US3784463A - Catalytic cracking of naphtha and gas oil - Google Patents

Catalytic cracking of naphtha and gas oil Download PDF

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US3784463A
US3784463A US00077479A US3784463DA US3784463A US 3784463 A US3784463 A US 3784463A US 00077479 A US00077479 A US 00077479A US 3784463D A US3784463D A US 3784463DA US 3784463 A US3784463 A US 3784463A
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catalyst
reaction zone
gas oil
elongated reaction
reactor
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D Reynolds
R Pratt
D Youngblood
D Bunn
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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

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  • Reis 5 7 ABSTRACT Low octane naphtha and fresh gas oil are catalytically cracked with a zeolite catalytic cracking catalyst in separate elongated reaction zones yielding a naphtha having an increased octane rating.
  • Recovering a naphtha fraction, particularly a heavy naphtha fraction, from the cracked product, and combining it with the fresh naphtha feed further enhances the octane rating of the naphtha product.
  • a cycle gas oil may be recovered from the reactor effluent and combined with the fresh naphtha feed or introduced into a separate (a third) elongated reaction zone to effect maximum recovery of naphthaand lighter stocks having improved product quality.
  • any of the feedstocks may be subjected to further cracking in a dense bed of the zeolite catalyst.
  • This invention relates to the catalytic cracking of hydrocarbons.
  • this invention relates to the fluid catalytic cracking of fresh gas oil and naphtha having a low octane rating and boiling in the range of IO450F.
  • Gasoline is frequently blended from stocks, including naphtha, the octane 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 isobutanes 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. Pat. Nos. 3,433,733 and 3,448,037, has been developed specifically for use with these improved catalysts.
  • This apparatus incorporates the concept of riser cracking wherein the feedstocks are cracked in elongated reaction zones or risers terminating in a tapered reactor containing a dense phase and dilute phase of catalyst.
  • a mixture of zeolite catalyst and gas oil passes through the riser under cracking conditions which are tailored to the particular feedstock and desired products. After passing through the riser further cracking of the feed can be achieved, if necessary, in the fluidized dense phase of catalyst in the reactor.
  • Naphtha is more difficult 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 relatively large amounts of gas and coke and producing small amounts of desirable olefins and aromatics.
  • U.S. Pat. No. 3,284,341 discloses a process for the catalytic cracking of naphtha with a silica-alumina. catalyst to produce substantial quantities of olefins and aromatics by maintaining the space velocity above about 4.5, the pressure between 0 and 20 psig and the reaction temperature between 1,000 and 1,200F.
  • our invention is directed to the catalytic cracking of gas oils boiling in the range of about 430-l,050lF. and naphthas boiling in the range of about l0O450F. to produce substantial quantities of naphtha having an octane rating significantly higher than that of the low octane naphtha feed and yielding substantial quantities of lighter hydrocarbons which may serve as feed for alkylate and petrochemical manufacture.
  • a fluid catalytic cracking unit having multiple risers and employing zeolite cracking catalysts has been found to offer particular utility for the catalytic cracking of such feed streams.
  • the naphtha and the gas oil are catalytically cracked in separate cracking zones under conditions specifically tailored to the particular feedstock.
  • a full range or heavy naphtha cut may be removed from the reactor effluent for recycling to the fresh naphtha cracking zone and a cycle gas oil may also be removed from the reactor effluent for introduction into the fresh naphtha cracking zone or into a separate (third) cracking zone to effect maximum recovery of naphtha and lighter stocks having improved product quality.
  • a cracking zone may be limited to an elongated reaction zone, also known as a riser, or a combination of an elongated reaction zone and the dense phase of catalyst in the reactor vessel.
  • FIG. I depicts a flow diagram of a preferred embodiment of the process of the invention
  • FIG. 2 depicts an apparatus for carrying out a preferred embodiment of the invention.
  • the octane rating of a low octane naphtha can be significantly improved by catalytically cracking it in a fluid catalytic cracking unit employing a multiplicity of elongated reaction zones, hereinafter called risers or riser conduits, wherein the low octane naphtha is introduced into one of the risers and fresh gas oil is introduced into a second riser.
