CA1241613A - Fluidized catalytic process - Google Patents
Fluidized catalytic processInfo
- Publication number
- CA1241613A CA1241613A CA000471030A CA471030A CA1241613A CA 1241613 A CA1241613 A CA 1241613A CA 000471030 A CA000471030 A CA 000471030A CA 471030 A CA471030 A CA 471030A CA 1241613 A CA1241613 A CA 1241613A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- reactor
- process according
- effluent
- recycled
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
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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
- C10G11/02—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
Abstract
FLUIDIZED CATALYTIC CRACKING PROCESS
ABSTRACT OF THE DISCLOSURE
A fluidized catalytic process preferably cracking of heavy oils, operating with equilibrium fluidized catalyst is operated with an entrainable catalyst which is removed by reactor effluent vapours. Preferred is addition of entrainable catalyst containing 10 to 40 weight % of ZSM-5 and having an average particle size of 4 to 10 microns. The entrainable catalyst is removed from the FCC reactor with reactor effluent, and preferably recycled to the reactor.
ABSTRACT OF THE DISCLOSURE
A fluidized catalytic process preferably cracking of heavy oils, operating with equilibrium fluidized catalyst is operated with an entrainable catalyst which is removed by reactor effluent vapours. Preferred is addition of entrainable catalyst containing 10 to 40 weight % of ZSM-5 and having an average particle size of 4 to 10 microns. The entrainable catalyst is removed from the FCC reactor with reactor effluent, and preferably recycled to the reactor.
Description
This invention relates to an improvement in hydeo-carbon conversion processes wherein a catalyst is contacted with a hydrocarbon feedstock in a fluidized bed reactor.
The fluidized catalytic cracking process is well 5 known. Cracked hydrocarbon vapours from the reactor pass to various product fractionators wherein the hydrocarbon mixture is separated into fractions. Some catalyst is usually carried along with the hydrocarbon vapours into the fraction-:
ator. This catalyst tends to accumulate in the fractionator 10 with the heaviest hydrocarbon fraction containea in the reactor effluent.
It is known to simply recycle this heavy oil, commonly called a slurry oil, back to the reactor to reduce the loss of relatively expensive FCC catalyst from the plant.
15 Unfortunately this slurry oil is highly aromatic, and relatively refractory or inert to the conditions which proouced it in the FCC reactor. Recycling of slurry oil to minimize catalyst losses will cause this slurry stream to grow in size because the highly aromatic slurry oil passes 20 through the FCC reactor unscathed and tends to accumulate.
The separation and recycle of catalyst fines from slurry oil is by now a standard technic~ue, as oescribed in US-A-3,338,821; 4,Q22,675; 4,285,805; and 4,345,991. .~11 of these patents taught recovery of catalyst fines generated in 25 the FCC reactor, and recycle of the fines to the reactor tc minimize catalyst loss.
It is known that the slurry oils can be cleanecd by passing these oils through an electrofilter, as disclosed in ~S-A-3,928,158.
US A-4,059,498 teaches an improved device in which a central tubular electrode extends downwardly through the filter t,ec. on outer vertical perforated cylindrical electron is col-centric with the centra1 electrode. R~ial Liquid flow is provided, permitting increased slow rate as compare(l to longit-ldinal flow.
Improvements in process efficiency have been made available to FCC ol~erators by the clevelopment of zeo1ites characterised by a Constraint Index in the range l to 12 (the significance and manner of determination of which term is set forth in Canadian Patent No. 1,032,558). The term "zeolite"
as here used denotes the class of porotectosilicates, i.e., porous crystalline silicates that contain silicon and oxygen atoms as the major components. Other components may be present in minor amounts, usually less than 14 mole and preferably less than 4 mole I. These components include aluminium, gallium, iron, chromium, boron and the like with lS aluminium being preferred and used herein for illustration purposesO The minor components may be present separately or in mixtures.
Constraint Index (CI) values for some typical materials are:
CI_ ZSM-4 o 5 ZSM-5 8.3 ZSM-ll 8.7 ZSM-l2 2 ZSM-23 9.l TMA Offretite 3.7 Clinoptilolite 3.4 H-Zeolon (mordenite) 0.4 Amorphous Silica-Alumina 0.6 Erionite 38 A crystalline zeolite when identified by any combination of conditions within the testing definition set forth in the aforesaid Canac3ian Patent No. 1,032,558 as having a Constraint Index in tl-e approximate range of 1 to 12 is intended to be included in the instant zeolite definition whetller or not the identical zeolite, when tested under other of the defined conditions, may give a Constraint Index value outside of the approximate range of 1 to 12.
The novel class of zeolites defined herein is exemplified by ZSM-5, ZSM-ll, ZSM-5/ZSM-ll intermediate, ZSM-12, ZSM-23, ZSM-35, ZSM-38 and ZSM-48, defined respectively by the x-ray data set forth in US-A-3,702,886;
3,709,979; 4,229,424; 3,832,4~9; 4,076,842i 4,016,245;
4,046,859; and 4,377,497.
The present invention contemplates utilization of such zeolites wherein the mole ratio of silica to alumina is essentially unbounded. Reference to the above-identified patents should not be construed as limiting the disclosed crystalline zeolites to those having the specific silica-alumina mole ratios discussed therein, it now being known that such zeolites may be substantially aluminium-free and yet, having the same crystal structure as the disclosed materials, may be useful or even preferred in some applications, as may zeolites which contain trivalent lattice elements other than aluminium.
ZSM-5 is a preferred catalyst because it is exceedingly active. Successful FCC processes may use catalysts containing relatively small amounts of ZSM-5 in an amorphous base such as silica, alumina, or silica-alumina.
One of the virtues of the ZSM-5 material, its great activity, causes some operations problems. When its high activity is tempered by incorporation of the ZSM-5 in an amorphous base, the ratio of ZSM-5 to amorphous material is fixed. It is possible to augment somewhat the ZSM-5 content of an operating FCC reactor by addition of additional particulate material containing neat ZS~!-S or enriched amounts of ZSM-5, as compared to the equilibrium catalyst in 5 the FCC reactor. Unfortunately there is no way to remove the ZSM-5 catalyst without removing the catalyst inventory from the reactor and replacing it with a different FCC catalyst.
nother problem with operation of ZSM-5 embedded in an amorphous matrix, is that the deactivation~reactivation 10 characteristics of the ZS~-5 and amorphous material are different. The ZS~7-5 material is relatively stable, as regards activity, in the FCC reactor. The 2SM-5 needs very little regeneration. The amorphous material rapidly deactivates after only a few minutes of operation due to coke 15 deposition. The only way to restore tile activity of the amorphous material is to burn the coke therefrom in an FCC
regenerator. Regeneration of the amorphous material tends to age, prematurely, the ZSM-5 catalyst passing through the re~el-erator, necessitating a continuing program of ZSM-5 20 addition to the FCC reactor to replace that ZSM-5 damaged by the regeneration process.
US-A-4,309,280 teaches adding a finely divided powder of zeolite additive promoter to coat the surface of FCC catalyst. This reference discloses that "the additive 25 promoter can also be introduced to and/or recycled through the recycle feed. See column 3, lines 28/29.
s the additive is of such a size as to coat the catalyst, the additive is locked onto the FCC catalyst, and behaves as FCC catalyst. Recycle of FCC catalyst front the 30 main column bottoms will result in additive recycle, plus recycle of a refractory slurry oil.
