KR20030059837A - Process for hydrotreating a heavy hydrocarbon fraction with permutable reactors and reactors that can be short-circuited - Google Patents

Abstract

In the hydroprocessing process according to the invention, after hydrotreating the hydrocarbon heavy fractionation in the first hydrometallurgical section, the effluent from the first hydrometallurgical section is introduced into the second hydrodesulfurization section. At least one guard zone is located before the hydrodemetallization section. The hydrogenation treatment step,

a) using a guard zone;

b) shorting the guard zone and regenerating and / or replacing the catalyst contained in the guard zone;

c) reconnecting the guard zone where the catalyst has been regenerated and / or replaced; And

d) shorting at least one of the reactors from the hydrodesulfurization section and / or the hydrodesulfurization section and regenerating and / or replacing the catalyst contained in the reactor

It includes.

Description

PROCESS FOR HYDROTREATING A HEAVY HYDROCARBON FRACTION WITH PERMUTABLE REACTORS AND REACTORS THAT CAN BE SHORT-CIRCUITED}

The problems associated with the catalytic hydrogenation of such raw materials stem from the fact that such impurities gradually accumulate in the catalyst in the form of metals and coke, rapidly dissipating the catalyst system and thus obstructing the catalyst system and thus stopping the catalyst system for replacement. Is caused.

Therefore, the process for hydroprocessing the raw material of this type should be designed to make the operation cycle as long as possible without stopping the unit, and the goal is to obtain an operation cycle of at least one year.

There are several types of treatments for this type of raw material. Until now, such processing,

In a process using a fixed catalyst bed (e.g. HYVAHL-F from Institut Francais du Petrole), or

A process comprising at least one reactor in which the catalyst can be replaced semi-continuously (eg HYVAHL-M mobile phase process from Institut Francais du Petrole)

Has been implemented.

The process of the present invention is an improvement on prior art processes, in particular fixed bed processes or ebullated bed processes. In such a process, the raw material is circulated through a plurality of reactors (preferably fixed bed reactors or boiling phase reactors) arranged in series. The first of the plurality of reactors is used in particular to carry out part of the hydrodesulfurization (HDM) of the raw materials and hydrodesulfurization. The final reactor is used for performing deep refining of the raw materials and in particular for hydrodesulfurization (HDS step). The effluent is withdrawn from the final HDS reactor.

In such a process, a catalyst specified for each stage is usually used, in which case the average operating conditions are from about 5 MPa to about 25 MPa, preferably from about 10 MPa to about 20 MPa, and the temperature is from about 370 ° C. to 420 ℃.

The ideal catalyst in the HDM stage should be suitable for the processing of asphaltene-rich raw materials, have a high demetallic capacity associated with high metal retention and a strong resistance to coking. The Applicant has developed a catalyst on a special macroporous support ("sea urchin" structure), which gives the catalyst the following characteristics exactly required for this step (European Patent EP-B-0 113 297). And EP-B-0 113 284).

Demetallization rate in the HDM step is at least 10% to 90%.

Metal holding capacity exceeding 10% by weight of new catalyst. This extends the operating cycle.

· Excellent resistance to coking at temperatures over 390 ℃. This contributes to extending the cycle duration, which is often limited by the loss of activity and increased pressure drop due to coke production. This excellent resistance allows most of the thermal conversion to be done at this stage.

The ideal catalyst for the HDS step should be hydrogenated so that the product can be subjected to depth purification (desulfurization, reducing the amount of Conradson carbon and possibly asphaltenes with continuous demetallization). Applicant has developed catalysts (EP-B-0 113 297 and EP-B-0 113 284) which are particularly suitable for such types of raw materials.

The disadvantage of the catalyst of the above-described type, which is excellent in hydrogenation power, is that the presence of metal or coke leads to rapid loss of activity. For this reason, a combination of a suitable HDM catalyst capable of operating at relatively high temperatures and carrying out most of the conversion and demetallization and a suitable HDS catalyst protected from metals and other impurities by this HDM catalyst and capable of operating at relatively low temperatures, Depth hydrogenation is promoted and coking is limited, resulting in overall purification performance than using a single catalyst system or similar HDM / HDS configurations with increased temperature profiles resulting in rapid coking of HDS catalysts. Better

The importance of the stationary bed process is to obtain high purification performance due to the high catalytic efficacy of the stationary bed. However, if the amount of metal in the raw material exceeds a certain level (eg 50 to 150 ppm), even better catalysts will result in insufficient performance (also in particular operating periods) of such processes. This is because the reactor (particularly the first HDM reactor) is soon filled with metal and the activity is lost. To compensate for such loss of activity, the temperature is raised to promote coke formation and increase pressure drop. It is also known that the first catalyst phase can be blocked very quickly due to the asphaltenes and precipitates contained in the raw materials or due to operational problems.

As a result, the unit must be shut down at least every two to six months to replace the lost or occluded first catalyst phase, which can take up to three weeks, further reducing the unit's utilization rate.

The importance of the boiling phase process lies in the excellent conversion performance due to the possibility of working at high temperatures. Applicant has developed a process that is very suitable for the processing of conventional heavy raw materials (Canada patent CA-2 171 894, French patent application FR-98 / 00530).

Although the best catalyst system is used, the operation time can be reduced when problems arise with the operation and / or when used on unsuitable raw materials. The unit must then be stopped depending on how much coke is in the reactor. Applicants have attempted to solve such manipulation problems and problems associated with the use of catalysts.

In addition, Applicants have endeavored to overcome the disadvantages of the fixed phase approach in other ways.

Therefore, it has been proposed to install one or more mobile phase reactors early in the HDM stage (US Pat. No. US-A-3 910 834 or UK Pat. GB-B-2 124 252). Such mobile phases can be operated in co-current mode (eg SHELL's HYCON process) or in counter-current mode (eg Applicant's HYVAHL-M process). . This protects the reactor, such as a fixed bed reactor, by performing part of the demetallic reaction and by filtering the particles contained in the raw material which may cause the blockage. In addition, in the mobile phase reactor the catalyst is replaced semi-continuously, eliminating the need to shut down the unit every three to six months.

Disadvantages of such mobile phase techniques are that their overall performance and efficiency are somewhat lower than those of fixed-size techniques of the same scale, which can cause wear of the circulating catalyst to occlude downstream stationary phases and, above all, under the operating conditions in use when using heavy raw materials. There is a risk of coking, which means that the probability of catalyst agglomerations forming is beyond negligible levels, even more so in case of problems. Such catalyst agglomerates prevent the catalyst from circulating inside the reactor or the catalyst take-off line in use and eventually cause the unit to shut down to clean the reactor and the catalyst take-off line.

