• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention describes a process for producing marine fuels from a hydrocarbon fraction obtained from a catalytic cracking unit, a so-called "slurry" slice with a sulfur content greater than 0.5% by weight, and containing at least 80% of compounds having a boiling temperature of at least 360 ° C, and a final boiling temperature of at least 520 ° C, said process comprising: a) a step of filtering the slurry cup so as to removing at least a portion of the fine particles it contains, b) a hydrotreatment step producing a hydrotreated effluent, c) a step of separating the hydrotreated effluent from step (b) to obtain at least a fraction gas and a liquid hydrocarbon fraction, said liquid fraction constituting the desired marine fuel.
    公开号:FR3013723A1
    申请号:FR1361690
    申请日:2013-11-27
    公开日:2015-05-29
    发明作者:Pascal Chatron-Michaud；Jerome Majcher；Frederic Morel
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The present invention relates to the production of marine fuels from a hydrocarbon fraction obtained from the catalytic cracking process, a partially filtered slurry type cut denoted CLO (abbreviation of the English terminology "Clarified oil" ) or decanted DO (for "decanted oil") containing, inter alia, sulfur impurities, and containing at least 80% of compounds having an initial boiling point of not less than 360 ° C, and a final temperature of boiling at least 520 ° C.
    [0002] In the remainder of the text, wherever CLO or DO type cutting will be discussed, it will be in the sense and with the characteristics previously defined. Catalytic cracking is known by the abbreviation FCC (abbreviation of the English terminology "Fluid Catalytic Cracking") and RFCC (abbreviation of the English terminology "Residual Fluid Catalytic Cracking"). The FCC and the RFCC are processes for the conversion of vacuum distillates and / or distillation residues which make it possible in particular to obtain the following products: light gases from liquefied petroleum gases from gasoline cuts a light distillate known under the name of LCO ("Light Cycle Oil") containing at least 80% of compounds having an initial boiling temperature of at least 200 ° C, and a final boiling temperature of at least 300 ° C, an interval of typical distillation of 220 ° C to 350 ° C a heavy distillate known as HCO ("Heavy Cycle Oil") containing at least 80% of compounds having an initial boiling point of at least 300 ° C, and a final boiling temperature of at least 520 ° C, ie a typical distillation range of 350 ° C to 500 ° C optionally (rather for the RFCC), a residue or "slurry" which is generally purified from the particles of catalyst it contains to obtain a clarified oil ("cl arified oil (or CLO) or a decanted oil (or DO). This residue usually has an initial boiling point above 360 ° C. It is this "slurry" cut which constitutes the load of the present process. More particularly, the invention relates to a process for producing marine fuels and marine fuel bases, having good combustion properties with low sulfur content, from a CLO type cut from an FCC or a FCC. a RFCC. The present invention aims to produce marine fuels and marine fuel bases in accordance with the recommendations of the MARPOL convention in terms of equivalent sulfur content, and preferably also complying with the IS08217 standard. Annex VI of the MARPOL Convention aims to gradually reduce the sulfur content of marine fuels. Ultimately, the maximum equivalent sulfur content will be 0.1% m / m in the Sulfur Emission Control Zones (ZCES or ECA "Emission Control Areas") and 0.5% m / m in the rest of the world. Among the marine fuels, IS08217 distinguishes between distillate type fuels and residual type fuels. There exist in these two categories several grades whose viscosity is one of the main elements of differentiation. For residual type fuels, the characteristic reflecting the quality of the combustion is measured by the CCAI (abbreviation of the English terminology "Calculated Carbon Aromaticity Index"). CCAI formula: CCAI = D 1-1 ('log (+0.85)} - S (.6 21 (lu + 273 formula in which 323 D = denotes the density at 15 ° C (kg / m3) V = designates the viscosity (cST) t = the temperature (° C) The correlation between the aromatic character of a fuel and the ignition delay is known to those skilled in the art The formula for calculating the CCIC is described in the latest revision of IS08217, which includes fuel density and viscosity, for all grades of marine residual fuels, IS08217 recommends a maximum CCIB of 870. EXAMINATION OF PRIOR ART The use of hydrocarbon fractions derived from catalytic cracking as fuel bases, especially as bases for marine fuels, has been known for a long time, in particular for lowering the viscosity of fuel oils because of the low viscosity of the cuts resulting from catalytic cracking. , this use is limited in proportion in the fuel pools, and in particular the marine fuel pools, because of the highly aromatic nature of the cuts from catalytic cracking. Beyond a certain content in the mixture, the combustion properties are degraded. In addition, the cuts from catalytic cracking are generally sulfurized, and their incorporation into fuel pools, especially marine fuel pools, becomes increasingly problematic to meet the sulfur specifications of the fuel recommended by Annex VI of the MARPOL Convention of the International Maritime Organization (IMO). In the relevant prior art, mention may be made of the following documents: FR2983208 describes a process for the selective hydrogenation of an HCO heavy cut and its recycling to the catalytic cracking unit in order to improve the production of middle distillates of the catalytic cracking. EP0432235 describes a process for the hydrogenation of LCO, HCO with recycling of the effluent to catalytic cracking in order to obtain gasoline cuts of better quality.