Petroleum refiners have had no economical and efficient means of reducing the ZS~-5 content of an FCC
P
reactor. It was possible to add ZS~-5 quickly, but not to remove it. It was possible to allow the ZSM-5 to naturally deactivate in the regenerator, but premature aging of the catalyst is an expensive way to remove its catalytic 5 activity. Thus there has been no completely satisfactory way to adjust the ZSM-5 content of an FCC reactor. Operation with ZS~-5 amorphous mixtures usually resulted in premature aging of the ZSM-5.
We have now discovered that it is possible to 10 increase or decrease the amount of the ZSM-5 catalyst contained within the fluidized catalytic cracking reactor.
ye have also discovered a way to keep the active ZSM-5 catalyst out of the deleterious environment of the catalyst regenerator.
According to the present invention a fluidised catalytic cracking process of the cyclic, regenerative kind in which a cracking feed contacts in a reactor a cracking catalyst having an average particle size of 30 to 80 em and a pore size sufficient to provide access to cracking sites for 20 at least the majority of feed components, the catalyst being continuously withdrawn from the reactor, regenerated, and returned to the reactor, hydrocarbon effluent being continuously withdrawn from the reactor and subjected to fractionation, is characterised in that a catalyst comE>rising 25 a crystalline zeolite having a constraint index in the range 1 to 12 and of average particle size 3 to 30 Lam is continuously added to said reactor and is withdrawn in entrainment in said effluent at at least 50% of the rate of its addition.
In a preferred embodiment added catalyst is withdrawn in entrainment in said effluent at at least 90% of the rate of its addition, and the quantity of said added catalyst in the reactor is 0.1 to 5% wt. of the quantity of said cracking catalyst in the reactor. Usually the added catalyst is recovered from entrainment in said effluent and recycled to the reactor, and at least 99~ wt. of said added catalyst present in the reactor can be recycled added 5 catalyst.
The cracking catalyst usually comprises from 5 to 50~ wt. of a synthetic faujasite suspended within and distributed throughout an inorganic oxide matrix, whilst the added catalyst usually comprises from 10 to 40% wt. of a 10 zeolite having the structure of zeolite ZSM-5 composited with an amorphous binder.
Accordingly the present invention provides a fluidized catalytic conversion process wherein a feedstream is charged to a fluidized bed reactor containing a fluidized 15 bed of equilibrium catalyst to produce cracked product, and a converted feedstream is removed as a product from the process, wherein the improvement comprises addition of an entrainable catalyst additive to said fluid bed, and removing a majority of said entrainable additive with said product 20 removed from the fluid bed reaction zone.
In another embodiment the present invention provides a process for fluidized catalytic conversion of a hydrocarbon feed comprising charging to a fluidized bed reactor containing equilibrium fluid cat cracking catalyst a 25 hydrocarbon feed and an entrainable catalyst additive to produce vapourized cat cacking products; removing said vapourized products containing at least 90 % wt. of said entrainable catalyst additive from said FCC reactor;
recovering from said vapourized product at least a portion of 30 said entrainable catalyst additive; and recycling at least a portion of said entrainable catalyst additive to said reactor.
In a more limited embodiment the present invention provides a process for fluidized catalytic cracking of hydrocarbons comprising charging to a fluidized bed reactor a hydrocarbon feed and hot regenerated equilibrium catalyst from a source hereafter specified; adding to said reactor fresh entrainable catalyst additive and recycle entrainable catalyst additive from a source hereafter specified; conver-ting in said fluid bed reactor said hydrocarbon feed to hydrocarbon products; removing from said reactor equilibrium catalyst, regenerating same in an oxysen-containing regenera-tion zone to to produce regenerated catalyst, and re~yclingsaid regenerated catalyst to said FCC reactor as said hot regenerated catalyst; removing from said reactor a reactor effluent vapour stream comprising hydrocarbon products and at least 50% wt. of said entrainable catalyst additive;
separating and fractionating said reactor effluent vapour to produce a plurality of relatively light hydrocarbon products and a relatively heavy liquid product stream containing said entrainable catalyst additive; recovering from said relatively heavy liquid stream at least 90% wt. of said entrainable catalyst additive contained therein and recycling said additive to said FCC reactor.
GRIEF DESCRIPTION OF THE DRAWING
The single figure is a simplified diagram representing an FCC unit with a reactor, regenerator and main fractionator.
The present invention solves two independent problems. The first problem solved is the fact that ZSM-5 catalyst, or other entrainable catalyst additive, can be continuously added to the catalyst contained in a fluid bed reactor, and quickly removed from the reactor independently of the equilibrium catalyst. The effect of catalyst additive addition can be made permanent by continuing to add it.
The second problem solved by this invention is the ability to recover the ZSM-5 catalyst or other entrainable catalyst additive, and recycle it to the reactor, without 5 passing through the high temperature FCC regenerator.
Avoiding the FCC catalyst regenerator prevents premature aging of the catalyst additive.
Each of the important process parameters will be discussed in turn.
10 Rl~ACTOR/REGENERATOR
These are conventional. The FCC reactor may be an entirely dense phase fluid bed, or may operate with all riser cracking, with a dilute phase bed, or some mixture of both modes of operation. The FCC regenerator can be a single dense bed, or two dense beds connected by a dilute phase transport riser connected to a second dense bed within the regenerator. The regenerator can operate in a CO
afterburning mode, or may be operated to produce substantial amounts of CO. The practice of the present invention will be most beneficial when the regenerator is run relatively hot;
usually this is associated with a CO afterburning type of operation. Hot catalyst regeneration promotes rapid deactivation of the ZSM-5 materials.
EOUILIBRIUM CATALYST
The equilibrium catalyst, which will comprise the bulk of the catalyst within the fluid bed reactor, may be any conventional fluid bed, or FCC catalyst, either amorphous or crystalline, or a mixture of both. Catalysts having an average particle size of 10 to 100 micrometers diameter are commonly used in fluidized beds. The particle size distribution of the catalyst will be that required for good -9- ~2~6~
fluidization characteristics in the reactor. By way of illustration, but not limitation, a good FCC equilibrium catalyst will have the following properties:
Particle Density, g/cc 1.42 Packed Density, g/cc .99 Average Particle Size, mm 74 Size Distribution Diameter ~icro-meters 80+ 37 15 ENT~AINABLE CATALYST
An acceptable catalyst additive is any which can be added to the fluid bed reactor and removed with the vapour-ised reactor effluent. The exact size of the entrainable catalyst additive will vary with operating conditions within 20 the reactor, and will be affected to some extent by the size of the equilibrium catalyst and by the efficiency of the cyclones used to eeturn the bulk of the equilibrium catalyst to the reactor.
