EP1170355A1 - Procédé et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres réactionelles successives - Google Patents
Procédé et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres réactionelles successives Download PDFInfo
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- EP1170355A1 EP1170355A1 EP01401737A EP01401737A EP1170355A1 EP 1170355 A1 EP1170355 A1 EP 1170355A1 EP 01401737 A EP01401737 A EP 01401737A EP 01401737 A EP01401737 A EP 01401737A EP 1170355 A1 EP1170355 A1 EP 1170355A1
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- effluents
- fractionation
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- reaction chamber
- reaction
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Images
Classifications
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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
- C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
Definitions
- the present invention relates to the cracking of hydrocarbons into presence of heat transfer particles, catalytic or not, circulating in fluidized phase. More particularly, it relates to a method of cracking in a fluidized bed, in which heat-carrying particles circulate in two successive reaction chambers, in each from which they are brought into contact with one or more sections of hydrocarbons to crack.
- the invention also relates to a device designed for setting implementing the method according to the invention.
- the hydrocarbon charge generally pulverized in the form of fines droplets
- the hydrocarbon charge is brought into contact with heat transfer particles high temperature and circulating in the reactor in the form of a bed fluidized, that is to say in more or less dense suspension within a gaseous fluid ensuring or assisting their transport.
- the cracking reaction is of the type thermal, when the particles have only one function heat transfer. It is catalytic, when the particles heat transfer fluids also have a catalytic function, i.e. have active sites promoting the cracking reaction, such as this is particularly the case in the so-called catalytic cracking process at the fluid state (commonly known as the FCC process, from the English “Fluid Catalytic Cracking ”).
- reaction effluents are separated from the particles.
- the latter deactivated due to the coke which settled on their surface, are generally stripped in order to recover entrained hydrocarbons, then regenerated by combustion coke, and finally brought back into contact with the load to be cracked.
- reactors used are most often vertical reactors of tubular type, in which the charge and the particles move following an essentially ascending flow (the reactor is then called “riser”) or following an essentially downward flow (the reactor is then called “dropper” or “downer”).
- a major difficulty in such processes consists in carrying out both complete and selective cracking of the charge, i.e. manage to crack the entire load, so as to obtain a maximum quantity of recoverable hydrocarbons, while minimizing the amount of unwanted byproducts.
- This objective is all the more difficult to reach as the charges to be cracked present relatively wide boiling ranges, and are made up of very diverse compounds which crack under appreciably conditions different to lead to various products.
- a first solution consists in recycling all or part of these products in the cracking reactor, so that they undergo a second cracking step.
- a measure turns out not to be only ineffective, but also harmful, insofar as a such recycling often has the effect of significantly affecting the quality of cracking of the fresh charge.
- a second solution is to increase the severity of the cracking, in order to further crack the injected charge and convert all types of hydrocarbons present.
- such measure if it increases the charge conversion rate, on the other hand promotes overcracking phenomena, which are reflected by a decrease in the selectivity of the conversion: a increased production of dry gases and coke at the expense of intermediate hydrocarbons sought.
- US Patent No. 2,488,713 proposed a process for catalytic cracking using two successive reactors, in each of which circulates catalytic particles.
- a heavy recycle cut (residue from fractionation of effluents from cracking, of the type known as "slurry") is cracked on contact with catalytic particles from regenerator.
- a fresh charge as well as a intermediate recycle cup of the distillate type is cracked contact of particles from the first reactor.
- the hydrocarbon effluents are separated particles and then are combined and directed to a column of classic fractionation.
- the first drawback of such a process is that the fresh charge is treated in the second reactor in the presence of particles which have have already been largely coked and deactivated in the first reactor, at contact with the heavy recycle charge, particularly rich in refractory polyaromatic compounds. It follows, in the second reactor, poor catalytic activity of these particles resulting in a poor quality of fresh charge cracking, conversion to both low and not very selective.
- a second drawback comes from the fact that the recycle cut heavy is gradually enriched with the most heavy compounds refractories, which, even recycled to the first reactor, do not crack or crack incomplete, and "go around in circles" in unity. This exacerbates the coking problems described above. premature particles in the first reactor.
- a purge planned on the recycling line does not solve the problem satisfactorily. Indeed, the recycle being made up of the fractionation residue of combined effluents from the two reactors, the purge not only extracts that some of the most refractory compounds that we want remove from the unit, but additionally extracts a fraction of compounds directly from the fresh charge, which have not been converted during of their passage in the second reactor, but which could have been cracked in the first reactor on contact with the regenerated particles. The poor selectivity of this purge system thus induces a loss additional yield of desired products.
- EP patent No. 573316 describes a method of catalytic cracking in which the reaction takes place in two successive reactors, the first reactor being downflow (downer), and the second being upward flow (riser).
- the charge to cracking is brought into contact with regenerated particles at the entrance of the downflow reactor, at the bottom of which the mixture charge / particles is transferred to the flow reactor ascending.
- the charge therefore flows in contact with the particles in two successive reactors, which increases the overall yield by cracked hydrocarbons.
- this process is absolutely not selective: the hydrocarbons already converted in the first reactor continue to crack in the second reactor, hence a phenomenon overcracking generating an increased production of dry gases and coke, to the detriment of the intermediate cuts sought.
- the present invention relates to a cracking process in a fluidized bed of a hydrocarbon charge in which particles heat transfer fluids, possibly catalytic, circulate in two successive reaction chambers? in each of which are brought into contact with at least one cut of hydrocarbons, and the reaction effluents from each of said chambers are directed towards the same fractionation unit.
- This process is characterized in that the effluents from each of the reaction chambers are partially fractionated separately in the same partially partitioned fractionation column, and in this at least one cut from the separate fractionation of the effluents of one of the two reaction chambers is, in whole or in part, reinjected into the other room.
- reaction chamber any enclosure provided with means for introducing particles heat transfer fluids (catalytic or not), injection means of one or several cuts of hydrocarbons to crack, of a reaction zone cracking and cracking effluent separation means and particles.
- This term includes in particular any type of reactor thermal or catalytic cracking in a fluidized bed, whatever its operating mode (ascending or descending).
- hydrocarbons are cracked in a first reaction chamber, in full contact with particles active from the regenerator. At the end of this first room, the effluents are separated from the particles, and the latter continue their journey in a second reaction chamber in which their residual activity is used to crack a additional quantity of hydrocarbons.
- the process according to the invention allows a conversion that is both more advanced and more selective of the load to be cracked. It allows the refiner to reinject low-value products obtained during a first conventional cracking step, so as to subject these products to a second cracking step.
- the fact that recycling of these products occurs doing in a different reactor has the advantage, on the one hand, of be able to perform this second cracking under appropriate conditions and, on the other hand, to avoid affecting the quality of the first stage of charge cracking.
- the process according to the invention makes it possible to submit the hydrocarbons constituting the charge in cracking circuits distinct, perfectly suited to the diverse natures of these hydrocarbons, so as to obtain a maximum amount of recoverable products.
