RU2033418C1

RU2033418C1 - Method of production of jet fuel

Info

Publication number: RU2033418C1
Application number: RU94025537A
Authority: RU
Inventors: И.С. Езунов; Л.Г. Гебель; А.К. Савинков; В.Н. Кузьмин; Н.П. Селиванов
Original assignee: Езунов Иван Семенович; Гебель Людмила Гергиевна; Савинков Анатолий Кузьмич; Селиванов Николай Павлович
Priority date: 1994-07-20
Filing date: 1994-07-20
Publication date: 1995-04-20
Also published as: RU94025537A

Abstract

FIELD: petroleum refining. SUBSTANCE: invention consists in electric demineralization of various petroleums in an electric dehydrator with a system of electrodes located at two levels, the height gradient between them being within 0.05 to 0.1 of the relative path section coinciding with the mean vector of petroleum current in the zone of the maximum midsection. After demineralization the petroleum current is fed to the atmospheric distillation column with a pack of nozzles and two branch pipes tangentially arranged in the column body. The column is provided with an internal cylindrical current deflector, whose diameter matches up with the body diameter in the feed zone as (0.59 - 0.75) to 1, and the height range of the petroleum currents inlet makes up 0,.21 to 0.28 of the column height from the column bottom base. Withdrawal of kerosine fraction at 140 to 240 C is conducted in the column height range equal to (0.58-0.81) counting from the column bottom base. The extracted kerosine fraction is divided into 3 currents, the third current in the mixture with 30 to 35 percent by mass of the residual kerosine fraction after petrol redistillation is fed to hydrofining. O.007 to 0.008 per cent by mass concentrate of a mixture of additives of naphthenic acids and ionol is introduced into the obtained product. EFFECT: facilitated procedure. 33 cl, 1 tbl, 6 dwg

Description

Изобретение относится к нефтепереработке и, конкретно, к получению реактивного топлива. Известны способы получения реактивного топлива из различных нефтей (малосерных, серных, высокосернистых), включающие стадии электрообессоливания с подачей потока нефти через систему электродов, расположенных в электродегидраторах, атмосферной и/или атмосферно-вакуумной перегонки обессоленной нефти с использованием колонн атмосферной перегородки с выделением керосиновой фракции, гидроочистки полученной керосиновой фракции в присутствии катализатора и использованием реакторов гидроочистки с последующим компаундированием полученных в процессах перегонки и гидроочистки фракций. The invention relates to oil refining and, specifically, to the production of jet fuel. Known methods for producing jet fuel from various oils (low-sulfur, sulfur, high-sulfur), including the stage of electrodesalting with the flow of oil through a system of electrodes located in electrodehydrators, atmospheric and / or atmospheric-vacuum distillation of desalted oil using columns of the atmospheric partition with the separation of the kerosene fraction hydrotreating the obtained kerosene fraction in the presence of a catalyst and using hydrotreating reactors with subsequent compounding obtained s in distillation and hydrotreating processes fractions.

Указанному способу свойственны такие недостатки, как относительно невысокие качества и выход целевых продуктов, а также повышенные энергозатраты на процесс и недостаточная эффективность конструктивных решений технологических схем. The specified method is characterized by such disadvantages as the relatively low quality and yield of the target products, as well as increased energy consumption for the process and the lack of efficiency of structural solutions to technological schemes.

Целью данного изобретения является устранение указанных недостатков. The aim of this invention is to remedy these disadvantages.

