RU2788947C1 - Method for obtaining aromatic hydrocarbons from a wide fraction of light hydrocarbons in the gas phase - Google Patents

Abstract

FIELD: refining and petrochemical industry.

SUBSTANCE: invention relates to the field of oil refining and petrochemical industry. Claimed is a method for producing aromatic hydrocarbons from a wide fraction of light hydrocarbons in the gas phase. To implement the method, hydrocarbon feedstock and water are distributed into the reactor, which includes at least two consecutive independent reaction zones, or at least two series-connected reactors. In this case, water is supplied to each reaction volume. Depending on the temperature parameters in different reaction zones, the volumetric rate of water supply can be adjusted. In this case, the supply of water and hydrocarbon fraction is carried out in the gas phase, and the total ratio of raw materials and water is in the ranges of 76...85%/15...24%, respectively.

EFFECT: creation of a method for producing aromatic hydrocarbons from a wide fraction of light hydrocarbons in the gas phase in a multi-shelf reactor or several independent sequential reactors with a distributed supply of raw materials and a distributed controlled supply of water.

14 cl, 2 tbl, 15 ex

Description

The invention relates to the field of oil refining and petrochemical industry. More specifically, the invention relates to a process for processing aliphatic hydrocarbons into an aromatics concentrate or a high-octane gasoline component for the production of gasolines or aromatics concentrates on a zeolite catalyst in a multi-rack reactor or several independent sequential reactors with a distributed supply of raw materials and a distributed controlled supply of water.

The production of synthetic fuel and (or) aromatics concentrate from associated petroleum gas is a well-known solved scientific and technical problem, including through the production of synthesis gas and its subsequent processing. However, this approach, which involves the production of methanol, is not the only possible option.

The prior art technology for producing a high-octane gasoline product by zeoforming is a process of catalytic processing of low-octane gasoline fractions (straight-run gasoline fractions of oils and gas condensates, gas gasolines and other fractions boiling away in the temperature range of 35-200 ° C) into high-octane unleaded gasolines on zeolite-containing catalysts , as well as various options for the development of this technology.

Known technology for the conversion of dimethyl ether, for example, [RU 2160160 Published: 10.12.2000 Bull. No. 34]. This invention relates to a process for producing liquid hydrocarbons enriched in iso- and cycloparaffins, which can be used as an additive in the production of high-octane gasolines with an aromatic hydrocarbon content of not more than 30 wt.%. Liquid hydrocarbons are obtained from dimethyl ether using a catalyst based on crystalline aluminosilicate of the pentasil type with SiO2/Al2O3 = 25-100, containing 0.05-0.1 wt.% sodium oxide, and a binder, which additionally contains zinc oxide and rare earth oxides. elements in the following ratio of components, wt.%: Zn0 0.5-3.0, REE oxides 0.1-5.0, crystalline aluminosilicate 65-70, binding the rest. The catalyst is activated in air at 540-560°C. The process is carried out at a pressure of 0.1-10 MPa, a temperature of 250-400°C, a feed space velocity of 250-1100 h-1.

Also known from the prior art is a zeolite-containing catalyst, a method for its preparation and a method for converting aliphatic hydrocarbons into an aromatic hydrocarbon concentrate or a high-octane component of gasoline [RU 2221643 Published: 20.01.2004 Bull. No. 2]. This technical solution describes the catalyst itself, a method for its production and a method for converting aliphatic hydrocarbons into an aromatic hydrocarbon concentrate or a high-octane gasoline component (options) by passing a gaseous mixture of low molecular weight saturated hydrocarbons or vapors of straight-run gasoline fraction of oil through a layer of zeolite-containing catalyst.

Also known solution [RU 2172212 Published: 20.08.2001 Bull. No. 23], related to the catalyst for the conversion of aliphatic hydrocarbons C2-C12, a high-octane component of gasoline or an aromatic hydrocarbon concentrate containing a high-silica zeolite of the pentaxyl group with a molar ratio of SiO2/Al2O3 = 20-80 and a residual sodium oxide content of not more than 0.4 wt. %, zinc oxide, a mixture of two or more oxides of rare earth elements selected from the group Ce, La, Nd, Pr, a binder (γ - Al2O3, crystalline silicon dioxide, synthetic aluminosilicate, clay, zirconium dioxide, etc.). However, in the exemplary embodiments of the invention, data are provided that this catalyst composition provides an increase in the yield of liquid C5+ hydrocarbons and an increase in the content of aromatic hydrocarbons in them. Samples of catalysts prepared according to this patent were tested in the reaction of the conversion of low-octane (O.h. = 52 points by MM) gas condensate gasoline under the conditions: temperature 430°C; pressure 1.5 MPa; volumetric feed rate of raw materials (liquid) 1.5 h ^-1 . According to the test results, the yield of С5+ hydrocarbons was achieved up to 76% wt. with an aromatic content of up to 34.7% wt. and OCH (according to the motor method) up to 85.8.

