US3238271A - Cracking of hydrocarbons to gaseous olefines - Google Patents

Cracking of hydrocarbons to gaseous olefines Download PDF

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Publication number
US3238271A
US3238271A US95674A US9567461A US3238271A US 3238271 A US3238271 A US 3238271A US 95674 A US95674 A US 95674A US 9567461 A US9567461 A US 9567461A US 3238271 A US3238271 A US 3238271A
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reactor
gas
particles
regenerator
fluidized
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Expired - Lifetime
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US95674A
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Nonnenmacher Helmut
Sinn Richard
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BASF SE
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BASF SE
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    • 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
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
    • C10G47/30—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
    • C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S585/00—Chemistry of hydrocarbon compounds
    • Y10S585/909—Heat considerations
    • Y10S585/91—Exploiting or conserving heat of quenching, reaction, or regeneration

Definitions

  • This invention relates to a process for the cracking of hydrocarbons to gaseous olefines. More particularly, the invention relates to a cracking process in which crude oils and similar products are cracked in a fluidized bed to form gaseous olefines.
  • hydrocarbon oils such as crude oils, crude oil fractions or distillation residues
  • Ethylene, propylene, and other gaseous olefines can be produced by this process.
  • An inert solid is used as the heat carrier which usually is the petroleum coke formed in the process.
  • the petroleum coke is often used in a grain size of 50 to 400 microns, i.e., so fine that even in the down pipes it can be kept in pseudo-liquid condition by blowing in a ventilating gas.
  • Another known cracking method uses sand rather than coke as the heat carrier.
  • the sand is heated in an upcurrent pipe by burning the carbon deposits and residual oil adhering thereto. It is a disadvantage of this process, however, that mechanical control of the circulation of solid by means of throttle valves is necessary.
  • it is necessary by reason of the low resistance to fracture and attrition of sand at high temperatures, continuously to discharge relatively large amounts of fine dust and to replace it by fresh material.
  • Another object of the invention is to provide a process for cracking hydrocarbons by which it is possible to obtain a high throughput.
  • Another object of the invention is to provide a cracking process which can be carried out in a simple manner and which requires less complicated equipment than the known processes.
  • the invention comprises the discovery that hydrocarbons containing high boiling constituents can be cracked more efiiciently in a fluidized reactor where the fluidized particles have a grain size of between about 0.05 mm. and about 4.0 mm. and wherein at least 10% by weight of the particles have a grain diameter greater than 1 mm.
  • the diameter of the grain particles ranges between about 0.10 mm. and 3.0 mm. and at least 20% by weight of the particles have a grain diameter greater than 1 mm.
  • the hydrocarbons are cracked at temperatures from about 680 to about 850 C. to produce gaseous olefines such as ethylene and propylene.
  • the cracked gases and vapors leaving the fluidized reactor are freed in a cyclone from the bulk of the entrained solid particles and are then quenched to a temperature of less than 400 C. by oil residues formed in the process which boil above 200 C.
  • the cracked gases are then freed from residual solid particles and are separated in a fractionating column into vaporizable liquid, cracked oil, and cracked gas.
  • solid particles having high resistance to attrition and heat, and having a grain size of between about 0.05 mm. and about 4.0 mm. are circulated between the reactor and a regenerator.
  • Particles are withdrawn from the reactor in the regenerator through down pipes and are returned to both vessels through rising pipes.
  • the particles flow downwardly in the pipe as a compact mass.
  • the particles are then returned to the reactor and regenerator as a dilute suspension by means of proportioning or metering gases.
  • the heat necessary for the cracking reaction is produced by the combustion of carbon deposits formed on the inert particles and by combustion of part of the quenching oil in the regenerator.
  • the process is especially suitable for the pyrolytic cracking of hydrocarbons which contain high boiling constituents.
  • the inert incombustible solids used may be granular or globular solids having high resistance to attrition and heat and high stability to changes in temperature. It is advantageous to use inert solids which have a small inner surface and are not porous, for example aluminum silicates which contain 50% by weight or more ofaluminum oxide. Other inert solids can be used in place of aluminum silicates provided they have the above-specified properties at temperatures of 700 to 1,000 C. Examples are corundum, sillimanite and mullite.
  • the special grain size distribution of the solid incombustible solids makes it possible to apply high gas velocities. Therefore, only a small reaction space is necessary in the reactor and regenerator.
  • the coarse grains can be removed in the down pipe without the necessity of using special devices for controlling circulation. Circulation is controlled only by a gas proportioning means provided at the lower end of the down pipe. This is a special advantage because mechanical devices for controlling circulation as required in the conventional processes, which are difficult to operate at high temperatures and which are subject to considerable corrosion at high temperatures are not necessary in the instant process.