Поставленная цель достигается способом получения реактивного топлива из малосернистых и/или сернистых, и/или высокосернистых нефтей путем электрообессоливания последних пропусканием потока через систему сетчато и/или ячеисто расположенных не менее чем в двух уровнях электродов, перекрывающих в совокупности высотный диапазон электродегидратора преимущественно в верхней половине высоты его корпуса, причем градиент высоты между уровнями электродов на пути восходящего потока нефти составляет 0,05-0,1 условного отрезка пути, совпадающего со средним вектором перемещения потока нефти в зоне наибольшего миделя электродегидратора, проходимого потоком за 1 час перемещения со средней скоростью процесса электрообессоливания. При перегонке обессоленной нефти используют колонны атмосферной перегонки, снабженные пакетами перекрестноточных насадок, размещенными с высотным или высотноугловым смещением адекватно температурным зонам конденсации паров, при этом по крайней мере часть пакетов размещены в зоне конденсации керосиновой фракции, и перегонку проводят при подаче нефти в колонны по крайней мере через два патрубка, тангенциально расположенные в корпусе колонны в зоне питания, снабженной внутренним цилиндрическим отражателем потока, диаметр которого соотносится с диаметром корпуса колонны в зоне питания как (0,59-0,75):1, а высотный диапазон ввода потоков нефти составляет (0,21-0,28) высоты колонны от низа днища колонны. This goal is achieved by a method of producing jet fuel from low-sulfur and / or sulfur, and / or high-sulfur oils by electrosalting the latter by passing a stream through a system of mesh and / or mesh located at least two electrode levels, covering in aggregate the altitude range of the electric dehydrator mainly in the upper half the height of its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05-0.1 conventional section of the path, matching with the average displacement vector of the oil flow in the zone of the largest midship of the electric dehydrator, passed by the stream in 1 hour of movement with an average speed of the process of electric desalination. At distillation of desalted oil, atmospheric distillation columns are used, equipped with packages of cross-flow nozzles placed with a high-altitude or high-angle displacement adequate to the temperature zones of vapor condensation, at least part of the packages are placed in the condensation zone of the kerosene fraction, and distillation is carried out when oil is supplied to the columns at least through at least two nozzles tangentially located in the column body in the supply zone, equipped with an internal cylindrical flow reflector, the diameter of which is related to the diameter of the column body in the feed zone as (0.59-0.75): 1, and the altitude range for introducing oil flows is (0.21-0.28) the height of the column from the bottom of the bottom of the column.

Вывод керосиновой фракции с температурой кипения 140-240^оС ведут в высотном интервале колонны первичной разгонки, составляющем 0,58-0,81, считая от низа днища колонны или с превышением соответственно нижней и верхней отметок диапазона вывода керосиновой фракции на величину 0,37-0,53 относительно оси ввода патрубков, подающих парогазонефтяную смесь в зону питания колонны. Выделенную керосиновую фракцию делят на три целевые потока в объемном соотношении (1,2-8,5):(12,8-15,5):(9,5-11,8) соответственно для последующей подачи на гидроочистку третьего потока в смеси с 30-35 мас. остаточной керосиновой фракции, полученной при вторичной перегонке бензиновой фракции. В продукт гидроочистки вводят через демпферную емкость предварительно приготовленный концентрат смеси присадок нафтеновых кислот и ионола в количестве 0,007-0,008 мас. и в массовом соотношении присадок (1-1,5):2.Conclusion kerosene fraction having a boiling point ^of 140-240 C are in the height range of the primary distillation column constituting 0,58-0,81, counting from the bottom of the column bottom or in excess of the lower and upper band output marks kerosene fraction by the value 0.37 -0.53 relative to the axis of entry of the pipes supplying the gas-oil mixture to the feed zone of the column. The extracted kerosene fraction is divided into three target streams in a volume ratio (1.2-8.5) :( 12.8-15.5) :( 9.5-11.8), respectively, for subsequent supply to the hydrotreating of the third stream in the mixture with 30-35 wt. residual kerosene fraction obtained by secondary distillation of the gasoline fraction. A pre-prepared concentrate of a mixture of additives of naphthenic acids and ionol in an amount of 0.007-0.008 wt. and in a mass ratio of additives (1-1.5): 2.

