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
  • 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
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
  • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

• the present invention relates to a process and a device for the catalytic cracking of hydrocarbon charges
• the yields that are generally obtained naturally depend on the quality of the loads treated Typically, as an indication, the yields observed (in% weight of the load) on the units are dry gas 1-5%
• the coke formed is burned in one or more enclosures called regenerators towards which the catalyst circulates on leaving the reactor.
• regenerators towards which the catalyst circulates on leaving the reactor.
• the heat produced by the combustion of the coke makes it possible to heat the catalyst which is then reintroduced at the inlet of the reactor and brought into operation.
• the catalytic cracking process is an adiabatic process
• the heat recovered by the catalyst during its passage through the regeneration zone is equal to the heat lost by the catalyst during its passage through the reaction zone This therefore requires the operator of operating conditions which are not independent of each other
• the operating conditions which most affect the yields and selectivities for a given reactor are essentially the flow rate of catalyst, which is generally referred to the feed rate under the designation C / O ( C for Catalyst and O for O ⁇ l)
• the reaction zones generally used in the majority of current catalytic cracking units make it easy to operate under mild cracking conditions (C / O from 4 to 8 and temperatures at the reactor outlet from 500 to 550 ° C).
• the residence time of the hydrocarbons in this reaction zone consisting at least of a tube of substantially circular section and of elongated shape in which the fluids generally flow from the bottom to the top commonly called ⁇ ser, and a separation system cracked vapors and of the catalyst is generally greater than 2 s, of the order of approximately 2 to 10 s
• the residence time of the hydrocarbons in contact with the catalyst is often itself greater than 1 s
• the essential advantage of this type of device is to be able to bring the catalyst into contact with the charge in an optimal manner thanks to the initial use of a descending reactor.
• the coke deposited on the catalyst tends to significantly deactivate the catalyst, all the more so since there is coke deposited typically, in conventional bottom-up reactors, the amount of coke present on the catalyst varies between 0.7 and 1 0.5% by weight, depending on the charge treated, the catalyst, the operating conditions and the size of the unit. It is known that under these conditions, the residual activity of the catalyst is low.
• the catalyst from the descending reactor can advantageously be again introduced into a reaction vessel such as a ⁇ ser, optionally mixed with a regenerated catalyst stream (that is to say directly from the vessel) It is therefore clear that these results make it possible to consider serenely a sequence of reaction zones first descending, then ascending where the catalyst from the descending reaction zone would be completely reintroduced at the inlet of the ascending reactor
• the object of the present invention is to remedy these shortcomings of the prior art by proposing a sequence of distinct reaction zones which can operate under very different temperature and C / O conditions. More specifically, the invention relates to a method of catalytic cracking composed of a reaction zone having at least two reactors, with in at least one of these reactors a flow of fluids and catalyst globally descending (reactor droppeur) and in at least one of these reactors a flow of fluid and catalyst generally ascending (reactor nser), these reactors being characterized in that in each reactor, hydrocarbons introduced into the reactor are in contact with hot catalyst which allows the vaporization of these hydrocarbons if they are introduced in liquid form, these vaporized hydrocarbons then reacting in the presence of the catalyst, these reacted hydrocarbons are then separated from the catalyst by separation means (inert separators and / or cyclones) and leave the reaction zone to undergo the usual downstream treatments (fractionation,)
• the reactors are also characterized by the fact that the descending reactor (s) are followed
• the invention relates to a process of catalytic cracking in ht entrained or fluidized of a hydrocarbon feed in two reaction zones, one with downward flow of catalyst, the other with upward flow of catalyst, the process being characterized in that a charge and catalyst from at least one regeneration zone are introduced into the upper part of the downflow zone, the charge and the catalyst are circulated in said zone according to a weight ratio of catalyst to charge C / O 5 to 20, the cracked gases are separated from the coke catalyst originating from the downflow zone in a first separation zone, the cracked gases are recovered, the coke catalyst is introduced into the lower part of the upward flow zone , a charge is introduced into the lower part of said upward flow zone, the coke catalyst is circulated therein and said charge lon a weight ratio C / O 4 to 8, the spent catalyst is separated from the effluent produced in a second separation zone, the catalyst is stnped by means of a stripping gas in a stripping zone, the effluent and stripping gases and the spent catalyst is
• the residence times of the charge in the dropper and the nser are respectively generally from 50 to 650 ms in the dropper and from 600 to 3000 ms in the nser and preferably 100 to 500 ms in the dropper and 1000 to 2500 ms in the nser