  • Starting materials for the instant process are crude oil and crude oil distillates, especially those having a final boiling point between 200 and 400 C. By final boiling point we understand the temperature at which a substance has passed over substantially without a residue. The distillates may also contain volatile components with boiling points below 200 C. Other starting materials are crude oil distillate residues and top crude oil. Besides ethylene and propylene, the main products formed in the cracking process, butylene and butadiene are obtained. Valuable by-products of the process include gases of high calorific value which can be processed into synthesis gas, low boiling aromatic compounds such as benzene and toluene.
  • the high boiling point constituents of the cracked product and the non-vaporizable portions are burned in the regenerator together with the carbon deposit to cover the heat requirement of the process.
  • the non-vaporizable fraction of the cracked product which contains asphalts and the solid washed out from the cracked gas, it is convenient to set up a small excess of oxygen of 0.3 to 3% by volume in the smoke gas. In this way and by a preliminary cracking on the hot heat carrier, the combustion in the regenerator can be carried out with optimum utilization of the heating power, i.e., without the formation of carbon monoxide.
  • the cyclone in the reactor is preferably adjusted so that not all the solid particles are separated and a certain concentration of solids is present in the gas outlet pipe.
  • the vapors should advantageously contain 5 to 50 grams per cubic meter (S.T.P.) of solid particles originating from the fluidized mass. This amount of solid particles is absorbed during quenching by the oil used for quenching which is partly injected into the regenerator to assist in covering the heat requirement.
  • the solid particles withdrawn from the reactor thus return to the regenerator by way of the quenching oil. At the same time, excessive enrichment of solid particles in the quenching oil is avoided. It is preferable to maintain a content of solid of less than by weight.
  • the process may be carried out, for example, in the following way: granular or globular inert solid particles, whose size lies between 0.05 and 4.0 mm. and which have been heated to a high temperature circulate in a system comprising a reactor fluidized layer, a regenerator fluidized layer and the two down pipes and rising pipes connecting them.
  • the dilute phases above the fluidized layers in the reactor and regenerator are preferably kept at the same pressure.
  • the liquid or partly vaporized initial oil may be injected into the fluidized layer of the reactor by means of an atomizing agent, for example, steam, and cracked therein at temepratures between about 680 and 850 C.
  • the preferred temperature range is between 720 and 780 C.
  • Superheated steam is preferred as the fluidizing gas.
  • the cracked gas and vapor leaving the reactor are first separated from the bulk of the entrained solids in a cyclone which leads back into the fluidized layer of the reactor.
  • the cyclone outlet is kept free from coke depos its by means of a small amount of solids not separated from the gas in the cyclone.
  • the cracked gas obtained is quenched to a temperature below 400 C. with the cracked oil residue boiling above 200 C. formed in the cracking, and at the same time the residual solid particles contained in the gas and any carbon black are washed out.
  • the cracked products are separated into condensable cracked oil and cracked gas.
  • the condensed fraction is returned from the bottoms of the column into the circulating quenching oil.
  • the cooled solid particles are withdrawn from the reactor fluidized layer through a down pipe and move as a compact mass downwardly through a substantially vertical tube. It is advantageous to arrange for a deviation from the vertical of not more than 20. In order that at such an inclination the same amount of solid should be conveyed, inclined pipes may be dimensioned about one and a half times the cross-section of a vertical pipe. At the lower end of the down pipe, the solid particles are supplied in a regulatable amount by a proportioning gas current to the actual conveyor gas stream and suspended therein.
  • part of this proportioning gas stream flows in countercurrent to the particles descending in the down pipe, the reducing medium in the reactor thus being separated from the oxidizing medium in the regenerator and the small amount of cracked gas entrained by the solid being stripped and re turned to the reactor.
  • steam is advantageous to use steam as the proportioning gas, but other gases, as for example nitrogen, smoke gas, hydrocarbons or even air, may also be used.
  • the overflow into the down pipe may be con structed as a stripper.
  • the conveyor gas for example, air, smoke gas, or nitrogen, carries the solid particles into the regenerator in which fluidization is effected with air or oxygen-containing gases, where it is heated to 700 to l,000 C.
  • the deposited coke adhering to the particles may be partly burnt off in the rising pipe.
  • part of the quenching oil together with the solids contained therein and originating from the fluidized material, and also the carbon black washed out are injected into the regenerator fluidized layer; air, steam or nitrogen, for example, may be used as the injection medium.
  • the smoke gas leaving the regenerator is substantially freed from solid particles in a cyclone.
  • the dust formed (grain size below about 0.05 mm.) may be discharged and separated in an external cyclone.
  • the fluidized material is replenished by adding appropriate amounts of coarser material.
  • the solid particles which have been heated up return to the reactor through an analogous arrangement of a down pipe and a rising pipe. It is preferred to use steam as the porportioning and conveying gas in order to obtain a concentrated cracked gas. In this case also, the proportioning gas provides a separation of the various media on the reactor and regenerator sides.
  • the excess of cracked oil is withdrawn at a tray in the column; it is a standard fuel oil.
  • Reactor '1 and regenerator 2 form with down pipes 3 and 5 and rising pipes 4 and 6 a flow system in which steam which is supplied to a distributor grate 7 through a pipe 8.
  • a conical grate instead of a conical grate as shown, other grate constructions may be used. It is also possible to introduce the fluidizing medium through jets without a grate.
  • the oil to be cracked, atomized with steam is introduced through a pipe 9 into the reactor fluidized layer which is at a temperature of 650 to 850 C.