- the load to be cracked undergoes a first conversion, as a result of which the undesirable products obtained are fractionated separately from the effluents from the other reactor, in a compartment of the partitioned zone of the fractionation column.
- These products are then reinjected into a separate reactor, in which they undergo a second cracking step, under conditions specifically appropriate to their nature.
- the effluents resulting from this second cracking are then fractionated in the same column as the effluents from the first cracked, and the partitioned fractionation system of this column prevents unwanted residual, unconverted compounds after passing through the two reactors (in particular compounds particularly resistant to cracking), are not recycled second time and "go around in circles" in the unit. Indeed, such compounds are recovered, in the fractionation column, in the partitioned compartment for effluent from the second cracking step. These compounds are thus recovered separately from the effluents from the first cracking stage, and they can for example be eliminated from the unit.
- This system allows reinject into one of the reaction chambers as hydrocarbons coming exclusively from the other chamber. This avoids any phenomenon of enrichment of recycled cuts in compounds refractory, which would gradually degrade the quality of cracking said cuts, while causing excessive coking of particles circulating in the unit.
- the method according to the invention makes it possible to best optimize unwanted products from a first cracking step conventional, in order to produce an additional quantity of products to greater added value.
- it offers the refiner the possibility of carrying out a cracking that is both more complete and more selective in favor of the type of products he wishes to obtain.
- the profitability of the unit is significantly improved.
- the present invention therefore also relates to a device cracking in a fluidized bed of a hydrocarbon feed, putting works two reaction chambers connected together by a means of transfer of heat transfer particles, a fractionation column and supply lines for hydrocarbon effluents from each of the two chambers at said fractionation column.
- a first advantage of the device according to the invention is linked to the fact that the hydrocarbon effluents from the two reaction chambers are partly treated separately, but in one and the same fractionation column. This system avoids having to resort to two separate columns, so having a compact unit and limiting investments.
- a second advantage of this device is linked to the fact that it allows optimal implementation of the method according to the invention.
- said partitioned fractionation zone is advantageously sized depending on the boiling ranges of the undesirable products to which the refiner wants to undergo a second cracking step.
- the area on the other hand is used for the splitting of products for which the refiner does not wish to differentiate those from each of the two reaction chambers, for example because that these are directly recoverable products, that he does not want recraquer.
- reaction chambers involved in the invention are designated in this presentation by "first" and "second” reaction chamber, it being understood that this order is adopted by reference to the direction of circulation of the heat transfer particles from the regenerator.
- injection of hydrocarbons can be done co-current and / or against the flow heat transfer particles.
- reaction chambers can in particular be consisting of all types of downflow reactors (downer), or ascending (riser). Although both rooms can completely identical, the method according to the invention is all the more advantageous when said chambers are different. This allows in particular to prevail in these two rooms conditions different operating procedures, adapted to the type of oil injected into each.
- the residence time of the hydrocarbons injected into the first reaction chamber is less than the residence time of the hydrocarbons injected into the second reaction chamber.
- the cracking in the first reaction chamber is done by presence of particles coming directly from the regenerator, so at particularly high temperature and maximum activity.
- the cracking occurs in milder conditions, since the particles have partially cooled or even deactivated during their passage through the first reaction chamber. From then on, it turned out to be advantageous to prolong the contact between the particles and the hydrocarbons, so as to allow a sufficiently complete cracking of these.
- the residence time of the injected hydrocarbons in the first reaction chamber is between 0.05 and 5 seconds, preferably between 0.1 and 1 seconds.
- the time of stay of the injected hydrocarbons in the second chamber reaction it is advantageously between 0.1 and 10 seconds, preferably between 0.4 and 5 seconds.
- the flow of the charge and of the catalyst in the first reaction chamber is carried out according to an essentially top-down direction.
- Said room reaction can then consist of a substantially reactive vertical downward flow of the type known as "downer", as described for example in the international application for WO 98/12279. Indeed, this type of reactor allows a time of particularly brief contact between the hydrocarbons and the fluidized bed of particles.
- the flow of the charge and the catalyst in the second reaction chamber are done in an essentially ascending direction.
- Said room reaction can then consist of a substantially reactive vertical upward flow, of the type known as "riser”. Indeed this type of reactor allows access to contact times longer between the oil and the fluidized bed of particles.
- the present invention presents numerous modes of implementation. work, from which the refiner will be able to choose the one that is the most adapted to the types of products he wishes to obtain, taking into account the type of fillers he has.
- a first particularly advantageous mode of implementation consists in partitioning the fractionation of the heavy part of the effluents from the two reactors.
- the heaviest effluents from each of the two reaction chambers are fractionated separately, while the lighter effluents are combined.
- said cut from separate fractionation of the effluents from one of the chambers which is, in whole or in part, fed back into the other chamber includes slurry and / or a heavy distillate of the HCO type.
- HCO from the English "heavy cycle oil”
- HCO from the English "heavy cycle oil”
- a heavy cut whose interval boiling point can extend from an initial point generally between 320 and 400 ° C to an end point generally between 450 and 480 ° C. It is a product with little value, rich in sulfur and compounds aromatic, which is generally used as a thinner for fuels heavy.
- slurry As for the product commonly called “slurry”, it is consisting of the fractionation residue from cracked effluents. It is a very heavy, very viscous product, the initial cutting point of which is generally between 450 and 480 ° C. This residue is all the more difficult to value that it is particularly rich in compounds polyaromatic, and that it includes an appreciable proportion of fines, i.e. dust from particle erosion heat transfer fluids circulating in the unit.
- a second particularly advantageous embodiment consists in partitioning the fractionation of the light part of the effluents from the two reactors.
- the lightest effluents from each of the two reaction chambers are fractionated separately while the heaviest effluents are combined.
- said cut from separate fractionation of the effluents from one of the chambers which is, in whole or in part, fed back into the other room includes gasoline.
- said cut from separate fractionation of the effluents from one of the chambers which is, in whole or in part, fed back into the other room includes gasoline.
- by essence of cuts with a boiling range of one point initial generally greater than or equal to 20 ° C up to an end point generally between 140 and 220 ° C. It can be particularly advantageous for the refiner to undergo a second stage of cracking to this type of products, to the extent that it increases the production of light olefins such as for example propenes and butenes, which are highly sought after products, especially for uses in petrochemicals.
- the proportions reinjected depend in particular on the nature (more or less dense, more or less difficult to crack, ...) cuts concerned. These proportions must also take into account the operating conditions prevailing in the reactor in which such cups are reinjected, so as to ensure complete vaporization and the cracking of recycled hydrocarbons.
- the proportion reinjected advantageously comprises from 10 to 100% of the flow of said cut. More preferably, this proportion is between 50 and 100%.
- each of the reinjected sections can be, prior to this reinjection, combined with other cuts hydrocarbons.
- the diluent can for example include fresh charge, in particular conventional loads such as diesel or distillates.
- the diluent can moreover comprise for example light recycling oils ("light cycle oils”, LCO) or heavy oils recycling ("heavy cycle oils", HCO).
