Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • 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
• • 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
  • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G9/002—Cooling of cracked gases
• • 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
  • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
  • C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique

Definitions

• the present invention relates to a steam cracking method and device for converting petroleum hydrocarbon fractions, in the fluidized phase of heat-carrying particles and at high temperature, for the production of olefins and, in particular, olefins comprising 2 to 4 carbon atoms, butadiene and monoaromatic compounds, such as benzene, or which can be branched, such as toluene, xylenes, etc.
• hydrocarbon cracking processes are commonly used in the petroleum and parapetroleum industries; they consist of dividing, by increasing the temperature, hydrocarbon molecules into smaller molecules.
• thermal cracking and catalytic cracking, which involve either the only influence of temperature or the active sites of a catalyst.
• thermocracking reaction takes place mainly in the part of the tubes receiving the maximum heat flux, where the temperature is determined by the nature of the hydrocarbons to be cracked: - for the so-called visbreaking processes, in which only the heaviest molecules are split into smaller molecules, the cracking temperature is between 450 and 600 ° C depending on the case;
• the necessary temperature is much higher and generally between 780 and 850 ° C, depending on the type of charge to be cracked, but it remains however limited by the conditions of implementation of the process and by the complexity of operation of the ovens, which use additional heating energy. Obtaining and maintaining the required temperature levels is all the more delicate since it gradually deposits unwanted coke on the walls of the tubes and the heat flow is limited. In addition, the higher wall temperature than that of the process is the cause of the formation of coke and degradation products such as gums and acetylenic compounds.
• Coke affects the quality of heat exchange; it leads to an increase in the pressure drop inside the tubes and an increase in the skin temperature imposing an excessive mechanical stress, which contributes to reducing the conversion rate of the load of hydrocarbons entering the unit. thermocracking and causes periodic stops for decoking. It also follows, on the one hand, that the process must be modular, so as to allow decoking operations in operation, and, on the other hand, that the loads to be treated must be "clean", so that that the duration of the cycles between two decokings is not too short. In practice, these charges are limited to LPG, gasoline, and certain favorable or hydrotreated gas oils.
• thermocracking reaction is very endothermic. There are therefore problems of temperature regulation and maintenance and, consequently, of selectivity, which are very difficult to solve.
• thermocrack petroleum hydrocarbon fractions which include light paraffins such as butanes, propane and especially ethane, as well as petroleum fractions such as gasolines, naphthas and diesel fuels, it is necessary to maintain the reaction temperature at a very high level, generally of the order of 750 to 850 ° C, for a very short time, but strictly controlled.
• the present invention aims to remedy these drawbacks by proposing a process for the conversion by steam cracking at high temperature of petroleum hydrocarbon fractions into olefins such as ethylene, propylene and butenes, butadiene and monoaromatic compounds, for example. introduction of said cuts into a dilute fluidized phase of heat-carrying particles and water vapor at high temperature, under reaction conditions of fluidization, of temperature and of strictly determined duration.
• the invention also aims to allow satisfactory conversion, by cracking the cuts introduced into the reactor, with a high selectivity for light olefins, butadiene and monoaromatic compounds.
• the invention also aims to allow effective control of the polymerization reactions of the reaction products.
• the invention finally aims to produce coke only reduced quantity, but sufficient to satisfy the thermal balance of the unit.
