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    • 专利摘要:
    A method of hydrotreating a vacuum distillate type hydrocarbonaceous feed containing nitrogen compounds having a first step in which the feedstock is contacted with a catalyst in its oxide form, and a second step in which the feed is contacting a dried catalyst comprising at least one organic compound containing oxygen and / or nitrogen.
    公开号:FR3013720A1
    申请号:FR1361800
    申请日:2013-11-28
    公开日:2015-05-29
    发明作者:Magalie Roy-Auberger；Emmanuelle Guillon；Aline Grezaud
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] The present invention relates to the field of hydrocracking and catalytic cracking processes and more particularly to a pretreatment of such processes by hydrotreating a vacuum distillate type feedstock by implementing a series of catalysts. The objective of the process is the production of desulfurized and deaerated vacuum distillate. The hydrotreatment process according to the invention is particularly suitable for the hydrotreatment of feeds comprising high levels of nitrogen. The hydrocracking process makes it possible to convert petroleum fractions, in particular vacuum distillates (DSV) into lighter and more valuable products (gasoline, middle distillates). The vacuum distillates contain variable contents of various contaminants (sulfur compounds, nitrogen compounds in particular): it is therefore necessary to carry out a step of hydrotreatment of the feedstock before the hydrocracking step itself, which will make it possible to break bonds. CC and produce the targeted light cuts. The same problem exists for a feedstock for a catalytic cracking process. The objective of the hydrotreating step, often called hydrocracking pretreatment, is to purify the feedstock without greatly modifying the average molecular weight thereof. In particular, it involves removing the sulfur or nitrogen compounds contained therein. The main targeted reactions are hydrodesulfurization, hydrodenitrogenation and hydrogenation of aromatics. The composition and use of the hydrotreatment catalysts are particularly well described in the article by B. S Clausen, HT Topsee, and FE Massoth, from Catalysis Science and Technology, Volume 11 (1996), Springer- Verlag. Hydrotreating catalysts generally have hydrodesulphurizing and hydrogenating functions based on Group VIB and VIII metal sulfide. The addition of an organic compound to hydrotreatment catalysts to enhance their activity is now well known to those skilled in the art. Many patents protect the use of different ranges of organic compounds, such as optionally etherified mono-, di- or polyalcohols (WO96 / 41848, WO001 / 76741, US4012340, US3954673, EP601722). Catalysts modified with C2-C14 monoesters are described in patent applications EP466568 and EP1046424. Other patents show that a specific chain of catalysts in the same reactor can be advantageous. Thus, patent application US2011 / 0079542 discloses that the replacement of a portion of a reference HDS catalyst at the head of the bed with a catalyst of lower activity does not modify the performance of the overall load compared with 100 % of reference catalyst, because on the first portion of the catalyst bed, the reaction is made on non-refractory sulfur species and does not require a high performance catalyst. EP 0651041 shows the interest of linking catalyst beds with different particle shapes. The present invention relates to a process for hydrotreating a vacuum distillate type feedstock by implementing a specific sequence of at least two different types of catalysts for increasing the overall activity and the overall stability of the process. hydrotreatment compared to a hydrotreatment process using in the same amount and under the same operating conditions as one of these two types of catalysts.
    [0002] Hydroprocessing is understood to include reactions including hydrodesulfurization (HDS), hydrodenitrogenation (HDN) and aromatic hydrogenation (HDA). According to the process of the invention, the feedstock is first brought into contact with a first type of catalyst comprising phosphorus and an active phase in its oxide form, that is to say that said first catalyst is prepared according to a process comprising at least one calcination step after the impregnation of the metal salts. This first type of catalyst is called "catalyst in oxide form" or "calcined catalyst". The feedstock is then contacted with a second type of catalyst which has been prepared by introducing phosphorous, the active phase and an organic compound containing oxygen and / or nitrogen followed by a step of 3013 72 0 3 drying, without subsequent calcination. It should be noted that this second type of catalyst does not undergo calcination, the active phase is not then in its oxide form. This second type of catalyst will be referred to as an "additivated catalyst". More particularly, the present invention relates to a process for the hydrotreatment of a hydrocarbon feed containing nitrogen compounds at a content greater than 250 ppm by weight, preferably greater than 500 ppm, and having a weighted average temperature greater than 380 ° C, comprising the following steps: a) in contact with hydrogen, said hydrocarbon feedstock 10 is contacted with at least a first catalyst comprising an amorphous carrier based on alumina, phosphorus, and an active phase formed of at least one metal group VIB in oxide form and at least one Group VIII metal in oxide form, said first catalyst being prepared by a process comprising at least one calcination step, b) contacting in the presence of hydrogen is carried out effluent obtained in step a) with at least a second catalyst comprising an amorphous support based on alumina, phosphorus, an active phase formed of at least one metal of group V IB and at least one Group VIII metal, and at least one organic compound containing oxygen and / or nitrogen, said second catalyst being prepared by a process comprising the following steps: i) contact with at least one component of a Group VIB metal, at least one component of a Group VIII metal, phosphorus and at least one organic compound containing oxygen and / or nitrogen with the carrier, In order to obtain a catalyst precursor, ii) said catalyst precursor from step i) is dried at a temperature below 200 ° C, without calcining it in the future, so as to obtain a hydrotreated effluent. It has been found that although the catalysts with an organic compound additive generally have an improved hydrotreatment capacity compared with non-additive catalysts, these catalysts are more easily inhibited by nitrogenous molecules, and in particular by basic nitrogenous molecules contained therein. in the feed, as catalysts not additive. This inhibition results in a decrease in activity and stability of the additive-treated catalyst with time and therefore a reduction in their hydrotreatment power. The Applicant has developed a process for the hydrotreatment of a vacuum distillate type feedstock comprising a series of catalysts making it possible initially to carry out a hydrotreatment on a catalyst in its oxide form (calcined catalyst), which has a good activity. in hydrodesulfurization and hydrodenitrogenation. This first type of catalyst is notably less inhibited by refractory basic nitrogenous molecules and therefore more active in hydrodenitrogenation than an additive-based catalyst. This makes it possible to carry out extensive hydrodenitrogenation in the first step of the process according to the invention and thus to relieve the additive catalyst of the second stage which is brought into contact with the effluent leaving this first stage. The hydrotreatment is then continued by contacting the feedstock free of a large part of its nitrogenous molecules and a part of its sulfur-containing molecules with an additivated catalyst that is particularly active in HDN and HDS, thus making it possible to finalize the hydrotreating. Due to the fact that the feedstock is brought into contact with a catalyst in oxide form before contacting with an additive-type catalyst, the additive catalyst is less inhibited by the nitrogenous molecules and therefore more active and stable with time. The specific sequence thus makes it possible to protect the highly active additive catalyst in HDS / HDN by a catalyst in oxide form that is very active in HDN, which results in an increase in the overall activity and in the overall stability of the catalytic chain. compared to a catalytic system containing only additivated catalysts. Thus, the overall activity is increased because the hourly volume velocity (the volume of charge that can be processed in time) can be increased or, alternatively, less catalyst can be used to process the same volume of charge. In addition, by increasing the activity, the temperature required to achieve a desired nitrogen content can be lowered. Likewise, the overall stability is increased because the cycle time is prolonged. The hydrotreatment process according to the invention is particularly suitable for the hydrotreatment of feedstocks comprising high levels of organic nitrogen, such as feedstocks resulting from catalytic cracking, coker or visbreaking. The process according to the present invention makes it possible to produce a hydrotreated hydrocarbon fraction, that is to say at the same time freed from any sulfur and nitrogen compounds. The contents of nitrogen compounds after hydrotreatment are generally less than or equal to 300 ppm nitrogen, preferably less than 200 ppm, very preferably less than 100 ppm. By 10 ppm nitrogen (or sulfur) is meant for the rest of the text ppm by weight relative to the elemental nitrogen (or elemental sulfur), regardless of the organic molecule or molecules in which the nitrogen (or the sulfur) is engaged. Preferably, according to the process according to the invention, the conversion to hydrodesulfurization is greater than 95%, preferably greater than 98%. Preferably, according to the process according to the invention, the conversion to hydrodenitrogenation is greater than 90%, preferably greater than 95%. According to one variant, for the catalyst of step a) or b), the metal of group VIB is chosen from molybdenum, tungsten and the mixture of these two elements, and the metal of group VIII is chosen from cobalt, nickel and the mixture of these two elements. According to one variant, for the catalyst of step a) or b), the content of group VIB metal is between 5 and 40% by weight of Group VIB metal oxide relative to the total weight of the catalyst, the content Group VIII metal is between 1 and 10% by weight of Group VIII metal oxide with respect to the total weight of the catalyst and the phosphorus content is between 0.1 and 10% by weight of P2O5 by weight total catalyst. Alternatively, the catalyst of step a) or b) further contains at least one dopant selected from boron and fluorine and a mixture of boron and fluorine. Alternatively, the organic compound is one or more selected from a carboxylic acid, an alcohol, an aldehyde, an ester, an amine, an amino carboxylic acid, an amino alcohol, a nitrile or an amide, preferably is one or more selected from ethylene glycol, glycerol, polyethylene glycol (with a molecular weight of 200 to 1500), acetophenone, 2,4-pentanedione, pentanole, acetic acid, maleic acid, oxalic acid, tartaric acid, formic acid, citric acid, and C1-C4 dialkyl succinate, particularly preferably it comprises at least the combination of C1-C4 dialkyl succinate. C4 and acetic acid. According to another particularly preferred variant, the organic compound comprises at least citric acid. Alternatively, the