EP0171330A1 - Verfahren und Vorrichtung für die katalystische Wirbelschichtspaltung - Google Patents

Verfahren und Vorrichtung für die katalystische Wirbelschichtspaltung Download PDF

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EP0171330A1
EP0171330A1 EP85401559A EP85401559A EP0171330A1 EP 0171330 A1 EP0171330 A1 EP 0171330A1 EP 85401559 A EP85401559 A EP 85401559A EP 85401559 A EP85401559 A EP 85401559A EP 0171330 A1 EP0171330 A1 EP 0171330A1
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Prior art keywords
catalyst
zone
reactor
regeneration
catalytic particles
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French (fr)
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EP0171330B1 (de
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Pierre Galtier
Christian Busson
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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
    • 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 invention relates to a new process (a) for catalytic cracking allowing more especially the treatment of heavy hydrocarbon oils and (b) for regeneration of the catalyst, as well as to the apparatus allowing the implementation of this process.
  • one of the most important consists in ensuring, at the level of the contact of the hydrocarbon feedstock - which is generally preheated and added with steam - and the regenerated hot catalyst used in the catalytic cracking unit, mixing such that the transfer of heat between charge and catalyst is carried out as quickly as possible and as regularly as possible; it is also essential that the renewal of the regenerated catalyst at the level of the introduction of the charge into the reaction zone is carried out permanently and efficiently, in particular avoiding the back-mixing phenomena which increase the contact times and cause a significant reduction in the formation of light cuts by increasing the weight percentage of the coke formed on the catalyst grains.
  • the present invention aims to simultaneously obtain the best conditions for accessing the three factors mentioned above: absence of back-mixing, radial homogeneity and piston-type flow.
  • This objective could be achieved by simultaneously using a new type of charge injection and mixing with the catalyst, and a reaction zone traversed by a co-current of charge and catalyst in the downward direction, as well as a separator. fast.
  • US Patent 4,385,985 describes an improved downstream catalytic cracking process for treating heavy loads, with a final boiling point greater than 560 ° C and having a Conradson carbon content of 3% or more; however, the system described in the mixture of regenerated catalyst and charge, which consists in introducing the catalyst by a perforated grid, and in introducing the charge by a conventional system of plurality of injectors located below the point of introduction of the regenerated catalyst is not capable of ensuring ultra-rapid vaporization of the charge or of a homogeneous mixture over the entire section of the reactor.
  • US Pat. No. 4,411,773 which describes an identical apparatus, at least as regards the essential parts, and in particular, the mixing-injection system.
  • US Patents 3,152 .065 and 3.246.960 teach a method of injecting hydrocarbon feedstock into the lower part of a "reactor" so as to introduce a feedstock mixture and water vapor, the charge being subjected to a helical movement before being mixed with water vapor, then passing the assembly through an orifice of restricted surface, the arrival of regenerated catalyst taking place below the injection system, at the base of the "reactor".
  • none of the devices mentioned makes it possible to carry out a suitable injection of heavy hydrocarbon feedstock into a catalytic cracking reaction zone by ensuring both rapid mixing - preferably less than 500 milliseconds - of the catalyst and the vaporized feedstock, and good radial homogeneity of the mixture over the entire surface of the reactor; moreover, these devices are provided for the introduction of charges in the case of FCH reactors, of the ascending co-current type, are not adapted to the case of the descending co-currents of catalyst and of charge.
  • the invention therefore relates to a new FCC process (Fluid catalytic cracking or catalytic cracking in a fluidized bed), more especially usable for the transformation of heavy hydrocarbon feedstocks;
  • these fillers can either be conventional fillers, that is to say having for example final boiling points of the order of 400 ° C., such as gas oils under vacuum, but also heavier hydrocarbon oils, such as crude and / or stripped oils, and residues from atmospheric distillation or vacuum distillation; these fillers may if necessary have received a preliminary treatment such as, for example, a hydrotreatment in the presence for example of catalysts of the cobalt-molybdenum or nickel-molybdenum type.
  • the preferred fillers of the invention will be those containing fractions normally boiling up to 700 ° C and above, which may contain high percentages of asphaltenes, and have a Conradson carbon content of up to 4% and above.
  • These charges may or may not be diluted by conventional lighter cuts, which may include cuts of hydrocarbons which have already undergone the cracking operation, which are recycled, such as for example light recycling oils ("light cycle oils", LCO) or heavy recycling oils ("heavy cycle oils", HCO).
  • these charges are preheated in a temperature range between 300 and 450 ° C before their treatment.
  • the invention consists in introducing the charge into the upper part of a substantially vertical reaction zone, by means of a charge injection and dispersion system, generally added with water vapor, allowing its spraying into droplets.
  • a charge injection and dispersion system generally added with water vapor, allowing its spraying into droplets.
