WO2015081395A1

WO2015081395A1 - Reactor with combined dynamic flow system for treating oil and derivatives thereof

Info

Publication number: WO2015081395A1
Application number: PCT/BR2014/000276
Authority: WO
Inventors: José Roberto NUNHEZ; Everton MORAES MATOS; Sebastian MORENO CÁRDENAS; José Luis GOMEZ VERGEL; Helver Crispiniano ALVAREZ CASTRO; Carlos Alberto DE ARAUJO MONTEIRO; Vivian PASSOS DE SOUZA
Original assignee: Petróleo Brasileiro S.A. - Petrobras; Universidade Estadual De Campinas - Unicamp
Priority date: 2013-12-06
Filing date: 2014-08-14
Publication date: 2015-06-11
Also published as: BR102013031411B8; BR102013031411A2; BR102013031411B1; AR098578A1; WO2015081395A8; UY35826A

Abstract

The present invention describes a reactor (1) for treating oil and oil derivatives, which consists of a central body (2) with a countercurrent flow system interconnected to a plurality of lateral bodies (3) with a cocurrent flow system; also described is a method for treating oil and oil derivatives.

Description

COMBINED FLUIDODYNAMIC REACTOR FOR THE TREATMENT OF OIL AND ITS DERIVATIVES

FIELD OF INVENTION

The present invention is in the field of processes using pressure vessels (atmospheric pressure or higher) and their application in chemical and / or biochemical unit operations under combined fluid-dynamic regime (co-current and counter-current).

More specifically, it deals with the invention of hydrotreating and / or hydrocracking hydrocarbon streams from the processing of petroleum and its derivatives, including streams from atmospheric distillation, vacuum distillation, retarded coking and catalytic cracking. co-processing of renewable origin cargo (bio-loads).

BACKGROUND OF THE INVENTION

Conventional Hydrotreating (HDT) and Hydrocracking (HCC) units of petroleum fractions, whether or not co-processed, adopt trickle bed reactors. In this type of reactor, the catalyst remains motionless (fixed bed) supported by trays, while the charge and hydrogen pass through it for hydrogenation and hydrocracking reactions to occur. Typically, the hydrogen-rich charge and gas are fed into the top section of the reactor, that is, in downward flow current. These reactors operate in multiphase regime, in which the solid phase is the catalyst; and the gas phase is hydrogen rich gas and the vaporized fraction of the charge; and the liquid phase is the net fraction of the charge. TECHNICAL STATE

The Co-flowing Flow Hydrotreating Process, a technology widely used to improve the quality of petroleum fractions, mainly involves the reactions of hydrodesulfurization (conversion of organosulfuric compounds into their corresponding hydrocarbons and H ₂ S), hydrodesunditrogenation (conversion of nitrogenous compounds into their corresponding hydrocarbons and NH ₃ ), hydrodesaromatization (hydrogenation of aromatic compounds to naphthenics), hydrogenation of olefins, among others. As the load distillation end point increases, the concentration of polysubstituted sulfur compounds increases. Increasing the degree of substitution in these compounds is known to make them more refractory to hydrodesulfurization (HDS) reactions, mainly due to the impedance of the sulfur molecule, which hinders its access to the catalyst's active site and, consequently, its hydrogenation. corresponding hydrocarbon and H ₂ S.

In the conventional process of HDS in co-current flow regime of petroleum fractions, with or without co-processing, the H2S concentration increases along the axial axis of the reactor. As a result, the H2S concentration becomes higher as the reaction progresses to the lower reactor zone, where more refractory sulfur compounds are expected. Regarding the H2 concentration profile, the opposite of H2S behavior is observed, being also responsible for the decrease of HDS rates along the reactor axial axis (top - bottom direction).