- each of the reinjected cups can, prior to this reinjection, be subjected to one or more intermediate treatments.
- an intermediate treatment includes a hydrotreatment, such as for example hydrogenation, hydrodearomatization, hydrodesulfurization, hydrodenitrogenation.
- Such treatments are usually carried out in the presence of catalysts known to those skilled in the art, and which comprise generally, deposited on a refractory mineral oxide support, a or more metals from Group VIII of the Periodic Table of Elements, sometimes associated with other metals such as those of the Group VI of the Periodic Table of the Elements.
- the cracking of hydrocarbons is produced in the presence of heat transfer particles coming from the first room, in which they were partially coked, or even deactivated, in contact with the injected charge in this first room.
- a particularly variant advantageous of the invention consists in introducing upstream of this second reaction chamber, in addition to the particles from the first reaction chamber, an addition of particles in from the regenerator. This variant is particularly beneficial when the heat provided by the particles from said first chamber is insufficient to vaporize the hydrocarbons injected into the second reaction chamber. Adding particles regenerated then provides an amount of heat additional, and to control the temperature prevailing in said second bedroom.
- this system has the additional advantage of introducing in the second chamber, an addition of fully catalytic sites active, so as to optimize the cracking reactions of hydrocarbons injected into this second chamber.
- the addition of particles is introduced between the area where the separation of particles and effluents from the first reaction chamber and the area where the sections are injected of hydrocarbons in the second reaction chamber. Said extra is advantageously introduced so as to ensure mixing homogeneous with the particles from the first reactor.
- a homogenization system for fluidized particle beds as described in EP patent application No. 99.401112 in the name of Applicant can be particularly helpful.
- the invention uses a fractionation column specific. Indeed, this must allow the simultaneous distillation of effluents from the two reactors, and be arranged so that the fractionation of these two types of effluent is partly carried out separately, partly in common.
- This partial segregation of the effluents from the two reactors is carried out using a partitioning arranged inside the column, which partitioning separates part of said column in two compartments which constitute said fractionation zone cloisonne.
- This partially partitioned fractionation column can be arranged in multiple ways, depending on the part of the effluents for which we want the splitting to be done separately.
- the area cloisonne fractionation corresponds to the lower part of the fractionation column.
- different modes of partitioning can be envisaged for the device according to the present invention.
- the fractionation zone partitioned is separated into two compartments by means of substantially vertical separation, extending from the bottom of the fractionation column over part of its height.
- he may for example be a flat vertical wall. It could be also of a vertical cylindrical wall whose axis of revolution is parallel to the longitudinal axis of the fractionating column.
- the area of partitioned partitioning is separated into two compartments thanks to a substantially horizontal separation means, for example constituted a tray extending over a horizontal section of the column, and provided with one or more chimneys allowing passage to the high, towards the common fractionation zone, light effluents from from the lower compartment to said tray.
- a substantially horizontal separation means for example constituted a tray extending over a horizontal section of the column, and provided with one or more chimneys allowing passage to the high, towards the common fractionation zone, light effluents from from the lower compartment to said tray.
- the partitioned fractionation zone corresponds to the upper part of the fractionation column.
- the fractionation zone partitioned is separated into two compartments by means of substantially vertical separation, extending from the head of the fractionation column over part of its height, such that for example a flat vertical wall or a vertical wall cylindrical whose axis of revolution is parallel to the longitudinal axis of the fractionation column.
- the area of partitioned partitioning is separated into two compartments thanks to a substantially horizontal separation means, for example constituted a tray extending over a horizontal section of the column, and provided with one or more chimneys allowing passage downwards, towards the common fractionation zone, heavy effluents from upper compartment to said tray.
- a substantially horizontal separation means for example constituted a tray extending over a horizontal section of the column, and provided with one or more chimneys allowing passage downwards, towards the common fractionation zone, heavy effluents from upper compartment to said tray.
- each of the two reaction chambers may vary. They are preferably different in each of these two rooms, taking into account the different types of hydrocarbons injected into it. On the one in general, these operating conditions include a temperature reaction between 450 and 900 ° C, and a pressure close to the atmospheric pressure. Those skilled in the art can perfectly optimize these conditions depending on the type of oil cuts to be cracked.
- Hydrocarbon charges likely to be cracked in the scope of the present invention can be extremely diverse. They include in particular, but not limited to, the charges usual cracking methods, such as distillates and / or gas oils from atmospheric or vacuum distillation, distillates and / or visbreaking gas oils, deasphalted residues.
- the method according to the invention is moreover perfectly suited to the conversion of heavier loads, containing fractions normally boiling up to 700 ° C and above, which may contain high amounts of asphaltenes and have a carbon content Conradson up to 4% and beyond. So the charge can include heavy distillates, distillation residues atmospheric, or even vacuum distillation residues.
- the injected charges may have received a pretreatment such as, for example, hydrotreating in presence of a suitable catalyst, for example a catalyst based of cobalt and molybdenum deposited on a porous refractory oxide.
- a suitable catalyst for example a catalyst based of cobalt and molybdenum deposited on a porous refractory oxide.
- the load to be cracked can also be diluted by one or more lighter cuts, which may include intermediate cuts from the cracked effluent fractionation zone.
- lighter cuts which may include intermediate cuts from the cracked effluent fractionation zone.
- the LCO or HCO mentioned above can constitute excellent diluents.
- Figure 1 is a schematic view of a first mode of implementation work of the cracking process according to the invention, in which it is partitioned the fractionation of the heavy part of the effluents from the two reactors.
- FIGs 2 and 3 show two possible variants for the partially partitioned fractionation column involved in the process illustrated in Figure 1.
- Figure 4 is a schematic view of a second embodiment work of the cracking process according to the invention, in which it is partitioned the fractionation of the light part of the effluents from the two reactors.
- FIG. 5 represents a possible variant for the column of partially partitioned fractionation involved in the process illustrated in figure 4.
- Figure 1 shows a catalytic cracking unit comprising two successive reaction chambers, the first at downflow and the second upward flow.
- This unit includes a first reaction chamber consisting of a downflow tubular reactor 1, known as name of "downer”.
- This reactor is connected in its upper part to a enclosure 2, from which it is fed by a flow of particles of regenerated catalyst, with a regulated flow by means of a valve 3.
- the load to be cracked is conveyed by line 4 and injected into the reactor 1 by means of injectors 5.
- the catalyst particles and the hydrocarbons then flow from top to bottom in reactor 1.
- the particles are then evacuated through line 10 out of enclosure 6, and transferred to the base of the second chamber reaction.
- the latter consists of a reactor 16 in the form of column, of a type known per se, known as a load elevator, or riser.
- the reactor 16 is supplied at its base by the conduit 10 with particles of catalyst.
- a lifting gas for example steam
- a load comprising a substantial proportion of a cut from the separate fractionation of the heaviest effluents from the first reactor 1
- a load comprising a substantial proportion of a cut from the separate fractionation of the heaviest effluents from the first reactor 1
- injector-sprayers 14 The particles of catalyst and the hydrocarbons then flow from bottom to top in the reactor 16.
