EP0861310A1 - Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne - Google Patents
Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionneInfo
- Publication number
- EP0861310A1 EP0861310A1 EP97919105A EP97919105A EP0861310A1 EP 0861310 A1 EP0861310 A1 EP 0861310A1 EP 97919105 A EP97919105 A EP 97919105A EP 97919105 A EP97919105 A EP 97919105A EP 0861310 A1 EP0861310 A1 EP 0861310A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- zone
- charge
- injection
- flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- C10G11/187—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
Definitions
- the invention relates to a process for catalytic cracking in a fluid bed (FCC) of a hydrocarbon feedstock in a reaction zone where the feedstock circulates from top to bottom (in English dropper).
- FCC fluid bed
- the major problem associated with this type of reactor relates to the intimate contact between the hot regenerated catalyst and the hydrocarbon feedstock.
- US Pat. No. 4,919,898 describes the formation of a curtain falling from the catalyst from rectangular openings coming from a bed pressurized by steam. This bed therefore regulates the pressure difference between the enclosure containing the pressurized bed and a chamber for mixing the catalyst and the charge downstream of the bed. This patent further describes the injection of the charge in the direction of the valve forming the curtain.
- US Patent 5,296,131 further describes a downwardly flowing catalyst curtain of annular shape.
- the charge is injected downward at least in part through a radial opening under the seat of a valve type valve of frustoconical shape, pressed against the upper part of the reactor.
- patent application EP-A-0 209 442 which describes the presence of a valve downstream of a first fluidization ring which disturbs the fluidization conditions until a defiuidization leading to obtaining a density corresponding to a bulk bed.
- the object of the invention is to remedy the drawbacks of the prior art.
- the invention relates to a process for catalytic cracking in a fluidized bed of an oil charge with lighter effluents in a catalytic cracking zone comprising a reaction or droppers zone into which is introduced, at an upper end called zone d injection of the regenerated catalyst from at least one regeneration zone, the catalyst is shaped by means of a shaping member having a restriction, the catalyst is brought into contact with the charge, a mixture flowing downward of catalyst and charge, and at least the majority of the charge is vaporized in said injection zone, said charge is cracked to obtain the lighter effluents, the effluents are separated from the spent catalyst in a separation zone at the lower end, the effluents are recovered and the spent catalyst is recycled in the regeneration zone, the process being characterized in that the regenerated catalyst from the regeneration zone is made to flow into a zone for conditioning the catalyst in a dense fluidized bed upstream of the injection zone comprising a gas disengagement zone, the speed of fluidization by a fluidizing gas being between 0.1 and 30
- the flow of catalyst flowing by gravity through the restriction with variable or constant passage cross section is, as a general rule, between 200 and 20,000 kg / m.s and preferably between 1,000 and 10,000 kg / m 2 . s, an excellent range of values between 4,000 and 6,000 kg / m 2 .s.
- the charge can be injected by a plurality of injectors arranged all around the wall of the injection zone at an angle less than or equal to 30 degrees relative to the horizontal and preferably at an angle of 5 to 25 degrees.
- the injection angle ⁇ is determined so that the result of the vectors taking into account the momentum of the charge and the momentum of the catalyst is substantially horizontal, for example at more or less ten degrees around the horizontal.
- the mass ratio of catalyst to charge in the injection zone can be between 5 and 20, preferably between 10 and 18.
- the speed of the catalyst flowing by gravity through the restriction can be from 0.1 to 20 m / s and advantageously from 0.5 to 5 m / s, while the speed of the atomized charge droplets is usually between 50 and 100 m / s and preferably 70 to 90 m / s.
- a catalyst curtain can be produced, for example, in two ways
- a member for shaping said curtain comprising a fixed part attached to the wall of the injection zone and integral with it and a central movable part cooperating with the fixed part to create said restriction having a variable catalyst passage section. Regulation of the flow of catalyst in the injection zone for a determined flow rate can then be achieved by varying the passage section between said fixed part and said movable part of said catalyst shaping member.
- This adjustable regulation mode is particularly advantageous when starting the unit, which includes a transient regime.