• the subject of the invention is a process of conversion by steam cracking, at high temperature and in the presence of a dilute fluidized phase of essentially heat-transferable particles, on the one hand, of at least one cut of light hydrocarbons little contaminated with metals, the boiling point of which is less than about 400 ° C and, on the other hand, a heavier hydrocarbon charge, consisting essentially of compounds with a boiling point above about 400 ° C, this process comprising a step of bringing said cut, then said load, in a staged manner and with decreasing severity, with heat transfer particles, catalytic or not, in a continuous reactor of tubular type with ascending flow or descending, a separation and stripping step making it possible to separate, on the one hand, at least 90% of said particles, which are then preferably regenerated by combustion of the coke deposited on r these before recycling them at a higher temperature to the feed to said continuous reactor and, on the other hand, the effluent hydrocarbons, which are recovered during a fractionation stage by distill
• the cut or cuts of lightly contaminated light hydrocarbons distilling at less than 400 ° C. may be advantageously chosen from the group consisting of light paraffins such as ethane, propane and butanes, and heavier hydrocarbons such as essences, naphthas and gas oils, or even certain cuts with higher boiling point, but strongly paraffinic or naphthenic, such as paraffins or slack oil or oil recycles.
• These hydrocarbon fractions can come either from different refinery units, such as atmospheric distillation, visbreaking, hydrocracking, oil manufacturing or olefin oligomerization units, or effluents from the conversion unit itself.
• These various cuts can also be injected alone or in combination with steam and possibly other fluidizing gases such as hydrogen and light gases.
• the steam cracking will be carried out in the continuous reactor in several zones of decreasing severity, by successive injections in the presence of steam and / or gaseous fluids of several distinct cuts, the first cut must necessarily have a boiling temperature lower than that of the next.
• This temperature profile is in fact particularly advantageous for optimizing the selectivity of the reactions involved. It is possible, for example, to successively inject a first cut containing mainly ethane, then optionally propane and butane, then in the liquid phase , a cut containing light gasolines, then possibly naphthas or gas oils and finally the heavier hydrocarbon charge, having a boiling point higher than about 400 ° C.
• the latter can advantageously be chosen from the group consisting of atmospheric or vacuum distillation residues, deasphalting pitches, catalytic slurries, or synthetic hydrocarbons.
• These charges can therefore be very heavy charges containing hydrocarbons whose boiling point can go up to 750 ° C. and more, and whose density can vary between 0 and 25 ° API.
• the quantity injected of these heavy hydrocarbon charges may advantageously, depending on the desired temperature profile and the needs of the thermal balance, represent 0.25 to 4 times the quantity of light cut injected in upstream.
• the continuous reactor In its most elaborate configuration, including successive injections of increasingly heavy cuts, for example of ethane or LPG (liquefied petroleum gas), then of petrol or diesel and, finally, of the heavier load , of the distillation residue type, in the continuous reactor zone located downstream, the continuous reactor will therefore, in fact, comprise several distinct reaction zones, operating successively under conditions of decreasing severity (decrease in temperature, in duration of contact with the heat transfer mass, the possibly catalytic activity of the heat transfer mass and the ratio between the flow rate of this mass and that of the hydrocarbons) and adapted to the nature of the charges to be treated and of the products sought.
• LPG liquefied petroleum gas
• the separation system generally ballistic, often made up of cyclones, is effective and, in this case, the duration of the separation is too long to be able to optimize production and avoid coking and the formation of acetylene-type contaminants;
• the separation system is instantaneous but less efficient, this time resulting in either an excessive loss of hydrocarbons by entrainment of the latter in the regeneration zone, or an excessive entrainment of solid particles with the gaseous effluents and in particular fines, which it is very expensive to isolate distillates, the latter then becoming difficult to recover, with the risk of undesirable side reactions, when the solid particles have a certain catalytic activity.
• the present invention aims to remedy the problems associated with the formation of coke and degradation products in the conduits leading the reaction effluents from the steam cracking units to the fractionation zone of these effluents.
• the temperature of these In order to be able to fractionate the effluent hydrocarbons from steam cracking units of the conventional type by distillation, the temperature of these must be lowered very sharply and above all very quickly, so as to obtain a fractionation tower inlet temperature lower than the "dew point" of effluents (ie at a temperature at which the heaviest fractions condense).
• the heaviest compounds produced by the steam cracking reaction tend to deposit on the wall of the pipes, which causes regular and costly shutdowns of the steam cracking units for decoking these pipes. .