A preferred additive is ZSM-5, either neat or 25 dispersed in an amorphous base. The practice of the present invention is most advantageous when a relatively concentrated ZSM-5 material, e.g., typically iO to 50~ wt. ZSM-5, is added as an entrainable catalyst additive. In most conventional FCC reactors containing conventional equilibrium catalysts, 6i~
an entrainable catalyst additive with an average particle size of 3 to 30, and preferably S to 20 micrometers will give good resultsO
The retention time of the entrainable catalyst 5 additive will vary from the residence time of the gas to about ten times as long as the gas residence time. Usually the entrainable catalyst particles will be swept along with the gas, so the entrainable catalyst particle residence time will be on the order of 100 to 200 percent of the gas 10 residence time within the reactor.
One additional benefit from the practice of the present invention is that the entrainable catalyst additive is disproportionately effective within, e.g., the FCC reactor because of its small particle size. oven operating in a 15 throwaway mode of operation, in the absence of recycle, the practice of our invention makes better use of the ZSM-5 because the ZSM-5 is in a highly divided state.
When ZSM-5 is the entrainable additive, it should have the following composition and properties.
PreferredAcceptable ZSM-5 Content 25~ 5-100 Chemical Composition SiO2 94% 10-100%
A123 6% 0-10 25 Particle Density 1.40 g/cc Particle Size Distribution 0-20 mm 78.6%
20-40 mm 21.4%
Average Particle Size 4.2 mm 3-30 mm --11~
MAIN FRACTIONATOR
The fractionation facilities are conventional. Any commonly used method of recovering valuable products from material contained in the reactor effluent can be used.
Usually the reactor effluent vapours are cooled and compressed and sent through a variety of absorber and fractionators. The heaviest material contained in the reactor effluent is usually removed as the bottom stream from a large fractionator, typically called the main fractionator 10 ENTRAINABLE CATALYST ~ECOVE~
We prefer to recycle all or a portion of the entrainable catalyst back to the reactor, or to mix with reactor feed. It is acceptable, and may be preferred, based upon the economics of a given location, to recycle only the 15 catalyst, or a liquid stream containing an enriched catalyst concentration.
The catalyst can be recovered from the slurry oil by filtration, settling, addition of an antisolvent, or any other known means of separating a finely divided powder from 20 a liquid.
It is preferred not to simply recycle, e.g., the main column bottoms back to the reactor. Such a recycle operatlon tends to produce a refractory slurry oil which is difficult to crack in the FCC unit. Such an operation also 25 recycles both entrainable additive and FCC catalyst carried out of the FCC, and sometimes it is preferred to recycle, preferentially, the entrainable additive.
It is also within the scope of the present invention to fractionate the recycled catalyst, i.e., 30 separate large fines from small fines by using staged filtration, or other conventional means. In this manner the fraction most enriched in ZSM-5, or other desired catalyst ~4~
additive, can be recycled to the reactor, without sending other catalyst fines or the entire stream from the main column bottoms back to the reactor.
It is also possible to recover ZSM-5 catalyst, or 5 other entrainable catalyst additive, using staged cyclone separators, a baghouse, electrostatic precipitators, or equivalent means. In this mode of operation the entrainable catalyst additive recovery and recycle would occur upstream of the product fractionator. The disadvantage of this type 10 of operation is that it requires some additional capital expense, but it may be cheaper on the new unit to install staged cyclones to recover and recycle to the reactor entrainable particles of ZSM-5 that would otherwise be removed from the reactor, rather than tolerate the problems 15 introduced with a large slurry oil recycle. Staged cyclonic separation of fine particles contained in reactor eifluent vapour could also accomplish the desired goal, namely recycle of entrainable ZSM-5 to the reactor without sending the ZSM-5 material or other entrainable additive through the 20 regeneratOr.
Once the additive has been recovered it could additionally be treated to recover any lost activity, such as by combustion of coke deposits under milder conditions than those prevailing in the main regenerator.
25 ELECT~OSTATI~ FILTER
The preferred method of recovering entrainable catalyst involves use of an electrostatic filter, such as the ones disclosed in US-A-3,928,158 and 4,059,498.
US-A-3,928,158 describes an electrostatic filter 30 in which an electrostatic gradient is imposed across a bed of glass beads. Liquid flows through the bed while the ~4~6~
electrical gradient is imposed across the bed. Solids are deposited in the filter bed at the point of contact of the glass beads. The filter can be repeatedly and readily reconditioned for further use by backflushing.
DETAILED D~SCRIPIION QF THE DRAWING
The invention is now further illustrated in connection with the drawing.
Fresh feed enters reactor 4 via line 1. The feed is mixed with a heavy recycle stream contained in line 2.
Catalyst additive may be added from two sources, fresh in line 3, recycled along with the heavy recycle stream in line
The fluidized catalytic cracking process is well 5 known. Cracked hydrocarbon vapours from the reactor pass to various product fractionators wherein the hydrocarbon mixture is separated into fractions. Some catalyst is usually carried along with the hydrocarbon vapours into the fraction-:
ator. This catalyst tends to accumulate in the fractionator 10 with the heaviest hydrocarbon fraction containea in the reactor effluent.
It is known to simply recycle this heavy oil, commonly called a slurry oil, back to the reactor to reduce the loss of relatively expensive FCC catalyst from the plant.
15 Unfortunately this slurry oil is highly aromatic, and relatively refractory or inert to the conditions which proouced it in the FCC reactor. Recycling of slurry oil to minimize catalyst losses will cause this slurry stream to grow in size because the highly aromatic slurry oil passes 20 through the FCC reactor unscathed and tends to accumulate.
The separation and recycle of catalyst fines from slurry oil is by now a standard technic~ue, as oescribed in US-A-3,338,821; 4,Q22,675; 4,285,805; and 4,345,991. .~11 of these patents taught recovery of catalyst fines generated in 25 the FCC reactor, and recycle of the fines to the reactor tc minimize catalyst loss.
It is known that the slurry oils can be cleanecd by passing these oils through an electrofilter, as disclosed in ~S-A-3,928,158.
US A-4,059,498 teaches an improved device in which a central tubular electrode extends downwardly through the filter t,ec. on outer vertical perforated cylindrical electron is col-centric with the centra1 electrode. R~ial Liquid flow is provided, permitting increased slow rate as compare(l to longit-ldinal flow.
Improvements in process efficiency have been made available to FCC ol~erators by the clevelopment of zeo1ites characterised by a Constraint Index in the range l to 12 (the significance and manner of determination of which term is set forth in Canadian Patent No. 1,032,558). The term "zeolite"
as here used denotes the class of porotectosilicates, i.e., porous crystalline silicates that contain silicon and oxygen atoms as the major components. Other components may be present in minor amounts, usually less than 14 mole and preferably less than 4 mole I. These components include aluminium, gallium, iron, chromium, boron and the like with lS aluminium being preferred and used herein for illustration purposesO The minor components may be present separately or in mixtures.
Constraint Index (CI) values for some typical materials are:
CI_ ZSM-4 o 5 ZSM-5 8.3 ZSM-ll 8.7 ZSM-l2 2 ZSM-23 9.l TMA Offretite 3.7 Clinoptilolite 3.4 H-Zeolon (mordenite) 0.4 Amorphous Silica-Alumina 0.6 Erionite 38 A crystalline zeolite when identified by any combination of conditions within the testing definition set forth in the aforesaid Canac3ian Patent No. 1,032,558 as having a Constraint Index in tl-e approximate range of 1 to 12 is intended to be included in the instant zeolite definition whetller or not the identical zeolite, when tested under other of the defined conditions, may give a Constraint Index value outside of the approximate range of 1 to 12.
