Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/005—Separating solid material from the gas/liquid stream
  • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/1818—Feeding of the fluidising gas
  • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/1872—Details of the fluidised bed reactor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/36—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed through which there is an essentially horizontal flow of particles
• • 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
  • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
  • C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00654—Controlling the process by measures relating to the particulate material
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00796—Details of the reactor or of the particulate material
  • B01J2208/00823—Mixing elements
  • B01J2208/00831—Stationary elements
  • B01J2208/0084—Stationary elements inside the bed, e.g. baffles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00796—Details of the reactor or of the particulate material
  • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1081—Alkanes
  • C10G2300/1085—Solid paraffins
• • 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
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/20—C2-C4 olefins
• • 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
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/22—Higher olefins

Definitions

• the NCC process (abbreviation of Naphtha Catalytic Cracking) can be defined as an evolution of the catalytic cracking process (FCC) whose characteristic is to crack light paraffinic loads of gasoline type, that is to say having from 5 to 12 carbon atoms, in particular to produce light olefins and aromatics.
• FCC catalytic cracking process
• the cracking of these light cuts into the desired products requires a contact time of the order of one second, and the catalyst needs to be regenerated frequently.
• the most suitable reactor to meet these criteria is a circulating turbulent fluidized bed reactor.
• the diameter of the industrial reactor can reach 10m and beyond, the height remaining relatively low to meet the criterion of the desired contact time which in the context of the NCC process is of the order of a few seconds , leading to reactors with a low ratio of height to diameter (H / D), generally less than 0.5.
• the invention describes a reactor adapted to the implementation of the cracking of light paraffinic sections, said reactor being compartmentalized, making it possible to reach diameters of 10 m and more, and having a low H / D ratio, that is to say less than 0.5.
• the present invention comprises not only the fluidized compartmentalized reactor, but also the central stripping chamber which is itself fluidized.
• the reactor / stripper assembly forms a whole. DESCRIPTION OF THE FIGURES
• Figure 1 shows a sectional view of the reaction zone (reactor + stripper) in the case of compartments in parallel. Four compartments have been represented by way of example without this being limiting.
• Figure 2 shows a top view of the reaction zone and allows to visualize the different compartments.
• Figure 3 is a 3D view of the reactor according to the invention in the configuration of compartments operating in parallel which makes it possible to better observe the flow direction of the compartments towards the central stripping enclosure.
• Figure 4 is a 3D view of the reaction zone (reactor + stripper) in the case of compartments operating in series. The heights of the partitions 4a, 4b, 4c and 4d are decreasing so as to allow a natural overflow from one compartment to the next. The transfer to the central stripping enclosure is done from the last compartment of the series.
• Figure 5 shows the equivalent diameter of each compartment.
• FIG. 1 is a sectional view of the reactor and the stripper according to the invention in which two compartments a and d are recognized, and the central chamber 5 represents the stripper, as well as the cyclones 7a and 7d which enable the solid gas separation before reintroduction of the catalytic solid in the compartment or compartments concerned.
• the reactor is fluidized using a crown or sparger type gas distributor 2, the gas being a mixture of the vaporized charge and the steam.
• FIG. 2 is a view from above of the stripping reactor according to the invention which makes it possible to clearly visualize the radial walls 4a, 4b, 4c and 4d delimiting the various compartments a, b, c and d, as well as the central chamber (5 ).
• the fluidization ring is on this figure common to the different compartments. It is also possible to consider independent distributors supplying the different compartments.
• Each compartment is supplied with regenerated catalyst through a pipe of its own (3a, 3b, 3c and 3d), the catalyst flow rate being regulated for each compartment. It is in this that this configuration is called "in parallel”.
• the catalyst of each compartment overflows at the top (6) of the central chamber (5), to be streaked and directed to the regenerator (not shown in the figures).
• FIG. 3 represents a 3D view of the preceding figures 1 and 2.
