RU2656601C1 - Method of obtaining synthetic oil - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: present invention relates to the method for the production of synthetic oil from the Fischer-Tropsch synthesis products, which comprises hydrogenating of the mixture of synthetic hydrocarbons in the fixed bed reactor of the nickel-containing catalyst in the hydrogenation gas stream, which comprises carbon monoxide and hydrogen. In this case, the fixed catalyst bed is filled with the mixture of synthetic hydrocarbons and heated up to the hydrogenation temperature before the hydrogenation gas is supplied, and after feeding the hydrogenation gas every 18–24 hours, the hydrogen gas volume velocity is reduced by 30–70 % for 1–3 hours, followed by reduction to the initial value, the ratio of hydrogen to carbon monoxide that is being maintained within 1.8…2.6, hydrogenation is carried out at the temperature of 210–260 °C, at the pressure of 10–50 atm, the hydrogen gas volume velocity is 10–1,000 h^-1, the volumetric flow rate of the mixture of synthetic hydrocarbons 1–10 h^-1, and the ratio of the volumetric flow rate of the mixture of synthetic hydrocarbons and the volumetric rate of the hydrogenation gas satisfies the following condition:

, where F(SH) is the volumetric flow of synthetic hydrocarbons, h^-1; ν – the volumetric velocity of the hydrogenation gas, h^-1; k is the proportion of olefins in the mixture of synthetic hydrocarbons, which are fed for their hydrogenation.

EFFECT: proposed method allows to achieve the degree of hydrogenation of olefins, which are contained in synthetic hydrocarbons, of at least 99 %, with the residual olefin content after hydrogenation of not more than 0_33 WT%.

1 cl, 1 tbl, 8 ex

Description

The invention relates to gas chemistry, and in particular to a technology for the hydrogenation of Fischer-Tropsch synthesis products.

Many companies are implementing compact mobile technologies for processing natural gas into synthetic hydrocarbons. The main advantage of such technologies is the possibility of their use in small and remote deposits of hydrocarbon resources. In particular, they are focused on the processing of associated petroleum gas, a significant proportion of which is burned at the fields, and the subsequent transportation of the resulting synthetic oil through the main pipeline system together with natural oil. The compact Fischer-Tropsch synthesis technology will increase utilization of associated gas and natural gas in small and remote fields, which will increase the profitability of their development.

и ROO вступать в реакции полимеризации и конденсации с образованием высокомолекулярных соединений, из которых формируются осадки. Присутствие непредельных соединений в смеси синтетической и природной нефти потенциально опасно для процессов их совместной транспортировки и хранения. В связи с этим перед смешиванием с природной нефтью целесообразно проводить гидрирование олефинов, содержащихся в смеси синтетических углеводородов, с получением синтетической нефти, содержащей не более 0,5 масс. %.The presence in the synthetic oil obtained in the Fischer-Tropsch process when it is implemented in a compact form, large quantities of olefins makes it more reactive and can affect its transportation, storage and processing in a mixture with natural oil. When atmospheric storage of natural oil occurs processes associated with the autooxidation of hydrocarbons, sulfur, nitrogen-containing compounds. These processes are catalyzed by transition metal complexes of vanadium, manganese, cobalt, and iron. The oxidation of hydrocarbons can lead to the formation of resins, the formation of precipitation. Unsaturated hydrocarbons that can be introduced with the products of the Fischer-Tropsch process are highly reactive compounds that, in the absence of oxygen, can polymerize to form high molecular weight compounds, and in the presence of oxygen, oxidize to form oxygen-containing compounds with high corrosion activity. The oxidation of unsaturated compounds has a number of features compared to the oxidation of limit compounds, but in general, oxidation proceeds through radical chain reactions with the formation of peroxide and oxide radicals. Multiple regenerated peroxide radicals undergo various transformations, including those leading to the formation of polyfunctional compounds capable of acting

and ROO enter into polymerization and condensation reactions to form high molecular weight compounds from which precipitates form. The presence of unsaturated compounds in a mixture of synthetic and natural oil is potentially dangerous for the processes of their joint transportation and storage. In this regard, before mixing with natural oil, it is advisable to hydrogenate olefins contained in a mixture of synthetic hydrocarbons, to obtain synthetic oil containing not more than 0.5 mass. %

Classical technologies for hydrogenation of olefins contained in synthetic hydrocarbons in a stream of hydrogen when carried out directly in the fields require the inclusion of an expensive and bulk hydrogen evolution unit in the GTL compact circuit, which will significantly increase the capital and operating costs of implementing the technology. It is advisable to use synthesis gas or exhaust gases of a Fischer-Tropsch synthesis reactor containing CO and H ₂ as well as inert impurities (nitrogen, methane, carbon dioxide, light hydrocarbon gases) as the hydrogenation gas. This makes it possible to exclude from the technological scheme for the production of synthetic oil, suitable for transportation and storage together with natural oil, from natural / associated petroleum gas, a hydrogen evolution unit and significantly reduce capital and operating costs.

