RU2458101C1 - Method of producing condensed aviation fuel (versions) - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing condensed aviation fuel, involving extraction from hydrocarbon material through preparation and fractionation of a mixture of paraffin hydrocarbons of general formula C_nH_2n+2, containing a C₃-C₈ paraffin fraction as the paraffin hydrocarbons. The hydrocarbon material used is associated petroleum gas or natural gas, from which the mixture of paraffin hydrocarbons is extracted, which additionally contains a C₉-C₁₂ fraction, with the following content of components in wt %: C₃H₈ - 0.1-12.0; ΣC₄H₁₀ - 24.0-72.0; ΣC₅H₁₂ - 4.0-36.0; ΣC₆H₁₄ - 0.3-14.0; ΣC₇H₁₆ - 0.1-9.0; ΣC₈H₁₈ - 0.01-3.0; ΣC₉H₂₀ - C₁₂H₂₆ - the rest up to 100%. Total content of aromatic and petroleum hydrocarbons is not more than 6.0 wt %, and pressure of saturated vapour of the mixture is as follows, MPa (kgf/cm, abs): at 20°C - not higher than 0.26 (2.6); at 45°C - not higher than 0.50 (5.0). The invention also relates to a version of the method of producing condensed aviation fuel.

EFFECT: wide range of aviation fuel obtained from hydrocarbon material, simple technique of producing condensed aviation fuel.

2 cl, 9 tbl, 6 ex

Description

The invention relates to processes for the production of motor fuels, mainly aviation, used in gas turbine engines, and intended for use mainly in places of production and processing of hydrocarbon raw materials.

A known method for producing aviation condensed fuel for gas turbine engines based on a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} -H-decanes and N-dodecans in an amount of at least 45 mass. aromatic hydrocarbons of the General formula C _n H _2n-6 in an amount of 12-16 mass. olefinic hydrocarbons of the general formula C _n H _{2n the} rest (US Patent No. 3985638, CL 208-15, 1976).

Common signs are:

- the selection of a mixture of paraffin hydrocarbons of the General formula C _n H _{2n + 2} .

The disadvantage of this method is that the resulting fuel has a high pour point (from -29 to -45 ° C), which complicates its use in the Far North, a significant tendency to smoke, increasing the content of toxic substances in the exhaust products of combustion, a rather complicated technology for obtaining as well as limited resources for obtaining this fuel.

The closest technical solution to the proposed method according to both options in terms of technical essence and the achieved result is a known method for producing aviation condensed fuel (ASKT) for gas turbine engines based on a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} containing paraffin fraction as paraffin hydrocarbons C ₃ -C ₈ in the following ratio of components, wt. propane C ₃ H ₈ - 6-10, n butane C ₄ H ₁₀ - 13-22, isobutane C ₄ H ₁₀ - 34-48, n. pentane C ₅ H ₁₂ - 10-12, isopentane C ₅ H ₁₂ - 10-15, hexanes C ₆ H ₁₄ - 5-11, heptanes C ₇ H ₁₆ - 0.8-5.0, octanes C ₈ H _{18+ higher} - 0.4-2.1. ASKT is obtained by a known method from hydrocarbon raw materials - a wide fraction of light hydrocarbons (BFLH) produced at a gas processing plant, for example, by low-temperature distillation under a pressure of 30-35 kgf / cm ² , while BFLW is prepared by throttling to a pressure of 17 kgf / cm ² and at a temperature of 78-80 ° C, and then fractionated in a distillation column. The top product from the distillation column is cooled to a temperature of 35 ° C and sent to a reflux tank, from which part of the product is propane-butane fraction (PBP) is fed to the column, and the other part is taken as automobile fuel, household liquefied gas or raw materials for petrochemicals or pumped into the bulk of NGL, not subjected to distillation. The lower product aviation fuel is cooled from 93 ° C to 35 ° C and served in the fleet as a finished product (ASKT) (RF Patent No. 2044032, IPC 6 C10L 1/04).

Common features of the known and proposed method according to the first embodiment are:

- the selection of hydrocarbons from the preparation and fractionation of a mixture of paraffin hydrocarbons;

- the general formula of a mixture of paraffin hydrocarbons C _n H _{2n + 2} ;

- as a paraffin hydrocarbon mixture contains a paraffin fraction C ₃ -C ₈ .

Common features of the known and proposed method according to the second embodiment are:

- the selection of hydrocarbons from the preparation and fractionation of a mixture of paraffin hydrocarbons;

- the general formula of a mixture of paraffin hydrocarbons C _n H _{2n + 2} .

The known method in comparison with the proposed method for both options has several disadvantages:

- A narrow range of use of raw materials for producing ASKT, since in the known method ASKT is obtained only from BFLH, excluding the possibility of using other hydrocarbon raw materials, the use of non-waste technology, which reduces the manufacturability and economy of the method, reduces the range of opportunities for expanding the production of facilities for the preparation and processing of hydrocarbon raw materials .

- The limitation of the propane content of 6-10% also does not allow to expand the range of raw materials used and reduces the manufacturability of ASKT.

- The limitation of the composition of the HFCS produced by the C ₃ -C ₈ hydrocarbon fraction often does not allow the use of BFLH, which is released during the processing of oil and natural gas, as well as in the stabilization of oil and products of secondary oil refining processes at refineries, as used in In the method, the feedstock initially has hydrocarbons up to C ₁₂ .

The technical result of the invention is the expansion of the range of aviation fuel derived from hydrocarbon raw materials, with the expansion of the raw material base and the possibility of using the method at various facilities for the preparation and processing of hydrocarbon raw materials, as well as the simplification of the production technology of aviation condensed fuel.