The novel class of zeolites defined herein is exemplified by ZSM-5, ZSM-ll, ZSM-5/ZSM-ll intermediate, ZSM-12, ZSM-23, ZSM-35, ZSM-38 and ZSM-48, defined respectively by the x-ray data set forth in US-A-3,702,886;
3,709,979; 4,229,424; 3,832,4~9; 4,076,842i 4,016,245;
4,046,859; and 4,377,497.
The present invention contemplates utilization of such zeolites wherein the mole ratio of silica to alumina is essentially unbounded. Reference to the above-identified patents should not be construed as limiting the disclosed crystalline zeolites to those having the specific silica-alumina mole ratios discussed therein, it now being known that such zeolites may be substantially aluminium-free and yet, having the same crystal structure as the disclosed materials, may be useful or even preferred in some applications, as may zeolites which contain trivalent lattice elements other than aluminium.
ZSM-5 is a preferred catalyst because it is exceedingly active. Successful FCC processes may use catalysts containing relatively small amounts of ZSM-5 in an amorphous base such as silica, alumina, or silica-alumina.
One of the virtues of the ZSM-5 material, its great activity, causes some operations problems. When its high activity is tempered by incorporation of the ZSM-5 in an amorphous base, the ratio of ZSM-5 to amorphous material is fixed. It is possible to augment somewhat the ZSM-5 content of an operating FCC reactor by addition of additional particulate material containing neat ZS~!-S or enriched amounts of ZSM-5, as compared to the equilibrium catalyst in 5 the FCC reactor. Unfortunately there is no way to remove the ZSM-5 catalyst without removing the catalyst inventory from the reactor and replacing it with a different FCC catalyst.
nother problem with operation of ZSM-5 embedded in an amorphous matrix, is that the deactivation~reactivation 10 characteristics of the ZS~-5 and amorphous material are different. The ZS~7-5 material is relatively stable, as regards activity, in the FCC reactor. The 2SM-5 needs very little regeneration. The amorphous material rapidly deactivates after only a few minutes of operation due to coke 15 deposition. The only way to restore tile activity of the amorphous material is to burn the coke therefrom in an FCC
regenerator. Regeneration of the amorphous material tends to age, prematurely, the ZSM-5 catalyst passing through the re~el-erator, necessitating a continuing program of ZSM-5 20 addition to the FCC reactor to replace that ZSM-5 damaged by the regeneration process.
US-A-4,309,280 teaches adding a finely divided powder of zeolite additive promoter to coat the surface of FCC catalyst. This reference discloses that "the additive 25 promoter can also be introduced to and/or recycled through the recycle feed. See column 3, lines 28/29.
s the additive is of such a size as to coat the catalyst, the additive is locked onto the FCC catalyst, and behaves as FCC catalyst. Recycle of FCC catalyst front the 30 main column bottoms will result in additive recycle, plus recycle of a refractory slurry oil.
Petroleum refiners have had no economical and efficient means of reducing the ZS~-5 content of an FCC
P
reactor. It was possible to add ZS~-5 quickly, but not to remove it. It was possible to allow the ZSM-5 to naturally deactivate in the regenerator, but premature aging of the catalyst is an expensive way to remove its catalytic 5 activity. Thus there has been no completely satisfactory way to adjust the ZSM-5 content of an FCC reactor. Operation with ZS~-5 amorphous mixtures usually resulted in premature aging of the ZSM-5.
We have now discovered that it is possible to 10 increase or decrease the amount of the ZSM-5 catalyst contained within the fluidized catalytic cracking reactor.
ye have also discovered a way to keep the active ZSM-5 catalyst out of the deleterious environment of the catalyst regenerator.
According to the present invention a fluidised catalytic cracking process of the cyclic, regenerative kind in which a cracking feed contacts in a reactor a cracking catalyst having an average particle size of 30 to 80 em and a pore size sufficient to provide access to cracking sites for 20 at least the majority of feed components, the catalyst being continuously withdrawn from the reactor, regenerated, and returned to the reactor, hydrocarbon effluent being continuously withdrawn from the reactor and subjected to fractionation, is characterised in that a catalyst comE>rising 25 a crystalline zeolite having a constraint index in the range 1 to 12 and of average particle size 3 to 30 Lam is continuously added to said reactor and is withdrawn in entrainment in said effluent at at least 50% of the rate of its addition.
In a preferred embodiment added catalyst is withdrawn in entrainment in said effluent at at least 90% of the rate of its addition, and the quantity of said added catalyst in the reactor is 0.1 to 5% wt. of the quantity of said cracking catalyst in the reactor. Usually the added catalyst is recovered from entrainment in said effluent and recycled to the reactor, and at least 99~ wt. of said added catalyst present in the reactor can be recycled added 5 catalyst.
The cracking catalyst usually comprises from 5 to 50~ wt. of a synthetic faujasite suspended within and distributed throughout an inorganic oxide matrix, whilst the added catalyst usually comprises from 10 to 40% wt. of a 10 zeolite having the structure of zeolite ZSM-5 composited with an amorphous binder.
Accordingly the present invention provides a fluidized catalytic conversion process wherein a feedstream is charged to a fluidized bed reactor containing a fluidized 15 bed of equilibrium catalyst to produce cracked product, and a converted feedstream is removed as a product from the process, wherein the improvement comprises addition of an entrainable catalyst additive to said fluid bed, and removing a majority of said entrainable additive with said product 20 removed from the fluid bed reaction zone.
In another embodiment the present invention provides a process for fluidized catalytic conversion of a hydrocarbon feed comprising charging to a fluidized bed reactor containing equilibrium fluid cat cracking catalyst a 25 hydrocarbon feed and an entrainable catalyst additive to produce vapourized cat cacking products; removing said vapourized products containing at least 90 % wt. of said entrainable catalyst additive from said FCC reactor;
recovering from said vapourized product at least a portion of 30 said entrainable catalyst additive; and recycling at least a portion of said entrainable catalyst additive to said reactor.
In a more limited embodiment the present invention provides a process for fluidized catalytic cracking of hydrocarbons comprising charging to a fluidized bed reactor a hydrocarbon feed and hot regenerated equilibrium catalyst from a source hereafter specified; adding to said reactor fresh entrainable catalyst additive and recycle entrainable catalyst additive from a source hereafter specified; conver-ting in said fluid bed reactor said hydrocarbon feed to hydrocarbon products; removing from said reactor equilibrium catalyst, regenerating same in an oxysen-containing regenera-tion zone to to produce regenerated catalyst, and re~yclingsaid regenerated catalyst to said FCC reactor as said hot regenerated catalyst; removing from said reactor a reactor effluent vapour stream comprising hydrocarbon products and at least 50% wt. of said entrainable catalyst additive;
separating and fractionating said reactor effluent vapour to produce a plurality of relatively light hydrocarbon products and a relatively heavy liquid product stream containing said entrainable catalyst additive; recovering from said relatively heavy liquid stream at least 90% wt. of said entrainable catalyst additive contained therein and recycling said additive to said FCC reactor.
