CA1055915A - Method and system for regenerating fluidizable catalyst particles - Google Patents
Method and system for regenerating fluidizable catalyst particlesInfo
- Publication number
- CA1055915A CA1055915A CA226,635A CA226635A CA1055915A CA 1055915 A CA1055915 A CA 1055915A CA 226635 A CA226635 A CA 226635A CA 1055915 A CA1055915 A CA 1055915A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- phase
- regeneration
- temperature
- zone
- 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
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
Abstract
METHOD AND SYSTEM FOR REGENERATING
FLUIDIZABLE CATALYST PARTICLES
ABSTRACT
A hydrocarbon conversion-catalyst regeneration operation is described which relies upon an upflowing fluid catalyst mass of decreasing particle density superimposed by an upflowing dispersed catalyst phase undergoing catalyst regeneration to effect elevated temperature regeneration of catalyst deactivated by hydrocarbonaceous material under conditions providing CO levels less than 0.15 mol percent in the flue gas. Regenerated catalyst is mixed with spent catalyst in a first contact zone to obtain an initial mix temperature of at least 1175°F. before contact with a second-ary oxygen containing regeneration gas stream as a part of the upflowing fluid catalyst mass. The ratio of hot regenerated catalyst to spent catalyst is restricted to obtain a mix temperature particularly promoting the combustion of hydro-carbonaceous material with oxygen containing gas in the up-flowing dense and dispersed catalyst phase so as to provide a discharged dispersed catalyst phase temperature of at least 1350°F.
FLUIDIZABLE CATALYST PARTICLES
ABSTRACT
A hydrocarbon conversion-catalyst regeneration operation is described which relies upon an upflowing fluid catalyst mass of decreasing particle density superimposed by an upflowing dispersed catalyst phase undergoing catalyst regeneration to effect elevated temperature regeneration of catalyst deactivated by hydrocarbonaceous material under conditions providing CO levels less than 0.15 mol percent in the flue gas. Regenerated catalyst is mixed with spent catalyst in a first contact zone to obtain an initial mix temperature of at least 1175°F. before contact with a second-ary oxygen containing regeneration gas stream as a part of the upflowing fluid catalyst mass. The ratio of hot regenerated catalyst to spent catalyst is restricted to obtain a mix temperature particularly promoting the combustion of hydro-carbonaceous material with oxygen containing gas in the up-flowing dense and dispersed catalyst phase so as to provide a discharged dispersed catalyst phase temperature of at least 1350°F.
Description
~05S9~5 BACKGROUND OF THE INVENTION
The field of catalytic cracking and particularly fluid catalyst operations have undergone significant development improvements due primarily to advances in catalyst technology and product distribution obtained therefrom. With the advent of high activity catalyst and particularly crystalline zeolite cracking catalysts, new areas of operating technology have been encountered requiring even further refinements in processing tech-niques to take advantage of the high catalyst activity, selectivity and operating sensitivity. The present invention therefore is concerned with a combination operation comprising hydrocarbon conversion and regener-ation of the catalyst employed therein. In a particular aspect the present invention is concerned with the tech-nique of regenerating a low coke producing crystalline zeolite hydrocarbon conversion catalyst containing de-activating deposits of carbonaceous material.
SUMMARY OF THE INVENTION
The present invention relates to the conversion of hydrocarbon feed materials in the presence of high activity fluidizable crystalline zeolite containing catalyst particles and the regeneration of the catalyst particles to remove deactivating coke deposits by burning.
In a more particular aspect the present invention is concerned with the method and system for regenerating fluidizable catalyst particles and particularly a crystal-line zeolite containing cracking catalyst containing ~7
The field of catalytic cracking and particularly fluid catalyst operations have undergone significant development improvements due primarily to advances in catalyst technology and product distribution obtained therefrom. With the advent of high activity catalyst and particularly crystalline zeolite cracking catalysts, new areas of operating technology have been encountered requiring even further refinements in processing tech-niques to take advantage of the high catalyst activity, selectivity and operating sensitivity. The present invention therefore is concerned with a combination operation comprising hydrocarbon conversion and regener-ation of the catalyst employed therein. In a particular aspect the present invention is concerned with the tech-nique of regenerating a low coke producing crystalline zeolite hydrocarbon conversion catalyst containing de-activating deposits of carbonaceous material.
SUMMARY OF THE INVENTION
The present invention relates to the conversion of hydrocarbon feed materials in the presence of high activity fluidizable crystalline zeolite containing catalyst particles and the regeneration of the catalyst particles to remove deactivating coke deposits by burning.
In a more particular aspect the present invention is concerned with the method and system for regenerating fluidizable catalyst particles and particularly a crystal-line zeolite containing cracking catalyst containing ~7
-2-carbonaceous dèposits under highly efficient regenerating conditions promoting the recovery of heat available through the burning of the carbonaceous deposits of a hydrocarbon conversion operation. In yet another aspect, the invention is concerned with a particular relationship of operating para~eters coupled in a manner promoting a suspended catalyst phase removal of deactivating deposits of carbonaceous material from high activity hydrocarbon conversion catalyst particles and heating thereof to an elevated temperature.
Thus, the invention in its brsadest sense relates to a process for regenerating a crystalline zeolite hydrocarbon con-version catalyst which comprises mixing a catalyst containing crystalline zeolite hydrocarbon conversion catalyst deactivated with carbonaceous deposits with sufficient hot regenerated catalyst to provide a mix temperature of at least 1135F. This catalyst mixture suspended in oxygen containing regeneration gases is then passed upwardly through a riser discharging into a dense fluid bed of catalyst particles. Sufficient oxygen containing re-generating gases are passed into the dense fluid bed of catalyst to carry the catalyst upwardly through a dispersed phase of catalyst particles into a catalyst separating and collecting zone. The temperature of the catalyst mixture passing through the dense catalyst phase and the dilute catalyst phase is raised to at least 1350F. and a portion of this hot regenerated catalyst separated from the dispersed catalyst phase is recycled directly to the riser mixing zone.
In order to achieve the desired mix temperature, a ratio of regenerated catalyst particles to deactivated 30 catalyst particles in the range of 0.5 to 4.0/1 is pre-ferably used, with a ratio of 0.8 to 4.0/1 being particularly ~ _ 3 _ B
preferred.