A known method of implementing the process of hydrogenation of olefins contained in synthetic hydrocarbons of the process (~ 30 wt.%), Described in patent US 4478955, 10.23.1984. The hydrogenation process is carried out in the gas phase at temperatures of 150-450 ° C and a pressure of 17-340 atm. Hydrogenation catalysts based on nickel or copper chromites are preferably used. Hydrogenation is carried out in a stream of hydrogen.

The disadvantage of this method is the high volume ratio of hydrogen to hydrocarbon consumption (> 3000: 1), high hydrogen pressure and the need to use pure hydrogen in the implementation of this method, which will require an increase in capital costs for the construction of the separation unit when implementing a compact high-performance synthetic oil technology hydrogen directly in the field.

A known method of hydrotreating Fischer-Tropsch synthesis products to obtain a middle distillate is described in patent EP 2586851 A1, 05/01/2013. Hydrotreating of products is carried out in the presence of hydrogen and a hydrogenation catalyst at temperatures of 150-380 ° C and pressures of 10-90 atm, the volume ratio of hydrogen / feed is 150-1500 l / l, the volumetric flow rate of synthetic hydrocarbons is 0.2-5 h ^-1 . Fischer-Tropsch synthesis products mainly consist of n-paraffins (> 60 wt.%), The content of oxygen-containing substances and olefins in them is less than 10 and 20 wt. %, respectively. As a hydrotreatment catalyst, a commercial hydrogenation catalyst of 0.3% Pd / Al ₂ O ₃ (AXENS) is used. As a result of hydroprocessing under these conditions, the content of unsaturated and oxygen-containing compounds is reduced to less than 0.5 wt. %

The disadvantage of this method is the need to use pure hydrogen in its implementation, as well as the use of an expensive palladium-containing catalyst as a catalyst, the use of which is impossible when using a CO-containing gas as a hydrogenation gas due to the rapid deactivation of active palladium centers under the influence of CO.

A known method of hydrotreating olefins and oxygen-containing compounds in hydrocarbon feedstocks obtained by Fischer-Tropsch synthesis, described in patent EP 0583836 A1, 02.23.1994. The olefin content in the feed may be 5-30 wt. % Hydrocarbon products interact with hydrogen in the presence of a hydrogenation catalyst at a temperature of 175-250 ° C and a pressure of 10-50 atm. The volumetric flow rate of hydrogen consumption is 250-5000 h ^-1 , the mass flow rate of hydrocarbons is 0.25-2.5 kg / l / h, while the ratio of hydrogen to hydrocarbon feed is 250-3000 l / kg.

The disadvantage of this method is the high selectivity with respect to the side hydrocracking reaction (up to 20%) and the need to use pure hydrogen.

A known method of hydrogenation of olefins contained in a mixture of synthetic hydrocarbons in the presence of a palladium-containing catalyst, proposed in the patent CN 105771983, providing a degree of hydrogenation of more than 98% at a temperature of 110-220 ° C and a space velocity of 2000 - 5000 h ^-1 in a stream of industrial waste gases of the composition ( vol.%): ethylene - 0.2, СО - 27, acetylene - 0.02, СО ₂ - 5, О ₂ - 0.4, propylene - 0.2, butene - 0.1, the rest is hydrogen (N ₂ about 67).

The disadvantage of this method is the need to use for its implementation as a catalyst an expensive palladium-containing catalyst, the use of which when used as a hydrogenation gas of CO-containing gas at high space velocities (2000-5000 h ^-1 ) will lead to rapid deactivation of the active centers of palladium under the influence of CO and reducing the degree of hydrogenation of olefins contained in a mixture of synthetic hydrocarbons.