GRIEF DESCRIPTION OF THE DRAWING
The single figure is a simplified diagram representing an FCC unit with a reactor, regenerator and main fractionator.
The present invention solves two independent problems. The first problem solved is the fact that ZSM-5 catalyst, or other entrainable catalyst additive, can be continuously added to the catalyst contained in a fluid bed reactor, and quickly removed from the reactor independently of the equilibrium catalyst. The effect of catalyst additive addition can be made permanent by continuing to add it.
The second problem solved by this invention is the ability to recover the ZSM-5 catalyst or other entrainable catalyst additive, and recycle it to the reactor, without 5 passing through the high temperature FCC regenerator.
Avoiding the FCC catalyst regenerator prevents premature aging of the catalyst additive.
Each of the important process parameters will be discussed in turn.
10 Rl~ACTOR/REGENERATOR
These are conventional. The FCC reactor may be an entirely dense phase fluid bed, or may operate with all riser cracking, with a dilute phase bed, or some mixture of both modes of operation. The FCC regenerator can be a single dense bed, or two dense beds connected by a dilute phase transport riser connected to a second dense bed within the regenerator. The regenerator can operate in a CO
afterburning mode, or may be operated to produce substantial amounts of CO. The practice of the present invention will be most beneficial when the regenerator is run relatively hot;
usually this is associated with a CO afterburning type of operation. Hot catalyst regeneration promotes rapid deactivation of the ZSM-5 materials.
EOUILIBRIUM CATALYST
The equilibrium catalyst, which will comprise the bulk of the catalyst within the fluid bed reactor, may be any conventional fluid bed, or FCC catalyst, either amorphous or crystalline, or a mixture of both. Catalysts having an average particle size of 10 to 100 micrometers diameter are commonly used in fluidized beds. The particle size distribution of the catalyst will be that required for good -9- ~2~6~
fluidization characteristics in the reactor. By way of illustration, but not limitation, a good FCC equilibrium catalyst will have the following properties:
Particle Density, g/cc 1.42 Packed Density, g/cc .99 Average Particle Size, mm 74 Size Distribution Diameter ~icro-meters 80+ 37 15 ENT~AINABLE CATALYST
An acceptable catalyst additive is any which can be added to the fluid bed reactor and removed with the vapour-ised reactor effluent. The exact size of the entrainable catalyst additive will vary with operating conditions within 20 the reactor, and will be affected to some extent by the size of the equilibrium catalyst and by the efficiency of the cyclones used to eeturn the bulk of the equilibrium catalyst to the reactor.
A preferred additive is ZSM-5, either neat or 25 dispersed in an amorphous base. The practice of the present invention is most advantageous when a relatively concentrated ZSM-5 material, e.g., typically iO to 50~ wt. ZSM-5, is added as an entrainable catalyst additive. In most conventional FCC reactors containing conventional equilibrium catalysts, 6i~
an entrainable catalyst additive with an average particle size of 3 to 30, and preferably S to 20 micrometers will give good resultsO
The retention time of the entrainable catalyst 5 additive will vary from the residence time of the gas to about ten times as long as the gas residence time. Usually the entrainable catalyst particles will be swept along with the gas, so the entrainable catalyst particle residence time will be on the order of 100 to 200 percent of the gas 10 residence time within the reactor.
One additional benefit from the practice of the present invention is that the entrainable catalyst additive is disproportionately effective within, e.g., the FCC reactor because of its small particle size. oven operating in a 15 throwaway mode of operation, in the absence of recycle, the practice of our invention makes better use of the ZSM-5 because the ZSM-5 is in a highly divided state.
When ZSM-5 is the entrainable additive, it should have the following composition and properties.
PreferredAcceptable ZSM-5 Content 25~ 5-100 Chemical Composition SiO2 94% 10-100%
A123 6% 0-10 25 Particle Density 1.40 g/cc Particle Size Distribution 0-20 mm 78.6%
20-40 mm 21.4%
Average Particle Size 4.2 mm 3-30 mm --11~
MAIN FRACTIONATOR
The fractionation facilities are conventional. Any commonly used method of recovering valuable products from material contained in the reactor effluent can be used.
Usually the reactor effluent vapours are cooled and compressed and sent through a variety of absorber and fractionators. The heaviest material contained in the reactor effluent is usually removed as the bottom stream from a large fractionator, typically called the main fractionator 10 ENTRAINABLE CATALYST ~ECOVE~
We prefer to recycle all or a portion of the entrainable catalyst back to the reactor, or to mix with reactor feed. It is acceptable, and may be preferred, based upon the economics of a given location, to recycle only the 15 catalyst, or a liquid stream containing an enriched catalyst concentration.
The catalyst can be recovered from the slurry oil by filtration, settling, addition of an antisolvent, or any other known means of separating a finely divided powder from 20 a liquid.
It is preferred not to simply recycle, e.g., the main column bottoms back to the reactor. Such a recycle operatlon tends to produce a refractory slurry oil which is difficult to crack in the FCC unit. Such an operation also 25 recycles both entrainable additive and FCC catalyst carried out of the FCC, and sometimes it is preferred to recycle, preferentially, the entrainable additive.
It is also within the scope of the present invention to fractionate the recycled catalyst, i.e., 30 separate large fines from small fines by using staged filtration, or other conventional means. In this manner the fraction most enriched in ZSM-5, or other desired catalyst ~4~
additive, can be recycled to the reactor, without sending other catalyst fines or the entire stream from the main column bottoms back to the reactor.
It is also possible to recover ZSM-5 catalyst, or 5 other entrainable catalyst additive, using staged cyclone separators, a baghouse, electrostatic precipitators, or equivalent means. In this mode of operation the entrainable catalyst additive recovery and recycle would occur upstream of the product fractionator. The disadvantage of this type 10 of operation is that it requires some additional capital expense, but it may be cheaper on the new unit to install staged cyclones to recover and recycle to the reactor entrainable particles of ZSM-5 that would otherwise be removed from the reactor, rather than tolerate the problems 15 introduced with a large slurry oil recycle. Staged cyclonic separation of fine particles contained in reactor eifluent vapour could also accomplish the desired goal, namely recycle of entrainable ZSM-5 to the reactor without sending the ZSM-5 material or other entrainable additive through the 20 regeneratOr.
Once the additive has been recovered it could additionally be treated to recover any lost activity, such as by combustion of coke deposits under milder conditions than those prevailing in the main regenerator.
25 ELECT~OSTATI~ FILTER
The preferred method of recovering entrainable catalyst involves use of an electrostatic filter, such as the ones disclosed in US-A-3,928,158 and 4,059,498.
US-A-3,928,158 describes an electrostatic filter 30 in which an electrostatic gradient is imposed across a bed of glass beads. Liquid flows through the bed while the ~4~6~
electrical gradient is imposed across the bed. Solids are deposited in the filter bed at the point of contact of the glass beads. The filter can be repeatedly and readily reconditioned for further use by backflushing.
DETAILED D~SCRIPIION QF THE DRAWING
The invention is now further illustrated in connection with the drawing.
Fresh feed enters reactor 4 via line 1. The feed is mixed with a heavy recycle stream contained in line 2.