It is widely recognized in the literature that, in addition to decreasing the partial pressure of H2 in the reactor, H2S is responsible for the strong inhibition of hydrodesulfurization (HDS) reactions, especially of the more refractory organosulfur compounds, as a result of competitive adsorption on the catalyst. In this sense, the conventional co-current HDS process is not an optimized configuration for deep desulphurization of petroleum fractions, requiring for this purpose the use of high operational severity (reduction of process load flow or increase of reactors volume or increase of pressure or increased reaction temperature).

Hydrocracking (HCC) is the process in which petroleum fractions heavier than the distillation range of diesel, whether or not co-processed, are converted, in the presence of catalyst, hydrogen and appropriate operating conditions (pressure, temperature and contact time), in light products of higher added value (naphtha, kerosene, diesel oil) and unconverted residue, the latter can be used in the production of lubricants or as fillers of other processes (Delayed Coking, Viseduction, Fluid-Cracking). Catalytic, among others).

Generally speaking, HCC involves two distinct reaction steps: hydrotreating the cargo followed by hydrocracking it. The first step is responsible for the removal of sulfur and nitrogen contaminants in the form of H ₂ S and NH ₃ , also accompanied by aromatic saturation reactions, hydrogenation of olefins, hydrodemetallization (hydrogenation of metallic compounds), hydrodeoxygenation (hydrogenation of oxygenated compounds). and some conversion of heavy to light compounds, depending on the operating condition and catalytic system employed.

In the hydrocracking reaction step, the heavy fractions are converted to lighter compounds. Although highly capital intensive and with a high operating cost, this process is extensively used in refining as it has significant flexibility in naphtha, kerosene and diesel production, depending on the operating conditions employed, catalyst types and process configuration (one or two stages). , with or without intermediate gas separation), transforming low value added loads into excellent quality fuels.

In the single stage HCC configuration without intermediate gas separation, all effluent obtained in the Hydrotreating, including much of the H ₂ S and NH ₃ formed in this first step, is sent to the section containing the hydrocracking catalyst. In this case, since ammonia is responsible for poisoning the cracking function of the hydrocracking catalyst (neutralization of the acid function of the HCC catalyst), to achieve higher conversions higher temperatures in the hydrocracking section are required, resulting in shorter melting times. campaign and worse quality of final products (increased aromatic content due to reversibility of aromatic hydrogenation reactions with increasing temperature). A variation of this two-stage process configuration involves recycling the unconverted residue in the reactor hydrocracking step to increase overall process conversion. However, if performed without intermediate gas separation, the HCC step will be subject to the limitations described above.

As a strategy of maximizing HCC process performance, especially for high organic nitrogen fillers, another process configuration is single stage hydrocracking with intermediate gas separation between the catalytic hydrotreating and hydrocracking systems. In this way, H ₂ S and NH ₃ are separated from the hydrotreating bed effluent generally in a flash pressure vessel, primarily preventing NH ₃ gas from reducing the cracking activity of the hydrocracking bed downstream of the HDT bed. . Due to its greater equipment complexity (larger number of high pressure vessels), this configuration requires higher investment than without intermediate gas separation, although allowing for longer campaign time and milder operating severity than the first configuration.

In Syn technology, licensed from ABB Lummus Global, hydrocarbon and hydrogen are run-off current to achieve certain desulphurization in a first reactor. The desulphurized product of the first step is hydrogen treated in a grinder to remove the produced H ₂ S and then must be reprocessed in a second countercurrent reactor, which allows a high partial hydrogen pressure in that part of the process to remove the less reactive sulfur compounds.

In this technology, the reactor design does not have any different conformation in the design of the reaction reactors in relation to the conventional process in downstream charge and hydrogen flow, only differing in the direction of the charge and gas flows.

In the multilayer catalytic reactive distillation process, the removal of sulfur from diesel oil by hydrotreating light and heavy fractions occurs in different catalytic beds, by heating and separating in a flash zone within the reactor. This arrangement has the advantages of a co-current reactor at the beginning and the advantages of a countercurrent reactor at the end.

The state of the art is rich in processes and equipment for hydrotreating and hydrocracking petroleum and its derivatives.