In one aspect of the hydrocarbon conversion-catalyst regeneration system of the present invention, a relatively dense fluid upflowing catalyst mass in open communication with an upflowing more dispersed phase catalyst regeneration is employed for effecting a relatively high temperature regeneration of catalyst particles and combustion of formed carbon monoxide. Regenerated catalyst is collected and transferred to an adjacent riser hydrocarbon conversion operation wherein at a temperature of at least about 900F.
conversion of a hydrocarbon feed such as gas oil and higher and lower boilding materials is accomplished with the hot regenerated cracking catalyst. The catalyst employed is preferably a high activity crystalline zeolite catalyst of fluidizable particle size which is transferred in suspended phase condition through one or more riser conversion zones providing a hydrocarbon residence time in the range of 0.5 to about 10 seconds and more usually less than about 8 seconds.
High temperature riser conversions of 1000F. at 1 to 4 seconds hydrocarbon residence time is desirable for some operations before separating vaporous - 3a -hydrocarbon materials comprising hydrocarbon conversion products from suspended catalyst. Cyclonic separation of catalyst frorn hydrocarbons is particularly desirable for restricting hydrocarbon residence time. During the hydrocarbon conversion step, carbonaceous deposits accumu-late on the catalyst particles and the particles entrain some hydrocarbon vapors upon removal from the catalyst separation step. The entrained hydrocarbons are thereafter removed from the catalyst with stripping gas in a separate catalyst stripping zone. Hydrocarbon conversion products separated from the catalyst and stripped materials are combined and passed to a product fractionation step.
Stripped catalyst containing deactivating amounts of carbonaceous material hereinafter referred to as coke is then passed to the catalyst regeneration operation of the present invention.
The regeneration technique and system of the present invention is unique in many respects for accomplish-ing the efficient removal of carbonaceous material or coke deposits on the catalyst particles. The recovery of heat available through such a coke rernoval operation is particularly desirable. The regeneration technique of this invention relies upon forming an initial mix of deactivated catalyst with hot regenerated catalyst to provide a predetermined mix temperature which is discharged into the lower portion of an upflowing dense fluid mass of catalyst of decreasing density of suspended catalyst particles. A relatively high temperature profile is maintained in the catalyst regeneration combination of this invention in which the density of catalyst particle in regeneration gas varies considerably and is generally in the ran(~e of about 2 to 40 lbs/cu. ft. but it may be as low as about 1.5 lbs/cu. ft. The regeneration gas velocity in the upflowing mass of catalyst is preferably at least
Thus, the invention in its brsadest sense relates to a process for regenerating a crystalline zeolite hydrocarbon con-version catalyst which comprises mixing a catalyst containing crystalline zeolite hydrocarbon conversion catalyst deactivated with carbonaceous deposits with sufficient hot regenerated catalyst to provide a mix temperature of at least 1135F. This catalyst mixture suspended in oxygen containing regeneration gases is then passed upwardly through a riser discharging into a dense fluid bed of catalyst particles. Sufficient oxygen containing re-generating gases are passed into the dense fluid bed of catalyst to carry the catalyst upwardly through a dispersed phase of catalyst particles into a catalyst separating and collecting zone. The temperature of the catalyst mixture passing through the dense catalyst phase and the dilute catalyst phase is raised to at least 1350F. and a portion of this hot regenerated catalyst separated from the dispersed catalyst phase is recycled directly to the riser mixing zone.
In order to achieve the desired mix temperature, a ratio of regenerated catalyst particles to deactivated 30 catalyst particles in the range of 0.5 to 4.0/1 is pre-ferably used, with a ratio of 0.8 to 4.0/1 being particularly ~ _ 3 _ B
preferred.
In one aspect of the hydrocarbon conversion-catalyst regeneration system of the present invention, a relatively dense fluid upflowing catalyst mass in open communication with an upflowing more dispersed phase catalyst regeneration is employed for effecting a relatively high temperature regeneration of catalyst particles and combustion of formed carbon monoxide. Regenerated catalyst is collected and transferred to an adjacent riser hydrocarbon conversion operation wherein at a temperature of at least about 900F.
conversion of a hydrocarbon feed such as gas oil and higher and lower boilding materials is accomplished with the hot regenerated cracking catalyst. The catalyst employed is preferably a high activity crystalline zeolite catalyst of fluidizable particle size which is transferred in suspended phase condition through one or more riser conversion zones providing a hydrocarbon residence time in the range of 0.5 to about 10 seconds and more usually less than about 8 seconds.
High temperature riser conversions of 1000F. at 1 to 4 seconds hydrocarbon residence time is desirable for some operations before separating vaporous - 3a -hydrocarbon materials comprising hydrocarbon conversion products from suspended catalyst. Cyclonic separation of catalyst frorn hydrocarbons is particularly desirable for restricting hydrocarbon residence time. During the hydrocarbon conversion step, carbonaceous deposits accumu-late on the catalyst particles and the particles entrain some hydrocarbon vapors upon removal from the catalyst separation step. The entrained hydrocarbons are thereafter removed from the catalyst with stripping gas in a separate catalyst stripping zone. Hydrocarbon conversion products separated from the catalyst and stripped materials are combined and passed to a product fractionation step.
Stripped catalyst containing deactivating amounts of carbonaceous material hereinafter referred to as coke is then passed to the catalyst regeneration operation of the present invention.
The regeneration technique and system of the present invention is unique in many respects for accomplish-ing the efficient removal of carbonaceous material or coke deposits on the catalyst particles. The recovery of heat available through such a coke rernoval operation is particularly desirable. The regeneration technique of this invention relies upon forming an initial mix of deactivated catalyst with hot regenerated catalyst to provide a predetermined mix temperature which is discharged into the lower portion of an upflowing dense fluid mass of catalyst of decreasing density of suspended catalyst particles. A relatively high temperature profile is maintained in the catalyst regeneration combination of this invention in which the density of catalyst particle in regeneration gas varies considerably and is generally in the ran(~e of about 2 to 40 lbs/cu. ft. but it may be as low as about 1.5 lbs/cu. ft. The regeneration gas velocity in the upflowing mass of catalyst is preferably at least
3 ft./sec. to obtain the desired upward catalyst flow in a restricted regeneration zone of smaller diameter in the upper portion than in the lower portion thereof and tapered therebetween. In some respects the regeneration zone resembles a bud vase in cross section to which the catalyst mix is introduced by riser means.
The high temperature profile of the regeneration operation is initially promoted by the mixing of hot regenerated catalyst with stripped deactivated catalyst in the lower portion of an initial riser mixing zone to provide an initial catalyst mix temperature of at leaat 1175F. and preferably about 1200F. so that upon contact with oxygen containing regeneration gas such as air com-bustion of carbonaceous deposits is rapidly promoted.
