US2723948A - Catalytic cracking heat exchange process - Google Patents

Catalytic cracking heat exchange process Download PDF

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Publication number
US2723948A
US2723948A US176979A US17697950A US2723948A US 2723948 A US2723948 A US 2723948A US 176979 A US176979 A US 176979A US 17697950 A US17697950 A US 17697950A US 2723948 A US2723948 A US 2723948A
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United States
Prior art keywords
oil
catalyst
heat exchange
oil feed
slurry
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Expired - Lifetime
Application number
US176979A
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English (en)
Inventor
Jr William N Mccurdy
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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Filing date
Publication date
Priority to BE501388D priority Critical patent/BE501388A/xx
Application filed by Exxon Research and Engineering Co filed Critical Exxon Research and Engineering Co
Priority to US176979A priority patent/US2723948A/en
Priority to GB3596/51A priority patent/GB689280A/en
Priority to FR1041659D priority patent/FR1041659A/fr
Application granted granted Critical
Publication of US2723948A publication Critical patent/US2723948A/en
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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

Definitions

  • This invention generally concerns a catalyticcracking operation in which a gas oil fraction of a petroleum crude oil is cracked to yield lower boiling constituents.
  • the present invention concerns the specific problem of operating heat exchangers in conjunction with a fluidized catalytic cracking operation.
  • the principal ⁇ object of this invention is -to overcome certain problems of heat exchanger fouling ordinarily encountered in processing the streams connected with a liuidized catalytic cracking operation.
  • the particular heat exchanger referred to is a heat exchanger conventionally used to preheat the oil fed to the catalytic cracking reactor.
  • a large portion of this heating requirement can be met by passing the oil feed in heat exchange relationship with certain streams of the catalytic cracking system.
  • relatively rapid fouling of the heat exchanger in which this is carried out occurs.
  • the fouling isapparently due to deposition on the heat exchange coils of gummy material; presumably caused by polymerization of constituents usually occurring in the presence of oxygen dissolved in the oil feed, or possibly due tocarbonization of portions of the feed. It appears that these fouling constituents deposit ⁇ on heat exchange tubes when the oil feed has been raised to temperatures in the range of 250 to 400 F.
  • the numeral 1 identifies a catalytic cracking reactor in which the cracking operation may be conducted.
  • the numeral 2 represents the associated catalyst regenerator and the remaining processing units shown in the drawing identify the slurry equipment and associated apparatus required.
  • the catalytic cracking process conducted in reactor l is of the nature identified as a liuidized catalytic cracking operation.
  • the term fluidized identities the manner in which the solid catalyst particles are maintained as a dense boiling bed by passing gas through the particles to maintain a high degree of turbulence.
  • catalyst and oil feed are continuously introduced to the lower portion of reactor 1 as described, while cracked products are removed at the top of the reactor through line 5 as described, and catalyst is continuously removed from the bottom of reactor 1 through draw-o 6.
  • the catalyst Withdrawn through draw-off 6 may be said to be spent catalyst, having been retained in the reactor 1 for sufficient periods of time to have become fouled with carbon and gummy material.
  • This catalyst may be regenerated by the process of burning the fouling constituents from the catalyst.
  • air may be passed through line 7 to carry the spent catalyst upwardly through line 8 to regeneration zone 2.
  • zone 2 as in reactor 1, the catalyst is maintained in a fluidized condition by the air.
  • the gas velocities employed to secure the desired fluidization of the catalyst in reactor 1 and regenerator 2 are a slurry, and is generally identified as slurry oil.
  • Reactor 1 is maintained at temperatures in the range of 900 to 1000 F.
  • regenerator 2 is maintained at temperatures of about 1050 to 1150 F.
  • the catalyst employed may be selected from vany of the known cracking catalysts, such as alumina supported on Group 6 metals.
  • the catalyst may be cobalt, nickel, iron or compounds of Group 6 oxides, with nickel, cobalt or iron.
  • the catalyst is preferably in powdered form having a size of about 200 to 400 mesh, although particles outside this range may be em- Y ployed.
  • the fractionator may consist of a conventional type of fractionator employing a bottom pump around circuit.
  • the fractionator may contain any desired type of fractionating plates, or packing material, or as illustrated, the upper part of fractionator 10 may contain fractionating plates 11, while the lower part of fractionator 10 may contain the disc and donut packing diagrammatically illustrated and-designated by numeral 12.
  • the products of line 5 are introduced to the bottom of fractionator 1t), and the fractionated constituents are then removed from fractionator 10 through overhead line 13, and side stream withdrawal lines 14 and 15.
  • the heavier boiling constituents existing in the material introduced to the fractionator are withdrawn from the bottom of fractionator 16, through line 16.
  • These heavier boiling constituents will contain catalyst carried over from reactor 1.
  • the catalyst concentration will be about 0.2 pound per gallon to about l pound per gallon, although normally the catalyst concentration is about 0.4 pound per gallon.
  • This concentration of catalyst in the heavy constituents of line 16 provides a heavy oil appearing as The stream of slurry oil withdrawn through line 16 is then subdivided to pass in part through the waste heat boiler 17 and the feed preheater 18.
  • the portion of the slurry oil passed through the waste heat boiler 17 is passed in heat exchange relationship with water so as to remove heat from the slurry oil and simultaneously produce useful steam.
  • the cooled slurry oil is then re-introduced to fractionator 10 through line 19.
  • the portion of the slurry oil pumped through the feed preheater 18 is similarly passed in heat exchange relationship with oil feed so as to preheat the oil feed. This is generally conducted, as shown by the solid lines, by passing theslurry oil of line 16 through the coils 20 of the preheater 18.
  • the oil feed pumped through line 1 is circulated around the outer portion of the coils 20 for removal from the heat exchanger through line 3.
  • the slurry oil withdrawn from fractionator 10 has a temperature of above 500 F., or preferably about 600 or 650 F., and in passing through preheater 18 is generally cooled to about 450 F.
  • This cooling of the slurry oil is effective to heat-oil feed, by heat exchange, to a temperature of about 400 F; and preferably to above 500 F.
  • operation of this feed preheater results in the deposition of fouling materials on the coils 2,0.
  • heat exchange coefficients can drop fromabout 50 to 30 in a period of l5 days, as a result of this fouling. Ordinarily this necessitates cleaning of coils 2t) after about l5 days of operation.
  • a catalytic cracking operation which comprises heating a gas oil feed to a temperature in the range of 400 to 650 F. in a preheating zone, catalytically cracking said heated gas oil in a fluid catalyst cracking zone, pass ing the cracked products from said cracking zone to# gether with entrained solid catalyst to a fractionation zone, and separating from the cracked product a hot high boiling hydrocarbon oil slurry fraction containing about 0.2 to 1% of solid catalyst particles per gallon of oil, passing the said hot high boiling hydrocarbon slurry fraction at a temperature of about 650 Fn from said fractionation zone in indirect heat exchanger relationship with the said gas oil feed stream in said preheating zone, and periodically reversing the flow of the feed gas oil and hot high boiling hydrocarbon slurry fraction while substantially maintaining ow of said liquids so as to bring the gas oil feed and high boiling slurry fraction on opposite sides of the heat exchange surfaces of the said preheating zone and maintaining such reversed flow for about 48 hours whereby the solid particles in the slurry remove fouling material

