EP2291489B1 - Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers - Google Patents

Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers Download PDF

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Publication number
EP2291489B1
EP2291489B1 EP09766003A EP09766003A EP2291489B1 EP 2291489 B1 EP2291489 B1 EP 2291489B1 EP 09766003 A EP09766003 A EP 09766003A EP 09766003 A EP09766003 A EP 09766003A EP 2291489 B1 EP2291489 B1 EP 2291489B1
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EP
European Patent Office
Prior art keywords
riser
catalyst
catalytic cracking
principal
cracking unit
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EP09766003A
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German (de)
English (en)
French (fr)
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EP2291489A2 (fr
Inventor
Frédéric FEUGNET
Thierry Gauthier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • 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
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • C10G11/182—Regeneration
    • 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present invention is in the field of catalytic cracking of petroleum fractions, more particularly so-called "heavy" cuts.
  • the main FCC (fluidized catalytic cracking abbreviation) feedstock of heavy cuts is generally a hydrocarbon or hydrocarbon mixture containing essentially (i.e., at least 80%) higher boiling molecules. at 340 ° C.
  • This feed contains quantities of metals (Ni + V) limited generally less than 50 ppm, preferably less than 20 ppm, and a hydrogen content in general greater than 11% by weight, typically between 11.5% and 14.5% and preferably between 11.8% and 13%. It is also preferable to limit the nitrogen content to below 0.5% by weight.
  • CCR carbon conradson
  • These heavy cuts can in particular come from atmospheric distillation, vacuum distillation, hydrocracking unit or deasphalting.
  • the objective of the catalytic cracking unit of a refinery is to produce gasoline bases, ie cuts having a distillation range of between 35 ° C and 250 ° C. More and more this primary objective is accompanied by a new objective which is the production of light olefins, essentially ethylene and propylene.
  • Gasoline is produced by cracking the heavy load in the main reactor (called the main riser in the rest of the text due to the upward flow of the catalyst and the slender form of this reactor, in accordance with the terminology of the person skilled in the art)
  • the co-production of propylene is, for its part, generally obtained by recycling in an additional reactor, called additional riser, part of the gasoline cut produced by the unit. catalytic cracking or from an equivalent charge such as C5, C6, C7 and C8 oligomers.
  • riser principal noted (1) to designate the riser oriented to the production of gasoline
  • secondary riser noted (2) to designate the riser dedicated to the production of propylene
  • a conventional riser operating under conditions of production of essence operates with a catalyst on charge ratio of between 4 and 15, and preferably between 5 and 10, and with riser outlet temperatures (denoted TS) of between 510 and 580 ° C., and preferably between 520 ° C. and 570 ° C. ° C.
  • the secondary riser therefore operates with operating conditions much more severe than the main riser.
  • Both risers are fed with regenerated catalyst, whose temperature results from the combustion of the coke.
  • the amount of catalyst circulating in the unit therefore depends on the regeneration temperature.
  • a change in the operation of the first riser can therefore change the regeneration temperature and directly affect the operation of the second riser.
  • the present invention makes it possible to implement an independent and optimized control of the operating conditions of each riser by independent control of the catalyst inlet temperatures in the two risers.
  • cat cooler means the heat exchanger external to the regeneration zone for cooling the catalyst taken from a point of said zone and reintroduced after cooling to another point in the regeneration zone.
  • the "cat cooler” or “coolers” used in the present invention differ from a “cat cooler” according to the prior art in that it (s) has (s) at least one specific output that brings the cooled catalyst directly to one of the risers.
  • This application does not describe the means for achieving independent and optimized control of the temperature of each of the risers.
  • International demand WO-A-0144409 also discloses a fluidized bed or fluidized catalytic cracking process associating the cracking of a hydrocarbon feedstock under conventional cracking conditions in a riser with the cracking of a recycle of riser products in a dropper working under severe cracking conditions to maximize the production of gasoline while maximizing the production of olefins and in particular propylene by recycling dropper gasoline produced riser.
  • Requirement US Patent 4584090 discloses a catalytic cracking unit for the production of liquid fuels comprising a regeneration zone in two consecutive steps and a two-riser reaction zone for parallel cracking of a heavy fraction of a crude oil residue and a light fraction of the crude oil residue in which gasoline production is maximized by recycling the LCO and HCO fractions from the separation of the cracking products.
  • the figure 1 represents a diagram of the catalytic cracking unit according to the invention with two risers and two cat coolers, each of the risers being fed with catalyst directly from the cat cooler dedicated to the corresponding riser.
  • the invention therefore consists of a process for the production of propylene gasoline and co-production using a new configuration of the catalytic cracking unit which makes it possible to independently control the temperature conditions and the contact time of the main riser fed. by a conventional load dedicated to the production of gasoline and working under moderate severity conditions on the one hand, and the secondary riser fueled by a gasoline or equivalent cut, dedicated to the production of propylene and working under conditions of high severity. somewhere else.
