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

Definitions

• the present invention relates to a process and a device for catalytic cracking of a hydrocarbon charge in a descending bed, using an improved zone of contact between the charge and the catalyst.
• the downer has, in particular, a drawback linked to the initial mixture between catalyst and charge: in fact, the catalyst tends to fall immediately without reflux or recirculation, which has a negative effect on the initial transfer of mass and heat with the charge. If the catalyst and feed inlet flows were perfectly regular, this effect would be minor. However, this is not the case, and that is why, in a cracking reactor, the solid-gas mixture consists of alternating zones rich in catalyst, then poor in catalyst.
• US Pat. No. 5,468,369 proposes a device in which the charge is sprayed, brought into contact with the catalyst and then partially cracked according to an upward flow. Then, the direction of the flow is reversed and the cracking is completed in a downward flow.
• this device appears difficult to achieve on a mechanical level and it does not allow a very efficient mixing in the case of large catalyst flows.
• the catalyst tends to agglomerate in the vicinity of the walls of the device and is therefore isolated from the vaporized charge.
• the object of the invention is therefore to reconcile the advantages of the upward flow, namely a satisfactory mixture between large feed and catalyst flow rates, and of the downward flow, namely a good selectivity of the cracking reactions proper.
• the present invention therefore relates to a process for catalytic cracking of hydrocarbons, comprising a phase of contacting the hydrocarbons and particles of a catalyst, a cracking reaction phase in a descending bed, a phase of separation of the deactivated catalyst. and effluent hydrocarbons, at least one phase of stripping of the deactivated catalyst, then a phase of regeneration of said catalyst under conditions of combustion of the coke carried by the catalyst and, finally, a phase of recycling of the regenerated catalyst in the supply zone.
• this process being characterized in that a substantial part of the hydrocarbons is pulverized and brought into contact with the catalyst in a specific contacting zone which consists of - a mixing chamber of maximum section S 2 , fed in its part upper in hot regenerated catalyst by an upper orifice defining a passage section of the catalyst Si, and a reaction zone with downward flow in which the solid gas mixture coming from the mixing chamber is poured by an intermediate orifice of section S 3 located at the lower part of said chamber, and in that the ratios Sj Sx and S 2 / ⁇ 3 have values between 1.5 and 8 and, preferably, between 2.5 and 6.
• the contacting zone according to the invention makes it possible to achieve the above-mentioned objectives. Its geometry is particularly applicable to short time insofar as it allows complete and rapid vaporization of the load.
• S ⁇ / S 3 between the section SI for passage of the catalyst through the annular orifice and the section S 3 of the intermediate orifice is between 0.8 and 1.25 and, preferably, between 0.9 and 1, 1, to allow optimal mixing within the mixing chamber.
• the hydrocarbons are injected against the current of the downward flow of catalyst particles, at an angle to the horizontal, between 2 ° and 45 °, and preferably between 5 and 35 °. In this way, the mixture between the feed and the catalyst is optimized, because this direction of injection allows the feed to break the mass of descending catalyst as well as possible.
• reaction zone flares out from the intermediate orifice at an angle with the vertical between
• the ratio S 4 / S 3 between the maximum section S 4 of the reaction zone and the section S 3 of the intermediate orifice has a value between 1.5 and 8 and, preferably, between 2, 5 and 6.
• the ratio S 2 / S 4 between the maximum section S 2 of the mixing chamber and the maximum section S 4 of the reaction zone is between 0.8 and 1 , 25 and, preferably, between 0.9 and 1.1
• the invention also relates to a device allowing the implementation of the method explained above.
• the subject of the present invention is a device for catalytic cracking of hydrocarbons, comprising a downflow cracking reactor, means for supplying said reactor under pressure with a charge of hydrocarbons and particles of a catalyst of regenerated cracking, a means for separating the products from the cracked charge and particles of deactivated catalyst, at least one means of stripping by at least one fluid of the deactivated catalyst particles, at least one unit for regenerating said catalyst by combustion of coke carried by the catalyst, and means for recycling the regenerated catalyst to said supply means, this device being characterized in that it comprises a specific contacting zone between the hydrocarbons and the catalyst, consisting
• FIG. 1 is a schematic view of a conversion assembly according to the invention.
• FIG. 2 is a more detailed view of the zone according to the invention of contact between the charge and the catalyst.
• the device shown comprises a tubular reactor 1 with downward flow, or “downer”, supplied at its upper part, from an enclosure 2, which is coaxial with it, in particles of regenerated catalyst.
• a valve 3 intended to regulate the ratio of the mass of catalyst to the mass of feedstock to be treated in the reactor, is interposed between the reactor 1 and the enclosure 2. Below this valve opens a supply line 4 of reactor 1 with the load of hydrocarbons to be treated, preheated in a manner known per se.
• This charge is sprayed into fine droplets, by injectors, at the top of the contacting zone 5, in order to mix with the catalyst particles, in contact with which the cracking reaction takes place.
• the direction of the injection of the charge, as well as the geometry of the contacting zone, will be detailed below.
• the catalyst particles and the charge to be treated therefore flow from top to bottom in the reactor 1.
• the spent catalyst particles pour into a stripping chamber 6, provided at its base with a diffuser 7, supplied with water vapor by a line 8.
• line 9 through which the cracked products and the hydrocarbons coming from the stripping are evacuated to a separation column 10.
• the gases evacuated by line 9 can optionally be quenched by a hydrocarbon or steam, introduced by a line 11 into line 9.