Электрообессоливание нефти проводят в электродегидраторах с горизонтально-ориентированным корпусом цилиндрической или составной конфигурации и рабочим объемом 80-200 м³, в электродегидраторах с корпусом сферической или сфероидальной, и/или эллипсовидной и/или овоидальной, и/или каплевидной формы, в электродегидраторах с цилиндрическим корпусом и выпуклокриволинейным торцевыми участками, и/или тороидальной формы, в электродегидраторах, продольная ось корпуса, по крайней мере, часть которых ориентирована вертикально, в электродегидраторах, продольная ось корпуса, по крайней мере, часть которых ориентирована горизонтально или под углом к горизонту.Electrical desalting of oil is carried out in electric dehydrators with a horizontally oriented body of cylindrical or composite configuration and a working volume of 80-200 m ³ , in electric dehydrators with a body of spherical or spheroidal and / or ellipsoidal and / or ovoid and / or drop-shaped, in electric dehydrators with a cylindrical body and convex curvilinear end sections, and / or toroidal shape, in electric dehydrators, the longitudinal axis of the body, at least part of which is oriented vertically, in the electric dehydrate peaks, the longitudinal axis of the body, at least some of which are oriented horizontally or at an angle to the horizontal.

Подачу нефти в колонне атмосферной перегонки осуществляют через патрубки, расположенные с углом разведения точек пересечения оcей патрубков с корпусом колонны в интервале 30-180^о с односторонней тангенциальной закруткой подаваемого потока, через патрубки, ось и внутренняя горловина одного из которых ориентируют поток подаваемой через него нефти в зоне питания колонны непосредственно на пересечение с аналогичным потоком, подаваемым через другой патрубок преимущественно в зоне выхода его из внутренней горловины последнего, через патрубки, оси которых ориентированы параллельно касательных к корпусу внутреннего цилиндрического отражателя и радиально удалены от условной точки касания с корпусом отражателя на расстояние b удовлетворяющее условию
b ≥ 0,25 (R_к R_о)
где R_к радиус с колонны в зоне питания;
R_о радиус отражателя.Oil is supplied in an atmospheric distillation column through nozzles located at an angle of dilution of the points of intersection of the axes of the nozzles with the column body in the range of 30-180 ^о with a one-sided tangential twist of the feed stream, through the nozzles, the axis and the inner neck of one of which orient the flow of oil supplied through it in the feed zone of the column directly to the intersection with a similar stream supplied through another nozzle, mainly in the zone of exit from the inner neck of the latter, through the nozzle and whose axes are oriented parallel to the tangent to the body of the inner cylindrical reflector and radially removed from the conventional point of tangency with the reflector body by a distance satisfying the condition b
b ≥ 0.25 (R _to R _o )
where R _{k is the} radius from the column in the feed zone;
R _{about the} radius of the reflector.

Перегонку проводят в колонне, цилиндрический отражатель в зоне питания которой установлен эксцентриситетно продольной оси колонны, выполнен с переменным радиусом кривизны в поперечном сечении и соединен с корпусом колонны кольцевой мембранной плоской, и/или ломаной, и/или криволинейной, и/или комбинированной конфигурации в поперечном сечении. The distillation is carried out in a column, a cylindrical reflector in the feed zone of which is mounted an eccentric longitudinal axis of the column, made with a variable radius of curvature in cross section and connected to the column body with an annular membrane, and / or broken, and / or curved, and / or combined configuration in cross section.

При перегонке используют колонну атмосферной перегонки, в которой регулярные пакеты перектрестноточных посадок выполнены из пространственно деформированных элементов из листовой нержавеющей стали, причем высота пакетов обеспечивает перекрытие температурных градиентов 2-8^оС по высоте колонны, а площадь прохода паров через них составляет 38-81% относительно поперечного сечения колонны.In the distillation of atmospheric distillation column is used, in which regular packets perektrestnotochnyh landings made of spatially deformed elements from stainless steel sheet, wherein the overlap provides a package height of the temperature gradient of 2-8 ^{° C} by adjustment of the column and a vapor passage therethrough area is 38-81% relative to the cross section of the column.

Перегонку в колонне атмосферной перегонки проводят при скорости прохождения паров разгоняемых фракций по крайней мере равной 1,0-1,7 м/с. Distillation in an atmospheric distillation column is carried out at a vapor velocity of the accelerated fractions of at least 1.0-1.7 m / s.

