US3161583A - Fluid catalytic cracking of hydrocarbons - Google Patents

Fluid catalytic cracking of hydrocarbons Download PDF

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Publication number
US3161583A
US3161583A US206271A US20627162A US3161583A US 3161583 A US3161583 A US 3161583A US 206271 A US206271 A US 206271A US 20627162 A US20627162 A US 20627162A US 3161583 A US3161583 A US 3161583A
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Prior art keywords
temperature
catalyst
stream
coke
regeneration zone
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Expired - Lifetime
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US206271A
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English (en)
Inventor
Jack B Pohlenz
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Universal Oil Products Co
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Universal Oil Products Co
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Publication date
Priority to BE623712D priority Critical patent/BE623712A/xx
Priority to NL283942D priority patent/NL283942A/xx
Application filed by Universal Oil Products Co filed Critical Universal Oil Products Co
Priority to US206271A priority patent/US3161583A/en
Priority to DEU9279A priority patent/DE1202925B/de
Priority to GB36652/62A priority patent/GB971966A/en
Priority to AT855062A priority patent/AT238859B/de
Priority to ES282531A priority patent/ES282531A1/es
Priority to FR920991A priority patent/FR1359156A/fr
Priority to CH302063A priority patent/CH446283A/de
Priority to OA50632A priority patent/OA00545A/xx
Application granted granted Critical
Publication of US3161583A publication Critical patent/US3161583A/en
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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
    • B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • 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 method for operating a fluid catalytic cracking unit and more specifically to a method for effecting improved product yields from a hydrocarbon charge stream by operating to have an increased differential temperature between the reaction and regeneration zones and to maintain a high temperature level within the regeneration zone.
  • a further object of the invention is to provide that one or more independent operating variables are utilized in an integrated manner in the lluidized unit' to insure a coke deposition on the catalyst which will result in an increased temperature spread between the contact zones and a resulting regenerating zone temperature level at above about 1150 F.
  • a conventional fluid catalytic cracking unit makes use of a reactor, stripper, spent catalyst slide valve, regenerator, standpipe, regenerated catalyst slide valve, and a riser line leading back into the reactor, with the catalyst flowing 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.
  • the mixture of fresh hydrocarbon feed stream and recycle referred to as combined feed, is vaporized upon contacting heated regenerated catalyst particles at the base of the riser lineand effects the lifting of catalyst in the reactor.
  • the reactor products 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 side-cut streams in accord with their volatility.
  • 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 the regenerator, is operated by catalyst level control means in the reactor.
  • an increased catalyst to oil ratio produces an increased ow rate of catalyst through the reaction zone. Although less coke will be formed on each unit of catalyst in view of a shorter contact time in the reaction zone, the total coke rate increases.
  • an increased or decreased contact time 4between the oil and catalyst can be accomplished by a change in the space velocity (weight hourly space velocity being defined as the fresh feed rate in pounds per hour divided by the mass of catalyst within the reaction zone).
  • a decrease in weight hourly space velocity means that a lesser quantity of oil is contacting a given quantity of catalyst per hour, or for a given time, such that there is an increase in conversion by reason of a longer contact time with to the reaction zone.
  • the feed preheat may be varied directly by the amount of heat transferred to the feed stream by an oil heater or heat exchanger, or alternatively, by the quantity and temperature of the recycle stream which is combined with the fresh feed stream to provide the combined feed ratio.
  • Important independent operating Variables may thus be considered the combined feed ratio, the combined feed temperature, and space velocity, although, of course, other variables such as the reactor pressure and the catalyst activity or quality will have an effect upon conversion.
  • the catalyst circulation rate in the system may be readily varied, however, it is regulated responsive to a temperature controller in turn connecting with the reaction zone, thus the circulation rate and the catalyst oil ratio are dependent Variables in the operation of the commercial fluidized units.
  • the present invention provides that in a continuous process for cracking a hydrocarbon charge stream in the presence of subdivided catalyst particles wherein the hydrocarbon stream effects a tluidized contacting of the particles in a confined reaction zone, conversion products are separated from the contacted particles, separated catalyst particles containing a coke deposit effect iluidized contacting of lan oxygen containing stream in a separate confined 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 with hydrocarbon charge stream, the improved method of effecting optimum product yields from the hydrocarbon charge stream by operating at a high temperature level in the regeneration zone, which comprises, varying the reaction zone temperature and the contact time of the hydrocarbon stream with the catalyst therein responsive to the refractory characteristics of said hydrocarbon charge stream and effecting a coke deposition on the catalyst particles providing a temperature above about 1150 F.