  • the cracked gas and vapor pass through a pipe 10 into a cyclone 11 whose drain 12 returns to the fluidized layer.
  • the water is drained off through a drain valve 23 while the gasoline fraction is in part returned through a reservoir 22 to the column 19, a temperature between 100 and 130 C. being maintained at the top of the column.
  • the level of the separating layer in the vessel 21 can, for example, be maintained by a regulator which actuates drain valve 23.
  • the bottoms of the column return through a pipe 24 and the receiver 17 into the circulating quenching oil.
  • a middle oil which serves as rinsing oil for the quenching oil circulatory pump 26.
  • the excess of cracked oil less the amount required in the regenerator is withdrawn as a standard fuel oil from column 19 through a pipe 28 which usually lies above pipe 25 where the rinsing oil is withdrawn.
  • the cooled solid particles are withdrawn from the reactor 1 through the down pipe 3 in a compact mass. They are proportioned at the lower end of down pipe 3 by means of a gas stream 29 into the rising pipe 4 and conveyed from a pipe 30 by means of air, preferably preheated air, or an inert gas into the regenerator 2.
  • the fluidized material in the generator is preferably fluidized with preheated air through pipe 31.
  • a partial stream is introduced through pipe 32 into the regenerator. It may be atomized, for example, with air, inert gas or steam. Introduction is preferably combined with the proportioning step. A temperature of 700 to 1,000 C. is maintained. To insure combustion without carbon black formation it is advantageous to use an excess of oxygen of 0.3 to 3% by volume in the smoke gas.
  • the latter leaves the regenerator through an inner cyclone 33 and an outer cyclone 34.
  • the dust formed in the system (grain sizes below about 0.05 to 0.1 mm. in diameter) can be removed and separated in a discharge 35.
  • the heat of the CO-free gas may be utilized in a heat exchanger (not shown) in conventional manner.
  • the solid particles which have been heated up are withdrawn from the regenerator through pipe 5, supplied to the rising pipe 6, preferably with steam from a pipe 36, and are conveyed into the reactor with steam from a pipe 37.
  • 98 kilograms of a preheated crude oil with a paraflinic base are injected together with kilograms of superheated steam into reactor 1, a temperature of 740 C. being set up.
  • the layer in the reactor is fluidized with about 70 kilograms per hour of superheated steam which is introduced partly below the grate through pipe 8 and partly as conveyer steam through pipe 37.
  • the vapors leaving the reactor are quenched to below 300 C. in vessel 13 and freed in column 19 from the residual high boiling fraction.
  • the cooled heat carrier particles are heated up to about 900 C. in regenerator 2 by burning the cracked coke deposited thereon and also by injecting about 16 kilograms per hour of the high boiling oil occurring in vessel 13.
  • the layer in the regenerator is fluidized with such an amount of preheated air that the smoke gas contains about 2% by volume of oxygen.
  • the cracked gas contains hydrocarbons up to and including C of which 39.0% by volume is ethylene and 12.3% by volume propylene.
  • the yield of the said olefines, with reference to a metric ton of crude oil, is 281 kilograms of ethylene and 133 kilograms of propylene.
  • a process for cracking hydrocarbons which contain high boiling constituents to produce gaseous olefines which comprises: injecting said hydrocarbons into a reactor containing fluidized solid particles, said reactor being maintained at a temperature of from about 680 to about 850 C., said fluidized solid particles being inert heat carriers having a grain size of between about 0.05 and about 4.0 mm., wherein at least 10% by weight of said particles have a grain size greater than about 1 mm., said particles being circulated between said reactor and a fluidized layer regenerator wherein said particles are reheated, the particles being withdrawn from the reactor and regenerator through down pipes in which they move as a compact mass, said particles being returned to said reactor and said regenerator through rising pipes in the form of a dilute suspension which is formed by the introduction of the gas into the compact mass; passing the cracked gas and vapor leaving the fluidized reactor into a cyclone wherein the bulk of the entrained solid particles are separated from said gas and said vapor, from 5 to 50 grams of solid per normal cubic meter
  • a process for cracking hydrocarbon selected from the group consisting of crude oil and crude oil distillates having a final boiling point between 200 C. and 400 C. to produce gaseous olefines which comprises: injecting said hydrocarbons into a reactor containing fluidized solid particles, said reactor being maintained at a temperature of from about 680 C.
  • said fluidized solid particles being inert heat carriers having a grain size of from about 0.1 and about 3.0 mm., wherein at least 20% by weight of said particles have a grain size greater than about 1 mm.
  • said particles being circulated between said reactor and a fluidized layer regenerator wherein said particles are heated, said particles being Withdrawn from the reactor and regenerator through down pipes in which they move as a compact mass, said particles being returned to said reactor and said regenerator through rising pipes in the form of a dilute suspension which is created by the introduction of a gas into the compact mass; passing the cracked gas and vapor leaving the fluidized reactor into a cyclone wherein the bulk of the entrained solid particles are separated from said gas and said vapor, from 5 to 50 grams of solid per normal cubic meter of cracked gas being left in the cracked gas leaving said cyclone; passing the gas and vapor to a quenching zone wherein said products are quenched to a temperature below about 400 C.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US95674A 1960-03-16 1961-03-14 Cracking of hydrocarbons to gaseous olefines Expired - Lifetime US3238271A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DEB57080A DE1222038B (de) 1960-03-16 1960-03-16 Verfahren zur Spaltung von Kohlenwasserstoffen zu gasfoermigen Olefinen