In order to maintain excellent performance while maintaining acceptable levels of utilization, it has been considered to add a guard reactor (space velocity HSV = 2 to 4), which is preferably a fixed bed reactor, before the HDM reactor (US-A- 4 118 310 and US-A-3 968 026). Typically, this guard reactor can be shorted, in particular by using an isolation valve. The main reactor is then temporarily protected from occlusion. If the guard reactor is closed, it will be shorted, but then the main reactor may be blocked, resulting in the unit shutting down. In addition, the guard reactors are small in size and insufficient for the high demetalization of the raw materials, and thus do not protect the main HDM reactors from metal deposition in the case of metal-rich raw materials (eg, 100 ppm or more). Thus, these reactors still have insufficient utilization because the frequency of loss of activity is accelerated, causing the unit to shut down too frequently.

FR-B1-2 681 871 has a combination of good stationary phase performance and high utilization in the treatment of raw materials with a high metal content (1-1500 ppm but mainly 100-1000 ppm, preferably 150-350 ppm). System is disclosed. In this system, the hydrotreatment process is carried out in at least two stages to hydrogenate hydrocarbon heavy fractions containing sulfur-containing impurities and metal impurities. In the first hydrodesulfurization section the hydrocarbon feedstock and hydrogen pass through the hydrodesulfurization catalyst under hydrodesulfurization conditions, and in the second stage the effluent from the first section passes through the hydrodesulfurization catalyst under hydrodesulfurization conditions. In this process, the first hydrodemetallization section comprises at least one hydrodemetallization zone, preferably having a stationary phase, and in front of this hydrodemetallurgical zone, at least two hydrodemetallurgical guard zones which likewise have a stationary phase. Located and these hydrodemetallization guard zones are arranged in series for periodic use, consisting of successive repetitions of steps b) and c) defined as follows.

a) the guard zone is used together for a period of time less than the active dissipation time and / or occlusion time of one of the guard zones.

b) the loss of activity and / or occlusion guard zone is short-circuited and the catalyst contained in the guard zone is regenerated and / or replaced with a new catalyst.

c) a step in which all guard zones are used together, wherein the guard zone in which the catalyst has been regenerated in the preceding step is reconnected and is run for a period of time less than the activity loss time and / or occlusion time of one of the guard zones.

This process typically has a cycle period of at least 11 months for the main HDM and HDS reactors, good purification and conversion performance, and maintains product stability. The overall desulfurization is about 90% and the overall demetallization is about 95%.

The disadvantages of this technique are that it is difficult to achieve total desulfurization performance of greater than about 90% and / or total demetallization performance of greater than about 95%, and cycle times of more than 11 months, regardless of performance levels. Is the point. Surprisingly, it has been found that shorting one or more reactors of the hydrodesulfurization section and / or hydrodesulfurization section allows for maintaining the activity of the catalyst and / or improving cycle time during each step.

The invention particularly relates to sulfur-containing impurities and metal impurities (e.g., atmospheric residues, reduced pressure residues, deasphalted oils, pitches, asphalt mixed with aromatics, coal hydrides, heavy oils of any type, in particular bituminous schist or sand). Purification and conversion of hydrocarbon heavy fractions containing heavy oils obtained). Specifically, the present invention relates to the treatment of liquid raw materials. In addition, the scope of the present invention includes asphaltenes also contained in the liquid raw material.

Raw materials that can be treated according to the invention usually comprise at least 0.5 ppm by weight of metals (nickel and / or vanadium) and at least 0.5% by weight of sulfur.

The purpose of catalytic hydrogenation of such raw materials is to purify the raw materials, that is, they significantly reduce metals, sulfur and other impurity components while increasing the ratio of hydrogen to carbon (H / C), while converting the raw materials to light oil. To some extent. The various effluents obtained in this process can provide the basis for the production of high quality fuels, gas oils and gasoline or can serve as raw materials for other units, such as residue cracking or cracking decompression fractions.

1 is a diagram briefly illustrating the present invention.

The present invention relates to the possibility of shorting one or more reactors in order to regenerate the catalyst and / or replace it with a new or regenerated catalyst upon loss of activity of the catalyst and / or blockage by precipitate or coke. The present invention relates both to reactors from hydrodesulfurization sections and to reactors from hydrodesulfurization sections.

According to the invention, the reactor from the hydrodemetallization section and / or hydrodesulfurization section is shorted, eg every 6 months, to replace the lost or occluded catalyst phase, and this operation improves the utilization of the unit.

In the hydroprocessing process according to the invention, after hydrotreating the hydrocarbon heavy fractionation in the first hydrometallurgical section, the effluent from the first hydrometallurgical section is introduced into the second hydrodesulfurization section. At least one guard zone is located before the hydrodemetallization section. The hydrogenation treatment step,

a) using a guard zone;

b) shorting the guard zone and regenerating and / or replacing the catalyst contained in the guard zone;

c) reconnecting the guard zone where the catalyst has been regenerated and / or replaced; And

d) shorting at least one of the reactors from the hydrodesulfurization section and / or the hydrodesulfurization section and regenerating and / or replacing the catalyst contained in the reactor

It includes.

One route for improving the performance of the stationary phase, also summarized below, is also described in Applicant's FR-A-2 784 687. The concept can also be applied to the present invention.

However, difficulties associated with high viscosities of the raw material and the entire liquid effluent, which can result in large pressure drops in the reactor, and operational difficulties in recycling compressors, which often lead to a somewhat low hydrogen pressure, which leads to poor hydrodemetallization or hydrodesulfurization. There is this. In addition, the gas oil fraction obtained has been found to be usually not directly usable since the sulfur component is higher than currently accepted specifications.

There is a need to improve the performance of the process as disclosed in the applicant's French applications FR-B1-2 681 871 and FR-A-2 784 687 and can do so. In particular, the process of the present invention can greatly reduce the viscosity of the liquid effluent, significantly reducing the pressure drop in the reactor, allowing the recycle compressor to operate better, and to increase the hydrogen pressure. As a result, the overall desulfurization is increased and the sulfur content in the gas oil fractionation is lower to meet the current specifications, which can be used directly in the gas oil pool of refineries. In addition, in the process of the present invention, since the function of the preheating furnace is improved due to good thermal conductivity, and the surface temperature of the preheating furnace is lower, it helps to extend the service life of the preheating furnace and contribute to the reduction of the operating cost of the unit.

