EP3275975A1 - Hydrotreating-verfahren, bei dem austauschbare schutzreaktoren mit umkehrung der ausflussrichtung und parallelschaltung der reaktoren verwendet werden - Google Patents

Hydrotreating-verfahren, bei dem austauschbare schutzreaktoren mit umkehrung der ausflussrichtung und parallelschaltung der reaktoren verwendet werden Download PDF

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EP3275975A1
EP3275975A1 EP17181791.9A EP17181791A EP3275975A1 EP 3275975 A1 EP3275975 A1 EP 3275975A1 EP 17181791 A EP17181791 A EP 17181791A EP 3275975 A1 EP3275975 A1 EP 3275975A1
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Prior art keywords
reactor
reactors
catalyst
pressure drop
flow
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EP17181791.9A
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English (en)
French (fr)
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EP3275975B1 (de
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Frederic Bazer-Bachi
Cecile Plais
Wilfried Weiss
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/002—Apparatus for fixed bed hydrotreatment processes
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/14—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
    • C10G65/16—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only including only refining steps

Definitions

  • the invention relates to fixed bed processes, and more generally to the hydrotreatment processes of heavy hydrocarbon feedstocks, in particular residues or any hydrogenation of petroleum fractions that can cause clogging of the fixed bed.
  • One of the problems with fixed bed heavy-lift catalytic hydrotreatment is clogging, especially in the upper part of the bed.
  • the catalytic beds more particularly the upper parts of the first catalytic bed in contact with the charge, are likely to clog rather quickly because of the asphaltenes and sediments contained in the charge, which is expressed initially by an increase in the pressure drop (DP) and sooner or later requires a stop of the unit for the replacement of the catalyst.
  • DP pressure drop
  • guard beds arranged upstream of the main reactors.
  • the main task of the guard beds is to protect the catalysts of the main hydrotreating reactors downstream by performing part of the demetallation and filtering the particles contained in the charge which can lead to clogging.
  • the guard beds contain at least hydrodemetallization catalyst, optionally supplemented with inert elements and / or pre-beds (grading in English) and are generally integrated in the hydrodemetallation section HDM in a hydrotreating process of charges heavy ones generally including a first hydrodemetallation section, then a second hydrotreating section HDT.
  • guard beds are generally used to carry out a first hydrodemetallation and filtration, other hydrotreatment reactions (HDS hydrodesulfurization, hydrodenitrogenation HDN, etc.) will inevitably take place in these reactors thanks to the presence of hydrogen and water. a catalyst.
  • PRS Permutable Reactors System
  • PRS Permutable Reactors System
  • the patent FR2681871 describes a hydrotreatment process in at least two stages of a heavy hydrocarbon fraction containing asphaltenes, sulfur impurities and metallic impurities in which, during the first hydrodemetallization stage, is passed through hydrodemetallation conditions, the charge of hydrocarbons and of hydrogen on a hydrodemetallization catalyst, and then during the second subsequent step, the effluent from the first stage is passed under hydrodesulfurization conditions over a catalyst.
  • hydrodesulphurisation characterized in that the hydrodemetallation step comprises one or more hydrodemetallation zones in fixed beds preceded by at least two hydrodemetallation guard zones also in fixed beds, arranged in series for cyclic use consisting of the successive repetition of steps b) and c) defined hereinafter and in that it comprises the following steps: a) a step, in which the guard zones are used together for a duration at most equal to the deactivation and / or clogging time of one of b) a step, during which the deactivated and / or clogged guard zone is short-circuited and the catalyst contained therein is regenerated and / or replaced by fresh catalyst, and c) a step, during which the guard zones are used together the guard zone whose catalyst has been regenerated during the previous step being reconnected and said step being continued for a time at most equal to the time s of deactivation
  • the patent FR2992971 discloses a process for hydrotreatment of heavy charges in a catalytic fixed bed with reversal of the flow direction of the fluids using at least one fixed-bed reactor co-flow descending a gas phase and a liquid phase in which during of the operating cycle of said method, the flow direction of the fluids is inverted to become ascending, the pressure drop threshold triggering the flow reversal is defined from a value DP1 between DP1 and DP1 + (0.5xDP2 ), DP1 being defined as the pressure drop at the beginning of the cycle and DP2 as the pressure loss at the end of the cycle equal to the maximum allowable pressure drop by the process equipment.