  • the improved method of effecting superior product distribution from a hydrocarbon charge stream comprises, increasing the preheat temperature of the fresh feed stream to in turn provide an increased fresh feed temperature while reducing catalyst circulation rate, and to effect an increased temperature spread between the reaction and regeneration zones, such that the temperature level in the regeneration zone is above about 1150 F. and up to the metallurgical limits thereof as the regeneration zone oxidizes the coke on the catalyst particles in the presence of a controlled oxygen containing stream introduced into the regeneration zone.
  • the improved method of effecting improved hydrocarbon product yields when operating at a higher temperature level in the regenerator may comprise, for a given fresh feed charge rate and temperature level, varying the combined feed ratio of fresh feed to recycle oils to increase the heavy oil content thereof and simultaneously increasing the reactor temperature and a temperature differential between the reactor and regenerator and a coke deposition on the catalyst particles providing a resulting temperature above about 1150 F. upon oxidizing the coke on such particles in the presence of a controlled oxygen containing stream being introduced into the regeneration zone.
  • 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 preheatin g 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 column to the lower end of the reactor 9.
  • 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 1S and resulting catalyst particles with a coke deposition and occluded hyrocarbons 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 Z0 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 carbonizcd 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 28, which in turn connects by way of line 29 to air heater 30.
  • the blower 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 only to heat the air during the initial start-up procedure.
  • a iluidized 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 chamber, a light phase zone permits the separation of catalyst particles from the flue gas stream being discharged by way of line 34 and valve 3S.
  • Suitable centrifugal separating means 36 provides for removing entrained catalyst particles from the combustion product stream and returns them by way of dip-leg 37 to the lower dense phase bed 33.
  • a suitable silencing means 38, connecting with line 35, serves to reduce the noise level of the combustion gas stream passing to -the outlet stack 39.
  • light recycle oil stream is indicated as being takenfrom 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 57 having valve 48. ⁇
  • a heavier recycle oil stream may be taken from the main, column by way of line 49 and side-cut accumulatorv 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 50 by line 52, pump 53, and line S4 having valve 55.
  • Suitable lines may be, utilized to transfer the light and heavy recycle oil streams from lines'i47 and 54 to the-recycle inlet line 13 which in turn connects ⁇ with catalyst riser line 6, such that recycle oil may be ⁇ 16, may be transferred 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 claried oil stream overhead by way ⁇ of line 69 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 iluidized 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 65Ato 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,
  • a control line 68 from controller LC connects with the slide valve 23 in the contacted catalyst standpipe 22 and provides ⁇ means for maintaining a desired dense phase bed 19 level and quantity of catalyst in the lower portion of the reactor 9.
  • the slide valve control means such as used in connection with slide valve 23, are pneumatic in opera-Y Ation such that the level control means LC may be of any conventional type suitable to regulate the pneumatic motor 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 vregulation of the slide valve 8 in the regenerated catalyst standpipe 7.
  • la variable quantity of hot regenerated catalyst maybe withdrawn from standpipe 7 to pass into riser line 6 and enter the reactor chamber 9 in accordance with variations in ternvperature 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.
  • Such indicating means are connective, through the respective lines 74 and 75, to a ditterential pressure regulator DPR in order to provide means for maintaining a desired differential pressure between the two separate contacting zones.
  • the diferential pressure regulator DPR connects through control line 76 with the control valve 35 so as kto regulate the ilue gas ow through line 34 and in turn vary lthe 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 diierential between the two zones is ofthe 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 standpipe lines and a continuous circulation of catalyst Vparticles between two separate zones.
  • Pressures in a fluidized unit are, of course, relatively low, being generally below about 425 to 30 p.s.i. because of the large size of the vessels involved. Pressure variation in the reactor may be an operating control variable, but because of structural and mechanical aspects, it is preferable to utilize low pressures which are merely suliicient to insure yadequate differentials land proper flow between various portions of the uni-t.
  • An improvedcontrol means integrated in connection with high temperature operations and indicated inthe present diagrammatic embodiment is the use of a 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 7S within the upper and lower portions of the regenerator 24, connect through the respective transmission lines 79 and S0 to a differential temperature controller DTC, which in turn connects through control line 81 with the valve 32 in the air vent line 31.
  • valve 32 ⁇ is :adjusted to bypass a greater portion 'of the air passing through line 29 and effect the reduction of air being introeduced by way of distributing grid 25 into the lower portion of theregenerator.