The high performance of the reactor, which is preferably a fixed bed reactor or a boiling phase reactor, and a high utilization rate for processing a raw material rich in metal (1 to 1500 ppm, but usually 100 to 1000 ppm, preferably 150 to 350 ppm) The combined process of the present invention, as one of its variants, may be defined as a process for hydrogenating hydrocarbon heavy fractions containing sulfur-containing impurities and metal impurities in at least two sections. According to this process, the hydrocarbon feedstock and hydrogen pass through a hydrodemetallurgical catalyst under hydrodemetallization conditions in a first hydrodemetallization section, and the effluent from the first hydrodemetallization section is subjected to a subsequent second section under hydrodesulfurization conditions. Pass the hydrodesulfurization catalyst at The first hydrodemetallization section comprises at least one hydrodemetallization zone, which is preferably a stationary bed or boiling phase zone, and at least one of which, in front of the hydrodemetallization zone, likewise is preferably a stationary bed or boiling phase zone, Or possibly two hydrogenated demetallization guard zones. These hydrodemetallization guard zones are arranged in series for use in a cycle consisting of successive repetitions of steps b) and c) defined below. The hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors which are preferably stationary or boiling phase reactors, which may be shorted individually or in other ways after step d) as defined below. Can be. If two guard zones are used, the process of the present invention,

a) all guard zones are used together for a period of time less than the active dissipation time and / or occlusion time of one of the guard zones;

b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst;

c) a step in which all guard zones are used together, wherein the guard zone where the catalyst has been regenerated and / or replaced in the preceding step is reconnected, and is run for a period of time less than the active disappearance time and / or occlusion time of one of the guard zones. Phosphorus step; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It is a hydrogenation process process containing.

Another variant of the process of the present invention is a process for hydrotreating a hydrocarbon heavy fraction containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon raw material and the hydrogen in the first hydrodemetallization section are hydrodegraded. Under metal conditions is passed through a hydrodesulfurization catalyst, and the effluent from this first step is passed through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions. The first hydrodemetallization section includes one or more hydrodemetallization zones, and at least one hydrodemetallization guard zone is located in front of the hydrodemetallization zone. The hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors which can be shorted individually or in other ways after zone d) defined below. The hydrogenation treatment step,

a) the guard zone is used for a period of time that is less than the time of active disappearance and / or occlusion of the guard zone;

b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst;

c) reattaching the guard zone in which the catalyst has been regenerated and / or replaced in a preceding step, wherein the run is carried out for a period of time less than the active disappearance time and / or the occlusion time of one of the guard zones; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It includes.

In one variant of the process of the invention, the raw materials used in the process are hydrocarbon heavy fractions containing sulfur content impurities and metal impurities generally at least 0.5 ppm by weight of the metal [eg, fractions obtained by vacuum distillation, ie Reduced pressure (VD)].

During the process of the present invention, it is preferred that an amount corresponding to about 0.5% to 80% of the weight of the hydrocarbon feedstock is introduced into the first guard zone in which the common intermediate fraction is operating.

The amount of intermediate fraction introduced is more preferably from about 1% to about 50% of the weight of the hydrocarbon feedstock, very preferably from about 5% to about 25%.

In one specific embodiment, the atmospheric pressure introduced with the hydrocarbon raw material is a direct gas oil.

In yet another embodiment, the product from the hydrodesulfurization step is sent to an atmospheric distillation zone from which atmospheric oil and atmospheric residues are recovered and at least a portion of the atmospheric oil is recycled to the inlet of the first guard zone in operation. .

In one particular variant, at least a portion of the gas oil fraction from the atmospheric fraction is recycled. In this case, the gas oil fraction to be recycled is usually an oil having an initial boiling point of about 140 ° C and a final boiling point of about 400 ° C. This fraction is typically a 150-370 ° C. fraction or a 170-350 ° C. fraction.

In another possible variant of the process of the invention, the gas oil from the unit operating using the HYVAHL process can be recycled. Or from a catalytic cracking unit, commonly referred to as LCO (light cycle oil), where the initial boiling point is generally in the range of about 140 ° C to about 220 ° C and the final boiling point is generally in the range of about 340 ° C to about 400 ° C. Light gas oil may also be recycled. Also, heavy gas from catalytic cracking, commonly referred to as HCO (high cycle oil), where the initial boiling point is in the range of about 340 ° C to about 380 ° C, and the final boiling point is generally in the range of about 350 ° C to about 550 ° C. The oil fraction can also be recycled.

The amount of atmospheric oil and / or gas oil to be recycled is about 1% to 50% of the raw material weight, preferably 5% to 25%, and more preferably about 10% to 20%.

In another variant, at least a portion of the atmospheric fraction from the atmospheric distillation zone is transferred to the vacuum distillation zone and at least a portion of the vacuum fraction recovered from this vacuum distillation zone is recycled to the inlet of the first guard zone in operation and the refinery Decompression residues that can be transferred to the fuel pool are also recovered from the reduced pressure distillation zone.

In another variant, at least a portion of the atmospheric and / or reduced pressure fraction is transferred to a catalytic cracking unit which is preferably a fluidized bed catalytic cracking unit, which is, for example, an R2R process developed by the applicant. It is a unit that uses. From this catalytic cracking unit, in particular LCO fractionation and HCO fractionation are recovered, and at least one of these fractions or mixtures thereof can be added to the fresh raw material fed to the hydroprocessing process of the invention. Usually, gas oil fractionation, gasoline fractionation and gas fractionation are also recovered. At least a portion of this gas oil fraction may optionally be recycled to the inlet of the first guard zone in operation.

The catalytic cracking step can be carried out in a conventional manner known in the art, under appropriate residue cracking conditions to produce low molecular weight hydrocarbon containing products. Descriptions of operations and catalysts that can be used for fluid bed cracking are described, for example, in US-A-4 695 370, EP-B-0 184 517, US-A-4 959 334, EP-B-0 323 297, US-A-4 965 232, US-A-5 120 691, US-A-5 344 544, US-A-5 449 496, EP-A-0 485 259, US-A-5 286 690, US- A-5 324 696 and EP-A-0 699 224, the disclosures of which are incorporated herein by reference.

