US3206393A - Fluid catalytic cracking of hydrocarbons - Google Patents

Fluid catalytic cracking of hydrocarbons Download PDF

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Publication number
US3206393A
US3206393A US413567A US41356764A US3206393A US 3206393 A US3206393 A US 3206393A US 413567 A US413567 A US 413567A US 41356764 A US41356764 A US 41356764A US 3206393 A US3206393 A US 3206393A
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stream
temperature
catalyst particles
catalyst
regeneration zone
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US413567A
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Jack B Pohlenz
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Universal Oil Products Co
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Universal Oil Products Co
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Priority to US413567A priority Critical patent/US3206393A/en
Priority to AT827065A priority patent/AT268484B/de
Priority to CH1261765A priority patent/CH474565A/de
Priority to GB38675/65A priority patent/GB1111588A/en
Priority to NL6511901A priority patent/NL6511901A/xx
Priority to ES0317389A priority patent/ES317389A1/es
Application granted granted Critical
Publication of US3206393A publication Critical patent/US3206393A/en
Priority to DEU12147A priority patent/DE1273101B/de
Priority to PL1965111673A priority patent/PL79138B1/pl
Priority to BE672625A priority patent/BE672625A/xx
Priority to CS6997A priority patent/CS176102B2/cs
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/187—Controlling or regulating