This result is achieved by the fact that, according to the first embodiment, in the method for producing aviation condensed fuel, which comprises separating from a hydrocarbon feedstock by preparing and fractionating a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} containing paraffin fraction C ₃ -C ₈ as paraffin hydrocarbons, new is the fact that as a hydrocarbon feedstock using associated gas or natural gas, the recovered mixture of paraffinic hydrocarbons, further comprising a C ₉ -C ₁₂ fraction at trace yuschem Component Content,% wt .:

C ₃ H ₈ - 0.1-12.0

ΣC ₄ H ₁₀ - 24.0-72.0

ΣC ₅ H ₁₂ - 4.0-36.0

ΣC ₆ H ₁₄ - 0.3-14.0

ΣC ₇ H ₁₆ - 0.1-9.0

ΣC ₈ H ₁₈ - 0.01-3.0

ΣC ₉ H ₂₀ -C ₁₂ H ₂₆ - the rest is up to 100%,

while the total content of aromatic and naphthenic hydrocarbons is not more than 6.0% by mass, and the saturated vapor pressure of the mixture is, MPa (kgf / cm, abs.):

at 20 ° С - no more than 0.26 (2.6);

at 45 ° С - not more than 0.50 (5.0).

The technical method, which consists in the fact that the claimed method of producing aviation condensed fuel (ASKT) of the proposed composition will allow to obtain a new type of highly liquid and highly profitable products through the use of waste-free production from existing raw materials - natural and petroleum gas using one of the known methods, such as obtaining a wide fraction light hydrocarbons (BFLH), and bypassing the stage of producing BFLH.

Known technologies that can be used to obtain the proposed mixture of paraffin hydrocarbons are implemented in all gas processing plants, integrated gas processing plants and small-sized field gas treatment plants, i.e. already at this stage of the preparation and processing of hydrocarbon gas, it is possible to obtain aviation condensed fuel. If necessary, further processing of the obtained hydrocarbons will allow the bottom product to produce aviation condensed fuel of the proposed composition.

When organizing production of ASKT in the field, the production technology will consist of the following main known technological processes: preparation, including compression, cooling, separation, drying, and further gas processing. The associated petroleum gas is prepared and processed by the method of low temperature separation, low temperature absorption or by the method of low temperature condensation using a propane or internal refrigeration cycle. Thus, the above technological methods provide the simplicity and manufacturability of ACCT.

The proposed method for producing a mixture of paraffin hydrocarbons, further comprising a fraction of C ₉ -C ₁₂ with the claimed ratio of components, with a total content of aromatic and naphthenic hydrocarbons of not more than 6.0% of the mass. and while ensuring the saturated vapor pressure of the mixture at 20 ° С - not more than 0.26 MPa ((2.6 kgf / cm ² , abs.), and at 45 ° С - not more than 0.50 MPa (5.0 kgf / cm ² , abs.), allows the use of this fuel in the entire temperature range in which aviation gas turbine equipment is operated, while expanding the range of products manufactured by gas processing plants or field installations for the preparation and processing of oil and natural gas.

The same result is also achieved by the fact that, according to the second embodiment, in a method for producing aviation condensed fuel, including the separation from a hydrocarbon feedstock by preparing and fractionating a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} , it is new that hydrocarbon feedstocks are used flows of a refinery or petrochemical plant, in the form of oil stabilization gases or condensate stabilization gases, stabilization gases of secondary oil refining processes, while emit a mixture of paraffin and olefin hydrocarbons, including a fraction of C ₃ -C ₁₂ in the following ratio of components,% mass .:

ΣC3H8-C3H6 - 2.0-12.0

ΣC4H10-C4H8 - 24.0-72.0

ΣC5H12-C5H10 - 4.0-36.0

ΣC6H14-C6H12 - 0.3-14.0

ΣC7H16-C7H14 - 0.1-9.0

ΣC8H18-C8H16 - 0.01-3.0

ΣC ₉ H ₂₀ -C ₁₂ H ₂₆ - the rest is up to 100%,

moreover, the total content of olefinic hydrocarbons C _n H _2n in the mixture is not more than 10% by mass, and the saturated vapor pressure of the mixture is, MPa (kgf / cm ² , abs.):

at 20 ° С - no more than 0.26 (2.6);

at 45 ° С - not more than 0.50 (5.0),

in addition, the content of aromatic and naphthenic hydrocarbons is not more than 6.0% of the mass.

The technical method, which also consists in the fact that the hydrocarbon streams of an oil refinery are used as hydrocarbon feedstocks in the inventive method for producing ASKT, in the form of oil stabilization gases or condensate stabilization gases, stabilization gases of secondary oil refining processes, for example catalytic cracking, reforming with the release of a paraffinic mixture and olefinic hydrocarbons, including the C ₃ -C ₁₂ fraction, and the total content of C _n H _2n olefin hydrocarbons in the mixture is limited and is not large less than 10 wt. -%, in addition, the content of aromatic and naphthenic hydrocarbons is not more than 6.0 wt. -%, while providing a saturated vapor pressure of the mixture at 20 ° C - not more than 0.26 MPa ((2.6 kgf / cm ² , abs.), and at 45 ° С - not more than 0.50 MPa (5.0 kgf / cm ² , abs.), this method allows to obtain aviation fuel, which can be used in the entire temperature range in which aviation gas turbine equipment is operated while expanding the range of products manufactured by oil refineries. To obtain mixtures of paraffin and olefin hydrocarbons from products of oil preparation and refining, known methods for separating hydrocarbon mixtures and recovering C _{3 +} mixtures from factory gases _above can be used as ASKT.

Thus, the proposed options for the production of ASKT allow you to expand the range of aviation fuel obtained from hydrocarbons, to expand the raw material base, i.e. to obtain ASKT from natural and associated petroleum gas, unstable oils and gas condensate, products of secondary processes of oil and condensate processing, and therefore, provide the possibility of using the method at various facilities for the preparation and processing of hydrocarbon raw materials: gas refineries, oil and gas refineries, gas treatment plants in remote areas, directly in places of oil and gas production, for example in Western Siberia.

A method of producing aviation condensed fuel is as follows.