The fluidized bed catalytic cracking reactor can be operated in either upflow mode or downflow mode. Although not a preferred embodiment of the present invention, catalytic cracking may be performed in a mobile phase reactor. Particularly preferred catalytic cracking catalysts are catalysts containing at least one zeolite, which are usually mixed with a suitable matrix such as alumina, silica or silica-alumina.

The process of the present invention comprises one special variant, in which the guard zone is used up during step c) and the guard zone where the catalyst has been regenerated in step b) is reconnected so that the connection of the guard zone is b). Same as before the short in step.

The process of the present invention includes another variant that constitutes a preferred embodiment of the present invention, which variant,

a) all guard zones are used together for a period of less than or equal to the active disappearance time and / or occlusion time of the most upstream guard zone relative to the overall circulation direction of the treated raw material;

b) the raw material is directly introduced into the guard zone immediately following the guard zone which was the most upstream in the preceding stage, the guard zone which was the most upstream in the preceding stage is shorted, and the catalyst contained therein is regenerated and / or fresh Replacing with catalyst or regenerated catalyst;

c) all guard zones are used together, in which the guard zone where the catalyst has been regenerated and / or replaced in the preceding step is reconnected and positioned downstream of the set of guard zones, which is based on the overall circulation direction of the treated raw material. Continuing for a period of time that is less than the time of active disappearance and / or occlusion of the guard zone located most upstream during the step; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It includes.

In a preferred embodiment of the process of the invention, the guard zone most upstream relative to the overall circulation direction of the raw material is gradually filled with metals, coke, precipitates, and various other impurities. This guard zone can be separated when needed, but usually when the contained catalyst is nearly saturated with metals and various impurities.

In one preferred embodiment, a special adjustment section is used during operation, i.e. it is possible to exchange these guard zones without interrupting the operation of the unit. First, a system operating under an appropriate pressure (1-5 MPa, but preferably 1.5-2.5 MPa) is subjected to washing, stripping and cooling operations in a separate guard reactor prior to draining the used catalyst. It is then charged with fresh catalyst and then heated and sulfided. Subsequently, additional pressurization / depressurization and tap / valve systems using appropriate technology effectively exchange these guard zones without stopping the unit, i.e. without affecting the utilization rate, which cleans, strips and discharges the used catalyst. This is because the recharging, heating and sulfiding operations of the new catalyst are all carried out in separate reactors or guard zones.

The reactor of the hydroprocessing unit usually operates at the following hourly space velocity (HSV).

HSV (h ^-1 ) HSV (h ^-1 ) Wide range Desirable range Total HDM Stage (with Guard Reactor) 0.2-4.0 0.3-0.4 Total HDS Stage 0.2-4.0 0.25-0.4 Full (HDM + HDS) 0.10-2.0 0.12-0.30

Preferred modes are achieved by manipulating the guard reactor or zone in use in such a way that the overall HSV is between about 0.1 and 4.0 h ⁻¹ , usually between about 0.2 and 1.0 h ⁻¹ , which is achieved using other guard reactors. Different from the process (particularly the process using a small guard reactor as disclosed in US-A-3 968 026). The HSV value of each running guard reactor is preferably about 0.5 to 8 h ⁻¹ , usually about 1 to 2 h ⁻¹ . The overall HSV of the guard reactors and the HSV of each reactor are selected to maximize the hydrodemetallization (HDM) while controlling the reaction temperature (limiting pyrogenicity).

According to one advantageous embodiment, the unit comprises an adjusting section (not shown in the drawing), which is provided with suitable separating means, circulation means, heating means and cooling means which operate independently of the reaction section. have. Thus, with the help of lines and valves, the operation of preparing new or regenerated catalyst contained in the guard reactor can be carried out with the unit in operation just before the shorted reactor is connected. In other words, the guard reactor is preheated during the exchange or short circuit, the catalyst contained therein is sulfided and the guard reactor is brought to the required pressure and temperature conditions. When an exchange or short-circuit operation of the guard reactor is carried out using an appropriate valve set, the operation of adjusting the used catalyst contained in the guard reactor may be performed immediately after the reaction section is separated. That is, under the necessary conditions, the used catalyst is washed, removed, cooled, and the operation of discharging the used catalyst is replaced with a new catalyst or a regenerated catalyst.

Further, these catalysts are preferably catalysts disclosed in the applicant's patent EP-B-0 098 764 and the French patent application No. 97/07149. These catalysts comprise a carrier and contain from 0.1% to 30% by weight (expressed as metal oxide) of at least one metal or metal compound belonging to at least one of Groups V, VI and VIII in the periodic table. do. The catalyst is in the form of a plurality of juxtaposed aggregates each formed from a plurality of needle platelets, the platelets of each aggregate being oriented radially with respect to each other and to the center of the aggregate.

More specifically, this patent application relates to a process for converting heavy petroleum or petroleum fractionation into light fractionation which is easier to transport or is processed using conventional refining processes. Oil from coal hydrides can also be treated. In this case, it is preferable to use a boiling phase reactor.

More specifically, the present invention relates to a viscous heavy oil which is rich in metals and sulfur and whose content is higher than the regular boiling point above 520 ° C., which cannot be transported due to the content of more than 50%, and whose metal and asphaltene content is lower than the normal boiling point higher than 520 ° C. The content of the components is reduced to, for example, less than 20% by weight to solve the problem of converting into stable hydrocarbon-containing products that are easy to transport.

In one particular embodiment, the raw materials are first mixed with hydrogen and then subjected to hydrovisbraking conditions before being sent to the guard reactor.

In another embodiment, deasphalting can be carried out on an atmospheric residue or a reduced pressure residue, for example using a solvent such as a hydrocarbon containing solvent or a solvent mixture. The most frequently used hydrocarbon-containing solvents are paraffinic hydrocarbons, olefinic hydrocarbons or aliphatic ring hydrocarbons (or hydrocarbon mixtures) containing 3 to 7 carbon atoms. This treatment is generally carried out under conditions capable of producing a deasphalted product containing less than 0.05% by weight of asphaltene precipitated by heptane according to the AFNOR NF T 60115 standard. This deasphalting treatment can be carried out using the procedure described in the applicant's patent US-A-4 715 946. The volume ratio of solvent to raw material is usually from about 3: 1 to about 4: 1, and the basic physicochemical operations (mixed-precipitation, gradient separation on asphaltenes, washing-precipitation on asphaltenes) involved in the overall deasphalting operation Usually done individually. The deasphalted product is then typically recycled at least partially to the inlet of the first guard zone in operation.

