US3776838A - Catalytic cracking of naphthas - Google Patents

Catalytic cracking of naphthas Download PDF

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US3776838A
US3776838A US00077480A US3776838DA US3776838A US 3776838 A US3776838 A US 3776838A US 00077480 A US00077480 A US 00077480A US 3776838D A US3776838D A US 3776838DA US 3776838 A US3776838 A US 3776838A
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naphtha
catalyst
cracking
zeolite
catalytic cracking
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D Youngblood
D Raynolds
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Texaco Inc
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Texaco Inc
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    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/02—Molecular sieve

Definitions

  • Gasoline is frequently blended from stocks, including naphtha, the octane rating of which has been increased through catalytic reforming. Both virgin and cracked stocks -may be upgraded by reforming operations. Catalytic reformers are usually operated to provide the desired octane improvement with the least conversion of gasoline to saturated butanes and lighter materials.
  • the gasoline blending pool is maintained by a variety of operations-isobutane and butenes, for example, are charged to alkylation units and light olefins are polymerized to provide high octane blending components while the catalytic cracking of gas oil augments the supply of naphtha as well as providing additional feed for alkylation and polymerization units.
  • hydrocracking provides additional quantities of gasoline blending naphthas, the heavy naphtha from hydrocracking often has a relatively low octane number.
  • catalytic cracking apparatus such as disclosed in U.S. Pats. 3,433,733 and 3,448,037, has been developed for use with these improved catalysts to take advantage of their unique properties.
  • This apparatus incorporates the concept of riser cracking wherein a substantial portion of the cracking takes place in elongated reaction zones or risers terminating in a tapered reactor containing a dense phase and a dilute phase of catalyst.
  • Naphtha is more diicult to crack than gas oil and up to the present time limited success has been obtained in cracking naphtha catalytically.
  • Traditional cracking catalyst such as silica-alumina, exhibited relatively poor selectivity and activity when employed to crack naphtha resulting in the formation of realtively large amounts of gas and coke and producing small amounts of desirable olens and aromatics.
  • U.S. 3,284,341 discloses a process for the catalytic cracking of naphtha with a silica-alumina catalyst to produce substantial quantities of olens and aromatics by maintaining the space velocity above about 4.5, the pressure betwen 0 and 20 p.s.i.g. and the reaction temperature betwen 1000 and 1200 F.
  • 889,714 discloses a process for the catalytic cracking of naphtha with type X or type Y crystalline aluminosilicates yielding substantial quantities of light hydrocarbons to serve as feed for petrochemical, polymer and alkylate manufacture and significant quantities of naphtha having an enhanced octane rating.
  • the development of methods for further enhancing the catalytic cracking of naphtha with zeolite cracking catalysts is highly desirable.
  • SUMMARY OF THE INVENTION Briey our invention is directed to the catalytic cracking with zeolite catalysts of naphtha boiling in the range of -450 F. to produce substantial quantities of naphtha having an octane rating signicantly higher than the low octane feed and also yielding substantial quantities of light hydrocarbons which may serve as feed for alkylate, polymer and petrochemical manufacture.
  • the feedstocks comprise a low octane fresh naphtha fraction and a recycle stream of full range or heavy naphtha recovered from the effluent from the catalytic cracking reactor.
  • a low octane naphtha and a recycle naphtha stream recovered from a catalytic cracking eiiiuent stream can be subjected to catalytic cracking with zeolite cracking catalysts in a fluid catalytic cracking unit employing a multiplicity of elongated reaction zones, hereinafter called risers, wherein the low octane naphtha is introduced into one of the risers and the recyle naphtha into a second riser to produce significant quantities of naphtha having an octane rating significantly higher than the low octane feed and also yielding substantial quantities of light hydrocarbons which may serve as feed for alkylate, polymer and petrochemical manufacture.