- Column 16 opens at its top into an enclosure 15, which it is for example concentric and in which the separation of the cracked charge and stripping of the deactivated particles of catalyst.
- the particles are separated from the charge treated by means a cyclone 17, which is housed in enclosure 15, at the top of which an effluent discharge line 18 from the second reactor is planned 16, which are routed to the fractionation zone.
- the deactivated particles move by gravity to the base of the enclosure 15.
- a line 20 supplies stripping fluid, generally of the water vapor, injectors or diffusers 21 for fluidizing gas regularly arranged at the base of the enclosure 15.
- the particles are then evacuated at the base of the enclosure 15 to a regenerator 23, via the conduit 22.
- the regenerator 23 the coke deposited on the particles is burned using air or another oxygen-rich gas, injected at the base of the regenerator 23 by a line 24, which supplies injectors or diffusers 25 regularly spaced.
- Particles entrained by are separated by cyclones 26, and the combustion gas is evacuated by a line 27, while the particles flow towards the base of the enclosure 23, from where they are recycled through the conduit 28 to enclosure 2 supplying the first reactor 1.
- the reaction effluents from each of reactors 1 and 16 are routed respectively by lines 7 and 18 to the column of fractionation 12.
- the latter consists of two zones: one partitioned lower zone 40, and an upper zone 41 common fractionation.
- Partitioned fractionation zone 40 is divided into two compartments 38 and 39 by a separation means 37, consisting of a flat vertical wall, extending from the bottom of column 12 over part of the height thereof.
- lines 7 and 18 for supplying effluents from the two reactors emerge on either side of the means of partition 37, in the respective compartments 39 and 38, in which the corresponding heavy products are fractionated separately.
- These products correspond to distillation residues or "slurry"
- the initial cutting point is preferably chosen to a value included between 450 and 480 ° C.
- the two compartments 38 and 39 communicate with the common fractionation 41, located in the upper part of the column 12, and in which the product fractionation takes place lighter contained in the combined effluents of the two reactors 1 and 16.
- fractionation zone can perfectly include additional conventional columns not shown, coupled to column 12, in which part of the fractionation of the common effluents described above and / or subsequent splits.
- the condensed residues in compartments 38 and 39 are drawn off respectively by lines 42 and 13.
- the section drawn off by the line 13, which corresponds to the slurry resulting from the separate splitting of effluent from the first reaction chamber 1, is, in accordance with the invention, recycled to the second reaction chamber 16.
- line 47 allows this bottom fraction to be diluted by cutting less viscous, for example all or part of the HCO cup withdrawn by line 46.
- line 48 allows to extract a part of said bottom fraction, so as to inject only one proportion given in reactor 16.
- cup drawn off by line 42 it corresponds to slurry from the separate effluent fractionation of the second reaction chamber 16.
- This section which includes compounds particularly refractory not converted after successive cracking in each of the two reactors, can for example be evacuated from unit.
- Figure 2 in which the organs already described in relation to Figure 1 are designated by the same reference numbers, represents a first alternative embodiment of the fractionation column 12, which brings up another means of partitioning the lower part 40 of said column.
- the column 12 comprises a separation means consisting, as in Figure 1, of a partitioning substantially vertical, extending from the bottom of column 12.
- this partition element here consists of a vertical wall cylindrical 37 'whose axis of revolution is parallel to the longitudinal axis of column 12.
- This cylindrical element is arranged internally and concentrically to the wall of column 12, and it extends from the bottom of it over a sufficient height, thus sharing the area of partitioned partitioning 40 into two compartments 39 and 38, in which lead respectively to line 7 for the routing of effluents from the first reaction chamber 1, and line 18 of effluent from the second reaction chamber 16.
- the two compartments 38 and 39 are therefore concentric.
- Each compartment 38 and 39 communicates directly with the common fractionation zone 41 situated above, in which is carried out, in a conventional manner, the fractionation of the more light contained in the combined effluents of the two reactors.
- the element of partitioning 37 extends over a greater height of the column 12, so as also to cover the distillation zone of the HCO type cuts. Furthermore, we do not separate the HCO from the slurry, if although the residues, drawn off by lines 42 and 13 at the bottom of each of the two respective compartments 38 and 39, are made up of a mixture of these two types of products.
- the residue drawn off by line 13, consisting of a mixture of HCO and slurry from the separate fractionation of heavy effluents from the first reaction chamber 1 is, in accordance with the invention, recycled in whole or in part to the second reaction chamber 16.
- supply lines 7 and 18 can completely be inverted, provided that the two lines 13 and 42 for racking the corresponding products.
- FIG. 3 shows a second variant of the column of fractionation 12 of this figure 1, in which the means 37 "of separation of the lower partitioned partition zone 40 is horizontal type.
- zone 40 includes an internal partitioning consisting of a 37 "horizontal plate, which is dimensioned so as to cover the entire cross section of the column 12 and to be in leaktight contact with the internal vertical wall thereof.
- This partitioning delimits a first upper compartment 39, into which the effluent routing line 7 of the first reaction chamber 1, and a second lower compartment 38, into which the line 18 for discharging effluents from the second reaction chamber 16.
- the two compartments 38 and 39 are therefore arranged one above the other.
- Each compartment, 38, 39 communicates directly with the common fractionation zone 41 situated above.
- the 37 "tray is provided with at least one chimney 50, which allows the passage upwards, towards said common fractionation zone 41, vaporized products from compartment 38 below the 37 "tray.
- the lightest effluents from the second reaction chamber 16 do they go up via this chimney towards the zone commune 41, where they are divided and drawn off by lines 43, 44 and 45, mixed with the light effluents from the first chamber reaction 1.
- the chimney 50 is surmounted by a cap 51, for example conical, which prevents hydrocarbons from passing from the upper compartment 39 to lower compartment 38. This system therefore ensures perfect segregation of heavy effluents from the two reactors 1 and 16.
- the cup drawn off by line 13 of compartment 39 of cloisonne fractionation of heavy effluents from the first reaction chamber 1 is, according to the invention, recycled to all or part to the second reaction chamber 16.
- the supply lines 7 and 18 can be interchanged (splitting separated from the heavy effluents from the first reactor 1 is then carried out in the lower compartment 38, while the separate split heavy effluents from the second reactor 16 is carried out in the upper compartment 39), provided that the two lines 13 and 42 for drawing off the corresponding products.
- Figure 4 also shows a catalytic cracking unit comprising, like that presented in FIG. 1, a first chamber reaction 1 downflow and a second chamber reaction 16 with ascending flow.
- This unit includes many elements in common with the unit shown in Figure 1 and designated by the same reference numbers, so that only the different elements will be described below.
- the process illustrated in this figure 4 corresponds to a mode of embodiment of the invention, in which the the lightest effluents from each of the two reactors 1 and 16, in order to reinject into one of them light products derived from the other.
- the fractionation column 12 includes a zone superior 40 of partitioned separation of light effluents, and a lower zone 41 for the common fractionation of heavy effluents.