При гидроочистке керосиновой фракции, пропускаемой не менее чем через два реактора, последние обвязаны по ходу газопаровой продуктовой смеси с возможностью прямого или обратного прохождения последней через слои катализатора, либо с возможностью их параллельного или попеременного раздельного включения в работу адекватно заданным объемам или степени гидроочистки бензиновой фракции. When hydrotreating a kerosene fraction, passed through at least two reactors, the latter are tied along the gas-steam product mixture with the possibility of direct or reverse passage of the latter through the catalyst beds, or with the possibility of their parallel or alternate separate inclusion in operation adequately to the specified volumes or degree of hydrotreating of the gasoline fraction .

При гидроочистке в реакторах гидроочистки используют алюмокобальтовый, или алюмоникельмолибденовый, или цеалитсодержащий катализаторы гидроочистки, или их сочетания. When hydrotreating in hydrotreating reactors, aluminum-cobalt, or aluminum-nickel-molybdenum, or zealite-containing hydrotreating catalysts, or combinations thereof are used.

При гидроочистке используют по крайней мере один реактор гидроочистки по крайней мере в верхней зоне которого слой катализатора пригружен дискретным, и/или комбинированным парогазопроницаемым элементом из инертного, коррозионнотермостойкого материала, или сочетания материалов с аналогичными свойствами, причем по крайней мере входная поверхность слоя катализатора на пути движения парогазопродуктового потока выполнена превышающей площадь сечения реактора гидроочистки, слой катализатора насыпан с наклоном по крайней мере части по крайней мере верхней поверхности. When hydrotreating, at least one hydrotreating reactor is used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-gas-permeable element of an inert, corrosion-resistant material, or a combination of materials with similar properties, with at least the inlet surface of the catalyst layer on the way the movement of the gas-vapor product stream is greater than the cross-sectional area of the hydrotreatment reactor, the catalyst layer is poured with at least a slope towards ayney least the upper surface.

Верхний слой катализатора насыпан с коническим, и/или переменно ломанным, и/или переменно криволинейным, и/или комбинированным наклоном от центральной зоны к стенкам корпуса реактора. The upper catalyst layer is poured with a conical, and / or alternately broken, and / or alternately curved, and / or combined slope from the central zone to the walls of the reactor vessel.

В верхней части насыпного массива катализатор снабжен включениями из инертных элементов с аэрогидравлическим сопротивлением, меньшим чем у эквивалентного по объему слоя катализатора. In the upper part of the bulk array, the catalyst is equipped with inclusions of inert elements with aerohydraulic resistance less than that of an equivalent volume catalyst layer.

При гидроочистке используют реактор, в котором элементы с повышенной аэрогидравлической проницаемостью выполнены в виде сетчатых и/или перфорированных цилиндрических или многогранных стаканов или патрубков, или в виде насыпных вкраплений из инертных частиц радиусом, большим, чем радиус или приведенный радиус частиц катализатора, или выполнена комбинированной с насыпным сердечником и гибкой, или жесткой сетчаткой, или перфорированной оболочкой. Hydrotreating uses a reactor in which elements with increased aero-hydraulic permeability are made in the form of mesh and / or perforated cylindrical or polyhedral glasses or nozzles, or in the form of bulk inclusions of inert particles with a radius greater than the radius or reduced radius of the catalyst particles, or made combined with a bulk core and a flexible, or rigid retina, or perforated shell.

Часть слоя катализатора смешана с более крупными частицами инертного материала. Part of the catalyst bed is mixed with larger particles of inert material.

Соотношение частиц выполнено переменным с убыванием процентной доли инертных частиц в направлении движения парогазопродуктового потока, подвергаемого гидроочистке. The particle ratio is made variable with a decrease in the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating.

Часть реакторов гидроочистки устанавливают с наклоном продольной оси относительно горизонта, или с горизонтально ориентированной продольной осью. Some hydrotreating reactors are installed with a slope of the longitudinal axis relative to the horizon, or with a horizontally oriented longitudinal axis.

По крайней мере один реактор гидроочистки может быть выполнен тороидальным. At least one hydrotreating reactor may be toroidal.