  • our invention contemplates a process for the catalytic cracking of naphtha with a zeolite cracking catalyst in a fluid catalytic cracking unit comprising a reactor, a regenerator and a multiplicity of elongated reaction zones, wherein said reactor contains a dense phase and a dilute phase of said catalyst and said elongated reaction zones terminate at said reactor, which comprises:
  • step (d) Passing the fraction from step (c) and a zeolite cracking catalyst through a second elongated reaction zone under naphtha cracking conditions
  • the catalyst phase into which the efiluent from either of the risers discharges may be either the dense phase or the dilute phase of catalyst in the reactor which leads to a number of optional embodiments incorporating various combinations or riser cracking and dense phase cracking, i.e., bed cracking.
  • the cracking of both the fresh naphtha and recycle naphtha is restricted to the risers by discharging the effluent from both risers into the dilute phase of catalyst in the reactor vessel.
  • the reactor vessel is utilized as a disengaging zone with little or no cracking taking place therein.
  • the recycle naphtha is subjected to further cracking in the dense catalyst phase. This is achieved by discharging the eiuent from the fresh naphtha riser into the dilute phase of catalyst and the jected only to riser cracking while the fresh -naphtha is cracked in both the riser and the dense phase of catalyst.
  • the eliiuent from the recycle naphtha riser is discharged directly into the dilute phase of catalyst in the reactor vessel while the elliuent from the fresh naphtha riser is discharged into the dense phase of catalyst, the vaporous reaction mixture from the fresh naphtha riser passes through this dense phase under catalytic cracking conditions effecting an additional conversion of 5 to 30 vol. percent and discharges into the dilute phase of catalyst.
  • both the fresh naphtha and the recycle naphtha are subjected to riser cracking and bed cracking by discharging the eiuent from both risers into the dense phase of catalyst.
  • the vaporous reaction mixture passes through the dense phase under catalytic cracking conditions to effect an additional conversion of each stream of 5 to 30 vol. percent and discharges into the dilute phase.
  • hydrocarbons boiling in the range of about to 450 F. comprise the fresh naphtha fedestock for this process.
  • Many refinery streams having low economic value may be upgraded by employing the process of our invention.
  • Useful feedstocks are usually highly parainic and include such light hydrocarbon fractions as low octane naphthas, Udex raffinate, low octane naphthas from thermal cracking or hydrocracking operations and straight runs naphthas.
  • the term low octane' fresh naphtha refers to these useful feedstocks.
  • the recycle naphtha is obtained from the efiiuent stream from the catalytic cracking unit usually by means of fractionation.
  • This recycle stream may either be a full range naphtha, i.e., having an initial boiling point (IBI) of about 100-120 F. and an end point- (EP)'of about S50-450 F. or a heavy naphtha, i.e., having an IBP of about 22S-275 F. and an EP of about 350-450 F.
  • IBI initial boiling point
  • EP end point-
  • a heavy naphtha i.e., having an IBP of about 22S-275 F. and an EP of about 350-450 F.
  • the term boiling between 100 and 450 F. is used to include the boiling range of a full range naphtha as well as a heavy naphtha.
  • Products from the process of our invention include naphthas with improved octane ratings, and hydrocarbons boiling below the initial boiling point of the feed which find particular utility as feed streams for petrochemical, polymer gasoline, and alkylate manufacture.
  • the catalyst employedY in the instant invention is a cracking catalyst of the zeolite type as exemplified by those catalysts where the crystalline'aluminosilicate is dispersed in a siliceous matrix.
  • zeolites which may be usefully employed in the catalyst used in the process of our invention are aluminosilicates of type X or type X, including both the naturallyoccurring and synthetic varieties. Because - ⁇ of their extremely high activity these zcolitic materials are composited with a material possessing a substantially lower levelof catalytic activity, a siliceous matrix, which may be of the synthetic, semi-synthetic or natural type.
  • the composite crystalline zeolite catalyst comprises about 1 to 50 wt. percent zeolite, about 5 to 50 wt. percent alumina and the remainder silica.