  • the invention is an improvement of existing technologies for extending the cycle time of PRS-type reactive reactors, through optimal use of the available fluxes and better use of the catalyst present in the reactors.
  • a step of inversion of the direction of flow and parallelization of the reactors is inserted each time one of the two reactive reactors starts to clog, so when the pressure drop reaches a value- threshold Dpi defined by those skilled in the art as a function of the maximum allowable pressure drop DPmax in the equipment.
  • At least one of the reactors comprises n catalytic beds and the effluent is discharged from said reactor in steps b) and / or e) by lateral withdrawal between a catalytic bed i and a catalytic bed i + 1, n being an integer greater than or equal to 2, i being an integer from 1 to n.
  • said catalytic bed i + 1 denotes the first catalytic bed clogged in the direction of flow.
  • the at least two permutable reactors may each have at least two catalytic beds.
  • the pressure drop threshold Dpi has a value between 30 and 60% of the maximum allowable pressure drop DPmax.
  • the pressure drop threshold Dpi has a value between 35 and 50% of the maximum allowable pressure drop DPmax.
  • the heavy hydrocarbon feed advantageously has an initial boiling temperature of at least 340 ° C and a final boiling temperature of at least 440 ° C.
  • the feedstock may be chosen from atmospheric residues, vacuum residues from direct distillation, crude oils, crude head oils, deasphalting resins, asphalts or deasphalting pitches, residues resulting from conversion processes, extracts aromatic compounds derived from lubricant base production lines, oil sands or derivatives thereof, bituminous shales or their derivatives, parent rock oils or their derivatives, whether alone or in admixture.
  • the filler is chosen from atmospheric residues or residues under vacuum, or mixtures of these residues.
  • the hydrotreatment process according to the invention is advantageously carried out at a temperature of between 320 ° C. and 430 ° C., under a hydrogen partial pressure of between 3 MPa and 30 MPa, at a space velocity (VVH) between 0.05 and 5 volume of filler per volume of catalyst per hour, and with a gaseous hydrogen ratio on hydrocarbon liquid feed of between 200 and 5000 normal cubic meters per cubic meter.
  • VVH space velocity
  • the preliminary hydrodemetallization step can be carried out in the presence of a hydrodemetallation catalyst comprising at least one Group VIII metal, and / or at least one Group VIB metal, on a support used chosen from the group formed.
  • a hydrodemetallation catalyst comprising at least one Group VIII metal, and / or at least one Group VIB metal, on a support used chosen from the group formed.
  • alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of these minerals preferably at a space velocity VVH of each switchable reactor operating between 0.5 and 4 charge volume per volume of catalyst and per hour, very preferably at a space velocity VVH of each operating switchable reactor of between 1 and 2 volume of charge per volume of catalyst per hour.
  • the maximum allowable pressure drop DPmax is between 0.3 and 1 MPa, preferably between 0.5 and 0.8 MPa.
  • the present invention proposes an improvement of existing technologies aimed at lengthening the cycle time of PRS reactors.
  • the proposed improvement is for both new and existing units with some modifications (lines, valves, reactor internals, distributor down flow and up flow, etc.).
  • the present invention consists in reversing the direction of flow during the operating cycle of the PRS permutable reactor system.
  • the present invention relates to a process for the hydrotreatment of a heavy hydrocarbon fraction generally containing asphaltenes, sediments, sulfur, nitrogen and metal impurities, in which the hydrotreatment conditions are previously passed under the hydrocarbon and hydrogen feedstock on a hydrotreating catalyst, in at least two fixed-bed permutable reactors each containing at least one catalytic bed,
  • the present invention thus improves the performance of the reactive reactors as described by the applicant in the patent FR2681871 , integrating, after the steps in which the charge successively passes through all the reactors, additional steps, in which the direction of flow is reversed and the two reactors in parallel.
  • the feed is simultaneously introduced on two reactors.
  • This reversal of the direction of flow makes it possible to delay the rise in the pressure drop of the first reactor put in contact with the charge and thus lengthens its service life.
  • the introduction of a part of the charge on the second reactor while another part of the charge continues to pass through the first reactor placed in contact with the charge also makes it possible to "relieve" the first reactor and also to use optimally all the catalyst present in the reactor.
  • the main advantage of this sequencing is not only a better use of the catalyst present in each reactor, but also a better distribution of the liquid flows, the two reactors having not necessarily being clogged in the same proportions (due to the prior operation in series the amount of clogger charged in each of the reactors is significantly different).