US 2004/0050753 A1 claims a one-stage hydrocracking process for fillers derived exclusively from atmospheric distillation heavy gas oil or vacuum light gas oil or mixtures thereof, with a temperature of 5% vaporized between 250 ° C and 400 ° C and 95 ° C. % vaporized to 470 ° C (ASTM D-2887 distillation). It also claims process use rights in diesel oil production of the following quality: ASTM D-2887 distillation 95% vaporized temperature below 360 ° C, sulfur content up to 50 ppm and minimum cetane number 51.

In said patent, the process is comprised of a preliminary hydrotreating step where the effluent is generated with organic nitrogen below 80 ppm (preferably below 10 ppm), followed by the moderate pressure hydrocracking step (H ₂ partial pressure between 70 bar and 100 bar) with conversion of at least 80% by volume. Both steps are conducted in the same reactor (single stage configuration) and without intermediate separation of the gases produced in the hydrotreating section. The unconverted residue (boiling point up to 535 ° C) from the hydrocracking step is optionally recycled to the beginning of the hydrocracking section after the purge step.

US2003 / 0085154 A1 describes an improvement of the single stage hydrocracking process, allowing the processing of hydrocarbon streams with high levels of organic nitrogen (500 ppm to 5,000 ppm). To this end, a partial NH ₃ elimination step (more than 70% of total NH ₃ generated in the hydrotreating section) is proposed between the hydrotreating and hydrocracking zones by employing a flash vessel at pressure close to that of the reactor. hydrotreating and temperature between 150 ° C and the outlet temperature of the hydrotreating reactor. Removal of NH ₃ allows the hydrocracking section to operate with shorter contact times (lower reactor volumes) and lower temperatures, thereby increasing campaign time and improving end product quality compared to the process described in the previous patent. . However this improvement is responsible for an increased investment as it requires the use of additional pressure vessels. The hydrocracking zone also has at least one hydrotreating catalyst bed, which is responsible for bringing the organic nitrogen content of the liquid below 10 ppm.

The patent claims the production of medium distillates and probably lubricating base oils, but does not describe their quality. However, all reaction steps use bed reactors. fixed in descending co-flowing fluid dynamics.

Therefore, as can be seen, there is no state of the art equipment that promotes the maximization of the hydrotreating and / or hydrocracking and / or hydroconversion process performance of petroleum fractions that combine one or more reactors in a single equipment. upstream reaction zones, and one or more countercurrent reactors / reaction zones and a rectifying section for removal of H ₂ S and NH ₃ from the oil fractions.

SUMMARY OF THE INVENTION

The present invention relates to a novel geometry / apparatus consisting of a combination, in a single apparatus, of one or more reactors / zones / sections / upstream reaction beds, and one or more reactors / zones / sections / countercurrent reaction beds and a rectification section / zone for the removal of gaseous contaminants for the process in question, formed mainly in the first section of the equipment.

The invention relates to a reaction vessel for the treatment of petroleum and petroleum derivatives, which hydrotreats and / or hydrocrackes the petroleum and its derivatives in a single reactor capable of reacting in co-current and countercurrent flow regime. section promoting the withdrawal of H ₂ S and NH ₃ .

The invention also relates to a process of treating petroleum and petroleum derivatives comprising the use of the reactor consisting of a central body in counterflow current interconnected by the upper end to a plurality of lateral bodies which present the flow current regime; the upper end surrounds the gaseous contaminant removal section, preferably ammonia and hydrogen sulfide; and, injecting one or more fluids into said reactor. BRIEF DESCRIPTION OF DRAWINGS

For complete and complete visualization of reactor / vessel reaction for the treatment of petroleum and petroleum derivatives, hereinafter referred to and the subject of the invention patent, accompany the drawing to which reference is made as below:

Figure 1 - Side view of the object of the invention.

Figure 2 - presents the volumetric fraction profile of the gas in the reactor.

Figure 3 - Axes of symmetry of the central body, in A = horizontal and vertical axes, in B = radial axes.