  • the speed of the charge at its injection level is preferably between 10 and 100 m / s.
  • This device comprises a plurality of injection nozzles, each of these nozzles is located in the upper part of a discharge tube of the regenerated hot catalyst, coaxially with this tube so that it occurs, in the upper part of the discharge tube, a substantially parallel flow of the partially vaporized charge jets on the one hand and the flow of grains of hot catalyst on the other hand, in order to promote in this part the heat exchanges by radiation between these two flows; the complete vaporization of the charge being carried out in the lower part of said catalyst discharge tubes.
  • the contact time between charge and catalyst generally does not exceed 500 milliseconds and is generally of the order of 100 milliseconds.
  • the co-current of feedstock (thus vaporized) and of catalyst then travels in the descending direction of the reaction zone, where the temperature is generally between 450 and 700 ° C., the residence time being between 0.1 and 10 seconds, and preferably from 0.2 to 4 seconds.
  • the co-current of catalyst and reaction effluent having undergone the cracking treatment is accelerated, then passes through an original rapid separation system (see the explanation of FIG. 3 below) which performs a separation of the vapors and the catalyst particles in less than 1 second; 50 to 90% of the catalyst grains are thus separated from the gaseous reaction effluent, the rest of the separation being carried out using one or more conventional cyclone systems.
  • the invention therefore allows rapid and thorough separation between catalyst and gaseous effluent (permitted by the use of cyclone (s) known as reverse (with reversal of the spiral obtained by the movement of the effluent)) but also a very rapid separation between catalyst and effluent since 50 to 90% of the catalyst grains are separated from the gaseous effluent by the prior use, before the thorough separation, of at least one cyclone with direct passage and with very long residence time short, with helical flow of the vapor flow obtained without spiral reversal.
  • cyclone s
  • reverse with reversal of the spiral obtained by the movement of the effluent
  • the effluent gases are separated, and the catalyst then passes into a stripping zone where it is treated with gases such as water vapor and / or inert gases such as C0, C0 2 , combustion gases or fuel gases -oil; the hydrocarbons and the stripping gases are removed, and the catalyst thus stripped is then transported in fluidized form in a first regeneration zone, substantially vertical ,. where the temperature is maintained between around 500 and 750 ° C.
  • a first regeneration zone an amount of oxygen or of a gas containing molecular oxygen is preferably introduced in the form of air, such that the combustion of the hydrogen of the products deposited on the catalyst is practically complete, or, at least, equal to 90% by weight.
  • This second regeneration zone is constituted by a substantially vertical reactor, having a length L much greater than its diameter 0, such that the ratio L ⁇ is between 3 and 90, lined internally with refractory materials.
  • the partially regenerated catalyst is introduced at the base of this second regeneration zone.
  • the temperature at which this second regeneration takes place is higher than that of the first; it is usually higher than 650 ° C and can reach 1000 ° C.
  • This second catalyst regeneration step is carried out in the presence of a large excess of oxygen (preferably dry air), and the gases formed are particularly rich in CO 2 . Catalyst free of most of the carbon which had deposited on its surface is thus obtained, since the percentage by weight of coke relative to the catalyst is generally less than 0.04%.
  • the catalyst thus regenerated is separated from the gas stream by cyclones external to the second regeneration zone; it is then at a temperature generally between 600 ° C (or even 700 ° C) and 950 ° C, and is brought back to the contactor-mixer by lowering legs provided with flow control valves.
  • the improvement of the radial distribution of the catalyst, the absence of back-mixing, the flow of fluids approaching a piston regime, the rapid separation of the catalyst and the products, increase the selectivity, reduce the formation of coke and of gas and allow the volume of the reaction zone to be reduced, which reduces investment costs as well as the inventory of the catalyst.
  • FIG. 1 shows a schematic illustration of the invention describing a possible embodiment of the unit of F.C.C.
  • FIG. 2 is a more detailed description of a preferred embodiment of the charge injection and dispersion device
  • FIG. 3 is a detailed description of the rapid disengagement device and the stripping reactor at the outlet of the cyclones for separation of gas-catalytic particle mixtures withdrawn from the FFC reactor
  • a hydrocarbon charge for example a higher boiling point diesel or hydrocarbon is introduced through the pipe (2) at the top of the downward vertical reactor (1).
  • a catalyst regenerated at high temperature is also introduced at the top of the reactor (1) by the lowering legs (3) and (4) of the external cyclones (5) and (6), equipped with valves (7) and (8) for control the flow rate.
  • the hydrocarbon charge is atomized and partially vaporized in a multi-nozzle injection system (9), one possible embodiment of which is described in more detail in FIG. 2 below.
  • the charge is then rapidly dispersed and mixed with the hot catalyst in a plurality of discharge tubes (10), of the contactor-mixer (11), down, multi-nozzle, rapid, one possible embodiment of which is described in more detail. detailed below in FIG. 2.