• the present invention also makes it possible to remedy the drawbacks mentioned above, insofar as the injection of a major part of the heaviest charge necessary for the thermal equilibrium of the steam cracking reaction is carried out after step separation of at least 90% of the particles and of the hydrocarbons and before that of fractionation by distillation.
• This particular mode of charge injection makes it possible to completely control the temperature and duration conditions of the steam cracking reaction for the following reasons:
• the quenching effect necessary for the instantaneous cessation of the thermal reactions is ensured by spraying the charge itself, which is thereby preheated, which, combined with the dilution effect of the condensed liquid effluents, allows effectively deactivate all the coke precursors present in the steam cracking effluents, by dissolving in the still liquid petroleum charge (this quenching effect can optionally be completed before the fractionation step, either by passing the hydrocarbons through a heat exchanger, or by a new injection of water, steam or any other cut of hydrocarbons); - 0.01 to 10% and, preferably 0.05 to 5%, of heat transfer particles entrained in the reactor effluents allow both permanent sweeping of the walls, thus preserving them from any fouling, and absorption of erasers being formed in the effluent transfer lines to the fractionation zone;
• the entrained heat transfer particles can be fully recycled and it is then possible, without excessive loss of heat transfer particles, to promote the rapid separation between the heat transfer particles and the gaseous effluents, even if this must be done at the expense of the efficiency of separation.
• an almost instantaneous heat transfer is provided between the heavier hydrocarbon charge and the effluents of the steam cracking reaction by spraying in a manner known per se (see, for this purpose , European Patent No. 312,428) said filler in the liquid state.
• the injector (s) will be adapted to allow spraying of the charge in drops of diameter less than 200 microns and, preferably, 100 microns.
• Said injectors may advantageously be equipped with mixing chambers making it possible to introduce certain quantities of water or steam, or other petroleum fractions, with the charge.
• the quality of the quenching will be optimum, insofar as the temperature of the hydrocarbons entering the fractionation zone and resulting from the dissolution of the steam cracking effluents in the feed. the heaviest to steam will be below the "dew point" of these hydrocarbons.
• the heat transfer thus carried out makes it possible to bring the hydrocarbons to a temperature which will preferably be between 300 and 450 ° C. in less than 0.3 seconds and, preferably, in less than 0.1 seconds.
• the charge of hydrocarbons entering the fractionation zone will have a temperature less than 100 ° C and, preferably, less than 50 ° C than the temperature corresponding to the "bubble point" of said charge (c (i.e. at a temperature where it is in the liquid state, but at which the first bubbles of gaseous hydrocarbons are formed).
• the production of olefins and of monoaromatic compounds can be notably increased by judicious reuse of the saturated hydrocarbons produced during the reaction: it will suffice, for this purpose, to separate from each cuts C2, C, C ⁇ and others produced, these hydrocarbons saturated with olefins and to recycle the hydrocarbons in the corresponding injection zone of the upstream part of the reactor described above.
• An additional advantage arising from the present invention resides in the fact that the hydrogen necessarily produced by steam cracking in the upstream part of the reactor is capable of reacting under the reaction conditions of the downstream part of the reactor, and, therefore, of improving the selectivity of the effluents from the conversion unit into better-valued and possibly more stable products.
• the deposition of coke resulting from thermal or catalytic cracking must, for economic reasons, be minimized, but nevertheless be sufficient to ensure the thermal balance in the upstream and downstream parts of the tubular reactor (failing this, the heat balance can be ensured by the introduction of an auxiliary fuel into the regenerator); also, at least 50% and preferably 80% by weight of the heavy feed should preferably have a boiling temperature above about 400 ° C. This value of approximately 400 ° C. being mainly linked to the cutting point of the distillation residues, it may of course vary between 300 and 550 ° C. without departing from the scope of the present invention.