  • the crystalline aluminosilicate portion of the catalyst composition is a natural or synthetic, type X or type Y, alkali metal, crystalline aluminosilicate which has been treated to replace all or at least a substantial portion of the original alkali metal ions with other ions such as hydrogen and/or a metal orcombination of metals such as barium, calcium, magnesium, manganese or rare earth metals, for example, cerium, lanthanum, neodyminum, praseodymium, samarium and ⁇ yttrium.
  • the crystalline zeolites contemplated above may be represented by the formula y Mg/IIOI AIZOgIxSlOZyHZO y where M represents hydrogen or a metal, n its valance, x has a value ranging from 2 to 10 and y ranges from to 10, in dehydrated zeolites, y will be substantially 0.
  • the crystalline zeolites are either natural or synthetic zeolite X or zeolite Y.
  • M is selected from the group consisting of hydrogen, calcium, magnesium and the rare earth metals.
  • the operating conditions contemplated herein for either the fresh naphtha riser or the recycle naphtha riser include a temperature of 750-1300 F., preferably 900-1000 F., a conversion per pass of 25-80 volume percent, preferably 30-60 volume percent, and a vapor velocity of 15-50 feet/ second, preferably 20-40 feet/ second.
  • Operating conditions in the fluidized bed in the reactor include a temperature of SOO-1150o F., a conversion of -30 volume percent, and a vapor velocity 0f 0.5-4 feet/second preferably 1.3-2.2 feet/second.
  • conversion, naphtha conversion, percent conversion or 115 F. conversion (see Table II) is defined as 100 minus the volume percent of product boiling above 115 F.
  • the process is conducted in a iluid catalytic cracking unit employing two risers with fresh naphtha being introduced into one while a recycle naphtha stream introduced into the other.
  • the eflluents from both risers are discharged into the iiuidized bed of catalyst in the reactor so that both feed streams are subjected to riser cracking and bed cracking.
  • the resultant catal /st-in-naphtha vapor passes up riser 12 to reactor 16.
  • Reactor 16 contains a bed of catalyst 18 referred to as the dense phase of catalyst and a vapor space 20 above the catalyst bed which functions as a catalyst disengaging space and is referred to as the dilute phase of catalyst.
  • the eluent from riser 12 discharges into the dense bed of catalyst passing upward through the densev phase of cracking catalyst 18 effecting further conversion of the fresh naphtha stream.
  • Eflluent gases containing the cracked products pass from the cyclone separators through line 32 to fractionator section 34 wherein the vapor mixture is separated into various product streams.
  • These products include: (1) a stream of C4 and lighter hydrocarbons passing through line 36, (2) a light naphtha side stream passing through line 38, (3) a heavy naphtha side stream recovered as a product through line 40, passed to line 22 as a recycle naphtha stream or combined with the light naphtha in line 38 to produce a full range naphtha in line 42 which may be passed through line 24 as a recycle naphtha stream and (6) a bottoms product recovered through line 44.
  • Catalyst is withdrawn from the bottom of the reactor through slide valves 46 and 48 passing into stripping zone 50 containing Ambers 52. Steam introduced into the lower portion of stripper 50 removes adsorbed and entrained hydrocarbons from the catalyst as it passes through the stripper. Stripped catalyst is withdrawn from the bottom of stripping zone 50 through spent catalyst standpipe 54 discharging into regenerator 56.
  • the zeolite catalyst forms a dense bed Iwithin regenerator 56 and is regenerated therein by contacting it with air to remove the car-bon from the catalyst surface. Regenerated catalyst is withdrawn from the bottom of regenerator 56 through standpipes 14 and 30 to supply the hot regenerated catalyst to risers 12 and 28 as hereinbefore described.
  • a series of five runs is performed with a uidized catalytic cracking unit having two feed risers. In the rst run of the series only one of the risers is employed, while both risers are utilized in the remaining runs.
  • the same zeolite-containing cracking catalyst is employed in all runs.