    [0003] None of these documents describe the production of fuel or low-sulfur fuel bases meeting the new recommendations of the International Maritime Organization, and with good combustion properties as required by the new version of the ISO standard. 8217/2012. The present invention describes the recovery conditions of a preferentially filtered "slurry" type hydrocarbon cut resulting from catalytic cracking, said "slurry" cut having a sulfur content greater than 0.5% by weight, and containing at least 80% of compounds having a boiling temperature of at least 360 ° C, and a final boiling temperature of at least 520 ° C, said cup CLO.
    [0004] SUMMARY DESCRIPTION OF THE FIGURE FIG. 1 represents a diagram of the process according to the invention in which the catalytic cracking unit (FILT) (FCC) or (RFCC) was denoted the filtration unit of the "slurry" cup. (RDS) and the hydrotreatment unit, (DIST) the distillation unit downstream of the hydrotreatment unit. The "slurry" charge (denoted C) derived from the unit (FCC) or (RFCC) fed by a conventional charge (A) is introduced into the clarification unit (FILT) so as to eliminate the majority of the particles of size less than 20 microns that are contained in the 20 "slurry" cup. The resulting clarified slurry (denoted CLO) has a fine particle content of less than 300 ppm and preferably less than 100 ppm. The clarified feedstock (CLO) can be mixed with one of the following feeds (denoted by C '): Vacuum residue from the vacuum distillation column, preferably not hydrotreated, Atmospheric residue from the atmospheric distillation column, preferentially no. hydrotreated, - Vacuum distillate from the vacuum distillation column, preferably not hydrotreated, The resulting mixture charge (C and C ', noted C ") is introduced into the hydrotreating unit (RDS) from which it is extracted. an effluent (E) which is sent to a distillation column (DIST) so as to separate at least one gaseous fraction (F) and a liquid hydrocarbon fraction (G), said liquid fraction constituting a marine fuel in the sense of IS08217 The gaseous fraction (F) joins the gasoline pool (PC) fueled at least in part by the FCC or RFCC cracking gasoline (B).
    [0005] SUMMARY DESCRIPTION OF THE INVENTION The present invention can be defined as a process for producing marine fuels from a hydrocarbon feedstock derived from a catalytic cracking (FCC or RFCC), called "slurry" feedstock, and preferentially filtered, so-called then "CLO", having a sulfur content of at least 0.5% by weight, and containing at least 80% of compounds having a boiling point of at least 360 ° C, and a final boiling temperature at least 520 ° C. The process according to the present invention makes it possible to obtain at least one liquid hydrocarbon fraction having a sulfur content of less than or equal to 0.5% by weight and a CCAI of less than 870, said process comprising the following successive stages: a) a filtration step (FILT) of the "slurry" cut so as to remove at least a portion of the fine particles it contains, leading to a clarified slurry cut noted CLO, b) a hydrotreatment step (RDS) of the CLO cut producing a hydrotreated effluent, c) a separation step (DIST) of the hydrotreated effluent from step (b) to obtain a gaseous fraction (F) and a liquid hydrocarbon fraction (G), said liquid fraction constituting the desired marine fuel. According to a variant of the process for producing marine fuel from a feedstock of the CLO type, the operating conditions of the hydrotreatment step are the following: a temperature of between 300 ° C. and 420 ° C., and preferably comprised between between 340 ° C. and 390 ° C., an absolute pressure of between 5 MPa and 20 MPa, preferably of between 8 MPa and 18 MPa, (MPa is the abbreviation of 106 Pascal), a space velocity of the hydrocarbon feedstock, commonly referred to as VVH, which is defined as the volumetric flow rate of the feed under standard conditions (1 atmosphere and 15 ° C) divided by the total volume of hydrotreatment catalysts, in a range of 0.1 hr-1 at 2.5 h -1, preferably from 0.3 h -1 to 0.8 h -1, a quantity of hydrogen mixed with the feed of between 100 and 3000 normal cubic meters (Nm 3) per cubic