RU2630774C1 - Method for hydraulic processing of hydrocarbon raw materials - Google Patents

Abstract

FIELD: oil and gas industry.

SUBSTANCE: method involves mixing heated liquid hydrocarbon raw mwterial with a diluent and hydrogen, contacting homogeneous raw mixture with catalyst in at least one reactor with at least one layer of catalyst to obtain hydrogenation, separation of the latter into the diluent and balance hydrogenate which is divided into commercial product, light hydrocarbon fraction and exhaust gas. Mixing is carried out to obtain homogeneous raw mixture, the catalyst contacts in the reactor with radial feed of raw material and at least two heat-exchange blocks located in catalyst layer, the balance hydrogenate is pre-reduced and heated in iiner space of at least one of the blocks of the heat-exchange elements, at that coolant is supplied to the inner space of the remaining units of the heat-exchange elements.

EFFECT: simplification of the method, exclusion of temperature rise in the reactor.

4 cl, 1 dwg

Description

The invention relates to methods for the hydroprocessing of hydrocarbons in the presence of a fixed catalyst bed and can find application in the refining industry.

For hydroprocessing processes, in which the chemical transformations of the components of the raw material are accompanied by the release of a significant amount of heat, it is important to ensure that the process is carried out in the region of optimal temperature under conditions close to isothermal.

Known and widely used method of hydrotreating [N.L. Solodova, N.A. Terentyev. Hydrotreating fuels. Kazan: Kazan Publishing House. state technol. University, 2008, p. 32], including mixing the raw material with fresh and circulating hydrogen-containing gas (hydrogen), heating in a heat exchanger and furnace, axial feeding into a catalytic reactor, cooling the reaction products in a heat exchanger, a refrigerator and separating them to obtain circulating hydrogen, which is purified from hydrogen sulfide, compress and recycle, and the unstable hydrogenate, which is reduced, is separated to obtain hydrocarbon gas and catalysis, which is divided into a commercial product, a light hydrocarbon fraction and stabilization gas tion.

The disadvantages of this method are the high energy consumption for hydrogen circulation, as well as increased gas and coke formation due to a rise in temperature in the reactor due to the heat of the hydroprocessing process.

Closest to the claimed invention, the control system, method and device for continuous liquid-phase hydroprocessing [RU 2411285, publ. 02/10/2011, IPC C10G 47/00, C10G 45/02]. The method includes mixing heated liquid hydrocarbon feedstock with a diluent and hydrogen, isolating a homogeneous feed mixture and contacting it with a catalyst in at least one reactor with an axial feed of the feedstock and at least one catalyst bed to provide blowing and hydrogenation, separating the latter into a diluent and a balance hydrogenate, which is divided into a commercial product, a light hydrocarbon fraction and exhaust (exhaust) gas. The diluent may be further mixed with the hydrocarbon fraction. To reduce the temperature rise in the reactors, cold hydrogen is fed between the catalyst beds and / or the reactors.

The disadvantages of this method are: increased gas and coke formation due to a rise in temperature in the reactor, complexity due to the need to supply cold hydrogen, high energy consumption for diluent circulation due to the large hydraulic resistance of the catalyst layer during axial feed.

The objective of the invention is the exclusion of temperature rise in the reactor, the simplification of the method and the reduction of energy consumption.

The technical result is the exclusion of temperature rise in the reactor by cooling the catalyst layer with reduced hydrogenated, simplifying the method by eliminating the allocation of a homogeneous feed mixture and supply of cold hydrogen, as well as reducing energy costs through the use of a reactor with a radial feed of raw materials.

The specified technical result is achieved by the fact that in the known method, comprising mixing heated liquid hydrocarbon feedstock with a diluent and hydrogen, contacting a homogeneous feed mixture with a catalyst in at least one reactor with at least one catalyst bed to produce hydrogenate, separating the latter into a diluent and balance hydrogenated, which is divided into a commercial product, a light hydrocarbon fraction and exhaust gas, the peculiarity is that the mixing is carried out with obtaining m of a homogeneous feed mixture, the contacting of which with the catalyst is carried out in a reactor with a radial feed of raw materials and at least two heat exchange units placed in the catalyst bed, and the balance hydrogenate is preliminarily reduced and heated in the inner space of at least one of the blocks of heat exchange elements, while refrigerant is fed into the interior of the remaining blocks of the heat exchange elements.