• the stripped catalyst particles are evacuated by gravity from the enclosure 6, through an inclined conduit 22, to an ascending column 12, in which they are conveyed upwards, to a regenerator 13, using a carrier gas. , disseminated at 14 at the base of column 12, starting from line 15.
• the column 12 opens into the regenerator 13 below a ballistic separator 16, which ensures the separation of the catalyst particles and the carrier gas.
• the catalyst particles are then regenerated, in a manner known per se, in the regenerator, by combustion of the coke which has deposited on their surface and of the remaining hydrocarbons, using a stream of air or oxygen. brought by line 17 to diffuser 18.
• the regenerated catalyst particles are removed by gravity through the pipe 19 in the direction of the enclosure 2, without thermal losses.
• the gases coming from the combustion are evacuated towards cyclones 23, which separate the fines, recycled by the conduit 20 towards the regenerator, and the gases, evacuated by the line 21.
• FIG. 2 shows more precisely the contacting zone 5 which is the subject of the invention.
• the contacting zone 5 is formed by a mixing chamber 24 and a reaction zone 25 disposed immediately below the latter.
• the mixing chamber 24 is supplied at its upper part with hot regenerated catalyst through the cylindrical conduit 26, of section S c , which is in communication with the enclosure 2 described in FIG. 1 (but not shown in FIG. 2) .
• a bulkhead 28, known per se, is disposed at the lower end of the conduit 26, thereby defining an upper annular orifice 30 of the mixing chamber 24, through which the catalyst pours into it. This orifice 30 thus delimits a section Sx for passage of the catalyst, which is less than the section S c of the conduit 26.
• the mixing chamber 24 widens from its upper orifice 30 along a frustoconical portion 32 of angle at the apex A, until it reaches its maximum cross section
• the angle A for example equal to 40 °, can be between 10 and 60 °, while the section S 2 is for example equal to 5 Sx, but can be between 1.5 and 8 S -
• the periphery 34 of the mixing chamber 24, at the maximum section of the latter, is provided with a series of injectors 36, making it possible to inject the charge after atomization of the latter outside the device.
• the injectors 36 are oriented so as to direct the charge droplets against the current of the descending flow of catalyst particles, at an angle B relative to the horizontal equal for example to 15 °, but which can be between 2 ° and 45 °.
• the number of injectors will be such that the entire descending catalyst can be reached by the droplets of the charge.
• the mixing chamber 24 then narrows from its maximum section S 2 along a frustoconical portion 38, until it reaches its lower end of cross section S 3 .
• the tapered portion 38 has an apex angle C, which is for example equal to 30 °, but may be between 10 and 50 °, while the section S 3 is for example equal to S 2/4, but can be understood between 2 S 2/3 and S 2/8.
• This mixing chamber which consists of two cone portions 32, 38 which widens and then narrows, is shaped so that there is a flow of perfectly agitated type, allowing the reflux and recirculation of catalyst necessary for a good mixing of the latter with the vaporized charge.
• reaction zone 25 Downstream of the mixing chamber 24, in the direction of flow of the charge, extends the reaction zone 25, which is in communication with the mixing chamber through the lower end of the latter, which constitutes an orifice intermediate 40 of section S 3 .
• reaction zone 25 widens from the intermediate orifice in a frustoconical portion 42 of angle at the apex D, until it reaches its maximum cross section.
• the angle D is for example equal to 6 °, but can be between 1 and 15 °, while the section S 4 is for example equal to 5 S 3 , but can be between 1.5 and 8 S 3 .
• the reaction zone Downstream of this frustoconical portion 42, in the direction of flow of the charge, the reaction zone is constituted by a cylindrical extension 44 and has a substantially constant section, close to S, so as to best preserve the flow of the type piston which was established during the passage of the load in the frustoconical section 42.
• the present description only refers to the dimensional relationships existing between the different parts of the contacting area object of the invention. Those skilled in the art will dimension the whole of this zone as a function of the respective flow rates of feed and catalyst and of the adequate residence time of the feed in the mixing chamber and in the reaction zone.
• the section S x of passage of the catalyst through the upper orifice 30, and the section S 3 of the intermediate orifice 40 are for example equal to 65 c 2, but can be between 10 and 500 cm- *.
• the maximum cross section S 2 of the mixing chamber 24 and the maximum cross section S of the reaction zone 25 are for example equal to 300 cm 2, but can be between
• the present description refers to a contacting zone which consists of a series of surfaces of revolution, namely cylindrical or frustoconical portions whose cross section is circular.
• the present invention also relates to any contacting zone for which there are certain relationships between the sections of its constituent elements, whether these sections are of polygonal, ovoid or any shape.
• the contact zone according to the invention finds its application to any catalytic cracking device the reactor of which has a downward flow of charge, whatever in particular the stripping and regeneration means of the deactivated catalyst.
• An oil charge has the following properties:
• This charge is introduced into an upward-flow catalytic cracker under the following operating conditions:
• the process according to the invention therefore makes it possible to increase the selectivity of cracking by allowing a higher catalyst / charge mass ratio than in the prior art (and therefore a lower ⁇ coke, that is to say a lower difference between the quantities of coke present on the catalyst at the inlet to and from the regeneration zone).
• the process according to the invention also makes it possible, when a given conversion is aimed at, to treat more difficult charges, in particular denser charges and whose percentage of Conradson carbon residue is higher.