Изобретение поясняется чертежом, где на фиг. 1 представлена принципиальная схема проведения способа получения дизельного топлива; на фиг. 2 поперечный разрез электродегидратора с электродами 9; на фиг. 3 колонна с корпусом, общий вид; на фиг. 4 разрез по А-А на фиг; 3; на фиг. 5 пакет перекрестноточных насадок; на фиг. 6 расположение штуцеров ввода сырья (разрез по А-А на фиг. 3 вариантное решение). The invention is illustrated in the drawing, where in FIG. 1 is a schematic diagram of a method for producing diesel fuel; in FIG. 2 is a cross-sectional view of an electric dehydrator with electrodes 9; in FIG. 3 column with a hull, general view; in FIG. 4 is a section along AA in FIG. 3; in FIG. 5 pack crossflow nozzles; in FIG. 6 location of the raw material input fittings (section along AA in FIG. 3 is an alternative solution).

Колонна состоит из корпуса 10, узла 11 ввода нефти, перекрестноточных насадок 12, 13, 14 штуцеры ввода сырья в колонну атмосферной перегонки; 9 электроды электрогидратора. The column consists of a housing 10, an oil input unit 11, cross-flow nozzles 12, 13, 14, raw material input fittings into an atmospheric distillation column; 9 electrodes of an electrohydrator.

Согласно принципиальной схеме способ проводят следующим образом. According to the schematic diagram, the method is carried out as follows.

Исходную нефть по линии 1 направляют на блок электрообессоливания 2. Затем по линии 3 подают на блок атмосферной или атмосферно-вакуумной перегонки 4. Полученную керосиновую фракцию направляют по линии 5 в блок гидроочистки 6, откуда по линии 7 в блок компаундирования 8. The initial oil is sent through line 1 to the electric desalting unit 2. Then, through line 3, it is sent to the atmospheric or atmospheric vacuum distillation unit 4. The resulting kerosene fraction is sent via line 5 to the hydrotreatment unit 6, from where, through line 7 to the compounding unit 8.

Изобретением предусмотрены также вариации различных стадий получения реактивного топлива, условно не показанные на принципиальной схеме (фиг. 1). The invention also provides for variations of the various stages of producing jet fuel, conventionally not shown in the schematic diagram (Fig. 1).

Данный способ позволяет получать реактивное топливо со стабильно высокими эксплуатационными качествами при снижении технологических энергозатрат на 5-18% на различных этапах разгонки, гидроочистки реактивного топлива, компаундирование и смешивание с присадками и повышает выход топлива на 2-4 мас. This method allows to obtain jet fuel with a stable high performance while reducing technological energy consumption by 5-18% at various stages of distillation, hydrotreating jet fuel, compounding and mixing with additives and increases the fuel yield by 2-4 wt.

Способ иллюстрирован примером, представленным в таблице. The method is illustrated by the example presented in the table.

Claims

1. METHOD FOR PRODUCING REACTIVE FUEL from low-sulfur, and / or sulfur, and / or high-sulfur oils by electric desalting of the latter by passing an oil stream through a system of electrodes located in electric dehydrators, atmospheric and / or atmospheric-vacuum distillation of desalted oil using atmospheric distillation columns, s the separation of the kerosene fraction, hydrotreating the obtained kerosene fraction in the presence of a catalyst using hydrotreating reactors, followed by compounding the obtained in the processes of distillation and hydrotreating of fractions, characterized in that the electric desalting of the oil is carried out by passing a stream through a system of mesh and / or mesh located at least two levels of electrodes, covering in aggregate the altitude range of the electric dehydrator mainly in the upper half of the height of its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05 0.1 conventional section of the path, which coincides with the average vector of movement of the oil flow in the zone of greatest m dividing the electrical dehydrators traversed stream for 1 hour with an average moving speed elektroobessolivaniya process; during distillation of desalted oil, atmospheric distillation columns are used, equipped with packages of cross-flow nozzles placed with a high-altitude or high-angle displacement adequate to the temperature zones of vapor condensation, at least some of the packets are placed in the condensation zone of the kerosene fraction, and distillation is carried out when oil is supplied to the columns at least through at least two nozzles tangentially located in the column body in the supply zone, equipped with an internal cylindrical flow reflector, the diameter of which correlates with the diameter of the column body in the feed zone as (0.59 0.75): 1, and the altitude range for introducing oil flows is (0.21 0.28) the height of the column from the bottom of the bottom of the column, the output of the kerosene fraction with a boiling point of 140,240 ^o lead in the altitude range of the primary acceleration column, comprising (0.57 0.81) the height of the column, counting from the bottom of the bottom of the column or exceeding the lower and upper marks of the output range of the kerosene fraction by (0.37 0.53) heights columns relative to the input axis of the nozzles supplying oil to the supply zone of the column, you The refined kerosene fraction is divided into three target streams in their volume ratio (1.2 8.5) (12.8 15.5) (9.5 11.8), respectively, for subsequent supply to the hydrotreating of the third stream in a mixture with 30 to 35 wt. . of the residual kerosene fraction obtained by the secondary distillation of the gasoline fraction, a pre-prepared concentrate of a mixture of additives of naphthenic acids and ionol in an amount of 0.007 to 0.008 wt. and the mass ratio of additives in their mixture (1 1,5) 2.