• fillers include vacuum gas oils and heavier hydrocarbon oils such as crude oils, whether or not topped, as well as residues from atmospheric distillation or vacuum distillation, pitches, bitumen emulsions, aromatic extracts , catalytic slurries, or synthetic or used oils.
• These fillers may, if necessary, have received a preliminary treatment such as, for example, a hydrotreatment. They may, in particular, contain fractions whose boiling point can go up to 750 ° C. and more, which may contain high percentages of asphaltenic products, and have a carbon content. Conradson high (10% and above).
• lighter cuts which may include cuts of hydrocarbons which have already undergone a cracking operation and which are recycled, such as LCOs ("Light Cycle Oils")
• LCOs Light Cycle Oils
• the interval d boiling is generally between 160-220 ° C (start of cut) and 320-380 ° C (end of cut)
• heavy recycling oils or HCOs Heavy Cycle Oils
• the boiling range is generally between 300-380 ° C (start of cut) and 460-500 ° C (end of cut)
• catalytic residues slurries
• the charges can advantageously be preheated in a temperature range generally between 100 and 400 ° C., preferably close to the bubble point, so as to promote instant and homogeneous vaporization when brought into contact with the hot solid grains.
• ° n can use, to implement the process according to the present invention, inert heat transfer particles of a type known per se, such as kaolin or silicate microspheres; it is also possible to use all the classes of catalysts having catalytic cracking capacities.
• a particularly advantageous class is constituted by catalysts having porous structures in which molecules can be brought into contact with active sites located in the pores; in this class, there are in particular silicates or aluminosilicates.
• catalysts comprising stable zeolites are commercially available with supports containing a variety of metallic cv-ydes and combinations of said oxides, in particular silica, alumina, magnesia and mixtures of these. substances, as well as mixtures of said oxides with clays.
• the catalytic composition can naturally contain one or more agents promoting one or more the other step of the process; the catalyst may therefore contain, in particular, agents promoting the combustion of coke, during regeneration, or contain agents capable of promoting the cyclization of olefins into aromatics and vice versa, if the production of aromatics becomes a priority objective .
• the invention therefore also relates to a steam cracking device, by conversion by direct contact, in the fluidized phase of heat-carrying particles and at high temperature, of petroleum hydrocarbon charges comprising, on the one hand, at least one light, slightly contaminated cut. by metals, the boiling point of which is less than about 400 ° C and, on the other hand, a charge of heavier hydrocarbons consisting essentially of compounds whose boiling point is above 400 ° C,
• this device comprising a continuous reactor for bringing petroleum fractions at high temperature into contact with heat transfer particles, catalytic or not, the continuous reactor being of tubular type with essentially ascending or descending flow, means in particular ballistic capable of effecting the separation of minus 90% of said particles and cracked hydrocarbons, means for stripping separate particles, means for r generation under combustion conditions of the coke deposited on these particles by air or steam, and means for recycling the regenerated particles to the feed of said reactor, as well as means for fractionating the gaseous effluents by distillation, said device being characterized in
• the injectors of the fractionation residues recycled in the downstream part of the continuous reactor will be adapted to allow spraying of the charge in drops with a diameter of less than 200 microns and, preferably, less than 100 microns. They will preferably be of the venturi type with a wide neck (see European patent n ° 312 428) to limit as much as possible the problems of attrition linked to the presence of recycled heat transfer particles.
• certain types of devices for separating effluents from steam cracking intended to limit the duration of the transfer of effluents to the fractionation zone by distillation could more advantageously be used in accordance with the present invention.
• the reactor when the reactor will operate in ascending mode (“riser"), due to the production of a large quantity of gaseous hydrocarbons, the heat-transfer particles will reach the reaction zone at high speeds (between 20 and 200 m / s and, preferably, between 40 and 100 m / s), and a simple device for separation by centrifugation can therefore possibly be used. The generally expensive use of cyclonic systems can thus be avoided.
• the reactor when the reactor is operating in descending mode (“dropper”), the heat-transfer particles will be collected in an enclosure arranged at the base of the dropper, where they will be stripped after being separated from the steam cracking effluents by simple ballistic effect.