• Figure 4 shows the reaction zone in a "series" compartment configuration. It differs from the "parallel" configuration in two main points:
• a single catalyst feed (3) feeds the reactor at the first compartment a.
• the passage of the catalyst from one compartment to another is by overflow, using walls of different heights.
• the catalyst enters the last compartment d in the stripper through the window (6).
• the number of compartments can vary between 2 and 12, and preferably between 3 and 9.
• FIG. 5 represents the equivalent diameter Deq of each compartment: the surface of a compartment corresponds to the surface of a disk of diameter Deq.
• EP0607363 discloses a series of fluidized bed rectangular zones for the continuous coating process of fertilizer substrate particles, with different gas velocities depending on the zones.
• a conduit having an upper opening in a portion of 1 fluidised bed, and a lower opening in a lower portion of the 2nd fluidized bed is used to circulate the particles from 1 to 2 nd bed by varying the velocity gradient of gas.
• US3236607 discloses a multi-stage iron ore reduction reactor for controlling the degree of conversion at each stage.
• the use of transverse walls in the reactor makes it possible to reduce the backmixing of the solid, thus favoring conversion.
• the passage of the solid from one compartment to another is by overflow. This configuration allows the use of different gases in the different zones.
• the patent KR100 360 1 10 describes a fluidized bed reactor to achieve high efficiency and reduce the phenomenon of back mixing (commonly called "back mixing" in the English terminology).
• the reactor described in this document comprises three fluidized chambers separated by vertical partitions and communicating with each other through orifices in submerged position.
• the present invention describes a fluidized reactor with a low ratio height / diameter (H / D less than 0.5) with a diameter D greater than 6 meters, up to 25 meters, this reactor having different compartments that can operate in series or in parallel.
• the reactor according to the invention also has a central chamber communicating with one or more compartments and for stripping the catalyst, before being sent to the regenerator.
• the present invention can be defined as a compartmentalized fluidized bed reactor for the catalytic cracking of light cuts in order to produce light olefins, said reactor having a diameter of between 6 and 25 meters, preferentially understood. between 10 and 20 meters, and an H / D ratio of between 0.1 and 1, and preferably between 0.2 and 0.6.
• This reactor therefore has a relatively flattened shape and has compartments obtained by radial vertical partitions extending substantially over the entire height H of the reactor.
• compartments therefore have the form of radial sectors, generally identical to each other, although it remains within the scope of the invention having compartments of different sizes.
• the reactor according to the invention is provided with a cylindrical chamber located substantially in the center of the reactor, which chamber will be called in the central chamber suite communicating by overflow with said compartments in the "parallel” case, or with the last compartment in the "serial” case.
• This chamber itself fluidized, has the function of ensuring the stripping of the catalyst, that is to say to desorb the adsorbed hydrocarbons on the catalyst surface before sending it to the regeneration zone.
• the regeneration zone will not be described in the present invention because it has no particular difference with respect to the regeneration zone of a conventional catalytic cracking unit.
• the ratio of the diameter of the central chamber to the reactor diameter is generally between 0.1 and 0.5 and preferably between 0.15 and 0.3.
• the diameter of the stripper is dimensioned so that the catalyst flow is between 20 and 250 kg / m 2 / s.
• the upper part of the reactor located above the compartments allows the separation of the fluidization gas and the catalytic solid particles, the latter being reintroduced into the fluidized compartments.
• the separation of gaseous effluents and catalyst particles is generally provided by one or more stages of cyclones whose return legs are immersed in the fluidized bed of each compartment, or only in certain compartments.
• the compartmentalised fluidized bed reactor-stripper according to the invention has a number of radial compartments substantially between 2 and 12, preferably between 3 and 9. This compartmentalization makes it possible to pass from a reactor of an H / D ratio to several compartmentalized reactors of ratio H / Deq.