Definitions

  • the present invention is directed to an improved manner of operating a fluid catalytic cracking unit and more specifically to obtaining improved product yields from a hydrocarbon charge stream by operating to increase the heavy oil content in the recycle portion thereof, as an independent step or in combination with fresh feed preheat, whereby to provide an increased dilerential temperature between the reaction and regeneration zones and high temperature levels within the regeneration zone.
  • a conventional fluid catalytic cracking unit makes use of a reactor, stripper, spent catalyst slide valve, regenerator, regenerator standpipe, regenerated catalyst slide valve and a riser line leading back into the reactor, with the catalyst owing through the various sections of the unit, in the order named.
  • a large fractionator or main column is also utilized to receive the overhead cracked vaporous product stream from the reactor.
  • Such fractionator provides gasoline and other desired side-cut product streams therefrom, as well as recycle oil streams which are charged back to the reaction zone.
  • k1965 lCe carbon feed stream and recycle referred to as combined feed, is vaporized upon contacting heated regenerated catalyst particles at the base of the riser line and there is a lluidized lcontacting and lifting of the catalyst to within the reactor.
  • the resulting reactor product vapors, along with a minute quantity of entrained catalyst, are introduced into the main column where, of course, the products are fractionated into the various overhead and sidecut streams in accordance with their volatility.
  • the reactor temperature controls the regenerator slide valve to provide, in turn, variations in catalyst flow from the regenerator to the reactor.
  • the spent catalyst valve, regulating catalyst flow from the reactor to regenerator is operated by catalyst level control means A in the reactor.
  • the important dependent control variables in a unit may be considered to be: catalyst cir-culation rate and hence catalyst to oil ratio and regenerator temperature.
  • the catalyst to oil ratio which is the relation of the rate of catalyst to the reactor to the rate of oil entering the reactor, is tied to catalyst circulation rate and does affect the severity of the cracking.
  • the severity is also affected by space velocity since, for example, a decrease in space velocity means a lesser quantity of oil is contacting a given quantity of catalyst, per hour, such that there is an increase in conversion following the longer con tact time with the catalyst.
  • catalyst circulation rate, catalyst to oil ratio and space velocity there is an interrelation between catalyst circulation rate, catalyst to oil ratio and space velocity.
  • the present invention provides in connection with a continuous process for cracking a hydrocarbon charge stream comprising fresh feed and recycle oil in the presence of subdivided catalyst particles, wherein the hydrocarbon stream is subjected to a fluidized contacting of the particles in a reaction zone, conversion yproducts are separated from the contacted particles, separated catalyst particles containing a coke deposit are subject to'a uidized contacting of an oxygen containing stream in a separate regeneration zone, combustion gas products are separated from regenerated catalyst particles and such regenerated catalyst particles with a reduced coke content are returned to the reaction zone for contact gwith the hydrocarbon charge stream, the improved method of effecting improved product yields from the hydrocarbon charge stream by operating to provide high temperature levels in the regeneration zone, which comprises,
  • the present invention provides in connection with a continuous process for cracking a hydrocarbon charge stream in the presence of subdivided catalyst particles, wherein the hydrocarbon stream is subjected to a fluidized contacting of the particles in a reaction zone, conversion products are separated from the contacted particles, separated catalyst particles containing a coke deposit are subjected yto uidized contacting of an oxygen containing stream in a separate regeneration zone, combustion gas products are separated from regenerated catalyst particles and such regenerated catalyst particles with a reduced coke content are returned to vthe reaction zone for contact with the hydrocarbon charge stream, the improved method of effecting improved product yields from the hydrocarbon stream by operating to provide a high temperature level in the regeneration zone,l which, comprises, decreasing the weight hourly space velocity in the reaction zone -and increasing the reaction Zone temperature to effect ya greater conversion of said hydrocarbon charge stream and providing a coke deposition on the catalyst particles sufiicient to provide a temperature above 1150 F.
  • Fresh hydrocarbon feed passes through line 1 and control valve 2 to a pump 3 that in turn discharges into line 4 connecting with a feed preheater 5.
  • the latter provides a predetermined or controlled variable preheating to the feed stream and passes it to the lower end of riser line 6 where heated catalyst particles combine therewith from standpipe 7, having control valve 8, such that a resulting vapor-catalyst mixture rises in an ascending. fluidized stream to the lower end of reactor 9.
  • the reactor 9 there may be further uidized contacting between the vaporous feed stream and the catalyst particles within a relatively dense fluidized bed 10 within the lower portion of the chamber, although generally a major portion of the necessary cracking and contact with the catalyst particles takes place in the riser line 6.
  • Catalyst in an oil slurry may be combined with the fresh feed stream in the riser line 6 from line 11 having control valve 12, while in addition, light and heavy recycle oils may be combined therewith by way of line 13 having control valve 14.
