WO2014096602A1 - Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif - Google Patents
Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif Download PDFInfo
- Publication number
- WO2014096602A1 WO2014096602A1 PCT/FR2013/052923 FR2013052923W WO2014096602A1 WO 2014096602 A1 WO2014096602 A1 WO 2014096602A1 FR 2013052923 W FR2013052923 W FR 2013052923W WO 2014096602 A1 WO2014096602 A1 WO 2014096602A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- solvent
- mixture
- fraction
- deasphalting
- coal
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/14—Hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/0463—The hydrotreatment being a hydrorefining
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
Definitions
- the present invention relates to a novel process for the refining of a heavy hydrocarbon feedstock, in particular from atmospheric distillation or vacuum distillation of crude oil.
- the filler mixed with hydrogen circulates through a plurality of fixed bed reactors arranged in series and filled with catalysts, the first reactor or reactors being used for predominantly hydrodemetallization of the filler (step called HDM) and a part of the hydrodesulphurization (step called HDS), the last reactor (s) being used to carry out the deep refining of the feedstock, and in particular the hydrodesulfurization.
- the total pressure is typically between 10 and 20 MPa and the temperatures between 340 and 420 ° C.
- SUBSTITUTE SHEET especially when a low sulfur content is required or good quality charges for other units such as catalytic cracking.
- the sequence of an RDS unit with a catalytic cracking unit in a fluidized bed of residues (RFCC according to the English terminology) with a view to producing predominantly gasoline or propylene is particularly sought after because the low content of metals and in Carbon Conradson (also called CCR) the heavy cut output of the RDS unit allows optimized use of the RFCC unit, especially in terms of the unit's operating expenses.
- the Conradson carbon content is defined by ASTM D 482 and represents for the skilled person a well-known evaluation of the amount of carbon residues produced after combustion under standard conditions of temperature and pressure.
- the RDS units have at least two major disadvantages: on the one hand, the residence times to reach the required specifications on the effluents are very high (typically from 3 to 7 hours) which requires large units.
- the cycle times time after which the performance of the unit can no longer be maintained, because the catalysts are deactivated and / or clogged) are relatively short compared to hydrotreating processes of lighter cuts. This induces shutdowns of the unit and the replacement of all or part of the spent catalysts by new catalysts.
- the reduction of the size of the RDS units as well as the increase of the cycle time is therefore a strong industrial challenge.
- US Patent Application No. 20/4/00696851 discloses a refining scheme based on the sequencing of a distillation step of a feedstock to produce a distillate M1 and a residue M2; a step of hydrogenation and desulfurization of the M1 distillate to produce an effluent M3; furthermore, a step of deasphalting the residue M2 with a solvent to produce a deasphalted oil DAO M4 and an asphalt residue M5; a step of hydrodemetallation / hydrodesulphurization of at least a portion of the deasphalted oil DAO M4 to obtain a refined oil M6; a step of combining the effluent M3 and the refined oil M6.
- SUBSTITUTE SHEET so-called ultimate asphalt ie specifically containing the refractory structures at the subsequent stages of the refining process, the feedstock and obtaining a deasphalted oil yield DAO that can go beyond the threshold of dependence on the aforementioned solvent.
- the present invention relates to a process for refining a heavy hydrocarbon feedstock comprising the following steps:
- step b) a step of hydrotreating at least a portion of the DAO deasphalted oil phase resulting from step a) in the presence of hydrogen in at least one fixed bed reactor containing at least one hydrodemetallization catalyst under conditions to obtain an effluent with a reduced content of metals and carbon Conradson, c) optionally, a step of catalytic cracking of at least a portion of the effluent from step b) in at least one fluidized bed reactor under conditions allowing to produce a gas fraction, a gasoline fraction, a LCO fraction, an HCO and slurry fraction.
- the polar solvent used is chosen from pure aromatic or naphtho-aromatic solvents, polar solvents containing heteroelements, or their mixture or sections rich in aromatics such as sections from the FCC (Fluid Catalytic Cracking). ), cuts derived from coal, biomass or biomass / coal mixture.
- the apolar solvent used comprises a solvent composed of saturated hydrocarbon comprising a carbon number greater than or equal to 2, preferably between 2 and 9.
- the volume ratio of the mixture of polar and apolar solvents on the mass of the load is between 1/1 and 10/1 expressed in liters per kilogram.
- the feed is a heavy feedstock resulting from atmospheric distillation or vacuum distillation of crude oil, typically having boiling temperatures of at least 300 ° C. and containing impurities, in particular sulfur. , nitrogen and metals or a residual fraction resulting from the direct liquefaction of coal or a H-Coal TM vacuum distillate or a residual fraction resulting from the direct liquefaction of the lignocellulosic biomass alone or mixed with coal and / or a residual petroleum fraction.
- step b) is carried out with at least one catalyst which mainly ensures the hydrodesulfurization under conditions making it possible to obtain a liquid effluent with a reduced content of metals, Conradson carbon and sulfur.
- step b) is carried out at a pressure of between 2 and 35 MPa, a temperature of between 300 and 500 ° C. and a hourly space velocity of between 0.1 and 5 h -1 .