- the catalyst curtain can be produced by a shaping member comprising a central fixed part cooperating with the wall of the injection zone or with a fixed part attached to said wall.
- the central part, fixed or mobile determines with the usually cylindrical wall a restriction of cross-section of passage of the catalyst constant or variable as the case may be and preferably annular.
- the fixed or mobile central part could be of cylindrical, spherical or ovoid shape.
- Such catalyst shaping members are described in the applicant's patent (FR 2631857) incorporated by reference, which also teaches charge injection perpendicular to the direction of flow of the catalyst.
- the catalyst can pass through a restriction on said shaping member, having a substantially constant passage section but of circular shape.
- the catalyst flow rate can be adjusted in the injection zone, by means of a variable opening valve which can be that according to the first variant, or a variable opening valve arranged on the line for introducing the regenerated and hot catalyst. from the regenerator to the packaging area. This valve is also slaved to a temperature probe at the outlet of the droppers.
- the catalyst conditioning zone can include a zone for disengaging the catalyst gas above the level of the dense fluidized bed, with a height between one third and half of the total height of the conditioning zone.
- the pressures in the conditioning zone and in the regeneration zone can be balanced by means of a pressure equalization line connecting the disengagement zone to the upper part of the regeneration zone. Under these conditions, the heights of the dense fluidized beds in the conditioning zone and in the regeneration zone are substantially at the same level.
- the injection chamber of the reaction zone is generally dimensioned to receive a given mass of catalyst such that the residence time in this zone is usually between 0.02 s and 0.5 s and preferably between 0.03 s and 0.1 s.
- the catalyst can be one of those known to those skilled in the art, for example those cited in US Patent 5,296,131.
- the member for introducing the hydrocarbon charge can be any member well known to those skilled in the art allowing the introduction of a hydrocarbon charge, preferably in the form of droplets preferably having a mean diameter. less than 5x10 " 4 meter (m) and advantageously less than 1x10" 4 (m). It is preferable that the hydrocarbon charge is introduced so as to form fine droplets distributed homogeneously at the level of the introduction zone.
- An auxiliary fluid called atomization promoting the production of fine droplets can also be introduced with the hydrocarbon charge.
- This auxiliary fluid will usually be a gas such as steam, or a gas relatively rich in hydrogen or hydrogenated compounds from other units of the refinery.
- the atomization is generally carried out outside the reaction zone.
- Conventional type injectors usually open at their ends inside the injection area.
- the jet of charge droplets of dimension substantially equal to that of the particles and under an injection angle according to the invention, breaks the falling curtain or the falling vein of catalyst.
- injectors are usually arranged at the periphery of the injection zone, under the catalyst shaping member and their end is located in at least one plane substantially perpendicular to the axis of the injection zone or of the dropper. .
- the distance of these injectors, counted from the theoretical impact points of the charge jets on the axis of the injection zone (or of the reaction zone), at the point the lower of the catalyst forming member is at most equal to 2 times the diameter of the injection zone.
- this distance can be 0.5 to 1 times the diameter of the injection zone.
- the invention also relates to a catalytic cracking unit with a falling reactor or a dropper for catalytically cracking a hydrocarbon feedstock in the presence of a cracking catalyst and for producing an effluent of light products and of the coke cracking catalyst.
- the unit comprises a member having a restriction for the shaping of the catalyst upstream of the dropper, a feed of charge communicating with an injection chamber at the top of the dropper and bringing the load into contact with the shaped catalyst , an enclosure for separating the effluents from the coke catalyst at the bottom of the dropper and at least one enclosure for regenerating the coke catalyst communicating with the separation enclosure and a line for supplying regenerated catalyst connecting the regeneration enclosure to the catalyst shaping member, said unit being characterized in that it comprises a chamber for conditioning the regenerated catalyst in a dense fluidized bed connected between the regenerator and the catalyst shaping member, said enclosure comprising means fluidization and having a disengagement zone of the gas catalyst, of volume suitable for the upper part ieure of said enclosure, which communicates by a pressure equalization line with the upper part of the regeneration enclosure, and in that the charge injection chamber comprises a plurality of injectors connected to the line supply of charge and introducing the charge against the flow of the catalyst, below the catalyst shaping member, towards the axis of said
- a device 1 for catalytic cracking in a driven fluidized bed known per se essentially comprises a dropper (descending reactor) 13 supplied in its upper part with catalyst conditioned in a conditioning enclosure 2.