Catalyst additive may be added from two sources, fresh in line 3, recycled along with the heavy recycle stream in line
2, or both. Catalyst additive may also be added in other parts of the plant, so long as the additive eventually enters the reactor. Regenerated equilibrium catalyst in line 11 is mixed with the incoming feed ir. the base of the riser 5 of reactor 4. Catalyst and reactor effluent vapours are discharged from riser reactor 5 via discharge means 6, shown schematically as a short length of pipe with a downfacing discharge, although cyclones may also be used. The equilibrium catalyst falls to the bottom of reactor 4 to form a dense bed of catalyst 7, while the entrainable catalyst additive is removed along with the eeactor effluent vapour via line 13. The riser reactor shown is merely illustrative of one suitable reactor. A single dense bed reactor, a series of fluid bed reactors, and ebullating bed reactor, or a moving bed reactor may also be used. All of these reactors operate with an equilibrium catalyst, and all may benefit by adding an entrainable catalyst additive.
Spent equilibrium catalyst is removed from dense bed 7 via line 9 and charged to conventional catalyst regenerator 8. Air, or oxygen containing gas or other regeneration fluid is added to the bottom of regenerator 8 - 14 - ~4~
via line 10. Flue gas is removed via line 12. Regenerated catalyst is removed via line 11.
The reactor effluent vapour in line 13 is charged to main column 14. Depending on the feed and catalyst, different products will be recovered. A typical product mix obtained by charging oil to an FCC unit is shown, but should not be limiting. Removed overhead from main column 14 is a wet gas via line 16, a light naphtha via line 17 and a heavy naphtha stream via line 18. A light cycle oil is removed via line 20. Heavy cycle oil is removed via line 22 or via line 23 if it is to be recycled to the reactor mixed with the recycled additive A main column bottom stream is withdrawn via line 24 and charged to electrofilter 26 wherein a heavy fraction enriched in catalyst fines and entrainable catalyst additive is recovered via line 27 and recycled via line 32 to line 23 containing heavy cycle oil, and from there it is charged via line 2 to mix with the fresh feed.
A portion of the main column bottom steam is withdrawn from the process via line 30 as clarified slurry oil, while the remaining portion of it is recycled via line 28 to the bottom of the main column. A portion of the catalyst fines and entrainable catalyst additive is removed from the process via line 34.
Although a recycle operation is shown in the drawing, wherein entrainable catalyst additive is recycled, it is possible to operate with once through operation wherein there is no flow in line 32. The optimum amount of recycle versus fresh addition of entrainable catalyst additive can be determined based on local economics. In general, a large slurry stream is undesirable because this brings a great deal of refractory material into the reactor. Operation with once thrcugh entrainable additive addition results in higher costs for catalyst additive. In general, recycle will be most attractive when the cost of the entrainable catalyst additive is relatively hish, the amount of catalyst fines produced during normal operation is relatively low, and the size of the slurry oil stream produced is relatively small.
When practicino this invention in an FCC plant designed to process 100,000 barrels (158,987 m3) per day of feed, and containing 400 tons (406,420 kg) of catalyst with an average particle size of 7a elm we would operate with 10 addition of 200 pounds (90.72 kg) per day of catalyst additive. The catalyst additive would have the following physical properties:
Preferred ZSM-5 Content 25 15 Chemical Compositior, SiC~2 ~4~
A1203 6%
Particle density 1. ao g/cc Particle Size Distribution 0-20 mm 20-40 Jim 21.4%
Average Particle cize 4.2 and would be added to the plant by pumping it in as a slurry in a light cycle oil stream. The amount of recycle additive 25 present in the recycle catalyst stream from the main column bottoms would be 12,500 pounds (5,670 kg) per hour. An electrofilter would be used to separate recycle additive frcn slurry oil so that recycle of the refractory slurry oil c2n be mininized. Preferably at least 90% of the slurry oil is removed from the process, while at least 90-99~ of the additive is recycled.
The riser feed would see a catalyst composition containing 0.25 weight percent Z~M-5 almost entirely due to recycle from the main column bottoms. The amount of ZSM-5 going to the regenerator should of course be minimized, but a small amount will pass through the regenerator.
ILLUSTRATIVE EMBODIMENT
Listed in the following table are estimates of product distributions that would be obtained in a prior art process, i.e., with no entrainable ZSM-5, as compared to the process described above it the description of best mode.
Prior Art Invention Wt % Vol % Wt % Vol %
15 Conversion 63.2 67.0 63.5 67.3 MCB 12.9 10.8 12.7 10.6 LCO (680F @ 90%)(360C) 23.9 22.2 23.8 22.1 C5+ Gasoline (385F @ 90%) (196C) 43.1 51.4 41.8 49.8 Total C4 7.5 11.6 8.0 12.3 20 Total C3 4.4 7-7 5.0 8.7 C2 and Lighter 3 5 3.9 4.0 4.5 Coke Total 100.0 107.6 100.0 108.0 Potential Alkylate 20.5 23.3 25 Outside IC4 Required 11.0 13.0 - ~7 -Prior Art Invention lot Vol % Wt Vol Light Hydrocarbons ~2 0.03 0.09 0.04 0.12 H2S 0.12 0.04 0.12 0.04 Cl 1.18 1.36 1.36 1.57 C2 1.23 1.48 1.48 1.70 c2- 0.89 0.97 1.03 1.12 C3 1.08 1.93 1.18 2.11 O 3.32 5.75 3.81 6.59 ~C4 1.2~ 1.86 1.23 1.91 IC4 2.10 3.37 2.03 3.25 C4- 4.20 6.33 4.71 7.10 Gasoline Octane R+O 89.8 90.8 M+O 79.5 79.9 Gasoline + Al~ylate R+O 90.9 91.7 M+O 83.1 83.8 Wt ZSM-5 Present 0.00 0.25 The significance of the present invention is that it gives refiners a way to change the catalyst character-istics in the FCC reactor without changing the catalyst inventory and without subjecting the entire catalyst inventory to the FCC regenerator. In the case of the ZSM-5 additive, it is possible to take advantage of the high activity and coke resistance of ZSM-5 without subjecting the ZSM-5 to the harsh conditions experienced in the modern CO
afterburing regenerators associated with ~CC units. If the ZSM-5 catalyst were added in a form where it behaved exactly as the equilibrium, the ZSM-5 would be subjected to high temperature regeneration every 3-10 minutes, and would lose most of its cracking activity within a few days, requiring very high ZSM-5 makeup rates to achi.eve the octane gains and gasoline plus alkylate yield gains described in the illustrative embodiment above.
In contrast, by the practice of the present 5 invention, it is possible to operate the FCC reactor with a very large presence of ZSM-5 catalyst, while a(l(lino only about one-tenth or one-hundredth the amount of ZSM-5 catalyst that would otherwise be needed to wake up for the rapid deactivation of ZSM-5 in the FCC reqenerator.
Spent equilibrium catalyst is removed from dense bed 7 via line 9 and charged to conventional catalyst regenerator 8. Air, or oxygen containing gas or other regeneration fluid is added to the bottom of regenerator 8 - 14 - ~4~
via line 10. Flue gas is removed via line 12. Regenerated catalyst is removed via line 11.