  • risers or riser conduits a multiplicity of elongated reaction zones
  • our process contemplates a process for the catalytic cracking of naphtha and gas oil 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:
  • the catalyst phase into which the effluent from a particular riser 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 of riser cracking and dense phase cracking, i.e., bed cracking.
  • the cracking of both naphtha and gas oil 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 gas oil is subjected to further cracking in the dense catalyst phase. This is achieved by discharging the effluent from the naphtha riser into the dilute phase of catalyst and the effluent from the gas oil riser into the dense phase of catalyst, the vaporous reaction mixture from the gas oil riser passes through the dense phase of catalyst under catalytic cracking conditions effecting an additional conversion of 5 to 30 volume percent and discharges into the dilute phase of catalyst.
  • the gas oil is subjected only to riser cracking while the naphtha is cracked in both the riser and the dense phase of catalyst.
  • the effluent from the gas oil riser is discharged directly into the dilute phase of catalyst in the reactor vessel while the effluent from the naptha riser is discharged into the dense phase of catalyst, the vaporous reaction mixture from the naphtha riser passes through this dense phase under catalytic cracking conditions effecting an additional conversion of 5 to 30 volume percent and discharges into the dilute phase of catalyst.
  • the gas oil and the naphtha are both subjected to riser cracking and bed cracking by discharging the effluent 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 volume percent and discharges into the dilute phase.
  • a cycle gas oil is recovered from the effluent from the catalytic cracking unit and recycled to the unit wherein it is subjected to riser cracking in a third elongated reaction zone and bed cracking in the dense phase of catalyst in the reactor.
  • step (e) passing said fraction of step (e) and a zeolite cracking catalyst through a third elongated reaction zone under cycle gas oil cracking conditions
  • cycle gas oil may be recovered from the effluent from the catalytic cracking unit and recycled to the naphtha riser where it is subjected, together with the naphtha, to both riser and bed cracking. This will permit two more optional embodiments wherein the fresh gas oil is subjected to riser cracking only or a combination of riser and bed cracking.
  • a naphtha cut which may be either a full range naphtha, i.e., about a -450F. boiling range, or a heavy naphtha, i.e., about a 250450F. boiling range, may be removed from the reactor effluent and recycled for introduction into the naphtha riser wherein it is combined with the fresh naphtha and subjected to both riser and bed cracking.
  • Fresh gas oil is introduced into a separate riser.
  • the fresh naphtha and the recycle naphtha are subjected to both riser and bed cracking. With the fresh gas oil subjected either to riser cracking only or riser and bed cracking, two more additional embodiments are possible. The following additional steps relating to the naphtha recycle are added:
  • step (j) introducing the fraction from step (j) into the first elongated reaction zone effecting conversion of said fraction.
  • Two more optional embodiments envision two recycle streams, cycle gas oil and recycle naphtha, and the use of three risers. Both recycle streams are recovered from the reactor effluent as explained above in describing other embodiments.
  • the recycle naphtha is combined with fresh naphtha and the combined streams are passed through the naphtha riser and subjected to both riser and bed cracking.
  • the cycle gas oil is introduced to its own riser and is cracked in both the riser and the bed of catalyst in the reactor.
  • the fresh gas oil passes through a third riser and is subjected to riser cracking only in one embodiment or both riser and bed cracking in the other.
  • the fresh feedstocks for this process comprise naphtha and gas oil.
  • the naphtha feedstocks comprise hydrocarbons boiling in the range of about lOO-450F. and include many refinery streams having low economic value which may be upgraded through the process of our invention.
  • Useful naphtha feedstocks are usually highly paraffinic and include such light hydrocarbon fractions as low octane naphtha, aromatic solvent extraction raffinate, thermal cracked naphtha, coker naphtha, low octane naphtha from hydrocracking operations and straight run naphthas.
  • the term low octane fresh naphtha refers to these useful feedstocks. Because of the refractory quality of these naphtha feed streams, they must be subjected to more severe conditions than is the fresh gas oil feed if significant conversion is to be obtained.
  • the gas oil feed in our process comprises petroleum stocks boiling from about 430 to 1,050F. and comprises heavy atmospheric gas oil, light and heavy vacuum gas oils, gas oil from coking operations, vis-broken gas oil, deasphalted gas oil, decarbonized gas oil, hydrotreated gas oil, hydrocracked gas oil and solvent extracted gas oil. All of these feedstocks are petroleum stocks whose processing has not previously included fluid catalytic cracking and are commonly referred to, therefore, as virgin gas oils.