- the partitioned partition zone 40 is divided into two compartments 38 and 39 by a separation means 37, consisting of a vertical wall plane extending downward from the head of column 12, on a part of its height.
- the gasoline cup drawn off by line 44 a resulting from the separate fractionation of the lightest effluents from the second reaction chamber, is conveyed to the injectors 5, from which it is reinjected into the first reaction chamber 1.
- the injectors 5 it is entirely possible to recycle this cut to the second reaction chamber 16, it has been found to be more effective in cracking such a cut in the first chamber 1, in contact with the particles maximum temperature coming directly from the regenerator 23. Consequently, the fresh charge can be wholly or partly injected into the second reactor 16. For this purpose, it is conveyed to the injectors 14 via the line 52.
- Figure 5 where the organs already described in relation to Figure 4 are designated by the same reference numbers, represents a alternative embodiment of the fractionation column 12 of this FIG. 4, in which the means 37 "for separating the upper zone 40 of partitioned fractionation is of horizontal type.
- the zone 40 includes an internal partitioning consisting of a 37 "horizontal plate, dimensioned to cover the entire cross section of column 12 and to be in tight contact with the internal vertical wall of that.
- This partitioning delimits a first upper compartment 39, into which the effluent routing line 7 of the first reaction chamber 1, and a second lower compartment 38, into which the line 18 for discharging effluents from the second reaction chamber 16.
- Each compartment 38, 39 communicates directly with the common fractionation zone 41 located below.
- the 37 "tray is provided with at least one chimney 50, which allows the downward passage, towards said common fractionation zone 41, of the heavy products from compartment 39 above the tray 37 ".
- the heaviest effluents from the first chamber reaction 1 do they descend via this route to the common area 41, where they are divided and drawn off by lines 45, 46 and 53, in mixing with heavy effluents from the second chamber reactionary 16.
- the chimney 50 is provided with a baffle 51, for example conical, which prevents hydrocarbons from passing from the lower compartment 38 to upper compartment 39. This system thus ensures perfect segregation of light effluents from the two reactors 1 and 16.
- the gasoline cup drawn off by line 44a of compartment 38 cloisonne fractionation of light effluents from the second reaction chamber 16 is, according to the invention, recycled to all or part of the first reaction chamber 1.
- the first test was carried out in an experimental unit of catalytic cracking in accordance with that shown in Figure 1, which has two successive reaction chambers (1; 16), the first (1) down flow, and the second (16) flow ascending ("riser").
- the catalyst used is a commercial catalyst classical, zeolitic type.
- the effluents of each of these two reaction chambers are directed to a same fractionation column (12), partitioned in its part lower (40) by a flat vertical wall (37).
- the fresh charge is injected into the first reaction chamber (1), while in the second reaction chamber (16), a cut from the separate fractionation of the effluents from the first chamber (1).
- test No. 2 a comparative test was carried out in the same conditions, but replacing the splitting column partially partitioned (12) by a conventional column, in which the effluents from each of the two chambers (1; 16) are combined and split in the traditional way.
- the fresh charge is injected into the first reaction chamber (1), while in the second reaction chamber (16) a section from the fractionation is recycled combined effluents from both chambers.
- the cup recycled in the second chamber reaction (16) corresponds to a heavy distillate or HCO, of interval boiling range from 380 ° C to 480 ° C.
- test 1 in accordance with the invention, all of the HCO from the partitioned fractionation effluent from the first reaction chamber (1) is injected into the second reaction chamber (16).
- the rate of recycle is 0.8.
- the cut of recycled HCO does not contains only hydrocarbons from a first cracking of the fresh charge, while in the second case it also contains hydrocarbons from the second chamber, not converted after passage in the two successive reactors, therefore particularly refractory to cracking, and which "go around in circles" in the unit.
- test 1 carried out in accordance with the invention the elimination of such compounds thanks to the partitioned fractionation system improves notably the quality of the cracking in the second chamber reaction. We can see that this conversion is both more complete (10-point increase in conversion rate), and more selective (sharp decrease in yield in slurry, which is a particularly undesirable product, in favor of an increase in yields sought intermediate products, such as species and LPG).
- This example therefore illustrates the fact that, in the method according to the invention, the qualities of the recycle cut are superior, which contributes to better yields, better selectivity and better quality of the products obtained during the cracking of this cut in the second reaction chamber 16.
- a first test (test No. 5) is carried out in accordance with the invention: the effluents from each of these two reaction chambers are directed towards the same fractionation column (12), partitioned in its upper part (40) by a flat vertical wall (37). Load fresh is injected into the second reaction chamber (16), while that in the first reaction chamber (1) we recycle a section from the separate fractionation of effluents from the second chamber (16).
- test n ° 6 a comparative test (test n ° 6) was carried out in the same conditions, but replacing the splitting column partially partitioned (12) by a conventional column, in which the effluents from each of the two chambers (1; 16) are combined and split in the traditional way.
- the fresh charge is injected into the second reaction chamber (16), while in the first reaction chamber (1) a section from the fractionation is recycled combined effluents from both chambers.
- the cup recycled in the first chamber reaction (1) is a light essence (of boiling range ranging from 20 ° C to 220 ° C).
- test 5 the all gasoline from the partitioned effluent fractionation of the second reaction chamber (16) is injected into the first reaction chamber (1).
- Comparative Trial 6 the recycling rate (report of the quantity of gasoline recycled in the first room reaction to the total amount of gasoline produced in the unit) is 0.8.
- the recycle cut is of significantly higher quality than that obtained in comparative test 6. Indeed, in test 5 this cut is lighter, less rich in sulfur impurities; its content in molecular hydrogen is higher, and its hydrocarbon content aromatic is less. This results in the cracking of such cutting in the first reaction chamber (1), not only higher yields, but also better qualities of cracking products.
- the examples above illustrate perfectly some of the many benefits brought by the present invention.
- they show that the invention allows to optimally recycle certain hydrocarbon cuts from a first step of cracking the fresh charge, which substantially increases the total yield of conversion of this charge, with increased selectivity in favor of specific products sought.
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Abstract
Description
- ladite colonne de fractionnement comporte dans sa partie interne au moins deux zones distinctes : une première zone de fractionnement cloisonné constituée de deux compartiments, communiquant chacun avec une seconde zone de fractionnement commun ;
- les conduites d'amenée des effluents issus de la première et de la deuxième chambre réactionnelle débouchent respectivement dans le premier et le deuxième compartiment de ladite zone de fractionnement cloisonné ;
- une zone de fractionnement cloisonné, dans laquelle les effluents issus des deux réacteurs sont fractionnés séparément, chacun dans un compartiment, de manière à éviter tout contact entre eux, et
- une zone de fractionnement commun, dans laquelle les effluents issus des deux réacteurs sont mélangés.
- les produits gazeux aux conditions normales de température et de pression (hydrocarbures en C1 à C4), soutirés par la ligne 43 ;
- une coupe d'essences, dont l'intervalle d'ébullition peut aller de 20°C jusque vers 140-220°C, soutirée par la ligne 44 ;
- une coupe de type gazole ou LCO, dont l'intervalle d'ébullition s'étend généralement de 140-220°C jusque vers 320-400°C, soutirée par la ligne 45.