Usually, the solvent used for washing on asphaltenes is the same as that used for precipitation.

Mixing between the raw material to be deasphalted and the deasphalted solvent is usually performed upstream of the exchanger which adjusts the temperature of the mixture to the values necessary for the direct precipitation and good decantation.

It is preferable that the mixture of the raw material and the solvent move inside the tube and not on the surface side of the exchanger.

The time for the mixture of raw material and solvent to stay in the mixed precipitation zone is generally from about 5 seconds to about 5 minutes, preferably from about 20 seconds to about 2 minutes.

The time for the mixture to stay in the gradient separation zone is usually from about 4 minutes to about 20 minutes.

The time for the mixture to stay in the washing zone is about 4 to 20 minutes.

The rate of rise of the mixture in the gradient separation zone and the washing zone is usually less than about 1 cm / s, preferably less than about 0.5 cm / s.

The temperature applied to the washing zone is usually lower than the temperature applied to the gradient separation zone. The temperature difference between these two zones is usually about 5 ° C to about 50 ° C.

The mixture from the washing zone is usually recycled to the decanter separator, advantageously to the upstream of the exchanger located at the inlet of the decanter separator zone.

The recommended ratio of solvent to asphaltene in the washing zone is from about 0.5: 1 to about 8: 1, preferably from about 1: 1 to about 5: 1.

The deasphalting treatment can consist of two stages, each stage comprising three basic phases: a settling phase, a gradient separation phase and a washing phase. In this precise case, the temperature recommended for each phase of the first step is preferably about 10 ° C. to about 40 ° C. lower than the temperature of the corresponding each phase of the second step.

The solvent used may be a C1 to C6 alcohol or a phenol or glycol type solvent. However, it is very advantageous to use paraffinic solvents and / or olefinic solvents containing 3 to 6 carbon atoms.

In summary, in one variant, the process of the present invention is a process for hydrotreating a hydrocarbon heavy fraction containing sulfur-containing impurities and metal impurities in at least two sections, according to the process, a first hydrodehydration section The hydrocarbon feedstock and hydrogen pass through a hydrodesulfurization catalyst under hydrodesulfurization conditions, and the effluent from this first step passes through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions. The first hydrodemetallization section includes one or more hydrodemetallization zones, in front of which are at least two hydrodemetallization guard zones. These hydrodemetallization guard zones are arranged in series for use in a cycle consisting of successive repetitions of steps b) and c) defined below. The hydrodesulfurization section and / or hydrodesulfurization section consists of one or more preferred reactors, which may be shorted individually or in other ways after step d) as defined below. The hydrogenation treatment step,

a) all guard zones are used together for a period of time less than the active dissipation time and / or occlusion time of one of the guard zones;

b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst;

c) a step in which all guard zones are used together, wherein the guard zone where the catalyst has been regenerated and / or replaced in the preceding step is reconnected, and is run for a period of time less than the active disappearance time and / or occlusion time of one of the guard zones Phosphorus step; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It includes.

In another variant, the process of the present invention is a process for hydroprocessing a hydrocarbon heavy fraction containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon feedstock and the hydrogen in the first hydrodemetallization section are hydrodegraded. Under metal conditions is passed through a hydrodesulfurization catalyst, and the effluent from this first step is passed through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions. The first hydrodemetallization section includes one or more hydrodemetallization zones, and at least one hydrodemetallization guard zone is located in front of the hydrodemetallization zone. The hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors, which may be shorted individually or in other ways after step d) as defined below. The hydrogenation treatment step,

a) the guard zone is used for a period of time that is less than the time of active disappearance and / or occlusion of the guard zone;

b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst;

c) the guard zone in which the catalyst has been regenerated and / or replaced in a preceding step is reconnected, said step being carried out for a period of time less than the time of active disappearance and / or occlusion of one of the guard zones; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It includes.

In another variant, the process of the present invention is a process for hydroprocessing a hydrocarbon heavy fraction containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon feedstock and the hydrogen in the first hydrodemetallization section are hydrodegraded. Under metal conditions is passed through a hydrodesulfurization catalyst, and the effluent from this first hydrodesulfurization section is passed through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions. The first hydrodemetallization section comprises one or more hydrodemetallization zones, in front of which are at least two hydrodemetallurgical guard zones which are preferably stationary phase or boiling phase zones. These hydrodemetallization guard zones are arranged in series for use in a cycle consisting of successive repetitions of steps b) and c) defined below. The hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors, which may be shorted individually or in other ways after step d) as defined below. The hydrogenation treatment step,

a) all guard zones are used together for a period of less than or equal to the active disappearance time and / or occlusion time of the most upstream guard zone relative to the overall circulation direction of the treated raw material;

b) the raw material is directly introduced into the guard zone immediately following the guard zone which was the most upstream in the preceding stage, the guard zone which was the most upstream in the preceding stage is shorted, and the catalyst contained therein is regenerated and / or fresh Replacing with catalyst or regenerated catalyst;

c) all guard zones are used together, and in step b) the guard zone where the catalyst has been regenerated and / or replaced is reconnected and positioned downstream of the set of guard zones, with reference to the overall circulation direction of the treated raw materials. Continuing for a period of time less than or equal to the active disappearance time and / or occlusion time of the guard zone located most upstream during this step; And

d) shorting at least one of the reactor from the hydrodemetallization section and / or hydrodesulfurization section during a cycle for the loss of activity and / or occlusion of the catalyst during regeneration and / or replacement of the catalyst with a new or regenerated catalyst. Steps

It includes.

In the process of the invention, it is generally preferred that an intermediate fraction in an amount corresponding to from 0.5% to 80% by weight of the hydrocarbon feed weight is introduced into the inlet of the first guard zone in operation. More preferably, the atmospheric pressure oil introduced together with the hydrocarbon raw material is a direct gas oil.

In the process of the invention, preferably, the product from the hydrodesulfurization step is sent to an atmospheric distillation zone from which atmospheric oil and atmospheric residues are recovered, at least a portion of which is at the inlet of the first guard zone in operation. It is preferable to recycle to. More preferably, at least a portion of the gas oil fractionation from the atmospheric distillation stage following the hydrodesulfurization stage is recycled to the inlet of the first guard zone in operation.