  • the catalyst consists of a 1:1 weight blend of a zeolite cracking catalyst and a high alumina amorphous cracking catalyst.
  • the zeolite catalyst comprises 18 wt. percent of a type X zeolite in a silica-alumina matrix and has a rare earth content of about 2.9 Wt. percent.
  • the amorphous silica-alumina catalyst has a high alumina content, a surface area of about m.2/g. and pore volume of about 0 .4 cc./g.
  • the fresh naphtha feed is either a heavy straight run gasoline or a heavy Udex raffinate having properties as set forth in Table I below.
  • the gasoline served as the fresh feed in Runs 1, 2 and 3 whles: the Udex raffinate was the fresh feed in Runs 4 an TABLE I.-FEEDSTOCK ANALYSIS Heavy straight Heavy run Udex gasoline ranate Annina p0in1;, F 12222 isig esearc oeane, cllear 50. 6 17.0
  • Run 1 is a once-through operation without any recycle naphtha being employed. In the remaining four runs a naphtha stream recovered from the effluent is recycled to the unit. In all instances the feeds are introduced to a riser in the catalytic cracking unit and the eluents discharge into the dilute phase of catalyst in the reactor vessel so that substantially all of the catalytic cracking is taking place in the risers with the reactor vessel acting mainly as a disengaging space. In Run 1 only one of the risers is utilized since no recycle is employed. The heavy Straight run gasoline is introduced to the riser together with the cracking catalyst.
  • Run 2 both risers are employed with heavy straight run gasoline passing through one riser and a heavy recycle naphtha having a 250 F. IBP passing through the other.
  • Run 3 also is a recycle operation and is in all respects the same as Run 2 except that the recycle naphtha is a full range naphtha having a 115 F. IBP. This full range naphtha is a depentanized naphtha.
  • the heavy Udex raiiinate serves as the fresh feed and the recycle naphtha is a heavy naphtha having a 250 F. IBP.
  • Runs 4 and 5 are the same in all respects except that the riser temperature in Run is higher than that in Run 4.
  • the operating conditions and the results obtained in the series of runs are set forth to form a rst mixture consisting essentially of said fresh naphtha stream and said iirst portion of catalyst,
  • Run 1 shows that the research octane of a heavy straight ⁇ run gasoline can be substantially increased from 74.8 to 89.8 in a once-through catalytic cracking operation.
  • alkylate produced by alkylat- Runs 2 and 3 show that by recycling either a heavy 45 naphtha or a full range naphtha substantial increases in the research octane of the naphtha can be achievedfrom 74.8 to 94.2 and 98.4, respectively.
  • higher yields of valuable C3C4 petrochemical feed stocks are produced in a recycle operation.
  • naphtha octanes can be significantly improved by recycling fullrange naphtha over those obtained with heavy naphtha recycle.
  • Runs 4 and 5 demonstrate that when two different riser heavy naphtha recycle, the octane of the low octane feed can be increased signilicantly-from 55.0 to 92.2 and 90.6, respectively.
  • the lower riser temperature operation of Run 4 produces higher yields of higher octane gasoline than obtained in Run 5.
  • Run 5 With the higher riser temperature of Run 5 more C3-C4 petrochemical feed stocks having a higher olefin content are produced than in Run 4.
  • a process for the catalytic cracking of naphtha with zeolite cracking catalyst in a iiuid catalytic cracking unit comprising a reactor, a regenerator and a multiplicity of elongated reaction zones, wherein said reactor contains a dense phase and a dilute phase of said catalyst and said elongated reaction zones terminate at said reactor, which comprises: j
  • step (e) introducing the fraction from step (d) and a second portion of freshly-regenerated zeolite cracking catalyst into a second elongated reaction zone to form a second mixture consisting essentially of said fraction from step (d) and said second portion of catalyst,
  • naphtha cracking conditions of steps (a) and (d) include a temperature of 750-1300-o F., a conversion of 25-80 volume percent and a vapor velocity of 15-50 feet/second.
