gas phase in excess of hydrogen by passing the reaction mixture over a layer of a composite consisting of a mechanical mixture of a hydrogenation catalyst and dehydration catalyst, at a temperature of 100-400 ° C and a pressure of 1-100 atm.

During the conversion, carbonyl compounds are converted into a mixture of carbonyl compound, alcohol and hydrocarbon, the ratio between the carbonyl compound, alcohol and hydrocarbon is controlled by changing the ratio of the hydrogenation catalyst and the dehydration catalyst from 0.01 to 100.

As a raw material for obtaining a stable high-octane component, a carbonyl compound of the general formula is used

where R ¹ is H or an alkoxide —OC _n H _{2n + 1;} or a hydrocarbon radical of the general formula —C _n H _{2n + 1} ;

R ² is a hydrocarbon radical of the general formula —C _n H _{2n + 1} ;

n is a number from 1 to 5.

As a raw material for obtaining a stable high-octane component, a mixture of carbonyl compounds of the general formula is also used:

where: R ¹ is H, alkoxide —OC _n H _{2n + 1} , or a hydrocarbon radical of the general formula —C _n H _{2n + 1} ;

R ² is a hydrocarbon radical of the general formula —C _n H _{2n + 1} ;

n is a number from 1 to 5.

The carbonyl compounds of the high octane component are completely converted to the corresponding alcohols or completely converted to the corresponding hydrocarbons.

As the hydrogenation catalyst, a metal selected from the series Pt, Pd, Ru, Au, Ni, Cu, which can be deposited on a support, is used.

As the active component of the hydrogenation catalyst, Pt and / or Pd and / or Ru and / or Au and / or Ni and / or Cu are used.

As the carrier, aluminum oxides and / or silicon oxides and / or carbon can be used.

As a dehydration catalyst, a cation exchange resin in the H-form and / or phosphoric and / or sulfuric acid and / or zeolite are used.

As a dehydrating component of the composite, zeolite in the H-form of a structure selected from the series MFI, MEL, BEA, MTT, TON, Y, FER is used.

The invention is illustrated by the following examples.

Example 1. Comparative

70 ml / min of a mixture of diisopropyl ketone (10 vol.%) And hydrogen (80 vol.%) In argon (10 vol.%) Is passed through a catalyst bed (1 g) at a temperature of 160 ° C for 10 hours. As a catalyst, use the catalyst is 15 wt. % Ni on γ-Al ₂ O ₃ . The composition of the reaction mixture was determined by sampling directly from a gas-vapor stream, followed by analysis of organic components on a flame ionization detector, inorganic components on two heat conductivity detectors. The organic components of the reaction mixture were separated on a DB 1701 capillary column. The resulting mixture contains unreacted hydrogen and diisopropyl ketone, diisopropyl alcohol, 2,4-dimethylpentane, 2,3-dimethylpentane, etc.

The conversion (X _K ) of ketone (diisopropyl ketone) in percent, taking into account changes in the volume of the reaction mixture, was calculated by the formula

,

,

и С_К - мольные доли кетона в исходной и конечной реакционной смеси соответственно, β - коэффициент изменения объема в ходе протекания реакции, который рассчитывали по формулеWhere

and С _К are the molar fractions of ketone in the initial and final reaction mixture, respectively, β is the coefficient of volume change during the course of the reaction, which was calculated by the formula

- мольная доля аргона в исходной реакционной смеси, %; C_Ar - мольная доля аргона в конечной реакционной смеси), отн. ед.Where:

- molar fraction of argon in the initial reaction mixture,%; C _Ar is the molar fraction of argon in the final reaction mixture), rel. units

The productivity (Pr) of the catalyst according to alkane (2,4-dimethylpentane) or alcohol (diisopropylcarbinol) in kg (product) / kg (cat.) H was calculated by the formula

,

,

where β is the coefficient of volume change during the course of the reaction, calculated by the above formula, rel. units;

C _product is the molar fraction of the product (2,4-dimethylpentane or diisopropylcarbinol) in the final reaction mixture,%;

F is the volumetric flow rate of the reaction mixture, cm ³ / s;

m - sample of catalyst, g.