  • the contactor-mixer (11) performing ultra-rapid heat transfers between the catalyst regenerated at high temperature and the charge, the latter is completely vaporized, and the heavy fractions it contains are thermally disintegrated under the effect of the initial thermal shock thus produced.
  • the charge / catalyst contact time generally does not exceed 500 milliseconds, and preferably remains less than 100 milliseconds.
  • the temperature reached by the hydrocarbon vapor / catalyst suspension can vary in the temperature range from 450 ° C to 700 ° C depending on the degree of conversion desired and the composition of the feed.
  • the hydrocarbon vapor / catalyst suspension then flows in a vertical direction descending through the reactor (1), the cross section of which can vary gradually to ensure the operating conditions of temperature and residence time required.
  • the suspension at high temperature, consisting of the vapors of hydrocarbons formed, the dilution gases and the entrained catalyst crosses the reactor under speed conditions ensuring a flow close to the piston flow.
  • the downward flow in particular has the advantage of reducing nota the relative sliding of the catalyst relative to the carrier gas.
  • the residence time of the hydrocarbon feedstock in the reaction zone (1) is from approximately 0.1 seconds to approximately 10 seconds, and preferably from approximately 0.2 seconds to 4 seconds.
  • the reactor (1) can be internally lined with baffles or lining (not shown), such as Ras rings, Berl saddles, Intalox saddles, etc. .
  • the hydrocarbon vapor / catalyst suspension is then accelerated in one (or more) conical or pyramidal convergent or equivalent shape (12) with 1/2 angle at the apex between 5 and 30 ° and preferably between 7 and 15 °, to enter a separator (or several in parallel) (13) with a short residence time, less than 1 second.
  • a possible and preferred embodiment of this rapid separation can be obtained in one (or more in parallel) cyclone without reversal of a spiral, called of the "uniflow" type with direct passage.
  • Figure 3 details one of these possible embodiments where a cyclone of the "uniflow" type is arranged horizontally. This first stage achieves in a very short time ( ⁇ 1 second) a relatively coarse first separation (but with efficiencies greater than 50 /).
  • the effluent passes through this "uniflow" cyclone without reversing the spiral created, and leads into one or more stages in parallel, and / or in series, of secondary separation (14), by cyclones known as reverse cyclones ("reverse flow cyclone"") conventional, known to those skilled in the art, which allow a very thorough separation of the catalyst, still entrained with the effluent at the outlet of the first rapid separation stage (13).
  • the reaction effluent is discharged through the line (16 bis).
  • the catalyst is removed by the lowering legs of the primary (15) and secondary (16) separation train, inside a reactor (17) where the stripping, generally by steam, of the hydrocarbons entrained with these powdery solids. This configuration allows a completely external arrangement of the reactor (1), which facilitates servicing and maintenance operations in the reaction section.
  • the lower section of the reactor (12) generally has a smaller diameter than that of the upper section, and contains a stripping zone (18), at the base of which a suitable stripping gas, such as water vapor, inert gases (C0, CO 2 , ...), combustion gases or fuel gases are introduced.
  • a conventional primary and secondary separation system (19) is used in the upper section of the reactor (17) to separate the stripped hydrocarbon products and the stripping gas from the catalyst particles. The stripping gases and the stripped hydrocarbons leave the separator (19) via the outlet pipes not shown.
  • the stripping effluents can be treated, with the effluents coming directly from the reactor, in the single train separation (14), sequential or parallel, possibly eliminating in this variant, the direct connection (24) between the primary separation (13) and this separation train (14).
  • This stripping operation is a conventional operation, well known to those skilled in the art, and it is not necessary to describe it in more detail.
  • the stripped catalyst is covered with a deposit of coke. It is withdrawn from the bottom of the stripping reactor (17), at a temperature of at least 450 ° C, by a flow leg (20) equipped with a valve (21) which serves to control the flow of solids .
  • This lowering leg (20) filled with solids in a dense manner, has a sufficient height for the solid plug thus produced to form a joint and ensure pressure balancing between the reaction section and the regeneration steps which follow.
  • the stripped catalyst, still covered with coke deposits, is transferred from the flow leg (20) to the bottom of the first regeneration stage (22), by the introduction of a transport gas, to the base of a substantially vertical elevator (23).
  • a transport gas can be preheated air, superheated steam, additions of hot oxygen, at temperatures of 150 to 300 ° C., under about 2 to 3 bars.
  • the quantity of transport gas introduced into this elevator is sufficient to form with the catalyst a solid / gas suspension, the density of which is such that it is forced to flow in an upward vertical movement in the conduit (23), up to 'to be poured into the lower part of the first regeneration stage (22).
  • the first catalyst regeneration stage consists of a dense fluidized bed (25), according to a technology known to those skilled in the art, which it is not necessary to detail here.
  • An oxygen-rich gas necessary for the regeneration of the catalyst is introduced into the lower part of the fluidized bed (25) by the conduit (23) and / or by a conduit (26) connected to a gas distributor (wall 27 a of the type perforated grid or tubes) (perforations 27).
  • a primary and secondary cyclonic separation system (28) is arranged in the flared upper part (31) of the reactor (22) in order to separate the catalyst drives from the CO-rich combustion gases.