  • the possible fluidization problems related to the change of direction are limited because the flow of fluids is divided by two (which justifies all the more to go into parallel flow), which limits the need for recourse to additional grid-type equipment for containing the expansion of the bed due to fluidization.
  • the loading / unloading of each of these reactors is done on increase of the pressure loss DP only, when one of the reactors is completely clogged, the active phase of the downstream catalyst being used at best.
  • the downstream reactors of the PRS permutable reactors will have an increased lifetime and a better utilization of the catalytic charge.
  • the permutable reactors used as guard zones especially the first guard zone placed in contact with the load, progressively load into metals, coke, sediments and other various impurities.
  • the reactors must be disconnected to perform the replacement or regeneration of catalyst (s).
  • the catalysts are replaced. This moment is called deactivation and / or clogging time.
  • the deactivation and / or clogging time varies depending on the load, the operating conditions and the catalyst (s) used, it is generally expressed by a drop in the catalytic performance (an increase in the concentration metals and / or other impurities in the effluent), an increase in the temperature necessary for the maintenance of a constant hydrotreatment or, in the specific case of a clogging, by a significant increase in the pressure drop.
  • the pressure drop DP expressing a degree of clogging, is measured continuously throughout the cycle on each of the reactors and may be define by a pressure increase resulting from the passage partially blocked through the reactor.
  • the deactivation and / or clogging time is thus defined as the time when the limit value of the pressure drop DPmax is reached.
  • the maximum allowable pressure drop DPmax is generally confirmed when the reactors are commissioned for the first time.
  • the limit value of the maximum allowable pressure drop or pressure drop DPmax is generally between 0.3 and 1 MPa (3 and 10 bar), preferably between 0 and , 5 and 8 MPa (5 and 8 bar).
  • the Up flow may involve the addition of two-phase distribution internals at the bottom of each reactor and the addition of grid type internals at the top of the reactor to prevent possible expansion of the bed.
  • the feedstock treated in the hydrotreatment process according to the invention is advantageously a hydrocarbonaceous feed having an initial boiling point of at least 340.degree. C. and a final boiling point of at least 440.degree.
  • its initial boiling point is at least 350 ° C., preferably at least 375 ° C.
  • its final boiling point is at least 450 ° C., preferably at least 460 ° C. C, more preferably at least 500 ° C, and even more preferably at least 600 ° C.
  • the hydrocarbon feedstock according to the invention may be chosen from atmospheric residues, vacuum residues resulting from direct distillation, crude oils, crude head oils, deasphalting resins, asphalts or deasphalting pitches, process residues. conversion products, aromatic extracts from lubricant base production lines, oil sands or derivatives thereof, oil shales or their derivatives, source rock oils or their derivatives, whether alone or in combination.
  • the fillers being treated are preferably atmospheric residues or vacuum residues, or mixtures of these residues.
  • the hydrocarbon feedstock treated in the process may contain, among other things, sulfur-containing impurities.
  • the sulfur content may be at least 0.1% by weight, preferably at least 0.5% by weight, preferably at least 1% by weight, more preferably at least 2% by weight. .
  • the hydrocarbon feedstock treated in the process may contain inter alia metal impurities, especially nickel and vanadium.
  • the sum of the nickel and vanadium contents is generally at least 10 ppm, preferably at least 50 ppm, preferably at least 100 ppm.
  • This co-charge may be a hydrocarbon fraction or a lighter hydrocarbon fraction mixture, which may preferably be chosen from the products resulting from a fluid catalytic cracking (FCC) process according to the English terminology. Saxon), a light cut (LCO or "light cycle oil” according to the English terminology), a heavy cut (HCO or "heavy cycle oil” according to the English terminology), a decanted oil, a residue of FCC, a gas oil fraction, especially a fraction obtained by atmospheric distillation or under vacuum, such as vacuum gas oil, or may come from another refining process such as coking or visbreaking.
  • FCC fluid catalytic cracking
  • the co-charge may also advantageously be one or more cuts resulting from the process of liquefying coal or biomass, aromatic extracts, or any other hydrocarbon cuts, or non-petroleum fillers such as pyrolysis oil.
  • the heavy hydrocarbon feedstock according to the invention may represent at least 50%, preferably 70%, more preferably at least 80%, and even more preferably at least 90% by weight of the total hydrocarbon feedstock treated by the process according to the invention.
