EP1242569A1 - Verfahren und einrichtung zur katalytischen spaltung mit parallelen afwärts- undabwärtsfliessenden reaktoren - Google Patents
Verfahren und einrichtung zur katalytischen spaltung mit parallelen afwärts- undabwärtsfliessenden reaktorenInfo
- Publication number
- EP1242569A1 EP1242569A1 EP00983393A EP00983393A EP1242569A1 EP 1242569 A1 EP1242569 A1 EP 1242569A1 EP 00983393 A EP00983393 A EP 00983393A EP 00983393 A EP00983393 A EP 00983393A EP 1242569 A1 EP1242569 A1 EP 1242569A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- zone
- reactor
- outlet
- coke
- 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
- 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 catalytic cracking device (FCC) in entrained bed comprising reactors in parallel comprising at least one downflow reactor (dropper) and at least one upward catalyst reactor (commonly called riser) from at least one regeneration zone.
- FCC catalytic cracking device
- catalytic cracking units comprising a double regeneration with injection of the charge in the form of fine droplets met the need to work on heavy cuts.
- Patent application FT98 / 14319 describes a chain of a dropper and a riser in series. It describes in detail the advantages of a second reactor which is operated under very different conditions in temperature and C / O of the main riser: in particular, this second reactor advantageously represents an additional capacity for treating a heavy load in producing a minimal amount of coke compared to a conventional reactor; it also becomes possible to crack certain cuts (called recycles) from the main riser that are not desirable (low recovery or cuts that do not meet certain specifications such as sulfur or aromatic contents) in order to maximize the yield of recovered cuts (LPG, petrol) .
- recycles certain cuts
- the fresh charge is introduced at the bottom of the riser and it is the LCO produced from the riser which is introduced as the charge for the dropper.
- the LCO produced from the riser which is introduced as the charge for the dropper.
- Such a configuration makes it possible to maximize the gasoline yield by exhausting the LCO under relatively severe cracking conditions.
- the drawback of this system with a dropper and a riser in series is that for a large load capacity at the dropper, the ascending reactor works with a non-negligible amount of catalyst partially deactivated by its passage through the dropper (deactivation coming from the deposit of coke on the catalyst). This results in a reduced efficiency which does not allow to draw the full potential of this association.
- US Patent 4116814 also illustrates the case of two reactors with upward flow in parallel, connected to a particle regenerator.
- An object of the invention is to remedy the drawbacks of the prior art.
- Another object is to crack both heavy and light hydrocarbons under reaction conditions which are severe, in a reactor adapted to this type of conditions, the dropper or downflow reactor and much less severe in a riser or reactor. upward flow so as to favor the formation of very different products meeting the specificities of each type of reactor.
- the invention relates to a process for catalytic cracking in a entrained or fluidized bed of at least one charge of hydrocarbons in at least two reaction zones, at least one of which is of upward flow, into which the charge is introduced and catalyst from at least one regeneration zone in the lower part of the upward flow reaction zone, the charge and the catalyst are circulated from bottom to top in said zone, the first gases produced from the coke catalyst are separated in a first separation zone, the catalyst is stripped by means of a stripping gas, a first cracking and stripping effluent is recovered and the coke catalyst is recycled in the regeneration zone and it is at least partly regenerated by means of '' an oxygen-containing gas, the process being characterized in that catalyst is introduced from at least one regeneration zone and a hydrocarbon charge e in the upper part of at least one reaction zone with downward flow, the catalyst and said charge are circulated there from top to bottom under appropriate conditions, the coke catalyst is separated from the second gases produced in a second separation zone, the second gases produced are recovered and the coke catalyst
- the temperature of the catalyst leaving the descending reactor can be higher than that leaving the ascending reactor.
- the catalyst originating from the second separation zone can be stripped by means of a recycling gas which is usually steam and the resulting hydrocarbons are generally recovered with the cracking gases. It is preferable to regenerate the coke catalyst in two consecutive regeneration zones, each of which has its own combustion gas discharge resulting from the regeneration of the coke catalyst.
- the catalyst to be regenerated from the first separation zone is introduced into a first regeneration zone operating at an appropriate temperature, the catalyst thus at least partially regenerated being sent to the second regeneration zone operating at a higher temperature and the catalyst regenerated from the second regeneration zone is introduced into the upward flow reaction zone and into the downflow reaction zone.