- une coupe de type distillat ou HCO, dont l'intervalle d'ébullition s'étend généralement de 320-400°C jusque vers 450-480°C, soutirée par la ligne 46.
- les produits gazeux aux conditions normales de température et de pression (hydrocarbures en C1 à C4), soutirés respectivement des compartiments 38 et 39 par les lignes 43a et 43b ;
- deux coupes de type essences, dont l'intervalle d'ébullition peut aller de 20°C jusque vers 140-220°C, soutirées respectivement des compartiments 38 et 39 par les lignes 44a et 44b.
- une coupe de type gazole ou LCO, dont l'intervalle d'ébullition s'étend généralement de 140-220°C jusque vers 320-400°C, soutirée par la ligne 45 ;
- une coupe de type distillat ou HCO, dont l'intervalle d'ébullition s'étend généralement de 320-400°C jusque vers 450-480°C, soutirée par la ligne 46 ;
- un résidu de distillation ou « slurry », dont le point de coupe initial est généralement choisi à une valeur comprise entre 450 et 480°C, soutiré par la ligne 53.
- Température de sortie de la première chambre réactionnelle (1) : 540°C
- Température de sortie de la deuxième chambre réactionnelle (16) : 515°C
- Rapport C/O dans la première chambre réactionnelle (1) (rapport massique entre la quantité de catalyseur C et celle O de la charge injectée dans cette chambre) : 6
- Rapport C/O dans la deuxième chambre réactionnelle (16) : 8
- Température du régénérateur (23) : 690°C
Essai 1 | Essai 2 (comparatif) | |
Rendements: | ||
Taux de conversion (% en poids) | 34,6 | 24,5 |
Rendement en gaz secs (% en poids) | 2,2 | 1,5 |
Rendement en GPL (% en poids) | 5,8 | 4,3 |
Rendement en essence (% en poids) | 13,1 | 10,1 |
Rendement en LCO (% en poids) | 20,0 | 20,8 |
Rendement en slurry (% en poids) | 45,4 | 54,7 |
Rendement en coke (% en poids) | 13,5 | 8,6 |
- gaz secs: hydrocarbures légers à 1 ou 2 atomes de carbone et hydrogène sulfuré (H2S);
- GPL: hydrocarbures légers à 3 ou 4 atomes de carbone;
- essence: coupe d'hydrocarbures dont l'intervalle d'ébullition s'étend de 20°C jusqu'à 220°C;
- LCO: coupe d'hydrocarbures dont l'intervalle d'ébullition s'étend de 220°C jusqu'à 380°C;
- slurry: résidu de distillation, qui contient des quantités importantes de poussières de catalyseur et dont l'intervalle d'ébullition s'étend à partir de 480°C.
Essai 3 | Essai 4 (comparatif) | |
Propriétés de la coupe de recycle : | ||
Densité (à 15°C) | 0,9522 | 0,9543 |
Viscosité (à 50°C) | 2,76 | 2,98 |
Teneur en soufre (% en poids) | 2,59 | 2,71 |
Teneur en hydrogène moléculaire (% en poids) | 10,10 | 9,79 |
- Température de sortie de la première chambre réactionnelle (1) : 540°C
- Température de sortie de la deuxième chambre réactionnelle (16) : 515°C
- Rapport C/O dans la première chambre réactionnelle (1) : 8
- Rapport C/O dans la deuxième chambre réactionnelle (16) : 6
- Température du régénérateur (23) : 690°C
Essai 5 | Essai 6 (comparatif) | |
Propriétés de la coupe de recycle: | ||
Densité (à 15°C) | 0,7130 | 0,7289 |
Teneur en soufre (% en poids) | 0,063 | 0,078 |
Teneur en hydrogène moléculaire (% en poids) | 14,30 | 13,77 |
Teneur en composés aromatiques (% en poids) | 16,0 | 17,5 |
Claims (28)
- Procédé de craquage en lit fluidisé d'une charge hydrocarbonée dans lequel des particules caloporteuses, éventuellement catalytiques, circulent dans deux chambres réactionnelles successives (1 ; 16), dans chacune desquelles elles sont mises en contact avec au moins une coupe d'hydrocarbures, et les effluents réactionnels issus de chacune desdites chambres sont dirigés vers une même unité de fractionnement, caractérisé en ce que les effluents de chacune des chambres réactionnelles (1 ;16) sont fractionnés en partie séparément dans une même colonne de fractionnement (12) partiellement cloisonnée, et en ce qu'au moins une coupe issue (13, 44a) du fractionnement séparé des effluents d'une des deux chambres réactionnelles (1 ;16) est, en tout ou partie, réinjectée dans l'autre chambre.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le temps de séjour des hydrocarbures injectés dans la première chambre réactionnelle (1) est inférieur au temps de séjour des hydrocarbures injectés dans la deuxième chambre réactionnelle (16).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le temps de séjour des hydrocarbures injectés dans la première chambre réactionnelle (1) est compris entre 0,05 et 5 secondes, de préférence entre 0,1 et 1 seconde.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le temps de séjour des hydrocarbures injectés dans la deuxième chambre réactionnelle (16) est compris entre 0,1 et 10 secondes, de préférence entre 0,4 et 5 secondes.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'écoulement de la charge et des particules dans la première chambre réactionnelle (1) se fait suivant une direction essentiellement descendante.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'écoulement de la charge et des particules dans la deuxième chambre réactionnelle (16) se fait suivant une direction essentiellement ascendante.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que, dans ladite colonne (12) de fractionnement partiellement cloisonnée, les effluents les plus lourds issus de chacune des deux chambres réactionnelles sont fractionnés séparément, tandis que les effluents les plus légers sont combinés.
- Procédé selon la revendication précédente, caractérisé en ce que ladite coupe (13) issue du fractionnement séparé des effluents de l'une des chambres réactionnelles et qui est, en tout ou partie, réinjectée dans l'autre chambre, comprend du slurry et/ou un distillat lourd du type des HCO et/ou une coupe du type gazole telle que du LCO.
- Procédé selon l'une quelconque des revendications 7 et 8, caractérisé en que au moins une coupe (13) issue du fractionnement séparé des effluents les plus lourds de la première chambre réactionnelle (1) est, en tout ou partie, réinjectée dans la seconde chambre réactionnelle (16).
- Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que, dans ladite colonne (12) de fractionnement partiellement cloisonnée, les effluents les plus légers issus de chacune des deux chambres réactionnelles sont fractionnés séparément, tandis que les effluents les plus lourds sont combinés.
- Procédé selon la revendication précédente, caractérisé en ce que ladite coupe (44a) issue du fractionnement séparé des effluents de l'une des chambres réactionnelles et qui est, en tout ou partie, réinjectée dans l'autre chambre, comprend de l'essence.