catalyst of step a) or b) has further undergone a sulfurization step. Alternatively, the basic nitrogen content in the feed is greater than or equal to 60 ppm. According to one variant, each of the steps a) and b) is carried out at a temperature of between 200 and 450 ° C., at a pressure of between 0.5 and 30 MPa, at an hourly space velocity of between 0.1 and 20 h. -1 and with a hydrogen / charge ratio expressed as a volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid charge is advantageously between 501 / and 20001/1. According to one variant, step a) is carried out in a first zone containing the first catalyst that occupies a volume V1, and step b) is carried out in a second zone containing the second catalyst that occupies a volume V2, the distribution of volumes V1 / V2 being between 10% vol / 90% vol and 50% vol / 50% vol respectively of the first and second zone. According to one variant, step i) of step b) comprises the following successive steps: i ') an amorphous alumina-based support is impregnated with at least one solution containing at least one Group VIB metal, at least a Group VIII metal and said phosphor to obtain an impregnated support, i ") the impregnated support obtained in step i ') is dried at a temperature below 180 ° C without subsequent calcination to obtain a dried impregnated support, i" the impregnated dried support obtained in step i ") is impregnated with an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an impregnated catalytic precursor, 3013 720 7 i "") is allowed to mature the impregnated catalyst precursor obtained in step im) to obtain said catalyst precursor. According to one variant, the effluent obtained in step a) is subjected to a separation step making it possible to separate a heavy fraction and one light fraction containing H25 and NH3 formed in step a), said heavy fraction being then introduced in step b). The invention also relates to a hydrocracking process using the hydrotreatment process according to the invention, in which said hydrotreated effluent is brought into contact with at least one of the hydrotreated effluents in the presence of hydrogen and under the hydrocracking operating conditions. hydrocracking catalyst so as to obtain a hydrocracked effluent. The invention also relates to a process for catalytic cracking in a fluidized bed employing the hydrotreatment process according to the invention, in which said hydrotreated effluent is brought into contact with the catalytic cracking operating conditions with at least one cracking catalyst. catalytic so as to obtain a cracked effluent. Detailed Description Charge and Operating Conditions The hydrocarbon feedstock treated according to the hydrotreatment process of the invention has a weighted average temperature (TMP) greater than 380 ° C. The TMP is defined from the temperature at which 5%, 50% and 70% of the volume of the charge distils according to the following formula: TMP = (T 5% + 2 × T 50% + 4 × T 70%) / 7. The TMP is calculated from simulated distillation values. The TMP of the feed is greater than 380 ° C and preferably less than 600 ° C, and more preferably less than 580 ° C. The treated hydrocarbon feedstock generally has a distillation range of between 250 ° C and 800 ° C, preferably between 300 and 580 ° C. In the rest of the text, we will conventionally call this vacuum distillate charge, but this designation has no restrictive character. Any sulfur-containing hydrocarbon feedstock and nitrogen compounds inhibiting hydrotreatment, and a TMP similar to that of a vacuum distillate cut may be concerned by the process object of the present invention. The hydrocarbon feed may be of any chemical nature, that is to say have any distribution between the different chemical families including paraffins, olefins, naphthenes and aromatics. Said hydrocarbon feedstock comprises nitrogenous and / or sulfur-containing organic molecules. Nitrogenous organic molecules are either basic, such as amines, anilines, pyridines, acridines, quinolines and their derivatives, or neutral such as pyrroles, indoles, carbazoles and their derivatives. It is in particular the basic nitrogenous molecules which inhibit the hydrotreatment catalysts, and in particular the additivated catalysts. The nitrogen content is greater than or equal to 250 ppm, preferably it is between 500 and 10000 ppm by weight, more preferably between 700 and 4000 ppm by weight and even more preferably between 1000 and 4000 ppm. The basic nitrogen content has at least a quarter of the total nitrogen content (nitrogen). The basic nitrogen content is generally greater than or equal to 60 ppm, more preferably between 175 and 1000 ppm by weight and even more preferably between 250 and 1000 ppm. The sulfur content in the filler is generally between 0.01 and 5% by weight, preferably between 0.2 and 4% by weight and even more preferably between 0.5 and 3% by weight. Said hydrocarbon feed may optionally advantageously contain metals, in particular nickel and vanadium. The cumulative nickel and vanadium content of said hydrocarbon feed, treated according to the hydrocracking process according to the invention, is preferably less than 1 ppm by weight. The asphaltene content of said hydrocarbon feedstock is generally less than 3000 ppm, preferably less than 1000 ppm, even more preferably less than 200 ppm. The treated feedstock generally contains resins, preferably the resin content is greater than 1 wt%, more preferably greater than 5 wt%. The resin content is measured according to ASTM D 2007-11.
    [0003] Said hydrocarbon feedstock is advantageously chosen from LCO or HCO (light cycle oil or heavy cycle oil according to the English terminology (light or heavy gas oils from a catalytic cracking unit)), the vacuum distillates, for example gas oils derived from direct distillation of crude or conversion units such as catalytic cracking, coker or visbreaking, feeds from aromatics extraction units, lubricating oil bases or from solvent dewaxing of bases of lubricating oil, the distillates from processes for desulphurization or hydroconversion to a fixed bed or an ebullated bed of atmospheric residues and / or vacuum residues and / or deasphalted oils, or the charge may be a deasphalted oil or include vegetable oils or come from the conversion of biomass feedstock. Said hydrocarbon feedstock treated according to the hydrocracking process of the invention may also be a mixture of said fillers previously mentioned.
    [0004] The process according to the invention can be carried out in one, two or more reactors. It is usually done in a fixed bed. When the process according to the invention is carried out in two reactors, step a) can be carried out in the first reactor through which the feed passes, and then step b) can be carried out in the second reactor placed downstream of the first reactor.
    [0005] Optionally, the effluent of step a) leaving the first reactor can be subjected to a separation step making it possible to separate a light fraction containing in particular the H 2 S and NH 3 formed during the hydrotreatment in step a) of a heavy fraction containing the partially hydrotreated hydrocarbons. The heavy fraction obtained after the separation step is then introduced into the second reactor to perform step b) of the process according to the invention. The separation step may be carried out by distillation, flash separation or any other method known to those skilled in the art. When the process is carried out in a single reactor, step a) is carried out in a first zone containing the first catalyst which occupies a volume V1, and step b) is carried out in a second zone containing the second catalyst which occupies a volume V2. The volume percentage of the first zone 3013 containing the oxide catalyst of step a) relative to the total volume of the zones is preferably at least 10% vol. The volume percentage of the first zone containing the oxide catalyst of step a) is adjusted so as to maximize the conversion of the nitrogenous inhibiting compounds, said basic. The distribution of volumes V1 / V2 is preferably between 10% vol / 90% vol and 50% vol / 50% vol respectively of the first and second zone. The Group VIB or Group VIII metals used to form the active phase of the catalysts of step a) or b) may be the same or different in each of steps a) or b). The operating conditions used in steps a) or b) of the hydrotreatment process according to the invention are generally as follows: the temperature is advantageously between 200 and 450 ° C., and preferably between 300 and 400 ° C., Advantageously, the pressure is between 0.5 and 30 MPa, and preferably between 5 and 20 MPa, the hourly space velocity (defined as the ratio of the volume flow rate of charge to the volume of the catalyst per hour) is advantageously between 0, 1 and 20 h-1 and preferably between 0.2 and 5 h-1, and the hydrogen / charge ratio expressed as a volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid charge is advantageously understood between 50 1/1 to 2000 1/1. The operating conditions may be the same or different in steps a) and b). Preferably they are identical. Step a): Hydrotreatment with a catalyst in oxide form According to step a) of the process according to the invention, said hydrocarbon feedstock is brought into contact with hydrogen with at least a first catalyst comprising an amorphous carrier based on alumina, phosphorus, and an active phase formed of at least one Group VIB metal in oxide form and at least one Group VIII metal in oxide form, said first catalyst being prepared by a process comprising at least one step calcination. The catalyst used in step a) according to the invention is composed of an amorphous support based on alumina, phosphorus, and an active phase formed of at least one metal of group VIB in the form of oxide and at least one Group VIII metal in oxide form. In general, the total content of group VIB metal and of group VIII metal is greater than 6% by weight, and preferably between 10 and 50% by weight of Group VIB and VIII metals, relative to the total weight of the Group VIII metal. catalyst. The metal content of group VIB is between 5 and 40% by weight, preferably between 8 and 35% by weight, and more preferably between 10 and 30% by weight of metal oxide (ux) of group VIB relative to to the total weight of the catalyst. The metal content of group VIII is between 1 and 10% by weight, preferably between 1.5 and 9% by weight, and more preferably between 2 and 8% by weight of Group VIII metal oxide with respect to weight. total catalyst. The Group VIB metal present in the active phase of the catalyst used in the hydrotreatment process according to the invention is preferably chosen from molybdenum, tungsten and the mixture of these two elements, and very preferably, the metal of the Group VIB is molybdenum. The Group VIII metal present in the active phase of the catalyst used in the hydrotreatment process according to the invention is preferably chosen from cobalt, nickel and the mixture of these two elements. Very preferably, the Group VIII metal is nickel. Preferably, the active phase of the catalyst used in step a) is chosen from the group formed by the combination of nickel-molybdenum, nickel-cobalt-molybdenum, nickel-tungsten or nickel-molybdenum-tungsten elements. Most preferably, the active phase of the catalyst used in step a) is the combination of nickel-molybdenum elements. The molar ratio of Group VIII metal to Group VIB metal in the catalyst in oxide form is preferably between 0.1 and 0.8, preferably between 0.15 and 0.6, and even more preferably between 30 and 30. between 0.2 and 0.5.