  • the regeneration gases rich in CO are extracted from the reactor (22) by a conduit (29) equipped with a valve (30) for controlling the pressure.
  • the first regeneration step carried out in the reactor (22) is carried out under relatively mild temperature conditions below 750 ° C, and is carried out with reduced oxygen concentrations selected to achieve combustion of at least 50% l hydrogen (and preferably substantially all of it) contained in the coke deposit deposited on the catalyst and burn part of the carbon (10 to 60% by weight of carbon present).
  • the operating conditions and the oxygen concentration used are sufficient to maintain the temperature of the dense fluidized bed (25) in the range of about 500 to about 750 ° C.
  • These relatively regenerative conditions soft are sought so as to prevent the presence of water vapor during the combustion of hydrogen from substantially reducing the activity of the catalyst.
  • the first regeneration stage at a temperature considered to be relatively low generates combustion gases which are particularly rich in C0.
  • the CO post combustion phenomena are particularly avoided in the dense fluidized bed (25), in the disengagement zone, and in the cyclonic separation system (28).
  • a CO boiler (not shown) is arranged downstream of the exhaust duct (29) to generate pressurized steam by transforming CO into C0 2 .
  • An energy recovery unit can also be arranged before this C0 combustion step, according to conventional techniques known to those skilled in the art.
  • the first regeneration step is carried out at a temperature, a pressure, a reduced concentration of O 2 , so as to leave a certain proportion of coke, with low hydrogen content, on the catalyst, which will be finished. then burn in a second high temperature regeneration stage (32). It is recommended to reduce the combustion of carbon in the first regeneration stage at a relatively low temperature, below 750 ° C, to the amount just necessary to support the combustion of a significant part of the hydrogen.
  • the partially regenerated catalyst, but the residual coke of which contains practically no more hydrogen or little hydrogen is extracted from the dense fluidized bed (25) by a withdrawal duct (33), communicating with an external, curved lowering leg ( 34), fitted with a solids flow control valve (35).
  • This transport gas is a non-combustible gas, containing oxygen, usually air; it should preferably be completely free of water vapor.
  • the catalyst in the form of a bed entrained by the oxygen-containing transport gas, enters a separate reactor (37), preferably lined with refractories for a second independent stage of regeneration at high temperature, carried out at a temperature above 650 ° C, which is accomplished substantially in the absence of water vapor.
  • the quantity of oxygen is sufficient to maintain a regeneration operation at high temperature by combustion of the coke, combined with the almost complete combustion of the CO to C0 2 .
  • the high temperature regeneration by combustion of all the residual carbon is not limited in temperature, and can reach 1000 ° C.
  • the temperature of the second regeneration stage is left free to settle at the level necessary to remove practically all of the residual coke deposited on the catalyst particles, so as to reach weight contents of coke in the catalyst less than 0.04%. .
  • This second independent high-temperature regeneration stage is constituted by an ascending vertical tubular reactor (37).
  • the spent catalyst is transported through this fast generator as a suspension in a regeneration gas, such as air, at a surface speed of about 0.5 to 10 m / s, and preferably from 1 to 5 m / s.
  • the height / diameter ratio of this regenerator must be in the range from 3 to 90 and preferably 10 to 25.
  • This rapid regenerator is equipped with injection nozzles for injecting regeneration gas at its base (not shown) and over its entire height for possible secondary injections (not shown) of the regeneration gases, usually dry air.
  • the present invention allows an appreciable gain in terms of the total volume and the size of the regenerator, by eliminating the volumes ordinarily used for the wind box, the distributors, the disengagement zones, the descent legs of the cyclones. He p ro- cure also an increase in the contact efficiency between the gas and regeneration of the catalyst to the high speed of passage and / or at very height / diameter ratio of the reactor (37), which improves the distribution and reduced foxing and back-mixing.
  • the flow which approximates a piston flow, avoids the segregation of large particles and the local presence of particles which are not completely regenerated. Control of afterburning in the second regeneration stage is facilitated, and eliminates the need for steam or water cooling devices which in conventional schemes cause significant losses of catalyst and reduction of their activity, as well as numerous damage to refractories and enclosures.
  • the suspension of regenerated catalyst in the combustion gases is discharged laterally in the duct (38) at a level slightly below the level of the top of the vertical reactor (37), so as to minimize the problems of erosion in this change zone 90 ° from the flow direction.
  • this suspension is accelerated to be separated in the first separation stage (5), which may consist of one or more cyclones in parallel, in which the regeneration gases are separated from the catalyst previously regenerated at high temperature.
  • the combustion gases then pass through a second high-efficiency separation stage (6) composed of one or more cyclones, in series and / or in parallel according to conventional techniques known to those skilled in the art.