- the effluent from step b) is subjected to a step c) of separation allowing to separate at least:
- step c) when step c) is carried out, that is carried out on at least one mixture comprising at least one vacuum distillate cut and / or a vacuum residue cut.
- the heavy hydrocarbon feedstock according to the process of the invention is advantageously a heavy load resulting from the atmospheric distillation or the vacuum distillation of crude oil, typically having boiling temperatures of at least 300 ° C. and containing impurities, in particular sulfur, nitrogen and metals.
- the filler according to the process of the invention may be of petroleum origin of atmospheric residue type or vacuum residue from conventional crude (API degree> 20 °), heavy (API degree between 10 and 20 °) or extra heavy (degree API ⁇ 10 °).
- Said filler may also be a residual fraction ex-direct liquefaction of coal (atmospheric residue or vacuum residue from, for example, the H-Coal TM process) or an H-Coal TM vacuum distillate or a residual fraction from direct liquefaction of lignocellulosic biomass alone or mixed with coal and / or a residual petroleum fraction
- solvent mixture according to the invention is understood to mean a mixture of at least one polar solvent and at least one apolar solvent according to the invention.
- the heavy hydrocarbon feedstock is subjected to a step a) of selective deasphalting carried out in one step.
- Said step a) of selective deasphalting comprises contacting said filler with a mixture of at least one polar solvent and at least one apolar solvent in an extraction medium. The proportions of polar solvent and apolar solvent are adjusted according to the properties of the filler and the degree of asphalt extraction desired.
- Step a) of selective deasphalting makes it possible to go further in maintaining the solubilization in the DAO oil matrix of all or part of the so-called refractory molecular structures. It makes it possible to go further in maintaining the solubilization in the DAO oil matrix of all or part of the polar structures of heavy resins and asphaltenes, which are the main constituents of the asphalt phase.
- the selective deasphalting step a) thus makes it possible to choose which type of polar structures remain solubilized in the DAO oil matrix. Therefore, step a) of selective deasphalting makes it possible to selectively extract the load only a part of this asphalt, that is to say the most polar and most refractory structures in the refining processes.
- Asphalt yield 100- [DAO oil yield]
- the step a) of selective deasphalting can be carried out in an extraction column, preferably in a mixer-settler. This step is carried out by liquid / liquid extraction in one step.
- the liquid / liquid extraction of step a) is carried out under subcritical conditions for the solvent mixture, that is to say at a temperature below the critical temperature of the solvent mixture.
- the extraction temperature is advantageously between 50 and 350 ° C, preferably between 90 and 320 ° C, more preferably between 100 and 310 ° C, even more preferably between 120 and 310 ° C, still more preferably between 150 and 310 ° C and the pressure is preferably between 0.1 and 6 MPa, preferably between 2 and 6 MPa.
- volume ratio of the solvent mixture according to the invention (volume of polar solvent + volume of apolar solvent) on the mass of filler is generally between 1/1 and 10/1, preferably between 2/1 to 8/1 , expressed in liters per kilogram.
- the solvent mixture according to the invention used in step a) is a mixture of at least one polar solvent and at least one apolar solvent.
- the polar solvent used may be chosen from pure aromatic or naphtho-aromatic solvents, polar solvents containing heteroelements, or their mixture.
- the aromatic solvent is advantageously chosen from monoaromatic hydrocarbons, preferably benzene, toluene or xylenes alone or as a mixture; diaromatic or polyaromatic; naphthenocarbon aromatic hydrocarbons such as tetralin or indane; heteroatomic aromatic hydrocarbons (oxygenated, nitrogenous, sulfurous) or any other family of compounds having a more polar character than saturated hydrocarbons such as, for example, dimethylsulfoxide (DMSO), dimethylformamide (DMF), tetrahydrofuran (THF) .
- the polar solvent used in the process according to the invention can also be a cut rich in aromatics.
- the sections rich in aromatics according to the invention can be, for example,
- SHEET FCC Fluid Catalytic Cracking
- cuts such as heavy gasoline or LCO (light cycle oil), as well as cuts derived from coal, biomass or biomass / coal mixture with possibly a residual petroleum charge after thermochemical conversion with or without hydrogen, with or without a catalyst
- the polar solvent used is a pure monoaromatic hydrocarbon or in admixture with another aromatic hydrocarbon.
- the apolar solvent used is preferably a solvent composed of saturated hydrocarbon, said saturated hydrocarbon comprising a carbon number greater than or equal to 2, preferably between 2 and 9.
- saturated hydrocarbon solvents are used pure or as a mixture (for example mixture of alkanes and / or cycloalkanes or light petroleum fractions such as naphtha).
- the boiling point of the polar solvent of the solvent mixture according to the invention is greater than the boiling point of the apolar solvent.
- the variation of the proportion between the polar solvent (s) and the apolar solvent (s) constitutes a true key for adjusting step a) of selective deasphalting according to the invention.
- step a) of selective deasphalting makes it possible to selectively extract, whatever the load, an ultimate so-called asphalt fraction, enriched with impurities and refractory compounds at the subsequent stages of the refining process. while leaving at least a portion of the polar structures of the heavy resins and the less polar asphaltenes non-refractory to the subsequent stages of the refining process solubilized in the oil matrix.