meter (m3 ) of liquid charge, preferably between 200 Nm3 / m3 and 2000 Nm3 / m3, and more preferably, between 300 Nm3 / m3 and 1500 Nm3 / m3. According to another variant of the process for producing marine fuel from a CLO type feedstock, in addition to said CLO feedstock, the hydrotreating step (RDS) processes in co-treatment one of the following charges taken alone or as a mixture, in a proportion of not more than 30% by weight relative to the total charge (CLO + co-processed feedstock): - Direct atmospheric or vacuum distillation gas oil, direct residues - OCH Catalytic cracking, - Atmospheric or vacuum direct coking gasoil, - Atmospheric or vacuum direct visco-reduction gasoil, - Hydroconversion gasoil (hydrotreatment and / or hydrocracking) of atmospheric or vacuum. - Catalytic cracking HCO - Hydrotreated or non-hydrotreated atmospheric residue - Hydroconverted or non-hydroconverted atmospheric residue - Hydroconverted or non-hydroconverted vacuum residue - Hydrotreated or non-hydrotreated vacuum residue DETAILED DESCRIPTION OF THE INVENTION In general, the term fuel is understood to mean invention, a hydrocarbon feedstock usable as marine fuel in the sense of the standard IS08217, and by fuel base means a hydrocarbon feedstock which, mixed with other bases, constitutes a marine fuel. Depending on the origin of these bases, in particular depending on the type of crude oil and the type of refining, the properties of these bases, in particular their sulfur content and their viscosity, are very diverse.
    [0006] The hydrocarbon feedstock The hydrocarbon feedstock is derived from a catalytic cracking unit. It has a sulfur content of at least 0.5% by weight, and contains at least 80% of compounds having a boiling point of at least 360 ° C, and a final boiling temperature of at least 520 ° C. The charge therefore consists of at least a portion of a CLO cut resulting from a catalytic cracking process (FCC or RFCC). The feed may also be a mixture of several CLO and / or HCO cuts from several different FCC or RFCC units.
    [0007] The catalytic cracking process producing the CLO feed may be of the FCC or RFCC type and process feedstocks derived from distillate-type petroleum under vacuum or distillation residues. It would not be outside the scope of the invention if catalytic cracking were operated from feedstock from coal, biomass, oil sands or their derivatives, oil shales or their derivatives, parent rock oils or their derivatives. , taken alone or mixed. This load can optionally be treated with at least one co-load. This is called co-treatment.
    [0008] Among the possible co-charges, there may be mentioned diesel-type cuts (containing at least 80% of compounds having a boiling point of at least 200 ° C., and a final boiling point of at least 300 ° C. C) or vacuum gas oil (containing at least 80% of compounds having a boiling temperature of at least 300 ° C, and a final boiling temperature of at least 450 ° C), these cuts being derived from direct distillation of the oils or obtained at the end of a conversion process (with addition of hydrogen or carbon rejection) of hydrocarbon feedstocks derived from petroleum, coal and / or biomass. 11 can therefore be diesel fuel cuts obtained by: Direct distillation ("straight mn diesel" or SRGO) Catalytic cracking ("light cycle oil" or LCO) Coking ("coker gas oil" or CGO) Viscoréduction ("visbreaker gas oil "or VBGO) Hydroconversion (hydrotreating and / or hydrocracking) of residues (" Hydroconverted Gas Oil ") 11 can also be vacuum gas oil cuts obtained by: Distillation (" vacuum gas oil "or VGO) Coking (" coker heavy gas oil "or HCGO) Viscoreduction (" visbreaker heavy gas oil "or VBHGO) Hydroconversion (hydrotreating and / or hydrocracking) of residues (" hydroconverted heavy gas oil ") 11 may also be distillation residue: atmospheric residue hydrotreated or not Hydroconverted or non-hydroconverted atmospheric residue Hydroconverted or non-hydroconverted vacuum residue Hydrotreated or non-hydrotreated vacuum residue The hydrocarbon feedstock CLO may represent at least 50%, and preferably 70% by weight, of the total hydrocarbon feedstock treated by the process. assigned according to the invention.