These analogs are characterized by obvious disadvantages - the use of a wide range of fractions, in some cases up to C12 reduces the value of the described technology. The processing of C1 - C4 fractions with high rates of obtaining gasoline or aromatic concentrate, which would seem to be a more valuable solution for industrial use, has not been adequately disclosed in these analogues.

Also known from the prior art is a method [US 4677235, Published 06/30/1987] for producing aromatic hydrocarbons from natural gas containing nitrogen, methane, ethane, propane and butane. The method includes compressing and supplying a stream containing hydrogen, ethane, propane and C6+ aromatic hydrocarbons leaving the dehydrocyclodimerization reaction zone to a vapor-liquid separation zone operating under conditions (including at a pressure above 2.8 MPa) effective for separating the incoming components into a vapor-phase effluent stream containing nitrogen, hydrogen and methane, and a liquid-phase I process stream containing ethane, propane and C6+ aromatic hydrocarbons, supplying raw natural gas to the vapor-liquid separation zone; feeding I process stream into a fractionation zone containing at least one distillation column operating under conditions effective to separate the hydrocarbons of I process stream into at least II process stream containing propane and I product stream containing C6+ hydrocarbons, and removing this stream from process; supply of process stream II to the dehydrocyclodimerization zone operating under dehydrocyclodimerization conditions, including at a pressure of less than 0.7 MPa, and producing a stream exiting the reaction zone.

In the process described, the feedstock entering the dehydrocyclodimerization reaction zone is separated from methane with an economically acceptable degree of purity, which, however, involves the use of high pressure or deep cold. In a preferred embodiment, the fractionation zone consists of several fractionation columns for separating ethane and propane-butane fraction, which is the raw material for the reaction zone. However, this feedstock can also be C2-C4 light hydrocarbons separated from the I process stream in one fractionating column as the II process stream.

Or the method [RU 2139844, Published: 20.10.1999]: non-condensable components and C2-C4 hydrocarbons of raw materials and recycle streams are fed into the dehydrocyclodimerization reaction zone. Nitrogen, methane, and ethane are coolants that provide endothermic conversion of propane and butane, which makes it possible to carry out the dehydrocyclodimerization reaction of feedstock in a single-stage adiabatic reactor without intermediate heating of the partially converted feedstock, which complicates the design of the reactor and furnace. In the method for obtaining aromatic hydrocarbons from associated gas during the reaction of dehydrocyclization of C3+ components of raw materials on zeolite-containing catalysts, the flow leaving the reaction zone and containing hydrogen, C1-C4 alkanes and C6+ aromatic hydrocarbons is fed into the separation zone, a vapor-phase stream containing hydrogen and methane, and liquid-phase I process stream containing propane, butane and C6+ aromatic hydrocarbons, feed I process stream to the fractionation zone and separate it into at least II process stream containing propane and butane, and I product stream containing C6+ aromatic hydrocarbons , the second process stream is fed to the dehydrocyclodimerization reaction zone operating under dehydrocyclodimerization conditions, and a stream leaving the reaction zone is obtained, characterized in that the vapor-phase stream from the separation zone also contains ethane, and raw materials containing C1-C4 alkanes are fed into the reaction zone, and part of the vapor phase flow from the separation zone.

The closest analogue is a method for converting aliphatic hydrocarbons into an aromatic hydrocarbon concentrate or a high-octane component of gasoline, patented as part of the group of inventions [RU 2221643, Published: 19.6.2002]. Within the group of inventions, information is provided on the possibility of obtaining, using a zeolite catalyst, a condensed phase of an aromatic hydrocarbon concentrate directly from low molecular weight gaseous hydrocarbons, for example, from associated petroleum gases and a wide fraction of light hydrocarbons (NGL). The technical result regarding the method based on the use of the proposed zeolite-containing catalyst for the conversion of aliphatic hydrocarbons into an aromatic hydrocarbon concentrate or a high-octane component of gasoline is achieved by passing a gaseous mixture of low molecular weight saturated hydrocarbons (raw material) (2.2 wt.% ethane, 73.7 wt.% propane, 24.1 wt.% i- and n-butane) through a layer of catalyst heated to a temperature of 500-600°C.