- the proportion of polar solvent in the mixture of polar solvent and apolar solvent is between 0.1 and 99.9%, preferably between 0.1 and 95%, preferably between 1 and 95%, so more preferably between 1 and 90%, even more preferably between 1 and 85%, and very preferably between 1 and 80%.
- the percentage of polar solvent in the polar and apolar solvent mixture is a function of the nature of the charge, the molecular structures composing a charge varying from one charge to another. All the charges do not have the same refractory character. The rate of asphalt to be extracted is not necessarily the same depending on the nature of the load.
- the nature of the load also depends on its origin: oil, derived from coal, or biomass type.
- the selective deasphalting step a) has the advantage of allowing a considerable improvement in the deasphalted DAO oil yield over a range hitherto unexplored by conventional deasphalting.
- the selective deasphalting makes it possible to cover by adjustment of the proportion polar solvent and of apolar solvent the range 75-99,9% of yield in oil DAO.
- the yield of DAO oil at the end of stage a), whatever the feedstock, is advantageously 50 and 99.9%, preferably 75 to 99.9%, more preferably 80 to 99%, 9%.
- step a) has the advantage of improving the properties of the initial charges by obtaining a deasphalted oil less sulfur-containing, containing less metals and less carbon-rich Conradson (CCR), which allows a
- Step b) of hydrotreating at least a portion of the oil phase DAO from step a) is carried out under fixed bed hydrotreatment conditions.
- Step b) is carried out under conditions known to those skilled in the art.
- step b) is carried out under a pressure of between 2 and 35 MPa and a temperature of between 300 and 500 ° C. and a hourly space velocity of between 0.1 and 5 h -1 ; preferably at a pressure between 10 and 20 MPa and a temperature between 340 and 420 ° C and a hourly volume velocity of between 0, 1 and 2 h "1 .
- Hydroprocessing is understood to mean, in particular, hydrodesulphurization (HDS) reactions, hydrodemetallation (HDM) reactions, accompanied by hydrogenation, hydrodeoxygenation, hydrodenitrogenation, hydrodearomatization, hydroisomerization, hydrogenation reactions. hydrodealkylation, hydrocracking, hydrodephalting and Conradson carbon reduction.
- the hydrotreatment step comprises a first hydrodemetallation step comprising one or more hydrodemetallation zones in fixed beds optionally preceded by at least two hydrotreatment guard zones, and a second subsequent step of hydrodesulfurization comprising one or more hydrodesulfurization zones in fixed beds and in which during the first hydrodemetallization stage, the charge and hydrogen are passed under hydrodemetallation conditions over a hydrodemetallization catalyst, and then during the second subsequent step, the effluent from the first step is passed under hydrodesulfurization conditions over a hydrodesulfurization catalyst.
- This process known as HYVAHL-F TM, is described in US5417846.
- step a) is carried out in one or more hydrodesulfurization zones in fixed beds.
- the hydrotreatment catalysts used are preferably known catalysts and are generally granular catalysts comprising, on a support, at least one metal or metal compound having a hydrodehydrogenating function. These catalysts are advantageously catalysts comprising at least one Group VIII metal, generally selected from the group consisting of nickel and / or cobalt, and / or at least one Group VIB metal, preferably molybdenum and / or tungsten. .
- a catalyst comprising from 0.5 to 10% by weight of nickel and preferably from 1 to 5% by weight of nickel (expressed as nickel oxide NiO) and from 1 to 30% 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 will, for example, be selected from the group formed by alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of these minerals.
- this support contains other doping compounds, in particular oxides chosen from the group formed by boron oxide, zirconia, ceria, titanium oxide, phosphoric anhydride and a mixture of these oxides.
- alumina support Most often an alumina support is used and very often a support of alumina doped with phosphorus and possibly boron.
- phosphorus pentoxide P2O5 When phosphorus pentoxide P2O5 is present, its concentration is less than 10% by weight.
- boron trioxide B 2 O 5 When boron trioxide B 2 O 5 is present, its concentration is less than 10% by weight.
- the alumina used is usually a ⁇ or ⁇ alumina. This catalyst is most often in the form of extrudates.
- the total content of Group VIB and VIII metal oxides is often from 5 to 40% by weight and generally from 7 to 30% by weight and
- SUBSTITUTE SHEET weight ratio expressed as metal oxide between metal (or metals) of group VIB on metal (or metals) of group VIII is in general from 20 to 1 and most often from 10 to 2.
- a hydrotreating step including a hydrodemetallation step (HDM) then a hydrodesulfurization step (HDS), it is most often used specific catalysts adapted to each step.
- Catalysts that can be used in the HDM step are, for example, indicated in the patents EP1 13297, EP113284, US5221656, US5827421, US7119045, US5622616 and US5089463.
- HDM catalysts are preferably used in the reactive reactors.
- Catalysts usable in the HDS step are for example indicated in the patents EP113297, EP1 13284, US6589908, US4818743 or US6332976. It is also possible to use a mixed catalyst that is active in HDM and HDS for both the HDM section and the HDS section as described in patent FR2940143. Prior to injection of the feedstock, the catalysts used in the process according to the present invention are preferably subjected to a treatment sulfurat / one (in-situ or ex-situ).