  • Products from the process of our invention include naphthas with improved octane ratings and hydrocarbons boiling below the initial boiling point of the naphtha feed which will find particular utility as feed streams for petrochemical and gasoline manufacture.
  • the catalyst employed in the instant invention is a cracking catalyst of the zeolite type as exemplified by those catalysts wherein a 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 those known as zeolite X and zeolite Y, including both the naturally occurring and synthetic varieties. Because of their extremely high activity, these zeolite materials are composited with a material processing a substantially lower level of catalytic activity, a siliceous matrix which may be of the synthetic, semi-synthetic or natural type.
  • the materials may include silica-alumina, silica-gel, silicaberyllia, silica-magnesia, silica-thoria or silica-zirconia which have been successfully employed heretofore.
  • the composite crystalline zeolite catalyst comprises about 1 to 50 weight percent zeolite, about 5 to 50 weight percent alumina and the remainder silica.
  • the crystalline aluminosilicate portion of the catalyst composition is a natural or synthetic, 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 or combination of metals such as barium, calcium, magnesium, manganese or rare earth metals, for example, cerium, lanthanum, neodymium, praseodymium, samarium and yttrium.
  • the crystalline zeolites contemplated above may be represented by the formula M21 0 1 A1203 I y H O where M represents hydrogen or a metal, n its valence, x has a value ranging from 2 to 10 and y ranges from 0 to Ml, in dehydrated zeolites y will be substantially O.
  • the preferred 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 cracking apparatus incorporates a stripping section be neath the dense fluid bed wherein entrained and adsorbed hydrocarbons are displaced from the catalyst by means of steam as the catalyst passes from the reactor to the regeneration vessel.
  • the catalyst is contacted with an oxygen-containing gas in the regenerator to effect combustion of at least a portion of the deposited coke.
  • the regenerated catalyst is then reintroduced into the bottom of the risers at a point where the feedstocks are introduced.
  • an apparatus such as depicted in FIG. 2 may be employed which is an improvement over the apparatus of Bunn et al.
  • this improved embodiment may be described as follows: in an apparatus for fluid catalytic cracking of a type comprising:
  • a reactor chamber having a tapered portion of greater diameter at the upper portion than at the lower h. means to withdraw solids from the lower portion of the reactor chamber and to discharge the same into the stripping chamber,
  • j. means to withdraw solids from the lower portion of the stripping chamber and to discharge the same into the regenerator chamber
  • k. means to introduce combustion gas into the lower portion of the regenerator chamber
  • m. means to withdraw regenerated catalyst from the regenerator chamber and to discharge the same into the inlet of the riser conduits
  • the first riser conduit may pass through the bottom wall of the reactor chamber, the second riser conduit through the side wall of the reactor chamber or the third riser conduit through the side wall of the reactor chamber.
  • the first riser conduit may terminate in the reactor chamber in an upwardly directed outlet, the second riser conduit in a downwardly directed outlet or the third riser conduit in a downwardly directed outlet.
  • the operating conditions contemplated herein include a temperature of 750-l ,300F., preferably 900-l ,000F., a conversion per pass of 25-80 volume percent, preferably 30-60 volume percent, and a vapor velocity of 15-50 feet/- second, preferably feet/second.
  • the operating conditions include a temperature of 840-l,lO0F., preferably 890l,000F., a conversion per pass of 30-80 volume percent, preferably 40-65 volume percent, and a vapor velocity of 15-50 feet/second, preferably 20-40 feet/second.
  • the operating conditions in this riser include a temperature of 800-l ,lF., preferably 850-l,00OF., a conversion per pass of 20-70 volume percent, preferably 30-50 volume percent, and a vapor velocity of 15-50 feet/- second, preferably 20-40 feet/second.
  • the operating conditions in the bed include a temperature of 800-l,l50F., a conversion of -30 volume percent and a vapor velocity of 0.5-4 feet/- second, preferably 1.3-2.2 feet/second.
  • FIG. 1 illustrates and exemplifies a means by which the process of the present invention may be practiced.