In the first embodiment. Mixtures of paraffin hydrocarbons of the general formula C _n H _{2n + 2} , containing C ₃ -C ₈ paraffin fraction, which further comprises C ₃ -C ₈ paraffin hydrocarbons, are isolated from hydrocarbon feedstocks, which use associated petroleum gas or natural gas, by known preparation and fractionation methods fraction C ₉ -C ₁₂ , with the following content of components,% mass .:

C ₃ H ₈ - 0.1-12.0

ΣC ₄ H ₁₀ - 24.0-72.0

ΣC ₅ H ₁₂ - 4.0-36.0

ΣC ₆ H ₁₄ - 0.3-14.0

ΣC ₇ H ₁₆ - 0.1-9.0

ΣC8H18 - 0.01-3.0

ΣC ₉ H ₂₀ -C ₁₂ H ₂₆ - the rest is up to 100%.

Moreover, the total content of aromatic and naphthenic hydrocarbons in the resulting mixture is not more than 6.0 wt.%, And the saturated vapor pressure of the mixture at 20 ° C is not more than 0.26 MPa ((2.6 kgf / cm ² , abs.) and at 45 ° С - not more than 0.50 MPa (5.0 kgf / cm ² , abs.).

As a known preparation and fractionation method, for example, a method can be used that includes compression of hydrocarbon feeds up to 35 kgf / cm ² and cooling by throttling, with an external or internal refrigeration cycle to minus 10 ... 30 ° C, and the release of condensed hydrocarbons. In this case, depending on the conditions of compression and cooling (pressure and temperature), as well as the distillation of its light part C ₁ -C _{3 by} known methods, a liquid hydrocarbon mixture of a given composition is formed, which is an aviation condensed fuel.

Examples of the method according to the first embodiment (calculated execution of the method).

Example 1. From associated petroleum gas of various compositions (tables 1 and 1.1) at a pressure of 25 kgf / cm ² and a cooling temperature of minus 20 ° C, unstable condensate is isolated, and then, the light part is driven away from it (at a pressure of 4 kgf / cm ² and at a temperature of 42 ° С), aviation condensed fuel is obtained, depending on the composition of associated petroleum gas, traces of naphthenic and aromatic hydrocarbons shown in Table 1, and including naphthenic and aromatic hydrocarbons, the total content of which is not more than 6.0% by mass, in that face 1.1.

Table 1 Name of indicator Value Raw materials - associated petroleum gas Component Content % of the mass. Carbon dioxide CO ₂ 1.16 Methane CH ₄ 29.50 Ethane C ₂ H ₆ 21.41 Propane C ₃ H ₈ 35.09 i-bhutan iC ₄ H ₁₀ 5.44 n-butane nC ₄ H ₁₀ 5.42 i-Pentane iC ₅ H ₁₂ 0.88 n-Pentane nC ₅ H ₁₂ 0.38 Hexane C ₆ H ₁₄ 0.47 Heptane C ₇ H ₁₆ 0.16 Octane C ₈ H ₁₈ 0,064 Nonan C ₉ H ₂₀ 0,021 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.0072 including Naphthenic hydrocarbons traces aromatic hydrocarbons traces The resulting product is aviation condensed fuel. Component Content % of the mass. Propane C ₃ H ₈ 3.92 i-bhutan iC ₄ H ₁₀ 25.77 n-butane n-C ₄ H ₁₀ 32.60 i-Pentane iC ₅ H ₁₂ 10.92 n-Pentane n-C ₅ H ₁₂ 5.50 Hexane C ₆ H ₁₄ 12.74 Heptane C ₇ H ₁₆ 5.01 Octane C ₈ H ₁₈ 2,34 Nonan C ₉ N ₂₀ 0.87 Dean + above C ₁₀ H ₂₂ - C ₁₂ H ₂₆ 0.32 including naphthenic hydrocarbons traces aromatic hydrocarbons traces Saturated vapor pressure, MPa abs. at 45 ° C 0.44 at 20 ° C 0.22 Calorific value (lowest), kJ / kg 45519 Density, kg / m ³ at 20 ° C 598 at minus 40 ° С 660

Table 1.1 Name of indicator Value Raw materials - associated petroleum gas Component Content % of the mass. Nitrogen N ₂ 0,03 Carbon dioxide CO ₂ 9.33 Methane CH ₄ 56.87 Ethane C ₂ H ₆ 17.01 Propane C ₃ H ₈ 10.03 i-bhutan iC ₄ H ₁₀ 3.01 n-butane n-C ₄ H ₁₀ 2.01 i-Pentane iC ₅ H ₁₂ 0.90 n-Pentane n-C ₅ H ₁₂ 0.40 Hexane C ₆ H ₁₄ 0.21 Heptane C ₇ H ₁₆ 0.10 Octane C ₈ H ₁₈ 0,03 Nonan C ₉ N ₂₀ 0.01 Dean C ₁₀ H ₂₂ 0.00 Methylcyclopentane C ₆ H ₁₂ 0,03 Methylcyclohexane C ₇ H ₁₄ 0.01 Benzene C ₆ H ₆ 0.02 Toluene C ₇ H ₈ 0.01 The resulting product is aviation condensed fuel. Component Content % of the mass. Nitrogen N ₂ 0.00 Carbon dioxide CO ₂ 0.00 Methane CH ₄ 0.00 Ethane C ₂ H ₆ 0.01 Propane C ₃ H ₈ 9.00 i-bhutan iC ₄ H ₁₀ 17.50 n-butane n-C ₄ H ₁₀ 18.03 i-Pentane iC ₅ H ₁₂ 20.25 n-Pentane nC ₅ H ₁₂ 11.66 Hexane C ₆ H ₁₄ 10.95 Heptane C ₇ H ₁₆ 6.26 Octane C ₈ H ₁₈ 1.96 Nonan C ₉ H ₂₀ 0.79 Dean C ₁₀ H ₂₂ 0.01 Methylcyclopentane C ₆ H ₁₂ 1.31 Methylcyclohexane C ₇ H ₁₄ 0.61 Benzene C ₆ H ₆ 1,04 Toluene C ₇ H ₈ 0.63 including naphthenic hydrocarbons 1.92 aromatic hydrocarbons 1,67 Saturated vapor pressure, MPa abs. at 45 ° C 0.44 at 20 ° C 0.06 Calorific value, kJ / kg 45381 Density, kg / m ³ at 20 ° C 608 at minus 40 ° С 669