• the compartmentalised fluidized bed reactor according to the invention is fluidized either by a gas distributor common to all the compartments, for example a single crown serving each compartment, or by an individual fluidization member at each compartment, it can be commonly a crown or a "sparger".
• Sparger is any system of distribution of the fluidization gas in the form of a grid provided with branches.
• These fluidization members, crown or “sparger” are well known to those skilled in the art, and will not be described further.
• the fluidization of the reactor is provided by a single crown serving each of the compartments and running through the entire reactor.
• the main application of the reactor-stripper according to the invention is the catalytic cracking process of light paraffinic slices in order to produce large intermediates in the petrochemical industry and in particular ethylene, propylene and BTX, a process called NCC by abbreviation for "Naphtha Catalytic Cracking".
• NCC by abbreviation for "Naphtha Catalytic Cracking”.
• FCC Fluidized Catalytic Cracking
• Another distinguishing feature of the FCC and NCC is the thermal balance of the unit.
• the thermal balance is naturally balanced, that is to say that the heat generated by the combustion of the coke deposited on the catalyst is sufficient to ensure the various heat consumption stations, vaporization of the charge and endothermicity of the cracking reactions.
• the formation of coke is much lower because of the low Carbon Conradson charges, it is necessary to introduce a cut in addition to the load to provide the necessary calories. This lower coke formation also explains the possibility of a longer residence time of the solid in the NCC reactor than in that of the FCC riser.
• the series operation of the reactor insofar as it makes it possible to adjust the charge flow rate in each compartment, can therefore make it possible to change this charge rate as a function of the average content of the charge. coke of the catalyst contained in each compartment, which content increases from one compartment to the next.
• the compartments of the reactor operate in parallel at a fluidization rate of between 0.5 and 1.5 m / s, preferably between 0.7 and 1.3. m / s, and more preferably between 0.8 and 1 m / s.
• the compartments operate in series, the passage from one compartment to the next taking place by overflow, and the fluidization speed at the passage from one compartment to the next can decrease by about 15%, preferably by 10%.
• the stripping function of the catalyst carried out by the central chamber makes it possible to eliminate the hydrocarbons adsorbed on the catalyst and operates in a fluidized bed at a fluidization velocity of between 0.1 and 0.5 m / s, and preferably between 0, 2 and 0.4 m / s.
• the catalyst flow in the stripper is between 20 and 250 kg / m 2 / s.
• the present invention describes a compartmentalised fluidized reactor with a diameter greater than 6 meters, up to 25 meters, and a low H / D ratio ( ⁇ 0.5) in order to:
• the contact between the gas and the solid is therefore essential in the case of the invention, both at the level of the reaction zone itself, and at the level of the stripper whose purpose is to eliminate as much as possible the fraction of gaseous effluents entrained with the catalyst stream as well as that adsorbed on the surface of the catalyst particles.
• the invention describes a compartmentalised fluidized reactor of large diameter (from 6m to 25m) and low H / D ratio ( ⁇ 0.5).
• Radial walls define several compartments in the reactor, each compartment representing an angular sector of the reactor.
• the compartments may or may not be identical in size. The multiplication of these compartments makes it possible to maintain a high degree of mixing of the solid in each compartment.
• the reactor according to the invention is therefore well suited to carrying out catalytic cracking reactions on light, olefinic and / or paraffinic fillers, in the range of carbon numbers ranging from 5 to 12, in order to produce large scale intermediates.
• the catalyst In this type of cracking, the catalyst must be regenerated in a unit carrying out the combustion of the adsorbed coke which has formed during the reaction phase, as in any catalytic cracking unit, even if, given the range of the charges concerned, the coke formation potential is low, coke formation is significantly less than in an FCC unit working on a conventional vacuum or atmospheric residue distillate charge.
• the catalyst before being regenerated, undergoes a stripping step in order to desorb the adsorbed hydrocarbons on the surface of the catalyst.