  • the combined feed ratio will vary in accordance with the amount of recycle oils combined with the fresh feed stream to be introduced into the reaction zone.
  • the catalyst particles are separated from the vaporous cracked reaction products by centrifugal separating means 15 and then transferred overhead by line 16 to the lower end of the fractionator or main column 17.
  • Separated catalyst particles from the light phase zone in the top of the reactor 9 are returned to the dense phase bed 10 by a suitable dip-leg 13 and resulting catalyst particles with a coke deposition and occluded hydrocarbons settle from the lower portion of reactor 9 into a stripping section 19 such that they may pass concurrently to a stripping gas stream introduced through line 20 having valve 21.
  • Steam, nitrogen or other substantially inert gaseous stripping medium may be utilized in the stripping section to effect the removal of absorbed and occluded hydrocarbon vaporous components.
  • Resulting stripped and coked catalyst particles move from the lower portion of stripping section 19 into the standpipe 22, having control valve 23, such that they may be transferred at a controlled rate to the regenerator 24.
  • the carbonized catalyst particles are subjected to oxidation and carbon removal in the presence of air being introduced by way of distribution grid 25.
  • the oxidizing air stream enters the regenerator by way of line 26, valve 27 and blower 2S, which in turn connects by way of line 29 to air heater 30.
  • the latter is indicated as connecting directly with the lower end of the regenerator 24 and the pipe grid distributor 25.
  • the air heater 30 is utilized in a manner only to heat the air during the initial start-up procedure.
  • a fluidized dense phase bed 33 provides for hindered settling contact between the coked catalyst particles and the oxidizing air stream while, in the upper portion of the charnber, a light phase zone permits the separation of catalyst particles from the flue gas stream being discharged by way of line 34 and valve 35.
  • Suitable centrifugal separating means 36 provides for removing entrained catalyst particles from the combustion product stream and returns thern by way of dip-leg 37 to the lower dense phase bed 33.
  • a suitable silencing means 38 connecting with the line 35, serves to reduce the noise level of the combustion gas stream passing to the outlet stack 39.
  • the cracked product vapor stream is fractionated to provide a desired overhead gasoline vapor stream passing by way of line 40 and valve 41 to suitable gas concentration equipment, not shown in the lpresent drawing.
  • various side-cut and recycle streams may be taken from the side of the fractionator 17 in accordance with desired molecular weight products.
  • a light recycle oil stream is indicated as being taken from column 16 by way of line 42 and side-cut accumulator 43.
  • An overhead vapor return line 44 returns uncondensed vapors from accumulator 43 to the main column 17 while a condensed light oil fraction is taken from the lower end of the accumulator 43 by Way of line 45, pump 46 and line 47 having valve 48.
  • a heavier recycle oil stream may be taken from the main column by way of line 49 and side-cut accumulator 50.
  • An uncondensed vapor stream may be returned to the main column by way of line 51 while a condensed heavy oil fraction passes from the lower end of accumulator 56 by line 52, pump 53 and line 54 having valve 55.
  • all cooling circuits and cooling lines to the column are not shown.
  • suitable lines not indicated in the present drawing, may be utilized to transfer the light and heavy recycle oil streams from lines 47 and 54 to the recycle inlet line 13 which in turn connects with catalyst riser line 6, such that recycle oil may be combined with fresh hydrocarbon feed stream from line 1 to provide a desired combined feed ratio to the reactor 9.
  • Light reflux to the top of the main column 17 is shown as being introduced by way of line 82 and control valve 83.
  • a bottoms slurry oil, containing catalyst particles which were entrained with the vapor product stream in line 16, is carried by way of the lower outlet line 56, pump 57 and line 58 to a suitable catalyst settling chamber 59.
  • the settler 59 serves to provide a substantially particle free clarified oil stream overhead by way of line 60 and valve 61, while at the same time effecting the return of the catalyst containing slurry stream through control valve 12 to transfer line 11 such that catalyst particles may be returned to the uidized bed by way of riser line 6.
  • a line 62, with control valve 63 is utilized to pass a portion of the bottoms stream from the main column 17 through a heat exchanger 64 such that heated oil may be returned by way of line 65 to the lower end of the main column 17 and provide a heat supply to such column.
  • control instrumentation means are associated with the reaction and regeneration zones to maintain appropriate dense phase bed levels in such zones and a catalyst circulation rate between such zones.
  • a level controller LC with level indicating taps 66 and 67, is connected with the side wall of the reactor.
  • a control line 68 from controller LC connects with the slide valve 23 in the contacted catalyst standpipe 2 and provides means for maintaining a desired dense phase bed 10 level and quantity of catalyst in the lower portion of the reactor 9.
  • the slide valve control means such as used in connection with the slide valve 23, are pneumatic in opera- ⁇ tion such that the level control means LC may be of any conventional type suitable to regulate the pneumatic mo- 'tor control means of the valve, although electrical control and motor means may be used.