Example 2. With the same parameters and the same composition of associated petroleum gas, which are indicated in example 1, the gas at a compression pressure of 25 kgf / cm ² and a cooling temperature of minus 20 ° C is fed to the separation stage at a pressure of 2.4 MPa and temperature 4 ° C of a wide fraction of light hydrocarbons (BFLH), (the compositions are shown in Table 2, 2.1), and then aviation condensed fuel (from 11 to 17 kgf) is obtained from the BFLH by distillation of the light fraction C ₃ -C ₄ in a distillation column / cm ² and a temperature of 70 ... 80 ° C), including depending on the rate of associated petroleum gas, and consequently, the emitted BFLH, traces of naphthenic and aromatic hydrocarbons, are given in table 2, and including naphthenic and aromatic hydrocarbons, the total content of which is not more than 6.0% by weight, are shown in table 2.1.

table 2 Name of indicator Value Composition of BFLH Component Content % of the mass. Carbon dioxide CO ₂ 0.04 Methane CH ₄ 0.10 Ethane C ₂ H ₆ 2.62 Propane C ₃ H ₈ 45.03 i-bhutan iC ₄ H ₁₀ 15.21 n-butane n-C ₄ H ₁₀ 17.83 i-Pentane iC ₅ H ₁₂ 5.87 n-Pentane nC ₅ H ₁₂ 2.95 Hexane C ₆ H ₁₄ 6.19 Heptane C ₇ H ₁₆ 2.44 Octane C ₈ H ₁₈ 1.14 Nonan C ₉ N ₂₀ 0.43 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.16 including naphthenic hydrocarbons traces aromatic hydrocarbons traces Product received Component Content % of the mass. Propane C ₃ H ₈ 10.60 i-butane iC ₄ H ₁₀ 15.84 n-butane nC ₄ H ₁₀ 2.68 i-Pentane iC ₅ H ₁₂ 14.94 n-Pentane nC ₅ H ₁₂ 10.39 Hexane C ₆ H ₁₄ 7.96 Heptane C ₇ H ₁₆ 6.98 Octane C ₈ H ₁₈ 3.24 Nonan C ₉ H ₂₀ 1.85 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.51 including naphthenic hydrocarbons traces aromatic hydrocarbons traces Saturated vapor pressure, MPa abs. Poi 45 ° C 0.49 at 20 ° C 0.25 Calorific value (lowest), kJ / kg 45526 Density, kg / m ³ at 20 ° C 600 at minus 40 ° С 662

Table 2.1 Name of indicator Value Raw materials - SHFLU Component Content % of the mass. Nitrogen N ₂ 0.00 Carbon dioxide CO ₂ 0.00 Methane CH ₄ 0.00 Ethane C ₂ H ₆ 2,50 Propane C ₃ H ₈ 30.70 i-bhutan iC ₄ H ₁₀ 9.69 n-butane n-C ₄ H ₁₀ 36.14 i-Pentane iC ₅ H ₁₂ 7.44 n-Pentane nC ₅ H ₁₂ 7.66 Hexane C ₆ H ₁₄ 3.92 Heptane C ₇ H ₁₆ 0.97 Octane C ₈ H ₁₈ 0.01 Nonan C ₉ H ₂₀ 0.01 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.00 Methylcyclopentane C ₆ H ₁₂ 0.41 Methylcyclohexane C ₇ H ₁₄ 0.19 Benzene C ₆ H ₆ 0.33 Toluene C ₇ H ₈ 0,03 The resulting product is aviation condensed fuel. Component Content % of the mass. Nitrogen N ₂ 0.00 Carbon dioxide CO ₂ 0.00 Methane CH ₄ 0.00 Ethane C ₂ H ₆ 0.00 Propane C ₃ H ₈ 3.00 i-bhutan iC ₄ H ₁₀ 12.84 n-butane n-C ₄ H ₁₀ 52.94 i-Pentane iC ₅ H ₁₂ 11.07 n-Pentane nC ₅ H ₁₂ 11.40 Hexane C ₆ H ₁₄ 5.83 Heptane C ₇ H ₁₆ 1.44 Octane C ₈ H ₁₈ 0.01 Nonan C ₉ H ₂₀ 0.02 Dean C ₁₀ H ₂₂ 0.01 Methylcyclopentane C ₆ H ₁₂ 0.62 Methylcyclohexane C ₇ H ₁₄ 0.29 Benzene C ₆ H ₆ 0.49 Toluene C ₇ H ₈ 0.05 including naphthenic hydrocarbons 0.91 aromatic hydrocarbons 0.53 Saturated vapor pressure, MPa abs. at 45 ° C 0.42 at 20 ° C 0.05 Calorific value. kJ / kg 45568 Density, kg / m ³ at 20 ° C 595 at minus 40 ° С 655

Example 3. When processing natural gas of various compositions (tables 3, 3.1), as a rule, the installation of integrated gas treatment (UKPG) uses the low-temperature separation method (NTS), in which the gas is throttled to 57 ... 60 kgf / cm ² , cooled due to the Joule-Thomson effect or with the use of a turbo-expander unit up to minus 15 ... 40 ° С, the prepared gas is sent to the main gas pipeline, and the separated condensed hydrocarbon phase is used to produce aviation condensed fuel. As in the previous examples, the conditions for the preparation of raw materials for obtaining aviation condensed fuel can vary: both through the stage of separation of unstable condensate and through the stage of separation of BFLH, and then, by distilling the light fraction C ₃ -C ₄ from the condensate or BFLH, by rectification ( for example, at a pressure of 2.5 MPa, temperature minus 7 ° C), we obtain aviation condensed fuel, which, depending on the composition of natural gas, includes traces of naphthenic and aromatic hydrocarbons, shown in table 3, and incl. sistent naphthenic and aromatic hydrocarbons, total content of not more than 6.0 wt.%, shown in Table 3.1.

