EP0874880B1 - Fluidkatalytisch krackverfahren und -einrichtung fur kohlenwasserstoffeinsätze - Google Patents
Fluidkatalytisch krackverfahren und -einrichtung fur kohlenwasserstoffeinsätze Download PDFInfo
- Publication number
- EP0874880B1 EP0874880B1 EP97919102A EP97919102A EP0874880B1 EP 0874880 B1 EP0874880 B1 EP 0874880B1 EP 97919102 A EP97919102 A EP 97919102A EP 97919102 A EP97919102 A EP 97919102A EP 0874880 B1 EP0874880 B1 EP 0874880B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- section
- hydrocarbons
- cracking
- mixing chamber
- 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.)
- Expired - Lifetime
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims description 30
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 30
- 238000000034 method Methods 0.000 title claims description 18
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 6
- 238000004231 fluid catalytic cracking Methods 0.000 title description 2
- 239000003054 catalyst Substances 0.000 claims description 95
- 238000006243 chemical reaction Methods 0.000 claims description 40
- 238000005336 cracking Methods 0.000 claims description 25
- 238000002156 mixing Methods 0.000 claims description 25
- 239000002245 particle Substances 0.000 claims description 25
- 230000008569 process Effects 0.000 claims description 16
- 239000000571 coke Substances 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 8
- 238000002485 combustion reaction Methods 0.000 claims description 7
- 238000004523 catalytic cracking Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 230000003134 recirculating effect Effects 0.000 claims 2
- 239000000203 mixture Substances 0.000 description 15
- 238000009835 boiling Methods 0.000 description 8
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 8
- 230000003197 catalytic effect Effects 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- -1 C 3 olefins Chemical class 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000008240 homogeneous mixture Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000003739 neck Anatomy 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000008685 targeting Effects 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
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 method and a catalytic cracker of a charge of hydrocarbons in a descending bed, implementing a improved zone of contact between the load and the catalyst.
- the cracking of the charge is carried out in the absence of hydrogen, in the gas phase; temperature reaction temperature is around 500 ° C and the pressure generally close to atmospheric pressure.
- the catalyst is covered with coke and traces of heavy oil and heat resulting from the combustion of this coke, during the operation regeneration in the presence of air or oxygen, allows bring the catalyst to the desired temperature for provide the calories necessary for the cracking reaction, after re-injection of the catalyst into the reactor.
- the ratio C / O, between the flow rate C of catalyst and the flow rate O of charge to be treated is limited by a maximum generally between 3 and 7, in the current reactors, and usually close to 5.
- upflow reactors occurs an accumulation of particles in the vicinity of the walls of the reactor, resulting in overcracking of the hydrocarbons at this level, which results in the formation of coke, hydrogen, methane and ethane, at location of the desired high octane products, while than at the center of the reactor, where fewer particles are present, an insufficient conversion of the charge.
- reaction times seem to be able to be significantly reduced compared to riser and be significantly less than 1 second, and it seems possible to freely increase the flow of catalyst, which has no of harmful influence on the movement of particles like in the case of the riser.
- the downer has, in particular, a related drawback to the initial mixture between catalyst and charge: in fact, the catalyst tends to fall off immediately without reflux or recirculation, which has a negative effect on the initial mass and heat transfer with the load.
- this device appears difficult to achieve on a plan mechanical and it does not allow a very efficient mixing in the case high catalyst flow rates. Indeed, when the direction of flow of the charge-catalyst mixture is reversed, the catalyst tends to agglomerate in the vicinity of the walls of the device and is therefore found isolated from the vaporized charge.
- the object of the invention is therefore to reconcile the advantages of the flow ascending, namely a satisfactory mixture between large flow rates of charge and catalyst, and downflow, ie good selectivity of the actual cracking reactions.
- the contacting zone according to the invention makes it possible to achieve the above objectives. Its geometry is particularly applicable to short time insofar as it allows a complete and rapid spraying of the load.