- the coke catalyst from the second separation zone can be recycled in the first regeneration zone either by gravity flow, generally in the dense zone, or by flow by means of a riser comprising fluidizing air as engine ( lift), usually in the diluted area of the first regeneration area.
- the hydrocarbon feedstock or each of the feedstocks, if they are different, can be introduced into the upward reaction zone and into the downward reaction zone by a co-current injection of the catalyst flow or against the current, or against the current. current for one and co-current for the other. However, an injection against the current in the two zones seems preferable for better vaporization of the droplets introduced.
- the operating conditions for catalytic cracking of the charges are usually as follows:
- catalyst temperature (RD outlet) 500-650 ° C, preferably 560-620 ° C;
- the charge supplying each of the reaction zones can be a so-called fresh charge, a recycle of part of the products from a downstream fractionation or a mixture of of them.
- the charge of one of the reaction zones can be either heavier or lighter than that circulating in the other zone. More particularly, the charge of the upward flow reaction zone can be a vacuum distillate or an atmospheric residue or a recycle of part of the products from the downward reaction zone and the charge of the downflow zone is a non-charge. cracked or recycled part of the products from the bottom-up reaction zone and preferably a petrol cut or an LCO cut.
- the feed rate and for example of recycle flow (LCO cut, HCO or gasoline) circulating in the descending reactor can represent less than 50% by weight of the feed rate to be converted in the upward reaction zone.
- the dropper loop can be adapted to most existing cracking units, to one or two regenerators and / or with a technology of separation, stripping and transfer of the catalyst best suited to the requirements of the client.
- the coke content is therefore reduced very significantly so that the amount of heat given off by the combustion of this additional coke in the regenerator (s) is much less than the quantity of heat consumed by the vaporization of the feedstock and the heat of reaction in the dropper reactor.
- the catalyst on the regeneration side is cooled compared to the previous situation comprising only one traditional riser.
- This heat extraction effect which can be obtained in an equivalent manner by a regeneration side heat exchanger (catcooler) or by the vaporization of an almost chemically inert recycle (TCM) downstream of the charge injection into the direction of flow of the catalyst in a riser or dropper reactor, makes it possible either to treat charges with a higher carbon Conradson, or to increase the charge rate, or to take advantage of the decrease in temperature at the regenerator (s) ) to increase the circulation of catalyst (C / O) at the riser and the dropper.
- the heat necessary for the reaction and for vaporization on the reaction side is supplied by the regenerated catalyst, heated by combustion of the coke to the regenerator (s).
- the heat extraction effect requires increasing the circulation of catalyst at a constant charge rate and therefore benefiting from better catalytic activity (more active sites). We can also treat more refractory charges in the dropper.
- the invention also relates to a catalytic cracking device in a entrained or fluidized bed of a hydrocarbon feedstock comprising: - At least one substantially vertical ascending reactor having a lower inlet and an upper outlet:
- a first means for supplying regenerated catalyst connected to at least one coke catalyst regenerator and connected to said lower inlet; - a first means for supplying the load disposed above the lower inlet of the ascending reactor;
- the device being characterized in that it comprises at least one substantially vertical descending reactor having an upper inlet and a lower outlet;
- a second means for supplying regenerated catalyst connected to said coke catalyst regenerator and connected to said upper inlet of the descending reactor; a second means for supplying the load disposed below the second supply means;
- a second enclosure for separation of the coke catalyst from a second gas phase connected to the lower outlet of the descending reactor and having an outlet from the second gas phase and an outlet from the coke catalyst, and second means for recycling the coke catalyst connected to said catalyst outlet from the second separation enclosure and connected to the regenerator.
- the second enclosure for separating the catalyst from the cracking effluents may not include a stripping chamber.
- prestripage means for example by water vapor can be introduced into the separation enclosure and the evacuation of the vapor can be carried out with the cracking and prestripage effluents.
- the second separation enclosure comprises a catalyst stripping chamber with injection of stripping vapor, in communication with it, like that described for example in the patent application of the Applicant FR 98 / 09.672 incorporated as reference. Cracking and stripping effluents are generally removed by common means.
- the device can comprise two superposed regenerators of coke catalyst, the second being located above the first, means for circulating the catalyst from the first regenerator to the second regenerator.
- the said first and second catalyst supply means are connected to the second regenerator and the lower outlet of the first separation enclosure is connected to the first regenerator via the first recycling means.