Table 3 Name of indicator Value Raw materials - natural gas Component Content % of the mass. Nitrogen N ₂ 0.313 Carbon dioxide CO ₂ 1,572 Methane CH ₄ 83,129 Ethane C ₂ H ₆ 5,303 Propane C ₃ H ₈ 4,504 i-bhutan iC ₄ H ₁₀ 1,136 n-butane n-C ₄ H ₁₀ 1,914 i-Pentane iC ₅ H ₁₂ 0.765 n-Pentane nC ₅ H ₁₂ 0.684 Hexane C ₆ H ₁₄ 0.404 Heptane C ₇ H ₁₆ 0.162 Octane C ₈ H ₁₈ 0,077 Nonan C ₉ H ₂₀ 0,029 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.008 including naphthenic hydrocarbons traces aromatic hydrocarbons traces Product received Component Content % of the mass. Ethane C ₂ H ₆ 0.003 Propane C ₃ H ₈ 3,500 i-bhutan iC ₄ H ₁₀ 14,867 n-butane n-C ₄ H ₁₀ 31,978 i-Pentane iC ₅ H ₁₂ 16,551 n-Pentane nC ₅ H ₁₂ 15,615 Hexane C ₆ H ₁₄ 10,215 Heptane C ₇ H ₁₆ 4,256 Octane C ₈ H ₁₈ 2,037 Nonan C ₉ H ₂₀ 0.766 Dean + above C ₁₀ H ₂₂ -C ₁₂ H ₂₆ 0.213 including naphthenic hydrocarbons traces aromatic hydrocarbons traces Saturated vapor pressure, MPa abs. at 45 ° C 0.38 at 20 ° C 0.19 Calorific value (lowest), kJ / kg 45490 Density, kg / m ³ at 20 ° C 604 at minus 40 ° С 665

Table 3.1 Name of indicator Value Raw materials - natural gas Component Content % of the mass. Carbon dioxide N ₂ 0.302 Nitrogen CO ₂ 0.862 Methane CH ₄ 85,092 Ethane C ₂ H ₆ 4,345 Propane C ₃ H ₈ 5,063 i-bhutan iC ₄ H ₁₀ 1,912 n-butane n-C ₄ H ₁₀ 1,844 i-Pentane iC ₅ H ₁₂ 0.350 n-Pentane nC ₅ H ₁₂ 0,200 Hexane C ₆ H ₁₄ 0,022 Heptane C ₇ H ₁₆ 0.003 Octane C ₈ H ₁₈ 0,000 Nonan C ₉ H ₂₀ 0,000 Dean + above C ₁₀ H ₂₂ 0,000 Methylcyclopentane C ₆ H ₁₂ 0.001 Methylcyclohexane C ₇ H ₁₄ 0,000 Benzene C ₆ H ₆ 0.004 Toluene C ₇ H ₈ 0.001 Product received Component Content % of the mass. Ethane C ₂ H ₆ 0,100 Propane C ₃ H ₈ 8,413 i-bhutan iC ₄ H ₁₀ 19,328 n-butane n-C ₄ H ₁₀ 31,520 i-Pentane iC ₅ H ₁₂ 17,365 n-Pentane nC ₅ H ₁₂ 14,438 Hexane C ₆ H ₁₄ 5,381 Heptane C ₇ H ₁₆ 1,739 Octane C ₈ H ₁₈ 0,000 Nonan C ₉ H ₂₀ 0,000 Dean + above C ₁₀ H ₂₂ 0,000 Methylcyclopentane C ₆ H ₁₂ 0.123 Methylcyclohexane C ₇ H ₁₄ 0.059 Benzene C ₆ H ₆ 0.894 Toluene C ₇ H ₈ 0.642 including naphthenic hydrocarbons 0.182 aromatic hydrocarbons 1,535 Saturated vapor pressure, MPa abs. at 45 ° C 0.48 at 20 ° C 0.06 Calorific value (lowest), kJ / kg 45542 Density, kg / m ³ at 20 ° C 591 at minus 40 ° С 654

From the above examples 1-3 of the implementation of the method according to option 1 it follows that in all cases the saturated vapor pressure of the obtained aviation condensed fuel does not exceed 0.26 MPa (2.6 kgf / cm ² , abs.) At 20 ° C and 0, 50 MPa (5.0 kgf / cm ² , abs.) At 45 ° С. The propane content in this case can be less than 6% and more than 10% by mass, which completely depends on the composition of the feedstock (oil or natural gas). The calorific value of the resulting fuel in all cases is higher than that of aviation kerosene (45519 versus 42900 kJ / kg).

From the foregoing, it follows that the compositions and properties of the resulting aviation condensed fuel are reasonable and acceptable for use.

The increase in propane content of more than 12% of the mass. leads to a sharp increase in saturated vapor pressure, for example, with a propane content of 13% of the mass. the saturated vapor pressure at 45 ° C is 0.54 MPa (5.4 kgf / cm ² abs.), which requires structural changes in the fuel supply system, and a decrease in propane content below 0.1% of the mass. leads to a decrease in calorific value and thereby to an increase in fuel consumption. Thus, the proposed composition of ASKT is optimal.