- the products obtained during step b) are subjected to a separation step from which it is advantageous to recover:
- the refining process according to the invention comprises a catalytic cracking step carried out on a mixture comprising at least one vacuum distillate (VGO) cut and / or a vacuum residue cut (VR) resulting from the step b).
- VGO vacuum distillate
- VR vacuum residue cut
- said cuts come from a prior separation step following step b).
- Step c) is carried out under conventional catalytic cracking conditions that are well known to those skilled in the art, in at least one fluidized-bed reactor so as to produce a gaseous fraction, a gasoline fraction, an LCO fraction or an HCO fraction. and slurry.
- This step can be carried out in a conventional manner known to those skilled in the art under the appropriate conditions for cracking the residue in order to produce lower molecular weight hydrocarbon products.
- Descriptions of operation and catalysts for use in fluidized bed cracking in this step are described, for example, in US-A-4695370, EP-B-184517, US-A-4959334, EP-B- 323297, US-A-4965232, US-A-5120691, US-A-5344554, US-A-5449496, EP-A-485259, US-A-5286690, US-A-5324696 and EP-A-699224 with the descriptions are considered incorporated in the present invention.
- 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%
- SUBSTITUTE SHEET by weight and often from about 0 to 20% by weight.
- the amount of matrix represents the complement at 100% by weight.
- the additive is generally chosen from the group formed by the oxides of the MA group metals of the periodic table of elements such as, for example, magnesium oxide or calcium oxide, rare earth oxides and titanates of metals. Group IIA.
- 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 depend on the desired products as a function of the feedstock treated, as described, for example, in the article by M. MARCILLY, pages 990-991 published in the review of the Institut für du Pperile 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 catalytic cracking step c) is advantageously a catalytic cracking step in a fluidized bed, for example according to the process developed by the Applicant called R2R. This step can be carried out in a conventional manner known to those skilled in the art under the appropriate conditions for cracking the residue in order to produce lower molecular weight hydrocarbon products.
- Particularly preferred catalytic cracking catalysts are those containing at least one zeolite usually in admixture with a suitable matrix such as, for example, alumina, silica, silica-alumina.
- the method according to the invention has various advantages, namely:
- Example 1 (comparative): Implementation of an RDS unit alone
- Example 1 corresponds to the implementation of a hydrotreatment of charge A without prior pretreatment, in an RDS unit alone in a fixed bed, in the presence of hydrogen, under the operating conditions of the beginning of cycle indicated in Table 2 .
- HF 858, HM 848 and HT 438 The catalysts marketed by the company Axens are used under the following commercial references: HF 858, HM 848 and HT 438:
- HF 858 active catalyst predominantly in HDM
- HM 848 active catalyst in HDM and HDS
- HT 438 active catalyst predominantly in HDS.
- Yields Yield, expressed as weight percent
- sulfur content S, expressed as weight percent
- viscosity at 100 ° C CSt
- the consumption of hydrogen represents 1.40% by weight of the filler.
- Example 2 (Comparative): Implementation of a conventional deasphalting unit before the RDS unit
- Example 2 the same charge A, the same RDS unit and the same catalysts as in Example 1 are used.
- a conventional deasphalting unit (conventional SDA) is added upstream of the RDS unit.
- the charge rate A at the input of the conventional SDA is identical to that at the input of the RDS unit of Example 1.
- the operating conditions of the conventional deasphalting unit and the yields and characteristics of the deasphalted DAO oil obtained are given in Tables 4 and 5.
- the solvent used is butane.
- the fixed bed RDS unit is used on the DAO deasphalted oil resulting from conventional SDA deasphalting, in the presence of hydrogen, under the cycle start operating conditions given in Table 6.
- Example 1 The same catalysts are used as in Example 1.
- the RDS unit is used under operating conditions that make it possible to have outlet effluents of the same yield and quality as those obtained.
- Yields Yield, expressed as a percentage by weight
- sulfur content S, expressed as a percentage by weight
- viscosity at 100 ° C CSt
- CCR Conradson carbon content
- the performance of the RDS unit is maintained during the cycle by increasing the temperature to a limiting temperature (typical of 410 ° C). This increase in temperature compensates for the loss of catalytic activity over time. Thus a lower cycle start temperature allows to extend the cycle time (gain of 5 months of cycle compared to Example 1).
- Example 3 (according to the invention): selective deasphalting + RDS
- Example 3 corresponds to Example 2 with the only difference that the selective deasphalting according to the invention (selective SDA step a)) is used upstream of the RDS unit, with an input charge flow rate.
- the SDA identical to the one at the input of the RDS of Example 1.
- the RDS unit is operated under operating conditions allowing output effluents of the same yield and quality as those obtained in Example 1 to be obtained , using less severe operating conditions on the RDS unit.
- Example 1 The same catalysts are used as in Example 1.
- the RDS unit is operated under operating conditions allowing output effluents of the same yield and quality as those obtained in Example 1, using less severe operating conditions on the RDS unit.
- Yields Yield, expressed as a percentage by weight
- sulfur content S, expressed as a weight percentage
- viscosity at 100 ° C CSt
- CCR Conradson carbon content
- the maintenance of the unit's performance is ensured by increasing the temperature to a limiting temperature (typical of 410 ° C). This increase in temperature compensates for the loss of catalytic activity over time. Thus a lower cycle start temperature allows to extend the cycle time (gain of 5 months of cycle compared to Example 1).