- This enclosure is supplied with catalyst by an oblique line 3, coming from a regeneration zone which in the specific case contains two superimposed regenerators 4 and 17 in a fluidized bed.
- the dropper is fed in its upper part by a charge introduced by injectors 12 and vaporized in contact with the hot regenerated catalyst (approximately 780 ° C.).
- the effluents are separated from the catalyst in a stripper 14 known per se, evacuated by a line 15 while the catalyst once stripped by steam for example and containing coke is recycled in the first regenerator 17 by a line of recycling 16.
- the partially regenerated catalyst in the presence of an oxygen-containing gas, is raised in the second regenerator 4 by a lift 25, where it undergoes a second combustion in the presence of an oxygen-containing gas.
- cyclones or fluidization means in the separator or regenerators which are well known to those skilled in the art, and which are not shown in the figure for the sake of simplification.
- the regenerated and hot catalyst coming from the second regeneration zone in dense fluidized phase is introduced by gravity through the inclined line 3 into the conditioning enclosure 2 in a dense fluidized bed upstream of the dropper 13.
- a fluidization ring 5 supplies a fluidization gas 5a which may be steam, the lower part of the enclosure for conditioning the catalyst at a speed of 10 cm / s.
- the catalyst then has a density, for example between 550 and 800 kg / m 3 and typically 600 kg / m 3 .
- the enclosure 2 for conditioning the catalyst is dimensioned so as to present in its upper part a zone 8 for disengaging the gas from the catalyst, situated above the inlet of the line 3 and with a height of between a third and a quarter of the total height of the conditioning enclosure.
- a pressure equalization line 9 connects the disengagement zone to the upper part of the second regenerator.
- the device Downstream of the conditioning enclosure 2, the device comprises an injection chamber 10 of diameter at least equal to that of the dropper, at the inlet of which a flow control valve 1 1 or shaping valve d 'A falling curtain of catalyst lets escape, through its annular opening or restriction section, a catalyst flow of about 800 kg / m 2 .s.
- This valve can have a fixed central part or insert which, with the wall of the injection zone, determines the cross-section of the flow of catalyst determined in combination with another flow control valve 19 on the catalyst intake line 3 .
- the curtain shaping valve may include a movable central part connected to a rod, according to patent FR 2631857, this rod being protected from the catalyst by a sheath containing a purging gas. Said movable central part of the valve determines with its seat an annular passage section suitable for a given flow rate of catalyst delivered by the control valve 19 and therefore an appropriate flow.
- the injection chamber generally has a larger diameter than that of the restriction (the largest diameter of the annular curtain of catalyst formed) so that the tips of charge injectors do not intercept the catalyst curtain.
- the charge after having been atomized outside the device, is injected by a plurality of injectors 12 arranged at the periphery, on a plane substantially perpendicular to the axis of the dropper and whose jet of charge droplets is directed towards said axis at an injection angle close to 25 degrees of angle under the valve 11, against the current of the curtain falling from the catalyst, which makes it possible to break it.
- the distance from the injectors, counted from the theoretical impact points of the charge jets on the axis of the injection chamber (or of the dropper), at the lowest point of the shaping member of the curtain catalyst is at most equal to 2 times the diameter of the injection enclosure and preferably between 0.5 and 1 times this diameter. This distance of the injectors relative to the valve 11 prevents on the one hand the erosion of the valve and on the other hand the recirculation zones above the injectors, the catalyst and / or the charge.
- This dropper may have a diameter smaller than that of the injection enclosure.
- the cracking effluents are collected after stripping with steam by line 15 and the catalyst is recycled to the first regenerator 17.
- the flow control valve 19 is generally controlled by a line 22 to a temperature measurement 20 given by a probe 21 disposed at the lower end of the dropper.