The value of the analogs described above seems to be precisely in the fact that, in this case, including technically, the methane component is excluded and light hydrocarbons are directly processed on a zeolite catalyst to obtain aromatic compounds as the target product.

The disadvantages include the non-uniformity of the reaction due to the use of one reaction volume, including due to the distribution of the temperature field over the catalyst layer and, as a result, a decrease in the yield of the target product, as well as a decrease in catalytic activity due to coking of the catalyst, which leads to to the need for replacement and/or regeneration. This problem is proportional to the technology scaling step. In larger reactors, the situation will be aggravated by these negative factors to a greater extent.

It should be noted that the use of a multi-reactor scheme, or reactors with several independent reaction zones, is a natural development of "zeoforming" technologies and its variations (metaforming, aroforming). In particular, it is necessary to note the optimality of the approach using multi-shelf reactors, that is, reactors in which several independent reaction volumes are intentionally smaller relative to one comparable in terms of weight and size characteristics of the reactor, which allow more controlled processing of raw materials and promptly adjust the reaction parameters in each of the reaction zones. This can be confirmed by solutions known from the prior art. For example, the method WO/2017/155424 [WO 2017155424, publication date 09/14/2017], in which the stream of raw components, similar to the previous method given in the prior art, is purified, and then fed into a multi-shelf reactor, where the reaction is carried out in the presence of a zeolite-containing catalyst, the target product of which is high-octane gasoline. At the outlet of the reactor, the conversion product is separated with simultaneous removal of the reaction water and exhaust gases. A reactor is used as a reactor, containing at least two reaction zones, between which there are additional means for mixing the reaction product from the previous reaction zone and the supplied alcohol and olefin-containing raw materials.

The claimed invention will make it possible to optimize the processes for producing gasolines or concentrated aromatic compounds from available and, as a rule, low-margin, and in some cases, recyclable, raw materials.

The technical result is a method for producing aromatic hydrocarbons from a wide fraction of light hydrocarbons in the gas phase in a multi-shelf reactor or several independent sequential reactors with a distributed supply of raw materials and a distributed controlled supply of water.

The technical result is achieved by solving the problem of carrying out the reaction in a reactor, including at least two independent reaction zones, or in at least two consecutive reactors (hereinafter referred to as independent reaction zones), in which hydrocarbon feedstock - NGLs, in particular - associated petroleum gas (hereinafter - hydrocarbon fraction, HCF), and water in the proportion of 76 ... 85% / 15 ... 24%, respectively. This ensures a distributed supply of raw material flows. The hydrocarbon fraction (UHF) is supplied to at least the first reaction zone. Water is supplied to the first and subsequent reaction zones. Water is supplied in the form of steam. Volumetric water supply is carried out in the ratio: to the first reaction zone - up to 50% of the total volume of water supplied, to the second - from the rest, when implementing the option with two reaction volumes. When implementing a scheme with three or more reaction zones, the water supply is carried out in the ratio: to the first reaction zone - 20 ... 30% of the total volume of water supplied, to the second and subsequent - the rest, while the volume from 70% to 80% is distributed between subsequent reaction zones in equal proportions or in such a way that more water is supplied to each subsequent reaction bottom than to the previous one. In this case, depending on the temperature parameters in different reaction zones, the volumetric rate of water supply can be adjusted, while the total volume of water supplied is maintained within the range specified in the total volume.

The use of water in catalytic refining processes is generally a common practice. However, in the development options for "zeoforming" technologies, reactions have not yet been practiced to obtain the target product with a distributed supply of raw materials in two or more reaction zones and controlled addition of water to each reaction zone depending on the temperature in the catalyst layer, namely, depending on from fluctuations in the temperature field, during the processing of NGLs on a zeolite catalyst. To control temperature differences in each reaction volume, there are three temperature sensors, for example, thermocouples, located in the upper part, in the middle and in the lower part of the reaction volume in the catalyst bed. In this case, the larger the reaction volume, the greater the number of temperature control points must be provided to control the uniformity of the temperature field. For example, it is possible to arrange temperature sensors from the center to the walls and more temperature control points in the distribution over the catalyst bed. The need to control the temperature and uniformity of the temperature field is due to the nature of the reaction with the release of heat.