- Example 4 (according to the invention): Selective deasphalting + RDS
- Example 4 corresponds to Example 3 with the only difference of the operating conditions of the RDS unit corresponding to those of Example 1.
- the aim is to evaluate the improvement in the quality of the effluents from the RDS unit (and therefore the load quality of a downstream RFCC unit), induced by the addition of the selective SDA upstream of the RDS unit. .
- the fixed bed RDS unit is used on the DAA deasphalted oil derived from the selective SDA (characteristics of the deasphalted oil DAO of Example 3), in the presence of hydrogen, under the operating conditions of the beginning of the cycle. shown in Table 1 1.
- Yields (Yield, expressed as weight percent), sulfur content (S, expressed as a weight percentage), viscosity at 100 ° C (CSt) and Conradson carbon content (CCR, expressed as a percentage by weight) of the cuts produced. at the output of the RDS unit are given in Table 12.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020157019527A KR20150096518A (ko) | 2012-12-18 | 2013-12-03 | 선택적 탈아스팔트화를 시행하는 중질 탄화수소 공급물의 정제 방법 |
US14/652,813 US9963643B2 (en) | 2012-12-18 | 2013-12-03 | Process for refining a heavy hydrocarbon feed using a selective deasphalting step |
CN201380066511.7A CN104995283B (zh) | 2012-12-18 | 2013-12-03 | 使用选择性脱沥青步骤精炼重质烃进料的方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR12/03471 | 2012-12-18 | ||
FR1203471A FR2999600B1 (fr) | 2012-12-18 | 2012-12-18 | Procede de raffinage d'une charge hydrocarbonee lourde mettant en oeuvre un desasphaltage selectif |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2014096602A1 true WO2014096602A1 (fr) | 2014-06-26 |
Family
ID=47902035
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2013/052923 WO2014096602A1 (fr) | 2012-12-18 | 2013-12-03 | Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif |
Country Status (5)
Country | Link |
---|---|
US (1) | US9963643B2 (fr) |
KR (1) | KR20150096518A (fr) |
CN (1) | CN104995283B (fr) |
FR (1) | FR2999600B1 (fr) |
WO (1) | WO2014096602A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3014110B1 (fr) * | 2013-12-03 | 2015-12-18 | Ifp Energies Now | Procede de conversion d'une charge hydrocarbonee lourde integrant un desasphaltage selectif en cascade avec recyclage d'une coupe desasphaltee |
SG11202002019XA (en) * | 2017-07-14 | 2020-04-29 | Exxonmobil Res & Eng Co | Forming asphalt fractions from three-product deasphalting |
Citations (30)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB708051A (en) * | 1949-04-13 | 1954-04-28 | Socony Vacuum Oil Co Inc | Hydrocarbon modified propane deasphalting |
US4305812A (en) | 1980-06-19 | 1981-12-15 | Mobil Oil Corporation | Solvent deasphalting by polarity gradient extraction |
US4450067A (en) * | 1981-04-30 | 1984-05-22 | Mobil Oil Corporation | Distillation-induced extraction process |
US4455216A (en) | 1980-12-04 | 1984-06-19 | Mobil Oil Corporation | Polarity gradient extraction method |
EP0113284A1 (fr) | 1982-12-30 | 1984-07-11 | Institut Français du Pétrole | Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères |
EP0113297A1 (fr) | 1982-12-31 | 1984-07-11 | Institut Français du Pétrole | Procédé d'hydrotraitement convertissant en au moins deux étapes une fraction lourde d'hydrocarbures contenant des impuretés soufrées et des impuretés métalliques |
US4695370A (en) | 1984-08-02 | 1987-09-22 | Institut Francais Du Petrole | Process and apparatus for fluid bed catalytic cracking |
EP0184517B1 (fr) | 1984-12-07 | 1988-05-18 | Compagnie De Raffinage Et De Distribution Total France | Perfectionnement aux procédés et dispositifs pour le craquage catalytique de charges d'hydrocarbures |
US4818743A (en) | 1983-04-07 | 1989-04-04 | Union Oil Company Of California | Desulfurization catalyst and the catalyst prepared by a method |
US4959334A (en) | 1987-12-21 | 1990-09-25 | C. Compagnie de Raffinage et de Distribution | Fluidized-bed catalyst regeneration |
US4965232A (en) | 1988-03-09 | 1990-10-23 | Compagnie De Raffinage Et De Distribution Total France | Process for fluidized-bed catalyst regeneration |
EP0323297B1 (fr) | 1987-12-30 | 1991-06-19 | Société Anonyme dite: COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE | Procédé de conversion d'hydrocarbures en lit fluidisé |
US5089463A (en) | 1988-10-04 | 1992-02-18 | Chevron Research And Technology Company | Hydrodemetalation and hydrodesulfurization catalyst of specified macroporosity |
EP0485259A1 (fr) | 1990-11-08 | 1992-05-13 | Total Raffinage Distribution S.A. | Procédé et dispositif d'homogénéisation, à l'intérieur d'un réacteur tubulaire de craquage d'hydrocarbures à lit de particules solides fluidisées, du mélange de ces particules et des vapeurs d'hydrocarbures à traiter |