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BE (1) BE601348A (en)van)
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FR (1) FR1316469A (en)van)
GB (1) GB926844A (en)van)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3624176A (en) * 1968-06-25 1971-11-30 Azote & Prod Chim Catalytic process for producing gas mixtures having high ethylene contents
US5043058A (en) * 1990-03-26 1991-08-27 Amoco Corporation Quenching downstream of an external vapor catalyst separator
WO1991014752A1 (en) * 1990-03-26 1991-10-03 Amoco Corporation Catalytic cracking with quenching
US5073249A (en) * 1989-11-21 1991-12-17 Mobil Oil Corporation Heavy oil catalytic cracking process and apparatus
US5234578A (en) * 1988-08-26 1993-08-10 Uop Fluidized catalytic cracking process utilizing a high temperature reactor
US5324484A (en) * 1987-08-11 1994-06-28 Stone & Webster Engineering Corp. Particulate solids cracking apparatus and process
US6482312B1 (en) 1987-08-11 2002-11-19 Stone & Webster Process Technology, Inc. Particulate solids cracking apparatus and process
US20040069684A1 (en) * 2002-10-10 2004-04-15 Kellogg Brown & Root, Inc. Catalyst recovery from light olefin FCC effluent
WO2008104250A1 (en) * 2007-02-27 2008-09-04 Outotec Oyj Method and apparatus for controlling a stream of solids
US20180171242A1 (en) * 2016-12-15 2018-06-21 Exxonmobil Research And Engineering Company Efficient process for upgrading paraffins to gasoline
EP4135877A4 (en) * 2020-04-17 2024-05-22 Uop Llc METHOD AND APPARATUS FOR RECOVERING CATALYST FROM A PRODUCT STREAM