    [0006] Said catalyst of step a) also comprises phosphorus as a dopant. The dopant is an added element which in itself has no catalytic character but which increases the catalytic activity of the active phase. The phosphorus content in said catalyst of step a) is preferably between 0.1 and 10% by weight of P2O5, preferably between 0.2 and 8% by weight of P2O5, very preferably between 0.3 and 8% weight of P2O5. The phosphorus to metal group VIB molar ratio in the catalyst of said step a) is greater than or equal to 0.05, preferably greater than or equal to 0.07, more preferably between 0.08 and 0.5.
    [0007] The catalyst used in step a) according to the invention may advantageously also contain at least one dopant selected from boron and fluorine and a mixture of boron and fluorine. When the hydrotreating catalyst contains boron as a dopant, the boron content in said oxide catalyst of said step a) is preferably between 0.1 and 10% by weight of boron oxide, preferably between 0.2 and 7% by weight of boron oxide, very preferably between 0.2 and 5% by weight of boron oxide. When the hydrotreatment catalyst contains fluorine as a dopant, the fluorine content in said oxide-form catalyst derived from said step a) is preferably between 0.1 and 10% by weight of fluorine, preferably between 0, 2 and 7% by weight of fluorine, very preferably between 0.2 and 5% by weight of fluorine. The amorphous support of said catalytic precursor is based on alumina, that is to say it contains more than 50% of alumina, and generally, it contains only alumina or silica-alumina as defined below - and possibly metals and / or dopants), which have been introduced outside the impregnations (introduced for example during the preparation (kneading, peptization ...) of the support or its formatting). The support is obtained after shaping (extrusion for example) and calcination, generally between 300 and 600 ° C. In a preferred case, the amorphous support is an alumina, and preferably an extruded alumina. Preferably, the alumina is gamma alumina. In a particularly preferred manner, the support consists of an alumina and preferably a gamma alumina. In another preferred case, the amorphous support is a silica-alumina containing at least 50% alumina. The silica content in the support is at most 50% by weight, most often less than or equal to 45% by weight, preferably less than or equal to 40% by weight. In a particularly preferred manner, the support consists of a silica-alumina. The pore volume of the amorphous support is generally between 0.1 cm3 / g and 1.5 cm3 / g, preferably between 0.4 cm3 / g and 1.1 cm3 / g. The total pore volume is measured by mercury porosimetry according to ASTM D4284-92 with a wetting angle of 140 °, as described in Rouquerol F .; Rouquerol J .; Singh K. "Adsorption by Powders & Porous Solids: Principle, methodology and applications", Academic Press, 1999, for example by means of an Autopore III TM model instrument of the MicromériticsTM brand. The specific surface of the amorphous support is generally between m2 / g and 350 m2 / g, preferably between 10 m2 / g and 300 m2 / g. The specific surface is determined in the present invention by the B.E.T method, described in the same work cited above. Said amorphous support is advantageously in the form of a powder, or is shaped into balls, extrudates, pellets, or irregular and non-spherical agglomerates, the specific shape of which may result from a crushing step. Very advantageously, said support is in the form of extrudates. The preparation of a fresh oxide catalyst used in step a) can be carried out by any method well known to those skilled in the art.
    [0008] The Group VIB and Group VIII metals of said catalyst can be advantageously introduced into the catalyst at various levels of the preparation and in a variety of ways. Said metals of group VIB and of group VIII may advantageously be introduced in part during the shaping of said amorphous support or preferably after this shaping.
    [0009] In the case where the metals of group VIB and of group VIII are introduced in part during the shaping of said amorphous support, they can be introduced in part only at the moment of mixing with an alumina gel chosen as the matrix. the rest of the metals are then introduced later. Preferably, when the Group VIB and Group VIII metals are introduced in part at the time of mixing, the proportion of the Group VIB metal introduced during this step is less than or equal to 20% of the total amount of the metal. of the group VIB introduced on the final catalyst and the proportion of the Group VIII metal introduced during this step is less than or equal to 50% of the total amount of the Group VIII metal introduced on the final catalyst. In the case where the Group VIB and Group VIII metals are introduced at least in part and preferably in all, after the shaping of said amorphous support, the introduction of the Group VIB and Group VIII metals onto the support The amorphous mixture can be advantageously carried out by one or more impregnations in excess of solution on the amorphous support, or preferably by one or more dry impregnations and, preferably, by a single dry impregnation of said amorphous support, with the aid of 15 aqueous or organic solutions containing metal precursors. The dry impregnation comprises contacting the support with a solution containing at least one precursor of said metal group VIB and / or group VIII, the volume of which is equal to the pore volume of the support to be impregnated. The solvent of the impregnating solution may be water or an organic compound such as an alcohol. Preferably, an aqueous solution is used as the impregnating solution. Very preferably, the Group VIB and Group VIII metals are introduced completely after the shaping of said amorphous support, by dry impregnation of said support with an aqueous impregnating solution containing the salts. precursors of metals. The introduction of the Group VIB and Group VIII metals can also be advantageously carried out by one or more impregnations of the amorphous support, by a solution containing the precursor salts of the metals. In the case where the metals are introduced in several impregnations of the corresponding precursor salts, a step of intermediate drying of the catalyst is generally carried out at a temperature between 50 and 180 ° C, preferably between 60 and 150 ° C and very preferably between 75 and 130 ° C.
    [0010] Preferably, the Group VIB metal is introduced at the same time as the Group VIII metal, regardless of the mode of introduction. The molybdenum precursors that can be used are well known to those skilled in the art. For example, among the sources of molybdenum, it is possible to use oxides and hydroxides, molybdic acids and their salts, in particular ammonium salts such as ammonium molybdate, ammonium heptamolybdate, phosphomolybdic acid ( H3PMo12040), and their salts, and optionally silicomolybdic acid (H4SiMo12040) and its salts. The sources of molybdenum may also be any heteropolycomposed Keggin type, Keggin lacunary, Keggin substituted, Dawson, Anderson, Strandberg, for example. Molybdenum trioxide and heteropoly compounds of the Keggin, Keggin lacunary, Keggin substituted and Strandberg type are preferably used. The tungsten precursors that can be used are also well known to those skilled in the art. For example, among the sources of tungsten, it is possible to use oxides and hydroxides, tungstic acids and their salts, in particular ammonium salts such as ammonium tungstate, ammonium metatungstate, phosphotungstic acid and their salts. salts, and optionally silicotungstic acid (H4SiW12O40) and its salts. Tungsten sources can also be any heteropolycomposed Keggin type, Keggin lacunary, Keggin substituted, Dawson, for example. Oxides and ammonium salts such as ammonium metatungstate or heteropolyanions of the Keggin, Keggin lacunary or substituted Keggin type are preferably used. The cobalt precursors which can be used are advantageously chosen from oxides, hydroxides, hydroxycarbonates, carbonates and nitrates, for example. Cobalt hydroxide and cobalt hydroxycarbonate are preferably used. The nickel precursors that can be used are advantageously chosen from oxides, hydroxides, hydroxycarbonates, carbonates and nitrates, for example. Nickel oxyhydroxide and nickel carbonate are preferably used.