US5120691A (en) | 1989-06-16 | 1992-06-09 | Institut Francais Du Petrole | Process for regulating or checking the thermal level of a pulverulent solid incorporating a heat exchanger with fluidized bed compartments |
US5221656A (en) | 1992-03-25 | 1993-06-22 | Amoco Corporation | Hydroprocessing catalyst |
US5286690A (en) | 1991-04-26 | 1994-02-15 | Institut Francais Du Petrole | Method of heat exchange of solid particles for regeneration in catalytic cracking |
US5324696A (en) | 1991-11-14 | 1994-06-28 | Institut Francais Du Petrole | Process and heat exchange apparatus for solid particles for double regeneration in catalytic cracking |
US5344554A (en) | 1990-10-03 | 1994-09-06 | Institut Francais Du Petrole | Downflow fluid catalytic cracking process and apparatus |
US5417846A (en) | 1990-03-29 | 1995-05-23 | Institut Francais Du Petrole | Hydrotreatment method for a petroleum residue or heavy oil with a view to refining them and converting them to lighter fractions |
EP0699224A1 (fr) | 1993-05-10 | 1996-03-06 | Inst Francais Du Petrole | Procede de regulation du niveau thermique d'un solide dans un echangeur de chaleur presentant des nappes cylindriques de tubes |
US5622616A (en) | 1991-05-02 | 1997-04-22 | Texaco Development Corporation | Hydroconversion process and catalyst |
US5827421A (en) | 1992-04-20 | 1998-10-27 | Texaco Inc | Hydroconversion process employing catalyst with specified pore size distribution and no added silica |
US6332976B1 (en) | 1996-11-13 | 2001-12-25 | Institut Francais Du Petrole | Catalyst containing phosphorous and a process hydrotreatment of petroleum feeds using the catalyst |
US6589908B1 (en) | 2000-11-28 | 2003-07-08 | Shell Oil Company | Method of making alumina having bimodal pore structure, and catalysts made therefrom |
US20040069685A1 (en) | 2000-11-30 | 2004-04-15 | Makoto Inomata | Method of refining petroleum |
US7119045B2 (en) | 2002-05-24 | 2006-10-10 | Institut Francais Du Petrole | Catalyst for hydrorefining and/or hydroconversion and its use in hydrotreatment processes for batches containing hydrocarbons |
FR2940143A1 (fr) | 2008-12-18 | 2010-06-25 | Inst Francais Du Petrole | Catalyseurs d'hydrodemetallation et d'hydrodesulfuration et mise en oeuvre dans un procede d'enchainement en formulation unique |
FR2958656A1 (fr) * | 2010-04-13 | 2011-10-14 | Inst Francais Du Petrole | Procede d'hydroconversion de charges petrolieres via une technologie en slurry permettant la recuperation des metaux du catalyseur et de la charge mettant en oeuvre une etape d'extraction. |
FR2964388A1 (fr) * | 2010-09-07 | 2012-03-09 | IFP Energies Nouvelles | Procede de conversion de residu integrant une etape de desasphaltage et une etape d'hydroconversion avec recyclage de l'huile desasphaltee |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3287254A (en) * | 1964-06-03 | 1966-11-22 | Chevron Res | Residual oil conversion process |
US4278529A (en) * | 1980-06-30 | 1981-07-14 | Kerr-Mcgee Refining Corporation | Process for separating bituminous materials with solvent recovery |
US4493765A (en) * | 1983-06-06 | 1985-01-15 | Exxon Research And Engineering Co. | Selective separation of heavy oil using a mixture of polar and nonpolar solvents |
US5092983A (en) * | 1986-09-12 | 1992-03-03 | The Standard Oil Company | Process for separating extractable organic material from compositions comprising said extractable organic material intermixed with solids and water using a solvent mixture |
GB8828335D0 (en) * | 1988-12-05 | 1989-01-05 | Shell Int Research | Process for conversion of heavy hydrocarbonaceous feedstock |
-
2012
- 2012-12-18 FR FR1203471A patent/FR2999600B1/fr not_active Expired - Fee Related
-
2013
- 2013-12-03 CN CN201380066511.7A patent/CN104995283B/zh not_active Expired - Fee Related
- 2013-12-03 WO PCT/FR2013/052923 patent/WO2014096602A1/fr active Application Filing
- 2013-12-03 KR KR1020157019527A patent/KR20150096518A/ko not_active Application Discontinuation
- 2013-12-03 US US14/652,813 patent/US9963643B2/en not_active Expired - Fee Related
Patent Citations (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB708051A (en) * | 1949-04-13 | 1954-04-28 | Socony Vacuum Oil Co Inc | Hydrocarbon modified propane deasphalting |
US4305812A (en) | 1980-06-19 | 1981-12-15 | Mobil Oil Corporation | Solvent deasphalting by polarity gradient extraction |
US4455216A (en) | 1980-12-04 | 1984-06-19 | Mobil Oil Corporation | Polarity gradient extraction method |
US4450067A (en) * | 1981-04-30 | 1984-05-22 | Mobil Oil Corporation | Distillation-induced extraction process |
EP0113284A1 (fr) | 1982-12-30 | 1984-07-11 | Institut Français du Pétrole | Procédé de traitement d'une huile lourde ou d'une fraction d'huile lourde pour les convertir en fractions plus légères |