  • a temperature indicating means 69 connects through control line 70 to a temperature controller TC and control line 71 which in turn connects with an air piston or other motor means .providing for the regulation of the slide valve 8 in the regenerated catalyst standpipe 7.
  • a variable quantity of hot regenerated catalyst may be withdrawn from standpipe 7 to pass into riser line 6 and enter the reactor chamber 9 in accordance with variations in temperature ,in the latter zone, as provided for by the temperature sensitive means 69 and controller TC.
  • a pressure sensitive means 72 is also positioned in the upper portion of the reactor 9 while a separate pressure indicating means 73 is positioned in the upper portion of the regenerator 24.
  • iSuch indicating means are connective, through the respective lines 74 and 75, to a differential pressure regulator lDPR in order to provide means for maintaining a deisired differential pressure between the two separate contacting zones.
  • the differential pressure regulator DPR connects through control line 76 with the control valve 35V so as to regulate the ilue gas flow through line 34 and 'in turn vary the internal pressure within the upper portion of the regenerator 24, whereby a predetermined pressure difference .may be maintained between the reactor and the regenerator.
  • the pressure differential between the two Zones is of the order of about 6 p.s.i. and is necessary to permit the maintenance of suitable pressure differentials across the slide valves in the two standf pipe linesand a continuous circulation of catalyst particles between two separate zones.
  • Pressures in a fluidized unit are, of course, relatively low, being generally below about 25 to 30 p.s.i.
  • the pressure variation in the reactor may be an operating control variable, but because of gas compressor limitations or certain structural and mechanical aspects, it is preferable to utilize low pressures which are merely suiicient to insure adequate differentials and proper flow between various portions of the unit.
  • An improved control means integrated in connection with high Vtemperature operations and indicated in the present diagrammatic embodiment is the use of differential temperature control means between the dense phase and light phase zones of regenerator 24 so as to regulate the quantity of air being introduced into the regeneration zone.
  • Temperature indicating means 77 and 78, within the upper and lower portions of the regenerator 24, connect through the respective transmission lines 79 and Si) to a differential temperature controller DTC, which in turn connects through control line 81 with the valve 32 lin the air vent line 31.
  • valve 52 is adjusted to bypass a greater portion of the air passing through line 29 and effect the reduction of air being introduced by way of distributing grid 25 into the lower portion of the regenerator.
  • the hydrocarbon charge is a typical feed for a fluidized unit, being a blend of atmospheric, vacuum and coking unit gas oilswith a API gravity of about 31.0; a sulfur content of about 0.4%; a molecular weight of 320; a UOP characterization factor, or K factor, of about 12.0; and a boiling range of from about 475 F. to about 1000 F.
  • the catalyst .circulation rates shown are based on a raw oil or fresh feed charge of 20,000 barrels per day. In each case, except for Example VII, there is 5 volume percent, based on fresh feed, of slurry in the feed, with the balance of the recycle being heavy cycle oil.
  • the catalyst activity in all cases is 32, based upon the UOP determination of weight activity such as described in Industrial Engineering Chemistry (1952), volume 44, pages 2857 to 2863 and/or Petroleum Rener, volume 31, No. 9 (September 1952), pages 274-276.
  • the fresh feed or raw oil temperature to the unit is at 400 F.; the combined feed ratio is 1.5; the weight hourly space velocity (WHSV) is set at 6; the temperature ranges for the reactor are 900 F. in the dense phase and 885 F. in the light phase, while the regenerator dense phase is 1120 F. and the light phase 1135 F.
  • the coke-make is 7.5 weight percent and catalyst circulation rate of 3.45
  • EXAMPLE II In another operation, the processing conditions provided are similar to those of Example I, except that there is feed preheat providing an increased raw oil temperature of the order of 600 F. The increase in the feed temperature will reduce catalyst circulation rate which in turn will reduce conversion. Thus, in order to maintain or increase conversion there is provided an increased dense phase reactor temperature. In this case, the reactor temperature level is raised to 945 F. and the resulting conversion is 72 volume percent, with debutanized gasoline production being 52.5 volume percent. The dense phase regenerator temperature is 1175 F. and the coke-make is 6.8 Weight percent. The catalyst circulation rate is 3.0)(106 pounds per hour. Other product yield quantities are shown in Table A.
  • EXAMPLE III In another operation, the processing conditions are modified from those of the rst example to provide for an increase in the quantity of heavy recycle oil such that the combined feed ratio to the reactor is 2.0 In this instance thel reactor temperature level is increased to 913 F. to in turn provide for a higher conversion of 75 volume percent.
  • the regenerator temperature increases to 1165 F. with a resulting temperature differential between the reactor and regenerator zones of 252 F.
  • the increased heavy oil content in the combined feed in the absence of other changes will, of course, result in a greater coke deposition on the catalyst particles and an overall increase in coke-make in the operation, with such coke production being 9.5 Weight percent.
  • the catalyst cir- 'culation rate increases to 3.82 106 pounds per hour.