    [0011] In the same way, the phosphorus can advantageously be introduced into the catalyst at various levels of the preparation and in various ways. Said phosphorus may advantageously be introduced during the shaping of said amorphous support or preferably after this shaping. It may for example be introduced just before or just after peptization of the chosen matrix, such as for example and preferably aluminum oxyhydroxide (boehmite) precursor of alumina. It may also advantageously be introduced alone or in admixture with at least one of Group VIB and VIII metals. Said phosphorus is preferably introduced in admixture with the Group VIB and Group VIII metal precursors, in whole or in part on the shaped amorphous support, preferably alumina or silica-alumina in extruded form, by a dry impregnation of said amorphous support with a solution containing the precursors of metals and the precursor of phosphorus. The preferred phosphorus source is orthophosphoric acid H 3 PO 4, but its salts and esters as ammonium phosphates are also suitable. Phosphorus may also be introduced together with the group VIB element (s) as Keggin, Keggin lacunary, Keggin substituted or Strandberg heteropolyanions. The catalyst used in step a) according to the invention may advantageously also contain at least one dopant selected from boron and fluorine and a mixture of boron and fluorine. The introduction of this dopant can be done in the same way as the introduction of phosphorus at various levels of the preparation and in various ways. It can be introduced at least partly during the preparation of the support (formatting included). It may advantageously be introduced alone or in admixture with the phosphorus or at least one of the group VIB and VIII metal precursors. It is preferably introduced in admixture with the Group VIB and Group VIII metal precursors and the phosphorus, in whole or in part on the shaped amorphous support, preferably alumina or silica-alumina in extruded form, by dry impregnation of said amorphous support with a solution containing the metal precursors, the phosphorus precursor and the precursor (s) of the dopant selected from boron and / or fluorine.
    [0012] The boron source may be boric acid, preferably orthoboric acid H3B03, biborate or ammonium pentaborate, boron oxide, boric esters. Boron may be introduced for example by a boric acid solution in a water / alcohol mixture or in a water / ethanolamine mixture.
    [0013] Fluoride sources that can be used are well known to those skilled in the art. For example, the fluoride anions can be introduced in the form of hydrofluoric acid or its salts. These salts are formed with alkali metals, ammonium or an organic compound. In the latter case, the salt is advantageously formed in the reaction mixture by reaction between the organic compound and the hydrofluoric acid. The fluorine may be introduced for example by impregnation with an aqueous solution of hydrofluoric acid, or ammonium fluoride or ammonium bifluoride. In a preferred embodiment, the process for preparing the catalyst of step a) of the process according to the invention comprises the following steps: a ') impregnating a solution containing at least one precursor of the group VIB metal, at least one precursor of the group VIII metal, phosphorus, optionally another dopant selected from boron and / or fluorine, on an amorphous support based on alumina, a ") the impregnated support resulting from step a ') is optionally dried (am) the optionally dried impregnated support is calcined so as to convert the Group VIB and Group VIII metal precursors into oxides, and the impregnation step a ') is carried out according to the variants described above. Very preferably, the Group VIB and Group VIII metals, the phosphorus and optionally another dopant selected from boron and / or fluorine are introduced completely after shaping of said amorphous support, by dry impregnation of the said support with an aqueous impregnating solution containing the precursor salts of metals, phosphorus and optionally dopant selected from boron and / or fluorine.
    [0014] The drying of step a ") is generally carried out at a temperature of between 50 and 180 ° C., preferably between 60 and 150 ° C. and very preferably between 75 and 130 ° C. The drying is generally carried out during a duration between 1 and 24 hours, preferably between 1 and 20 hours Drying is carried out in air, or in an inert atmosphere (nitrogen for example) .The calcination of step a "") is generally carried out at a temperature of between 250 ° C and 900 ° C, preferably between 350 ° C and 750 ° C. The calcination time is generally between 0.5 hours and 16 hours, preferably between 1 hour and 5 hours. It is usually done under air. Calcination makes it possible to convert the precursors of Group VIB and VIII metals into oxides.
    [0015] Prior to its use, it is advantageous to convert the catalyst in oxide (calcined) form used in step a) of the process according to the invention into a sulphurized catalyst in order to form its active species. This activation or sulphurization phase is carried out by methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere in the presence of hydrogen and hydrogen sulphide. This conversion to sulphurized catalyst is preferably carried out on all types of catalyst in oxide form, that is to say that it can be carried out on a fresh catalyst or a regenerated catalyst. The sulphurisation step is advantageously carried out ex situ or in situ. The sulfurizing agents are H2S gas or any other sulfur-containing compound used for activating the hydrocarbon feeds to sulphurize the catalyst. Said sulfur-containing compounds are advantageously chosen from alkyldisulphides such as, for example, dimethyl disulphide (DMDS), alkylsulphides, such as, for example, dimethylsulphide, n-butylmercaptan, polysulfide compounds of tertiononylpolysulphide type or any other compound. known to those skilled in the art to obtain a good sulfuration of the catalyst. Preferably, the catalyst is sulfided in situ in the presence of a sulfurizing agent and a hydrocarbon feedstock. Very preferably, the catalyst is sulphurized in situ in the presence of a hydrocarbon feed additive of dimethyl disulfide. Step b): Hydrotreatment with an Additized Catalyst According to step b) of the process according to the invention, contact is made with in the presence of hydrogen, the effluent obtained in step a) with at least one second catalyst comprising an amorphous support based on alumina, phosphorus, an active phase formed of at least one Group VIB metal and at least one Group VIII metal and at least one organic compound containing oxygen and / or nitrogen, said second catalyst being prepared by a process comprising the following steps: i) contacting at least one component of a Group VIB metal, at least one component of a Group VIII metal, phosphorus and at least one organic compound containing oxygen and / or nitrogen with the carrier, so as to obtain a precursor of catalyst, ii) dry ledi Catalyst precursor from step i) at a temperature below 200 ° C., without subsequently calcining it The catalyst used in step b) according to the invention is composed of an amorphous support based on alumina, phosphorus, an active phase formed of at least one Group VIB metal and at least one Group VIII metal, and an organic compound containing oxygen or nitrogen. The catalyst used in step b) is a so-called additivated catalyst. During its preparation it does not undergo calcination, that is to say that its active phase comprises the metals of group VIB and VIII which have not been converted into oxide form. The total content of Group VIII metal and Group VIB metal as well as the Group VIII metal to Group VIB metal molar ratio of the catalyst according to Step b) are in the same ranges as those described for the catalyst of the step a). The Group VIB metal present in the active phase of the catalyst used in step b) according to the invention is preferably chosen from molybdenum, tungsten and the mixture of these two elements, and very preferably, the metal of the group. VIB is molybdenum.
    [0016] The group VIII metal present in the active phase of the catalyst used in step b) according to the invention is preferably chosen from cobalt, nickel and the mixture of these two elements. In a particularly preferred manner, Group VIII metal is nickel. Preferably, the active phase of the catalyst used in step b) is chosen from the group formed by the combination of nickel-molybdenum, cobalt-molybdenum and nickel-cobalt-molybdenum elements. In a particularly preferred manner, the active phase consists of nickel-molybdenum. The additive catalyst used in step b) also comprises phosphorus as a dopant. The phosphorus content of the catalyst according to step b) as well as the phosphorus to metal molar ratio of the group VIB of the catalyst according to step b) are in the same ranges as those described for the catalyst of step a). The catalyst used in step b) according to the invention may advantageously also contain at least one dopant chosen from boron and / or fluorine. When the catalyst used in step b) contains boron and / or fluorine, the boron and / or fluorine content are in the same ranges as those described for the catalyst of step a). The amorphous support of said catalyst used in step b) is based on alumina. It has been described in step a). The catalyst support additive according to step b) may be identical to or different from the catalyst support used in step a). The catalyst used in step b) further contains an organic compound containing oxygen and / or nitrogen. This compound is an organic compound containing more than 2 carbon atoms and at least one oxygen and / or nitrogen atom.
    [0017] The organic oxygen-containing compound may be one or more selected from a carboxylic acid, an alcohol, an aldehyde or an ester. By way of example, the oxygen-containing organic compound may be one or more selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol (with a molecular weight of 200 to 1500), and acetophenone, 2,4-pentanedione, pentanole, acetic acid, maleic acid, oxalic acid, tartaric acid, formic acid, citric acid and C1-C4 dialkyl succinate . The dialkyl succinate used is preferably included in the group consisting of dimethyl succinate, diethyl succinate, dipropyl succinate and dibutyl succinate. Preferably, the Cl -C 4 dialkyl succinate used is dimethyl succinate or diethyl succinate. Very preferably, the C1-C4 dialkyl succinate used is dimethyl succinate. At least one C1-C4 dialkyl succinate is used, preferably one, and preferably dimethyl succinate. The nitrogen-containing organic compound may be selected from an amine. By way of example, the organic compound containing nitrogen may be ethylene diamine or tetramethylurea. The organic compound containing oxygen and nitrogen may be selected from an amino carboxylic acid, an amino alcohol, a nitrile or an amide. By way of example, the organic compound containing oxygen and nitrogen may be aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, mono- ethanolamine, acetonitrile, N-methylpyrrolidone or dimethylformamide. or else EDTA. Preferably, the organic compound contains oxygen. Particularly preferably, the organic compound comprises at least the combination of C1-C4 dialkyl succinate, and in particular dimethyl, and acetic acid.