Thus, in the system of the present invention a required amount of hot regenerated catalyst mixed with coke deactivated catalyst in the riser is conveyed with oxygen containing gas into the lower portion of an upflowing relatively dense fluid mass of catalyst undergoing regeneration. Additional regeneration gas at an elevated temperature is passed into the bottom or lower portion of the dense catalyst mass portion of the regeneration operation. In the dense fluid mass section of catalyst regeneration, additional secondary regeneration oxygen containing gas or air is added to the catalyst thereby causing it to move upwardly through the regeneration zone. Provision is also made for adding supplemental oxyge~n containing regeneration gas to one or more upper portions of the riser regeneration zone to promote the conversion of CO to CO2. In this arrangement, it has been found that to high a particle density in the upflowing dispersed catalyst phase may operate to quench the conversion of CO to CO2 desired to be accomplished before discharge from the riser regenerator into the enlarged catalyst settling zone. Elowever, maintaining a particle density in the suspended catalyst phase below about ~ lbs/cu. ft.
and more usually about 5 lbs/cu. ft. permits burning of CO in an upper portion of the riser regeneration section as well as in the enlarged settling section under even lower catalyst particle density conditions.
The riser regeneration zone or regeneration vessel may take on substantially any shape, cylindrical, tapered or shaped as shown in the drawing or a combination thereof which will provide the restricted operating parameters of the invention as herein defined.
The regenerating technique and system of this invention relies upon forming an initial high mix temp-erature with regenerated and coke deactivated catalyst to initiate coke burning temperature conditions. A dense and dispersed catalyst phase regeneration system promoting the conversion of formed CO to CO2 is particularly promoted and the recovery of heat thus generated is absorbed by catalyst particles dispersed therein. In this combination the combustion gas-catalyst particle suspension discharged from the upper end of the riser regeneration zone will normally reach a tem-perature of at least about 1350F., preferably 1350 - 1400F., e.g. 1380F. In such a system the first oxygen containing regeneration gas stream is introduced with the catalyst mix to the bottom or lower portion of a relatively large mass of catalyst in the lower portion of the re~eneration zone and secondary regeneration gas is introduced to a lower portion of the cross sectional area of the large mass of catalyst in regeneration section as required. One or more downstream regeneration gas inlets are also provided to promote a more complete conversion of coke deposits and CO to CO2. Preheating of the primary regenerated gas stream is desirable and more usually practiced with low coke producing crystalline zeo-lite catalyst conversion systems so that an initial catalyst mix temperature of at least 1175F. in the dense fluid bed of catalyst will be more easily attained.
In the arrangement of the present invention it is contemplated supplementing residual carbonaceous material such as coke transferred to the regeneration system by the introduction of torch oil. In a particular aspect it is contemplated adding torch oil to the spent catalyst passed to the riser mixing zone or the torch oil may be added with the air passed to the riser mixing zone. It also is con-templated adding the-torch oil to an air line burner exit to aid with vaporization of the torch oil. On the other hand, a second torch oil vaporizer may be separately employed for injecting torch oil at spaced apart intervals across a lower portion of the dense fluid bed of catalyst to be regenerated.
It is preferred in the combination operation of this invention 10559~5 to inject the torch oil to the riser mixing zone along with regeneration air as more specifically shown in the drawing.
The regenerating technique of the present invention relies upon a particular relationship of operating parameters which will accomplish the removal of carbonaceous deposits down to at least .OS weight percent and preferably as low as about .03 weight percent or lower in combination with limiting the amount of carbon monoxide in the combustion flue gases not to exceed about 0.15 mole percent. Thus it is essential to the processing concepts of this invention to rapidly initiate burning of deposited carbonaceous material at an elevated temperature of at least about 1175 F. with an amount of oxygen containing regenerating gas such as air providing a catalyst temperature rise of at least about 100 degrees and preferably sufficient to heat the catalyst particles carried through the regeneration system to an elevated temperature of at least 1300F. Furthermore, to reap the advantage of the heat generated in the system, the regeneration gas flow rate is selected to provide a density of catalyst particles in the enlarged bottom portion of the regeneration zone within the range of 10 to 40 lbs/cu. ft. and in the upper more dispersed catalyst phase section thereof adjacent the discharge therefrom at a density of catalyst particles as low as about 2 lbs/cu. ft. and preferably not above about 8 lbs/cu. ft.
It will be recognized from the above discussion that a relatively delicate balance in operating parameters is maintained to obtain a desired coke burning and removal thereof without producing undesired oxygen and carbon monoxide concentrations in the combustion flue gases and these operating restrictions are dictated in substantial measure by the ratio of hot regenerated catalyst that can be mixed with spent catalyst obtained from hydrocarbon conversion. For example, it has been observed that low initial catalyst mix ratios of regenerated catalyst to spent catalyst are accompanied by high concentrations of carbon monoxide and oxygen being emitted from the regenerator riser to the outlet cyclones. However, as the carbon on spent catalyst is increased by a change in feed reaction conditions etc. or by the addition of torch oil, for example, in the regeneration system, the mix ratio of regenerated catalyst to spent catalyst must be adjusted as required to provide the desired temperature profile in the regenerator.
BRIEF DESCRIPTION OF THE DRAr~ING
.
The figure presents diagrammatically in elevation one arrangement of apparatus for accomplishing the catalytic conversion of hydrocarbons and the regeneration of catalyst particles in an upflowing catalyst regeneration zone wherein an upflowing relatively dense fluid mass of catalyst is transformed into a more dispersed catalyst phase regeneration operation before separation of flue gases of restricted CO content from regenerated catalyst particles is accomplished.
DISCUSSION OF SPECIFIC EMBODIMENT
Referring now to the drawing, a hydrocarbon feed such as a gas oil boiling range feed is introduced by conduit 2 to the bottom of a riser conversion zone 4.
Hot regenerated catalyst in conduit 6 provided with flow control valve 8 enters the bottom portion of riser 4 for admixture with the oil feed to form a catalyst-oil suspension at an elevated conversion temperature of at least about 850F. and more usually at least 1000F.