EP0113297A1 (fr) | 1982-12-31 | 1984-07-11 | Institut Français du Pétrole | Procédé d'hydrotraitement convertissant en au moins deux étapes une fraction lourde d'hydrocarbures contenant des impuretés soufrées et des impuretés métalliques |
US4818743A (en) | 1983-04-07 | 1989-04-04 | Union Oil Company Of California | Desulfurization catalyst and the catalyst prepared by a method |
US4695370A (en) | 1984-08-02 | 1987-09-22 | Institut Francais Du Petrole | Process and apparatus for fluid bed catalytic cracking |
EP0184517B1 (fr) | 1984-12-07 | 1988-05-18 | Compagnie De Raffinage Et De Distribution Total France | Perfectionnement aux procédés et dispositifs pour le craquage catalytique de charges d'hydrocarbures |
US4959334A (en) | 1987-12-21 | 1990-09-25 | C. Compagnie de Raffinage et de Distribution | Fluidized-bed catalyst regeneration |
EP0323297B1 (fr) | 1987-12-30 | 1991-06-19 | Société Anonyme dite: COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE | Procédé de conversion d'hydrocarbures en lit fluidisé |
US4965232A (en) | 1988-03-09 | 1990-10-23 | Compagnie De Raffinage Et De Distribution Total France | Process for fluidized-bed catalyst regeneration |
US5089463A (en) | 1988-10-04 | 1992-02-18 | Chevron Research And Technology Company | Hydrodemetalation and hydrodesulfurization catalyst of specified macroporosity |
US5120691A (en) | 1989-06-16 | 1992-06-09 | Institut Francais Du Petrole | Process for regulating or checking the thermal level of a pulverulent solid incorporating a heat exchanger with fluidized bed compartments |
US5417846A (en) | 1990-03-29 | 1995-05-23 | Institut Francais Du Petrole | Hydrotreatment method for a petroleum residue or heavy oil with a view to refining them and converting them to lighter fractions |
US5449496A (en) | 1990-10-03 | 1995-09-12 | Institut Francais Du Petrole | Downflow fluid catalytic cracking process and apparatus |
US5344554A (en) | 1990-10-03 | 1994-09-06 | Institut Francais Du Petrole | Downflow fluid catalytic cracking process and apparatus |
EP0485259A1 (fr) | 1990-11-08 | 1992-05-13 | Total Raffinage Distribution S.A. | Procédé et dispositif d'homogénéisation, à l'intérieur d'un réacteur tubulaire de craquage d'hydrocarbures à lit de particules solides fluidisées, du mélange de ces particules et des vapeurs d'hydrocarbures à traiter |
US5286690A (en) | 1991-04-26 | 1994-02-15 | Institut Francais Du Petrole | Method of heat exchange of solid particles for regeneration in catalytic cracking |
US5622616A (en) | 1991-05-02 | 1997-04-22 | Texaco Development Corporation | Hydroconversion process and catalyst |
US5324696A (en) | 1991-11-14 | 1994-06-28 | Institut Francais Du Petrole | Process and heat exchange apparatus for solid particles for double regeneration in catalytic cracking |
US5221656A (en) | 1992-03-25 | 1993-06-22 | Amoco Corporation | Hydroprocessing catalyst |
US5827421A (en) | 1992-04-20 | 1998-10-27 | Texaco Inc | Hydroconversion process employing catalyst with specified pore size distribution and no added silica |
EP0699224A1 (fr) | 1993-05-10 | 1996-03-06 | Inst Francais Du Petrole | Procede de regulation du niveau thermique d'un solide dans un echangeur de chaleur presentant des nappes cylindriques de tubes |
US6332976B1 (en) | 1996-11-13 | 2001-12-25 | Institut Francais Du Petrole | Catalyst containing phosphorous and a process hydrotreatment of petroleum feeds using the catalyst |
US6589908B1 (en) | 2000-11-28 | 2003-07-08 | Shell Oil Company | Method of making alumina having bimodal pore structure, and catalysts made therefrom |
US20040069685A1 (en) | 2000-11-30 | 2004-04-15 | Makoto Inomata | Method of refining petroleum |
US7119045B2 (en) | 2002-05-24 | 2006-10-10 | Institut Francais Du Petrole | Catalyst for hydrorefining and/or hydroconversion and its use in hydrotreatment processes for batches containing hydrocarbons |
FR2940143A1 (fr) | 2008-12-18 | 2010-06-25 | Inst Francais Du Petrole | Catalyseurs d'hydrodemetallation et d'hydrodesulfuration et mise en oeuvre dans un procede d'enchainement en formulation unique |
FR2958656A1 (fr) * | 2010-04-13 | 2011-10-14 | Inst Francais Du Petrole | Procede d'hydroconversion de charges petrolieres via une technologie en slurry permettant la recuperation des metaux du catalyseur et de la charge mettant en oeuvre une etape d'extraction. |
FR2964388A1 (fr) * | 2010-09-07 | 2012-03-09 | IFP Energies Nouvelles | Procede de conversion de residu integrant une etape de desasphaltage et une etape d'hydroconversion avec recyclage de l'huile desasphaltee |
Non-Patent Citations (2)
Title |
---|
M. MARCILLY, REVUE DE L'INSTITUT FRANÇAIS DU PÉTROLE, November 1975 (1975-11-01), pages 969 - 1006 |
ULLMANS ENCYCLOPEDIA OF INDUSTRIAL CHEMISTRY, vol. A 18, 1991, pages 61 - 64 |
Also Published As
Publication number | Publication date |