In one preferred variant of the invention, the recycled gas oil fraction is an oil having an initial boiling point of about 140 ° C. and a final boiling point of about 400 ° C.

In these preferred variants, the amount of atmospheric oil and / or gas oil introduced simultaneously with the feed into the inlet of the first guard zone in operation preferably corresponds to about 1% to 50% of the feed weight.

In addition, at least a portion of the atmospheric pressure fraction from the atmospheric distillation zone is transferred to the vacuum distillation zone, and at least a portion of the vacuum fraction recovered from the vacuum distillation zone is recycled to the inlet of the first guard zone in operation, and the vacuum residue is also depressurized. It is also possible to recover from the distillation zone. In this case, in one preferred variant, at least a portion of the atmospheric and / or reduced pressure fraction is sent to a catalytic cracking unit from which the LCO fraction and the HCO fraction are recovered and one or more of these fractions are recovered. At least a portion of the mixture is conveyed to the inlet of the first guard zone in operation.

In one preferred embodiment of the process of the invention, the guard zone is used up during step c) and the guard zone where the catalyst has been regenerated in step b) is reconnected so that the connection of the guard zones is the same as before the shorting in step b). Become.

In another preferred embodiment of the process of the invention, the adjusting section is associated with the guard zone, allowing shorting or replacement of the guard zone during operation, ie without interrupting the operation of the unit. By adjusting the adjusting section, the catalyst accommodated in the inoperative guard zone is adjusted to a pressure range of 1 MPa to 5 MPa.

In one preferred embodiment of the process of the present invention, in order to treat a crude oil or heavy oil fraction containing asphaltenes, hydrobisbreaking conditions are first applied after mixing with hydrogen prior to sending the crude to the guard zone.

In one preferred embodiment of the process of the present invention, a deasphalting treatment using a solvent or a mixture of solvents is performed on the atmospheric residue obtained from the optional atmospheric distillation step, wherein at least a portion of the deasphalted product is in operation with a first guard. Recycle to the inlet of the zone.

In one preferred embodiment of the process of the invention, the depressurized residue obtained from the optional reduced pressure distillation step is subjected to deasphalting with a solvent or solvent mixture and at least a portion of the deasphalted product is in operation. Recycle to the inlet of the zone.

In another preferred embodiment of the process of the invention, all reactors are fixed bed reactors. In another preferred variant, at least one of the guard reactor and / or hydrodesulfurization section reactor and / or hydrodesulfurization section reactor is a boiling phase reactor. In another preferred variant, the reactor for the guard zone is a fixed bed reactor and the reactors in the hydrodesulfurization zone are all boiling phase reactors.

In another preferred variant, all of the reactors in the guard zone are fixed bed reactors, all of the reactors in the hydrodesulfurization zone are boiling phase reactors, and optionally, and very preferably all of the reactors in the hydrodesulfurization zone are also boiling phase reactors. It is also possible to operate the process of the invention with only the boiling phase reactor in the guard zone, the hydrodesulfurization section and the hydrodesulfurization section.

After the raw material reaches guard zones 1A and 1B via line 1, it leaves the guard zone via line 13, line 23 and / or line 24. The raw material leaving the guard zone arrives via line 13 in the HDM section, shown as reaction section 2, which consists of one or more reactors, each of which can be shorted. The effluent from the reaction section 2 is withdrawn via line 14 and sent to the hydrodesulfurization section 3. This hydrodesulfurization section 3 comprises one or more reactors, which may be arranged in series, optionally shorted respectively. Effluent from the hydrodesulfurization section 3 is withdrawn via line 15.

As shown in FIG. 1, intermediate fractions are introduced via line 55 and mixed with hydrocarbon feedstock flowing through line 1.

In the case shown in FIG. 1, the guard zone comprises two reactors. In a preferred embodiment, the process comprises a series of cycles each comprising four consecutive periods as follows.

First period in which raw material passes continuously through guard zone 1A and guard zone 1B, and gas oil fractionation from the atmospheric pressure fraction being recycled is introduced into guard zone 1A with the raw material. During this first period (step a) of the process), the raw material is introduced via line 21, which comprises a line 1 and a valve 31 open towards the guard reactor 1A. During this period the valves 32, 33 and 35 are closed. Effluent from the guard zone 1A is conveyed to the guard reactor 1B via line 26 and line 22 comprising line 23 and open valve 34. The effluent from the guard zone 1B is conveyed to the HDM section 2 via a line 24 comprising an open valve 36 and a line 13 comprising an open valve 37.

A second period in which the raw material passes only the guard zone 1B, and gas oil fractionation from the atmospheric pressure fraction recycled is introduced into the guard zone 1B together with the raw material. During this second period (step b) of the process) the valves 31, 33, 34 and 35 are closed and the raw material is guarded via a line 22 which comprises a line 1 and an open valve 32. 1B). During this period, the effluent from the guard zone 1B is conveyed to the HDM section 2 via a line 24 comprising an open valve 36 and a line 13 comprising an open valve 37. .

A third period in which the raw material passes continuously through the guard zone 1B and the guard zone 1A, and gas oil fractionation from the atmospheric pressure fraction recycled is introduced into the guard zone 1B together with the raw material. During this third period (step c) of the process), the valves 31, 34, and 36 are closed, and the valves 32, 33, and 35 are opened. Raw material is introduced into guard zone 1B via line 1 and line 22. Effluent from this guard zone 1B is sent to guard reactor 1A via lines 24, 27 and 21. Effluent from the guard zone 1A is conveyed to the HDM section 2 via a line 13 comprising a line 23 and an open valve 37.

A fourth period in which the raw material passes only the guard zone 1A and gas oil fractionation from the atmospheric pressure fraction recycled is introduced into the guard zone 1A together with the raw material.

The number of cycles performed for the guard reactor is a function of the duration of the operating cycle of the entire unit and the average exchange frequency of the guard zones 1A and 1B. During the fourth period, the valves 32, 33, 34 and 36 are closed and the valves 31 and 35 are open. Raw materials are introduced into guard zone 1A via lines 1 and 21. During this period, the effluent from the guard zone 1A is transferred to the HDM section 2 via a line 13 comprising a line 23 and an open valve 37.

In the case shown in FIG. 1, the hydrodemetallization (HDM) section 2 may comprise one or more reactors. Each or a plurality of these reactors may be temporarily sequestered for periodic update of the catalyst (step d) of the process). In a preferred embodiment, the process comprises a series of cycles each comprising three consecutive periods as follows.