- a regeneration zone (1) of the coke catalyst comprises two regeneration chambers (2) and (3) superimposed in which the catalyst is regenerated in a fluidized bed, air being introduced at the base of each chamber by means not shown in the figure.
- Each enclosure has its own dedusting means (4, 5) (cyclones) and evacuation (9, 10) of the coke combustion effluents.
- each enclosure (2) and (3) can be controlled by valves located on the lines allowing the evacuation of the combustion effluents at least partially dusted.
- the catalyst is transported between the two enclosures by means of a lift column (6).
- Air generally introduced at the base by an injector (7), at a sufficient speed makes it possible to transport the catalyst between the two enclosures.
- the proportion of air required for regeneration is 30 to 70% in the lower enclosure (2) operating at a lower temperature (670 ° C for example) and 15 to 40% in the upper enclosure (3 ) operating at a higher temperature (770 ° C for example), 5 to 20% of air circulating in the lift to transport the catalyst.
- a valve on solid (8), of the plug valve type makes it possible to control the flow of circulation between the chambers (2) and (3).
- the substantially regenerated catalyst from the second regenerator located above the first (3) is sent from a dense bed (11) into a disengagement well (13) by a conduit (12) inclined at an angle usually between 30 and 70 degrees from the horizontal.
- the circulation of the catalyst is slowed down to allow any gas bubbles to be evacuated towards the second regeneration enclosure (3) through a pressure equalization line (14).
- the catalyst is then accelerated and descends through a transfer tube (15) to the entry of a downflow reactor (16).
- the catalyst is kept in the fluidized state by the addition of small quantities of gas throughout the transport. If the catalyst is thus maintained in the fluidized state, this makes it possible to obtain a pressure at the inlet of the dropper greater than that of the fumes from the external cyclones (5).
- the dropper (16) comprises means for introducing the regenerated catalyst (17) which can be a valve on solid, an orifice or simply the opening of a conduit, in a contacting zone (18) located under the valve (17), where the catalyst meets countercurrent for example, the hydrocarbon charge, introduced by injectors (19), generally consisting of atomizers where the charge is finely divided into droplets thanks to the introduction of auxiliary fluids such as water vapor.
- injectors (19) generally consisting of atomizers where the charge is finely divided into droplets thanks to the introduction of auxiliary fluids such as water vapor.
- the means for introducing the catalyst are located above the means for introducing the charge.
- a reaction zone (21) of substantially elongated shape, shown vertically in the figure but this condition is not exclusive.
- the average residence time of the hydrocarbons in zones (18) and (21) will, for example, be less than 650 ms, preferably between 50 and 500 ms.
- the dropper effluents are then separated in the separator (20), for example as 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 cyclones, for example external cyclones (22) arranged downstream on a line (23). These gaseous effluents (cracked gases) are discharged through a line (24).
- the catalyst in the fluidized bed (28) then undergoes stripping (contact with a light gas such as water vapor, nitrogen, ammonia, hydrogen or even hydrocarbons, the number of carbon atoms is less than 3) by means which are well described in the prior art before being transferred to the riser (25) through the conduit (26).
- the stripping gas effluents are generally evacuated from the fluidized bed (28) through the same means (23, 22) which allow the evacuation of the gaseous effluents from the dropper (16) by the line (24).
- the coke catalyst is raised by a fluidizing gas (29) in the dense fluidized bed of the second regenerator (3).
- the riser reaction zone (30) is a substantially elongated tubular zone, many examples of which are described in the prior art.
- the hydrocarbon charge is introduced by means (31), generally consisting of atomizers where the charge is finely divided into droplets, generally using the introduction of auxiliary fluids such as water vapor, introduced through the means (31).
- the means for introducing the catalyst are located below the means for introducing the charge.
- the feed introduction is located above the catalyst inlet.
- These means for introducing the catalyst into the riser (30) comprise a withdrawal well (32) conforming to that (13) which supplies the dropper, connected to the dense bed of the second catalyst regenerator (3) by a conduit (33). inclined at substantially the same angle as that of the conduit (12).
- the well (32) is furthermore connected to the diluted fluidized bed by a pressure equalization line (34).
- a line (35) At the base of the well, a line (35) first vertical then inclined is connected to the lower part of the riser.
- a control valve (36) arranged on the line (35) regulates the flow rate of regenerated catalyst at the inlet of the riser as a function of the catalyst outlet temperature and of the effluents at the top of the riser.