    [0018] According to another particularly preferred variant, the organic compound comprises at least citric acid. The catalyst used in step b) is prepared according to a process comprising the following steps: i) at least one component of a Group VIB metal, at least one component of a Group VIII metal, the phosphorus and at least one organic compound containing oxygen and / or nitrogen with the support, so as to obtain a catalyst precursor, ii) drying said catalyst precursor from step i) at a temperature below 200 ° C, without further calcining step i) of contacting comprises several modes of implementation. According to the first embodiment of step i) of the process for preparing the catalyst used in step b), the said components of the Group VIB and Group VIII metals, phosphorus, are deposited. and that of said organic compound, on said support, by at least one co-impregnation step, preferably by dry impregnation. According to this embodiment, also known as "co-impregnation", said components of Group VIB and Group VIII metals, phosphorus, and the organic compound are introduced simultaneously into said support. Said first embodiment of step i) comprises the implementation of one or more co-impregnation steps, each co-impregnation step being preferably followed by a drying step as described according to the invention. step i ") below According to the second embodiment of step i) of the catalyst preparation process used in step b), at least one catalytic precursor comprising at least one metal of at least one group VIII, at least one Group VIB metal, said phosphorus and at least said amorphous alumina support with at least one organic compound containing oxygen and / or nitrogen. second embodiment is a so-called "post-impregnation" preparation According to this variant embodiment, the catalyst precursor is prepared by depositing at least one component of a Group VIB metal and at least one a component of a group VIII metal and p hosphorus on said support by any method known to those skilled in the art, preferably by dry impregnation, impregnation in excess or by deposition-precipitation according to methods well known to those skilled in the art. The deposition of the Group VIB and VIII metal components and phosphorus can be carried out by one or more impregnations, preferably followed by a drying step as described in step i ") below. particularly preferred, the contacting according to step i) is carried out by the second embodiment of step i), that is to say by post-impregnation.according to a particularly preferred variant, the catalyst used In step b) is prepared according to the preparation method described in US 2013/008829. More specifically, step i) of the catalyst preparation process 3013 720 23 of step b) can comprise the following successive steps which will be detailed below: (i ') an amorphous alumina-based support is impregnated with at least one solution containing at least one Group VIB metal, at least one Group VIII metal and said phosphorus to obtain a suppor When impregnated, the impregnated support obtained in step i ') is dried at a temperature below 180 ° C. without subsequent calcination to obtain a dried impregnated support, and the dried impregnated support obtained is impregnated with the dried impregnated support. step i ") by an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an impregnated catalytic precursor, i" ") is allowed to mature the impregnated catalyst precursor obtained at step im) to obtain said catalyst precursor. In step i '), the introduction of the Group VIB and Group VIII metals onto the amorphous support can be advantageously effected by one or more excess solution impregnations on the amorphous support, or preferably one or more dry impregnation and preferably by dry impregnation of said amorphous support, with an aqueous or organic solution containing metal precursors. The impregnation step may be carried out in the same manner as described for the preparation of the oxide catalyst described in step a). The Group VIB and Group VIII metal precursors are those described for step a). Said phosphorus and any other dopant selected from boron and / or fluorine may be introduced in the same manner as described in step a). The precursors of phosphorus, boron and fluorine are those described in step a). The introduction of the group VIB and group VIII and phosphorus metals into or onto the amorphous support is then advantageously followed by a drying step i ") during which the solvent (which is usually water) is removed at a temperature between 50 and 180 ° C, preferably between 60 and 150 ° C or between 65 and 145 ° C and very preferably between 70 and 140 ° C or between 75 and 130 ° C C. The step of drying the dried impregnated support thus obtained is never followed by a step of calcining in air at a temperature above 200 ° C. Preferably, in step i '), said impregnated support is obtained by dry impregnation of a solution comprising Group VIB and Group VIII metal precursors, and phosphorus on a shaped calcined alumina-based amorphous support, followed by drying at a temperature below 180 ° C, preferably between 50 and 180 ° C, d preferred way between 60 and 150 ° C and very preferably between 75 and 130 ° C is thus obtained an impregnated support dried at the end of step i ").
    [0019] According to step i "), said dried impregnated support is impregnated with an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen, and preferably C1-C4 dialkyl succinate. (and in particular dimethyl succinate) and acetic acid According to another variant, the impregnating solution of step im) preferably comprises citric acid The impregnation solution comprising at least one of said organic compound is preferably an aqueous solution The molar ratio of organic compound (s) containing oxygen and / or nitrogen by group VIB element (s) impregnated with the catalytic precursor, engaged on the catalyst is between 0.05 to 2 mol / mol, preferably between 0.1 to 1.8 mol / mol, preferably between 0.15 and 1.5 mol / mol before drying of step ii) When the organic component is a mixture of Cl -C 4 dialkyl succinate (and of dimethyl succinate) and acetic acid, said components are advantageously introduced into the impregnating solution of stage i "') of the process according to the invention in an amount corresponding to: - a molar ratio of succinate dialkyl (for example dimethyl) group (s) of group VIB impregnated with the catalyst precursor of between 0.05 to 2 mol / mol, preferably between 0.1 to 1.8 mol / mol, preferably between 0.15 and 1.5 mol / mol, at a molar ratio of acetic acid per element (s) of the group VIB impregnated with the catalytic precursor of between 0.1 and 5 mol / mol, preferably between 0.5 at 4 mol / mol, preferably between 1.3 and 3 mol / mol and very preferably between 1.5 and 2.5 mol / mol. The said organic compound (s) can (advantageously) be deposited in one or more steps, either by slurry impregnation, by excess impregnation, or by impregnation with water. dry, or by any other means known to those skilled in the art. According to step i "), the organic compound containing oxygen or nitrogen is introduced onto the dried impregnated support by at least one impregnation step and preferably by a single impregnation step of an impregnating solution on said dried catalyst precursor, and particularly preferably by a single dry impregnation step, According to step i "") of the preparation process according to the invention, the impregnated catalytic precursor resulting from of step i "') is subjected to a maturation step. It is advantageously carried out at atmospheric pressure and at a temperature of between 17 ° C. and 50 ° C. and generally a maturation period of between ten minutes and forty eight hours and preferably between thirty minutes and five hours is sufficient. Longer durations are not excluded. It is thus obtained is a catalyst precursor at the end of step i ". In accordance with step ii) of the preparation process according to the invention, the catalyst precursor resulting from step i) is subjected to in a drying step at a temperature of less than 200 ° C., without calcining it beforehand, the drying step ii) of the process according to the invention is advantageously carried out by any technique known to those skilled in the art. carried out at atmospheric pressure or under reduced pressure, this step is preferably carried out at atmospheric pressure.This step ii) is advantageously carried out at a temperature of between 50 and less than 200 ° C., preferably of between 60 and 180 ° C. and most preferably between 80 and 160 ° C. Step ii) is advantageously carried out in a traversed bed using air or any other hot gas. heat is carried out in a fixed bed, the gas used is either air or an inert gas such as argon or nitrogen. Very preferably, the drying is carried out in a traversed bed in the presence of nitrogen.
    [0020] Preferably, this step has a duration of between 30 minutes and 4 hours, and preferably between 1 hour and 3 hours. At the end of step ii) of the process according to the invention, a dried catalyst is obtained, also called "additivated catalyst", which is not subjected to any subsequent calcination step in air, for example at a temperature greater than 200 ° C. Prior to its use, it is advantageous to convert the additive catalyst used in step b) into a sulphurized catalyst in order to form its active species. This activation or sulphurization phase is carried out by methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere in the presence of hydrogen and hydrogen sulphide. At the end of step ii) of the process according to the invention, the said additive catalyst obtained is therefore advantageously subjected to a step iii) of sulphurization, without an intermediate calcination step.