The closest technical solution to this invention is a method for the hydrogenation of olefins in a mixture of synthetic hydrocarbons in the presence of a nickel-containing catalyst, described in patent CN 102218323. The method consists in carrying out the process of hydrogenation of olefins in a mixture of synthetic hydrocarbons in a fixed-bed reactor under the following conditions: 1-4 MPa , 200-300 ° С, hydrogenation gas composition - СО 8.3-27.4%, Н ₂ 35.3-61.3%, СО ₂ 3.6-16.6%, СН ₄ 4.2-30 , 2%, 0.6% ethylene, 1.39% propylene, 0.6% butenes, the rest is nitrogen, with a space velocity of 1000-2000 h ^-1 . The degree of hydrogenation is more than 95%.

The disadvantage of the proposed hydrogenation method is the high volumetric rate of the hydrogenation gas, which, due to the presence of a high CO content therein, can lead to an intensification of the side reaction of CO methanation occurring in the presence of nickel and to uncontrolled heating of the reactor. Another disadvantage of this method is the insufficient degree of hydrogenation to ensure the content of olefins in synthetic oil is not more than 0.5 wt. % when the olefin content in the mixture of synthetic hydrocarbons is more than 10 wt. %

The technical task of this invention is to develop a method for producing synthetic oil from synthetic hydrocarbons containing olefins in the process of hydrogenation of olefins in a stream of gas containing CO and H ₂ .

The technical result from the implementation of this invention is to achieve a degree of hydrogenation of olefins contained in the composition of the synthetic hydrocarbons of the Fischer-Tropsch process, more than 99.0% in a stream of gas containing CO and H ₂ .

The technical result from the implementation of the claimed invention is achieved in that the hydrogenation of olefins contained in the composition of synthetic hydrocarbons in an amount of from 2 to 33 mass. %, is carried out in a reactor with a fixed bed of nickel-containing catalyst in a stream of hydrogenation gas comprising carbon monoxide and hydrogen, while the fixed bed of catalyst is filled with a mixture of synthetic hydrocarbons and heated to a temperature of hydrogenation before supplying a hydrogenation gas, and after supplying a hydrogenation gas every 18-24 hours the volumetric rate of the hydrogenation gas is reduced by 30-70% for 1-3 hours, followed by restoration to the initial value, in a gas stream containing CO and H ₂ , while the ratio of H ₂ / CO is about t 1.8 to 2.6. Hydrogenation gas may also contain up to 35 vol. % impurities, which may include CO ₂ , CH ₄ , N ₂ , light hydrocarbons C ₂ -C ₄ . Hydrogenation of olefins in a mixture of synthetic hydrocarbons according to this method is carried out at 210-260 ° C, a pressure of 10-50 atm, a volumetric rate of a hydrogenation gas of 10-1000 h ^-1 , a volumetric flow rate of a mixture of synthetic hydrocarbons 1-10 h ^-1 , while the ratio of volumetric the flow rate of the mixture of synthetic hydrocarbons and the space velocity of the hydrogenation gas satisfies the condition:

where P (SU) is the volumetric flow rate of synthetic hydrocarbons, h ^-1 ;

v is the space velocity of the hydrogenation gas, h ^-1 ;

k is the proportion of olefins in the mixture of synthetic hydrocarbons supplied to hydrogenation.

These distinguishing features are significant.

The implementation of the hydrogenation method of the proposed method provides a degree of hydrogenation of olefins of synthetic hydrocarbons in a gas stream containing CO and hydrogen, not less than 99.0% with a residual olefin content in the composition obtained after hydrogenation of synthetic oil not more than 0.33 mass. %

The implementation according to this invention of a method for producing synthetic oil from synthetic hydrocarbons containing olefins, in the process of hydrogenation of olefins in a stream of gas containing CO and hydrogen, is carried out in a reactor with a fixed bed of a nickel-containing catalyst, for example, containing 43% nickel and mesoporous alumina - the rest. The catalyst used in the implementation of the proposed method can be prepared, for example, by the method of repeated impregnation or coprecipitation. The fixed catalyst bed is filled with a mixture of synthetic hydrocarbons and heated to a hydrogenation temperature before the hydrogenation gas is supplied.