Additional gasiform reactant material comprising C5 and lighter hydrocarbons, related alcohols and ethers may also be introduced with the gas oil feed. The suspension formed is passed upwardly through the riser conversion zone under hydrocarbon conversion conditions promoting the cracking of the gas oil feed to lower and higher boiling products including carbonaceous material deposited on the catalyst. The products include gasoline, fuel oils and normally gaseous hydrocarbon products. The hydrocarbon feed with suspended catalyst particles may be maintained in the riser conversion zone for a hydrocarbon residence time within the range of 1 to 10 seconds. However, a hydrocarbon residence time within the range of 0.5 to 4 seconds may be employed with particular advantage when using hydrocarbon conversion temperatures up to about 1100F. Spaced apart hydrocarbon feed inlets 2' and 2" are provided in riser 4. The suspension is discharged from the upper end of the riser conversion zone into two or more cyclonic separating means 14 and 14' as shown. Stripping gas and stripped hydrocarbons pass through cyclonic separating means 16. Of course cyclone separators 14 and 16 may each be a plurality of cyclonic separation means suitably connected to accomplish the results desired. Gasiform hydrocarbon material and stripping gas obtained as provided below is withdrawn by conduits 18 and 20 communicating with plenum chamber 22 and withdrawal conduit 24. Conduit 24 communicates with product separation equipment not shown. Catalyst 10559~5 particles separated by the velocity reduction above discussed and by cyclonic means are collected as a bed of catalyst 26 which moves downwardly through a stripping vessel and countercurrent to rising stripping gas such as steam introduced by conduit 28. The stripping gas maintains the bed of catalyst 26 in a fluid condition and removes entrained hydrocarbon vapors and other strippable material flom the catalyst as the catalyst moves downwardly through the stripping zone. Stripped catalyst is withdrawn by standpipe 30 provided with flow control valve 32 and is passed to the bottom portion of a riser mixing-catalyst regeneration zone 34 shown. Riser 34 discharges into the lower portion of a dense fluid bed or mass of catalyst to be regenerated as herein provided. Regenerated catalyst obtained as hereinafter defined, withdrawn by standpipe 36 and provided with flow control valve 38 communicates with the lower portion of riser 34 and provides the hot regenerated catalyst at a temperature of at least 1300 F.
for mixing with the spent catalyst at a lower temperature in the range of about 850F. up to about 1000F.
In the enlarged settling section comprising the upper enlarged portion of the regenerator vessel about the upper end of riser 34 a dense fluid bed of catalyst comprising the collected hot freshly regenerated catalyst particles are maintained in a dense fluid bed condition by a hot fluidizing gas such as hot CO2 rich product gas added by conduits 39 and 41. In the bottom enlarged bulb portion of the catalyst regenerator, a relatively large dense fluid bed or mass of catalyst p~ cles is formed providing a mixture temperature of at least 1175F. and a density of catalyst particles ~)55915 within the range of 10 to 40 lb/cu. ft. A first regeneration gas inlet stream 44 is provided in the bottom portion of riser 34 to which the catalyst streams are initially fed.
Heating of the regeneration gas or air stream introduced by conduits 40, 42 and 44 is preferred. Thus with a spent catalyst temperature of about 960 F. and containing 0.9 wt. ~ carbon thereon, it is desirable to preheat the regeneration gas to about 325F. and use a 1 to 1 ratio of spent catalyst to recycle regenerated catalyst at a temperature of about 1350F. In the dense fluid bed of catalyst, the temperature of the bed is caused to be elevated by the burning of carbonaceous material with introduced oxygen containing regeneration gas. Furthermore, combustion of carbonaceous material is rapidly initiated by the hot catalyst mix so that catalyst particles carried into the dense bed of catalyst by oxygen containing combustion gases and overhead therefrom will complete the removal of carbonaceous deposits, transform carbon monoxide to carbon dioxide and produce a less dense catalyst-combustion gas suspension temperature of at least 1350F. and preferably at least about 1375F. As mentioned above, the density of particles in the upwardly flowing suspension is decreased in the direction of flow to at least 8 lbs/cu. ft. and preferably it is reduced to 3-5 lbs/cu. ft. before discharge from the riser regenerator into an enlarged catalyst separation zone. In any event the suspended catalyst phase passing into cyclonic separating means in the enlarged settling zone will be less than 3 lbs/cu. ft.
The catalyst regeneration-combustion gas suspension is discharged from the upper end of riser regenerator 46 through a plurality of outwardly extending ~12-10559~5 arms provided with downwardly facing openings. Additional oxygen containing gas such as air may be added to the upflowing suspension in riser 46 by one or more spaced inlets represented by conduit 48. The catalyst-combustion gas suspension passed upwardly through the restricted cross-sectional regeneration zone or riser 46 discharges against the upper closed end 50 which deflects the suspension outwardly through a plurality of elongated peripheral slots or suitable arms with openings that open generally downwardly into an enlarged settling zone 52. Discharging the suspension into the enlarged zone 52 lowers the velocity of the suspension thereby causing the catalyst particles to settle out and separate from flue gases.
In settling zone 52 a major portion of the catalyst particles separates from the combustion flue gases by a reduction in gas velocity before the flue gases pass through a plurality of cyclone separators represented by separators 54 and 56. Combustion flue gases comprising carbon dioxide rich gases are removed from separators 54 and 56 by conduits 58 and 60, plenum chamber 62 and withdrawal conduit 64.
Catalyst particles separated at an elevated regeneration temperature as above identified are collected as an annular dense fluid bed of catalyst 66 about an upper portion of regenerator riser 46 at an elevated temperature up to about 1400F. from which regenerated catalyst is withdrawn by standpipes 6 and 36 as herein discussed.
The catalyst regeneration method and system of the present invention is unique over that of the known prior art by at least the riser mixing of hot freshly regenerated catalyst with coke contaminated catalyst separated from the conversion zone in an amount sufficient to provide an elevated mix temperature of at least 1175F.
This high temperature mix of catalyst is sufficient for promoting the combustion of carbonaceous deposits in the presence of added oxygen containing regeneration gas such as air in an initial riser contact zone and the conversion of formed carbon monoxide to carbon dioxide is particularly promoted on a once through basis in an upflowing suspended catalyst atmosphere thereabove varying in particle density from about 40 lb/cu. ft. down to about 3 lbs/cu. ft. and less.
Having thus generally described the invention and discussed specific embodiments in support thereof, it is to be understood that no undue restrictions are to be imposed by reason thereof.