    [0021] Said additivated catalyst is advantageously sulphured ex situ or in situ. The same sulfurizing agents as those described for the catalyst in oxide form can be used in step a). When the sulphurization is carried out in situ, the sulphurization of the catalyst of step b) is advantageously carried out at the same time as the sulphidation of the catalyst of step a). Application of the Process According to the Invention in a Hydrocracking Process The hydrotreatment process according to the invention is advantageously used as pretreatment in a hydrocracking process, and more particularly in a so-called "one-step" hydrocracking process. Or in a so-called "two-step" hydrocracking process. The hydrocracking process makes it possible to convert petroleum fractions, in particular vacuum distillates (DSV) into lighter and more valuable products (gasoline, middle distillates). A so-called "one-step" hydrocracking process initially comprises, in a general manner, a high hydrotreatment, the purpose of which is to carry out extensive hydrodenitrogenation and desulphurisation of the feed before it is sent to the feed (s). hydrocracking catalysts. The one-step hydrocracking process is particularly advantageous when the said hydrocracking catalyst (s) comprises a support comprising zeolite crystals. This high hydrotreatment of the feed causes only a limited conversion of the feedstock into lighter fractions, which remains insufficient and must therefore be completed on the more active hydrocracking catalyst (s). However, it should be noted that no effluent separation takes place between the different catalytic beds: all of the effluent leaving the catalytic hydrotreatment bed is injected onto the catalyst bed (s) containing the said hydrocracking catalyst (s) then a separation of the products formed is carried out. This version of the hydrocracking has a variant which has a recycling of the unconverted fraction to at least one of the hydrocracking catalytic beds for further conversion of the feedstock. Advantageously, the hydrotreatment process according to the invention comprising the specific sequence according to steps a) and b), is carried out upstream of a hydrocracking catalyst in a one-step hydrocracking process. It also makes it possible to limit the organic nitrogen content at the end of the pretreatment stage in order to protect the zeolite hydrocracking catalyst which is very sensitive to organic nitrogen. "two stages", comprises a first step which aims, as in the "one step" process, to perform the hydrotreatment of the feed, but also to achieve a conversion of the latter of the order in general of 40 at 60%. The effluent from the first step then undergoes separation, generally by distillation, usually called intermediate separation, which aims to separate the conversion products from the unconverted fraction. In the second stage of the two-stage hydrocracking process according to the invention, only the fraction of the feedstock not converted in the first stage is treated. This separation allows the two-stage hydrocracking process according to the invention to be more selective in middle distillate (kerosene + diesel) than the one-step process according to the invention. Indeed, the intermediate separation of the conversion products avoids their "over-cracking" in naphtha and gas in the second step on the (s) hydrocracking catalyst (s). Furthermore, it should be noted that the unconverted fraction of the feedstock treated in the second step generally contains very low levels of NH 3 as well as organic nitrogen compounds, generally less than 20 ppm by weight or even less than 10 ppm by weight. . Said first step is carried out in the presence of the specific sequence of catalysts according to the invention, and a hydrocracking catalyst in order to perform a hydrotreatment and a conversion of the order in general of 40 to 60%. The catalytic beds of the specific sequence of catalysts according to the invention are advantageously upstream of the hydrocracking catalyst. Said second step is generally carried out in the presence of a hydrocracking catalyst of different composition from that present for the implementation of said first step. The hydrocracking processes are generally carried out at a temperature of between 250 and 480 ° C., advantageously between 320 and 450 ° C., preferably between 330 and 435 ° C., in an IDession of between 2 and 25 MPa, preferably between 3 and 20 MPa, the space velocity (volume flow rate of charge divided by the volume of the catalyst) being between 0.1 and 20 h -1 and preferably between 0.1 and 6 h -1, preferably between 0.2 and 3h-1, and the amount of hydrogen introduced is such that the volume ratio of hydrogen liter / liter of hydrocarbon is between 80 and 50001/1 and most often between 100 and 2000 1/1.
    [0022] The hydrocracking catalysts are of the bifunctional type: they combine an acid function with a hydro-dehydrogenating function. The acid function is provided by porous supports whose surfaces generally vary from 150 to 800 m 2 g -1 and having a surface acidity, such as halogenated aluminas (chlorinated or fluorinated in particular), combinations of boron oxides and aluminum, amorphous or crystalline mesoporous aluminosilicates and zeolites dispersed in an oxide binder. The hydro-dehydrogenating function is provided by the presence of an active phase based on at least one Group VIB metal and optionally at least one Group VIII metal of the periodic table of the elements. The most common formulations are nickel-molybdenum (NiMo) and nickel-tungsten (NiW) and more rarely cobalt-molybdenum (CoMo). After preparation, the hydro-dehydrogenating function is often in oxide form. The usual methods leading to the formation of the hydro-dehydrogenating phase of the HCK catalysts consist in depositing the molecular precursor (s) of at least one Group VIB metal and optionally at least one metal of the group. group VIII on an acidic oxide support by the so-called "dry impregnation" technique followed by the maturation, drying and calcination steps leading to the formation of the oxidized form of the said metal (s) used ( s). Since the active and stable form for the HCK processes is the sulphurized form, these catalysts must undergo a sulphurization step. This can be carried out in the unit of the associated process (this is called in-situ sulphurization) or prior to the loading of the catalyst into the unit (this is called ex situ sulphurization). Application of the process according to the invention in an FCC process Alternatively, the hydrotreatment process according to the invention is advantageously carried out as pretreatment in a fluidized-bed catalytic cracking process (or FCC method for Fluid Catalytic Cracking according to US Pat. Anglo-Saxon terminology). The FCC process can be performed in a conventional manner known to those skilled in the art under suitable cracking conditions to produce lower molecular weight hydrocarbon products. For example, a brief description of catalytic cracking (the first industrial implementation of which dates back to 1936 (HOUDRY process) or 1942 for the use of fluidized bed catalyst) can be found in ULLMANS. ENCYCLOPEDIA OF INDUSTRIAL CHEMISTRY VOLUME A 18, 1991 , pages 61 to 64. A conventional catalyst comprising a matrix, optionally an additive and at least one zeolite is usually used. The amount of zeolite is variable but usually from about 3 to 60% by weight, often from about 6 to 50% by weight and most often from about 10 to 45% by weight. The zeolite is usually dispersed in the matrix. The amount of additive is usually about 0 to 30% by weight and often about 0 to 20% by weight. The amount of matrix represents the complement at 100% by weight. The additive is generally selected from the group formed by the oxides of Group IIA metals of the Periodic Table of Elements such as for example magnesium oxide or calcium oxide, rare earth oxides and titanates of Group IIA metals. The matrix is most often a silica, an alumina, a silica-alumina, a silica-magnesia, a clay or a mixture of two or more of these products. The most commonly used zeolite is zeolite Y. The cracking is carried out in a substantially vertical reactor either in riser mode or in dropper mode. The choice of the catalyst and the operating conditions are functions of the desired products as a function of the filler treated as is for example described in the article by M. MARCILLY pages 990-991 published in the review of the French Petroleum Institute nov. -Dec. 1975 pages 969-1006. The operation is usually at a temperature of about 450 to about 600 ° C and reactor residence times of less than 1 minute often from about 0.1 to about 50 seconds. The pretreatment also makes it possible to limit the organic nitrogen content at the end of the pretreatment stage in order to protect the zeolite-based catalytic cracking catalyst which is very sensitive to organic nitrogen.
    [0023] Examples The following examples demonstrate that a hydrotreatment process according to the invention using an additivated oxide / catalyst catalyst chain has improved activity, especially in terms of HDN, and improved stability compared to a process using only catalysts with additives.
    [0024] Preparation of catalysts A, B, C and D: Preparation of support A matrix composed of ultrafine tabular boehmite or alumina gel was used. This gel was mixed with an aqueous solution containing 66% nitric acid (7% by weight of acid per gram of dry gel), then kneaded for 15 minutes. At the end of this mixing, the paste obtained is passed through a die having cylindrical orifices with a diameter of 1.6 mm. The extrudates are then dried overnight at 120 ° C and then calcined at 600 ° C for 2 hours in moist air containing 50 g of water per kg of dry air. Extruded supports having a specific surface area of 300 m 2 / g are thus obtained. X-ray diffraction analysis reveals that the support is composed solely of cubic gamma-alumina of low crystallinity. Catalyst A: Calcined NiMoP / Alumina Catalyst The alumina support described above, which is in the extruded form, is added in the case of nickel-based catalyst A, nickel, molybdenum and phosphorus. . The impregnating solution is prepared by hot dissolving the molybdenum oxide and nickel hydroxycarbonate in the solution of phosphoric acid in aqueous solution in order to obtain a formulation of approximately 4/22/5 expressed in weight% of oxides of nickel, of molybdenum and in weight of phosphoric anhydride relative to the amount of dry matter of the final catalyst. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 8 hours and then dried overnight at 90 ° C. Calcination at 450 ° C. for 2 hours leads to catalyst A. The final composition of catalyst A expressed in the form of oxides is then the following: MoO 3 = 22.0 ± 0.2 (% by weight), NiO = 4 , 1 + - 0.1 (wt%) and P2O5 = 5.0 + - 0.1 (wt%). Catalyst B: NiMoP / alumina catalyst additive with acetic acid and dimethyl succinate (DMSU) On the alumina support described above and which is in the extruded form, is added in the case of catalyst B based on nickel, nickel, molybdenum and phosphorus. The impregnating solution is prepared by hot dissolving the molybdenum oxide and nickel hydroxycarbonate in the solution of phosphoric acid in aqueous solution in order to obtain a formulation of approximately 5/25/6 expressed in weight% of oxides of nickel, of molybdenum and in weight of phosphoric anhydride relative to the amount of dry matter of the final catalyst. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 8 hours and then dried overnight at 90 ° C. The dried impregnated support of the catayseur C is then additivé by dry impregnation of a solution containing a mixture of dimethyl succinate (DMSU) and acetic acid (at 75% purity). The molar ratios are as follows: DMSU / Mo = 0.85 mol / mol, DMSU / acetic acid = 0.5 mol / mol. The catalyst is further matured for 3 hours at 20 ° C in air and then dried in a bed-type oven passed through 120 ° C for 3 hours.
    [0025] The final composition of the catalyst B expressed in the form of oxides is then the following: MoO3 = 25.1 + - 0.2 (% by weight), NiO = 5.1 + - 0.1 (% by weight) and P2O5 = 6.0 + - 0.1 (% by weight). Catalyst C: NiMoP / alumina catalyst additive with citric acid The alumina support described above, which is in the extruded form, is added in the case of nickel-based catalyst C, nickel, molybdenum and phosphorus. The impregnating solution is prepared by hot dissolving the molybdenum oxide and nickel hydroxycarbonate and citric acid in the solution of phosphoric acid in aqueous solution in order to obtain a formulation of approximately / 25/6 expressed in% by weight of oxides of nickel, molybdenum and% by weight of phosphoric anhydride relative to the amount of dry matter of the final catalyst. The amount of citric acid expressed in molar ratio to molybdenum is citric acid / Mo = 0.4 mol / mol. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 8 h, then dried overnight at 90 ° C and then dried in a bed-type oven passed through at 140 ° C for 3 h. The final composition of the catalyst C expressed as oxides is then the following: MoO3 = 22.5 + - 0.2 (% by weight), NiO = 4.2 + - 0.1 (% by weight) and P2O5 = 5.0 + - 0.1 (% by weight).