- EP-A-0 209 442 discloses a cracking device catalytic of hydrocarbons, including the contact zone between the catalyst and hydrocarbon consists only of one area elongated reaction vessel (see claim 6, column 3, rows 21 to 24), that is to say of a single part.
- EP-A-0 344 032 a bed reactor entrained fluidized, usable in particular for catalytic cracking hydrocarbons.
- This reactor substantially vertical and shaped elongated, has a particle flow regulator solids comprising a fixed part projecting inside the reactor as well as a mobile part which slides by means of a rod (cf. claim 1).
- This "regulatory body” is a system analogous to a piston, and its function is to regulate the flow of particles catalysts entering the contact zone between the catalyst and hydrocarbons (see column 11, lines 5 to 10).
- the ratio S 1 / S 3 between the section S 1 of 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, in order to allow optimal mixing within the mixing chamber.
- the hydrocarbons are injected at counter-current of the downward flow of catalyst particles, according to an angle to the horizontal, between 2 ° and 45 °, and preferably between 5 and 35 °.
- the mixture between the charge and the catalyst is optimized, because this direction of injection allows the charge to break down the mass of descending catalyst as well as possible.
- the reaction zone widens from the intermediate orifice at an angle with the vertical of between 1 and 20 °, and preferably 2 and 15 °, until it reaches its cross section. maximum S 4 .
- This flare allows to gradually transform perfectly agitated flow, prevailing within the mixture, in a piston type flow in the reaction zone. Since such a flow is particularly favorable to the selectivity of cracking reactions, the process of the invention combines so also the specific advantages of the downflow reactor usual.
- 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 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 process for the 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 separation phase 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 sprayed and brought into contact with the catalyst in a specific contacting zone of the catalytic cracking device defined above.
- the device shown comprises a tubular flow reactor 1 descending, or "downer”, fed at its upper part, from an enclosure 2, which is coaxial to it, made of catalyst particles regenerated.
- a valve 3 intended to regulate the mass ratio of catalyst to the mass of feedstock to be treated in the reactor, is interposed between reactor 1 and enclosure 2. Below this valve opens a line 4 for supplying reactor 1 with the load of hydrocarbons to be treated, preheated so known per se. This charge is sprayed into fines droplets, by injectors, at the top of the brought into contact 5, to mix with the particles of catalyst, in contact with which the reaction of cracking.
- the direction of charge injection, as well that the geometry of the contact area, will be detailed below.
- the catalyst particles and the charge to process therefore flow from top to bottom in reactor 1.
- the spent catalyst particles pour into a stripping chamber 6, provided at its base of a diffuser 7, supplied with water vapor by a line 8.
- the stripped catalyst particles are removed by gravity of the enclosure 6, by an inclined conduit 22, towards a ascending column 12, in which they are routed to the top, towards a regenerator 13, using a carrier gas, disseminated at 14 at the base of column 12, from the line 15.
- the regenerated catalyst particles are removed by gravity through the conduit 19 in the direction of the enclosure 2, without heat losses.
- Figure 2 shows the area more precisely contact 5 object of the invention.
- the contacting zone 5 is formed by a mixture 24 and a reaction zone 25 arranged immediately below it.
- the mixing chamber 24 is supplied at its upper part with hot regenerated catalyst by 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 S 1 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 with an angle at the apex A, until it reaches its maximum cross section S 2 .
- 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 S 1 , but can be between 1.5 and 8 S 1 .
- the periphery 34 of the mixing chamber 24, at the level of the maximum section of the latter, is provided with a series of injectors 36, allowing the charge to be injected after atomization thereof outside the device.
- the injectors 36 are oriented so as to direct the charge droplets countercurrent to the downward flow of catalyst particles, at an angle B with respect 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 load droplets.
- 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 widening then narrowing, is shaped so that there is a type flow perfectly agitated, allowing reflux and recirculation of catalyst necessary for a good mixture 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 .
- the 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 S 4 .
- 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 .
- This flare allows a progressive modification of the nature of the flow of the charge-catalyst mixture.