    [0009] Advantageously, the co-charge (s), as well as the relative proportions of charge and co-charge (s), are chosen so that the hydrotreatment step operates under operating conditions, preferably milder than if the load was treated alone (without co-loading) in order to obtain the same quality of marine fuel. Hydroprocessing step In the context of the present invention, it is understood that the hydrotreatment step (RDS) can be carried out according to all the known embodiments of the person skilled in the art, generally with at least one catalytic bed of type fixed bed and / or bubbling bed type and / or type bed trained.
    [0010] The preferred implementation comprises at least one fixed bed. According to the present invention, the process for treating the catalytic cracking hydrocarbon feedstock of the CLO type comprises a hydrotreating step working under the following conditions: a temperature of between 300.degree. C. and 420.degree. C., and more preferably between 340.degree. ° C and 390 ° C an absolute pressure of between 5 MPa and 20 MPa, preferably between 8 MPa and 18 MPa, a space velocity of the hydrocarbon feedstock, commonly called VVH, which is defined as the volumetric flow of the load in the standard conditions (1 atmosphere and 15 ° C.) divided by the total volume of hydrotreatment catalysts, ranging from 0.1 h -1 to 2.5 h -1, preferably 0.3 h -1 at 0.8 h -1, a quantity of hydrogen mixed with the feedstock of between 100 and 3000 normal cubic meters (Nm3) per cubic meter (m3) of liquid feed, preferably between 200 Nm3 / m3 and 2000 Nm3 / m3, and more preferably between 300 Nm 3 / m3 and 1500 Nm3 / m3.
    [0011] According to another preferred embodiment, the hydrocarbon feedstock of CLO type resulting from catalytic cracking (FCC or RFCC) is mixed before the hydrotreatment step in a proportion of at most 30% by weight relative to the total charge (CLO + co-processed feedstock) with one or more of the following cuts: - direct or atmospheric direct distillation gas oil direct residues - catalytic cracked LCO, - direct atmospheric or vacuum coking gasolines, - direct visco-reduced viscosity or vacuum gasolines, - Hydroconversion gas oil (hydrotreatment and / or hydrocracking) atmospheric or vacuum. - Catalytic cracking HCO - Hydrotreated or non-hydrotreated atmospheric residue - Hydroconverted or non-hydroconverted atmospheric residue - Hydroconverted or non-hydroconverted vacuum residue - Hydrotreated or non-hydrotreated vacuum residue The hydrotreatment catalysts used are generally granular catalysts comprising, on a support, at minus a metal or metal compound having a hydrodehydrogenating function. These catalysts may advantageously be catalysts comprising at least one Group VIII metal, generally selected from the group consisting of nickel and cobalt, and / or at least one Group VIB metal, preferably molybdenum and / or tungsten. . For example, a catalyst comprising from 0.5% to 10% by weight of nickel, preferably from 1% to 5% by weight of nickel (expressed as nickel oxide NiO), and from 1% to 30% may be used. by weight of molybdenum, preferably from 5% to 20% by weight of molybdenum (expressed as molybdenum oxide MoO 3) on a mineral support. This support may for example be chosen from the group consisting of alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of these minerals. The process according to the invention comprises a step of separating (DIST) the effluent from the hydrotreatment step, allowing at least one gaseous fraction to be obtained and at least one gaseous fraction to be separated off. minus a liquid hydrocarbon fraction. The step of separating the effluent from the hydrotreating step generally comprises atmospheric distillation and / or vacuum distillation. Advantageously, the separation step comprises an atmospheric distillation which makes it possible to obtain a liquid fraction. At the end of the separation step, a liquid hydrocarbon fraction (G) having a sulfur content of less than or equal to 0.5% by weight, preferably less than or equal to 0.3% by weight, and more preferably still less than or equal to 0.1% by weight. This liquid hydrocarbon fraction constitutes the marine fuel base or directly a marine fuel, within the meaning of the present invention. Advantageously, all of the liquid hydrocarbon effluent obtained at the end of the separation step (DIST) has a sulfur content of less than or equal to 0.5% by weight, and preferably less than or equal to 0, 3% by weight. EXAMPLES ACCORDING TO THE INVENTION The following examples illustrate the invention without however limiting its scope. A CLO-type catalytic cracking cup containing 95% by weight of compounds boiling at a temperature above 360 ° C was treated, having a density at 15 ° C of 1.117 g / cm 3, a viscosity of 32.0. cSt at 70 ° C and a sulfur content of 3.70% by weight. Without hydrotreatment, this feedstock does not constitute a marine fuel within the meaning of ISO 8217.