The high temperature profile of the regeneration operation is initially promoted by the mixing of hot regenerated catalyst with stripped deactivated catalyst in the lower portion of an initial riser mixing zone to provide an initial catalyst mix temperature of at leaat 1175F. and preferably about 1200F. so that upon contact with oxygen containing regeneration gas such as air com-bustion of carbonaceous deposits is rapidly promoted.
Thus, in the system of the present invention a required amount of hot regenerated catalyst mixed with coke deactivated catalyst in the riser is conveyed with oxygen containing gas into the lower portion of an upflowing relatively dense fluid mass of catalyst undergoing regeneration. Additional regeneration gas at an elevated temperature is passed into the bottom or lower portion of the dense catalyst mass portion of the regeneration operation. In the dense fluid mass section of catalyst regeneration, additional secondary regeneration oxygen containing gas or air is added to the catalyst thereby causing it to move upwardly through the regeneration zone. Provision is also made for adding supplemental oxyge~n containing regeneration gas to one or more upper portions of the riser regeneration zone to promote the conversion of CO to CO2. In this arrangement, it has been found that to high a particle density in the upflowing dispersed catalyst phase may operate to quench the conversion of CO to CO2 desired to be accomplished before discharge from the riser regenerator into the enlarged catalyst settling zone. Elowever, maintaining a particle density in the suspended catalyst phase below about ~ lbs/cu. ft.
and more usually about 5 lbs/cu. ft. permits burning of CO in an upper portion of the riser regeneration section as well as in the enlarged settling section under even lower catalyst particle density conditions.
The riser regeneration zone or regeneration vessel may take on substantially any shape, cylindrical, tapered or shaped as shown in the drawing or a combination thereof which will provide the restricted operating parameters of the invention as herein defined.
The regenerating technique and system of this invention relies upon forming an initial high mix temp-erature with regenerated and coke deactivated catalyst to initiate coke burning temperature conditions. A dense and dispersed catalyst phase regeneration system promoting the conversion of formed CO to CO2 is particularly promoted and the recovery of heat thus generated is absorbed by catalyst particles dispersed therein. In this combination the combustion gas-catalyst particle suspension discharged from the upper end of the riser regeneration zone will normally reach a tem-perature of at least about 1350F., preferably 1350 - 1400F., e.g. 1380F. In such a system the first oxygen containing regeneration gas stream is introduced with the catalyst mix to the bottom or lower portion of a relatively large mass of catalyst in the lower portion of the re~eneration zone and secondary regeneration gas is introduced to a lower portion of the cross sectional area of the large mass of catalyst in regeneration section as required. One or more downstream regeneration gas inlets are also provided to promote a more complete conversion of coke deposits and CO to CO2. Preheating of the primary regenerated gas stream is desirable and more usually practiced with low coke producing crystalline zeo-lite catalyst conversion systems so that an initial catalyst mix temperature of at least 1175F. in the dense fluid bed of catalyst will be more easily attained.
In the arrangement of the present invention it is contemplated supplementing residual carbonaceous material such as coke transferred to the regeneration system by the introduction of torch oil. In a particular aspect it is contemplated adding torch oil to the spent catalyst passed to the riser mixing zone or the torch oil may be added with the air passed to the riser mixing zone. It also is con-templated adding the-torch oil to an air line burner exit to aid with vaporization of the torch oil. On the other hand, a second torch oil vaporizer may be separately employed for injecting torch oil at spaced apart intervals across a lower portion of the dense fluid bed of catalyst to be regenerated.
It is preferred in the combination operation of this invention 10559~5 to inject the torch oil to the riser mixing zone along with regeneration air as more specifically shown in the drawing.
The regenerating technique of the present invention relies upon a particular relationship of operating parameters which will accomplish the removal of carbonaceous deposits down to at least .OS weight percent and preferably as low as about .03 weight percent or lower in combination with limiting the amount of carbon monoxide in the combustion flue gases not to exceed about 0.15 mole percent. Thus it is essential to the processing concepts of this invention to rapidly initiate burning of deposited carbonaceous material at an elevated temperature of at least about 1175 F. with an amount of oxygen containing regenerating gas such as air providing a catalyst temperature rise of at least about 100 degrees and preferably sufficient to heat the catalyst particles carried through the regeneration system to an elevated temperature of at least 1300F. Furthermore, to reap the advantage of the heat generated in the system, the regeneration gas flow rate is selected to provide a density of catalyst particles in the enlarged bottom portion of the regeneration zone within the range of 10 to 40 lbs/cu. ft. and in the upper more dispersed catalyst phase section thereof adjacent the discharge therefrom at a density of catalyst particles as low as about 2 lbs/cu. ft. and preferably not above about 8 lbs/cu. ft.
It will be recognized from the above discussion that a relatively delicate balance in operating parameters is maintained to obtain a desired coke burning and removal thereof without producing undesired oxygen and carbon monoxide concentrations in the combustion flue gases and these operating restrictions are dictated in substantial measure by the ratio of hot regenerated catalyst that can be mixed with spent catalyst obtained from hydrocarbon conversion. For example, it has been observed that low initial catalyst mix ratios of regenerated catalyst to spent catalyst are accompanied by high concentrations of carbon monoxide and oxygen being emitted from the regenerator riser to the outlet cyclones. However, as the carbon on spent catalyst is increased by a change in feed reaction conditions etc. or by the addition of torch oil, for example, in the regeneration system, the mix ratio of regenerated catalyst to spent catalyst must be adjusted as required to provide the desired temperature profile in the regenerator.
BRIEF DESCRIPTION OF THE DRAr~ING
.
The figure presents diagrammatically in elevation one arrangement of apparatus for accomplishing the catalytic conversion of hydrocarbons and the regeneration of catalyst particles in an upflowing catalyst regeneration zone wherein an upflowing relatively dense fluid mass of catalyst is transformed into a more dispersed catalyst phase regeneration operation before separation of flue gases of restricted CO content from regenerated catalyst particles is accomplished.
DISCUSSION OF SPECIFIC EMBODIMENT
Referring now to the drawing, a hydrocarbon feed such as a gas oil boiling range feed is introduced by conduit 2 to the bottom of a riser conversion zone 4.
Hot regenerated catalyst in conduit 6 provided with flow control valve 8 enters the bottom portion of riser 4 for admixture with the oil feed to form a catalyst-oil suspension at an elevated conversion temperature of at least about 850F. and more usually at least 1000F.