According to the second variant, the method is as follows: from hydrocarbon feedstocks, which are used as hydrocarbon streams of a refinery or petrochemical plants, in the form of oil stabilization gases or condensate stabilization gases, stabilization gases of secondary oil refining processes obtained, for example, by catalytic cracking, reforming, by known methods of preparation and fractionation emit a mixture of paraffin and olefin hydrocarbons of the General formula C _n H _{2n + 2} , which includes a fraction C ₃ -C ₁₂ . In the resulting mixture, the total content of olefinic hydrocarbons C _n H _{2n is} limited and is not more than 10% by mass, and the saturated vapor pressure of the mixture at 20 ° C is not more than 0.26 MPa (2.6 kgf / cm ² , abs.), and at 45 ° C - not more than 0.50 MPa (5.0 kgf / cm ² , abs.). The mixture has a limited content of aromatic and naphthenic hydrocarbons, which is not more than 6.0 wt.%, While a mixture of paraffin and olefin hydrocarbons is isolated in the following ratio of components,% wt .:

ΣC ₃ H ₈ -C ₃ H ₆ - 2.0-12.0

ΣC ₄ H ₁₀ -C ₄ H ₈ - 24.0-72.0

ΣC ₅ H ₁₂ -C ₅ H ₁₀ - 4.0-36.0

ΣC ₆ H ₁₄ -C ₆ H ₁₂ - 0.3-14.0

ΣC ₇ H ₁₆ -C ₇ H ₁₄ - 0.1-9.0

ΣC ₈ H ₁₈ -C ₈ H ₁₆ - 0.01-3.0

ΣC ₉ H ₂₀ -C ₁₂ H ₂₆ - the rest is up to 100%.

To obtain ASKT of the proposed composition, for example, from oil stabilization gases or condensate stabilization gases, stabilization gases of secondary oil refining processes, a known method is used (as described in the first embodiment), including compression of the gas, its cooling by throttling, by an external or internal refrigeration cycle to minus 30 ° C, the release of condensed hydrocarbons.

Depending on the conditions of compression and cooling, as well as the distillation of its light part of C ₁ -C _{3 by} known methods, the isolated liquid hydrocarbon mixture is an aviation condensed fuel.

Examples of the method according to the second embodiment.

Example 4. The feedstock - gas stabilization of catalysis - a product of a secondary oil refining, namely reforming (the composition of which is given in table 4), after its compression to a pressure of 25 kgf / cm ² , is cooled by throttling, external or internal refrigeration cycle to minus 20 ° C, and then a liquid hydrocarbon mixture of a given composition, which is an aviation condensed fuel, shown in table 4, is isolated by rectification.

Table 4 Name of indicator Value Raw materials - reforming catalysis stabilization gas Component Content % of the mass. Methane CH ₄ 4,455 Ethylene C ₂ H ₄ 2,091 Ethane C ₂ H ₆ 6,361 Propene C ₃ H ₆ 2,768 Propane C ₃ H ₈ 52,627 i-bhutan i-C ₄ H ₁₀ 10,588 Butene C ₄ H ₈ 1,580 n-butane n-C ₄ H ₁₀ 11,219 i-Pentane iC ₅ H ₁₂ 2,942 Penten C ₅ H ₁₀ 0,099 n-Pentane n-C ₅ H ₁₂ 1,988 2,2-dimethylbutane i-C ₆ H ₁₄ 0.368 2-methylpentane i-C ₆ H ₁₄ 0.692 Hexen C ₆ H ₁₂ 0,063 n-hexane C ₆ H ₁₄ 0.298 Methylcyclopentane C ₆ H ₁₂ 0.206 Benzene C ₆ H ₆ 0.151 Cyclohexane C ₆ H ₁₂ 0,064 2,2-dimethylpentane C ₇ H ₁₆ 0.193 1,1-Dimethylcyclopentane C ₇ H ₁₄ 0.123 Methylcyclohexane C ₇ H ₁₄ 0.244 Toluene C ₇ H ₈ 0.279 2,2-dimethylhexane C ₈ H ₁₈ 0,065 1-trans-2-cis-3-trimethylcyclopentane C ₈ H ₁₆ 0.230 n-octane C ₈ H ₁₈ 0.007 Ethylbenzene C ₈ H ₁₀ 0,028 m-xylene C ₈ H ₁₀ 0.145 2,4-dimethylheptane C ₉ N ₂₀ 0,048 n nonan C ₉ N ₂₀ 0.003 1-methyl-3-ethylbenzene C ₉ H ₁₂ 0,046 Cyclodecan C ₁₀ N ₂₀ 0,0008 2,7-Dimethyloctane C ₁₀ H ₂₂ 0.008 N-Dean C ₁₀ H ₂₂ 0,0006 m-cumene C ₁₀ H ₁₄ 0.012 n-undecan C ₁₁ H ₂₄ 0,0002 Undeken C ₁₁ H ₂₂ 0.003 Dodecan C ₁₂ H ₂₆ 0.004 The resulting product is aviation condensed fuel. Component Content % of the mass. Ethane C ₂ H ₆ 0,000 Propene C ₃ H ₆ 0,093 Propane C ₃ H ₈ 5,010 i-bhutan i-C ₄ H ₁₀ 27,617 Butene C ₄ H ₈ 4,003 n-butane n-C ₄ H ₁₀ 34,448 i-Pentane iC ₅ H ₁₂ 9,526 Penten C ₅ H ₁₀ 0.322 n-Pentane n-C ₅ H ₁₂ 6,474 2,2-dimethylbutane i-C ₆ H ₁₄ 1,206 2-methylpentane i-C ₆ H ₁₄ 2,271 Hexen C ₆ H ₁₂ 0.208 n-hexane C ₆ H ₁₄ 0.981 Methylcyclopentane C ₆ H ₁₂ 0.676 Benzene C ₆ H ₆ 0.496 Cyclohexane C ₆ H ₁₂ 0.209 2,2-dimethylpentane C ₇ H ₁₆ 0.636 1,1-Dimethylcyclopentane C ₇ H ₁₄ 0.404 Methylcyclohexane C ₇ H ₁₄ 0.684 Toluene C ₇ H ₈ 0.921 2,2-dimethylhexane C ₈ H ₁₈ 0.214 1-trans-2-cis-3-trimethylcyclopentane C ₈ H ₁₆ 0.758 n-octane C ₈ H ₁₈ 0,023 Ethylbenzene C ₈ H ₁₀ 0,091 m-xylene C ₈ H ₁₀ 0.479 2,4-dimethylheptane C ₉ N ₂₀ 0.156 n nonan C ₉ N ₂₀ 0.008 1-methyl-3-ethylbenzene C ₉ H ₁₂ 0.150 Cyclodecan C ₁₀ N ₂₀ 0.003 2,7-Dimethyloctane C ₁₀ H ₂₂ 0,027 N-Dean C ₁₀ H ₂₂ 0.002 m-cumene C ₁₀ H ₁₄ 0,039 n-undecan C ₁₁ H ₂₄ 0,0007 Undeken C ₁₁ H ₂₂ 0.003 Dodecan C ₁₂ H ₂₆ 0.009 including olefinic hydrocarbons 4,50 naphthenic hydrocarbons 2.73 aromatic hydrocarbons 2.18 Saturated vapor pressure, MPa abs. at 45 ° C 0.49 at 20 ° C 0.24 Calorific value (lowest), kJ / kg 44752 Density, kg / m ³ at 20 ° C 592 at minus 40 ° С 656