  • EXAMPLE IV In still another fluidized operation, the processing conditions are modified to include an increase in feed preheat such that the raw oil temperature is 600 F. (as in Example II) and, in addition, the combined feed ratio is increased to 2.0, by providing a greater quantity of heavy cycle oil to the reactor, in a manner similar to the operation of Example III.
  • the reactor temperature level is increased to 936 F. while the regenerator temperature increases to 1200 F., with a resulting differential of some 264 F.
  • An overall conversion of 75 volume percent is attained, while debutanized gasoline production increases to 54.5 volume percent.
  • Coke yield is slightly greater, at 8.6 weight percent, than that of Example I, and catalyst circulation rate is slightly lower at 3.30 106 pounds per hour. Additional yield data are again set forth in the accompanying Table A.
  • EXAMPLE V In this modified fluidized catalytic cracking operation, there is embodied a change in the reactor temperature level to increase conversion while, of course, at the same time increasing the regenerator temperature to a substantially higher level.
  • a charge stream as set forth under the conditions of Example I, being introduced to the unit at CFR of 400, a WHSV of 6.0 and a raw oil temperature of 400 F.
  • there may be set an increased level of temperature in the reactor to 950 F., and a resulting higher regenerator temperature to 1180 F.
  • the resulting conversion is 78 volume percent with the debutanized gasoline yield being 54.5 volume percent.
  • the coke make is 8.2 weight percent and the catalyst circulation rate will be slightly higher at 3.61)( 106 pounds per hour following the reactor temperature adjustment to the higher level.
  • Other product yield data are shown in the Table A.
  • EXAMPLE VI In this modified operation, the space velocity is reduced, as compared with the conditions of Example I, to show how this operational variable causes an increase in the temperature spread between the reaction and regeneration zones and an increase in conversion with little or no increase in coke-make.
  • Raw oil temperature is held to 400 F. and the combined feed ratio maintained at 1.5.
  • debutanized gasoline yield increases from 47.5 to 51.0 volume percent and that heavy cycle oil production decreases substantially by dropping from 10.0 to 5.0 volume percent.
  • EXAMPLE VII In still another operation, there may be provided an increase in the heavy oil content of the raw oil charge to in turn illustrate the use of the higher regenerator temperature operation in effecting the conversion of heavy stocks to gasoline. Specifically, in this case, there is provided an 8 volume percent quantity of slurry as compared to the 5 volume percent slurry in Example I. The conibined feed ratio remains at 1.5, raw oil temperature at 400 F., and WHSV at 6.0. Reactor temperature is raised to 910 F. to increase conversion slightly and the regenerator temperature raises to l F. with cokemake being 7.6 weight percent and catalyst circulation rate going to a decreased rate of 2.75 X106 pounds per hour.
  • the improved method of effecting improved product yields from the hydrocarbon charge stream by operating to provide a high temperature level in the regeneration zone which comprises, increasing the combined feed ratio with an increase in the heavy recycle 15 oil content of the charge stream being introduced to the reaction zone, effecting both a greater conversion in said reaction zone and an increased coke deposition level on the catalyst particles sufficient to provide a temperature above 1150 F.
  • WHSV Weight hourly space velocity
  • Catalyst activity (UOP) 32 32 32 32 32 32 32 32 32 32 Catalyst cir. rate, lb./hr. 10fi 3. 45 3.00 3 82 3 30 3. 61 2 75 2 75 Conversion, volume percent 65 72 75 75 78 72 67 Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Wt. Vol. Vol. Per- Per- Per- Per- Per- Per- Per- Per- Per- Per- Per- Per- Percent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent cent
  • the improved method of effecting improved product yields from the hydrocarbon charge stream by operating to provide a high temperature level in the regeneration zone, which comprises, preheating the fresh feed portion of the hydrocarbon stream, concom-it'antly therewith increasing the combined feed ratio with an increase in heavy recycle oil, varying the catalyst circulation rate to effect a coke deposition level on the catalyst particles :sufficient to provide a greater temperature spread between the reaction and regeneration zones with a temperature above 1150 F, in the regeneration zone when oxidizing the coke deposit on the catalyst particles in the presence of a controlled oxygen containing stream introduced to such regeneration zone, and regulating the introduction of the oxygen containing stream to the regeneration zone directly responsive to a predetermined temperature differential between the gas outlet section and the catalyst
  • improved method of effecting improved product yields from the hydrocarbon charge stream by operating to provide a high temperature level in the regeneration zone which comprises, increasing the reaction zone temperature and effecting a greater conversion of said ch-arge stream in said reaction zone, varying the catalyst circulation rate to effect a coke deposition on the catalyst sufficient to provide a temperature above 1150 F. in the regeneration zone when oxidizing the coke deposition on the catalyst particles in the presence of a controlled oxygen containing stream introduced to such regeneration zone, and regulating the introduction of the oxygen containing stream to the regeneration zone directly responsive to a predetermined temperature differential between the gas outlet section and the catalyst contacting section of the regeneration zone to minimize excess oxygen therein and to control afterburning in the upper portion of the regeneration zone.