  • a heavy naphtha recycle is combined with fresh naphtha and introduced to one riser, fresh gas oil is fed to another riser and cycle gas oil to the third riser.
  • the combined naphtha streams and the cycle gas oil are subjected to both riser and bed cracking while the fresh gas oil only undergoes riser cracking.
  • the heavy naphtha is a cracked stream and is recovered from an effluent stream as described hereinafter.
  • These combined streams are introduced into riser 14 where they are brought into contact with hot regenerated zeolite cracking catalyst from standpipe 16.
  • the resulting suspension of catalyst-naphtha vapor passes up riser 14 into reactor 18.
  • the reactor contains a bed of catalyst 20 referred to as the dense phase of catalyst, and a vapor space 22 above the bed of catalyst which functions as a catalyst disengaging space and is referred to as the dilute phase of catalyst.
  • the effluent from riser l4 discharges into the lower portion of reactor 18 and passes upward through the dense phase of catalytic cracking catalyst 20 effecting further conversion of the combined naphtha streams.
  • a fresh gas oil stream is introduced through line 24 to riser 26 where it is contacted with regenerated zeolite cracking catalyst from standpipe 28.
  • the resultant catalyst-in-gas oil vapor passes up riser 26 to reactor 18 discharging into the dilute phase of catalyst 22 wherein the catalyst particles disengage from the vaporous reaction mixture and fall into the bed of catalyst 20.
  • An intermediate gas oil stream obtained from the effluent from the catalytic cracking unit as described hereinafter, passes through line 30 into riser 32 where it is contacted with hot regenerated zeolite cracking catalyst from standpipe 34.
  • the resultant suspension of catalyst-in-cycle gas oil vapor passes up riser 32 into reactor 18 discharging into the dense phase of catalyst 20.
  • the vapor mixture passes upwardly through the bed of catalyst effecting some further conversion of the cycle gas oil.
  • These products include: (I) a stream of C4 and lighter hydrocarbons passing through line 40, (2) a light naphtha side stream passing through line 42, (3) a heavy naphtha side stream recovered as a product through line 44 or recycled to the fresh naphtha feed line through line 12, (4) a light gas oil side stream passing through line 46, (5) an intermediate gas oil recovered through line 30 as a cycle gas oil stream and recycled as feed to the catalytic cracking unit, and (6) a heavy gas oil bottoms product recovered through line 43.
  • Catalyst is withdrawn from the bottom of the reactor through slide valves 50 and 52 passing into stripping zone 54 containing baffles 56. Steam is introduced into the lower portion of stripper 54 to remove adsorbed and entrained hydrocarbons from the catalyst as it passes through the stripper. Stripped catalyst is withdrawn from the bottom of the stripping zone through spent catalyst standpipe 5S and discharges into regen erator 60. The catalyst forms a dense bed within regenerator 160 and is regenerated therein by contacting it with air to remove the carbon from the catalyst surface. Regenerated catalyst is withdrawn from the bottom of regenerator 60 through standpipes 16, 28 and 34 to supply the hot regenerated catalyst to risers 14, 26 and 32, respectively, as hereinbefore described.
  • FIG. 1 The process described above and illustrated in FIG. 1 may be conducted in the apparatus depicted in FIG. 2.
  • those items identified by numbers with prime notations designate corresponding portions of the equipment illustrated in FIG. 1 by the same numbers but without the prime notation. Additional numbers are employed in FIG. 2 to designate portions of the apparatus not illustrated or detailed in FIG. 1.
  • the charge stocks, fresh naphtha and recycle naphtha, cycle gas oil and fresh gas oil in lines 10', 30' and 24, respectively, are introduced into risers 14', 32 and 26', respectively, where they are contacted with zeolite cracking catalyst from standpipes 16', 34 and 28', respectively.
  • the mixtures of oil and catalyst pass through their respective risers discharging into reactor 18' where risers 26' and 32 terminate in downwardly directed outlets 19.
  • the serrated edge provides smooth flow of the effluent from the risers, particularly when the dense bed level 21 fluctuates near the downwardly projecting portion of the riser.
  • the fresh gas oil will be only riser cracked while the cycle gas oil will be riser cracked and bed cracked. Dropping the level below the outlet of riser 32 results in the cycle gas oil and fresh gas oil only being riser cracked. In all these situations the naphtha stream would be subjected to both riser and bed cracking.