Example 5. The feedstock — gas stabilization gas — hydrocarbon stream of an oil refinery (the composition of which is shown in Table 5), after compression to 25 kgf / cm ^{2, is} cooled by throttling, by an external or internal refrigeration cycle, to minus 20 ° С, and then it is isolated by rectification liquid hydrocarbon mixture of a given composition, which is an aviation condensed fuel, are presented in table 5.

Table 5 Name of indicator Value Raw materials - oil stabilization gas Component Content % of the mass. Nitrogen N ₂ 1,773 Methane CH ₄ 34,125 Carbon dioxide CO ₂ 0.551 Ethane C ₂ H ₆ 3,520 Propane C ₃ H ₈ 19,087 isobutane iC ₄ H ₁₀ 15,119 n-butane n-C ₄ H ₁₀ 22,993 isopentane iC ₅ H ₁₂ 1,691 n-pentane nC ₅ H ₁₂ 0.980 methylpentane i-C ₆ H ₁₄ 0.108 hexane C ₆ H ₁₄ 0,029 methylcyclopentane C ₆ H ₁₂ 0.014 benzene C ₆ H ₆ 0.003 heptane C ₇ H ₁₆ 0.005 methylcyclohexane C ₇ H ₁₄ 0.002 toluene C ₇ H ₈ 0,000 octane C ₈ H ₁₈ 0,000 nonan C ₉ N ₂₀ 0,000 dean + above C ₁₀ H ₂₂ 0,000 including olefinic hydrocarbons traces The resulting product is aviation condensed fuel. Component Content % of the mass. propane C ₃ H ₈ 0.487 isobutane iC ₄ H ₁₀ 36,614 n-butane n-C ₄ H ₁₀ 55,682 isopentane iC ₅ H ₁₂ 4,311 n-pentane nC ₅ H ₁₂ 2,499 methylpentane i-C ₆ H ₁₄ 0.274 hexane C ₆ H ₁₄ 0,074 benzene C ₆ H ₁₂ 0,036 heptane C ₆ H ₆ 0.007 methylcyclohexane C ₇ H ₁₆ 0.012 toluene C ₇ H ₁₄ 0.004 octane C ₈ H ₁₈ 0,000 nonan C ₉ H ₂₀ 0,000 dean + above C ₁₀ H ₂₂ 0,000 including olefinic hydrocarbons traces naphthenic hydrocarbons 0,040 aromatic hydrocarbons 0.007 Saturated vapor pressure, MPa abs. At 45 ° C 0.48 at 20 ° C 0.06 Calorific value, kJ / kg 45682 Density, kg / m ³ at 20 ° C 573 at minus 40 ° С 639

Example 6. The feedstock — condensate stabilization gas — hydrocarbon stream of an oil refinery (the composition of which is shown in Table 6) after compression to a pressure of 25 kgf / cm ^{2 is} cooled by throttling, by an external or internal refrigeration cycle, to minus 20 ° С, and then it is isolated by rectification liquid hydrocarbon mixture of a given composition, which is an aviation condensed fuel, presented in table 6.

Table 6 Name of indicator Value Raw materials - condensate stabilization gas Component Content % of the mass. Nitrogen N ₂ 0,025 Carbon dioxide CO ₂ 26,074 Methane CH ₄ 40,493 Ethane C ₂ H ₆ 13,274 Propane C ₃ H ₈ 12,480 i-bhutan iC ₄ H ₁₀ 3,239 n-butane n-C ₄ H ₁₀ 3,042 Butene nC ₄ H ₈ 0,120 i-Pentane iC ₅ H ₁₂ 0.757 n-Pentane n-C ₅ H ₁₂ 0.237 Hexane C ₆ H ₁₄ 0,090 Hexen C ₆ H ₁₂ 0.010 Heptane C ₇ H ₁₆ 0,068 Octane C ₈ H ₁₈ 0.005 Nonan C ₉ H ₂₀ 0.001 Dean C ₁₀ H ₂₂ 0.001 Benzene C ₆ H ₆ 0.013 Toluene C ₇ H ₈ 0.004 Methylcyclopentane C ₆ H ₁₂ 0,048 Methylcyclohexane C ₇ H ₁₄ 0.019 n-C11 C ₁₁ H ₂₄ 0,00020 The resulting product is aviation condensed fuel. Component Content % of the mass. Nitrogen N ₂ 0,000 Carbon dioxide CO ₂ 0,000 Methane CH ₄ 0,000 Ethane C ₂ H ₆ 0,000 Propane C ₃ H ₈ 4,997 i-bhutan iC ₄ H ₁₀ 26,213 n-butane n-C ₄ H ₁₀ 34,514 Butene C ₄ H ₈ 1,200 i-Pentane iC ₅ H ₁₂ 17,295 n-Pentane n-C ₅ H ₁₂ 6,310 Hexane C ₆ H ₁₄ 3,208 Hexen C ₆ H ₁₂ 0.350 Heptane C ₇ H ₁₆ 2,610 Octane C ₈ H ₁₈ 0.196 Nonan C ₉ H ₂₀ 0,039 Dean C ₁₀ H ₂₂ 0,032 Benzene C ₆ H ₆ 0.462 Toluene C ₇ H ₈ 0.135 Methylcyclopentane C ₆ H ₁₂ 1,711 Methylcyclohexane C ₇ H ₁₄ 0.721 n-C11 C ₁₁ H ₂₄ 0.008 including olefinic hydrocarbons 1,550 naphthenic hydrocarbons 2,433 aromatic hydrocarbons 0.596 Saturated vapor pressure, MPa abs. at 45 ° C 0.46 at 20 ° C 0.23 Calorific value, kJ / kg 45527 Density, kg / m ³ at 20 ° C 590 at minus 40 ° С 654