  • the figure 1 shows a preferred implementation scheme of the invention
  • the main riser (1) is fed with catalyst from the regeneration zone which has been cooled in a "cat cooler” (7), called “cat cooler” principal, and directly sent out of said "cat cooler” to the base of the main riser (1) via the transfer line (10).
  • the catalyst circuit passing through the regeneration zone, the cat cooler (7), the transfer line (10) and the main riser (1) is called the main circuit.
  • the secondary riser (2) is fed with catalyst from the regeneration zone which has been cooled in a "cat cooler” (6) separate from the main “cat cooler” (7), referred to as “secondary cat cooler” (6). , and directly sent out of said secondary “cat cooler” at the base of the secondary riser (2) via the transfer line (12).
  • the catalyst circuit passing through the regeneration zone, the "cat cooler” (6), the transfer line (12), and the secondary riser (2) is called secondary circuit.
  • the main riser (1) is optimized for working at moderate severity conditions, and the secondary riser (2) at high severity conditions.
  • the present invention is compatible with any type of configuration of the regeneration zone, whether this zone is a single stage or two stages working in series.
  • the secondary riser works with a contact time between 50 and 500 ms, and with a catalyst flow of between 150 kg / m2.s and 600 kg / m2.s (ms is the abbreviation of millisecond or 10 -3 s ).
  • the catalytic cracking unit according to the invention has a first riser said main riser (1) treating a conventional vacuum distillate type charge or hydro-treated residue or not and a second riser said secondary riser (2) treating a light load in view of olefin production.
  • This light load consists of a portion of the gasoline produced by the cracking unit itself, which is then recycled to the base of the secondary riser (2) and any cut whose distillation range is between 35 ° C and 250 ° C, such as oligomers C5, C6, C7 and C8.
  • cat cooler means an exchanger external to the regeneration zone, working in a fluidized bed and allowing the cooled catalyst to be cooled in the regeneration zone before being reintroduced into the reaction zone, via a line bringing the cooled catalyst out of the reactor.
  • cat cooler at the base of the riser.This transfer line is noted (10) for feeding the main riser (1) and denoted (12) for feeding the secondary riser (2).
  • the catalyst is generally taken from the second stage at a temperature between 715 and 800 ° C, and preferably close to 750 ° C.
  • the catalyst is taken from said stage at a temperature of between 650 ° C. and 780 ° C., and preferably close to 750 ° C.
  • the solid gas separation in the reaction zone can be carried out by any system known to those skilled in the art such as those described in the patent application. FR06 / 10982 .
  • the catalyst recovered after the solid-gas separation system is sent to a stripping zone (8) and then to the regeneration zone via a so-called standpipe pipe (5) in which the catalyst circulates with a density of between 450 and 600 kg / m3.
  • the catalyst system used for this invention contains at least one base zeolite usually dispersed in a suitable matrix such as, for example, alumina, silica or silica-alumina, to which at least one zeolite with a shape selectivity can be added. .
  • zeolite Y The most commonly used basic zeolite is zeolite Y, but another zeolite can be advantageously used, alone or as a mixture with zeolite Y.
  • the catalyst may especially comprise, in the process according to the invention, at least one zeolite having a shape selectivity, said zeolite comprising silicon and at least one element selected from the group consisting of aluminum, iron, gallium, phosphorus, boron and preferably aluminum.
  • the zeolite having a shape selectivity can be of one of the following structural types: MEL (eg ZSM-11), MFI (eg ZSM5), NES, EUO, FER, CHA.
  • the proportion of zeolite having a shape selectivity with respect to the total amount of zeolite may vary depending on the charges used and the spectrum of the desired products. In the present invention, from 2% to 60%, preferably from 3% to 40%, and more preferably from 3% to 30% by weight of zeolite (s) having a shape selectivity are used.
  • Example 1 and 2 are according to the prior art, Example 3 is according to the invention.
  • the catalyst is a zeolite Y additive of 10% by weight of ZSM5.
  • the light cut recycled to the secondary riser is a C6 + -220 ° C cut from the main heavy duty conversion riser, recycled to 50% of all gasoline produced in the two-riser cracking unit. .
  • This example illustrates the case of a catalytic cracking unit with 2 risers and 1 "cat cooler", and a 2-stage regeneration zone, the riser 1 being optimized for gasoline production, and the non-optimized riser 2 and fed by a portion of the catalytic gasoline from the main riser.
  • the decrease in this ratio reflects the fact that the gain in propylene does not compensate for the associated increase in dry gases. Dry gases are not recoverable products and their production is to be minimized.
  • This example according to the invention illustrates the case of a catalytic cracking unit with two risers, each having a dedicated "cat cooler” that allows it to operate under optimized conditions.
  • the 2-stage regeneration zone is the same as in Examples 1 and 2.
  • This case illustrates the invention which allows to independently adjust the C / O of each riser.
  • a C / O of 25 is reached for the main riser, and a C / O of 8 is maintained in the main riser.
  • Reg1 temperatures of 681 ° C and reg2 of 732 ° C are found in the desired operating ranges and provide optimal catalyst regeneration.
  • the selectivity C3 / dry gas is maintained or even improved with a ratio of 1.60 against 1.56 for the conventional case.
  • the increase in dry gases in case 3 is therefore offset by the associated propylene gain.