The method is carried out in a gas stream, which is either synthesis gas used in the Fischer-Tropsch synthesis stage, or the exhaust gases of a Fischer-Tropsch synthesis reactor containing CO and H ₂ , wherein the ratio of H ₂ / CO is from 1.8 to 2 , 6, as well as up to 35 vol. % impurities, which may include CO ₂ , CH ₄ , N ₂ , light hydrocarbons C ₂ -C ₄ . The use of such gases for the hydrogenation of olefins can reduce the capital and operating costs for the implementation of the synthetic oil production process chain, suitable for transportation and storage together with natural oil, from natural / associated petroleum gas, eliminating the hydrogen evolution unit from it. The gas volumetric velocity is from 10 to 1000 h ^-1 . Synthetic hydrocarbons obtained in the Fischer-Tropsch process may contain from 2 to 33 mass. % olefins and fed into the hydrogenation reactor with a volumetric flow rate of 1-10 h-1. After supplying the hydrogenation gas every 18-24 hours, the volumetric rate of the hydrogenation gas is reduced by 30-70% for 1-3 hours, followed by restoration to the original value. The temperature in the hydrogenation reactor is from 210 to 260 ° C, the pressure is from 10 to 50 atm. The implementation according to this invention a method of producing synthetic oil from synthetic hydrocarbons containing olefins, in the process of hydrogenation of olefins in a stream of gas containing CO and H ₂ , to achieve a degree of hydrogenation of olefins of more than 99% requires the following conditions:

,

,

where P (SU) is the volumetric flow rate of synthetic hydrocarbons, h ^-1 ;

v is the space velocity of the hydrogenation gas, h ^-1 ;

k is the proportion of olefins in the mixture of synthetic hydrocarbons supplied to hydrogenation.

The effectiveness of the method was evaluated by the residual content of olefins contained in a mixture of synthetic hydrocarbons leaving the hydrogenation reactor.

The calculation of the degree of hydrogenation of olefins contained in a mixture of synthetic hydrocarbons was carried out according to the following formula:

,

,

- массовое содержание олефинов в исходной смеси синтетических углеводородов, % масс.;Where

- mass content of olefins in the initial mixture of synthetic hydrocarbons,% mass .;

- массовое содержание олефинов в синтетической нефти (смеси гидрированных синтетических углеводородов), % масс.

- mass content of olefins in synthetic oil (a mixture of hydrogenated synthetic hydrocarbons),% of the mass.

The composition of the initial mixture of synthetic hydrocarbons and the mixture of synthetic hydrocarbons leaving the hydrogenation reactor can be determined by any known method, for example, gas chromatography.

The method is implemented in accordance with the following examples.

Example 1

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 1.2 h ^-1 mixture of synthetic hydrocarbons containing 24 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.2, with a space velocity of 800 h ^{- 1} at 15 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 220 ° C before supplying the hydrogenation gas, and after supplying the hydrogenation gas every 20 hours, the volumetric rate of the hydrogenation gas was reduced by 37.5% to 500 h ^-1 for 2 hours, followed by restoration to the original values of 800 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.0%, and the residual olefin content in the composition of synthetic oil was 0.24 mass. %

Example 2

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volumetric flow rate of 10 h ^-1 mixture of synthetic hydrocarbons containing 4 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.0, with a space velocity of 500 h ^{- 1} at 30 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 260 ° C before supplying the hydrogenation gas, and after supplying the hydrogenation gas every 21 hours, the volumetric rate of the hydrogenation gas was reduced by 40% to 300 h ^-1 for 1.5 hours, followed by restoration to the original values of 500 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 100%, and there was no residual olefin content in the composition of synthetic oil.

Example 3

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 1.0 h ^-1 mixture of synthetic hydrocarbons containing 33 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ CO ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 1.8, with a space velocity of 1000 h ^{- 1} at 10 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 210 ° C before the hydrogenation gas was supplied, and after the hydrogenation gas was supplied every 16 hours, the volumetric rate of the hydrogenation gas was reduced by 30% to 700 h ^-1 for 3 hours, followed by restoration to the initial value of 1000 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.3%, and the residual olefin content in the composition of synthetic oil was 0.33 mass. %

Example 4

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 8.0 h ^-1 mixture of synthetic hydrocarbons containing 2 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 1.8, with a space velocity of 300 h ^{- 1} at 25 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 230 ° C before supplying the hydrogenation gas, and after supplying the hydrogenation gas every 22 hours, the space velocity of the hydrogenation gas was reduced by 50% to 150 h ^-1 for 2.5 hours, followed by restoration to the original values of 300 h ^-1 .