  • the cyclonic separators (5) and (6) can be located outside the reactor (37) used for the second regeneration step, so that the problems of metallurgy at high temperatures are eliminated. Combustion gases rich in CO 2 leave the cyclonic separation train (5) and (6), through valves maintaining the pressure of the unit, and can then be used to generate process steam in a boiler (not shown).
  • the catalyst particles leave the second high temperature regeneration stage with preferred carbon contents, less than 0.04% by weight of the catalyst.
  • the regenerated catalyst the temperature of which is higher than the pseudo-critical temperature of the feed, is led into the mixer-contactor (11) by the lowering legs (3) and (4) of the separation train (5) and (6).
  • These lowering legs (3) and (4) in which a dense flow of the pulverulent solids is maintained by virtue of the flow control valves (7) and (8), are of a sufficient height to ensure pressure balancing. of unity.
  • the hot regenerated catalyst is kept in the fluidized state by injections (not shown in FIG. 1) of aeration gases, such as hydrocarbons of less than 4 carbon atoms, or other suitable gases such as inert gases.
  • aeration gases such as hydrocarbons of less than 4 carbon atoms, or other suitable gases such as inert gases.
  • the hot regenerated catalyst at a temperature higher than the pseudo-critical temperature of the feed, is then discharged through the overflow tubes (10), where it is intimately contacted with the hydrocarbon feed.
  • a catalyst withdrawal pipe (39) is provided in the lower part of the stripping zone (18); the fresh catalyst is added to the first regeneration stage (25) by the line (40), according to conventional devices.
  • FIG. 2 shows in more detail a preferred embodiment of one invention of the device for injecting and dispersing the hydrocarbon feedstock, at the top of the descending vertical reactor (101).
  • the catalyst regenerated at high temperature coming from the second regeneration stage (132) in an ascending vertical transfer line, arrives at the top of the reactor (101) by the lowering legs (103) and (104 ) one (or more in parallel) separation train (s) formed by the external cyclones (105) and (106), provided with solids flow control valves (107) and (108).
  • the hot, regenerated catalyst is received in an enclosure (located above the horizontal wall 113 a) in the form of a catalytic bed maintained in the dense fluidized state by injection of an aeration gas through at least a distributor (113).
  • This distributor (113) consisting for example of a grid or a set of perforated tubes (“sparge tubes”) is of conventional design known to those skilled in the art.
  • the aeration gas injected through this distributor (113) consists of inert gases or light hydrocarbons ("fuel gas") coming for example from the downstream fractionation stream of the unit outlet effluents (not shown), as well as any other suitable mixture or gaseous fluidizing agent.
  • fuel gas inert gases or light hydrocarbons
  • a possible injection of steam at this level may be carried out, within the limits permitted by the hydrothermal stability of the catalyst regenerated at high temperature in accordance with the invention.
  • the hot catalyst and the fluidizing gases are directed downwards by overflow into a plurality of pouring tubes (110).
  • the liquid hydrocarbon feedstock, preheated upstream (by a system not shown), to which a certain quantity of dispersion vapor can be added, is introduced by a supply ramp (102), which is subdivided into a plurality of conduits d 'feed (109), opening into the discharge tubes (110).
  • These supply tubes (109) terminate at their ends with spray and atomization nozzles (114) of conventional design known to those skilled in the art.
  • the hydrocarbon feedstock is atomized as finely as possible in the multi-nozzle injection system (114) with possible addition of dispersion vapor, up to droplet sizes smaller than the average particle size of the regenerated catalyst, ie usually smaller at 100 ⁇ (100 x 10 m), and preferably less than 90 and even 50u (50 x 10 -6 m).
  • the hydrocarbon droplets are ejected from the spray nozzles (114) at speeds of between 10 and 100 m / s, and therefore experience the start of vaporization at this level.
  • each of the discharge tubes (110) there therefore occurs a central, conical, dispersive jet of charge droplets surrounded by a ring of regenerated catalyst at high temperature which flows, transported by the fluidizing gas, along the walls of each of the discharge tubes (110).
  • this upper part (zone A) of each of the discharge tubes (110) there therefore occurs a set of two flows substantially parallels of the charge droplet jet, and concentrically of catalyst regenerated at high temperature. The contact between the two flows is relatively reduced in this zone A, and the heat transfers between the catalyst particles and the hydrocarbon droplets is essentially carried out radially, thus taking advantage of the high regeneration temperature in two steps to obtain very rapid heat transfers in this zone A.
  • Partial but already significant vaporization is thus carried out at the immediate exit of the injection nozzles (114). Thanks to the particular mode of heating the jets of droplets by flows of solids (catalytic particles) at high temperature, the temperature rise of the charge is very rapid, which promotes cracking reactions to the detriment of coking reactions. It is important that the size of the droplets is as small as possible so that the heat exchange process is not diminished by thermal diffusion from the outside to the inside of the droplets. Although the heat exchange is essentially carried out by radiation in this zone A, it is by no means excluded that the other forms of exchange, by conduction and / or convection, participate partially in the heat transfer process.