- the agitated flow within the mixing chamber is transformed in this way into a piston type flow in the reaction zone, which is perfectly suited for ensure good selectivity of the cracking reactions which occur there.
- 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 4 , so as to best conserve the flow of piston type which was established during the passage of the load in the frustoconical section 42.
- the section S 1 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 cm 2 , but can be between 10 and 500 cm2.
- the maximum section S 2 of the mixing chamber 24, and the maximum section S 4 of the reaction zone 25 are for example equal to 300 cm 2 , but can be between 30 and 2000 cm 2 .
- This description refers to an area of contact which consists of a series of surfaces of revolution, namely cylindrical portions or frustoconical whose cross section is circular.
- the present invention also relates to any area of contact for which there are certain reports between the sections of its constituent parts, that these sections are either polygonal, ovoid or shaped any.
- the contact area according to the invention finds its application to any cracking device catalytic whose reactor is downflow from charge, whatever the means of stripping and regeneration of the deactivated catalyst.
- the process according to the invention therefore makes it possible to increase the selectivity of cracking by authorizing a mass ratio catalyst / charge higher than in the prior art (and therefore a lower ⁇ coke, i.e. a lower difference between the quantities of coke present on the catalyst at the entrance to the regeneration zone and at the exit from it).
- the process according to the invention also allows, when we are targeting a given conversion, to process more difficult, especially denser and the 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)
Claims (9)
- Vorrichtung zum katalytischen Cracken von Kohlenwasserstoffen, mit einem Crackreaktor (1) unter absteigendem Fluß, Einrichtungen zum Zuliefern des Reaktors unter Druck mit einer Kohlenwasserstoffbeladung und mit Teilchen eines regenerierten Crackkatalysators, einer Einrichtung zum Trennen von Produkten der gecrackten Beladung und von Teilchen des deaktiverten Katalysators, mindestens einer Abzieheinrichtung (6) für mindestens ein Fluid von Teilchen des deaktivierten Katalysators, mindestens einer Regenerationseinheit (13) des besagten Katalysators durch Verbrennung von durch den Katalysator getragenem Koks, und Einrichtungen (19; 2; 3) zum Recyceln des regenerierten Katalysators zu den besagten Zuliefereinrichtungen,
wobei diese Vorrichtung dadurch gekennzeichnet ist, daß sie eine Zone (5) zum spezifischen Kontaktieren der Kohlenwasserstoffe und des Katalysators umfaßt, die aufgebaut ist miteiner Mischkammer (24) mit maximalem Querschnitt S2, die mit den Zuliefereinrichtungen des regenerierten Katalysators durch eine obere Öffnung (30) in Verbindung steht, welche einen Katalysator-Passierquerschnitt S1 definiert,und einer Reaktionszone (25) mit maximalem Querschnitt S4, die mit der Mischkammer (24) durch eine Zwischenöffnung (40) mit Querschnitt S3 in Verbindung steht, - Vorrichtung gemäß Anspruch 1, dadurch gekennzeichnet, daß das Verhältnis S1/S3 zwischen dem Querschnitt S1 der Passage des Katalysators durch die obere Öffnung (30) und dem Querschnitt S3 der Zwischenöffnung (40) im Bereich von 0,8 bis 1,25 und vorzugsweise von 0,9 bis 1,1 liegt.
- Vorrichtung gemäß Anspruch 1 oder 2, dadurch gekennzeichnet, daß die Reaktionszone (25), ausgehend von der Zwischenöffnung (40), sich unter einem Winkel mit der Vertikalen von zwischen einschließlich 1 und 20° und vorzugsweise zwischen 2 und 15° konisch aufweitet, bis der maximale Querschnitt S4 erreicht ist.
- Vorrichtung gemäß Anspruch 3, dadurch gekennzeichnet, daß das Verhältnis S4/S3 einen Wert von zwischen einschließlich 1,5 und 8 annimmt.