2. The method according to claim 1, characterized in that the electric desalting of oil is carried out in electric dehydrators with a horizontally oriented case of cylindrical or composite configuration and a working volume of 80,200 m ³ .

3. The method according to p. 1, characterized in that the electric desalting of the oil is carried out in electric dehydrators with a spherical or spheroidal and / or ellipsoidal and / or ovoid and / or teardrop-shaped body.

4. The method according to p. 1, characterized in that the electric desalting of the oil is carried out in electrohydrators with a cylindrical body and convex curved end sections, and / or toroidal shape.

5. The method according to p. 4, characterized in that the electric desalting of the oil is carried out in electrohydrators, the longitudinal axis of the housing at least part of which is oriented vertically.

6. The method according to p. 4, characterized in that the electric desalting of the oil is carried out in electrohydrators, the longitudinal axis of the body at least part of which is oriented horizontally or at an angle to the horizontal.

7. The method according to claims 1-6, characterized in that the oil in the atmospheric distillation column is supplied through nozzles located at an angle of dilution of the points of intersection of the axes of the nozzles with the column body in the range of 30 180 ^{° C.} with a one-sided tangential swirl of the feed stream.

8. The method according to claims 1 to 7, characterized in that the oil is supplied to the atmospheric distillation column through nozzles, the axis and the inner neck of one of which orient the flow of the vapor-liquid oil mixture supplied through it in the feed zone of the column directly to the intersection with a similar stream, fed through another pipe, mainly in the zone of exit from the inner neck of the latter.

9. The method according to claims 1 to 8, characterized in that the oil is supplied to the atmospheric distillation column through nozzles whose axes are oriented parallel to the tangent to the body of the internal cylindrical reflector and radially removed from the conditional contact point with the reflector body by a distance b satisfying the condition b≥0.25 (R _to -R _o ), where R _{to the} radius of the column in the feed zone, R _{about the} radius of the reflector.

10. The method according to claims 1 to 9, characterized in that the distillation is carried out in a column, a cylindrical reflector in the feed zone of which is installed eccentric to the longitudinal axis of the column.

11. The method according to claims 1 to 10, characterized in that the distillation is carried out in an atmospheric distillation column, the cylindrical reflector of which is made with a variable radius of curvature in cross section.

12. The method according to claims 1 to 11, characterized in that the distillation is carried out in an atmospheric distillation column, the cylindrical reflector of which is connected to the column body with an annular membrane of a flat and / or broken, and / or curved, and / or combined configuration in cross section .

13. The method according to PP. 1 12, characterized in that the distillation uses an atmospheric distillation column in which regular packages of cross-flow nozzles are made of spatially deformed stainless steel sheet elements, and the height of the packages provides overlapping temperature gradients of 2 8 ^o C along the height of the column, and the area of vapor passage through they are 38 81% relative to the cross section of the column.