  • Persons famili-ar with the operation of iluidized cracking units realize that uncontrolled after-burning can be a major problem inasmuch as theV high temperature resulting from the oxidation of fcarbon monoxide to carbon dioxide in a dilute phase and the cyclone separators at the outlet of the regenerator may -cause severe mechanical damage.
  • a stock which is of parat-line base having a high K value, or characterization factor, and is low in metals and Conradson carbon
  • B stock which has a low K value and is high in contaminants.
  • the reactor temperature being adjusted to provide a 65 volume percent conversion to gasoline, then the resulting steady-state operation providesy a reactor temperature of 890 F., regenerator temperature of 1100 F., and 7.7 weight percent of coke.
  • reactor temperature 915 F., a regenerator temperature of 1200 F., and coke amounting to 8.3 weight percent.
  • the 0.6 weight percent difference in coke-make is due to sensible heat in the reactor and/ or regenerator vapors.
  • the poorer charge stock B can be cracked in the conversion unit lat a high temperature conversion level to give a relatively high 65 percent conversion and there will be no problems in maintaining a steady-state operation as long as the 1200 F. temperature in the regenerator is below the limits of any metallurgical problems encoun- -tered in the regenerator section of the system.
  • the charge stock A could be treated in the system to provide substantially greater yields of gasoline or light materials by effecting changes in the operating variables so as to provide an increased regenerator temperature of the order of 1200 F. In other words, there may bean increase in the preheating of the feed stream, say to the order of 700 F. rather than the 400 F.
  • a fluid catalytic cracking unit can be varied in its operation in accordance with the refractory characteristics of the feed and, in fact, evaluate a particular charge stock in terms of reactor and regenerator temperature levels such that with the better charge stocks it is possible to consistently improve yields by operating to maintain a high temperature level in the regenerator as long as the high temperature level pre- -cludes metallurgical damage to the unit.
  • a series of performance tests were conducted in a uid catalytic cracking unit in a manner which illustrates the advantage of a high temperature level in the system and an increased temperature differential between the reactor and regenerator zones.
  • three different levels of feed preheat were used, with conversion being maintained constant by adjustments in the reactor temperature. Specifically, the raw oil introduction rate was maintained at 28,000 barrels per day, the combined feed ratio was held constant for each performance test at 2.30, and catalyst content in the reactor or weight hourly space velocity was held substantially constant.
  • a Test #2 the fresh feed was preheated to a temperature of 568 F. such that the combined feed temperature was 567 F. and a resulting reactor temperature and regenerator temperature were respectively 881 F. and 1168 F.
  • the catalyst circulation rate in this instance was 3.8 10fi while the coke-make rate was 8.6 weight percent.
  • the debutanized gasoline production was 50.1 Volume percent while other yields were in accordance with the quantities shown in Table I, under the column headed Test (2).
  • the weight fraction of C4 and lighter components remain substantially constant, but the C3 and C4 fractions decreased with a corresponding increase in the C2 and lighter fractions.
  • the isobutane content of the C4 paraftins remains substantially unchanged as well as the properties of the liquid product.
  • any combination of control variables may be employed up to the regenerator temperature limit set by the metallurgical aspects of that portion of the unit, such that temperature may range up to the order of 1250 F.
  • High temperature with good operating practices, provides no problem with catalyst sintering or deactivation and, in fact, regenerator operation appears to improve with respect to more uniform coke removal. Uncontrolled after-burning may be precluded at the high regeneration temperature levels by the hereinbefore described system of utilizing a temperature dierential control means across the upper and lower portions of the regenerator chamber to effect the control of the quantity of air being introduced into the dense phase zone of the regenerator.
  • Temperature dilerential becomes a sensitive measure of the quanti-ty of oxygen present and by having insufficient oxygen present to permit the oxidation of carbon monoxide to carbon dioxide in the light phase zone of the unit, there is proper control to prevent a temperature runaway.
  • a temperature diierential of 25 F. as a maximum will permit a differential temperature controller to regulate the proportion of air to the regenerator by adjustment of the valve in the air vent line from the air blower, to in turn provide for a steady-state regenerator operation wh-ich will preclude afterburning and at the same time effect a suitable reduction in the coke level to less than 0.5 percent coke by weight and preferably to 0.3 to 0.4 percent residual on the catalyst particles.
  • a temperature diierential of 25 F. as a maximum will permit a differential temperature controller to regulate the proportion of air to the regenerator by adjustment of the valve in the air vent line from the air blower, to in turn provide for a steady-state regenerator operation wh-ich will preclude afterburning and at the same time effect a suitable
  • the coke production rate and the catalyst circulation rate Vary inversely with the regenerator temperature, as, for example, a cool regenerator operating temperature at say ll F. results in a high coke rate for a given combined feed ratio and combined feed temperature. Stated another way, the coke rate opposes the direction in which the regenerator temperature moves, so that operations at high temperature levels in the regenerator are in the direction of improved product yields.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
US206271A 1962-06-29 1962-06-29 Fluid catalytic cracking of hydrocarbons Expired - Lifetime US3161583A (en)