- the unit is generally started by closing the restriction 1 1 with variable flow or by closing an all-or-nothing valve not shown in the figure, placed for example below the member 11, when the latter, at fixed central part, determines a constant passage section of catalyst.
- the part of the catalyst shaping member facing the injected charge may have a concave shape and thus determine a confinement zone for the vaporization of the latter capable of improving the selectivity of the cracking reaction.
- Fluidization speed in the packaging area 15 cm / s corresponding to a density of 580 kg / m 3 .
- Exit temperature of the second regenerator equal to the temperature of the catalyst conditioning zone: 780 ° C
- the distance along the axis of the charge injectors from the insert (lowest point) is 0.5 times the diameter of the injection chamber.
Landscapes
- 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)
- Catalysts (AREA)
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9611379 | 1996-09-18 | ||
FR9611379A FR2753454B1 (fr) | 1996-09-18 | 1996-09-18 | Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne |
PCT/FR1997/001630 WO1998012280A1 (fr) | 1996-09-18 | 1997-09-16 | Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0861310A1 true EP0861310A1 (fr) | 1998-09-02 |
EP0861310B1 EP0861310B1 (fr) | 2001-12-12 |
Family
ID=9495851
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP97919105A Expired - Lifetime EP0861310B1 (fr) | 1996-09-18 | 1997-09-16 | Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne |
Country Status (13)
Country | Link |
---|---|
US (1) | US6099720A (fr) |
EP (1) | EP0861310B1 (fr) |
JP (1) | JP4281026B2 (fr) |
KR (1) | KR100493753B1 (fr) |
CN (1) | CN1134528C (fr) |
AT (1) | ATE210712T1 (fr) |
CA (1) | CA2236296C (fr) |
DE (1) | DE69709050T2 (fr) |
ES (1) | ES2169860T3 (fr) |
FR (1) | FR2753454B1 (fr) |
ID (1) | ID18268A (fr) |
MX (1) | MX9803790A (fr) |
WO (1) | WO1998012280A1 (fr) |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BR0101433B1 (pt) * | 2001-04-10 | 2011-02-22 | método e dispositivo de entrada multi-funcional para reator tubular de fluxo descendente. | |
US20040206669A1 (en) * | 2001-06-08 | 2004-10-21 | Andrea De Rezende Pinho | Process for fluid catalytic cracking |
US7087154B2 (en) * | 2002-12-30 | 2006-08-08 | Petroleo Brasileiro S.A. - Petrobras | Apparatus and process for downflow fluid catalytic cracking |
CN1332742C (zh) * | 2004-05-14 | 2007-08-22 | 中国石油化工股份有限公司 | 催化裂化装置催化剂/助剂补充方法 |
US20080011644A1 (en) * | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of heavy oils in conjuction with FCC unit operations |
US20080011645A1 (en) * | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations |
US7758817B2 (en) * | 2006-08-09 | 2010-07-20 | Uop Llc | Device for contacting high contaminated feedstocks with catalyst in an FCC unit |
BRPI0909856B1 (pt) * | 2008-06-04 | 2017-12-12 | Inibicon A/S. | "previously treated high pressure biomass dispensing device for lower and higher pressure biomass discharge method for lowest" |
FR2959748B1 (fr) | 2010-05-06 | 2012-05-18 | Inst Francais Du Petrole | Procede de craquage catalytique avec recycle d'une coupe olefinique prelevee en amont de la section de separation des gaz afin de maximiser la production de propylene. |
US9458394B2 (en) | 2011-07-27 | 2016-10-04 | Saudi Arabian Oil Company | Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor |