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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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
EP09766003A 2008-06-17 2009-06-03 Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers Active EP2291489B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0803384A FR2932495B1 (fr) 2008-06-17 2008-06-17 Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers.
PCT/FR2009/000639 WO2009153441A2 (fr) 2008-06-17 2009-06-03 Dispositif de controle des conditions operatoires dans une unite de craquage catalytique a deux risers

Publications (2)

Publication Number Publication Date
EP2291489A2 EP2291489A2 (fr) 2011-03-09
EP2291489B1 true EP2291489B1 (fr) 2012-01-18

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Country Status (11)

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US (1) US8957267B2 (https=)
EP (1) EP2291489B1 (https=)
JP (1) JP5814115B2 (https=)
KR (1) KR101610052B1 (https=)
CN (1) CN102066528B (https=)
AT (1) ATE541915T1 (https=)
ES (1) ES2379938T3 (https=)
FR (1) FR2932495B1 (https=)
RU (1) RU2500790C2 (https=)
SA (1) SA109300382B1 (https=)
WO (1) WO2009153441A2 (https=)

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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.
CN102276402B (zh) * 2010-06-11 2013-12-04 中国石油化工股份有限公司 生产低碳烯烃的组合反应装置
JP5764214B2 (ja) * 2010-11-11 2015-08-12 宝珍 石 接触分解方法及び装置
US20130130889A1 (en) * 2011-11-17 2013-05-23 Stone & Webster Process Technology, Inc. Process for maximum distillate production from fluid catalytic cracking units (fccu)
US8895790B2 (en) 2013-02-12 2014-11-25 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products
US9428695B2 (en) 2013-02-12 2016-08-30 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products with product recycle
US9447332B2 (en) 2013-02-12 2016-09-20 Saudi Basic Industries Corporation Conversion of plastics to olefin and aromatic products using temperature control
FR3016370B1 (fr) * 2014-01-10 2017-06-16 Ifp Energies Now Procede de craquage catalytique permettant une valorisation amelioree des calories des fumees de combustion.
EP3167026B1 (en) * 2014-07-07 2019-05-15 Albemarle Europe Sprl. Alkylation process using a catalyst comprising cerium rich rare earth containing zeolites and a hydrogenation metal
US9981888B2 (en) * 2016-06-23 2018-05-29 Saudi Arabian Oil Company Processes for high severity fluid catalytic cracking systems
CA3054985C (en) * 2017-03-01 2022-03-01 Albemarle Europe Srl Alkylation process with improved octane number
US10954453B2 (en) 2018-05-02 2021-03-23 Technip Process Technology, Inc. Maximum olefins production utilizing multi-stage catalyst reaction and regeneration

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Also Published As

Publication number Publication date
KR20110034594A (ko) 2011-04-05
WO2009153441A3 (fr) 2010-02-25
ES2379938T3 (es) 2012-05-07
JP5814115B2 (ja) 2015-11-17
JP2011524453A (ja) 2011-09-01
FR2932495B1 (fr) 2011-03-25
EP2291489A2 (fr) 2011-03-09
RU2011101430A (ru) 2012-07-27
KR101610052B1 (ko) 2016-04-07
CN102066528A (zh) 2011-05-18
CN102066528B (zh) 2013-09-25
US20110178347A1 (en) 2011-07-21
RU2500790C2 (ru) 2013-12-10
FR2932495A1 (fr) 2009-12-18
ATE541915T1 (de) 2012-02-15
US8957267B2 (en) 2015-02-17
SA109300382B1 (ar) 2013-05-18
WO2009153441A2 (fr) 2009-12-23

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