Additional gasiform reactant material comprising C5 and lighter hydrocarbons, related alcohols and ethers may also be introduced with the gas oil feed. The suspension formed is passed upwardly through the riser conversion zone under hydrocarbon conversion conditions promoting the cracking of the gas oil feed to lower and higher boiling products including carbonaceous material deposited on the catalyst. The products include gasoline, fuel oils and normally gaseous hydrocarbon products. The hydrocarbon feed with suspended catalyst particles may be maintained in the riser conversion zone for a hydrocarbon residence time within the range of 1 to 10 seconds. However, a hydrocarbon residence time within the range of 0.5 to 4 seconds may be employed with particular advantage when using hydrocarbon conversion temperatures up to about 1100F. Spaced apart hydrocarbon feed inlets 2' and 2" are provided in riser 4. The suspension is discharged from the upper end of the riser conversion zone into two or more cyclonic separating means 14 and 14' as shown. Stripping gas and stripped hydrocarbons pass through cyclonic separating means 16. Of course cyclone separators 14 and 16 may each be a plurality of cyclonic separation means suitably connected to accomplish the results desired. Gasiform hydrocarbon material and stripping gas obtained as provided below is withdrawn by conduits 18 and 20 communicating with plenum chamber 22 and withdrawal conduit 24. Conduit 24 communicates with product separation equipment not shown. Catalyst 10559~5 particles separated by the velocity reduction above discussed and by cyclonic means are collected as a bed of catalyst 26 which moves downwardly through a stripping vessel and countercurrent to rising stripping gas such as steam introduced by conduit 28. The stripping gas maintains the bed of catalyst 26 in a fluid condition and removes entrained hydrocarbon vapors and other strippable material flom the catalyst as the catalyst moves downwardly through the stripping zone. Stripped catalyst is withdrawn by standpipe 30 provided with flow control valve 32 and is passed to the bottom portion of a riser mixing-catalyst regeneration zone 34 shown. Riser 34 discharges into the lower portion of a dense fluid bed or mass of catalyst to be regenerated as herein provided. Regenerated catalyst obtained as hereinafter defined, withdrawn by standpipe 36 and provided with flow control valve 38 communicates with the lower portion of riser 34 and provides the hot regenerated catalyst at a temperature of at least 1300 F.
for mixing with the spent catalyst at a lower temperature in the range of about 850F. up to about 1000F.
In the enlarged settling section comprising the upper enlarged portion of the regenerator vessel about the upper end of riser 34 a dense fluid bed of catalyst comprising the collected hot freshly regenerated catalyst particles are maintained in a dense fluid bed condition by a hot fluidizing gas such as hot CO2 rich product gas added by conduits 39 and 41. In the bottom enlarged bulb portion of the catalyst regenerator, a relatively large dense fluid bed or mass of catalyst p~ cles is formed providing a mixture temperature of at least 1175F. and a density of catalyst particles ~)55915 within the range of 10 to 40 lb/cu. ft. A first regeneration gas inlet stream 44 is provided in the bottom portion of riser 34 to which the catalyst streams are initially fed.
Heating of the regeneration gas or air stream introduced by conduits 40, 42 and 44 is preferred. Thus with a spent catalyst temperature of about 960 F. and containing 0.9 wt. ~ carbon thereon, it is desirable to preheat the regeneration gas to about 325F. and use a 1 to 1 ratio of spent catalyst to recycle regenerated catalyst at a temperature of about 1350F. In the dense fluid bed of catalyst, the temperature of the bed is caused to be elevated by the burning of carbonaceous material with introduced oxygen containing regeneration gas. Furthermore, combustion of carbonaceous material is rapidly initiated by the hot catalyst mix so that catalyst particles carried into the dense bed of catalyst by oxygen containing combustion gases and overhead therefrom will complete the removal of carbonaceous deposits, transform carbon monoxide to carbon dioxide and produce a less dense catalyst-combustion gas suspension temperature of at least 1350F. and preferably at least about 1375F. As mentioned above, the density of particles in the upwardly flowing suspension is decreased in the direction of flow to at least 8 lbs/cu. ft. and preferably it is reduced to 3-5 lbs/cu. ft. before discharge from the riser regenerator into an enlarged catalyst separation zone. In any event the suspended catalyst phase passing into cyclonic separating means in the enlarged settling zone will be less than 3 lbs/cu. ft.
The catalyst regeneration-combustion gas suspension is discharged from the upper end of riser regenerator 46 through a plurality of outwardly extending ~12-10559~5 arms provided with downwardly facing openings. Additional oxygen containing gas such as air may be added to the upflowing suspension in riser 46 by one or more spaced inlets represented by conduit 48. The catalyst-combustion gas suspension passed upwardly through the restricted cross-sectional regeneration zone or riser 46 discharges against the upper closed end 50 which deflects the suspension outwardly through a plurality of elongated peripheral slots or suitable arms with openings that open generally downwardly into an enlarged settling zone 52. Discharging the suspension into the enlarged zone 52 lowers the velocity of the suspension thereby causing the catalyst particles to settle out and separate from flue gases.
In settling zone 52 a major portion of the catalyst particles separates from the combustion flue gases by a reduction in gas velocity before the flue gases pass through a plurality of cyclone separators represented by separators 54 and 56. Combustion flue gases comprising carbon dioxide rich gases are removed from separators 54 and 56 by conduits 58 and 60, plenum chamber 62 and withdrawal conduit 64.
Catalyst particles separated at an elevated regeneration temperature as above identified are collected as an annular dense fluid bed of catalyst 66 about an upper portion of regenerator riser 46 at an elevated temperature up to about 1400F. from which regenerated catalyst is withdrawn by standpipes 6 and 36 as herein discussed.
The catalyst regeneration method and system of the present invention is unique over that of the known prior art by at least the riser mixing of hot freshly regenerated catalyst with coke contaminated catalyst separated from the conversion zone in an amount sufficient to provide an elevated mix temperature of at least 1175F.
This high temperature mix of catalyst is sufficient for promoting the combustion of carbonaceous deposits in the presence of added oxygen containing regeneration gas such as air in an initial riser contact zone and the conversion of formed carbon monoxide to carbon dioxide is particularly promoted on a once through basis in an upflowing suspended catalyst atmosphere thereabove varying in particle density from about 40 lb/cu. ft. down to about 3 lbs/cu. ft. and less.
Having thus generally described the invention and discussed specific embodiments in support thereof, it is to be understood that no undue restrictions are to be imposed by reason thereof.