• the residence time is defined as the ratio of the volume of each of the reaction chambers (nser or dropper), related to the volume flow rate of the gaseous effluents from each chamber under the outlet conditions
• the spent catalyst can be regenerated in two superimposed regeneration zones, the spent catalyst to be regenerated is introduced into a first lower regeneration zone, the catalyst thus at least partly regenerated being sent to the second upper regeneration zone and the regenerated catalyst coming from the upper regeneration zone is introduced into the downflow zone
• the catalyst to oil ratio (C / O) can advantageously be between 7 and 15 for the downflow reactor and between 5 and 7 for the upward flow reactor
• the temperature of the catalyst leaving the dropper is generally higher than that leaving the nser It can be from 500 ° C to 700 ° C and advantageously from 550 "C to 600 ° C while that that of the catalyst at the outlet of nser can be from 500 ° C. to 550 ° C. and advantageously from 515 ° C. to 530 ° C. These temperatures are closely dependent on the values of the respective ratios of C / O, the C / O ratio of the dropper being higher than that of the nser
• the feed supplying each of the reactors can be either a fresh feed, or a recycling of part of the products resulting from a fractionation downstream, or a mixture of the two
• a fresh charge can be introduced into the ascending reactor and said recycle at least partially in the descending reactor
• the charge can be injected cocurrently or countercurrently into each of the two reactors.
• the charge flow rate, for example of recycle, in the descending reactor can represent less than 50% by mass of the charge flow rate to be converted circulating in the ascending reactor
• the invention also relates to the device for the implementation of method II generally comprises a first substantially vertical descending reactor having an upper inlet and a lower outlet, a first means for supplying regenerated catalyst connected to at least one regenerator for spent catalyst connected to said upper inlet, a first means for supplying the atomized charge disposed below the first catalyst supply means, a first enclosure for separating the catalyst from a gas phase connected to the lower outlet of the first descending reactor having an outlet from the gas phase and an outlet for coke catalyst, a second substantially vertical ascending reactor having a lower inlet and an upper outlet, a second catalyst supply means being connected to the outlet for coke catalyst first separation enclosure and at the lower entrance to the second reactor, a second means for supplying a charge located above the lower inlet of the second reactor, a second enclosure for separating spent catalyst and a second gaseous phase connected to said upper outlet of the second reactor, said second enclosure comprising a catalyst stripping chamber and having an upper outlet of a gas phase and a lower outlet of spent catalyst, said lower outlet being connected
• FIG. 1 shows a schematic description of the process, the flow of the catalyst being in solid line while that of the hydrocarbons is in dotted lines.
• FIG. 2 schematically illustrates a device comprising a dropper, an intermediate separator and an nser Figure 1 attached is a representation of the process under these conditions
• the catalyst regenerated in a regeneration zone (3) is transported to the inlet d '' a globally descending reactor by transfer means (4), withdrawn from the descending reactor by transport means (5) and introduced into an ascending reactor (2), then, having traversed the ascending reactor, is transported by a line ( 7) to the regeneration zone (3)
• the ascending reactor can also be supplied with freshly regenerated catalyst by means (6) of transporting the catalyst from the regeneration zone to the bottom of the ascending reactor (2)
• the charge supplying each of the reactors can either be a fresh load (line (8) for the descending reactor, line (9) for the ascending reactor), or a recycle of part of the products from the downstream fractionation (line (16) for the descending reactor, line (14) for the ascending reactor), i.e.
• FIG. 2 describes a possible arrangement of the various constituents of the process which is the subject of the invention It is indeed necessary, for the catalyst to circulate correctly between the different enclosures, that the pressures of each of the enclosures are compatible with the rates of circulation of catalyst and of hydrocarbons desired in each of the enclosures
• the regeneration zone (3) consists of two enclosures (301) and (302) in which the catalyst is regenerated in fluidized ht, air being introduced into each enclosure .
• the catalyst is transported between the two enclosures by means of a lift (303), in which gas introduced to the base at a sufficient speed makes it possible to transport the catalyst between the two enclosures
• This transport gas can be air
• the proportion of air required for regeneration is 30 to 70% in the enclosure (301), 5 to 20% in the lift (303) in order to transport the catalyst and 15 to 40% in the enclosure (302)
• Means (304), such as a valve on solid of the “plug valve” type, make it possible to control the flow rate of circulation between the chambers (301) and (302)
• the combustion gaseous effluents are dusted off through a passage through separators (such as cyclones, shown HERE schematically (306 and 307)
• the pressure in each enclosure (301) and (302) can be controlled by valves located on the lines allowing the evacuation of combustion effluents stion, at least partially dusted
• FIG. 2 a sequence of two reaction zones has been shown, one being downward (1), the other downstream being upward (2)
• all the catalyst circulating in the reactor (2) also circulating in the reactor (1) Nevertheless, it is in certain cases interesting to mix, at the inlet of the nser (2), the catalyst resulting from (1) with catalyst coming directly from l regeneration enclosure (3)