DETAILED DESCRIPTION OF THE INVENTION

The reactor (1) for the treatment of petroleum and petroleum derivatives of the present invention consists of a central body (2) in countercurrent flow of liquid and gas interconnected to a plurality of side bodies (3) operating in a regime of cocurrent flow of liquid and gas.

The central body (2) has an upper opening (2.1) and a lower opening (2.2); such a central body is interconnected by the upper end to a set of 2 to 8 side bodies (3). Preferably, the central body (2) is interconnected to a set of 2 to 8 side bodies (3); more preferably, 4 side bodies (3) are arranged on opposite sides of the radial symmetry axis of the central body (2).

The upper opening (2.1) of the central body (2) is connected to one or more equipment commonly used in downstream petroleum hydrofoil (flash vessels in different temperature and pressure conditions, heat exchangers, air or water chillers). , among others). Upstream of this vessel / reactor is positioned one or more equipment commonly used in oil hydrorefining, which connects to the central body (2) through the lower opening (2.2), for example, ovens, referrers, heat exchangers, charge pumps, among others). The central body (2) and side bodies (3) are also provided with prior art devices in countercurrent (or co-current) regimes such as distributors, bulkheads, catalysts, quenchers and others.

The lateral bodies (3) are positioned on opposite sides of the same axis of symmetry of the central body (2); each of the bodies of the plurality of side bodies (3) consists of a lower region and an upper region.

For purposes of the invention, axis of symmetry is the exact similarity of shape around a given straight line; the axis; point or plane.

The lower region (3.1), shown in figure 2 of each side body (3) acts in the co-current flow regime; It is optionally provided with one or more prior art devices such as dispensers, bulkheads, catalysts, quenchers and the like.

The catalyst used is preferably a catalyst usually employed in a fixed bed, and may be a catalyst with hydrogenated and / or acidic, supported or mass active functions. More preferably, the catalyst component responsible for the hydrogenating function may be Ni, Mo, Co, W, Pt, Pd, Rh, Ir, Ru and combinations thereof. More preferably, the acid function of the catalyst may be provided by the following supports: alumina, chlorinated alumina, silica alumina, zeolites and combinations thereof. They may also be comprised of additives with hydrogenating, acidic function and coking resistance promoter. Additionally they can be used in extruded form or as structured beds.

In order to generate the co-current regime, two or more fluids are injected in an upward flow into the lower region (3.1) of each lateral body (3). For the purpose of the invention, by injection the use of fluid pumping systems and gas compressors is considered.

For purposes of the invention, the injected fluids are a gaseous fluid, such as hydrogen gas or hydrogen enriched gas; and a liquid fluid such as petroleum or a stream of petroleum derived hydrocarbons. Preferably, the side bodies 3 act under the co-current regime and are fixed bed, the gaseous fluid is hydrogen rich gas, and the liquid fluid is a petroleum derivative, such as diesel and gas oils, from various processes of refining or renewable sources or a mixture of both.

Thus, petroleum hydrochloride and its derivatives begin in the lower region (3.1) by passing a stream of petroleum derivatives through a fixed catalytic bed and by contacting such a stream with a gas, more specifically hydrogen, injected into a gas. Co-current regimen.

In the upper region (3.2) of each side body (3), gas-liquid separation occurs, such as the removal of H ₂ S and NH ₃ molecules.

In the vertical portion of the upper region (3.2) of each of the lateral bodies (3) the fluids from the lower part (3.1) of the lateral body remain upwards, but in the upper portion (2.1) that connects the lateral bodies (3). ) to the central body (2), the gaseous fluids coming from both the lateral body (3) and the central body (2), being less dense than the liquid fluids, tend to leave the reactor (1) for the subsequent equipments responsible for the gas phase processing. However, liquid fluids, which are denser than gaseous fluids, tend to flow downward as they enter the central body (2).