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS499104B1 (en)van) * 1969-12-29 1974-03-01

Citations (6)

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US2684931A (en) * 1949-08-20 1954-07-27 Union Oil Co Fluidized solids process for contacting solids and vapors with the conveyance of the solids in dense phase suspension
US2696461A (en) * 1950-11-30 1954-12-07 Kellogg M W Co Regeneration of hydrocarbon conversion catalysts
US2700642A (en) * 1951-05-08 1955-01-25 Standard Oil Dev Co Coking of heavy hydrocarbonaceous residues
US2867676A (en) * 1956-01-04 1959-01-06 Sinclair Refining Co Process for conducting high temperature conversions using fluidized solids as heat exchange media
US2870087A (en) * 1951-09-24 1959-01-20 Phillips Petroleum Co Cracking process
US2884368A (en) * 1956-02-17 1959-04-28 United Eng & Constructors Inc Process for the pyrolysis and gasification of hydrocarbonaceous materials

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US2400176A (en) * 1941-09-20 1946-05-14 Standard Oil Co Catalytic conversion
US2445351A (en) * 1941-12-27 1948-07-20 Standard Oil Dev Co Process of adding heat in the regeneration of catalyst for the conversion of hydrocarbons
US2458862A (en) * 1943-07-24 1949-01-11 Standard Oil Dev Co Preventing secondary reactions in catalytic processes
US2471104A (en) * 1944-11-10 1949-05-24 Standard Oil Dev Co Production of unsaturated hydrocarbons and hydrogen
US2608526A (en) * 1946-12-14 1952-08-26 Standard Oil Dev Co Coking of carbonaceous fuels
AT198863B (de) * 1950-07-28 1958-07-25 Houdry Process Corp Verfahren und Vorrichtung zur Kreislaufführung freifließender, körniger, fester Stoffe
US2763601A (en) * 1953-05-27 1956-09-18 Exxon Research Engineering Co Conversion of hydrocarbons
DE1083805B (de) 1958-06-07 1960-06-23 Basf Ag Verfahren zur Spaltung von hochsiedenden Kohlenwasserstoffoelen
DE1107216B (de) 1959-12-29 1961-05-25 Basf Ag Verfahren zur Spaltung von hochsiedenden Kohlenwasserstoffoelen

Patent Citations (6)