- Fluidizing gas introduced at the base of the riser by injection means (37) circulates the catalyst cocurrently with the charge in the riser.
- the charge could have been injected against the current of the downward flow of the riser.
- an injection of a light cut of hydrocarbons or a heavier cut (LCO or HCO for example), coming from a distillation downstream of the riser cracking effluents, can be carried out in this riser.
- the cut introduced can represent 10 to 50% by weight of the load introduced into the riser and can contribute to maximizing the production of gasoline.
- the cracking reaction takes place in the riser.
- the cracked effluents are then separated in a separator (38), for example as described in PCT application FR 98/01866 incorporated as a reference.
- the catalyst resulting from the separation is then introduced into a fluidized bed (39) of a stripping chamber (40) located below the separator, through conduits (41) or openings.
- the catalyst in the chamber (39, 40) is then stripped (contact with a light gas such as water vapor, nitrogen, ammonia, hydrogen or even hydrocarbons with a number of carbon atoms less than 3) by means not shown in the figure.
- the stripped catalyst is then transferred to the dense bed of the first regeneration enclosure (2) by a conduit (45).
- the gaseous effluents from cracking and stripping separated in the separator (38) are discharged through a conduit (42) to a secondary separator (43) such as a cyclone, for example internal to the chamber (39, 40) before be directed to the downstream fractionation section by a conduit (44).
- a secondary separator (43) such as a cyclone, for example internal to the chamber (39, 40) before be directed to the downstream fractionation section by a conduit (44).
- the results of this comparison are based on industrial results obtained with the unit with the riser and pilot tests of 'cracking the reporting cut.
- the new conditions enabling the thermal balance of the unit as a whole to be satisfied are recalculated with a process model.
- the fresh charge (vacuum distillate) has the following characteristics: - Density d 15 : 0.937 - Sulfur content: 0.5%
- This catalyst based on Y zeolite has the following characteristics:
- the catalyst comes from the second regenerator.
- the cracked effluents are distilled and part of the HCO cut obtained as well as all of a heavy gasoline cut (170 ° C-200 ° C) are recycled into the riser.
- This recycle consisting of 49.3% HCO and 50.7% of heavy petrol cut, represents 27.1% by weight of the fresh charge at the riser.
- An additional cut is recycled as feed to the dropper which is in turn fed with catalyst from the second regenerator.
- the coke catalyst from the stripper connected to the riser is recycled in the dense phase of the first regenerator while that from the stripper connected to the dropper is recycled by means of a lift in the dense phase of the second regenerator.
- the conditions are maintained at the riser (ROT and recycles) by increasing the C / O of the riser.
- RD descending reactor (residence time: 0.4 s)
- REG1 first regeneration enclosure
- REG2 second regeneration chamber
- propylene can be produced in substantial quantity (53% more) by a really severe cracking with a dropper, while maintaining a satisfactory fuel yield.
- the temperature of the second regenerator dropped by 21 ° C (catcooler effect).
- a gain in conversion of the fresh charge of 1.9% is obtained by exhausting the LCO and slurry.
- the conditions are maintained at the riser (ROT and recycles) by increasing the C / O of the riser.