  • the heat exchange by radiation is predominant, at least in zone A as defined above. This makes it possible to reduce as much as possible the formation of agglomerates produced by the direct contact between the particles of hot catalyst, playing the role of heat transfer solids, and droplets of non-vaporized charge.
  • zone B In the lower part (zone B) of each of the discharge tubes (110), the two charge and catalyst flows are intimately mixed under the effect of the dispersion and the partial, but already significant vaporization, carried out previously in zone A, droplets of hydrocarbon charge.
  • the contact and the intimate mixture which are sought at the level of zone B between the catalyst and the hydrocarbon charge, are all the more effective as they are preceded by a significant vaporization of charge droplets in zone A.
  • the complete vaporization of the droplets is completed by mixing and intimate contact with the regenerated catalyst at high temperature. This mixing and this intimate contact are necessary to obtain very rapid heat transfers in this zone B.
  • the descending nature of the flows avoids back-mixing of the catalyst, promotes renewal of the catalyst around the injection nozzles and avoids the formation of a suspension in dense phase at the injection nozzles and in their immediate vicinity, as is the case for the feed systems of the ascending reactors traditionally used in FCC.
  • the retromixing at the injection nozzles the coke formed on the catalyst is considerably reduced, as well as the phenomena of agglomeration and growth of carbon deposits ("carbon build up"") which are harmful and inevitable in all the feed systems of the bottom-up reactors traditionally used in FCC.
  • All zones A and B carry out very rapid heat transfers between the regenerated catalyst at high temperature and the droplets of finely divided charge.
  • the length of the discharge tubes (110) is adjusted so that the charge / catalyst contact time does not exceed 500 milliseconds, and preferably remains less than 100 milliseconds.
  • the implementation, in this suitable mixing device, of very rapid thermal transfers achieves, at the level of the charge droplets, a real initial thermal shock, which completely vaporizes the light fractions of the charge, while thermally disintegrating the heavy fractions and the asphaltic structures it contains.
  • the implementation of such an initial thermal shock is necessary and favors the treatment of fillers containing significant amounts of heavy fractions and / or asphaltenic structures.
  • the hydrocarbon vapor / catalyst suspension then flows in a vertical direction descending through the reactor (101), the cross section of which can gradually vary to ensure the operating conditions required temperature and residence, as well as flow conditions close to piston flow.
  • FIG. 3 represents an adequate embodiment of the device for separating the effluent from the descending reactor (101) and the catalyst entrained by this effluent.
  • the suspension of hydrocarbon vapors / catalyst is accelerated in a convergent (212) with a half-angle at the apex between about 5 and 30 ° and preferably between 7 and 15 °, to enter the primary separator (213).
  • the primary separation device comprises only a single cyclone with direct passage (213) of the "uniflow cyclone" type, and tangential inlet, arranged here horizontally.
  • Other possible embodiments of the invention may include a plurality of these cyclones, arranged in parallel horizontally or vertically.
  • the gaseous effluent thus separated from the solid particles is discharged through the central coaxial conduit (209) which enters inside the outer body (213).
  • the solids are removed by the substantially vertical lowering leg (215).
  • This type of cyclone makes it possible to achieve, with a relatively short residence time, less than a second, a coarse primary separation, but nevertheless with efficiencies greater than 50%, up to 90%. To improve the efficiency of this primary separation, it is necessary to allow, with the flow of solids in the lowering leg; 215), the passage of a certain quantity of the gaseous effluent, which can reach 10% of the total volume flow of this effluent.
  • the outlet (209) could lead to the interior of the reactor or stripping zone (217), but preferably is connected directly by the conduit (224) to the inlet mouth of a secondary separation system (214) comprising one or more stages, in parallel and / or in series, constituted by conventional reverse flow cyclones known to those skilled in the art, which then allow very thorough separation of the catalyst still entrained in the 'gaseous effluent at the outlet (209) of the first rapid separation stage.
  • the stripping reactor (217) is generally then equipped in its upper part with one or more separation trains (219) for stripping effluents, conventional, composed of one or more stages of separation, in parallel and / or in series, constituted by conventional reverse cyclones according to devices known to those skilled in the art.
  • the outlet (208) of the separation train (214) discharges only the effluents from the reaction section (201), while the outlet (207) of the separation train (219) discharges only effluents from the stripping zone (217).
  • there are adjustment valves (237) and (238) which make it possible to control the balancing of the pressures at the level of the entire reactor or zone (217) stripping.
  • the stripping reactor (217) is generally flared at its upper part and lined with baffles or baffles (220) in its lower part (218) to improve the efficiency of the stripping operation.
  • a stripping gas such as steam, inert gases (CO, C0 2 , N 2 ,.) Is injected by a suitable distributor (221) (grid or perforated tubes). ..), combustion gases, or fuel gas.
  • the stripped catalyst is evacuated against the current from the reactor (217) by the lower withdrawal conduit (239-).