The separation of the hydrogenated balance is carried out by any method known in the art. As hydrocarbon feedstocks, straight-run or secondary hydrocarbon fractions can be used. Hydroprocessing is carried out by hydrogenation, or hydrotreating, or hydrocracking, or hydroisomerization, for example hydrodewaxing, or other processes carried out in the presence of hydrogen and a fixed catalyst, or by a combination of the above processes. The diluent may be further mixed with the hydrocarbon fraction.

Mixing to obtain a homogeneous raw mix allows to exclude the allocation of a homogeneous raw mix, which simplifies the method. Contacting the raw material mixture in the reactor with a radial feed of raw materials can reduce the hydraulic resistance, thereby reducing energy consumption for circulation. Placing the heat exchange units in the catalyst bed eliminates the temperature rise in the reactor due to cooling with reduced balance hydrogenate and refrigerant. Cold hydrogen is not supplied, which also simplifies the method.

For hydroprocessing, a homogeneous feed mixture obtained by mixing heated hydrocarbon feedstock 1, diluent 2 and hydrogen 3 is brought into contact with the catalyst in the reactor 4 with blocks of heat exchange elements 5 and 6 (two blocks are conventionally shown) placed in the catalyst bed 7. From reactor 4 hydrogenate is removed, which is divided into diluent 2 and balance hydrogenate 8, which is reduced, for example, by means of a throttle valve 9, is heated in the interior of at least one block of heat exchange elements 5 and yayut in the stabilization unit 10 to the commodity product 11, light hydrocarbon fraction 12 and the exhaust gas 13. The reactor 4 is further cooled refrigerant 14 supplied to the flow of heat exchange elements 6. Diluent 2 may be mixed with the hydrocarbon fraction 15 - shown by dotted lines.

The invention is illustrated by an example of hydrotreating a secondary distillate fraction of 150-350 ° C in order to increase its stability to oxidation by hydrogenation, for which a heated homogeneous liquid feed mixture (100 wt.%) Containing 25% of the secondary distillate fraction, 74.93% of the circulating hydrogenate and 0.07% hydrogen-containing gas, at 5.5 MPa and 280 ° C are fed into a reactor with a radial feed of raw materials, equipped with a catalyst basket with two blocks of radial-spiral type heat exchange elements filled with granular nickel-containing them a catalyst, the resulting hydrogenate is separated into a diluent and 25.07% of the balance hydrogenated, which is reduced to 0.8 MPa and at 264 ° C is fed to the first heat exchange unit, where it is heated to 276 ° C and separated to obtain 0.09% of the exhaust gas , 0.20% of the light hydrocarbon fraction and 24.78% of commercial marine fuel of the DMX brand in accordance with GOST R 54299-2010. Condensate of water vapor at 250 ° C and 4.0 MPa is supplied to the second block of heat-exchange elements as a refrigerant, and a steam-water mixture with the same temperature is removed from it. The estimated energy consumption for diluent circulation was 0.054 kWh / t of raw materials. The maximum temperature difference in the reactor was 1.4 ° C; no temperature rise was observed.

Under the conditions of the prototype, the estimated energy consumption for the circulation of the diluent amounted to 0.283 kWh / t of raw materials. The temperature rise in the reactor was 9.5 ° C.

From the example it follows that the proposed method is simpler, allows to reduce energy consumption, eliminates the temperature rise in the reactor and can find application in the oil refining industry.

Claims (4)

1. The method of hydroprocessing of hydrocarbon feedstock, comprising mixing heated liquid hydrocarbon feedstock with a diluent and hydrogen, contacting the homogeneous feed mixture with a catalyst in at least one reactor with at least one catalyst bed to produce hydrogenate, separating the latter into a diluent and balance hydrogenate, which divided into a commercial product, a light hydrocarbon fraction and exhaust gas, characterized in that the mixing is carried out to obtain a homogeneous feed mixture, the activation of which with the catalyst is carried out in a reactor with a radial feed of raw materials and at least two heat-exchange units placed in the catalyst bed, the hydrogenated hydrogenate is preliminarily reduced, heated in the inner space of at least one of the heat-exchange element blocks, while in the inner space of the remaining heat-exchange blocks elements supply refrigerant. 2. The method according to p. 1, characterized in that straight-run or secondary hydrocarbon fractions are used as the hydrocarbon feed. 3. The method according to p. 1, characterized in that the hydroprocessing of the hydrocarbon feed is carried out by hydrogenation, or hydrotreating, or hydrocracking, or hydroisomerization, for example, hydrodewaxing, or other processes carried out in the presence of hydrogen and a fixed catalyst, or by any combination of the above processes. 4. The method according to p. 1, characterized in that the diluent is mixed with the hydrocarbon fraction.

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