  • Stripping chamber 54' is provided with baffles 56' attached to the wall of stripper 54]" and riser 14'. As the catalyst cascades down over the baffles steam introduced through steam rings 53 and 55 displaces and removes adsorbed and entrained hydrocarbon vapors which pass upwardly through the stripper venting through stripper vent line 57 and. discharge into vapor space 22 of reactor 18'.
  • Stripped catalyst is withdrawn from the bottom of stripping chamber 54 passing through line 58' and discharges into regenerator 60.
  • Air introduced through air ring 62 at the bottom of regenerator 60 burns the carbon from the surface of the catalyst in dense bed 64.
  • the resulting flue gas passes upwardly entering cyclone where entrained catalyst is separated and returned to catalyst bed 64 through dip leg 72.
  • Flue gas passes from the cyclone into plenum chamber 74 and through flue gas line 76 to vent facilities.
  • Regenerated catalyst is withdrawn from the bottom of the regenerator at rates controlled by slide valves 80, 82 and 84 to supply hot regenerated catalyst to standpipes 28, 34' and 16', respectively, as described above.
  • a series of four runs are performed with a fluidized catalytic cracking unit having two feed risers.
  • 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 weight percent of a type X zeolite in a silicaalumina matrix and has a rare earth content of about 2.9 weight percent.
  • the amorphous silica-alumina catalyst has a high alumina content, a surface area of about m /g, and a pore volume of about 0.44 cc/g. in each of the runs fresh naphtha and fresh gas oil serve as the feedstocks.
  • the properties of the naphtha, a heavy straight run gasoline, are set forth in Table I while those of the gas oil are presented in Table II.
  • a process for the catalytic cracking of naphtha and Ag 0 gas oil with a zeolite cracking catalyst in a fluid cata- 50 632 lytic cracking unit comprising a reactor, a regenerator 2% gig and a multiplicity of elongated reaction zones wherein said reactor contains a dense phase and a dilute phase Atmospheric equivalent temperatures of said catalyst and said elongated reaction zones terminate at said reactor which comprises: ht Ruhs 1 and 3 the gas oil and naphtha are combined W a. introducing a low octane fresh naphtha stream and in a ratio of 3:1 and introduced into a single riser.
  • step (a) include a temperature of 750-l,300F., a conversion of 25-80 volume percent and a vapor velocity of 15-50 feet/second and the gas oil cracking conditions of step (b) include a temperature of 840-l,l00F., a conversion of 30-80 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 effluent 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 effecting an additional conversion of 5-30 volume percent and discharging into a dilute phase of catalyst.
  • step (g) introducing the fraction from step (g) and a third portion of freshly-regenerated zeolite cracking catalyst into a third elongated reaction zone to form a third mixture consisting essentially of said fraction from step (g) and said third portion of catalyst,
  • step (g) introducing the fraction from step (g) and a third portion of freshly-regenerated zeolite cracking catalyst into a third elongated reaction zone to form a third mixture consisting essentially of said fraction from step (g) and said third portion of catalyst,
  • step (g) introducing the fraction from step (g) and a third portion of freshly-regenerated zeolite cracking catalyst into a third elongated reaction zone to form a third mixture consisting essentially of said fraction from step (g) and said third portion of catalyst,
  • a process according to claim 4 wherein the catalytic cracking conditions in the dense phase include a temperature of 800-1,150F. and a vapor velocity of 0.5-4 feet/second.
  • a process according to claim 5 wherein the catalytic cracking conditions in the dense phase include a temperature of 800-l,l50F. 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 800-1,l50F. and a vapor velocity of 0.5-4 feet/second.
  • step (f) include a temperature of 800-1 ,100F., a conversion of 20-70 volume percent and a vapor velocity of 15-50 feet/second and the catalytic cracking conditions in the dense phase include a temperature of 800-1,l50F. and a vapor velocity of 0.5-4 feet/second.
  • step (f) includes a temperature of 800-l,100F., a conversion of 20-70 volume percent and a vapor velocity of 15-50 feet/second and the catalytic cracking conditions in the dense phase include a temperature of 800-l,l50F. and a vapor velocity of 0.5-4 feet/second.