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EP85401559A 1984-08-02 1985-07-31 Verfahren und Vorrichtung für die katalystische Wirbelschichtspaltung Expired EP0171330B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8412388A FR2568580B1 (fr) 1984-08-02 1984-08-02 Procede et appareil pour craquage catalytique en lit fluide
FR8412388 1984-08-02

Publications (2)

Publication Number Publication Date
EP0171330A1 true EP0171330A1 (de) 1986-02-12
EP0171330B1 EP0171330B1 (de) 1988-03-30

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EP85401559A Expired EP0171330B1 (de) 1984-08-02 1985-07-31 Verfahren und Vorrichtung für die katalystische Wirbelschichtspaltung

Country Status (6)

Country Link
US (1) US4695370A (de)
EP (1) EP0171330B1 (de)
JP (1) JPH0633360B2 (de)
CA (1) CA1259577A (de)
DE (1) DE3562016D1 (de)
FR (1) FR2568580B1 (de)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2589875A1 (fr) * 1985-11-12 1987-05-15 Inst Francais Du Petrole Procede et appareil de craquage catalytique en lit fluide avec pretraitement de la charge hydrocarbonee
EP0226483A1 (de) * 1985-11-12 1987-06-24 Institut Français du Pétrole Verfahren und Vorrichtung für die katalytische Spaltung eines mit wenig aktiven Festteilchen vorbehandelten Kohlenwasserstoffeinsatzes
EP0254333B1 (de) * 1986-06-16 1991-01-16 Shell Internationale Researchmaatschappij B.V. Reaktor und Verfahren für katalytisches Cracken mit abwärts betriebenem Fliessbett
EP0617113A1 (de) * 1993-03-19 1994-09-28 Bar-Co Processes Joint Venture Fliessbettverfahren zur Verbesserung der Qualität von festen regenerierten Teilchen

Families Citing this family (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2607145B1 (fr) * 1986-11-25 1990-06-08 Inst Francais Du Petrole Procede ameliore de conversion thermique de fractions lourdes de petrole et de residus de raffinage, en presence de composes oxygenes du soufre, de l'azote ou du phosphore
US5112576A (en) * 1990-05-25 1992-05-12 Amoco Corporation Catalytic cracking unit with combined catalyst separator and stripper
US6714212B1 (en) 1993-10-05 2004-03-30 Canon Kabushiki Kaisha Display apparatus
FR2791354B1 (fr) 1999-03-25 2003-06-13 Inst Francais Du Petrole Procede de conversion de fractions lourdes petrolieres comprenant une etape d'hydroconversion en lits bouillonnants et une etape d'hydrotraitement
JP2002333870A (ja) 2000-10-31 2002-11-22 Matsushita Electric Ind Co Ltd 液晶表示装置、ｅｌ表示装置及びその駆動方法、並びに副画素の表示パターン評価方法
ES2187387B1 (es) * 2001-11-20 2004-04-16 Universidad Politecnica De Valencia. Una unidad de ensayo para el estudio de catalizadores en reacciones de corto tiempo de contacto entre el catalizador y los reactivos.
US7026262B1 (en) 2002-09-17 2006-04-11 Uop Llc Apparatus and process for regenerating catalyst
FR2981659B1 (fr) 2011-10-20 2013-11-01 Ifp Energies Now Procede de conversion de charges petrolieres comprenant une etape d'hydroconversion en lit bouillonnant et une etape d'hydrotraitement en lit fixe pour la production de fiouls a basse teneur en soufre
FR2983866B1 (fr) 2011-12-07 2015-01-16 Ifp Energies Now Procede d'hydroconversion de charges petrolieres en lits fixes pour la production de fiouls a basse teneur en soufre
CN102989409A (zh) * 2012-10-11 2013-03-27 田原宇 重油热解和气化耦合的双反应管循环床装置
FR2999600B1 (fr) 2012-12-18 2015-11-13 IFP Energies Nouvelles Procede de raffinage d'une charge hydrocarbonee lourde mettant en oeuvre un desasphaltage selectif
FR3000098B1 (fr) 2012-12-20 2014-12-26 IFP Energies Nouvelles Procede avec separation de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
FR3000097B1 (fr) 2012-12-20 2014-12-26 Ifp Energies Now Procede integre de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
FI125978B (fi) * 2013-02-22 2016-05-13 Endev Oy Kiertomassakuivuri ja menetelmä märän lietteen kuivaamiseksi
US9353029B2 (en) * 2013-03-14 2016-05-31 Honeywell International, Inc. Fluorination process and reactor
CN104610995B (zh) * 2013-11-05 2018-10-12 中国石油化工股份有限公司 一种基质沥青的生产方法
CN105441114B (zh) * 2014-09-12 2017-05-24 中石化洛阳工程有限公司 一种催化裂化装置
US9327278B1 (en) * 2014-12-17 2016-05-03 Uop Llc Process for catalyst regeneration