- the HCO slurry
- the temperature of the second regenerator dropped by 11 ° C (catcooler effect)
- a gain in conversion of the fresh charge of 4.8% is obtained by exhausting the slurry, leading to better yields of recoverable products (more than 1.5% of LPG and 2.3% more petrol)
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)
- Processing Of Solid Wastes (AREA)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9915747 | 1999-12-14 | ||
FR9915747A FR2802211B1 (fr) | 1999-12-14 | 1999-12-14 | Procede et dispositif de craquage catalytique comprenant en parallele au moins un reacteur a ecoulement ascendant et au moins un reacteur a ecoulement descendant |
PCT/FR2000/003315 WO2001044409A1 (fr) | 1999-12-14 | 2000-11-28 | Procede et dispositif de craquage catalytique comprenant en parallele au moins un reacteur a ecoulement ascendant et au moins un reacteur a ecoulement descendant |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1242569A1 true EP1242569A1 (de) | 2002-09-25 |
EP1242569B1 EP1242569B1 (de) | 2011-02-02 |
Family
ID=9553233
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00983393A Expired - Lifetime EP1242569B1 (de) | 1999-12-14 | 2000-11-28 | Verfahren und vorrichtung zur katalytischen spaltung mit aufwärts- und abwärtsbetriebenen parallelen reaktoren |
Country Status (10)
Country | Link |
---|---|
US (1) | US7220351B1 (de) |
EP (1) | EP1242569B1 (de) |
JP (1) | JP4671089B2 (de) |
AT (1) | ATE497527T1 (de) |
DE (1) | DE60045600D1 (de) |
ES (1) | ES2359623T3 (de) |
FR (1) | FR2802211B1 (de) |
MX (1) | MXPA02005794A (de) |
WO (1) | WO2001044409A1 (de) |
ZA (1) | ZA200204751B (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104245892A (zh) * | 2012-03-20 | 2014-12-24 | 沙特***石油公司 | 用于处理原油的集成加氢处理和流体催化裂化 |
Families Citing this family (40)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2894849B1 (fr) * | 2005-12-20 | 2008-05-16 | Inst Francais Du Petrole | Nouveau reacteur a deux zones reactionnelles fluidisees avec systeme de separation gaz/solide integre |
US20080011645A1 (en) * | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations |
US20080011644A1 (en) * | 2006-07-13 | 2008-01-17 | Dean Christopher F | Ancillary cracking of heavy oils in conjuction with FCC unit operations |
FR2909897B1 (fr) * | 2006-12-13 | 2009-06-26 | Inst Francais Du Petrole | Nouveau systeme de separation gaz solide pour les regenerateurs des unites de craquage catalytique en lit fluidise |
FR2932495B1 (fr) | 2008-06-17 | 2011-03-25 | Inst Francais Du Petrole | Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers. |
RU2547152C2 (ru) * | 2009-10-22 | 2015-04-10 | Чайна Петролеум & Кемикал Корпорейшн | Способ каталитической конверсии с увеличенным выходом дизельного топлива с высоким цетановым числом |
US8415264B2 (en) * | 2010-04-30 | 2013-04-09 | Uop Llc | Process for regenerating catalyst in a fluid catalytic cracking unit |
EP2591073B1 (de) | 2010-07-08 | 2019-07-03 | Indian Oil Corporation Ltd. | Zweistufiges katalytisches fluid-cracking-verfahren |
EP2591071B1 (de) | 2010-07-08 | 2018-12-12 | Indian Oil Corporation Ltd. | Aufstromregeneration eines fcc-katalysators für mehrstufiges cracken |
FR2966160B1 (fr) * | 2010-10-14 | 2013-11-15 | IFP Energies Nouvelles | Procede de craquage catalytique adapte au traitement de charges a faible carbon conradson comportant le recycle d'une coupe cokante selon une technologie nouvelle |
WO2012062173A1 (zh) | 2010-11-11 | 2012-05-18 | Shi Baozhen | 一种催化裂化方法及装置 |
KR101954472B1 (ko) * | 2011-07-27 | 2019-03-05 | 사우디 아라비안 오일 컴퍼니 | 하향류 반응기에서 파라핀계 나프타의 유동접촉분해 방법 |
FR2983208B1 (fr) * | 2011-11-24 | 2015-03-06 | IFP Energies Nouvelles | Procede de production de distillat moyen a partir d'une charge lourde conventionnelle incluant une etape d'hydrogenation selective de la coupe hco ex fcc |
US9290705B2 (en) | 2012-10-19 | 2016-03-22 | Saudi Arabian Oil Company | Process for high severity catalytic cracking of crude oil |
CN104275037A (zh) * | 2013-07-09 | 2015-01-14 | 刘英聚 | 一种同轴式防结焦气固分离方法和设备 |
US9422487B2 (en) | 2014-04-09 | 2016-08-23 | Uop Llc | Process for fluid catalytic cracking and hydrocracking hydrocarbons |
US9399742B2 (en) | 2014-04-09 | 2016-07-26 | Uop Llc | Process for fluid catalytic cracking and hydrocracking hydrocarbons |
US9243195B2 (en) | 2014-04-09 | 2016-01-26 | Uop Llc | Process and apparatus for fluid catalytic cracking and hydrocracking hydrocarbons |