The selectivity (S) for the formation of alkane (2,4-dimethylpentane) or alcohol (diisopropylcarbinol) from ketone (diisopropyl ketone) in percent was calculated by the formula

,

,

where β is the coefficient of volume change as a result of the reaction, calculated by the above formula, rel. units;

C _product and C _ketone are the mole fractions of the product (2,4-dimethylpentane or diisopropylcarbinol) and the initial ketone (diisopropyl ketone), respectively, in the reaction mixture at the outlet of the reactor,%.

The results are presented in the table.

The composition of the composite, the conversion conditions, the conversion of the ketone, the selectivity of the conversion of the ketone to the corresponding alcohol and alkane, as well as by-products of isomerization, demethylation, cracking, condensation are given here. It can be seen that the conversion of the ketone on the nickel catalyst is 58%. The main conversion product on the nickel catalyst is alcohol, which is formed with a selectivity of 94 mol. %, followed by by-products, which are mainly represented by methylhexanes, 2,4-dimethylpentene, cracking and condensation products. Alkane (2,4-dimethylpentane is formed with a selectivity of only 1 mol.%.

Example 2. Comparative

The reaction is carried out analogously to example 1, with the difference that instead of a nickel catalyst, 0.5 wt. % Pd / Al ₂ O ₃ and the experiment is carried out at a temperature of 180 ° C. In this case, the conversion of ketone is reduced to 10%, and the ratio between alcohol and ketone in the products is significantly reduced.

Example 3. Comparative

The reaction is carried out analogously to example 1, with the difference that instead of a nickel catalyst, 0.5 wt. % Pt / C and the experiment is carried out at a temperature of 180 ° C. In this case, the conversion of ketone is reduced to 10%, and the ratio between alcohol and ketone in the products is significantly reduced.

Example 4. Comparative

The reaction is carried out analogously to example 1, with the difference that instead of a nickel catalyst, zeolite (1 g) with an MFI structure is loaded into the reactor. In this case, the conversion of ketone is reduced to 3% and the main product is the condensation products of ketone.

Example 5

The reaction is carried out analogously to example 1, with the difference that instead of a nickel catalyst, a composite is loaded into the reactor - a mechanical mixture of a nickel catalyst (1 g) with a zeolite with an MFI structure (1 g). It is seen that the replacement of the nickel catalyst with a composite leads to an increase in the conversion of the initial ketone, and alkane (2,4-dimethylpentane) is formed as the main product.

Example 6

The reaction is carried out analogously to example 5, with the difference that instead of the MFI zeolite, a zeolite with an MTT structure is used. Replacing zeolite leads to a decrease in the formation of by-products by 2%, mainly due to a decrease in the formation of methylhexanes.

Example 7

The reaction is carried out analogously to example 5, with the difference that instead of the MFI zeolite, a zeolite with a FER structure is used. Replacing the zeolite leads to a slight decrease in conversion, the appearance of traces of alcohol (diisopropyl ketone) in the reaction mixture and an increase in selectivity for by-products by 1 mol. %

Example 8

The reaction is carried out analogously to example 5, with the difference that instead of the zeolite MFI use a zeolite with a TON structure. In a first approximation, the results coincide with the results of example 3, if you do not take into account the decrease of 1% selectivity for by-products.

Example 9

The reaction is carried out analogously to example 5, with the difference that instead of using MFI zeolite, a zeolite with a Y structure is used. Zeolite replacement is accompanied by a slight increase in ketone conversion, but the selectivity for alkane (2,4-dimethylpropane) decreases due to an increase in selectivity for by-products.

Example 10

The reaction is carried out analogously to example 5, with the difference that the process is conducted at a pressure of 5 atm. It can be seen that an increase in pressure is accompanied by an increase in conversion and an increase of 1% in selectivity for alkane due to a decrease in selectivity for by-products.

Example 11

The reaction is carried out analogously to example 5, with the difference that the process is conducted at a pressure of 20 atm. It can be seen that an increase in pressure is accompanied by an increase in conversion and an increase of 2% in selectivity for alkane due to a decrease in selectivity for by-products.