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  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US413567A 1964-11-24 1964-11-24 Fluid catalytic cracking of hydrocarbons Expired - Lifetime US3206393A (en)

Priority Applications (10)

Application Number Priority Date Filing Date Title
US413567A US3206393A (en) 1964-11-24 1964-11-24 Fluid catalytic cracking of hydrocarbons
AT827065A AT268484B (de) 1964-11-24 1965-09-09 Verfahren zur kontinuierlichen Herstellung von Benzinkohlenwasserstoffen
GB38675/65A GB1111588A (en) 1964-11-24 1965-09-10 Continuous process for producing gasoline hydrocarbons
CH1261765A CH474565A (de) 1964-11-24 1965-09-10 Kontinuierliches Verfahren zur Herstellung von Benzinkohlenwasserstoffen
NL6511901A NL6511901A (enrdf_load_stackoverflow) 1964-11-24 1965-09-13
ES0317389A ES317389A1 (es) 1964-11-24 1965-09-13 Un procedimiento continuo para la produccion de hidrocarburos de gasolina.
DEU12147A DE1273101B (de) 1964-11-24 1965-10-26 Kontinuierliches Verfahren zur Herstellung von Benzinkohlenwasserstoffen
PL1965111673A PL79138B1 (enrdf_load_stackoverflow) 1964-11-24 1965-11-18
BE672625A BE672625A (enrdf_load_stackoverflow) 1964-11-24 1965-11-22
CS6997A CS176102B2 (enrdf_load_stackoverflow) 1964-11-24 1965-11-23

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US413567A US3206393A (en) 1964-11-24 1964-11-24 Fluid catalytic cracking of hydrocarbons

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US3206393A true US3206393A (en) 1965-09-14

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US (1) US3206393A (enrdf_load_stackoverflow)
AT (1) AT268484B (enrdf_load_stackoverflow)
BE (1) BE672625A (enrdf_load_stackoverflow)
CH (1) CH474565A (enrdf_load_stackoverflow)
CS (1) CS176102B2 (enrdf_load_stackoverflow)
DE (1) DE1273101B (enrdf_load_stackoverflow)
ES (1) ES317389A1 (enrdf_load_stackoverflow)
GB (1) GB1111588A (enrdf_load_stackoverflow)
NL (1) NL6511901A (enrdf_load_stackoverflow)
PL (1) PL79138B1 (enrdf_load_stackoverflow)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3394075A (en) * 1966-07-05 1968-07-23 Mobil Oil Corp Utilization of superactive catalysts containing residual coke
US3410793A (en) * 1966-06-27 1968-11-12 Texaco Inc Method and apparatus for controlling the regeneration of contaminated solids in a fluidized system
US3513087A (en) * 1968-08-30 1970-05-19 Continental Oil Co Control system for fluid cat cracker
US3629097A (en) * 1970-01-06 1971-12-21 Continental Oil Co Control system for fluid catalytic cracking process
US3850582A (en) * 1969-12-10 1974-11-26 Exxon Research Engineering Co Apparatus for controlled addition of fluidized particles to a processing unit
US4006075A (en) * 1975-01-06 1977-02-01 Exxon Research And Engineering Company Method of regenerating a cracking catalyst with substantially complete combustion of carbon monoxide
US4180454A (en) * 1978-01-03 1979-12-25 Exxon Research & Engineering Co. Method for combusting carbon monoxide in a fluid catalytic cracking process
US4243518A (en) * 1979-07-18 1981-01-06 Exxon Research & Engineering Co. External method for reducing transverse oxygen gradients in FCCU regeneration
US4243517A (en) * 1979-07-18 1981-01-06 Exxon Research & Engineering Co. Internal method for reducing transverse oxygen gradients in FCCU regeneration
US4354957A (en) * 1980-10-03 1982-10-19 Phillips Petroleum Company Regenerator temperature control
WO1995024965A1 (en) * 1994-03-15 1995-09-21 Exxon Research And Engineering Company Combustion control in a fluid catalytic cracking regenerator
EP0933135A2 (en) 1998-01-30 1999-08-04 ExxonMobil Oil Corporation Atomizing nozzle and method of use thereof
US6142457A (en) * 1998-01-30 2000-11-07 Mobil Oil Corporation Atomizing feed nozzle
CN113213656A (zh) * 2021-03-23 2021-08-06 高和平 一种新型催化氧化法处理焦化废水的系统