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  • Chemical & Material Sciences (AREA)
  • 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)
US176979A 1950-08-01 1950-08-01 Catalytic cracking heat exchange process Expired - Lifetime US2723948A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BE501388D BE501388A (en, 2012) 1950-08-01
US176979A US2723948A (en) 1950-08-01 1950-08-01 Catalytic cracking heat exchange process
GB3596/51A GB689280A (en) 1950-08-01 1951-02-14 Catalytic cracking heat exchange process
FR1041659D FR1041659A (fr) 1950-08-01 1951-03-12 Procédé d'échange de chaleur pour des opérations de cracking catalytique

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US176979A US2723948A (en) 1950-08-01 1950-08-01 Catalytic cracking heat exchange process

Publications (1)

Publication Number Publication Date
US2723948A true US2723948A (en) 1955-11-15

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US176979A Expired - Lifetime US2723948A (en) 1950-08-01 1950-08-01 Catalytic cracking heat exchange process

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US (1) US2723948A (en, 2012)
BE (1) BE501388A (en, 2012)
FR (1) FR1041659A (en, 2012)
GB (1) GB689280A (en, 2012)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2768934A (en) * 1952-02-26 1956-10-30 American Oil Co Heat exchanger system
US2945799A (en) * 1956-05-10 1960-07-19 Exxon Research Engineering Co Catalytic conversion of hydrocarbons with removal of fouled material from heat exchangers
US3164541A (en) * 1960-08-08 1965-01-05 Oil Shale Corp Transport of balls by oil
US4615795A (en) * 1984-10-09 1986-10-07 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process
US4732740A (en) * 1984-10-09 1988-03-22 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2210257A (en) * 1939-08-12 1940-08-06 Universal Oil Prod Co Catalytic conversion of hydrocarbons
US2353399A (en) * 1940-05-25 1944-07-11 Sinclair Refining Co Manufacture of gasoline
US2423833A (en) * 1944-08-19 1947-07-15 Foster Wheeler Corp Fluid catalytic conversion of hydrocarbon oils
US2493494A (en) * 1945-04-11 1950-01-03 Standard Oil Dev Co Heat recovery in a fluidized catalyst regeneration
US2576843A (en) * 1944-12-30 1951-11-27 Rosenblads Patenter Ab Heat exchange apparatus

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2210257A (en) * 1939-08-12 1940-08-06 Universal Oil Prod Co Catalytic conversion of hydrocarbons
US2353399A (en) * 1940-05-25 1944-07-11 Sinclair Refining Co Manufacture of gasoline
US2423833A (en) * 1944-08-19 1947-07-15 Foster Wheeler Corp Fluid catalytic conversion of hydrocarbon oils
US2576843A (en) * 1944-12-30 1951-11-27 Rosenblads Patenter Ab Heat exchange apparatus
US2493494A (en) * 1945-04-11 1950-01-03 Standard Oil Dev Co Heat recovery in a fluidized catalyst regeneration

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2768934A (en) * 1952-02-26 1956-10-30 American Oil Co Heat exchanger system
US2945799A (en) * 1956-05-10 1960-07-19 Exxon Research Engineering Co Catalytic conversion of hydrocarbons with removal of fouled material from heat exchangers
US3164541A (en) * 1960-08-08 1965-01-05 Oil Shale Corp Transport of balls by oil
US4615795A (en) * 1984-10-09 1986-10-07 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process
US4732740A (en) * 1984-10-09 1988-03-22 Stone & Webster Engineering Corporation Integrated heavy oil pyrolysis process

Also Published As

Publication number Publication date
FR1041659A (fr) 1953-10-26
GB689280A (en) 1953-03-25
BE501388A (en, 2012) 1951-03-15

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