Example 12

The reaction is carried out analogously to example 5, with the difference that the process is carried out at a temperature of 200 ° C. It can be seen that an increase in temperature leads to a slight increase in conversion, but a significant increase in the contribution of adverse reactions is observed. Thus, the selectivity of the conversion of diisopropyl ketone to dimethyl pentanes decreases from 94% to 70%.

Example 13

The reaction is carried out analogously to example 5, with the difference that instead of the MFI zeolite, a cationic exchange resin in the A-form Amberlyst 36 is used and the process is carried out at a temperature of 140 ° C. It can be seen that this leads to a decrease in conversion. Alcohol appears in the products and selectivity for alkane is significantly reduced due to an increase in selectivity for by-products.

Example 14

The reaction is carried out analogously to example 5, with the difference that instead of using MFI zeolite, a catalyst based on perfluorinated sulfocationionite 30% Nafion / SiO _{2 is used} . It is seen that the replacement of zeolite with sulfocationionite leads to a slight increase in the conversion of diopropyl ketone, which may indicate an increase in the rate of the process.

Example 15

The reaction is carried out analogously to example 5, with the difference that instead of the MFI zeolite, a sulfuric acid dehydration catalyst H ₂ SO ₄ / SiO _{2 is used} . It is seen that the replacement of zeolite with a sulfuric acid catalyst leads to a decrease in the conversion of diopropyl ketone and an increase in selectivity for by-products.

Example 16

The reaction is carried out analogously to example 5, with the difference that instead of the Ni / Al ₂ O ₃ catalyst, a Cu-Ni / SiO ₂ catalyst is used. It is seen that the conversion of ketone decreases and alcohol appears in the reaction products, due to which alkane selectivity decreases.

Example 17

The reaction is carried out analogously to example 2, with the difference that instead of a nickel catalyst, a composite is loaded into the reactor — a mechanical mixture of a hydrogenation catalyst 0.5% Pd / Al ₂ O ₃ (1 g) with a zeolite with an MFI structure (1 g). It can be seen that the replacement of the palladium catalyst with a composite leads to an increase in the conversion of the initial ketone with an increase in the proportion of alkane (2,4-dimethylpentane) in the reaction products.

Example 18

The reaction is carried out analogously to example 2, with the difference that instead of a nickel catalyst, a composite is loaded into the reactor - a mechanical mixture of a hydrogenation catalyst 1% Pt / C (1 g) with a zeolite with an MFI structure (1 g). It can be seen that the replacement of the platinum catalyst with a composite leads to an increase in the conversion of the initial ketone with an increase in the proportion of alkane (2,4-dimethylpentane) in the reaction products.

Example 19

The reaction is carried out analogously to example 5, with the difference that the loading of MFI zeolite is reduced to 0.4 g. A decrease in the zeolite content in the composite layer leads to a decrease in ketone conversion, the appearance of alcohol in the reaction mixture and a decrease in alkane selectivity. The decrease in alkane selectivity is mainly due to the formation of by-products.

Example 20

The reaction is carried out analogously to example 5, with the difference that the loading of MFI zeolite is reduced to 0.2 g. A further decrease in the zeolite content in the composite layer leads to an increase in the reduction of ketone conversion, an increase in the concentration of alcohol in the reaction mixture and a further decrease in alkane selectivity. It should be noted that the decrease in alkane conversion and selectivity varies disproportionately with the decrease in the zeolite content in the composite.

Example 21. Comparative

The reaction is carried out analogously to example 1, with the difference that 2-methyl-butanal is used as the starting material instead of diisopropyl ketone and the experiment is carried out at a temperature of 130 ° C. An incomplete conversion of the starting 2-methyl-butanal is observed, and the corresponding alcohol is formed as the main product.

Example 22. Comparative

The reaction is carried out analogously to example 21, with the difference that instead of a nickel catalyst, a dehydration catalyst, a zeolite with an MTT structure, is loaded into the reactor. Replacing the nickel catalyst with zeolite leads to a significant reduction in conversion and the predominant formation of by-products of condensation of 2-methyl-butanal.