14. The method according to PP. 1 13, characterized in that the distillation in the column of atmospheric distillation is carried out at a speed of passage of the vapor of the dispersed fractions of at least 1.0 1.7 m / s.

15. The method according to PP. 1 14, characterized in that when hydrotreating a kerosene fraction, passed through at least two reactors, the latter are tied along the gas-vapor product mixture with the possibility of direct or reverse passage of the latter through the catalyst layers, or with the possibility of their parallel or alternately separate inclusion in work adequately specified volumes and degrees of hydrotreating the gasoline fraction.

16. The method according to PP. 1 to 15, characterized in that when hydrotreating in hydrotreating reactors use aluminum cobalt or aluminum-nickel-molybdenum, or zeolite-containing hydrotreating catalysts, or combinations thereof.

17. The method according to PP. 1 16, characterized in that at least one hydrotreating reactor is used in hydrotreating, at least in the upper zone of which the catalyst layer is immersed with a discrete and / or combined vapor-gas-permeable element of an inert or corrosion-resistant material or a combination of materials with similar properties, at least the inlet surface of the catalyst layer along the path of the vapor-gas product stream is made exceeding the cross-sectional area of the hydrotreatment reactor.

18. The method according to PP. 1 to 17, characterized in that when hydrotreating use a reactor in which the catalyst layer is deposited with an inclination of at least part of at least the upper surface.

19. The method according to PP. 1 to 18, characterized in that when hydrotreating a reactor is used, in which at least the upper catalyst layer is poured with a conical and / or alternately broken and / or alternately curved and / or combined slope from the central zone to the walls of the reactor vessel.

20. The method according to PP. 1 19, characterized in that the hydrotreatment uses a reactor in which the catalyst, at least in the upper part of the bulk array, is equipped with inclusions of inert elements with aerohydraulic resistance less than that of an equivalent volume catalyst layer.

21. The method according to PP. 1 to 20, characterized in that when hydrotreating a reactor is used, in which elements with increased aerohydraulic permeability are made in the form of mesh, and / or perforated cylindrical, or polyhedral glasses or nozzles.

22. The method according to PP. 1 21, characterized in that the hydrotreatment uses a reactor in which part of the aerohydraulically permeable elements is made in the form of bulk inclusions of inert particles with a radius greater than the radius or reduced radius of the catalyst particles.

23. The method according to item 22, wherein the hydrotreating uses a reactor in which at least part of the elements with high aero-hydraulic permeability is made combined with a bulk core and a flexible or rigid retina or perforated shell.

24. The method according to PP. 19 to 23, characterized in that when hydrotreating use a reactor in which at least in the upper zone at least part of the catalyst layer is mixed with larger particles of inert material.

25. The method according to PP. 19 24, characterized in that when hydrotreating use a reactor in which the particle ratio is made variable with a decrease in the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreatment.

26. The method according to PP. 1 26, characterized in that during hydrotreating at least part of the hydrotreating reactors are installed with a slope of the longitudinal axis relative to the horizon.

27. The method according to PP. 1 26, characterized in that when hydrotreating use at least part of the reactor with a horizontally oriented longitudinal axis.

28. The method according to PP. 1 27, characterized in that during hydrotreating at least one hydrotreating reactor is made toroidal.

29. The method according to PP. 1 28, characterized in that the compounding of gasoline fractions is carried out in a tank equipped with at least one injector, which is installed in the lower half of the tank at an angle to the horizontal axis.

30. The method according to PP. 1 28, characterized in that the compounding is carried out in a tank in which the injector is mounted on a rigid inner pipe in the lower third of the central zone of the tank with an upward slope of the injected gas stream.

31. The method according to PP. 1 29, characterized in that the compounding is carried out in a tank in which the injector is installed by means of a tangentially mounted nozzle.

32. The method according to PP. 1 29, characterized in that the compounding is carried out using at least two injectors fixed on tangentially mounted nozzles with an opposite flow swirl.

33. The method according to PP. 1 27, characterized in that the compounding is carried out using at least two injectors mounted with the possibility of reactive rotation in the lower or bottom of the tank.