• FIG. 1 illustrates the application of the invention to a set of steam cracking in an ascending column or riser or "riser” and to a single regeneration chamber at high temperature of the heat-carrying particles, suitable in particular for the regeneration of contact masses ;
• the ballistic separation device is provided with a simple centrifugal ballistic separation device;
• FIGS. 2 and 3 illustrate the application of the invention to a steam cracking assembly with an essentially descending reaction zone ("dropper").
• the ascending fluidized phase steam cracking device shown diagrammatically in FIG. 1 comprises a reaction column 1, known as a load riser, or “riser”. This is supplied at its base, via line 2, with regenerated heat-transfer particles, in a quantity determined for example by the opening or closing of a valve 3.
• the regenerated particles are fluidized by injection at the base of the riser, using a diffuser 5, steam arriving via line 4, or any other suitable gas flow.
• a first line 6 here supplies a diffuser 7, making it possible to inject a saturated light gas such as ethane into the upstream part of the reactor.
• a cut which here is a propane cut, but which could just as well be a butane cut or a mixture of the two, can then be injected identically by line 8 using the diffuser 9.
• a cut of gasoline or diesel can finally be vaporized here using an injector 11 supplied by line 10.
• a charge of distillation residue coming from line 14 from the fractionation zone 12 is introduced, possibly mixed with a little of fresh charge supplied by the line 40, using an injector 13, in the downstream part of the reactor, under temperature conditions close to the bubble point of said residue, in order to facilitate instant and homogeneous vaporization.
• Column 1 opens at its top in an enclosure
• a line 20 supplies stripping gas , generally water vapor, diffusers 21, regularly arranged at the base of the enclosure 15.
• the quenching effect of the effluents from the steam cracking reaction, caused in 17 by the direct contact between the droplets of the fresh charge and said effluents, is here reinforced by the injection by line 50 of a residue recycle of the distillation carried out in the fractionation zone 12.
• the distillation residue can be cooled by passing through a heat exchanger 51 and the calories thus recovered can be used to form water vapor for the entire installation, without that it is necessary to use additional quenching, as is the case with conventional methods.
• the presence of a small quantity of grains or fines of the solid heat carrier in the reactor effluents not only allows effective sweeping of the walls, but also constitutes a means of adsorption of the gum precursors and of coke deposits.
• additional fuel can be injected.
• the regeneration gas is separated from the heat-carrying particles entrained in the cyclone 27, from which the regeneration gas is evacuated by a line 28, while the regenerated and hot heat-carrying particles are extracted from the regulator, from where they are recycled by the conduit 2 to the elevator supply or riser 1.
• a gasoline section the boiling range of which generally extends from section c 5 to around 200-220 ° C;
• a diesel type cut the boiling range of which generally extends from 160-220 ° C (start of cut) up to around 320-400 ° C (end of chopped off ) ;
• Part of this fractionation residue is therefore injected at 13 into the steam cracking reactor, in accordance with the present invention; depending on the case and after recovery of the heat by passing through the exchanger 51, another part can either be recycled for quenching, by the line 50, in mixture with the charge to be steam cracked, or withdrawn from the device by the purge line 52.
• ethane, propane, gasoline cut, from this fractionation device can be recycled in the reaction section by lines 30, 31, 36, then 6, 8 and 10, while the olefins in C 2 , C3 produced by steam cracking are isolated by lines 33 and 34 respectively.
• An essential advantage of this fluidized phase steam cracking device lies in the fact that good use of the temperature profile in the reaction zone 1 makes it possible to selectively crack several petroleum fractions.
• steam can be introduced via line 4, as well as ethane through line 6, coming from either from the fractionation device via line 31, or from another unit of the refinery;
• the temperature of the reaction zone decreases appreciably, and it is then possible to inject saturated hydrocarbons downstream more heavy, such as propane (in 8) or butane (in 11) or even light gasolines (in 11) or naphthas, with possible addition of water vapor by lines 38, 39 and 40.