First period in which the raw material passes continuously through the guard zones 1A and 1B and the HDM section 2 and finally the HDS section 3. During this period, gas oil fractionation from the recycled atmospheric fraction is introduced into the guard zone 1A with the raw materials. During this period the valves 32, 33, 35, 38 and 41 are closed. Raw materials are introduced into guard zone 1A via lines 1 and 21. Effluent from the guard zone 1A is conveyed to the guard reactor 1B via line 26 and line 22 comprising line 23 and open valve 34. The effluent from this guard zone 1B is conveyed to the HDM section 2 via a line 24 comprising an open valve 36 and a line 13 comprising an open valve 37. The effluent from this HDM section 2 is conveyed to the HDS section 3 via a line 14 comprising two open valves 42 and 39. The effluent from this HDS section 3 is then sent to a splitting unit (not shown) via a line 15 comprising an open valve 40.

Second period in which the raw material passes continuously through guard zones 1A and 1B and HDS section 3. During this period, gas oil fractionation from the recycled atmospheric fraction is introduced into the guard zone 1B with the raw materials. The valves 32, 33, 35, 37, 41 and 42 are closed during this operation. Raw materials are introduced into guard zone 1A via lines 1 and 21. Effluent from this guard zone 1A is conveyed to guard zone 1B via line 26 and line 22 comprising line 23 and open valve 34. Effluent from this guard zone 1B is conveyed to HDS section 3 via line 24 comprising open valve 36 and line 25 comprising two open valves 38 and 39. do. The effluent from this HDS section 3 is then sent to a splitting unit (not shown) via a line 15 comprising an open valve 40. During this time the HDM catalyst is updated, after which the catalyst is adjusted using the methods described herein. This control is particularly necessary when the catalyst is in oxide form.

A third period of time in which the raw material passes through the guard zones 1A and 1B and the HDM section 2 and the HDS section 3 continuously. During this period, gas oil fractionation from the recycled atmospheric distillation stage is introduced into the guard zone 1B together with the raw materials. This situation is the same as the first period, allowing the reactor containing the new catalyst to be replaced at the same location in the fluid circuit as compared to the case described above with respect to the first period.

In the case shown in FIG. 1, the hydrodesulfurization section 3 may comprise one or more reactors. Each or a plurality of these reactors may be temporarily sequestered for periodic update of the catalyst (step d) of the process). In a preferred embodiment, the process comprises a series of cycles each comprising three consecutive periods as follows.

First period in which the raw material passes continuously through guard zones 1A and 1B and HDM section 2 and HDS section 3. During this period, gas oil fractionation from the recycled atmospheric fraction is introduced into the guard zone 1A with the raw materials. During this period the valves 32, 33, 35, 38 and 41 are closed. Raw materials are introduced into guard zone 1A via lines 1 and 21. Effluent from the guard zone 1A is conveyed to the guard reactor 1B via line 26 and line 22 comprising line 23 and open valve 34. The effluent from this guard zone 1B is conveyed to the HDM section 2 via a line 24 comprising an open valve 36 and a line 13 comprising an open valve 37. The effluent from this HDM section 2 is conveyed to the HDS section 3 via a line 14 comprising two open valves 42 and 39. The effluent from this HDS section 3 is then sent to a splitting unit (not shown) via a line 15 comprising an open valve 40.

A second period in which the raw material passes continuously through the guard zones 1A and 1B and the HDM section 2. During this period, gas oil fractionation from the recycled atmospheric fraction is introduced into the guard zone 1B with the raw materials. During this operation valves 32, 33, 35, 38, 39 and 40 are closed. Raw materials are introduced into guard zone 1A via lines 1 and 21. Effluent from this guard zone 1A is conveyed to guard zone 1B via line 26 and line 22 comprising line 23 and open valve 34. The effluent from this guard zone 1B is conveyed to the HDM section 2 via a line 24 comprising an open valve 36 and a line 13 comprising an open valve 37. The effluent from this HDM section 2 is then conveyed to the splitting unit (not shown) via line 14 including open valve 42 and line 16 including open valve 41. do. During this period the catalyst from the HDS section 3 is updated, after which the catalyst is adjusted using the methods described herein. This control is particularly necessary when the catalyst is in oxide form.

A third period of time in which the raw material passes continuously through the guard zones 1A and 1B and the HDM section 2 and the HDS section 3. During this period, gas oil fractionation from the recycled atmospheric distillation stage is introduced into the guard zone 1B together with the raw materials. This situation is the same as the first period, allowing the reactor containing the new catalyst to be replaced at the same location in the fluid circuit as compared to the case described above with respect to the first period.

Claims (20)