  • a process according to claim 2 wherein the effluent from the second elongated reaction zone is discharged into a dilute phase of catalyst and the eiuent from the first elongated reaction zone is discharged into a dense phase of catalyst, said vaporous reaction mixture from said first elongated reaction zone passing through said dense phase under catalytic cracking conditions elTecting an additional conversion of 5-30 volume percent and discharging into a dilute phase of catalyst.
  • catalytic cracking conditions in the dense phase include a temperature of 800-1150" F. and a vapor velocity of 0.5-4 eet/ second.
  • a process according to claim 5 wherein the catalytic cracking conditions in the dense phase include a ternperature of 8001150 F. and a vapor velocity of 0.5-4 feet/second.
  • a process according to claim 6 wherein the catalytic cracking conditions in the dense phase include a temperature of 800-1150 'F. and a Vapor velocity of 0.5-4 feet/second.

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  • Engineering & Computer Science (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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AT (1) AT310909B (fr)
AU (1) AU458343B2 (fr)
BE (1) BE773099A (fr)
CA (1) CA966795A (fr)
DE (1) DE2148121C3 (fr)
ES (1) ES395549A1 (fr)
FI (1) FI54139C (fr)
FR (1) FR2111650B1 (fr)
GB (1) GB1367306A (fr)
IT (1) IT945974B (fr)
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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3894936A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3894935A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3923641A (en) * 1974-02-20 1975-12-02 Mobil Oil Corp Hydrocracking naphthas using zeolite beta
US3928172A (en) * 1973-07-02 1975-12-23 Mobil Oil Corp Catalytic cracking of FCC gasoline and virgin naphtha
US4067798A (en) * 1976-02-26 1978-01-10 Standard Oil Company (Indiana) Catalytic cracking process
US4148710A (en) * 1977-06-13 1979-04-10 Occidental Oil Shale, Inc. Fluidized bed process for retorting oil shale
US5310477A (en) * 1990-12-17 1994-05-10 Uop FCC process with secondary dealkylation zone
US5565090A (en) * 1994-11-25 1996-10-15 Uop Modified riser-reactor reforming process
WO1999057230A1 (fr) * 1998-05-05 1999-11-11 Exxon Research And Engineering Company Procede de craquage catalytique fluide a deux phases pour la production selective d'olefines c2-c¿4?
US6036845A (en) * 1998-05-04 2000-03-14 Uop Llc Modified riser-reactor reforming process with prereactor
US6238548B1 (en) 1999-09-02 2001-05-29 Uop Llc FCC process for upgrading gasoline heart cut
US6616899B1 (en) 1998-06-08 2003-09-09 Uop Llc FCC process with temperature cracking zone
US20110240520A1 (en) * 2006-07-13 2011-10-06 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjunction with fcc unit operations
WO2011121613A2 (fr) 2010-03-31 2011-10-06 Indian Oil Corporation Ltd Procédé de craquage simultané de charges d'hydrocarbures légères et lourdes, et système associé
US8808535B2 (en) 2010-06-10 2014-08-19 Kellogg Brown & Root Llc Vacuum distilled DAO processing in FCC with recycle
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
FR3104604A1 (fr) 2019-12-16 2021-06-18 IFP Energies Nouvelles Dispositif et procédé de production d’oléfines légères et d’aromatiques par craquage catalytique.
FR3104605A1 (fr) 2019-12-16 2021-06-18 IFP Energies Nouvelles Dispositif et procédé de production d’oléfines légères par craquage catalytique et vapocraquage.