Priority Applications (10)

Application Number Priority Date Filing Date Title
BE623712D BE623712A (zh) 1962-06-29
NL283942D NL283942A (zh) 1962-06-29
US206271A US3161583A (en) 1962-06-29 1962-06-29 Fluid catalytic cracking of hydrocarbons
DEU9279A DE1202925B (de) 1962-06-29 1962-09-22 Kontinuierliches Verfahren zum Kracken eines Frischoel und Kreislaufoel enthaltendenKohlenwasserstoffstromes
GB36652/62A GB971966A (en) 1962-06-29 1962-09-27 Continuous process for cracking hydrocarbon oil
AT855062A AT238859B (de) 1962-06-29 1962-10-29 Kontinuierliches Verfahren zum Kracken eines Kohlenwasserstoffbeschickungsstromes
ES282531A ES282531A1 (es) 1962-06-29 1962-11-16 Un procedimiento continuo para desintegrar una corriente de carga de hidrocarburo
FR920991A FR1359156A (fr) 1962-06-29 1963-01-10 Procédé continu de craquage des huiles hydrocarbonées
CH302063A CH446283A (de) 1962-06-29 1963-03-11 Kontinuierliches Verfahren zum Kracken eines Kohlenwasserstoffstromes
OA50632A OA00545A (fr) 1962-06-29 1964-11-18 Procédé continu de craquage des huiles hydrocarbonées.

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US206271A US3161583A (en) 1962-06-29 1962-06-29 Fluid catalytic cracking of hydrocarbons

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US3161583A true US3161583A (en) 1964-12-15

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US (1) US3161583A (zh)
AT (1) AT238859B (zh)
BE (1) BE623712A (zh)
CH (1) CH446283A (zh)
DE (1) DE1202925B (zh)
ES (1) ES282531A1 (zh)
FR (1) FR1359156A (zh)
GB (1) GB971966A (zh)
NL (1) NL283942A (zh)
OA (1) OA00545A (zh)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3206393A (en) * 1964-11-24 1965-09-14 Universal Oil Prod Co Fluid catalytic cracking of hydrocarbons
US3494858A (en) * 1967-11-17 1970-02-10 Exxon Research Engineering Co Two-stage countercurrent catalyst regenerator
US4149963A (en) * 1977-09-28 1979-04-17 Phillips Petroleum Company Control of afterburning in catalytic cracking
US4217243A (en) * 1976-04-30 1980-08-12 Phillips Petroleum Company Catalyst regenerator control
US4356082A (en) * 1980-12-18 1982-10-26 Mobil Oil Corporation Heat balance in FCC process
US4411773A (en) * 1980-12-18 1983-10-25 Mobil Oil Corporation Heat balance in FCC process and apparatus with downflow reactor riser
US4780195A (en) * 1983-07-25 1988-10-25 Ashland Oil, Inc. Addition of water to regeneration air
WO1995024965A1 (en) * 1994-03-15 1995-09-21 Exxon Research And Engineering Company Combustion control in a fluid catalytic cracking regenerator
US20040104149A1 (en) * 1999-08-20 2004-06-03 Lomas David A. Controllable volume reactor and process
US20040104148A1 (en) * 1999-08-20 2004-06-03 Lomas David A. Controllable space velocity reactor and process
WO2004058388A2 (en) 2002-12-20 2004-07-15 Uop Llc Fluidized bed reactor with residence time control
CN1819870B (zh) * 2002-12-20 2010-12-08 环球油品公司 带有停留时间控制的流化床反应器
US8932452B2 (en) 2012-01-11 2015-01-13 Cameron International Corporation Method for separating entrained catalyst and catalyst fines from slurry oil
CN115739059A (zh) * 2022-12-29 2023-03-07 安徽国孚润滑油工业有限公司 一种废硅油胶的脱附再生装置