Citations (5)

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Publication number Priority date Publication date Assignee Title
US3152065A (en) * 1961-09-14 1964-10-06 Exxon Research Engineering Co Feed injector for cracking of petroleum
US3923686A (en) * 1972-05-30 1975-12-02 Universal Oil Prod Co Fluidized catalyst regeneration by oxidation in a dense phase bed and a dilute phase transport riser
US4097243A (en) * 1976-11-04 1978-06-27 Uop Inc. Hydrocarbon-feed distributor of injecting hydrocarbon feed
US4336160A (en) * 1980-07-15 1982-06-22 Dean Robert R Method and apparatus for cracking residual oils
US4411773A (en) * 1980-12-18 1983-10-25 Mobil Oil Corporation Heat balance in FCC process and apparatus with downflow reactor riser

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2607662A (en) * 1946-01-30 1952-08-19 Universal Oil Prod Co Stripper for subdivided catalyst particles
US2850808A (en) * 1956-07-02 1958-09-09 Cons Coal Company Grid structure for fluidized solids contacting apparatus
US2965454A (en) * 1957-04-30 1960-12-20 Phillips Petroleum Co Fluidized conversion and stripping apparatus
US3246960A (en) * 1961-11-17 1966-04-19 Humble Oil & Refining Company Catalytic conversion apparatus
US3835029A (en) * 1972-04-24 1974-09-10 Phillips Petroleum Co Downflow concurrent catalytic cracking
US4385985A (en) * 1981-04-14 1983-05-31 Mobil Oil Corporation FCC Reactor with a downflow reactor riser
US4514285A (en) * 1983-03-23 1985-04-30 Texaco Inc. Catalytic cracking system

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3152065A (en) * 1961-09-14 1964-10-06 Exxon Research Engineering Co Feed injector for cracking of petroleum
US3923686A (en) * 1972-05-30 1975-12-02 Universal Oil Prod Co Fluidized catalyst regeneration by oxidation in a dense phase bed and a dilute phase transport riser
US4097243A (en) * 1976-11-04 1978-06-27 Uop Inc. Hydrocarbon-feed distributor of injecting hydrocarbon feed
US4336160A (en) * 1980-07-15 1982-06-22 Dean Robert R Method and apparatus for cracking residual oils
US4411773A (en) * 1980-12-18 1983-10-25 Mobil Oil Corporation Heat balance in FCC process and apparatus with downflow reactor riser

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2589875A1 (fr) * 1985-11-12 1987-05-15 Inst Francais Du Petrole Procede et appareil de craquage catalytique en lit fluide avec pretraitement de la charge hydrocarbonee
EP0226483A1 (de) * 1985-11-12 1987-06-24 Institut Français du Pétrole Verfahren und Vorrichtung für die katalytische Spaltung eines mit wenig aktiven Festteilchen vorbehandelten Kohlenwasserstoffeinsatzes
EP0254333B1 (de) * 1986-06-16 1991-01-16 Shell Internationale Researchmaatschappij B.V. Reaktor und Verfahren für katalytisches Cracken mit abwärts betriebenem Fliessbett
EP0617113A1 (de) * 1993-03-19 1994-09-28 Bar-Co Processes Joint Venture Fliessbettverfahren zur Verbesserung der Qualität von festen regenerierten Teilchen

Also Published As

Publication number Publication date
FR2568580B1 (fr) 1987-01-09
FR2568580A1 (fr) 1986-02-07
JPH0633360B2 (ja) 1994-05-02
EP0171330B1 (de) 1988-03-30
JPS6142591A (ja) 1986-03-01
CA1259577A (fr) 1989-09-19
DE3562016D1 (en) 1988-05-05
US4695370A (en) 1987-09-22

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