Claims (7)
1. A method for regenerating a crystalline zeolite hydro-carbon conversion catalyst which comprises mixing a crystalline zeolite containing hydrocarbon conversion catalyst deactivated with carbonaceous deposits with sufficient hot regenerated catalyst in a riser mixing zone to provide a mix temperature of at least 1175°F., passing the catalyst mixture thus formed suspended in oxygen containing regeneration gases upwardly through a first riser discharging into a dense fluid bed of catalyst particles, passing sufficient oxygen containing regeneration gases into said dense fluid bed of catalyst to carry the catalyst upwardly through a dispersed phase of cat-alyst particles into a catalyst separating and collecting zone, raising the temperature of the catalyst mixture passing through said dense catalyst phase and said dispersed catalyst phase to at least 1350°F., and recycling a portion of said hot regen-erated catalyst separated from said dispersed catalyst phase directly to the riser mixing zone.
2. In a process for converting hydrocarbons in the presence of fluidized crystalline zeolite cracking catalyst parti-cles and regeneration of the catalyst particles to remove deposited carbonaceous material by burning thereby heating the catalyst particles to an elevated temperature suitable for hydrocarbon conversion reactions, the improvement which comprises, combining crystalline zeolite catalyst particles contain-ing deactivating carbonaceous material in a riser mixing zone with hot freshly regenerated catalyst particles in amounts pro-viding a mix temperature of at least 1175°F., the ratio of regen-erated catalyst particles to deactivated catalyst particles being within the range of 0.5 to 4.0/1, passing the catalyst mix at a temperature of at least 1175°F. suspended in oxygen containing gas into the lower portion of an upwardly flowing fluid mass of catalyst, introducing additional preheated oxygen containing gas to a lower portion of said upwardly flowing fluid mass of catalyst in an amount further promoting the combustion of carbonaceous deposits and carbon monoxide, passing suspended catalyst particles overhead from said upwardly flowing fluid mass of catalyst with oxygen containing combustion gases upwardly through a dispersed catalyst phase regeneration zone, maintaining the ratio of oxygen containing regeneration gas with suspended catalyst passing from said upwardly flowing fluid mass of catalyst through said dispersed catalyst phase regeneration zone sufficient to raise the temperature thereof to at least 1350°F., and passing high temperature catalyst of at least 1350°F. separated from said dispersed phase regeneration zone directly to each of said hydrocarbon conversion zone and said riser mixing zone.
3. A method for regenerating a crystalline zeolite cracking catalyst of low coke producing characteristics obtained from a hydrocarbon conversion zone with deposited carbonaceous material, which comprises, providing a fluid mass of catalyst particles passing through a dense and a more dispersed phase of catalyst in a regeneration zone, mixing hot regenerated catalyst at a temperature of at least 1350°F. with catalyst containing carbonaceous deposits at a ratio within the range of 0.8 to 4.0/1, to give a catalyst mixture having a temperature of at least 1175°F., passing the mixed catalyst into the lower portion of the dense phase of catalyst in the regeneration zone with oxygen containing regeneration gas, raising the temperature of the catalyst mixture by burning carbonaceous deposits with oxygen containing gases, passing the catalyst during said burning operation overhead from said dense phase of catalyst through said dispersed catalyst phase with gaseous products of combustion comprising oxygen wherein the gases and entrained catalyst particles attain a temperature of at least 1350°F., maintaining excess oxygen in said entraining combustion gases in said dispersed phase regeneration operation, using temperature catalyst separated from said dispersed phase regeneration zone in said hydrocarbon conversion zone and passing a portion of said high temperature regenerated catalyst separated from said dispersed phase ergeneration before significant cooling thereof for admixture with contamin-ated catalyst passed to the lower portion of said dense phase of catalyst with regeneration gases.
4. A method of regenerating crystalline zeolite cracking catalyst particles containing deactivating amounts of carbonaceous material which comprises, (a) combining hot regenerated catalyst particles at a temperature with in the range of 1300 to 1400°F. with coke deactivated catalyst particles at a mix ratio within the range of 0.5 to 4.0/1 in the lower portion of a first riser contact zone, to provide a catalyst mixture having a temperature of at least 1175°F.
(b) contacting the mixture of regenerated catalyst and coke deactivated catalyst with oxygen containing regeneration gas in said first riser contact zone to form a suspension, passing the suspension into the lower portion of a dense fluid mass of catalyst superimposed by a dispersed catalyst phase mass upwardly extending regeneration zone, maintaining gas velocity conditions sufficient to contin-uously entrain catalyst from said dense catalyst mass upwardly through said dispersed catalyst phase zone during heating of the catalyst to a temperature within the range of 1350°F.
to 1400°F.
(c) separating catalyst particles from oxygen containing flue gases after traversing said dispersed catalyst phase regeneration zone and, (d) recycling portions of said catalyst separated from said dispersed catalyst phase regeneration zone for admixture with spent catalyst passed to said dense fluid mass of catalyst.
(b) contacting the mixture of regenerated catalyst and coke deactivated catalyst with oxygen containing regeneration gas in said first riser contact zone to form a suspension, passing the suspension into the lower portion of a dense fluid mass of catalyst superimposed by a dispersed catalyst phase mass upwardly extending regeneration zone, maintaining gas velocity conditions sufficient to contin-uously entrain catalyst from said dense catalyst mass upwardly through said dispersed catalyst phase zone during heating of the catalyst to a temperature within the range of 1350°F.
to 1400°F.
(c) separating catalyst particles from oxygen containing flue gases after traversing said dispersed catalyst phase regeneration zone and, (d) recycling portions of said catalyst separated from said dispersed catalyst phase regeneration zone for admixture with spent catalyst passed to said dense fluid mass of catalyst.
5. The method of claim 4 wherein the density of catalyst particles in said dense catalyst bed phase and said dis-persed phase varies from about 40 lbs./cu.ft. down to at least 3 lbs./cu.ft.
6. The method of claim 4 wherein the density of the catalyst particles in the flue gas discharged from the dis-persed phase regeneration zone is not above about 3 lbs./
cu.ft.
cu.ft.