The process of producing synthetic oil took place at a degree of hydrogenation of olefins of 99.9%, and the residual olefin content in the composition of synthetic oil was 0.02 mass. %

Example 5

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 4.0 h ^-1 mixture of synthetic hydrocarbons containing 27 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.0, with a space velocity of 10 h ^{- 1} at 50 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 250 ° C before the hydrogenation gas was supplied, and after the hydrogenation gas was fed every 24 hours, the volumetric rate of the hydrogenation gas was reduced by 60% to 4 h ^-1 for 1 h, followed by restoration to the initial value of 10 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.7%, and the residual olefin content in the composition of synthetic oil was 0.27 mass. %

Example 6

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 6.0 h ^-1 mixture of synthetic hydrocarbons containing 10 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.4, with a space velocity of 100 h ^{- 1} at 40 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 240 ° C before the hydrogenation gas was supplied, and after the hydrogenation gas was supplied every 18 hours, the volumetric rate of the hydrogenation gas was reduced by 55% to 45 h ^-1 for 1.0 h, followed by restoration to the original values of 100 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.8%, and the residual olefin content in the composition of synthetic oil was 0.10 mass. %

Example 7

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 3.0 h ^-1 mixture of synthetic hydrocarbons containing 20 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas including hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.6, with a space velocity of 50 h ^{- 1} at 20 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 220 ° C before the hydrogenation gas was supplied, and after the hydrogenation gas was fed every 20 hours, the volumetric rate of the hydrogenation gas was reduced by 70% to 15 h ^-1 for 3 hours, followed by restoration to the initial value of 50 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.5%, and the residual olefin content in the composition of synthetic oil was 0.20 mass. %

Example 8

Obtaining synthetic oil from Fischer-Tropsch synthesis products, representing a stream with a volume flow of 2.0 h ^-1 mixture of synthetic hydrocarbons containing 15 mass. % olefins, in the process of hydrogenation in a reactor with a fixed bed of nickel-containing catalyst 43% Ni / Al ₂ O ₃ , was carried out in a stream of hydrogenation gas comprising hydrogen and carbon monoxide in the ratio of H ₂ / CO = 2.0, with a space velocity of 650 h ^{- 1} at 35 atm. The fixed catalyst bed was filled with a mixture of synthetic hydrocarbons and heated to 240 ° C before the hydrogenation gas was supplied, and after the hydrogenation gas was fed every 22 hours, the volumetric rate of the hydrogenation gas was reduced by 45% to 292.5 h ^-1 for 1 h, followed by restoration to the initial one values of 650 h ^-1 .

The process of producing synthetic oil was carried out at a degree of hydrogenation of olefins of 99.6%, and the residual olefin content in the composition of synthetic oil was 0.15 mass. %

The conditions of the method for producing synthetic oil in the process of hydrogenation of synthetic hydrocarbons containing 2-33 mass. % olefins, in a stream of gas containing hydrogen and carbon monoxide in a ratio of H ₂ / CO from 1.8 to 2.6, and the results of the method according to the invention are presented in the table.

Proposed in this invention, the method allows to obtain synthetic oil with a content of not more than 0.33 mass. % olefins with a degree of hydrogenation of olefins contained in synthetic hydrocarbons, not less than 99.0%. The synthetic oil obtained according to this invention is suitable for mixing with mineral oil for joint transportation and storage.

The method of producing synthetic oil proposed in this invention is more effective than known in the art.

Claims (5)

A method of producing synthetic oil from Fischer-Tropsch synthesis products, comprising hydrogenating a mixture of synthetic hydrocarbons in a reactor with a fixed bed of nickel-containing catalyst in a stream of hydrogenation gas comprising carbon monoxide and hydrogen, characterized in that the fixed bed of catalyst is filled with a mixture of synthetic hydrocarbons and heated to a hydrogenation temperature before supplying the hydrogenation gas, and after supplying the hydrogenation gas every 18-24 hours, the space velocity of the hydrogenation gas is reduced by 30-70% for 1-3 hours, followed by restoration to the original value, while the ratio of hydrogen to carbon monoxide is maintained within 1.8 ... 2.6, and hydrogenation is carried out at a temperature of 210-260 ° C, a pressure of 10-50 atm, gas volumetric velocity hydrogenation of 10-1000 h ^-1 , the volumetric flow rate of the mixture of synthetic hydrocarbons 1-10 h ^-1 , and the ratio of the volumetric flow rate of the mixture of synthetic hydrocarbons and the volumetric velocity of the hydrogenation gas satisfies the condition

where P (SU) is the volumetric flow rate of synthetic hydrocarbons, h ^-1 ; ν is the space velocity of the hydrogenation gas, h ^-1 ; k is the proportion of olefins in the mixture of synthetic hydrocarbons supplied to hydrogenation.