  • the hydrotreatment process according to the invention may advantageously be carried out at a temperature of between 320 ° C. and 430 ° C., preferably 350 ° C. C at 410 ° C, under a hydrogen partial pressure advantageously between 3 MPa and 30 MPa, preferably between 10 and 20 MPa, at a space velocity (VVH) advantageously between 0.05 and 5 volume of charge per volume of catalyst and per hour, and with a hydrogen gas ratio on a hydrocarbon liquid feed advantageously between 200 and 5000 normal cubic meters per cubic meter, preferably 500 to 1500 normal cubic meters per cubic meter.
  • the value of the VVH of each operating switchable reactor is preferably between 0.5 and 4 volume of catalyst per volume of charge per hour, and most often between 1 and 2 catalyst volume per volume of charge per hour.
  • the overall VVH value of the reactive reactors and that of each reactor is chosen by those skilled in the art so as to achieve the maximum of hydrodemetallation (HDM) while controlling the reaction temperature (limitation of the exothermicity).
  • the catalysts used in the hydrotreatment process according to the invention, and in particular in the permutable guard reactors, are preferably known hydrotreatment catalysts and are generally granular catalysts comprising, on a support, at least one metal or compound of metal 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. .
  • the support used is generally chosen from the group formed by alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of these minerals.
  • the catalysts used in the process according to the present invention are preferably subjected to a sulphurization treatment making it possible, at least in part, to transform the metallic species into sulphide before they come into contact with the charge. treat.
  • This activation treatment by sulfurization is well known to those skilled in the art and can be performed by any method already described in the literature either in-situ, that is to say in the reactor, or ex-situ.
  • the system of permutable guard zones with reversal of the direction of flow and paralleling of the permutable reactors making it possible to perform a prior hydrodemetallation of the charge advantageously precedes a hydrotreatment section of heavy hydrocarbon feeds in fixed bed or bubbling bed. Preferably, it precedes a hydrotreatment section comprising at least one hydrodemetallation unit and at least one hydrodesulfurization unit.
  • the permutable reactors are preferably integrated upstream of the hydrodemetallation unit, the permutable reactors being used as guard beds.
  • the hydrotreating process according to the invention advantageously makes it possible to carry out 50% and more hydrodemetallation of the feedstock at the outlet of the permutable reactors, and more preferably from 50 to 95% of hydrodemetallation), thanks to the speed selected VHV hourly volume and the effectiveness of HDM hydrodemetallization catalyst.
  • the charge 1 arrives in the reactive reactors or reactors by the pipe 1 and leaves the reactor or these reactors by the pipe 13.
  • the charge leaving the reactor (s) of guard arrives via the pipe 13 in the section d hydrotreatment 14 and more precisely in the hydrodemetallation unit HDM comprising one or more reactors.
  • the effluent from the hydrodemetallation unit HDM 15 is withdrawn via line 16 and then sent to the hydrotreating unit HDT 17 comprising one or more reactors.
  • the final effluent is withdrawn through line 18.
  • At least one of the permutable reactors comprises at least two catalytic beds.
  • Short-circuiting of a clogged bed can be effected externally by lateral withdrawal and a short-circuit line, comprising a valve. It is thus possible for steps b) and / or e) to "bypass" the already clogged catalytic beds, and to discharge the effluent from this reactor via a pipe situated between the catalytic beds in the case of two beds.
  • i + 1 denotes the first bed clogged in the direction of flow, the reaction effluent therefore leaves the reactor just before the flow has encountered the clogged zone.
  • all the permutable reactors comprise at least two catalytic beds.
  • steps b) and e) it is possible for both steps b) and e) to remove the effluent from the reactor being clogged by a pipe located between the catalytic beds in the case of two catalytic beds or between a bed i and a bed i + 1 in the case where the reactor comprises n catalytic beds, i being an integer ranging from 1 to n.
  • the guard zone comprises two reactive reactors each comprising two catalytic beds. In this configuration, it is possible for both steps b) and e) to remove the effluent from the reactor being clogged by a lateral withdrawal between the two catalytic beds, just before the catalytic zone already clogged.
  • the figure 3 illustrates a short-circuiting of the catalytic bed already clogged during steps b) and e).
  • step a) of the process charge 1 is introduced via line 3 and line 21 comprises a valve V1 open to line 21 'and the guard reactor R1a containing a fixed bed A of catalyst. During this period the valves V3, V4 and V5, V8, V9, V12, V13 are closed.