    [0012] Examining the 2012 revision of IS08217, both the density and the sulfur content of the load are too high. The feed is therefore subjected to a hydrotreatment step (RDS), which will allow both to reduce the sulfur content and to reduce the density of the feedstock. The operating conditions are given in Table 1 below. Catalysts HDM / catalyst HDS ratio 1/5 volume H2 / HC inlet section fixed bed excluding 600 consumption H2 (Nm3 / m3 fresh feed) Table 1: Operating conditions of the hydrotreating step Several experiments were carried out: Casl - a Hydrotreatment stage (RDS) treating the CLO feed at the pressure of 18 MPa. Case 2 - a hydrotreating step (RDS) treating the CLO feed at the pressure of 8 MPa. Case 3 - a hydrotreating step (RDS) treating the CLO feedstock and a "straight run" vacuum residue co-feed at a level of 10% by weight at 8 MPa. For each experiment, the effluents from the hydrotreating section are then subjected to a separation step to separate the gases and liquids by means of separators and atmospheric distillation columns. Among the liquids, the compounds boiling at a temperature above 200 ° C constitute the fuel base on which the analyzes are carried out (sulfur, viscosity and CCAI). 25 Casl Case 2 Case 3 Composition of the filler 100% 100% 90% CLO + 10% VR CLO CLO SR Sulfur content of the filler (% m / m) 3.70 3.70 3.59 Density at 15 ° Load C (kg / m3) 1117 1117 1104 Viscosity of the load at 50 ° C (cSt) 47.2 47.2 60 CCAI of the load 1004 1004 988 Temperature (° C) 370 390 380 Partial pressure H2 (MPa) ) 18 8 9 VVH (in hu) 0.3 0.5 0.5 Fuel base performance (% m / m)> 95> 95> 95 Sulfur content of the base 0,04 0,09 0,1 fuel ( % m / m) density at 15 ° C of the fuel base (kg / m3) 986 995 978 viscosity of the fuel base at 50 ° C (cSt) 140 376 390 CCAI of the fuel base 859 856 840 Table 2: Table Comparative step of hydrotreatment The 3 cases are in accordance with the present invention. - Case 1 operates the hydrotreatment step at a pressure of 18 MPa, a temperature of 370 ° C, and a VVH of 0.3h-1 and produces a fuel base obtained at a CCIC less than 860.
    [0013] Due to this CCIC, the low sulfur content, the density and the viscosity lower than the specifications of the RME grade of IS08217, the fuel base obtained according to experiment 1 can be directly upgraded to marine fuel of the RME type. (Can eventually be used in ZCES because of the very low sulfur content of less than 0.1% w / w). - Case 2 operates the hydrotreatment step at a pressure of 8 MPa, a temperature of of 390 ° C, and a VVH of 0.5h-1 and produces a combustible base obtained at a CCAI lower than 860. Because of this CCAI, the low sulfur content, the density and the viscosity below the specifications of the RMK grade of IS08217, the fuel base obtained according to experiment 2 can be directly upgraded to RMK-type marine fuel (which can eventually be used in ZCESs because of the very low sulfur content of less than 0.1. % m / m). Case 3 is a case illustrating the co-treatment of the CLO feedstock with a residue of direct distillation vacuum (so-called "straight run"), having good characteristics, in particular a CCIC of less than 860, and can therefore be valorized in RMG-type marine fuel (which may ultimately be used in ZCESs because of the very low sulfur content of less than 0.1% m / m).