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Publication number Priority date Publication date Assignee Title
US2684931A (en) * 1949-08-20 1954-07-27 Union Oil Co Fluidized solids process for contacting solids and vapors with the conveyance of the solids in dense phase suspension
US2696461A (en) * 1950-11-30 1954-12-07 Kellogg M W Co Regeneration of hydrocarbon conversion catalysts
US2700642A (en) * 1951-05-08 1955-01-25 Standard Oil Dev Co Coking of heavy hydrocarbonaceous residues
US2870087A (en) * 1951-09-24 1959-01-20 Phillips Petroleum Co Cracking process
US2867676A (en) * 1956-01-04 1959-01-06 Sinclair Refining Co Process for conducting high temperature conversions using fluidized solids as heat exchange media
US2884368A (en) * 1956-02-17 1959-04-28 United Eng & Constructors Inc Process for the pyrolysis and gasification of hydrocarbonaceous materials

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3624176A (en) * 1968-06-25 1971-11-30 Azote & Prod Chim Catalytic process for producing gas mixtures having high ethylene contents
US5324484A (en) * 1987-08-11 1994-06-28 Stone & Webster Engineering Corp. Particulate solids cracking apparatus and process
US5340545A (en) * 1987-08-11 1994-08-23 Stone & Webster Engineering Corp. Particulate solids cracking apparatus
US6482312B1 (en) 1987-08-11 2002-11-19 Stone & Webster Process Technology, Inc. Particulate solids cracking apparatus and process
US5234578A (en) * 1988-08-26 1993-08-10 Uop Fluidized catalytic cracking process utilizing a high temperature reactor
US5073249A (en) * 1989-11-21 1991-12-17 Mobil Oil Corporation Heavy oil catalytic cracking process and apparatus
US5043058A (en) * 1990-03-26 1991-08-27 Amoco Corporation Quenching downstream of an external vapor catalyst separator
WO1991014752A1 (en) * 1990-03-26 1991-10-03 Amoco Corporation Catalytic cracking with quenching
US7011740B2 (en) 2002-10-10 2006-03-14 Kellogg Brown & Root, Inc. Catalyst recovery from light olefin FCC effluent
EP1413621A1 (en) * 2002-10-10 2004-04-28 Kellogg Brown & Root, Inc. Catalyst recovery from light olefin FCC effluent
US20040069684A1 (en) * 2002-10-10 2004-04-15 Kellogg Brown & Root, Inc. Catalyst recovery from light olefin FCC effluent
EP2161322A1 (en) * 2002-10-10 2010-03-10 Kellogg Brown & Root, Inc. Catalyst recovery from light olefin FCC effluent
WO2008104250A1 (en) * 2007-02-27 2008-09-04 Outotec Oyj Method and apparatus for controlling a stream of solids
US20100118641A1 (en) * 2007-02-27 2010-05-13 Outotec Oyj Method and apparatus for controlling a stream of solids
EA015768B1 (ru) * 2007-02-27 2011-12-30 Оутотек Ойй Способ и устройство для регулирования потока твёрдых материалов
AU2008221091B2 (en) * 2007-02-27 2012-07-05 Metso Metals Oy Method and apparatus for controlling a stream of solids
US8602693B2 (en) 2007-02-27 2013-12-10 Outotec Oyj Method and apparatus for controlling a stream of solids
DE102007009758B4 (de) 2007-02-27 2024-11-28 Metso Outotec Finland Oy Verfahren und Vorrichtung zur Regelung eines Feststoffstromes
US20180171242A1 (en) * 2016-12-15 2018-06-21 Exxonmobil Research And Engineering Company Efficient process for upgrading paraffins to gasoline
EP4135877A4 (en) * 2020-04-17 2024-05-22 Uop Llc METHOD AND APPARATUS FOR RECOVERING CATALYST FROM A PRODUCT STREAM

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FR1316469A (fr) 1963-02-01
DE1222038B (de) 1966-08-04
GB926844A (en) 1963-05-22
BE601348A (en)van)

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