  • the effluent from the reactor R1a is sent via the pipe 23, the pipe 26 comprising an open valve V2 and the pipe 22 'into the guard reactor R1b enclosing a fixed bed B of catalyst.
  • the reactor effluent R1 b is sent through lines 24 and 24 'comprising an open valve V6 and via line 13 comprising a valve V10 open to the main hydrotreatment section 14. The flow is in downflow.
  • the effluent from the reactor R1b is sent via the pipes 22 'and 30 having an open valve V9 and the pipe 31 to the main hydrotreatment section 14.
  • the reactor effluent R1 a is sent through the lines 32 and 30 having an open valve V12 and the pipe 31 to the main hydrotreatment section 14.
  • the valve V8 is closed.
  • the already clogged catalytic bed is thus short-circuited.
  • step c) the valves V1, V2, V4, V5, V7, V8, V9, V12, V13 are closed and the valves V3, V6, V10, and V11 are open.
  • the charge is introduced via line 3 and lines 22 and 22 'to reactor R1b.
  • the effluent from the reactor R1b is sent via the pipes 24 and 24 'comprising an open valve V6 and the pipe 13 comprises a valve V10 open to the main hydrotreatment section 14.
  • the sealed reactor R1a is thus bypassed in order to allow the intervention on the reactor R1a for the replacement / reloading of the catalyst.
  • step d) the valves V1, V2, V6, V7, V8, V9, V12, V13 are closed and the valves V3, V4, V5, V10 and V11 are open.
  • the charge is introduced via line 3 and lines 22 and 22 'to reactor R1b, valves V3 and V11 being open.
  • the effluent from the reactor R1b is sent via the pipes 24 and 27 'comprising an open valve V4 and the pipe 21' to the reactor R1a.
  • the reactor effluent R1a is sent via a line 23 having an open valve V5 and a valve V10 open to the main hydrotreatment section 14. The flow is downward in the reactors R1b and R1a placed in series.
  • the effluent from the reactor R1b is sent via the pipes 33 and 30 comprising an open valve V13 and the pipe 31 to the main hydrotreatment section 14.
  • the effluent from the reactor R1a is sent via the pipes 22 '. and having an open valve V8 and line 31 to the main hydrotreatment section 14.
  • step f the valves V2, V3, V4, V6, V7, V8, V9, V12, V13 are closed and the valves V1, V5, V10, and V11 are open.
  • the charge is introduced via line 3 and lines 21 and 21 'to reactor R1a.
  • the effluent from the reactor R1a is sent via the pipes 23 and 23 'comprising an open valve V5 and the pipe 13 comprising a valve V10 open towards the section Main hydrotreatment 14.
  • the reactor R1b clogged is thus short-circuited to allow intervention on the reactor R1 for the replacement / reloading of the catalyst.
  • Example 1 (comparative, not according to the invention, according to FR2681871)
  • the feed consists of a mixture (70/30% wt) of atmospheric residue (RA) of Middle East origin (Arabian Medium) and a vacuum residue (VR) of Middle East origin (Arabian Light).
  • This mixture is characterized by a high viscosity (0.91 cP) at room temperature, a density of 994 kg / m 3 , high contents of Conradson carbon (14% by weight) and asphaltenes (6% by weight) and a high amount of nickel (22 ppm by weight), vanadium (99 ppm by weight) and sulfur (4.3% by weight).
  • the hydrotreatment process is carried out according to the process described in FR2681871 and involves the use of two reactive reactors (R1A and R1B of the figure 1 ). Both reactors are charged with a HDM CoMoNi / alumina hydrodemetallization catalyst.
  • a cycle is defined as integrating the steps of a) to d) (see Table 1). The deactivation and / or clogging time is reached when the pressure drop reaches 0.7 MPa (7bar) and / or the average temperature of a bed reaches 405 ° C and / or when the temperature difference on a catalytic bed becomes radially greater than 5 ° C.
  • the figure 4 shows the evolution of cycles in terms of operating time (in days) for the process according to FR2681871 .
  • a cycle being defined here as the alternative operation of R1a then R1b.
  • DPmax 0.7 MPa or 7 bar
  • the operating time of the reactor R1a is therefore 210 days.
  • the pressure drop in the reactor R1b reached about 3 bars.
  • the time of deactivation and / or clogging (or the duration of operation) of the first zone is therefore 210 days. In total, there is a cycle time of 320 days for the first cycle and 627 days for two cycles.
  • the hydrotreatment process is repeated with the same filler, the same catalyst and under the same operating conditions according to Example 1.
  • the hydrodemetallization rate HDM is maintained at 60%.
  • the schema used for the example is that presented on the figure 2 .
  • the figure 4 shows that according to the prior art, the cycle time is 320 days for the first cycle.
  • the pressure loss increases in the catalytic bed until reaching the maximum permissible pressure loss DPmax for the equipment installed in this example of 0.7 MPa (7 bar) after 210 days for the first reactor and 320 days for the second.
  • the hydrotreatment process incorporating a step of flow direction change and parallelization of the reactors makes it possible to significantly increase the cycle time of the catalytic hydrodemetallation zone, in particular with a gain of 260 days (80%).