    [0026] Catalyst D: NiMoWP / silica-alumina catalyst additive with citric acid A silica-alumina powder was prepared by coprecipitation with a composition of 30% SiO 2 and 70% Al 2 O 3. A catalyst support containing this silica-alumina was then manufactured. For this purpose, a matrix composed of the silica alumina prepared above is mixed with an aqueous solution containing 66% nitric acid (7% by weight of acid per gram of dry gel) and then kneaded for 15 minutes. At the end of this mixing, the paste obtained is passed through a die having trilobal orifices with a diameter of 2 mm. The extrudates are then dried overnight at 120 ° C and calcined at 550 ° C for 2 hours in air. The extrudates are finally treated under steam at 750 ° C. for 2 hours.
    [0027] These extrudates constitute the silica-alumina support. The impregnating solution is prepared by hot dissolving the molybdenum oxide and nickel hydroxycarbonate, phosphotungstic acid and citric acid in the solution of phosphoric acid in aqueous solution in order to obtain a formulation approximately 6/2/18/5 expressed in% by weight of oxides of nickel, molybdenum, tungsten and% by weight of phosphoric anhydride relative to the amount of dry matter of the final catalyst. The amount of citric acid expressed in molar ratio to molybdenum is citric acid / Mo = 0.4 mol / mol. The final composition of the catalyst D expressed in the form of oxides is then the following: MoO3 = 6.2 + - 0.2 (% by weight), NiO = 2.4 + - 0.1 (% by weight) W03 = 18.1 + - 0 , 1 (wt%) and P205 = 5.0 + - 0.1 (wt%). Evaluation of different sequences of catalysts A, B, C and D in hydrotreatment of a vacuum distillate The feed used is a vacuum distillate and has a TMP of 474 ° C. (T5% = 389 ° C., T50% = 468 ° C. C, T 70% = 498 ° C). Characteristics of the feed are as follows: sulfur 2.6% wt, nitrogen 1350 ppm, basic nitrogen 392 ppm, resins 9.1% wt. The test is conducted in an isothermal pilot reactor fixed bed traversed, flowing fluids from bottom to top. The reactor comprises two catalytic zones making it possible to evaluate different sequences of the catalysts A, B, C and D. The charge first passes through the first zone charged with the first catalyst and then the second zone charged with the second catalyst. According to Example 1 (not in accordance with the invention), the entirety of the two catalytic zones (100% of the volume) contains additivated catalyst (catalyst B). According to Example 2 (not in accordance with the invention), all of the two catalytic zones (100% of the volume) contain calcined catalyst (catalyst A).
    [0028] According to Examples 3, 4 and 5 (in accordance with the invention), the first zone is charged with a calcined catalyst (catalysts A: 30% of the volume), then the second with an additivated catalyst (catalyst B, C or D: 70% of the volume). After sulphurization in situ at 350 ° C. in the unit under pressure using the vacuum distillate of the test, to which 2% by weight of dimethyl disulphide is added, the hydrotreating test was carried out under the following operating conditions: a total pressure of 150 bar (15 MPa), a VHV of 2 h -1, an H2 / charge ratio of 1000 l / h and a temperature of 380 ° C. The following table shows the percentage of HDN and HDS carried out in the reactor as well as the stability of the catalytic sequence. The HDN percentage is calculated in the following way: HDN (%) = (N outbound) Nentry. The HDS percentage is calculated as follows: HDS (%) = (Sentredress) Input - The stability is calculated as follows: (% HDN at 600h /% HDN at 300h). The results clearly show that the "catalyst in oxide / catalyst additivated" sequence (Examples 3, 4 and 5) makes it possible to obtain a higher catalytic activity in HDN while maintaining a high HDS, and a higher stability than a series of catalyst additives alone (Example 1) or a sequence "catalyst in the form of oxide" alone (Example 2). Table HDN, HDS and stability Example Loading catalyst (s) in the reactor HDN HDS Stability (first zone / second zone) (%) (`) / ()) 1 100% vol catalyst B (NiMoP additive) 93 99.8 90 comparative 2 100% vol. Catalyst A (calcined NiMoP) 84 99.8 90 comparative 3 30% vol. Catalyst A (calcined NiMoP) 96 99.8 95 according to + 70% vol. Catalyst B (NiMoP additive) the invention 4 30% vol. Catalyst A (calcined NiMoP) + 70 vol. C catalyst (NiMoP additive) 94 99.9 92 according to the invention 5 70% vol catalyst A (calcined NiMoP) 95 99.8 92 according to + 30% vol. Catalyst D (NiMoWP additive) the invention
    权利要求:
    Claims (15)
    [0001]
    REVENDICATIONS1. Process for the hydrotreatment of a hydrocarbon feedstock containing nitrogen compounds with a content greater than 250 ppm by weight and having a weighted average temperature greater than 380 ° C., comprising the following steps: a) said feed is contacted in the presence of hydrogen hydrocarbon product with at least a first catalyst comprising an amorphous support based on alumina, phosphorus, and an active phase formed of at least one Group VIB metal in oxide form and at least one Group VIII metal in oxide form said first catalyst being prepared according to a process comprising at least one calcination step, b) the effluent obtained in step a) is brought into contact with the hydrogen in the presence of hydrogen, with at least one second catalyst comprising an amorphous carrier based on of alumina, phosphorus, an active phase formed of at least one Group VIB metal and at least one Group VIII metal, and at least one organic compound containing oxygen and / or nitrogen, said second catalyst being prepared by a process comprising the following steps: i) at least one component of a Group VIB metal, at least one component of a Group VIII metal, phosphorus and at least one organic compound containing oxygen and / or nitrogen with the support, so as to obtain a catalyst precursor, ii) drying said catalyst precursor from step i) at a temperature below 200 ° C, without calcining it later, so as to obtain a hydrotreated effluent.
    [0002]
    2. Method according to claim 1, wherein for the catalyst of step a) or b), the metal of group VIB is selected from molybdenum, tungsten and the mixture of these two elements, and the metal of group VIII is selected from cobalt, nickel and the mixture of these two elements.
    [0003]
    3. Method according to one of claims 1 or 2, wherein for the catalyst of step a) or b), the metal content of group VIB is between 5 and 40% by weight of metal oxide group VIB relative to the total weight of the catalyst, the group VIII metal content is between 1 and 10% by weight of group VIII metal oxide relative to the total weight of the catalyst and the phosphorus content is between 0.1 and 10% by weight of P2O5 relative to the total weight of the catalyst.
    [0004]
    4. Method according to one of claims 1 to 3, wherein the catalyst of step a) or b) further contains at least one dopant selected from boron and fluorine and a mixture of boron and fluorine.
    [0005]
    5. Method according to one of claims 1 to 4, wherein the organic compound is one or more selected from a carboxylic acid, an alcohol, an aldehyde, an ester, an amine, an amino carboxylic acid, an amino alcohol , a nitrile or an amide.
    [0006]
    The process according to claim 5, wherein the organic compound is one or more selected from ethylene glycol, glycerol, polyethylene glycol (with a molecular weight of 200 to 1500), acetophenone, 2 , 4-pentanedione, pentanole, acetic acid, maleic acid, oxalic acid, tartaric acid, formic acid, citric acid and C1-C4 dialkyl succinate.
    [0007]
    The process according to claim 5, wherein the organic compound comprises at least the combination of C1-C4 dialkyl succinate and acetic acid or wherein the organic compound comprises at least citric acid.
    [0008]
    8. Method according to one of claims 1 to 7, wherein the catalyst of step a) or b) has further undergone a sulfurization step.
    [0009]
    9. Method according to one of claims 1 to 8, wherein the basic nitrogen content in the feed is greater than or equal to 60 ppm.
    [0010]
    The method according to one of claims 1 to 9, wherein each of the steps a) and b) is carried out at a temperature between 200 and 450 ° C, at a pressure of between 0.5 and 30 MPa, at a temperature of hourly volume velocity between 0.1 and 20 h -1 and with a hydrogen / charge ratio expressed as a volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid charge of between 501 and 20001/1 .
    [0011]
    11. Method according to one of claims 1 to 10, wherein step a) is performed in a first zone containing the first catalyst that occupies a volume V1, and step b) is performed in a second zone containing the second catalyst which occupies a volume V2, the distribution of volumes V1 / V2 being between 10% vol / 90% vol and 50% vol / 50% vol respectively of the first and second zone.