US9394496B2 (en) | 2014-04-09 | 2016-07-19 | Uop Llc | Process for fluid catalytic cracking and hydrocracking hydrocarbons |
CN104437307B (zh) * | 2014-11-07 | 2016-04-13 | 广德瑞邦涂料有限公司 | 一种用于合成阴极水溶性电泳漆乳液的乳化釜 |
US9567537B2 (en) | 2015-03-10 | 2017-02-14 | Uop Llc | Process and apparatus for producing and recycling cracked hydrocarbons |
US9809766B2 (en) | 2015-03-10 | 2017-11-07 | Uop Llc | Process and apparatus for producing and recycling cracked hydrocarbons |
US9732290B2 (en) | 2015-03-10 | 2017-08-15 | Uop Llc | Process and apparatus for cracking hydrocarbons with recycled catalyst to produce additional distillate |
US9890338B2 (en) | 2015-03-10 | 2018-02-13 | Uop Llc | Process and apparatus for hydroprocessing and cracking hydrocarbons |
US9783749B2 (en) | 2015-03-10 | 2017-10-10 | Uop Llc | Process and apparatus for cracking hydrocarbons with recycled catalyst to produce additional distillate |
US9777229B2 (en) | 2015-03-10 | 2017-10-03 | Uop Llc | Process and apparatus for hydroprocessing and cracking hydrocarbons |
US9777228B2 (en) | 2015-06-30 | 2017-10-03 | Uop Llc | Process for cracking hydrocarbons to make diesel |
US9896627B2 (en) | 2015-10-14 | 2018-02-20 | Saudi Arabian Oil Company | Processes and systems for fluidized catalytic cracking |
US10870802B2 (en) | 2017-05-31 | 2020-12-22 | Saudi Arabian Oil Company | High-severity fluidized catalytic cracking systems and processes having partial catalyst recycle |
JP2020528347A (ja) * | 2017-07-28 | 2020-09-24 | ハーテーエー・ゲーエムベーハー・ザ・ハイ・スループット・イクスペリメンテイション・カンパニー | 0.1〜10秒の範囲の滞留時間で化学物質を触媒転換するための装置および方法 |
US10889768B2 (en) | 2018-01-25 | 2021-01-12 | Saudi Arabian Oil Company | High severity fluidized catalytic cracking systems and processes for producing olefins from petroleum feeds |
US11629298B2 (en) | 2020-05-14 | 2023-04-18 | Saudi Arabian Oil Company | Dual fluid catalytic cracking reactor systems and methods for processing hydrocarbon feeds to produce olefins |
US11434432B2 (en) | 2020-09-01 | 2022-09-06 | Saudi Arabian Oil Company | Processes for producing petrochemical products that utilize fluid catalytic cracking of a greater boiling point fraction with steam |
US11505754B2 (en) | 2020-09-01 | 2022-11-22 | Saudi Arabian Oil Company | Processes for producing petrochemical products from atmospheric residues |
US11332680B2 (en) | 2020-09-01 | 2022-05-17 | Saudi Arabian Oil Company | Processes for producing petrochemical products that utilize fluid catalytic cracking of lesser and greater boiling point fractions with steam |
US11230673B1 (en) | 2020-09-01 | 2022-01-25 | Saudi Arabian Oil Company | Processes for producing petrochemical products that utilize fluid catalytic cracking of a lesser boiling point fraction with steam |
US11230672B1 (en) | 2020-09-01 | 2022-01-25 | Saudi Arabian Oil Company | Processes for producing petrochemical products that utilize fluid catalytic cracking |
US11242493B1 (en) | 2020-09-01 | 2022-02-08 | Saudi Arabian Oil Company | Methods for processing crude oils to form light olefins |
US11352575B2 (en) | 2020-09-01 | 2022-06-07 | Saudi Arabian Oil Company | Processes for producing petrochemical products that utilize hydrotreating of cycle oil |
CN116196848A (zh) * | 2021-12-01 | 2023-06-02 | 中国石油天然气股份有限公司 | 一种原料油和轻烃催化转化的装置和方法 |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4116814A (en) * | 1977-07-18 | 1978-09-26 | Mobil Oil Corporation | Method and system for effecting catalytic cracking of high boiling hydrocarbons with fluid conversion catalysts |
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 |
US4814067A (en) * | 1987-08-11 | 1989-03-21 | Stone & Webster Engineering Corporation | Particulate solids cracking apparatus and process |
US4873389A (en) * | 1988-08-04 | 1989-10-10 | Mobil Oil Corp. | Conversion of light olefins to gasoline using low-temperature catalyst regeneration |
US5009769A (en) * | 1989-02-06 | 1991-04-23 | Stone & Webster Engineering Corporation | Process for catalytic cracking of hydrocarbons |
FR2667609B1 (fr) * | 1990-10-03 | 1993-07-16 | Inst Francais Du Petrole | Procede et dispositif de craquage catalytique en lit fluide a courant descendant. |
US5126036A (en) * | 1991-11-05 | 1992-06-30 | Mobil Oil Corporation | Process and apparatus for split feed of spent catalyst to high efficiency catalyst regenerator |
US5435906A (en) * | 1992-08-20 | 1995-07-25 | Stone & Webster Engineering Corporation | Process for catalytically cracking feedstocks paraffin rich comprising high and low concarbon components |