The reactor effluent vapour in line 13 is charged to main column 14. Depending on the feed and catalyst, different products will be recovered. A typical product mix obtained by charging oil to an FCC unit is shown, but should not be limiting. Removed overhead from main column 14 is a wet gas via line 16, a light naphtha via line 17 and a heavy naphtha stream via line 18. A light cycle oil is removed via line 20. Heavy cycle oil is removed via line 22 or via line 23 if it is to be recycled to the reactor mixed with the recycled additive A main column bottom stream is withdrawn via line 24 and charged to electrofilter 26 wherein a heavy fraction enriched in catalyst fines and entrainable catalyst additive is recovered via line 27 and recycled via line 32 to line 23 containing heavy cycle oil, and from there it is charged via line 2 to mix with the fresh feed.
A portion of the main column bottom steam is withdrawn from the process via line 30 as clarified slurry oil, while the remaining portion of it is recycled via line 28 to the bottom of the main column. A portion of the catalyst fines and entrainable catalyst additive is removed from the process via line 34.
Although a recycle operation is shown in the drawing, wherein entrainable catalyst additive is recycled, it is possible to operate with once through operation wherein there is no flow in line 32. The optimum amount of recycle versus fresh addition of entrainable catalyst additive can be determined based on local economics. In general, a large slurry stream is undesirable because this brings a great deal of refractory material into the reactor. Operation with once thrcugh entrainable additive addition results in higher costs for catalyst additive. In general, recycle will be most attractive when the cost of the entrainable catalyst additive is relatively hish, the amount of catalyst fines produced during normal operation is relatively low, and the size of the slurry oil stream produced is relatively small.
When practicino this invention in an FCC plant designed to process 100,000 barrels (158,987 m3) per day of feed, and containing 400 tons (406,420 kg) of catalyst with an average particle size of 7a elm we would operate with 10 addition of 200 pounds (90.72 kg) per day of catalyst additive. The catalyst additive would have the following physical properties:
Preferred ZSM-5 Content 25 15 Chemical Compositior, SiC~2 ~4~
A1203 6%
Particle density 1. ao g/cc Particle Size Distribution 0-20 mm 20-40 Jim 21.4%
Average Particle cize 4.2 and would be added to the plant by pumping it in as a slurry in a light cycle oil stream. The amount of recycle additive 25 present in the recycle catalyst stream from the main column bottoms would be 12,500 pounds (5,670 kg) per hour. An electrofilter would be used to separate recycle additive frcn slurry oil so that recycle of the refractory slurry oil c2n be mininized. Preferably at least 90% of the slurry oil is removed from the process, while at least 90-99~ of the additive is recycled.
The riser feed would see a catalyst composition containing 0.25 weight percent Z~M-5 almost entirely due to recycle from the main column bottoms. The amount of ZSM-5 going to the regenerator should of course be minimized, but a small amount will pass through the regenerator.
ILLUSTRATIVE EMBODIMENT
Listed in the following table are estimates of product distributions that would be obtained in a prior art process, i.e., with no entrainable ZSM-5, as compared to the process described above it the description of best mode.
Prior Art Invention Wt % Vol % Wt % Vol %
15 Conversion 63.2 67.0 63.5 67.3 MCB 12.9 10.8 12.7 10.6 LCO (680F @ 90%)(360C) 23.9 22.2 23.8 22.1 C5+ Gasoline (385F @ 90%) (196C) 43.1 51.4 41.8 49.8 Total C4 7.5 11.6 8.0 12.3 20 Total C3 4.4 7-7 5.0 8.7 C2 and Lighter 3 5 3.9 4.0 4.5 Coke Total 100.0 107.6 100.0 108.0 Potential Alkylate 20.5 23.3 25 Outside IC4 Required 11.0 13.0 - ~7 -Prior Art Invention lot Vol % Wt Vol Light Hydrocarbons ~2 0.03 0.09 0.04 0.12 H2S 0.12 0.04 0.12 0.04 Cl 1.18 1.36 1.36 1.57 C2 1.23 1.48 1.48 1.70 c2- 0.89 0.97 1.03 1.12 C3 1.08 1.93 1.18 2.11 O 3.32 5.75 3.81 6.59 ~C4 1.2~ 1.86 1.23 1.91 IC4 2.10 3.37 2.03 3.25 C4- 4.20 6.33 4.71 7.10 Gasoline Octane R+O 89.8 90.8 M+O 79.5 79.9 Gasoline + Al~ylate R+O 90.9 91.7 M+O 83.1 83.8 Wt ZSM-5 Present 0.00 0.25 The significance of the present invention is that it gives refiners a way to change the catalyst character-istics in the FCC reactor without changing the catalyst inventory and without subjecting the entire catalyst inventory to the FCC regenerator. In the case of the ZSM-5 additive, it is possible to take advantage of the high activity and coke resistance of ZSM-5 without subjecting the ZSM-5 to the harsh conditions experienced in the modern CO
afterburing regenerators associated with ~CC units. If the ZSM-5 catalyst were added in a form where it behaved exactly as the equilibrium, the ZSM-5 would be subjected to high temperature regeneration every 3-10 minutes, and would lose most of its cracking activity within a few days, requiring very high ZSM-5 makeup rates to achi.eve the octane gains and gasoline plus alkylate yield gains described in the illustrative embodiment above.
In contrast, by the practice of the present 5 invention, it is possible to operate the FCC reactor with a very large presence of ZSM-5 catalyst, while a(l(lino only about one-tenth or one-hundredth the amount of ZSM-5 catalyst that would otherwise be needed to wake up for the rapid deactivation of ZSM-5 in the FCC reqenerator.
Claims (19)
1. A fluidised catalytic cracking process of the cyclic, regenerative kind in which a cracking feed contacts in a reactor a cracking catalyst having an average particle size of 30 to 80 µm and a pore size sufficient to provide access to cracking sites for at least the majority of feed components, the catalyst being continuously withdrawn from the reactor, regenerated, and returned to the reactor, hydrocarbon effluent being continuously withdrawn from the reactor and subjected to fractionation, characterised in that a catalyst comprising a crystalline zeolite having a constraint index in the range 1 to 12 and of average particle size 3 to 30 µm is continuously added to said reactor and is withdrawn in entrainment in said effluent at at least 50% of the rate of its addition.
2. A process according to claim 1 wherein said added catalyst is withdrawn in entrainment in said effluent at at least 90% of the rate of its addition.
3. A process according to claim 1 wherein the quantity of said added catalyst in the reactor is 0.1 to 5%
wt. of the quantity of said cracking catalyst in the reactor.
wt. of the quantity of said cracking catalyst in the reactor.
4. A process according to claim 1, 2 or 3 wherein said added catalyst is recovered from entrainment in said effluent and recycled to the reactor.
5. A process according to claim 1, 2 or 3 wherein said added catalyst is recovered from entrainment in said effluent and recycled to the reactor and at least 99% wt. of said added catalyst present in the reactor is recycled added catalyst.
6. A process according to claim 1, 2 or 3 wherein one of the products of said fractionation is a relatively heavy liquid stream containing the majority of the catalyst entrained in said effluent.