The method is carried out as follows:

A hydrocarbon stream, in particular associated petroleum gas (APG), which may be a by-product of oil production, is sent through the process line to the mixing chamber, or the mixing valve is also supplied with a water flow.

The proportions of the components supplied to the first reaction zone are 76...85 (hydrocarbons) - 15...24 (water). A zeolite catalyst based on ZSM-5 zeolite is loaded into each reaction zone. The reaction is carried out under the following parameters: temperature 550 ... 650°C, pressure 10 ... 12 atm., the reaction time is proportional to the volume of the reaction zones, depending on the volumetric feed rate of the raw material.

Further to the second and, if any, subsequent reaction zones, water and, depending on the embodiment, a hydrocarbon stream are supplied through the summed process pipelines. The volumetric water flow is adjustable. The number of reaction zones is determined by the performance of the installation, based on the fact that a larger volume is more prone to non-uniformity of the temperature field across the catalyst bed. The parameters of the distributed supply and the reaction carried out in various versions are shown in table 1.

A zeolite based on ZSM-5 with the following composition was used as a catalyst:

ZSM-5 zeolite modulus, SiO2/Al2O3, mol/mol: 43;

The proportion of zeolite of the pentasil group, wt. %: 68.

The proportion of catalyst components, wt. % (in terms of calcined at 550°С):

Silica: 72.5;

Aluminum oxide: 22.6;

Zinc oxide: 3.4;

Sodium oxide: 0.007;

Sum of REE oxides: 1.5.

However, the practice of using zeolite catalysts of a different composition with minor deviations in reaction parameters from the described embodiments and without compromising the quality of the resulting product is known.

The product stream after successive passage of all reaction volumes is divided into a hydrocarbon fraction of the product and an aqueous fraction of the product. The aqueous fraction of the product is withdrawn.

The hydrocarbon fraction of the product is further separated into a liquid hydrocarbon product and a gaseous product, in particular by fractionation and stabilization methods. The gaseous product may be further separated into a fraction of the gaseous product enriched in C3-C4 hydrocarbons and a fraction of the gaseous product enriched in C1-C2 hydrocarbons.

The main component of the liquid hydrocarbon product is C5+ hydrocarbons (hydrocarbons with five or more carbon atoms). Depending on the goals of a particular production, a liquid hydrocarbon product may contain not only C5+ hydrocarbons, but also various amounts of dissolved C1-C4 gases. In particular, in the production of motor gasoline, the presence of up to 3-5 wt. % of dissolved gases in summer gasolines and up to 5-7 wt. % of dissolved gases in winter gasolines. The gaseous product may include C1-C4 hydrocarbons, nitrogen, hydrogen and other inorganic gases, as well as heavier hydrocarbons. It is noted that it is possible to achieve a final boiling point of the resulting hydrocarbon product of less than 215°C, as well as a resin content in the product below 5 mg/cm3, to ensure uniformity and controllability of the process in terms of temperature, to simplify raw material logistics and, at the same time, to reduce the cost of raw materials used. In addition, the implementation of the invention leads to a reduction in coke deposits while maintaining sufficient catalytic activity of the catalyst.

Further, the implementation of the invention and its industrial applicability are illustrated by a number of examples.

For the experiments, we used the installation of the above scheme with equal volumes of the reaction zones of 3 liters, the catalyst loading volume was not more than 2 liters. for each reaction zone. Working pressure 10 - 12 atm.

A model APG mixture of the following composition was used as a raw material for experiments: normal paraffins - 79.05%, isoparaffins - 20.95%. The composition of the liquid hydrocarbon product is detailed in Table 2.

Example 1. (according to the prior art, without water, with one reaction volume)

Temperature: 550°C. Volumetric feed rate 338.7 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 40.0%; EYES 110.8.

Example 2. (according to the prior art, but with water, with one reaction volume

Supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively. Temperature: 550°C. Volumetric feed rate 338.7 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 33.9%; EYES 113.7.

Example 3

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 67% first reaction volume; 33% second reaction volume.

Water: 50% first reaction volume; 50% second reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2, respectively, 227.2/341.4 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 35.1%; EYES 113.9.

Example 4

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 2 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 30% first reaction volume; 70% second reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2, respectively, 268.9/356.0 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 34.8%; EYES 112.9.