CN1089641A (zh) * | 1992-08-20 | 1994-07-20 | 史东及韦伯斯特工程公司 | 含高和低康拉逊残炭组分的富石蜡原料的催化裂化方法 |
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 |
-
1999
- 1999-12-14 FR FR9915747A patent/FR2802211B1/fr not_active Expired - Lifetime
-
2000
- 2000-11-28 US US10/149,597 patent/US7220351B1/en not_active Expired - Lifetime
- 2000-11-28 WO PCT/FR2000/003315 patent/WO2001044409A1/fr not_active Application Discontinuation
- 2000-11-28 ES ES00983393T patent/ES2359623T3/es not_active Expired - Lifetime
- 2000-11-28 DE DE60045600T patent/DE60045600D1/de not_active Expired - Lifetime
- 2000-11-28 EP EP00983393A patent/EP1242569B1/de not_active Expired - Lifetime
- 2000-11-28 JP JP2001545489A patent/JP4671089B2/ja not_active Expired - Lifetime
- 2000-11-28 AT AT00983393T patent/ATE497527T1/de active
-
2002
- 2002-06-11 MX MXPA02005794A patent/MXPA02005794A/es active IP Right Grant
- 2002-06-13 ZA ZA200204751A patent/ZA200204751B/en unknown
Non-Patent Citations (1)
Title |
---|
See references of WO0144409A1 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104245892A (zh) * | 2012-03-20 | 2014-12-24 | 沙特***石油公司 | 用于处理原油的集成加氢处理和流体催化裂化 |
CN104245892B (zh) * | 2012-03-20 | 2016-10-12 | 沙特***石油公司 | 用于处理原油的集成加氢处理和流体催化裂化 |
Also Published As
Publication number | Publication date |
---|---|
FR2802211B1 (fr) | 2002-02-01 |
MXPA02005794A (es) | 2003-01-28 |
JP2003517088A (ja) | 2003-05-20 |
DE60045600D1 (de) | 2011-03-17 |
ZA200204751B (en) | 2003-06-13 |
JP4671089B2 (ja) | 2011-04-13 |
US7220351B1 (en) | 2007-05-22 |
ES2359623T3 (es) | 2011-05-25 |
ATE497527T1 (de) | 2011-02-15 |
FR2802211A1 (fr) | 2001-06-15 |
WO2001044409A1 (fr) | 2001-06-21 |
EP1242569B1 (de) | 2011-02-02 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP1242569B1 (de) | Verfahren und vorrichtung zur katalytischen spaltung mit aufwärts- und abwärtsbetriebenen parallelen reaktoren | |
EP1800742B1 (de) | Reaktor mit zwei fluidisierbaren Reaktionsstufen und einem integrierten Gas/Feststofftrennsystem | |
EP0208609B1 (de) | Verfahren und Einrichtung für das katalytische Kracken von Kohlenwasserstoffen mit Kontrolle der Reaktionstemperatur | |
EP1170355B1 (de) | Verfahren und Einrichtung zum Cracken von Kohlenwasserstoffen in zwei aufeinanderfolgenden Reaktionstufen | |
EP0171330B1 (de) | Verfahren und Vorrichtung für die katalystische Wirbelschichtspaltung | |
EP1656989A1 (de) | Einrichtung und Verfahren zur katalytischen Spaltung von zwei unterschiedlichen Kohlenwasserstoffeinsätzen | |
EP2627736B1 (de) | Mehrstufiges rissbildungs- und ablösungsverfahren in einer fcc-einheit | |
FR2953851A1 (fr) | Procede de craquage catalytique avec maximisation des bases gazoles | |
EP1131389B1 (de) | Verfahren und einrichtung zum katalytischen cracken mit abwärts- und aufwärtsströmenden reaktoren | |
EP0489726B1 (de) | Verfahren und einrichtung zum dampfkracken von kohlenwasserstoffen in der wirbelschichtphase | |
FR2659346A1 (fr) | Procede de craquage avec oligomerisation ou trimerisation des olefines presentes dans les effluents. | |
FR2574422A1 (fr) | Perfectionnements aux procedes et dispositifs pour le craquage catalytique a l'etat fluide de charges d'hydrocarbures | |
EP0282371B1 (de) | Verfahren und Vorrichtung für das katalytische Kracken von Kohlenwasserstoffeinsätzen | |
EP0874880B1 (de) | Fluidkatalytisch krackverfahren und -einrichtung fur kohlenwasserstoffeinsätze | |
EP0663434A1 (de) | Fluidkatalytisch Krachverfahren für Kohlenwasserstoffeinsätze, insbesondere Einsätze mit hoher basischen Stickstoffgehalten | |
EP3897953A1 (de) | Umwandlung eines rohöls in ein wirbelbett mit zonen mit unterschiedlichen kontaktzeiten | |
EP0291408A1 (de) | Dampfspaltungsverfahren in einer Wirbelschicht-Reaktionszone | |
FR2770225A1 (fr) | Procede et dispositif de vaporisation selective des charges d'hydrocarbures en craquage catalytique | |
EP0265347A1 (de) | Verfahren und Vorrichtung für die katalytische Wirbelschichtspaltung von Kohlenwasserstoffeinsätzen | |
EP0322276A1 (de) | Verfahren und Einrichtung für das katalytische Kracken von schweren Einsätze, die eine zweite Wirbelschichtabstreifzone enthalten | |
FR2658833A1 (fr) | Procede de craquage a l'etat fluide d'une charge d'hydrocarbures. | |
FR3090683A1 (fr) | Conversion d’un brut pétrolier en lit fluidisé compartimenté | |