    [0012]
    12. Method according to one of claims 1 to 11, wherein step i) of step b) comprises the following successive steps: i ') impregnating an amorphous support based on alumina with at least one solution containing at least one Group VIB metal, at least one Group VIII metal and said phosphorus to obtain an impregnated support, i ") the impregnated support obtained in step i ') is dried at a temperature below 180 ° C without subsequently calcining to obtain a dried impregnated support, the dried impregnated support obtained in step i ") is impregnated with an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an impregnated catalyst precursor, i "") is allowed to mature the impregnated catalyst precursor obtained in step im) to obtain said catalyst precursor.
    [0013]
    13. Method according to one of claims 1 to 12, wherein the effluent obtained in step a) is subjected to a separation step for separating a heavy fraction and a light fraction containing the H2S and NH3 formed during of step a), said heavy fraction being subsequently introduced in step b).
    [0014]
    14. hydrocracking process using the hydrotreatment process according to claims 1 to 13, wherein is brought into contact in the presence of hydrogen and under the hydrocracking operating conditions said hydrotreated effluent with at least one catalyst; hydrocracking so as to obtain a hydrocracked effluent.
    [0015]
    15. Fluidized catalytic cracking process using the hydrotreatment process according to claims 1 to 13, wherein the catalytic cracking operating conditions are brought into contact with said hydrotreated effluent with at least one catalytic cracking catalyst so as to form a catalytic cracking process. to obtain a cracked effluent.
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    同族专利:
    公开号 | 公开日
    HRP20171637T1|2017-12-15|
    CN104673373B|2018-01-12|
    RU2651269C2|2018-04-19|
    CL2014003244A1|2015-11-20|
    US20150144529A1|2015-05-28|
    HUE035024T2|2018-03-28|
    EP2878651A1|2015-06-03|
    EP2878651B1|2017-07-26|
    RU2014147969A|2016-06-20|
    CN104673373A|2015-06-03|
    CA2872293A1|2015-05-28|
    CA2872293C|2021-07-27|
    PT2878651T|2017-10-23|
    ES2643987T3|2017-11-27|
    US9683180B2|2017-06-20|
    FR3013720B1|2015-11-13|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US4574120A|1984-10-15|1986-03-04|Shell Oil Company|Method for preparing high activity silica supported hydrotreating catalysts|
    US20050247602A1|2004-04-22|2005-11-10|Shih Stuart S|Process to manufacture low sulfur diesel fuels|
    WO2007084438A2|2006-01-17|2007-07-26|Exxonmobil Research And Engineering Company|Selective catalysts for naphtha hydrodesulfurization|
    WO2008045550A1|2006-10-11|2008-04-17|Exxonmobil Research And Engineering Company|Hydroprocessing methods for bulk group viii/vib metal catalysts|FR3075220A1|2017-12-19|2019-06-21|IFP Energies Nouvelles|PROCESS FOR HYDROTREATING VACUUM DISTILLATES USING A SPECIFIC COMBINATION OF CATALYSTS|JPS526711B1|1971-02-01|1977-02-24|
    US4012340A|1971-02-01|1977-03-15|Chiyoda Kako Kensetsu Kabushiki Kaisha|Process for preparing catalysts for hydrodesulfurization|
    US4392945A|1982-02-05|1983-07-12|Exxon Research And Engineering Co.|Two-stage hydrorefining process|
    US4534852A|1984-11-30|1985-08-13|Shell Oil Company|Single-stage hydrotreating process for converting pitch to conversion process feedstock|
    US4902404A|1988-07-05|1990-02-20|Exxon Research And Engineering Company|Hydrotreating process with catalyst staging|
    FR2664507B1|1990-07-13|1995-04-14|Eurecat Europ Retrait Catalys|PROCESS FOR PRETREATING A CATALYST WITH A MIXTURE OF A SULFUR AGENT AND AN ORGANIC REDUCING AGENT.|
    JP2900771B2|1992-11-18|1999-06-02|住友金属鉱山株式会社|Method for producing catalyst for hydrotreating hydrocarbon oil|
    US5389595A|1993-09-30|1995-02-14|Union Oil Company Of California|Hydroprocessing catalyst, its use, and method of preparation|
    DK121993D0|1993-10-28|1993-10-28|Topsoe Haldor As|GRADED CATALYST SYSTEM|
    JP3802106B2|1995-06-08|2006-07-26|日本ケッチェン株式会社|Hydrocarbon oil hydrotreating catalyst, production method thereof and activation method thereof|
    US6235190B1|1998-08-06|2001-05-22|Uop Llc|Distillate product hydrocracking process|
    EP1041133A1|1999-04-02|2000-10-04|Akzo Nobel N.V.|Process for effecting ultra-deep HDS of hydrocarbon feedstocks|
    FR2792551B1|1999-04-20|2001-06-08|Atochem Elf Sa|PROCESS FOR SULFURIZING HYDROTREATMENT CATALYSTS|
    CA2405841C|2000-04-11|2010-02-09|Akzo Nobel N.V.|Process for sulphiding an additive-containing catalyst|
    WO2002020702A1|2000-09-04|2002-03-14|Akzo Nobel N.V.|Process for effecting ultra-deep hds of hydrocarbon feedstocks|
    CA2540286C|2003-10-03|2014-04-15|Albemarle Netherlands B.V.|Process for activating a hydrotreating catalyst|
    CA2776766A1|2009-10-05|2011-04-14|Exxonmobil Research And Engineering Company|Stacking of low activity or regenerated catalyst above higher activity catalyst|
    DK2512662T3|2009-12-16|2014-08-11|IFP Energies Nouvelles|Catalyst for use in hydrotreating comprising metals of groups VIII and VIB and preparation with acetic acid and dialkyl succinate C1-C4|
    FR2972648B1|2011-03-18|2013-04-26|Ifp Energies Now|CATALYST FOR USE IN HYDROTREATMENT COMPRISING METALS OF GROUP VIII AND VIB AND PREPARATION WITH CITRIC ACID AND C1-C4 DIALKYL SUCCINATE|
    FR3013720B1|2013-11-28|2015-11-13|IFP Energies Nouvelles|METHOD FOR HYDROPROCESSING VACUUM DISTILLATES USING A CATALYST SURFACE|FR3013720B1|2013-11-28|2015-11-13|IFP Energies Nouvelles|METHOD FOR HYDROPROCESSING VACUUM DISTILLATES USING A CATALYST SURFACE|
    FR3013721B1|2013-11-28|2015-11-13|Ifp Energies Now|GASOLINE HYDROTREATMENT PROCESS USING A CATALYST SURFACE|
    RU2605950C1|2015-12-25|2017-01-10|Акционерное общество "Всероссийский научно-исследовательский институт по переработке нефти" |Method of vacuum distillates processing|
    EP3778021A4|2018-04-10|2021-11-17|China Petroleum & Chemical Corporation|Hydrorefining catalyst, preparation method therefor and use thereof|
    FR3094985B1|2019-04-12|2021-04-02|Axens|Hydrotreatment process for naphtha|
    CN112717963B|2019-10-28|2022-03-04|中国石油化工股份有限公司|Hydrogenation pretreatment catalyst, and preparation method and application thereof|
    RU2753597C2|2020-01-24|2021-08-18|Публичное акционерное общество "Нефтяная компания "Роснефть" |Method for hydroskimming vacuum gas oil |
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    优先权:
    申请号 | 申请日 | 专利标题
    FR1361800A|FR3013720B1|2013-11-28|2013-11-28|METHOD FOR HYDROPROCESSING VACUUM DISTILLATES USING A CATALYST SURFACE|FR1361800A| FR3013720B1|2013-11-28|2013-11-28|METHOD FOR HYDROPROCESSING VACUUM DISTILLATES USING A CATALYST SURFACE|
    HUE14306682A| HUE035024T2|2013-11-28|2014-10-23|Method for hydrotreating vacuum distillate using a sequence of catalysts|
    EP14306682.7A| EP2878651B1|2013-11-28|2014-10-23|Method for hydrotreating vacuum distillate using a sequence of catalysts|
    ES14306682.7T| ES2643987T3|2013-11-28|2014-10-23|Vacuum distillation hydrotreatment procedure using a sequence of catalysts|
    PT143066827T| PT2878651T|2013-11-28|2014-10-23|Method for hydrotreating vacuum distillate using a sequence of catalysts|
    CA2872293A| CA2872293C|2013-11-28|2014-11-24|Hydrotreatment process for vacuum distillates implementing a catalyst sequence|
    US14/554,242| US9683180B2|2013-11-28|2014-11-26|Vacuum distillate hydrotreatment process employing a concatenation of catalysts|
    RU2014147969A| RU2651269C2|2013-11-28|2014-11-27|Method for hydrotreatment of vacuum distillate using sequence of catalysts|
    CL2014003244A| CL2014003244A1|2013-11-28|2014-11-28|Vacuum distillation hydrotreatment process that uses a concatenation of catalysts.|
    CN201410705782.9A| CN104673373B|2013-11-28|2014-11-28|Using the vacuum distillate hydroprocessing process of catalyst cascade|
    HRP20171637TT| HRP20171637T1|2013-11-28|2017-10-25|Method for hydrotreating vacuum distillate using a sequence of catalysts|
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