In the upper portion (2.1) of the central body (2) gaseous fluid from the side bodies (3) and a gaseous upward fluid injected into the central body itself (2) tend to mix and leave the equipment by the upper portion (2.1); and, concomitantly, the descending liquid fluid that has been partially hydrotreated on the hydrocarbon-rich side bodies (3) and sulfur and nitrogen compounds more refractory to hydrotreating reactions _, continues its downward course and is contrary to the flow of injected gaseous fluid. rich in hydrogen, becoming deeply hydrotreated, in the lower portion (2.2). Additionally the lower portion (2.2) may contain a mixed bed of catalysts with hydrogenating and hydrocracking function, or only hydrocracking and thus the descending liquid fluid will be hydrotreated and / or hydrocracked.

Due to its particular shape, reactor (1) for hydrotreating and hydrocracking of petroleum and its derivatives requires the injection of a final volume of gaseous fluid at least equal to the chemical hydrogen consumption of the process.

Furthermore, the object of this invention makes it unnecessary to use an additional ratification tower between hydrotreating and hydrocracking reaction sections / zones, further upstream and downstream of this reactor (1) for hydrotreating and / or hydrocracking Petroleum and petroleum products may be connected to other equipment commonly used in the refining of petroleum and petroleum products.

The reactor (1) for hydrotreating and / or hydrocracking of petroleum and petroleum derivatives of the present invention combines in a single reactor (1) of particular geometry the hydrotreating and / or hydrocracking in countercurrent and co-current flow reactions commonly employed in the present invention. petroleum derivatives, especially diesel and gas oils. In hydrotreating and hydrocracking processes of petroleum derivatives known to those skilled in the art, countercurrent and co-current flow regimes are always performed in separate and physically separate reactors or pressure vessels.

Therefore, it is also an object of the present invention a process for treating petroleum and petroleum derivatives comprising the use of reactor (1) consisting of a central body (2) with countercurrent regime interconnected by the upper end to a plurality of lateral bodies (3) presenting the co-current regime; and, injecting one or more fluids in a controlled range of temperature and pressure.

Catalytic reactions in co-current and counter-current flow occur in the same reactor (1), in conjugated bodies, in a temperature range from 100 ° C to 500 ° C, and pressure from 1 bar to 200 bar.

In the process according to the invention, the co-current reactions occur within the set of 2 to 8 side bodies (3). In the lower opening of each side body (3) two or more fluids are injected in the same direction and direction.

For purposes of this object of the invention, the injected fluids are a gaseous fluid such as hydrogen or a hydrogen rich gas; and a liquid fluid, such as petroleum or a petroleum-derived liquid. Preferably, the side bodies (3) act under the co-current regime and are fixed bed, the gaseous fluid is hydrogen or a hydrogen rich gas, and the liquid fluid is a petroleum derivative, such as diesel and gas oils.

As the gaseous fluid and liquid fluid are injected co-current in the lower region of each of the side bodies (3), at this stage of the process of the present invention, the injected liquid fluid will be at least partially hydrotreated and hydrocracked. These reactions are accelerated by the presence of one or more catalysts located in the lower region (3.1) of each lateral body (3).

The catalytic system employed is preferably a catalyst usually employed in a fixed bed, and may be a catalyst with active or supported hydrogenic and / or acidic functions. More preferably, the catalyst component responsible for the hydrogenating function may be Ni, Mo, Co, W, Pt, Pd, Rh, Ir, Ru and combinations thereof. More preferably, the acid function of the catalyst may be provided by the following supports: alumina, chlorinated alumina, silica alumina, zeolites and combinations thereof. They may also be comprised of additives with hydrogenating, acidic function and coking resistance promoter. Additionally they can be used in extruded form or as structured beds.

In the upper region (3.2) of each of the side bodies (3) there is the separation of the gas phase rich in H ₂ S and NH ₃ from the liquid phase rich in partially hydrotreated hydrocarbons. H ₂ S and NH ₃ gases exit the reactor (1) through the upper opening (2.1) of the central body (2).