  • step (f) include a temperature of 800-l,100F., a conversion of 20-70 volume percent and a vapor velocity of 15-50 feet/second and the catalytic cracking conditions in the dense phase include a temperature of 800-1,150F. and a vapor velocity of 0.5-4 feet/second.
  • step (f) include a temperature of 800l,l00F., a conversion of 20-70 volume percent and a vapor velocity of :50 feet/- second and the catalytic cracking conditions in the dense phase include a temperature of 800-l,150F. and a vapor velocity of 0.5-4 feet/second.
  • a process for the catalytic cracking of naphtha and gas oil 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 (h) introducing a low octane fresh naphtha stream, the hydrocarbon fraction boiling above aboutt 592? of step (h) herein and a first portion of a freshlyregenerated zeolite cracking catalyst into a first elongated reaction zone to form a fourth mixture consisting essentially of said fresh naphtha stream, said fraction boiling above abogt 500F. and said I first portion of catalyst,
  • step (c) passing said vaporous reaction mixture from step (c) through said dense phase under catalyst cracking conditions and discharging into a dilute phase of catalyst
  • step (b) include a temperature of 750-l,300F., a conversion of 25-80 volume percent and a vapor velocity of l5-50 ft/sec.
  • the gas oil cracking conditions of step (f) include a temperature of 840-1,100F., a conversion of 30-80 volume percent and a vapor velocity of 15-50 ft/sec.
  • the catalytic cracking conditions in the dense phase in clude a temperature of 800-l ,150F., a vapor velocity of 0.5-4 ft/sec. and an additional conversion of 5-30 XQlHFPEPi EFHP .7
  • a process for the catalytic cracking of naphtha and gas oil 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 (c) passing said vaporous reaction mixture from step (c) through said dense phase under catalytic cracking conditions and discharging into a dilute phase of catalyst
  • step (b) A process according to claim 22 wherein the naphtha cracking condtions of step (b) include a temperature of 750-l,300F., a conversion of 25-80 voume percent and a vapor velocity of l550 ft/sec.
  • the gas oil cracking conditions of step (f) include a temperature of 840 l,llF., a conversion of 30-80 volume percent and a vapor velocity of l-50 ft/sec.
  • the catalytic cracking conditions in the dense phase include a temperature of 800-l,l50F., a vapor velocity of 0.5-4 ft/sec. and an additional conversion of 5-30 volume percent.
  • a process according to claim 23 wherein the effluent from the second elongated reaction zone is discharged into a dense of catalyst, said vaporous reaction mixture from said second elongated reaction zone passing through said dense phase under catalytic cracking conditions and discharging into a dilute phase of catalyst.
  • step (j) introducing said fraction of step (j) and a third portion of freshly-regenerated zeolite cracking catalyst into a third elongated reaction zone to form an eighth mixture consisting essentially of said fraction from step (j) and said third portion of catalyst,
  • step (j) introducing said fraction of step (j) and a third portion of freshly-regenerated zeolite cracking catalyst into a third elongated reaction zone to form an eighth mixture consisting essentially of said fraction from step (j) and said third portion of catalyst,
  • a process according to claim 26 wherein the cycle gas oil cracking conditions of step (1) include a temperature of 800-l,l0OF., a conversion of 20-70 volume percent and a vapor velocity of 15-50 ft/sec.