US20210300843A1 (en) * 2018-08-03 2021-09-30 Neste Oyj Method to produce bio-renewable propylene from oils and fats

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3928172A (en) * 1973-07-02 1975-12-23 Mobil Oil Corp Catalytic cracking of FCC gasoline and virgin naphtha
US3894936A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3894935A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3923641A (en) * 1974-02-20 1975-12-02 Mobil Oil Corp Hydrocracking naphthas using zeolite beta
US4067798A (en) * 1976-02-26 1978-01-10 Standard Oil Company (Indiana) Catalytic cracking process
US4148710A (en) * 1977-06-13 1979-04-10 Occidental Oil Shale, Inc. Fluidized bed process for retorting oil shale
US5310477A (en) * 1990-12-17 1994-05-10 Uop FCC process with secondary dealkylation zone
US5565090A (en) * 1994-11-25 1996-10-15 Uop Modified riser-reactor reforming process
US5770045A (en) * 1994-11-25 1998-06-23 Uop Modified riser-reactor reforming process
US6036845A (en) * 1998-05-04 2000-03-14 Uop Llc Modified riser-reactor reforming process with prereactor
WO1999057230A1 (fr) * 1998-05-05 1999-11-11 Exxon Research And Engineering Company Procede de craquage catalytique fluide a deux phases pour la production selective d'olefines c2-c¿4?
US6106697A (en) * 1998-05-05 2000-08-22 Exxon Research And Engineering Company Two stage fluid catalytic cracking process for selectively producing b. C.su2 to C4 olefins
US6616899B1 (en) 1998-06-08 2003-09-09 Uop Llc FCC process with temperature cracking zone
US6238548B1 (en) 1999-09-02 2001-05-29 Uop Llc FCC process for upgrading gasoline heart cut
US20110240520A1 (en) * 2006-07-13 2011-10-06 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjunction with fcc unit operations
WO2011121613A2 (fr) 2010-03-31 2011-10-06 Indian Oil Corporation Ltd Procédé de craquage simultané de charges d'hydrocarbures légères et lourdes, et système associé
US9433912B2 (en) 2010-03-31 2016-09-06 Indian Oil Corporation Limited Process for simultaneous cracking of lighter and heavier hydrocarbon feed and system for the same
US8808535B2 (en) 2010-06-10 2014-08-19 Kellogg Brown & Root Llc Vacuum distilled DAO processing in FCC with recycle
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
US20210300843A1 (en) * 2018-08-03 2021-09-30 Neste Oyj Method to produce bio-renewable propylene from oils and fats
US11981633B2 (en) * 2018-08-03 2024-05-14 Neste Oyj Method to produce bio-renewable propylene from oils and fats
FR3104604A1 (fr) 2019-12-16 2021-06-18 IFP Energies Nouvelles Dispositif et procédé de production d’oléfines légères et d’aromatiques par craquage catalytique.
FR3104605A1 (fr) 2019-12-16 2021-06-18 IFP Energies Nouvelles Dispositif et procédé de production d’oléfines légères par craquage catalytique et vapocraquage.
EP3839013A1 (fr) 2019-12-16 2021-06-23 IFP Energies nouvelles Dispositif et procédé de production d'oléfines légères et d'aromatiques par craquage catalytique
EP3839012A1 (fr) 2019-12-16 2021-06-23 IFP Energies nouvelles Dispositif et procédé de production d oléfines légères par craquage catalytique et vapocraquage

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NL7113477A (fr) 1972-04-05
DE2148121C3 (de) 1974-02-14
DE2148121A1 (de) 1972-04-06
FR2111650A1 (fr) 1972-06-09
AU3323971A (en) 1973-03-15
JPS51962B1 (fr) 1976-01-13
ES395549A1 (es) 1973-12-16
DE2148121B2 (de) 1973-06-28
CA966795A (en) 1975-04-29
AT310909B (de) 1973-10-25
GB1367306A (en) 1974-09-18
BE773099A (fr) 1972-03-24
ZA715955B (en) 1973-01-31
FI54139B (fi) 1978-06-30
IT945974B (it) 1973-05-10
FR2111650B1 (fr) 1974-08-19
FI54139C (fi) 1978-10-10
AU458343B2 (en) 1975-02-27

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