A hydrotreating process for hydrotreating hydrocarbon heavy fractions containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon feedstock and hydrogen pass through a hydrodemetalization catalyst under hydrodemetalization conditions in a first hydrodemetalization section And the effluent from this first stage passes through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions, said hydrodesulfurization section comprising at least one hydrodesulfurization zone, which precedes the hydrodesulfurization zone. At least two hydrodemetallization guard zones are located, and these hydrodehydration guard zones are arranged in series for use in a cycle consisting of successive repetitions of steps b) and c) defined below. Sections and / or hydrodesulfurization sections consist of one or more reactors, these The reactors can be shorted individually or in other ways after step d), defined below, wherein the hydroprocessing process a) all guard zones are used together for a period of time less than the active disappearance time and / or occlusion time of one of the guard zones; b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst; c) a step in which all guard zones are used together, in which the guard zone where the catalyst has been regenerated and / or replaced in the preceding step is reconnected and is carried out for a period of time less than the active disappearance time and / or occlusion time of one of the guard zones. Step; And d) short-circuit at least one of the reactor from the hydrodesulfurization section and / or hydrodesulfurization section during a cycle for loss of activity and / or occlusion of the catalyst and / or replacement of the catalyst with a new or regenerated catalyst. Steps you can make Hydrogen treatment process comprising a. A hydrotreating process for hydrotreating hydrocarbon heavy fractions containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon feedstock and hydrogen pass through a hydrodemetalization catalyst under hydrodemetalization conditions in a first hydrodemetalization section And the effluent from this first stage passes through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions, said hydrodesulfurization section comprising at least one hydrodesulfurization zone, which precedes the hydrodesulfurization zone. At least one guard zone is located, wherein the hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors, which may be shorted individually or in other ways after step d) as defined below; , The hydrogenation treatment step, a) the guard zone is used for a period of time less than or equal to the active disappearance time and / or occlusion time of the guard zone; b) short-circuit activity and / or occlusion guard zone, and the catalyst contained in the guard zone is regenerated and / or replaced with new or regenerated catalyst; c) reconnecting the guard zone in which the catalyst has been regenerated and / or replaced in the preceding step, wherein the run is carried out for a period of time less than the time of active disappearance and / or occlusion of one of the guard zones; And d) short-circuit at least one of the reactor from the hydrodesulfurization section and / or hydrodesulfurization section during a cycle for loss of activity and / or occlusion of the catalyst and / or replacement of the catalyst with a new or regenerated catalyst. Steps you can make Hydrogen treatment process comprising a. A hydrogenation process for hydroprocessing hydrocarbon heavy fractions containing sulfur-containing impurities and metal impurities in at least two sections, wherein the hydrocarbon feedstock and hydrogen pass through a hydrodemetallization catalyst under hydrodemetallization conditions in a first hydrodemetallization section. And the effluent from this first stage passes through a hydrodesulfurization catalyst in a subsequent second section under hydrodesulfurization conditions, said hydrodesulfurization section comprising at least one hydrodesulfurization zone, which precedes the hydrodesulfurization zone. At least two hydrodemetallization guard zones are located, and these hydrodemetallization guard zones comprise at least one reactor which preferably is a fixed bed reactor or an boiling phase reactor, the reactor of steps b) and c) defined below. Placed in series for use in cycles of continuous repetition Wherein the hydrodesulfurization section and / or hydrodesulfurization section consists of one or more reactors, which reactors may be shorted individually or in other ways after step d) defined below, said hydroprocessing process being a) all guard zones are used together for a period of less than or equal to the active disappearance time and / or occlusion time of the most upstream guard zone relative to the overall circulation direction of the treated raw material; b) the raw material is directly introduced into the guard zone immediately following the guard zone which was the most upstream in the preceding stage, the guard zone which was the most upstream in the preceding stage is shorted, and the catalyst contained therein is regenerated and / or fresh Replacing with catalyst or regenerated catalyst; c) all zones are used together, and in step b), the guard zone where the catalyst has been regenerated and / or replaced is reconnected and positioned downstream of the set of guard zones, based on the overall circulation direction of the treated raw material. Continuing for a period of time that is less than the time of active disappearance and / or occlusion of the guard zone located most upstream during the step; And d) shorting at least one of the reactors from the hydrodesulfurization section and / or hydrodesulfurization section during a cycle for loss of activity and / or occlusion of the catalyst and / or replacement of the catalyst by a new or regenerated catalyst. Steps you can make Hydrogen treatment process comprising a. The process of any one of claims 1 to 3, wherein an intermediate fraction in an amount corresponding to 0.5% to 80% of the weight of the hydrocarbon feed is introduced into the inlet of the first guard zone in operation. The hydroprocessing process according to claim 4, wherein the atmospheric pressure introduced with the hydrocarbon raw material is a direct gas oil. The product from any one of claims 1 to 5, wherein the product from the hydrodesulfurization step is sent to an atmospheric distillation zone, from which atmospheric pressure oil and atmospheric residues are recovered, and at least of the recovered atmospheric oil fraction. A portion of which is recycled to the inlet of the first guard zone in operation. 7. The process of claim 6, wherein at least a portion of the gas oil fractionation from the hydrodesulfurization step following the atmospheric distillation step is recycled to the inlet of the first guard zone in operation. 8. The process of claim 5 or 7, wherein the gas oil fraction being recycled is an oil having an initial boiling point of about 140 ° C and a final boiling point of about 400 ° C. The method according to any one of claims 4 to 8, wherein the amount of atmospheric oil and / or gas oil introduced simultaneously with the inlet feedstock in the first guard zone in operation corresponds to about 1% to 50% of the feedstock weight. Hydroprocessing process. 8. The process according to claim 6 or 7, wherein at least a portion of the atmospheric residue from the atmospheric distillation zone is transferred to a vacuum distillation zone from which the vacuum fraction and the vacuum residue are recovered. At least a portion of which is recycled to the inlet of the first guard zone in operation. 12. The process of claim 10 wherein at least a portion of the atmospheric and / or reduced pressure fraction is sent to a catalytic cracking unit from which the LCO fraction and the HCO fraction are recovered and at least some of these fractions or a mixture of these fractions. Is sent to the inlet of the first guard zone in operation. The method according to any one of claims 1 to 3, wherein all guard zones are used together during step c) and the guard zone where the catalyst is regenerated in step b) is reconnected so that the connection of the guard zones is short-circuited in step b). Hydrogenation process to become the same as before. 13. The control section according to any one of the preceding claims, wherein an adjustment section is associated with the guard zone, allowing the guard zone to be shorted or exchanged during operation without interrupting operation of the unit, the adjustment section being actuated. And to adjust the catalyst contained in the unguarded zone to a pressure range of 1 MPa to 5 MPa. 14. The hydrobisbreaking condition according to any one of claims 1 to 13, in order to treat the raw material consisting of heavy oil or heavy oil fraction containing asphaltenes, the raw material is first mixed with hydrogen before being sent to the guard zone. Hydrogenation process to apply. 12. The first guard according to any one of claims 7, 10 or 11, wherein the atmospheric residue is subjected to deasphalting treatment using a solvent or solvent mixture and wherein at least a portion of the deasphalted product is in operation. Recycling to the inlet of the zone. 12. The process of claim 10 or 11, wherein the depressurized residue is subjected to a deasphalted treatment with a solvent or solvent mixture and wherein at least a portion of the deasphalted product is recycled to the inlet of the first guard zone in operation. Hydroprocessing process. 17. The process of any of claims 1 to 16, wherein all of the reactors are fixed bed reactors. 18. The hydroprocessing process according to claim 1, wherein at least one of the guard zone reactor and / or hydrodesulfurization section reactor and / or hydrodesulfurization section reactor is a boiling phase reactor. 19. The process of claim 18, wherein all of the reactors for the guard zone are fixed bed reactors and all of the reactors in the hydrodesulfurization zone are boiling phase reactors. 20. The process of claim 18 or 19, wherein all of the reactors in the guard zone are fixed bed reactors and all of the reactors in the hydrodemetalization zone are boiling phase reactors.