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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)

Publications (2)

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Family Applications (1)

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Family Cites Families (5)

• 1996
  • 1996-09-18 FR FR9611369A patent/FR2753453B1/fr not_active Expired - Fee Related
• 1997
  • 1997-09-16 ES ES97919102T patent/ES2224238T3/es not_active Expired - Lifetime
  • 1997-09-16 US US09/068,500 patent/US5997726A/en not_active Expired - Lifetime
  • 1997-09-16 CN CN97191272A patent/CN1125867C/zh not_active Expired - Lifetime
  • 1997-09-16 DE DE69729785T patent/DE69729785T2/de not_active Expired - Lifetime
  • 1997-09-16 EP EP97919102A patent/EP0874880B1/de not_active Expired - Lifetime
  • 1997-09-16 ID IDW980007A patent/ID20024A/id unknown
  • 1997-09-16 ZA ZA9708333A patent/ZA978333B/xx unknown
  • 1997-09-16 CA CA002236839A patent/CA2236839C/fr not_active Expired - Lifetime
  • 1997-09-16 WO PCT/FR1997/001627 patent/WO1998012279A1/fr active IP Right Grant
  • 1997-09-16 AT AT97919102T patent/ATE270700T1/de not_active IP Right Cessation
  • 1997-09-16 JP JP51434098A patent/JP3955332B2/ja not_active Expired - Lifetime
  • 1997-09-16 KR KR10-1998-0703555A patent/KR100493978B1/ko not_active IP Right Cessation
  • 1997-09-18 AR ARP970104274A patent/AR008431A1/es unknown
  • 1997-10-23 TW TW086113666A patent/TW366359B/zh not_active IP Right Cessation

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