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4708785A (en) * 1979-11-14 1987-11-24 Ashland Oil, Inc. Carbo-metallic oil conversion
US4376696A (en) * 1979-11-14 1983-03-15 Ashland Oil, Inc. Addition of MgCl2 to catalyst for cracking carbo-metallic feed oils
US4376038A (en) * 1979-11-14 1983-03-08 Ashland Oil, Inc. Use of naphtha as riser diluent in carbo-metallic oil conversion

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3161583A (en) * 1962-06-29 1964-12-15 Universal Oil Prod Co Fluid catalytic cracking of hydrocarbons

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3161583A (en) * 1962-06-29 1964-12-15 Universal Oil Prod Co Fluid catalytic cracking of hydrocarbons

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3410793A (en) * 1966-06-27 1968-11-12 Texaco Inc Method and apparatus for controlling the regeneration of contaminated solids in a fluidized system
US3394075A (en) * 1966-07-05 1968-07-23 Mobil Oil Corp Utilization of superactive catalysts containing residual coke
US3513087A (en) * 1968-08-30 1970-05-19 Continental Oil Co Control system for fluid cat cracker
US3850582A (en) * 1969-12-10 1974-11-26 Exxon Research Engineering Co Apparatus for controlled addition of fluidized particles to a processing unit
US3629097A (en) * 1970-01-06 1971-12-21 Continental Oil Co Control system for fluid catalytic cracking process
US4006075A (en) * 1975-01-06 1977-02-01 Exxon Research And Engineering Company Method of regenerating a cracking catalyst with substantially complete combustion of carbon monoxide
US4180454A (en) * 1978-01-03 1979-12-25 Exxon Research & Engineering Co. Method for combusting carbon monoxide in a fluid catalytic cracking process
US4243517A (en) * 1979-07-18 1981-01-06 Exxon Research & Engineering Co. Internal method for reducing transverse oxygen gradients in FCCU regeneration
US4243518A (en) * 1979-07-18 1981-01-06 Exxon Research & Engineering Co. External method for reducing transverse oxygen gradients in FCCU regeneration
US4354957A (en) * 1980-10-03 1982-10-19 Phillips Petroleum Company Regenerator temperature control
WO1995024965A1 (en) * 1994-03-15 1995-09-21 Exxon Research And Engineering Company Combustion control in a fluid catalytic cracking regenerator
US6114265A (en) * 1994-03-15 2000-09-05 Exxon Research And Engineering Company Combustion control in a fluid catalytic cracking regenerator
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CS176102B2 (enrdf_load_stackoverflow) 1977-06-30
AT268484B (de) 1969-02-10
NL6511901A (enrdf_load_stackoverflow) 1966-05-25
PL79138B1 (enrdf_load_stackoverflow) 1975-06-30
CH474565A (de) 1969-06-30
ES317389A1 (es) 1966-03-01
DE1273101B (de) 1968-07-18
BE672625A (enrdf_load_stackoverflow) 1966-03-16
GB1111588A (en) 1968-05-01

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