Example 23

The reaction is carried out analogously to example 21, with the difference that instead of a nickel catalyst, a composite is loaded into the reactor - a mechanical mixture of a nickel catalyst (1 g) with a zeolite with an MTT structure (1 g). It is seen that replacing the nickel catalyst with a composite leads to an increase in the conversion of the starting aldehyde, with alkane (2-methyl-butane) being formed as the main product.

Example 24. Comparative

The reaction is carried out analogously to example 1, with the difference that 3-methyl-2-butanone is used as the starting material instead of diisopropyl ketone and the experiment is carried out at a temperature of 130 ° C. An incomplete conversion of the starting 3-methyl-2-butanone is observed, and the corresponding alcohol is formed as the main product.

Example 25. Comparative

The reaction is carried out analogously to example 24, with the difference that instead of a nickel catalyst, a dehydration catalyst, a zeolite with an MTT structure, is loaded into the reactor. Replacing the nickel catalyst with zeolite leads to a significant reduction in conversion and the predominant formation of by-products of the condensation of 3-methyl-2-butanone.

Example 26

The reaction is carried out analogously to example 25, with the difference that instead of a nickel catalyst, a composite is loaded into the reactor - a mechanical mixture of a nickel catalyst (1 g) with a zeolite with an MTT structure (1 g). It is seen that the replacement of the nickel catalyst with a composite leads to an increase in the conversion of the initial ketone, and alkane (2-methyl-butane) is formed as the main product.

Example 27

The reaction is carried out analogously to example 6, with the difference that instead of diisopropyl ketone, a mixture of 3-methyl-2-butanone (4 vol.%), 2-methyl-butanal (4 vol.%) And diisopropyl ketone (2 vol. %). The experiment is carried out at a temperature of 140 ° C. There is an incomplete conversion of reagents. The highest level of conversion among the components of the reaction mixture is observed for 2-methyl-butanal. The main reaction products are the corresponding alkanes.

Example 28

The reaction is carried out analogously to example 5, with the difference that 3-methylbutanoic acid ethyl ester is used as the starting material instead of diisopropyl ketone. The experiment is carried out at a temperature of 250 ° C and a pressure of 30 atm. There is an incomplete conversion of ether with the predominant formation of alcohols.

Claims (14)

1. The method of controlling the oxygen content in the high-octane component of motor fuel based on carbonyl compounds of the General formula

where R ¹ is H, either an alkoxide —OC _n H _{2n + 1} , or a hydrocarbon radical of the general formula —C _n H _{2n + 1} ; R ² is a hydrocarbon radical of the general formula —C _n H _{2n + 1} ; n is a number from 1 to 5; or mixtures thereof, and regulating the chemical stability of this fuel component, namely, that the carbonyl compounds of the above general formula or their mixture in the gas phase in excess of hydrogen is passed over a layer of a composite consisting of a mechanical mixture of a hydrogenation catalyst and a dehydration catalyst at a temperature of 100-400 ° C and a pressure of 1-100 atm. 2. The method according to p. 1, characterized in that during the conversion of the carbonyl compounds are converted into a mixture of carbonyl compounds, alcohols and hydrocarbons, and the ratio between them is regulated by changing the ratio of the hydrogenation catalyst and the dehydration catalyst from 0.01 to 100. 3. The method according to p. 1, characterized in that as the hydrogenation catalyst use a metal selected from the series Pt, Pd, Ru, Au, Ni, Cu. 4. The method according to p. 1, characterized in that as the active component of the hydrogenation catalyst using Pt, and / or Pd, and / or Ru, and / or Au, and / or Ni, and / or Cu. 5. The method according to p. 4, characterized in that the metal is applied to the carrier. 6. The method according to p. 5, characterized in that as a carrier use aluminum oxides and / or silicon oxides and / or carbon. 7. The method according to p. 1, characterized in that the cation exchange resin in the H-form and / or phosphoric and / or sulfuric acid and / or zeolite are used as a dehydration catalyst. 8. The method according to p. 1, characterized in that the zeolite in the H-form of a structure selected from the series MFI, MEL, BEA, MTT, TON, FER, Y is used as a dehydration catalyst in the composite.