• FIG. 2 a sequence of two reaction zones has been shown, one being downward (1), the other downstream being upward (2)
• all the catalyst circulating in the reactor (2) also circulating in the reactor (1) Nevertheless, it is in certain cases interesting to mix, at the inlet of the nser (2), the catalyst resulting from (1) with catalyst coming directly from l regeneration enclosure (3)
• FIG. 2 shows how it is possible to transfer catalyst from a regeneration enclosure (302) to the reactor (1)
• the catalyst is withdrawn from the wall through a line inclined (304) at an angle generally between 30 and 70 ° relative to the horizontal leading the catalyst to an enclosure (305) in which the circulation of the catalyst is slowed down to allow possible bubbles of gas to the e regeneration enclosure through a balancing line (308).
• the catalyst is then accelerated and descends through a transfer tube (309) to the inlet of the reactor.
• the catalyst Throughout its journey from the regeneration enclosure, the catalyst is maintained in the fluidized state by the addition of small quantities of gas throughout the transport If the catalyst is thus kept in the fluid state, this makes it possible to obtain at the inlet of the reaction zone (1) a pressure higher than that of the fumes from the external cyclones (307 ).
• the reaction zone (1) defined as descending generally consists of means for introducing the catalyst (101), which can be a valve on solid, an orifice, or simply the opening of a conduit, of a contacting zone (103) located under (101) where the catalyst meets against the current for example the hydrocarbon charge, introduced by means (102), generally consisting of atomizers where the charge is finely divided into droplets generally using the introduction of auxiliary fluids such as steam
• the means for introducing the catalyst are located above the means for introducing the charge.
• a reaction zone (104) of substantially elongated shape, shown vertically in FIG. 2 but this condition is not exclusive.
• the average residence time of the hydrocarbons in zones 103 to 104 will be less than 650 ms, preferably ely between 50 and 500ms.
• the effluent from the dropper is then separated in a separator (105) described in application FR98 / 09672 incorporated as a reference where the residence time must be limited as much as possible
• the gaseous effluents (cracked gases) from the separator can then undergo an additional dusting step through external cyclones (108) arranged downstream on a line (106)
• the gaseous effluents (cracked gases) are evacuated by a line (107) It is also possible to cool the gaseous effluents, in order to limit the thermal degradation of the products, for example by injecting liquid hydrocarbons into the effluent leaving the cyclones (108) via the line (107)
• the catalyst separated in the separator (105) is then either reinjected directly at the base of a ascending reactor (201) through a conduit (110), as shown in Figure
• the reaction zone (2) is a substantially elongated tubular zone, many examples of which are described in the prior art.
• the hydrocarbon charge is introduced by means (202), generally consisting atomizers where the charge is finely divided into droplets, generally using the introduction of auxiliary fluids such as water vapor, introduced at the base of the reactor.
• Means for introducing the catalyst are located below the means for introducing the charge.
• the introduction of the charge must be located above at least one catalyst inlet In the case of FIG.
• the catalyst resulting from the separation (203) is then introduced into a fluidized ht (211 ) d a stripping chamber (212) through conduits or openings (204)
• the catalyst in (211) then undergoes stripping (contact with a light gas such as water vapor, nitrogen, ammonia, hydrogen or even hydrocarbons, the number of carbon atoms of which is less than 3 by means which are well described in the prior art) before being transferred to the regeneration zone (301) through conduits ( 7)
• the reaction gaseous effluents separated in (203) are discharged through a pipe (205) to a secondary separator (207) such as a cyclone before being sent to the fractionation section (10) by a pipe (206 )
• the stripping gaseous effluents are generally evacuated from the fluidized ht (211) through the same means (206) which allow the evacuation of gaseous effluents from the reaction zone (2)
• the coke catalyst is withdrawn from the stripping chamber (212) and recycled in the first regeneration enclosure (301), located under the regeneration enclosure 302
• REG1 first regeneration enclosure
• REG2 second regeneration enclosure
• CUFCC total fresh charge at the entrance to the FCC unit.
• the properties of the hydrocarbon feedstock considered are:

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

Applications Claiming Priority (3)

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• 1998
  • 1998-11-13 FR FR9814319A patent/FR2785907B1/fr not_active Expired - Lifetime
• 1999
  • 1999-11-12 JP JP2000582495A patent/JP2002530467A/ja active Pending
  • 1999-11-12 ES ES99972244T patent/ES2226502T3/es not_active Expired - Lifetime
  • 1999-11-12 AT AT99972244T patent/ATE271114T1/de not_active IP Right Cessation
  • 1999-11-12 DE DE69918710T patent/DE69918710T2/de not_active Expired - Lifetime
  • 1999-11-12 WO PCT/FR1999/002801 patent/WO2000029508A1/fr active IP Right Grant
  • 1999-11-12 KR KR1020017005947A patent/KR100607922B1/ko active IP Right Grant
  • 1999-11-12 US US09/831,659 patent/US6641715B1/en not_active Expired - Lifetime
  • 1999-11-12 EP EP99972244A patent/EP1131389B1/de not_active Expired - Lifetime

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