JP5823911B2 (ja) * | 2012-04-27 | 2015-11-25 | Jx日鉱日石エネルギー株式会社 | 流動接触分解装置における原料と触媒を混合する混合装置 |
CN108726507B (zh) * | 2017-04-21 | 2020-11-13 | 山东大展纳米材料有限公司 | 一种单级连续化制备碳纳米管的装置及方法 |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2668755A (en) * | 1948-11-23 | 1954-02-09 | Kellogg M W Co | Plug-type control valve for fluidized catalyst conversion system |
JPS624784A (ja) * | 1985-07-16 | 1987-01-10 | コンパニ−・フランセ−ズ・ド・ラフイナ−ジユ | 炭化水素仕込物の接触クラツキングのための方法および装置の改良 |
US4919898A (en) * | 1987-08-11 | 1990-04-24 | Stone & Webster Engineering Corp. | Particulate solids cracking apparatus |
US4985136A (en) * | 1987-11-05 | 1991-01-15 | Bartholic David B | Ultra-short contact time fluidized catalytic cracking process |
FR2631857B1 (fr) * | 1988-05-24 | 1990-09-14 | Inst Francais Du Petrole | Reacteur a lit fluidise entraine comprenant un moyen de regulation du flux de particules solides et son utilisation dans un procede de craquage catalytique |
FR2667609B1 (fr) * | 1990-10-03 | 1993-07-16 | Inst Francais Du Petrole | Procede et dispositif de craquage catalytique en lit fluide a courant descendant. |
FR2683743B1 (fr) * | 1991-11-14 | 1994-02-11 | Institut Francais Petrole | Procede et dispositif d'echange thermique de particules solides pour double regeneration en craquage catalytique. |
US5296131A (en) * | 1992-12-02 | 1994-03-22 | Mobil Oil Corporation | Process for short contact time cracking |
FR2715163B1 (fr) * | 1994-01-18 | 1996-04-05 | Total Raffinage Distribution | Procédé de craquage catalytique en lit fluidisé d'une charge d'hydrocarbures, notamment d'une charge à forte teneur en composés azotés basiques. |
-
1996
- 1996-09-18 FR FR9611379A patent/FR2753454B1/fr not_active Expired - Fee Related
-
1997
- 1997-09-15 ID IDP973186A patent/ID18268A/id unknown
- 1997-09-16 KR KR10-1998-0703660A patent/KR100493753B1/ko not_active IP Right Cessation
- 1997-09-16 WO PCT/FR1997/001630 patent/WO1998012280A1/fr active IP Right Grant
- 1997-09-16 EP EP97919105A patent/EP0861310B1/fr not_active Expired - Lifetime
- 1997-09-16 ES ES97919105T patent/ES2169860T3/es not_active Expired - Lifetime
- 1997-09-16 CA CA002236296A patent/CA2236296C/fr not_active Expired - Lifetime
- 1997-09-16 JP JP51434198A patent/JP4281026B2/ja not_active Expired - Lifetime
- 1997-09-16 AT AT97919105T patent/ATE210712T1/de not_active IP Right Cessation
- 1997-09-16 US US09/077,007 patent/US6099720A/en not_active Expired - Lifetime
- 1997-09-16 DE DE69709050T patent/DE69709050T2/de not_active Expired - Lifetime
- 1997-09-16 CN CNB97191706XA patent/CN1134528C/zh not_active Expired - Lifetime
-
1998
- 1998-05-13 MX MX9803790A patent/MX9803790A/es unknown
Non-Patent Citations (1)
Title |
---|
See references of WO9812280A1 * |
Also Published As
Publication number | Publication date |
---|---|
KR19990067633A (ko) | 1999-08-25 |
DE69709050D1 (de) | 2002-01-24 |
KR100493753B1 (ko) | 2005-09-02 |
JP2001503080A (ja) | 2001-03-06 |
FR2753454B1 (fr) | 1999-06-04 |
FR2753454A1 (fr) | 1998-03-20 |
ES2169860T3 (es) | 2002-07-16 |
ATE210712T1 (de) | 2001-12-15 |
CA2236296A1 (fr) | 1998-03-26 |
DE69709050T2 (de) | 2002-05-02 |
MX9803790A (es) | 1998-09-30 |
EP0861310B1 (fr) | 2001-12-12 |
JP4281026B2 (ja) | 2009-06-17 |
CN1208432A (zh) | 1999-02-17 |
CA2236296C (fr) | 2007-01-16 |
ID18268A (id) | 1998-03-19 |
US6099720A (en) | 2000-08-08 |
WO1998012280A1 (fr) | 1998-03-26 |
CN1134528C (zh) | 2004-01-14 |
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