7. The method of claim 4 wherein fluid gases recovered from hot regenerated catalyst contain not more than 0.20 mole percent CO.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US47972674A | 1974-06-17 | 1974-06-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1055915A true CA1055915A (en) | 1979-06-05 |
Family
ID=23905166
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA226,635A Expired CA1055915A (en) | 1974-06-17 | 1975-05-09 | Method and system for regenerating fluidizable catalyst particles |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS5847219B2 (en) |
| CA (1) | CA1055915A (en) |
| DE (1) | DE2526839A1 (en) |
| FR (1) | FR2274353A1 (en) |
| GB (1) | GB1495843A (en) |
| IT (1) | IT1039008B (en) |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4167492A (en) * | 1976-10-12 | 1979-09-11 | Uop Inc. | Spent-catalyst combustion regeneration process with recycle of hot regenerated catalyst and spent catalyst |
| US4118338A (en) * | 1977-09-01 | 1978-10-03 | Mobil Oil Corporation | Method for regenerating a fluid cracking catalyst |
| US4285908A (en) * | 1978-05-22 | 1981-08-25 | Uop Inc. | Catalyst regeneration apparatus |
| US4197189A (en) * | 1978-05-22 | 1980-04-08 | Uop Inc. | Catalyst regeneration process |
| US4219442A (en) * | 1978-12-14 | 1980-08-26 | Uop Inc. | Fluid coke contaminated catalyst regeneration process |
| US4309308A (en) * | 1978-12-14 | 1982-01-05 | Uop Inc. | Fluid catalyst regeneration process and apparatus |
| US4272402A (en) * | 1979-07-16 | 1981-06-09 | Cosden Technology, Inc. | Process for regenerating fluidizable particulate cracking catalysts |
| US4243634A (en) * | 1979-11-05 | 1981-01-06 | Uop Inc. | Fluid catalyst regeneration apparatus |
| US4371501A (en) * | 1980-02-04 | 1983-02-01 | Uop Inc. | Fluid catalyst regeneration apparatus |
| FR2476672B1 (en) * | 1980-02-25 | 1985-06-21 | Uop Inc | METHOD AND APPARATUS FOR REGENERATION OF A HYDROCARBON CONVERSION CATALYST |
| US4511434A (en) * | 1981-08-17 | 1985-04-16 | Standard Oil Company (Indiana) | Fluid bed retorting system |
| US4430300A (en) | 1981-09-17 | 1984-02-07 | Uop Inc. | Fluid catalyst regeneration apparatus |
| JPS61156514U (en) * | 1985-03-22 | 1986-09-29 | ||
| CA1333748C (en) * | 1987-12-30 | 1995-01-03 | John Duncan Humble | High efficiency regenerator apparatus |
| WO2003053558A2 (en) * | 2001-12-21 | 2003-07-03 | Shell Internationale Research Maatschappij B.V. | Process to regenerate fcc spent catalyst |
| EP3454985A4 (en) * | 2016-05-12 | 2019-12-18 | Uop Llc | Partial burn combustor regenerator |
| CN114516795A (en) * | 2022-02-25 | 2022-05-20 | 北京石油化工工程有限公司 | Method for producing methyl acrylate by using methanol and methyl acetate as raw materials |
| WO2024050014A1 (en) * | 2022-09-01 | 2024-03-07 | T.En Process Technology Inc. | Systems and processes for temperature control in fluidized catalytic cracking |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3351548A (en) * | 1965-06-28 | 1967-11-07 | Mobil Oil Corp | Cracking with catalyst having controlled residual coke |
| BE792165A (en) * | 1971-11-30 | 1973-05-30 | Standard Oil Co | PERFECTED PROCESS OF CATALYTIC CRACKING WITH SENSITIVELY COMPLETE COMBUSTION OF CARBON MONOXIDE DURING CATALYST REGENERATION |
-
1975
- 1975-05-09 CA CA226,635A patent/CA1055915A/en not_active Expired
- 1975-05-22 GB GB2225975A patent/GB1495843A/en not_active Expired
- 1975-06-04 FR FR7517380A patent/FR2274353A1/en active Granted
- 1975-06-16 DE DE19752526839 patent/DE2526839A1/en active Granted
- 1975-06-16 IT IT2439975A patent/IT1039008B/en active
- 1975-06-17 JP JP50072793A patent/JPS5847219B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| GB1495843A (en) | 1977-12-21 |
| JPS5847219B2 (en) | 1983-10-21 |
| FR2274353B1 (en) | 1978-09-22 |
| IT1039008B (en) | 1979-12-10 |
| JPS5113398A (en) | 1976-02-02 |
| FR2274353A1 (en) | 1976-01-09 |
| DE2526839C2 (en) | 1988-05-26 |
| DE2526839A1 (en) | 1976-01-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4283273A (en) | Method and system for regenerating fluidizable catalyst particles | |
| US4057397A (en) | System for regenerating fluidizable catalyst particles | |
| EP0106052B1 (en) | Demetallizing and decarbonizing heavy residual oil feeds | |
| US4419221A (en) | Cracking with short contact time and high temperatures | |
| US4219407A (en) | Fluid cracking process and the method for separating a suspension discharged from a riser cracking zone | |
| CA1055915A (en) | Method and system for regenerating fluidizable catalyst particles | |
| US4514285A (en) | Catalytic cracking system | |
| US4088568A (en) | Catalytic cracking of hydrocarbons | |
| US4116814A (en) | Method and system for effecting catalytic cracking of high boiling hydrocarbons with fluid conversion catalysts | |
| US4090948A (en) | Catalytic cracking process | |
| CA1140490A (en) | Method and apparatus for cracking residual oils | |
| EP0086580B1 (en) | Method and apparatus for fluid catalytic cracking | |
| EP0753037B1 (en) | Process and apparatus for producing light olefins | |
| US4118338A (en) | Method for regenerating a fluid cracking catalyst | |
| US4036779A (en) | Method of regenerating catalyst in a swirl type regenerator containing a dilute phase baffle | |
| US3904548A (en) | Regenerating catalyst with tangential introduction and circumferential swirl in a fluidized bed | |
| US3406112A (en) | Catalytic cracking process | |
| CA1058600A (en) | Method of regenerating a cracking catalyst with substantially complete combustion of carbon monoxide | |
| US3926843A (en) | Fcc ' 'multi-stage regeneration procedure | |
| US2965454A (en) | Fluidized conversion and stripping apparatus | |
| US4444722A (en) | System for regenerating fluidizable catalyst particles | |
| US3161582A (en) | Two-stage hydrocarbon conversion process | |
| US3970587A (en) | Combustion regeneration of hydrocarbon conversion catalyst with recycle of high temperature regenerated catalyst | |
| US4430201A (en) | Regeneration of fluidizable catalyst | |
| CA1110568A (en) | Fluid cracking process and the method for separating a suspension discharged from a riser cracking zone |