• the stripping enclosure is an integral part of the reactor and is in the center in the form of a central cylindrical chamber.
• This central cylindrical chamber is generally provided with a packing (called “packing” in the English terminology) or any other element that promotes the contact between the gas phase and the dispersed solid phase.
• reaction compartments are attached (generally by welding, but any other means known to those skilled in the art remains within the scope of the present invention) to the enclosure of the stripper to overcome thermal expansion.
• the different compartments of the reactor operate in parallel.
• each reaction compartment feeds each reaction compartment through a pipe, each pipe being provided with a valve for regulating the catalyst flow (as shown in Figures 1, 2 and 3).
• the residence time of the catalyst is the same in both configurations:
• the difference between the serial operation mode and the parallel operation mode is that, in the case of the series compartments, the catalyst is increasingly coked advancing from one compartment to another. It is therefore more advantageous to distribute the load flow regressively in the different compartments. Regressive distribution is understood to mean a decrease in the feed rate as a function of the coke content of the catalyst, a content that increases when moving from one compartment to the next.
• the vaporized charge is injected via a gas distributor at the bottom of the reactor, in order to fluidize the different compartments and convert the charge into contact with the catalyst.
• the introduction of the catalyst is substantially above the charge injectors of a given compartment so as to avoid any formation of a fixed bed below the level of injection of the charge.
• each compartment allows overflow to the central stripping enclosure by increasing the level of the bed in each compartment.
• reaction compartments operate in series, then the overflow to the stripping chamber is from the last compartment of the series.
• each reaction compartment operates with a triplet temperature / residence time / gas / solid contact time which allows the maintenance of a certain reaction efficiency.
• the catalyst may be any type of catalyst, preferably containing a high proportion of zeolite Y and / or zeolite ZSM-5. It may even be composed of 100% zeolite ZSM-5.
• the present example provides the design of a reactor-stripper according to the invention for treating a straight run gasoline load (so-called "straight run") having a distillation range between 30 and "l OO, in order to produce in propylene priority
• the charge from C5 to C9 is a paraffinic feed having the composition given in Table 1 below:
• P stands for paraffins
• IP stands for isoparaffins or branched paraffins
• O stands for olefins
• N stands for naphthenes
• A stands for aromatics.
• the feedstock does not contain olefins, but in some cases it is quite possible that it contains up to 40%.
• Table 2 shows the yields of ethylene, propylene and BTX obtained 6 ' ⁇ 0 C for contact times from 1 00 ms, 600 ms, 1600 ms and 4000 ms following an experiment in small pilot.
• the ethylene and BTX yields continue to increase at least up to 4000ms.
• the contact time of 1.6 seconds is obtained in a compartmentalised turbulent fluidized bed reactor dimensioned as follows:
• the feedstock is injected with steam (20% by mass of steam with respect to the feedstock).
• Reactor diameter D 15 meters
• Reactor height H 4 meters
• Diameter of the central stripper 3 meters
• the ratio H / D (height to diameter) of the reactor is 0.27.
• Fluidisation speed in the central stripper 20 cm / s (solid flow of 50 kg / m 2 / s)
• Fluidisation velocity in compartment 2 1, 1 m / s at the top
• Fluidisation velocity in compartment 4 0.9 m / s at the top.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

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• 2016
  • 2016-12-15 FR FR1662537A patent/FR3060415B1/fr not_active Expired - Fee Related
• 2017
  • 2017-12-08 EP EP17808961.1A patent/EP3554680A1/de not_active Withdrawn
  • 2017-12-08 WO PCT/EP2017/082087 patent/WO2018108751A1/fr not_active Ceased
  • 2017-12-08 CN CN201780077708.9A patent/CN110290861B/zh active Active
  • 2017-12-08 US US16/469,750 patent/US20190314781A1/en not_active Abandoned
• 2019
  • 2019-05-28 SA SA519401880A patent/SA519401880B1/ar unknown

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