- Vorrichtung gemäß Anspruch 3 oder 4, dadurch gekennzeichnet, daß das Verhältnis S2/S4 zwischen dem maximalen Querschnitt S2 der Mischkammer (24) und dem maximalen Querschnitt S4 der Reaktionszone (25) im Bereich von 0,8 bis 1,25 und vorzugsweise von 0,9 bis 1,1 liegt.
- Vorrichtung gemäß irgendeinem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß der Querschnitt S1 der Passage des Katalysators durch die obere Öffnung (30) und der Querschnitt S3 der Zwischenöffnung (40) im Bereich von 10 bis 500 cm2 liegen.
- Vorrichtung gemäß irgendeinem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß der maximale Querschnitt S2 der Mischkammer (24) und der maximale Querschnitt S4 der Reaktionszone (25) im Bereich von 30 bis 2.000 cm2 liegen.
- Verfahren zum katalytischen Cracken von Kohlenwasserstoffen, umfassend
eine Stufe des Kontaktierens von Kohlenwasserstoffen und von Teilchen eines Katalysators, eine Stufe der katalytischen Reaktion unter absteigendem Flußbett, eine Stufe zur Trennung des deaktivierten Katalysators und von Kohlenwasserstoff-Ausflüssen, mindestens einer Stufe des Abziehens von deaktiviertem Katalysator, dann eine Stufe der Regenerierung des besagten Katalysators unter Verbrennungsbedingungen von durch den Katalysator getragenem Koks, und schließlich eine Stufe des Recycelns des regenerierten Katalysators in die Zulieferzone,
wobei dieses Verfahren dadurch gekennzeichnet ist, daß ein substantieller Teil der Kohlenwasserstoffe versprüht wird und in Kontakt gebracht wird mit dem Katalysator in einer solchen spezifischen Kontaktierzone, wie sie in einem der Ansprüche 1 bis 7 definiert ist. - Verfahren zum Cracken gemäß Anspruch 8, dadurch gekennzeichnet, daß die Kohlenwasserstoffe in die Mischkammer im Gegenstrom des absteigenden Flusses der Katalysatorteilchen injiziert werden unter einem Winkel im Verhältnis zur Horizontalen, der im Bereich von 2° bis 45° und vorzugsweise von 5° bis 35° liegt.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9611369 | 1996-09-18 | ||
FR9611369A FR2753453B1 (fr) | 1996-09-18 | 1996-09-18 | Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures, mettant en oeuvre une zone de mise en contact amelioree |
PCT/FR1997/001627 WO1998012279A1 (fr) | 1996-09-18 | 1997-09-16 | Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0874880A1 EP0874880A1 (de) | 1998-11-04 |
EP0874880B1 true EP0874880B1 (de) | 2004-07-07 |
Family
ID=9495845
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP97919102A Expired - Lifetime EP0874880B1 (de) | 1996-09-18 | 1997-09-16 | Fluidkatalytisch krackverfahren und -einrichtung fur kohlenwasserstoffeinsätze |
Country Status (15)
Country | Link |
---|---|
US (1) | US5997726A (de) |
EP (1) | EP0874880B1 (de) |
JP (1) | JP3955332B2 (de) |
KR (1) | KR100493978B1 (de) |
CN (1) | CN1125867C (de) |
AR (1) | AR008431A1 (de) |
AT (1) | ATE270700T1 (de) |
CA (1) | CA2236839C (de) |
DE (1) | DE69729785T2 (de) |
ES (1) | ES2224238T3 (de) |
FR (1) | FR2753453B1 (de) |
ID (1) | ID20024A (de) |
TW (1) | TW366359B (de) |
WO (1) | WO1998012279A1 (de) |
ZA (1) | ZA978333B (de) |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2778859B1 (fr) * | 1998-05-25 | 2000-08-11 | Total Raffinage Distribution | Procede et dispositif d'introduction de particules de catalyseur dans un reacteur de craquage catalytique a l'etat fluide |