Example 5

The supply of hydrocarbon fraction (APG) and water in the proportion of 85/15, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 271.8/349.5/401.8 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 33.8%; EYES 110.9.

Example 6

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 600°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 271.8/349.5/401.8 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 46.7%; EYES 111.6.

Example 7

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 650°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 271.8/349.5/401.8 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 55.8%; EYES 112.9.

Example 8

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 20% first reaction volume; 30% second reaction volume; 50% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 248.3/278.9/354.1 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 31.2%; EYES 113.1.

Example 9

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 70% first reaction volume; 30% second reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 198.5/250.4/376.3 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 44.2%; EYES 110.9.

Example 10

The supply of hydrocarbon fraction (APG) and water in the proportion of 85/15, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 70% first reaction volume; 30% second reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 195.5/248.4/372.3 h ^-1 . Pressure: 10 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 41.3%; EYES 108.9.

Example 11

The supply of hydrocarbon fraction (APG) and water in the proportion of 76/24, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 70% first reaction volume; 30% second reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 224.3/305.1/423.3 h ^-1 . Pressure: atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 35.4%; EYES 107.4.

Example 12

In this example, overheating was deliberately carried out in the third reaction volume. At the moment the temperature was raised to 600°C. The supply of hydrocarbon fraction (APG) and water was initially assumed in the proportion of 79/21, respectively.

With a uniform reaction, the distribution over the reaction volumes would be:

APG: 100% first reaction volume.

Water: in equal volumes everywhere - 33, (3)

To eliminate overheating, the water supply to the third volume was increased. Due to the additional water supplied to the second volume, the water ratio changed as follows: 30% of the first reaction volume; 30% second reaction volume; 40% third reaction volume.

The ratio of all supplied components (UVF - D, OF - A and water) was respectively: 76.3 / 23.7

The temperature was stabilized at a set value of 550°C. Reaction pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 43.1%; EYES 109.3.

Example 13

The supply of hydrocarbon fraction (APG) and water in the proportion of 76/24, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 100% first reaction volume.

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 600°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 301.8/367.5/432.8 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 45.2%; EYES 110.2.

Example 14

The supply of hydrocarbon fraction (APG) and water in the proportion of 84.8/15.2, respectively, was carried out distributed over 3 reaction volumes as follows:

APG: 60% first reaction volume; 40% second reaction volume

Water: 30% first reaction volume; 30% second reaction volume; 40% third reaction volume.

Temperature: 550°C. The volumetric feed rate for the reaction volumes R1/R2/R3, respectively, 212.8/278.5/384.1 h ^-1 . Pressure: 12 atm.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 46.7%; EYES 111.5.

Example 15 (comparative)

The conditions are similar to example 14 with the only difference that the water supply is carried out with a different distribution.

Water: 50% first reaction volume; 30% second reaction volume; 20% third reaction volume.

According to the test results, the yield of C5+ hydrocarbons per ton of raw materials: 43.9%; EYES 110.5.

Table 1. Examples of testing under various conditions. Example 1 2 3 four five 6 7 8 nine 10 eleven 12* 13 fourteen 15 UVF AND AND AND AND AND AND AND AND AND AND AND AND AND AND AND Temperature, °С 550 550 550 550 550 600 650 550 550 550 550 550 600 550 550 Pressure, atm. 12 12 12 12 12 12 12 12 12 10 10 12 12 12 12 Hydrocarbon fraction R1 one hundred one hundred 67 one hundred one hundred one hundred one hundred one hundred 70 70 70 one hundred one hundred 60 60 R2 - - 33 - - - - - thirty thirty thirty - - 40 40 R3 - - - - - - - - - - - - - - - Water, % R1 - one hundred 50 70 thirty thirty thirty 20 thirty thirty thirty thirty thirty thirty 50 R2 - - 50 thirty thirty thirty thirty thirty thirty thirty thirty thirty thirty thirty thirty R3 - - - - 40 40 40 50 40 40 40 40 40 40 20 Ratio of raw materials components, total UVF one hundred 84.8 84.8 84.8 85 84.8 84.8 84.8 84.8 85 76 76 76 84.8 84.8 Water - 15.2 15.2 15.2 15.0 15.2 15.2 15.2 15.2 15 24 24 24 15.2 15.2 TOTAL: one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred Volumetric feed rate, h ^-1 R1 338.7 371.5 227.2 268.9 271.8 271.8 271.8 248.3 198.5 195.5 224.3 301.8 301.8 212.8 240.1 R2 - - 341.4 356.0 349.5 349.5 349.5 278.9 250.4 248.4 305.1 367.5 367.5 278.5 298.7 R3 - - - - 401.8 401.8 401.8 354.1 376.3 372.3 423.3 432.8 432.8 384.1 359.9 results Output from / to C5 + per ton of raw materials 40.0 33.9 35.1 34.8 33.8 46.7 55.8 31.2 44.2 41.3 35.4 43.1 45.2 46.7 43.9 EYES 110.8 113.7 113.9 112.9 110.9 111.6 112.9 113.1 110.9 108.9 107.4 109.3 110.2 111.5 110.5