WO1991003527A1 (fr) | Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 20020715 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR |
|
AX | Request for extension of the european patent |
Free format text: AL;LT;LV;MK;RO;SI |
|
17Q | First examination report despatched |
Effective date: 20050329 |
|
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE TR |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: FG4D Free format text: NOT ENGLISH |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: EP |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: LANGUAGE OF EP DOCUMENT: FRENCH |
|
REF | Corresponds to: |
Ref document number: 60045600 Country of ref document: DE Date of ref document: 20110317 Kind code of ref document: P |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R096 Ref document number: 60045600 Country of ref document: DE Effective date: 20110317 |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: T3 |
|
REG | Reference to a national code |
Ref country code: GR Ref legal event code: EP Ref document number: 20110400656 Country of ref document: GR Effective date: 20110412 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: TRGR |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2359623 Country of ref document: ES Kind code of ref document: T3 Effective date: 20110525 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R081 Ref document number: 60045600 Country of ref document: DE Owner name: IFP ENERGIES NOUVELLES, FR Free format text: FORMER OWNER: INSTITUT FRANCAIS DU PETROLE, RUEIL-MALMAISON, HAUTS-DE-SEINE, FR Effective date: 20110331 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: PT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110602 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: CY Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110202 Ref country code: FI Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110202 |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FD4D |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110202 Ref country code: DK Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110202 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed |
Effective date: 20111103 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R097 Ref document number: 60045600 Country of ref document: DE Effective date: 20111103 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: MC Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20111130 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LI Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20111130 Ref country code: CH Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20111130 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20111128 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: TR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20110202 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: PLFP Year of fee payment: 16 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: PLFP Year of fee payment: 17 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: PLFP Year of fee payment: 18 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 20191127 Year of fee payment: 20 Ref country code: SE Payment date: 20191128 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 20191127 Year of fee payment: 20 Ref country code: IT Payment date: 20191122 Year of fee payment: 20 Ref country code: GR Payment date: 20191121 Year of fee payment: 20 Ref country code: FR Payment date: 20191128 Year of fee payment: 20 Ref country code: ES Payment date: 20191219 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: AT Payment date: 20191121 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GB Payment date: 20191128 Year of fee payment: 20 Ref country code: DE Payment date: 20200130 Year of fee payment: 20 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R071 Ref document number: 60045600 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: MK Effective date: 20201127 |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: PE20 Expiry date: 20201127 |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: MK07 Ref document number: 497527 Country of ref document: AT Kind code of ref document: T Effective date: 20201128 Ref country code: BE Ref legal event code: MK Effective date: 20201128 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20201127 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20210309 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20201129 |