FR2785907B1 (fr) * | 1998-11-13 | 2001-01-05 | Inst Francais Du Petrole | Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant |
FR2811327B1 (fr) | 2000-07-05 | 2002-10-25 | Total Raffinage Distribution | Procede et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres reactionnelles successives |
US6613290B1 (en) | 2000-07-14 | 2003-09-02 | Exxonmobil Research And Engineering Company | System for fluidized catalytic cracking of hydrocarbon molecules |
GB2403434B (en) | 2002-04-26 | 2005-09-14 | China Petroleum & Chemical | A downflow catalytic cracking reactor and its application |
FR2895413B1 (fr) | 2005-12-27 | 2011-07-29 | Alstom Technology Ltd | Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone |
KR101954472B1 (ko) * | 2011-07-27 | 2019-03-05 | 사우디 아라비안 오일 컴퍼니 | 하향류 반응기에서 파라핀계 나프타의 유동접촉분해 방법 |
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 |
US10913043B2 (en) | 2018-09-28 | 2021-02-09 | Uop Llc | Apparatuses for mixing of staged methanol injection |
FR3140776A1 (fr) | 2022-10-13 | 2024-04-19 | IFP Energies Nouvelles | Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène. |
FR3140778A1 (fr) * | 2022-10-13 | 2024-04-19 | IFP Energies Nouvelles | Réacteur à lit fluidisé à co-courant gaz-solide descendant à injecteur orienté. |
FR3140777A1 (fr) | 2022-10-13 | 2024-04-19 | IFP Energies Nouvelles | Chambre de mélange pour réacteur à lit fluidisé à co-courant gaz-solide descendant. |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
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. |
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 FR9611369A patent/FR2753453B1/fr not_active Expired - Fee Related
-
1997
- 1997-09-16 ID IDW980007A patent/ID20024A/id unknown
- 1997-09-16 ES ES97919102T patent/ES2224238T3/es not_active Expired - Lifetime
- 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 JP JP51434098A patent/JP3955332B2/ja not_active Expired - Lifetime
- 1997-09-16 ZA ZA9708333A patent/ZA978333B/xx unknown
- 1997-09-16 CN CN97191272A patent/CN1125867C/zh not_active Expired - Lifetime
- 1997-09-16 KR KR10-1998-0703555A patent/KR100493978B1/ko not_active IP Right Cessation
- 1997-09-16 DE DE69729785T patent/DE69729785T2/de not_active Expired - Lifetime
- 1997-09-16 AT AT97919102T patent/ATE270700T1/de not_active IP Right Cessation
- 1997-09-16 EP EP97919102A patent/EP0874880B1/de not_active Expired - Lifetime
- 1997-09-16 US US09/068,500 patent/US5997726A/en not_active Expired - Lifetime
- 1997-09-18 AR ARP970104274A patent/AR008431A1/es unknown
- 1997-10-23 TW TW086113666A patent/TW366359B/zh not_active IP Right Cessation
Also Published As
Publication number | Publication date |
---|---|
TW366359B (en) | 1999-08-11 |
AR008431A1 (es) | 2000-01-19 |
CN1205028A (zh) | 1999-01-13 |
WO1998012279A1 (fr) | 1998-03-26 |
ATE270700T1 (de) | 2004-07-15 |
DE69729785D1 (de) | 2004-08-12 |
ZA978333B (en) | 1998-03-24 |
KR19990067533A (ko) | 1999-08-25 |
ID20024A (id) | 1998-09-10 |
CN1125867C (zh) | 2003-10-29 |
CA2236839C (fr) | 2007-03-20 |
FR2753453B1 (fr) | 1998-12-04 |
KR100493978B1 (ko) | 2005-09-02 |
US5997726A (en) | 1999-12-07 |
JP3955332B2 (ja) | 2007-08-08 |
JP2000500820A (ja) | 2000-01-25 |
FR2753453A1 (fr) | 1998-03-20 |
ES2224238T3 (es) | 2005-03-01 |
EP0874880A1 (de) | 1998-11-04 |
DE69729785T2 (de) | 2005-07-14 |
CA2236839A1 (fr) | 1998-03-26 |
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