- Procédé selon l'une quelconque des revendications 10 et 11, caractérisé en ce que au moins une coupe (44a) issue du fractionnement séparé des effluents les plus légers de la deuxième chambre réactionnelle (16) est, en tout ou partie, réinjectée dans la première chambre réactionnelle (1).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que ladite coupe (13 ; 44a) issue du fractionnement séparé des effluents de l'une des chambres réactionnelles et qui est, en tout ou partie, réinjectée dans l'autre chambre est, préalablement à cette réinjection, combinée à d'autres coupes d'hydrocarbures.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que ladite coupe (13 ; 44a) issue du fractionnement séparé des effluents de l'une des chambres réactionnelles et qui est, en tout ou partie, réinjectée dans l'autre chambre est, préalablement à cette réinjection, soumise à un ou plusieurs traitements intermédiaires.
- Procédé selon la revendication 14, caractérisé en ce que ledit traitement intermédiaire inclut un hydrotraitement, tel que par exemple une hydrogénation, une hydrodéaromatisation, une hydrodésulfuration, une hydrodéazotation.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on introduit en amont de la seconde chambre réactionnelle (16), en plus des particules issues de la première chambre réactionnelle (1), un appoint de particules en provenance du régénérateur (23).
- Dispositif de craquage en lit fluidisé d'une charge hydrocarbonée, mettant en oeuvre deux chambres réactionnelles (1 ; 16) reliées entre elles par un moyen (10) de transfert des particules caloporteuses, une colonne de fractionnement (12) et des conduites (7; 18) d'amenée des effluents hydrocarbonés issus de chacune des deux chambres (1; 16) à ladite colonne de fractionnement (12), caractérisé en ce que :ladite colonne de fractionnement (12) comporte, dans sa partie interne, au moins deux zones distinctes : une première zone (40) de fractionnement cloisonné constituée de deux compartiments (38 ; 39), communiquant chacun avec une seconde zone de fractionnement commun (41) ;
les conduites (7 ; 18) d'amenée des effluents issus de la première et de la deuxième chambre réactionnelle (1 ;16) débouchent respectivement dans le premier et le deuxième compartiment (39 ; 38) de ladite zone (40) de fractionnement cloisonné ;des moyens sont prévus (13 ; 44a) pour le recyclage et l'injection dans l'une des chambres réactionnelles (1 ; 16) d'au moins une coupe soutirée du compartiment de fractionnement cloisonné des effluents de l'autre chambre réactionnelle. - Dispositif selon la revendication précédente, caractérisé en ce que lesdites chambres réactionnelles (1 ; 16) sont différentes.
- Dispositif selon l'une quelconque des revendications 17 et 18, caractérisé en ce que la première chambre réactionnelle (1) est constituée d'un réacteur sensiblement vertical à écoulement descendant du type connu sous le nom de downer.
- Dispositif selon l'une quelconque des revendications 17 à 19, caractérisé en que la seconde chambre réactionnelle (16) est constituée d'un réacteur sensiblement vertical à écoulement ascendant, du type connu sous le nom de riser.
- Dispositif selon l'une quelconque des revendications 17 à 20, caractérisé en que la zone de fractionnement cloisonné (40) correspond à la partie inférieure de la colonne de fractionnement (12).
- Dispositif selon la revendication 21, caractérisé en ce que la zone de fractionnement cloisonné (40) est séparée en deux compartiments (38 ; 39) grâce à un moyen de séparation sensiblement vertical (37 ; 37'), s'étendant à partir du fond de la colonne de fractionnement (12) sur une partie de la hauteur de celle-ci.
- Dispositif selon la revendication 21, caractérisé en que la zone de fractionnement cloisonné (40) est séparée en deux compartiments (38 ; 39) grâce à un moyen de séparation sensiblement horizontal, constitué d'un plateau (37") s'étendant sur une section horizontale de la colonne (12), et pourvu d'une ou plusieurs cheminées (50) permettant le passage vers le haut, vers la zone (41) de fractionnement commun, des effluents légers issus du compartiment (38) inférieur audit plateau (37").
- Dispositif selon l'une quelconque des revendications 17 à 20, caractérisé en que la zone de fractionnement cloisonné (40) correspond à la partie supérieure de la colonne de fractionnement (12).
- Dispositif selon la revendication 24, caractérisé en ce que la zone de fractionnement cloisonné (40) est séparée en deux compartiments (38 ; 39) grâce à un moyen de séparation sensiblement vertical (37 ; 37'), s'étendant à partir de la tête de la colonne de fractionnement (12) sur une partie de la hauteur de celle-ci.
- Dispositif selon la revendication 24, caractérisé en que la zone de fractionnement cloisonné (40) est séparée en deux compartiments (38 ; 39) grâce à un moyen de séparation sensiblement horizontal, constitué d'un plateau (37") s'étendant sur une section horizontale de la colonne (12), et pourvu d'une ou plusieurs cheminées (50) permettant le passage vers le bas, vers la zone de fractionnement commun (41), des effluents lourds issus du compartiment (39) supérieur audit plateau (37").
- Dispositif selon l'une quelconque des revendications 22 ou 25, caractérisé en que ledit moyen de séparation est constitué d'une paroi verticale plane (37).