7. A process according to claim 1, 2 or 3 wherein one of the products of said fractionation is a slurry oil containing the majority of the catalyst entrained in said effluent.
8. A process according to claim 1, 2 or 3 wherein one of the products of said fractionation is a relatively heavy liquid stream containing the majority of the catalyst entrained in said effluent and said stream containing said catalyst is recycled.
9. A process according to claim 1 wherein said added catalyst is recovered from entrainment in said effluent by separation from hydrocarbon product and recycled to the reactor.
10. A process according to claim 9 wherein the separation is effected by an electrostatic filter.
11. A process according to claim 9 wherein the separation is effected by passing said effluent through staged cyclones.
12. A process according to claim 9 wherein the separation is effected by filtration, settling or use of an antisolvent.
13. A process according to claim 12 in which the filtration is staged and separates said added catalyst in preference to said cracking catalyst.
14. A process according to claim 1, 2 or 3 wherein said added catalyst is recovered from entrainment in said effluent and recycled to the reactor and said recovered catalyst is regenerated before being recycled.
15. A process according to claim 1, 2 or 3 wherein one of the products of said fractionation is a relatively heavy liquid stream containing the majority of the catalyst entrained in said effluent and at least 90% wt. of said added catalyst contained in said stream is recycled.
16. A process according to claim 1, 2 or 3 wherein the reactor is a riser reactor.
17. A process according to claim 1, 2 or 3 wherein the cracking feed is a heavy oil.
18. A process according to claim 1, 2 or 3 wherein said cracking catalyst comprises from 5 to 50% wt. of a synthetic faujasite suspended within and distributed throughout an inorganic oxide matrix.
19. A process according to claim 1, 2 or 3 wherein said added catalyst comprises from 10 to 40% wt. of a zeolite having the structure of zeolite ZSM-5 composited with an amorphous binder.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US56801484A | 1984-01-04 | 1984-01-04 | |
| US568,014 | 1984-01-04 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1241613A true CA1241613A (en) | 1988-09-06 |
Family
ID=24269565
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000471030A Expired CA1241613A (en) | 1984-01-04 | 1984-12-27 | Fluidized catalytic process |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0148024A3 (en) |
| JP (1) | JPS60158290A (en) |
| AU (1) | AU555438B2 (en) |
| CA (1) | CA1241613A (en) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1264693A (en) * | 1985-02-20 | 1990-01-23 | Robert A. Lengemann | Reducing the temperature in a regeneration zone of a fluid catalytic cracking process |
| FR2587629B1 (en) * | 1985-09-25 | 1993-07-16 | Raffinage Cie Francaise | PROCESS FOR SEPARATION OF FINE CATALYST PARTICLES FROM A HYDROCARBON CHARGE, BY FILTRATION THROUGH MINERAL BARRIERS AND FILTRATION LOOP |
| AU608770B2 (en) * | 1986-09-03 | 1991-04-18 | Mobil Oil Corporation | Apparatus and process for fluidized catalytic cracking with separation of catalyst components in a catalyst stripper |
| US4871446A (en) * | 1986-09-03 | 1989-10-03 | Mobil Oil Corporation | Catalytic cracking process employing mixed catalyst system |
| US7223896B2 (en) | 2004-04-29 | 2007-05-29 | Exxonmobil Chemical Patents Inc. | Fines co-feed for maintaining efficient reactor hydrodynamics |
| EP1660614B1 (en) * | 2003-08-05 | 2018-07-18 | ExxonMobil Chemical Patents Inc. | Fines co-feed for maintaining efficient reactor hydrodynamics |
| BRPI0821358A2 (en) * | 2007-12-20 | 2015-06-16 | Chevron Usa Inc | System and process for separating heavy oil from catalyst particles, system for separating hydrocarbons, process for separating heavy oil from catalyst particulates, process for removing hydrocarbons, and process for benefiting a heavy oil feed load. |
| US8178461B2 (en) | 2008-12-30 | 2012-05-15 | Chevron U.S.A. Inc | Thermal treatment processes for spent hydroprocessing catalyst |
| US8414687B2 (en) * | 2010-09-23 | 2013-04-09 | Chevron U.S.A. Inc. | Method to control particulate matter emissions |
| CN106938849A (en) * | 2016-12-13 | 2017-07-11 | 江苏天诺新材料科技股份有限公司 | The method that the molecular sieves of ZSM 5 are synthesized using waste and old molecular sieve catalyst |
| EP3860745A1 (en) * | 2018-10-01 | 2021-08-11 | Shell Internationale Research Maatschappij B.V. | Process for removing catalyst fines by nanofiltration |
| CN109225320B (en) * | 2018-11-05 | 2021-09-21 | 宁夏大学 | Method for crystallization regeneration of waste molecular sieve with MFI structure |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3338821A (en) * | 1964-11-18 | 1967-08-29 | Phillips Petroleum Co | Quenching of catalytic cracking reactor vapors in feed line to fractionator |
| US3380911A (en) * | 1966-02-15 | 1968-04-30 | Mobil Oil Corp | Method for converting hydrocarbons in two stages |
| US3527694A (en) * | 1968-12-09 | 1970-09-08 | Exxon Research Engineering Co | Fluid solids system |
| US3758403A (en) * | 1970-10-06 | 1973-09-11 | Mobil Oil | Olites catalytic cracking of hydrocarbons with mixture of zsm-5 and other ze |
| US3928158A (en) * | 1973-05-22 | 1975-12-23 | Gulf Research Development Co | Electrofilter |
| US4022675A (en) * | 1975-08-01 | 1977-05-10 | Gulf Research & Development Company | Filtering process |
| US4385805A (en) * | 1978-05-03 | 1983-05-31 | Rca Corporation | Liquid crystal lens display system |
| US4309279A (en) * | 1979-06-21 | 1982-01-05 | Mobil Oil Corporation | Octane and total yield improvement in catalytic cracking |
| US4285805A (en) * | 1980-03-20 | 1981-08-25 | Phillips Petroleum Company | Time-delay process and control system for electrostatic filter |
| US4309280A (en) * | 1980-07-18 | 1982-01-05 | Mobil Oil Corporation | Promotion of cracking catalyst octane yield performance |
| US4345991A (en) * | 1980-12-10 | 1982-08-24 | Phillips Petroleum Company | Catalytic cracking process |
| US4490241A (en) * | 1983-04-26 | 1984-12-25 | Mobil Oil Corporation | Secondary injection of ZSM-5 type zeolite in catalytic cracking |
-
1984
- 1984-12-21 AU AU37061/84A patent/AU555438B2/en not_active Ceased
- 1984-12-27 CA CA000471030A patent/CA1241613A/en not_active Expired
- 1984-12-27 JP JP27426484A patent/JPS60158290A/en active Granted
- 1984-12-27 EP EP84309081A patent/EP0148024A3/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| EP0148024A3 (en) | 1986-12-17 |
| AU555438B2 (en) | 1986-09-25 |
| JPH0149439B2 (en) | 1989-10-24 |
| JPS60158290A (en) | 1985-08-19 |
| AU3706184A (en) | 1985-07-11 |
| EP0148024A2 (en) | 1985-07-10 |
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