• regulation, 41 to 44 can also make it possible, in a manner known per se, to modulate the quantities injected into the reaction zone, in order to maintain the desired temperature profiles thanks to temperature probes placed for this purpose in said zones.
• FIGS. 2 and 3 are variants of that of FIG. 1, in which the reaction zone is operating this time in descending mode.
• the reactor will therefore be called “dropper”, by reference to the English term.
• the parts of this device identical to those of FIG. 1 are designated therein by the same reference numerals, assigned the index 'for Figure 2 and the index' 'for Figure 3.
• regenerator a different type of regenerator is used, capable of better withstanding the high temperatures required by steam cracking.
• the regeneration fumes leave the unit in 28 'after passing through a cyclone 27' external to the regeneration chamber 22 '.
• the regeneration chamber 22' is located in the upper part of the unit, and the particles to be regenerated come from the stripping zone by line 23 'must be transported by an ascending column 55'. This transport is carried out by fluidization with a gas diffused in 26 'by line 25'.
• a primary combustion of the coke deposited on the catalyst particles can take place under conditions known per se with a fluidizing gas containing air or oxygen.
• the particles of the catalyst and the fluidizing gas are then separated ballistically by means of the device 56 'and the particles of the catalyst are regenerated in a manner known per se in the chamber 22', where the particles are burned against the flow of oxygen. brought by line 45 'to diffuser 46 •.
• the regenerated particles of the catalyst can be introduced without thermal losses into the upstream part of the reactor l 'in an amount determined by the flow rate of the diffuser 57'; the homogeneity of the grain distribution is ensured by a device of a type known per se and not shown here.
• the particles dive directly into the dense fluidized stripping zone 15 ', while the hydrocarbon vapors as well as the stripping vapor coming from the diffuser 21' supplied by the line 20 'and the stripped hydrocarbons are evacuated almost instantaneously by line 17 ', where they are immediately quenched by dissolution in the heavy load which enters the unit by line 18'.
• the regenerated and hot particles coming from line 2" are first transported inside an ascending column 58 "by injection of a fluid such as water vapor arriving via line 4". After passing through the two elbows 59 “and 60", at right angles, the particles are discharged homogeneously into the dropper 1 ", into which, for example, are successively injected, in 7" and 8 “, ethane and gasoline Then, the effluents are quenched by the heavy load at 19 ", and the distillation residue from the fractionation zone 12" is injected at 13 "at a temperature close to its bubble point.
• the particles are stripped and leave zone 15 "by line 23", at the bottom of which an injection of fluid, such as steam or air, makes it possible to transfer them by line 55 "to the regeneration chamber 22".
• a ballistic separation device 56 "allows them to be poured into the combustion zone in a fluidized bed.
• EXAMPLE shows the advantages of a device according to the present invention, of the type shown in FIG. 3.
• the tests were carried out using ethane, a gasoline cut (straight-run cut) and two charges A and B, which are respectively an atmospheric distillation residue and a vacuum distillation residue of a crude oil of the SHENGLI type.
• contact mass particles composed of microspheres, mainly kaolin, with a specific surface of approximately 10 m 2 / g and an average diameter of approximately 70 microns are used.
• the charge injectors in the quenching zone and in the reactor are of the type described in European patent application No. 312,428.

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• Thermal Sciences (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

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• 1989
  • 1989-09-01 DE DE68914291T patent/DE68914291T2/de not_active Expired - Fee Related
  • 1989-09-01 EP EP89910120A patent/EP0489726B1/de not_active Expired - Lifetime
  • 1989-09-08 CA CA000610736A patent/CA1337477C/fr not_active Expired - Fee Related
• 1992
  • 1992-04-10 US US07/836,330 patent/US5538625A/en not_active Expired - Fee Related

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