The central body (2) acts countercurrent due to the injection of gaseous fluid into its lower opening. At this stage of the process liquid fluid which is already partially hydrotreated and / or hydrocracked becomes more deeply hydrotreated and / or hydrocracked.

The upper opening and lower opening of the central body (2) are connected to one or more prior art devices such as mixers, pumps, compressors and others. Devices connected to the upper opening capture the gas phase rich in H ₂ S and NH ₃ , while devices connected to the lower opening are responsible for injecting the gaseous fluid into the central body (2), promoting countercurrent regime in this region of the reactor. (1) and by receiving the hydrotreated and / or hydrocracked liquid.

Although the other stages of the oil treatment process belong to the state of the art, we see that the process of this invention has the advantage of performing in one reactor co-current and countercurrent flow catalytic reactions that occur in separate bodies of the same reactor (1). in a temperature range from 100 ° C to 500 ° C, and pressure from 1 bar to 200 bar and with a high partial hydrogen pressure in the region where the less reactive sulfur compounds are concentrated.

Although the present invention is susceptible to different embodiments, a preferred embodiment thereof is shown, with the aim of It is understood that the present disclosure is to be considered an exemplification of the principles of the invention and is not intended to be limited to what is illustrated and described herein.

The example given is merely evidence of the embodiments made by the inventors and is not intended to restrict or delimit the rights of the invention, rights which should only be restricted or delimited by the appended claims.

Example 1: Technical Specifications - Digital Simulation.

To demonstrate the functioning of geometry, a simulation was made using CFX Ansys software.

Diameter of side reactors: 1, 5 cm.

Length of side reactors: 10 cm.

Central reactor diameter: 2.5 cm.

Central reactor length: 10 cm.

Flow of the liquid: 0.00026 kg / s.

Volumetric ratio in the arms: 200 m ³ gas / m ³ liquid.

Volumetric ratio in central reactor: 20 m3 gas / m3 liquid.

Pressure: 7 MPa.

Temperature: 380 ° C.

Although the simulation simply shows fluid dynamics without any kinetics, it proves the viability of the flow.

Figure 2 shows the volume fraction of the gas. It can be seen that the gas is more concentrated at the top of the column due to the density difference that causes it to rise relative to the injected liquid. This means that the H ₂ S and NH ₃ produced in the reactor, or any other inhibitor of a specific gas-liquid-solid chemical reaction, will be removed at the top of the column.

Example 2: Volumetric fractional profile of gas inside reactor ().

The liquid rises up the side arms (3), by the action of an injector equipment, such as a pump and goes down the central body (2) of the reactor (1) due to gravity. The body centers! (2) reactor (1) is countercurrent. This demonstrates that it is possible to combine both types of flows in one reactor.

Claims

1- REACTOR (1) FOR TREATMENT OF OIL AND OIL DERIVATIVES, AND THEIR MIXTURES OR NOT WITH RENEWABLE CHAINS, characterized in that it consists of a central body (2) with a countercurrent flow regime connected to a plurality of lateral bodies (3) presenting the co-current flow regime of liquid and gas.

Reactor (1) according to Claim 1, characterized in that the central body (2) has an upper opening (2.1) and a lower opening (2.2); being interconnected by the upper end to a set of 2 to 8 side bodies (3).

Reactor (1) according to Claim 2, characterized in that the central body (1) is interconnected with an assembly of 4 to 6 lateral bodies (3).

REACTOR (1) according to claim 2, characterized in that the upper opening (2.1) of the central body (2) is connected to equipment commonly used in downstream oil refining; Upstream is positioned another equipment commonly used in oil refining, which connects to the central body (2) through the lower opening (2.2), which also connects to a gaseous fluid injection device. This system may replace one or more reactors of conventional petroleum hydrorphin units and their derivatives.

REACTOR (1) according to claim 1, characterized in that the lateral bodies (3) are positioned on opposite sides of the same axis of symmetry of the central body (2); each of the bodies of the plurality of side bodies (3) consists of a lower region acting in the co-current flow regime; and an upper region is where the H ₂ S and NH ₃ contaminating molecules are removed due to the density difference between the H ₂ S and NH ₃ rich gas phase and the hydrocarbon rich liquid phase. REACTOR (1) according to Claim 1, characterized in that it has one or more internal distributors, bulkheads, catalysts, quenchers and others.