- Dispositif selon l'une quelconque des revendications 22 ou 25, caractérisé en que ledit moyen de séparation est constitué d'une paroi verticale cylindrique (37'), dont l'axe de révolution est parallèle à l'axe longitudinal de la colonne de fractionnement (12).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0008732A FR2811327B1 (fr) | 2000-07-05 | 2000-07-05 | Procede et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres reactionnelles successives |
FR0008732 | 2000-07-05 |
Publications (2)
Publication Number | Publication Date |
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EP1170355A1 true EP1170355A1 (fr) | 2002-01-09 |
EP1170355B1 EP1170355B1 (fr) | 2004-12-29 |
Family
ID=8852125
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Application Number | Title | Priority Date | Filing Date |
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EP01401737A Expired - Lifetime EP1170355B1 (fr) | 2000-07-05 | 2001-06-29 | Procédé et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres réactionelles successives |
Country Status (7)
Country | Link |
---|---|
US (2) | US6767451B2 (fr) |
EP (1) | EP1170355B1 (fr) |
AT (1) | ATE286107T1 (fr) |
CA (1) | CA2352018C (fr) |
DE (1) | DE60108007T2 (fr) |
ES (1) | ES2236159T3 (fr) |
FR (1) | FR2811327B1 (fr) |
Cited By (3)
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WO2008127956A1 (fr) * | 2007-04-13 | 2008-10-23 | Shell Oil Company | Systèmes et procédés de fabrication d'un produit distillé intermédiaire et d'oléfines inférieures à partir d'une charge d'hydrocarbure |
WO2008134612A1 (fr) * | 2007-04-30 | 2008-11-06 | Shell Oil Company | Systemes et procedes de fabrication de produit de distillat moyen et d'olefines inferieures a partir d'une charge d'hydrocarbures |
CN111013500A (zh) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | 一种浆态床连续加氢反应装置 |
Families Citing this family (18)
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FR2785907B1 (fr) * | 1998-11-13 | 2001-01-05 | Inst Francais Du Petrole | Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant |
WO2006020547A1 (fr) * | 2004-08-10 | 2006-02-23 | Shell Internationale Research Maatschappij B.V. | Méthode et appareillage permettant d’obtenir un distillat moyen et des oléfines légères à partir d’une charge d’hydrocarbures |
US20060231459A1 (en) * | 2005-03-28 | 2006-10-19 | Swan George A Iii | FCC process combining molecular separation with staged conversion |
FR2895413B1 (fr) | 2005-12-27 | 2011-07-29 | Alstom Technology Ltd | Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone |
US20080011645A1 (en) | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations |
US20080011644A1 (en) * | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of heavy oils in conjuction with FCC unit operations |
AU2007285741A1 (en) * | 2006-08-18 | 2008-02-21 | Shell Internationale Research Maatschappij B.V. | Process to separate particles from a particles-containing gas stream |
RU2474606C2 (ru) * | 2007-10-10 | 2013-02-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Системы и способы получения средних дистиллятов и низших олефинов из углеводородного сырья |
WO2010061986A1 (fr) * | 2008-11-26 | 2010-06-03 | Sk Energy Co., Ltd. | Procédé de préparation d'un combustible propre et d’aromatiques à partir de mélanges hydrocarbonés de craquage catalytique en lit fluide |
CN101921611B (zh) * | 2009-06-12 | 2013-07-31 | 中国石油天然气股份有限公司 | 一种降低汽油硫含量的催化裂化方法及系统 |
WO2011068666A1 (fr) * | 2009-12-01 | 2011-06-09 | Exxonmobil Research And Engineering Company | Hydrotraitement à deux étages avec appareil de fractionnement sur colonne à paroi divisée |
WO2012004809A1 (fr) * | 2010-07-08 | 2012-01-12 | Indian Oil Corporation Ltd. | Procédé et appareil de craquage catalytique fluide à deux étages |
RU2531589C1 (ru) * | 2010-12-14 | 2014-10-20 | Юоп Ллк | Способ и установка для извлечения тяжелых полициклических ароматических соединений из потока гидрообработки |
US9458394B2 (en) | 2011-07-27 | 2016-10-04 | Saudi Arabian Oil Company | Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor |
US8822747B2 (en) * | 2011-12-21 | 2014-09-02 | Uop Llc | Combined xylene isomerization and transalkylation process unit |
US8888899B2 (en) * | 2012-04-12 | 2014-11-18 | Kellogg Brown & Root Llc | Transfer line for the primary cyclone of a gasifier |
FR3015514B1 (fr) | 2013-12-23 | 2016-10-28 | Total Marketing Services | Procede ameliore de desaromatisation de coupes petrolieres |
CN114426877B (zh) * | 2020-10-29 | 2023-07-14 | 中国石油化工股份有限公司 | 一种原油催化裂解生产低碳烯烃和btx的方法 |
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US2488713A (en) * | 1947-05-01 | 1949-11-22 | Universal Oil Prod Co | Catalytic cracking of residual hydrocarbons |
EP0573316A1 (fr) * | 1992-05-07 | 1993-12-08 | Institut Francais Du Petrole | Procédé et dispositif de craquage catalytique dans deux zones réactionnelles successives |
WO1998012279A1 (fr) * | 1996-09-18 | 1998-03-26 | Total Raffinage Distribution S.A. | Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures |
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US5582711A (en) * | 1994-08-17 | 1996-12-10 | Exxon Research And Engineering Company | Integrated staged catalytic cracking and hydroprocessing process |
US5755933A (en) * | 1995-07-24 | 1998-05-26 | The M. W. Kellogg Company | Partitioned distillation column |
FR2757872B1 (fr) * | 1996-12-31 | 1999-06-25 | Total Raffinage Distribution | Procede d'hydrotraitement d'une charge hydrocarbonee et dispositif pour sa mise en oeuvre |
FR2785907B1 (fr) * | 1998-11-13 | 2001-01-05 | Inst Francais Du Petrole | Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant |
US6630066B2 (en) * | 1999-01-08 | 2003-10-07 | Chevron U.S.A. Inc. | Hydrocracking and hydrotreating separate refinery streams |
-
2000
- 2000-07-05 FR FR0008732A patent/FR2811327B1/fr not_active Expired - Fee Related
-
2001
- 2001-06-29 DE DE60108007T patent/DE60108007T2/de not_active Expired - Lifetime
- 2001-06-29 ES ES01401737T patent/ES2236159T3/es not_active Expired - Lifetime
- 2001-06-29 EP EP01401737A patent/EP1170355B1/fr not_active Expired - Lifetime
- 2001-06-29 AT AT01401737T patent/ATE286107T1/de not_active IP Right Cessation
- 2001-07-03 CA CA002352018A patent/CA2352018C/fr not_active Expired - Fee Related
- 2001-07-03 US US09/897,436 patent/US6767451B2/en not_active Expired - Fee Related
-
2004
- 2004-05-18 US US10/847,374 patent/US7544333B2/en not_active Expired - Fee Related
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US2488713A (en) * | 1947-05-01 | 1949-11-22 | Universal Oil Prod Co | Catalytic cracking of residual hydrocarbons |
EP0573316A1 (fr) * | 1992-05-07 | 1993-12-08 | Institut Francais Du Petrole | Procédé et dispositif de craquage catalytique dans deux zones réactionnelles successives |
WO1998012279A1 (fr) * | 1996-09-18 | 1998-03-26 | Total Raffinage Distribution S.A. | Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008127956A1 (fr) * | 2007-04-13 | 2008-10-23 | Shell Oil Company | Systèmes et procédés de fabrication d'un produit distillé intermédiaire et d'oléfines inférieures à partir d'une charge d'hydrocarbure |
WO2008134612A1 (fr) * | 2007-04-30 | 2008-11-06 | Shell Oil Company | Systemes et procedes de fabrication de produit de distillat moyen et d'olefines inferieures a partir d'une charge d'hydrocarbures |
CN111013500A (zh) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | 一种浆态床连续加氢反应装置 |
CN111013500B (zh) * | 2019-10-25 | 2022-02-25 | 河北美邦工程科技股份有限公司 | 一种浆态床连续加氢反应装置 |
Also Published As
Publication number | Publication date |
---|---|
CA2352018C (fr) | 2010-02-02 |
US20040211704A1 (en) | 2004-10-28 |
FR2811327A1 (fr) | 2002-01-11 |
US20020096452A1 (en) | 2002-07-25 |
DE60108007D1 (de) | 2005-02-03 |
DE60108007T2 (de) | 2005-12-08 |
EP1170355B1 (fr) | 2004-12-29 |
US7544333B2 (en) | 2009-06-09 |
FR2811327B1 (fr) | 2002-10-25 |
ATE286107T1 (de) | 2005-01-15 |
CA2352018A1 (fr) | 2002-01-05 |
ES2236159T3 (es) | 2005-07-16 |
US6767451B2 (en) | 2004-07-27 |
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