    权利要求:
    Claims (3)
    [0001]
    1) Process for producing marine fuels from a hydrocarbon feedstock from a catalytic cracking unit, called "slurry" filler, having a sulfur content of at least 0.5% by weight, and containing at least 80% of compounds having a boiling point of at least 360 ° C, and a final boiling temperature of at least 520 ° C, process for obtaining at least one liquid hydrocarbon fraction having a lower sulfur content or equal to 0.5% by weight and a CCAI of less than 870, said process comprising the following successive stages: a) a filtration step (FILT) of the "slurry" cut, so as to eliminate at least a portion of the fines particles it contains, resulting in a filtered cut called CLO, b) a hydrotreatment step (RDS) of the CLO feed optionally in co treatment with another hydrocarbon feedstock producing a hydrotreated effluent, c) a separation step (DIST ) of the hydrotreated effluent from the hydrotreating step (RDS) to obtain at least a gaseous fraction F and a liquid hydrocarbon fraction G, said liquid fraction constituting a marine fuel in the sense of the IS08217 standard.
    [0002]
    2) A process for producing marine fuel from a CLO type feedstock according to claim 1, wherein the operating conditions of the hydrotreating step (RDS) are as follows: a temperature of between 300 ° C and 420 ° C ° C, and more preferably between 340 ° C and 390 ° C, an absolute pressure of between 5 MPa and 20 MPa, preferably between 8 MPa and 18 MPa, a space velocity of the hydrocarbon feedstock, (VVH defined as the flow rate volumetric load under the standard conditions (1 atmosphere and 15 ° C) divided by the total volume of hydrotreatment catalysts), in a range from 0.1 h-1 to 2.5 h-1, preferably from 0.3 h-1 to 0.8 h-1, a quantity of hydrogen mixed with the feedstock of between 100 and 3000 normal cubic meters (Nm3) per cubic meter (m3) of liquid feed, preferably between 200 Nm3 / m3 and 2000 Nm3 / m3, and more preferably between 300 Nm3 / m3 and 1500 Nm3 / m3,
    [0003]
    3) A process for producing marine fuel from a CLO type feedstock according to claim 1, wherein in addition to the CLO feed, the hydrotreatment step (RDS) processes in co-treatment one of the following feeds singly or in a mixture, in a proportion of not more than 30% by weight relative to the total charge (CLO + co-treated feedstock): - Direct atmospheric or vacuum distillation gas oil - Catalytic cracked LCO, - Direct atmospheric coking gas oil or under vacuum, - Gas visco-reduced direct atmospheric or vacuum, - Hydroconversion gas oil (hydrotreatment and / or hydrocracking) direct residues atmospheric or vacuum. - HCO catalytic cracking - Hydrotreated or non-hydrotreated atmospheric residue - Hydroconverted or non-hydroconverted atmospheric residue - Hydroconverted or non-hydroconverted vacuum residue - Hydrotreated or non-hydrotreated vacuum residue
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    引用文献:
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    法律状态:
    2015-11-05| PLFP| Fee payment|Year of fee payment: 3 |
    2017-08-25| ST| Notification of lapse|Effective date: 20170731 |
    优先权:
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    FR1361690A|FR3013723B1|2013-11-27|2013-11-27|PROCESS FOR THE PRODUCTION OF LOW SULFUR CONTENT OF MARINE FUELS FROM A HYDROCARBON CUT FROM SLURRY CATALYTIC CRACKING, USING A SPECIFIC HYDROTREATMENT STEP.|FR1361690A| FR3013723B1|2013-11-27|2013-11-27|PROCESS FOR THE PRODUCTION OF LOW SULFUR CONTENT OF MARINE FUELS FROM A HYDROCARBON CUT FROM SLURRY CATALYTIC CRACKING, USING A SPECIFIC HYDROTREATMENT STEP.|
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    JP2014191091A| JP2015059220A|2013-09-20|2014-09-19|Method of producing ship fuel of low sulfur content from hco produced by catalytic decomposition or slurry-type hydrocarbon-containing fraction using hydrogenation treatment stage|
    KR20140125000A| KR20150032815A|2013-09-20|2014-09-19|Process for producing marine fuels with low sulphur content from a hydrocarbon-containing cut originating from catalytic cracking of the hco or slurry type, and employing a hydrotreating stage|
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