REACTOR (1) according to Claim 6, characterized in that it is provided with one or more catalysts usually employed in a fixed bed and can be a catalyst with active and / or acidic, hydrogenating and supported functions. More preferably, the catalyst component responsible for the hydrogenating function may be Ni, Mo, Co, W, Pt, Pd, Rh, Ir, Ru and combinations thereof. More preferably, the acid function of the catalyst may be provided by the following supports: alumina, chlorinated alumina, silica alumina, zeolites and combinations thereof. They may also be comprised of additives with hydrogenating, acidic function and coking resistance promoter. Additionally they can be used in extruded form or as structured beds.

Reactor (1) according to claim 1, characterized in that the injected fluids are a gaseous fluid and a liquid fluid.

Reactor (1) according to Claim 8, characterized in that the gaseous fluid is hydrogen-rich gas and the liquid fluid is petroleum or a petroleum-derived liquid, whether or not combined with renewable charges.

REACTOR (1) according to Claim 8, characterized in that it simultaneously carries out the hydrotreating and / or hydrocracking of petroleum fractions in countercurrent and co-current flow reactions.

Reactor (1) according to Claim 8, characterized in that the gaseous fluid from the side bodies (3) and the rising gaseous fluid injected into the central body itself (2) mix, increasing the removal of H ₂ S and NH. ₃ ; and, concomitantly, the partially hydrotreated downstream liquid rich in hydrocarbons and free of H ₂ S and NH _3, continues its downward course and contrary to the flow of the injected gaseous fluid becoming, in the lower portion (3.2) more deeply hydrotreated and or hydrocracked.

12. OIL TREATMENT PROCESS AND OIL DERIVATIVES UNDERSTANDING THE USE OF THE REACTOR (1), characterized in that it consists of a central body (2) with countercurrent regime interconnected by the upper end to a plurality of lateral bodies (3) which present the co-current regime; and, injecting one or more fluids in a controlled range of temperature and pressure.

Process according to claim 12, characterized in that the catalytic reactions in co-current and counter-current flow regime occur in separate bodies of the same reactor (1) in a temperature range between 100 ° C to 500 ° C, and pressure from 1 bar to 200 bar.

Process according to Claim 12, characterized in that the catalytic reactions in the co-flowing flow regime occur within the set of 2 to 8 lateral bodies (3); Two or more fluids should be injected in the same direction and direction into the lower opening of each side body (3).

Process according to Claim 12, characterized in that the injected fluids are a gaseous fluid and a liquid fluid.

Process according to claim 15, characterized in that the gaseous fluid is a hydrogen-rich gas and the liquid fluid is petroleum or a petroleum-derived liquid.

Process according to Claim 12, characterized in that the gaseous fluid and the liquid fluid are injected in a co-current regime in the lower region of each side body (3), the injected liquid fluid will be at least partially hydrotreated and / or hydrocracked. . Process according to Claim 12, characterized in that the separation of the gas phase from the liquid phase occurs in the upper region (3.2) of each side body (3).

Process according to Claim 12, characterized in that the gases H ₂ S and NH ₃ exit the reactor (1) through the upper opening of the central body (2).

Process according to Claim 12, characterized in that the central body (2) operates in countercurrent due to the injection of the gaseous fluid into its lower opening.

Process according to Claim 12, characterized in that the upper opening and the lower opening of the central body (2) are connected to one or more prior art devices, such as mixers, pumps, compressors and others.

Process according to Claim 12, characterized in that the devices connected to the upper opening capture the gas phase rich in H ₂ S and NH ₃ , while the devices connected to the lower opening are responsible for injecting the gaseous fluid into the central body (2). ), promoting the countercurrent regime in this region of the reactor (1).