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1434111A (en) * 1972-06-29 1976-05-05 Texaco Development Corp Continuous fluidised catalytic cracking process
EP0931587A1 (en) 1998-01-08 1999-07-28 Evc Technology Ag Catalyst, process for its preparation, and its use in the synthesis of 1,2-dichloroethane

Citations (4)

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US2409751A (en) * 1943-12-22 1946-10-22 Universal Oil Prod Co Catalytic conversion of hydrocarbons
US2414002A (en) * 1944-02-28 1947-01-07 Universal Oil Prod Co Regeneration of subdivided solid contact material
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
US2891001A (en) * 1953-12-14 1959-06-16 Kellogg M W Co Fluidized hydrocarbon conversion system with an improved regenerator distributor

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1010683B (de) * 1954-11-08 1957-06-19 Otto & Co Gmbh Dr C Verfahren zur thermischen Spaltung von Kohlenwasserstoffen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
US2409751A (en) * 1943-12-22 1946-10-22 Universal Oil Prod Co Catalytic conversion of hydrocarbons
US2414002A (en) * 1944-02-28 1947-01-07 Universal Oil Prod Co Regeneration of subdivided solid contact material
US2891001A (en) * 1953-12-14 1959-06-16 Kellogg M W Co Fluidized hydrocarbon conversion system with an improved regenerator distributor

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3206393A (en) * 1964-11-24 1965-09-14 Universal Oil Prod Co Fluid catalytic cracking of hydrocarbons
US3494858A (en) * 1967-11-17 1970-02-10 Exxon Research Engineering Co Two-stage countercurrent catalyst regenerator
US4217243A (en) * 1976-04-30 1980-08-12 Phillips Petroleum Company Catalyst regenerator control
US4149963A (en) * 1977-09-28 1979-04-17 Phillips Petroleum Company Control of afterburning in catalytic cracking
US4356082A (en) * 1980-12-18 1982-10-26 Mobil Oil Corporation Heat balance in FCC process
US4411773A (en) * 1980-12-18 1983-10-25 Mobil Oil Corporation Heat balance in FCC process and apparatus with downflow reactor riser
US4780195A (en) * 1983-07-25 1988-10-25 Ashland Oil, Inc. Addition of water to regeneration air
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
US20040104148A1 (en) * 1999-08-20 2004-06-03 Lomas David A. Controllable space velocity reactor and process
US20040104149A1 (en) * 1999-08-20 2004-06-03 Lomas David A. Controllable volume reactor and process
US7169293B2 (en) 1999-08-20 2007-01-30 Uop Llc Controllable space velocity reactor and process
US20070122316A1 (en) * 1999-08-20 2007-05-31 Lomas David A Controllable Space Velocity Reactor and Process
US7575725B2 (en) 1999-08-20 2009-08-18 Uop Llc Controllable space velocity reactor
WO2004058388A2 (en) 2002-12-20 2004-07-15 Uop Llc Fluidized bed reactor with residence time control
WO2004058388A3 (en) * 2002-12-20 2004-09-02 Uop Llc Fluidized bed reactor with residence time control
CN1819870B (zh) * 2002-12-20 2010-12-08 环球油品公司 带有停留时间控制的流化床反应器
US8932452B2 (en) 2012-01-11 2015-01-13 Cameron International Corporation Method for separating entrained catalyst and catalyst fines from slurry oil
CN115739059A (zh) * 2022-12-29 2023-03-07 安徽国孚润滑油工业有限公司 一种废硅油胶的脱附再生装置
CN115739059B (zh) * 2022-12-29 2024-03-19 安徽国孚环境科技股份有限公司 一种废硅油胶的脱附再生装置

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FR1359156A (fr) 1964-04-24
DE1202925B (de) 1965-10-14
GB971966A (en) 1964-10-07
BE623712A (zh)
ES282531A1 (es) 1963-06-16
AT238859B (de) 1965-03-10
CH446283A (de) 1967-11-15
NL283942A (zh)
OA00545A (fr) 1966-07-15

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