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US3869378A (en) * 1971-11-16 1975-03-04 Sun Oil Co Pennsylvania Combination cracking process
US3894935A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3894936A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3923637A (en) * 1973-03-29 1975-12-02 Gulf Research Development Co Hydrodesulfurization process with a portion of the feed added downstream
US3928172A (en) * 1973-07-02 1975-12-23 Mobil Oil Corp Catalytic cracking of FCC gasoline and virgin naphtha
US3948757A (en) * 1973-05-21 1976-04-06 Universal Oil Products Company Fluid catalytic cracking process for upgrading a gasoline-range feed
US3954600A (en) * 1974-02-15 1976-05-04 Exxon Research & Engineering Co. Catalytic cracking process for producing middle distillate
US4172812A (en) * 1978-04-03 1979-10-30 Exxon Research & Engineering Co. Catalytic cracking process
US4176049A (en) * 1978-04-03 1979-11-27 Exxon Research & Engineering Co. Catalytic cracking process
US5100534A (en) * 1989-11-29 1992-03-31 Mobil Oil Corporation Hydrocarbon cracking and reforming process
US5104517A (en) * 1990-05-17 1992-04-14 Uop Vented riser apparatus and method
US5154818A (en) * 1990-05-24 1992-10-13 Mobil Oil Corporation Multiple zone catalytic cracking of hydrocarbons
US5824208A (en) * 1994-05-27 1998-10-20 Exxon Research & Engineering Company Short contact time catalytic cracking process
CN1081220C (zh) * 1999-06-23 2002-03-20 中国石油化工集团公司 一种汽油改质的催化转化方法
US6416656B1 (en) 1999-06-23 2002-07-09 China Petrochemical Corporation Catalytic cracking process for increasing simultaneously the yields of diesel oil and liquefied gas
US20030111388A1 (en) * 2001-05-30 2003-06-19 China Petroleum & Chemical Corporation And Research Institute Of Petroleum Processing Process for catalytic upgrading light petroleum hydrocarbons accompanied by low temperature regenerating the catalyst
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
US20090299118A1 (en) * 2008-05-29 2009-12-03 Kellogg Brown & Root Llc FCC For Light Feed Upgrading
CN1888021B (zh) * 2005-06-30 2010-04-28 洛阳石化设备研究所 一种烃类原料催化裂化转化方法及催化裂化转化反应器
CN102199447A (zh) * 2010-03-25 2011-09-28 中国石油化工股份有限公司 一种生产高十六烷值轻柴油和低烯烃汽油的催化转化方法
US20130006028A1 (en) * 2009-10-30 2013-01-03 China Petroleum & Chemical Corporation Catalytic cracking apparatus and process
CN103571536A (zh) * 2013-09-17 2014-02-12 中国石油大学(华东) 催化裂化与加氢生产清洁汽油并增产丙烯的装置及方法
CN105368493A (zh) * 2014-09-02 2016-03-02 中国石油化工股份有限公司 一种生产高辛烷值汽油的催化转化方法
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
US20210222073A1 (en) * 2018-06-12 2021-07-22 Sabic Global Technologies B.V. Naphtha splitter integration with hncc technology
US20220275284A1 (en) * 2019-08-05 2022-09-01 Sabic Global Technologies B.V. High-density fluidized bed systems
US11851622B1 (en) 2022-07-15 2023-12-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit and steam enhanced catalytic cracker
US20240018432A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit, steam enhanced catalytic cracker, and an aromatics complex
US20240018433A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex
US11939541B2 (en) 2022-07-15 2024-03-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex

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EP0022883B1 (en) * 1979-07-18 1983-11-23 Exxon Research And Engineering Company Catalytic cracking and hydrotreating process for producing gasoline from hydrocarbon feedstocks containing sulfur
US4693808A (en) * 1986-06-16 1987-09-15 Shell Oil Company Downflow fluidized catalytic cranking reactor process and apparatus with quick catalyst separation means in the bottom thereof

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Cited By (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3869378A (en) * 1971-11-16 1975-03-04 Sun Oil Co Pennsylvania Combination cracking process
US3923637A (en) * 1973-03-29 1975-12-02 Gulf Research Development Co Hydrodesulfurization process with a portion of the feed added downstream
US3948757A (en) * 1973-05-21 1976-04-06 Universal Oil Products Company Fluid catalytic cracking process for upgrading a gasoline-range feed
US3928172A (en) * 1973-07-02 1975-12-23 Mobil Oil Corp Catalytic cracking of FCC gasoline and virgin naphtha