- * with local overheating in the moment

Table 2. Group composition of the liquid hydrocarbon product (wt.%) Example 1 2 3 four five 6 7 8 nine 10 eleven 12 13 fourteen 15 Paraffins 1.0 0.5 0.5 0.6 1.1 0.7 0.5 0.9 1.1 1.9 2.2 2.0 1.6 1.0 1.1 Isoparaffins 0.8 0.6 0.5 0.7 0.9 0.8 0.5 0.9 1.0 1.5 2.3 1.9 1.5 1.1 1.2 Naphthenes - - - - - - - - - - - - - - - Olefins - - - - - - - - - - - - - - - aromatic hydrocarbons 98.2 98.9 99.0 98.7 98.0 98.5 99.0 98.2 97.9 97.5 95.5 96.1 96.9 97.9 97.7 Naphthalene 1.3 0.4 0.5 0.9 1.1 1.4 2.6 2.8 2.8 2.4 1.2 1.4 1.2 2.9 2.4 Total one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred one hundred Benzene content 33.3 34.9 33.9 32.8 31.8 34.5 37.9 36.1 38.1 33.1 31.3 33.8 35.2 37.5 36.9

Claims (14)

1. A method for producing aromatic hydrocarbons from a wide fraction of light hydrocarbons in the gas phase, in which hydrocarbon feedstock and water are distributed distributed into a reactor that includes at least two consecutive independent reaction zones, or at least two series-connected reactors in such a way that water is supplied into the first and subsequent reaction zones so that water is supplied to each reaction volume, and, depending on the temperature parameters in different reaction zones, the volumetric rate of water supply can be controlled, while the supply of water and hydrocarbon fraction is carried out in the gas phase, and the total the ratio of raw materials and water is in the ranges of 76...85%/15...24%, respectively. 2. The method according to claim 1, in which the reaction takes place in two or three reaction volumes. 3. The method according to claim 1, in which the hydrocarbon fraction is supplied to the first reaction volume, water is supplied to the first and second reaction volumes. 4. The method according to claim 1, in which the hydrocarbon fraction and water are fed into the first and second reaction volumes. 5. The method according to claim 1, in which the hydrocarbon fraction is supplied to the first reaction volume, water is supplied to the first, second and third reaction volumes. 6. The method according to claim 1, in which the hydrocarbon fraction is supplied to the first and second reaction volumes, water is supplied to the first, second and third reaction volumes. 7. The method according to claim 1, in which water is supplied distributed in such a way that each subsequent reaction volume is supplied with water as much or more than the previous one. 8. The method according to claim 1, in which the hydrocarbon fraction is supplied only to the first reaction volume, and water is distributed distributed to the first and second reaction volumes in a ratio of % 30 ... 50 / 70 ... 50, respectively. 9. The method according to claim 1, in which the hydrocarbon fraction is supplied only to the first reaction volume, and water is supplied distributed to the first, second and third reaction volumes in a ratio of 20 ... 30 / 20 ... 30 / 40 ... 60%, respectively. 10. The method according to claim 1, in which the hydrocarbon fraction is supplied distributed to the first and second reaction volumes in a ratio of % 60 ... …30/20…30/40…60. 11. The method according to claim 1, in which to control temperature differences in each reaction volume, three temperature sensors are located. 12. The method according to claim 1, in which the product stream after sequential passage of all reaction volumes is separated into a hydrocarbon fraction of the product and an aqueous fraction of the product, and in which the main component of the target liquid hydrocarbon product is C5+ hydrocarbons. 13. The method according to claim 1, in which the hydrocarbon fraction and water are fed into the reaction zones mixed in the gas phase. 14. The method according to claim 1, in which associated petroleum gas is used as the hydrocarbon fraction.