---|---|
KR20150096518A (ko) | 2015-08-24 |
CN104995283B (zh) | 2018-09-18 |
FR2999600A1 (fr) | 2014-06-20 |
CN104995283A (zh) | 2015-10-21 |
US20150337223A1 (en) | 2015-11-26 |
FR2999600B1 (fr) | 2015-11-13 |
US9963643B2 (en) | 2018-05-08 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2015091033A1 (fr) | Nouveau procede integre de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre et en sediments | |
WO2015082313A1 (fr) | Procede de raffinage d'une charge hydrocarbonee lourde mettant en œuvre un desasphaltage selectif en cascade | |
CA2464796C (fr) | Procede de valorisation de charges lourdes par desasphaltage et hydrocraquage en lit bouillonnant | |
EP3303523B1 (fr) | Procede de conversion de charges comprenant une etape d'hydrotraitement, une etape d'hydrocraquage, une etape de precipitation et une etape de separation des sediments pour la production de fiouls | |
EP3018188B1 (fr) | Procede de conversion de charges petrolieres comprenant une etape d'hydrotraitement en lit fixe, une etape d'hydrocraquage en lit bouillonnant, une etape de maturation et une etape de separation des sediments pour la production de fiouls a basse teneur en sediments | |
WO2017186484A1 (fr) | Procédé de conversion comprenant des lits de garde permutables d'hydrodemetallation, une etape d'hydrotraitement en lit fixe et une etape d'hydrocraquage en reacteurs permutables | |
EP3018189B1 (fr) | Procede de conversion de charges petrolieres comprenant une etape de viscoreduction, une etape de maturation et une etape de separation des sediments pour la production de fiouls a basse teneur en sediments | |
CA2607443A1 (fr) | Procede de preraffinage de petrole brut avec hydroconversion moderee en plusieurs etapes de l'asphalte vierge en presence de diluant | |
CA2891872C (fr) | Procede de conversion d'une charge hydrocarbonee lourde integrant un desasphaltage selectif en amont de l'etape de conversion | |
CA2915282C (fr) | Procede de conversion profonde de residus maximisant le rendement en essence | |
CA2891129C (fr) | Procede de conversion d'une charge hydrocarbonee lourde integrant un desasphaltage selectif avec recycle de l'huile desasphaltee | |
WO2019121073A1 (fr) | Procede de conversion de charges lourdes d'hydrocarbures avec recycle d'une huile desasphaltee | |
FR3075810A1 (fr) | Procede ameliore de conversion de residus integrant des etapes d’hydroconversion profonde et une etape de desasphaltage | |
FR3030568A1 (fr) | Procede de conversion profonde de residus maximisant le rendement en gazole | |
FR3008711A1 (fr) | Procede de raffinage d'une charge hydrocarbonee de type residu sous-vide mettant en œuvre un desasphaltage selectif, un hydrotraitement et une conversion du residu sous-vide pour la production d'essence et d'olefines legeres | |
WO2014096602A1 (fr) | Procédé de raffinage d'une charge hydrocarbonée lourde mettant en oeuvre un des désasphaltage sélectif | |
WO2012085406A1 (fr) | Procede de conversion de charge hydrocarbonee comprenant une huile de schiste par hydroconversion en lit bouillonnant, fractionnement par distillation atmospherique et extraction liquide/liquide de la fraction lourde. | |
FR2933711A1 (fr) | Procede de conversion comprenant une viscoreduction de residu, puis un desasphaltage et une hydroconversion | |
WO2012085408A1 (fr) | Procede de conversion de charge hydrocarbonee comprenant une huile de schiste par decontamination, hydroconversion en lit bouillonnant, et fractionnement par distillation atmospherique | |
FR3084372A1 (fr) | Procede de traitement d'une charge hydrocarbonee lourde comprenant un hydrotraitement en lit fixe, deux desasphaltages et un hydrocraquage en lit bouillonnant de l'asphalte | |
FR3084371A1 (fr) | Procede de traitement d'une charge hydrocarbonee lourde comprenant un hydrotraitement en lit fixe, un desasphaltage et un hydrocraquage en lit bouillonnant de l'asphalte | |
FR2970478A1 (fr) | Procede d'hydroconversion en lit fixe d'un petrole brut, etete ou non, un fractionnement, puis un desasphaltage de la fraction lourde pour la production d'un brut synthetique preraffine | |
WO2016192893A1 (fr) | Procédé de conversion de charges comprenant une étape de viscoréduction, une étape de précipitation et une étape de séparation des sédiments pour la production de fiouls |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 13808150 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: P701/2015 Country of ref document: AE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 14652813 Country of ref document: US |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 20157019527 Country of ref document: KR Kind code of ref document: A |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 13808150 Country of ref document: EP Kind code of ref document: A1 |