US3894935A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3894936A (en) * 1973-11-19 1975-07-15 Mobil Oil Corp Conversion of hydrocarbons with {37 Y{38 {0 faujasite-type catalysts
US3954600A (en) * 1974-02-15 1976-05-04 Exxon Research & Engineering Co. Catalytic cracking process for producing middle distillate
US4172812A (en) * 1978-04-03 1979-10-30 Exxon Research & Engineering Co. Catalytic cracking process
US4176049A (en) * 1978-04-03 1979-11-27 Exxon Research & Engineering Co. Catalytic cracking process
US5100534A (en) * 1989-11-29 1992-03-31 Mobil Oil Corporation Hydrocarbon cracking and reforming process
US5104517A (en) * 1990-05-17 1992-04-14 Uop Vented riser apparatus and method
US5154818A (en) * 1990-05-24 1992-10-13 Mobil Oil Corporation Multiple zone catalytic cracking of hydrocarbons
US5824208A (en) * 1994-05-27 1998-10-20 Exxon Research & Engineering Company Short contact time catalytic cracking process
CN1081220C (zh) * 1999-06-23 2002-03-20 中国石油化工集团公司 一种汽油改质的催化转化方法
US6416656B1 (en) 1999-06-23 2002-07-09 China Petrochemical Corporation Catalytic cracking process for increasing simultaneously the yields of diesel oil and liquefied gas
US20030111388A1 (en) * 2001-05-30 2003-06-19 China Petroleum & Chemical Corporation And Research Institute Of Petroleum Processing Process for catalytic upgrading light petroleum hydrocarbons accompanied by low temperature regenerating the catalyst
CN1888021B (zh) * 2005-06-30 2010-04-28 洛阳石化设备研究所 一种烃类原料催化裂化转化方法及催化裂化转化反应器
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
US8877042B2 (en) 2006-07-13 2014-11-04 Saudi Arabian Oil Company Ancillary cracking of heavy oils in conjunction with FCC unit operations
US20110226668A1 (en) * 2006-07-13 2011-09-22 Dean Christopher F Ancillary cracking of heavy oils in conjunction with fcc unit operations
US20090299118A1 (en) * 2008-05-29 2009-12-03 Kellogg Brown & Root Llc FCC For Light Feed Upgrading
US9234143B2 (en) * 2009-10-30 2016-01-12 China Petroleum & Chemical Corporation Catalytic cracking apparatus and process
US20130006028A1 (en) * 2009-10-30 2013-01-03 China Petroleum & Chemical Corporation Catalytic cracking apparatus and process
CN102199447B (zh) * 2010-03-25 2014-03-26 中国石油化工股份有限公司 一种生产高十六烷值轻柴油和低烯烃汽油的催化转化方法
CN102199447A (zh) * 2010-03-25 2011-09-28 中国石油化工股份有限公司 一种生产高十六烷值轻柴油和低烯烃汽油的催化转化方法
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor
CN103571536A (zh) * 2013-09-17 2014-02-12 中国石油大学(华东) 催化裂化与加氢生产清洁汽油并增产丙烯的装置及方法
CN103571536B (zh) * 2013-09-17 2014-07-30 中国石油大学(华东) 催化裂化与加氢生产清洁汽油并增产丙烯的装置及方法
CN105368493A (zh) * 2014-09-02 2016-03-02 中国石油化工股份有限公司 一种生产高辛烷值汽油的催化转化方法
CN105368493B (zh) * 2014-09-02 2018-07-31 中国石油化工股份有限公司 一种生产高辛烷值汽油的催化转化方法
US20210222073A1 (en) * 2018-06-12 2021-07-22 Sabic Global Technologies B.V. Naphtha splitter integration with hncc technology
US20220275284A1 (en) * 2019-08-05 2022-09-01 Sabic Global Technologies B.V. High-density fluidized bed systems
US11851622B1 (en) 2022-07-15 2023-12-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit and steam enhanced catalytic cracker
US20240018432A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a gasification unit, steam enhanced catalytic cracker, and an aromatics complex
US20240018433A1 (en) * 2022-07-15 2024-01-18 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex
US11939541B2 (en) 2022-07-15 2024-03-26 Saudi Arabian Oil Company Methods for processing a hydrocarbon oil feed stream utilizing a delayed coker, steam enhanced catalytic cracker, and an aromatics complex

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IE35665B1 (en) 1976-04-14
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GB1349912A (en) 1974-04-10
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TR16793A (tr) 1973-05-01
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CH563449A5 (it) 1975-06-30
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IT945973B (it) 1973-05-10
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NL7113476A (it) 1972-04-05
AU458765B2 (en) 1975-03-06
CA966796A (en) 1975-04-29
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EG10951A (en) 1976-09-30
DE2147547B2 (de) 1974-01-17
FI53981B (fi) 1978-05-31
NO130278B (it) 1974-08-05

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