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP17181791.9A 2016-07-27 2017-07-18 Hydrotreating-verfahren, bei dem austauschbare schutzreaktoren mit umkehrung der ausflussrichtung und parallelschaltung der reaktoren verwendet werden Active EP3275975B1 (de)

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FR1657215A FR3054559B1 (fr) 2016-07-27 2016-07-27 Procede d'hydrotraitement utilisant des reacteurs de garde permutables avec inversion du sens d'ecoulement et mise en parallele des reacteurs.

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110684555A (zh) * 2018-07-06 2020-01-14 中国石油化工股份有限公司 一种加氢处理的方法和装置
CN114608376A (zh) * 2022-02-18 2022-06-10 国家能源集团宁夏煤业有限责任公司 循环气冷凝器不停车置换清洗的方法、系统及其应用

Citations (4)

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FR2970261A1 (fr) * 2011-01-10 2012-07-13 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de permutation progressive
FR2970260A1 (fr) * 2011-01-10 2012-07-13 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de court-circuitage d'un lit catalytique
FR2992971A1 (fr) * 2012-07-04 2014-01-10 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes en lit fixe catalytique avec inversion du sens d'ecoulement des fluides

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FR2681871A1 (fr) * 1991-09-26 1993-04-02 Inst Francais Du Petrole Procede d'hydrotraitement d'une fraction lourde d'hydrocarbures en vue de la raffiner et de la convertir en fractions plus legeres.
FR2970261A1 (fr) * 2011-01-10 2012-07-13 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de permutation progressive
FR2970260A1 (fr) * 2011-01-10 2012-07-13 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de court-circuitage d'un lit catalytique
FR2992971A1 (fr) * 2012-07-04 2014-01-10 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes en lit fixe catalytique avec inversion du sens d'ecoulement des fluides

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CN110684555A (zh) * 2018-07-06 2020-01-14 中国石油化工股份有限公司 一种加氢处理的方法和装置
CN110684555B (zh) * 2018-07-06 2021-10-08 中国石油化工股份有限公司 一种加氢处理的方法和装置
CN114608376A (zh) * 2022-02-18 2022-06-10 国家能源集团宁夏煤业有限责任公司 循环气冷凝器不停车置换清洗的方法、系统及其应用
CN114608376B (zh) * 2022-02-18 2024-03-19 国家能源集团宁夏煤业有限责任公司 循环气冷凝器不停车置换清洗的方法、系统及其应用

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