From the above examples 4, 5, 6 of the implementation of the method according to the second embodiment, it follows that in this case, the saturated vapor pressure of the obtained aviation condensed fuel does not exceed 0.26 MPa (2.6 kgf / cm ² , abs.) At 20 ° C and 0.50 MPa (5.0 kgf / cm ² , abs.) At 45 ° С. The content of olefinic hydrocarbons is not more than 10% by mass., Aromatic and naphthenic hydrocarbons is not more than 6.0% by mass. The content of these hydrocarbons in aviation condensed fuel depends on their presence in the feedstock, and what processing process the hydrocarbon feedstock of the refinery or petrochemical plants was subjected to (for example, catalytic cracking, reforming, etc.). The calorific value of the resulting fuel is higher than that of aviation kerosene (44752 versus 42900 kJ / kg).

From the foregoing, it follows that the composition and properties of the proposed aviation condensed fuel are reasonable and acceptable for use.

The increase in the content of aromatic hydrocarbons more than 6.0% of the mass. leads to increased pollution of exhausts, and thereby worsens the environmental situation, and an increase in the content of olefinic hydrocarbons more than 10% of the mass. leads to a decrease in fuel stability. Thus, the proposed composition of aviation condensed fuel is optimal.

Thus, the proposed method allows to obtain aviation condensed fuel in a wide range of its component composition from various hydrocarbon feedstocks at various facilities for the preparation and processing of hydrocarbon feedstocks in the fuel and energy complex: field facilities for collecting and preparing oil and gas from oil and gas companies, product pipelines transporting NGL or unstable condensate, gas refineries, oil refineries. Production is most effective when organized on equipped sites with a certain infrastructure (availability of electricity, heat, access roads, etc.). Using a simplified production technology, the method allows to solve the problems of production of aviation fuel for gas turbine aircraft (helicopters) in close proximity to places of consumption from available and often unused raw materials. A method of producing aviation condensed fuel will simultaneously allow to obtain a new type of highly liquid and highly profitable products due to the introduction of non-waste production from existing raw materials - natural and associated petroleum gas.

Claims (2)

1. A method of producing aviation condensed fuel, comprising the allocation of hydrocarbon raw materials by preparing and fractionating a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} containing paraffin hydrocarbon fraction C ₃ -C ₈ , characterized in that as a hydrocarbon feed use associated petroleum gas or natural gas, while emitting a mixture of paraffin hydrocarbons, further comprising a fraction of C ₉ -C ₁₂ , with the following components, wt.%:
C ₃ H ₈ 0.1-12.0
ΣC ₄ H ₁₀ 24.0-72.0
ΣC ₅ H ₁₂ 4.0-36.0
ΣC ₆ H ₁₄ 0.3-14.0
ΣC ₇ H ₁₆ 0.1-9.0
ΣC ₈ H ₁₈ 0.01-3.0
ΣC ₉ H ₂₀ -C ₁₂ H _{26 the} rest is up to 100%,
the total content of aromatic and naphthenic hydrocarbons is not more than 6.0 wt.%, and the saturated vapor pressure of the mixture is, MPa (kgf / cm ² , abs.):
at 20 ° C no more than 0.26 (2.6);
at 45 ° C no more than 0.50 (5.0). 2. A method of producing aviation condensed fuel, including the allocation of hydrocarbon feedstock by preparing and fractionating a mixture of paraffin hydrocarbons of the general formula C _n H _{2n + 2} , characterized in that hydrocarbon streams of a refinery or petrochemical plant are used as hydrocarbon feedstocks in the form of oil stabilization gases or condensate stabilization gases, stabilization gases of secondary oil refining processes, and a mixture of paraffinic and olefinic hydrocarbons is isolated, including th fraction C ₃ -C ₁₂ , in the following ratio of components, wt.%:
ΣC ₃ H ₈ -C ₃ H ₆ 2.0-12.0
ΣC ₄ H ₁₀ -C ₄ H ₈ 24.0-72.0
ΣC ₅ H ₁₂ -C ₅ H ₁₀ 4.0-36.0
ΣC ₆ H ₁₄ -C ₆ H ₁₂ 0.3-14.0
ΣC ₇ H ₁₆ -C ₇ H ₁₄ 0.1-9.0
ΣC ₈ H ₁₈ -C ₈ H ₁₆ 0.01-3.0
ΣC ₉ H ₂₀ -C ₁₂ H _{26 the} rest is up to 100%,
moreover, the total content of olefinic hydrocarbons C _n H _2n in the mixture is not more than 10 wt.%, and the saturated vapor pressure of the mixture is, MPa (kgf / cm ² , abs.):
at 20 ° C no more than 0.26 (2.6);
at 45 ° С no more than 0.50 (5.0),
in addition, the content of aromatic and naphthenic hydrocarbons is not more than 6.0 wt.%.