GB708956A - Hydrocarbon conversion process - Google Patents

Hydrocarbon conversion process

Info

Publication number
GB708956A
GB708956A GB22192/51A GB2219251A GB708956A GB 708956 A GB708956 A GB 708956A GB 22192/51 A GB22192/51 A GB 22192/51A GB 2219251 A GB2219251 A GB 2219251A GB 708956 A GB708956 A GB 708956A
Authority
GB
United Kingdom
Prior art keywords
reactor
separator
tower
pipe
vapours
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
GB22192/51A
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 Oil Corp
Original Assignee
Socony Vacuum Oil Co Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Socony Vacuum Oil Co Inc filed Critical Socony Vacuum Oil Co Inc
Publication of GB708956A publication Critical patent/GB708956A/en
Expired legal-status Critical Current

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/10Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Landscapes

  • 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)

Abstract

A heavy hydrocarbon oil such as crude petroleum or topped crude petroleum, is heated so that partial vaporization is effected, the mixture of residual oil and vapours is passed to a phase separator, the vapours from the separator are fed to a cracking zone containing a moving or fluidized bed of solid particles (catalytic or inert), the residual oil from the separator is submitted to vacuum distillation until a heavy material having an ASTM soft point between 60 DEG and 90 DEG F. remains as residue, the vacuum distillate is condensed, and the condensate is introduced as liquid feed <PICT:0708956/III/1> into the cracking zone. The heavy material withdrawn from the vacuum distillation zone may be mixed with a fraction of the cracked products boiling above 400 DEG F. to give a fuel oil having a viscosity (Saybolt Furol) between 45 and 300 seconds. The contact material may be a synthetic association of silica and/or alumina to which small amounts of other materials, such as metal oxides, can be added. Other contact materials mentioned are natural or treated clays, bauxite, mullite, zirkite, corhart, metals, and stones. Instead of passing the vapours from the separator and the condensate from the vacuum distillation to a cracking zone they may be passed to a zone in which reforming, hydrogenation, dehydrogenation, aromatization, or alkylation is effected. The feed stock is charged through pipe 1 to furnace 2, wherein it is heated to a temperature between 700 DEG and 900 DEG F.; and the mixture of liquid and vapour so produced is passed to separator 4 which is maintained at a pressure between 10 and 30 p.s.i.g. If desired, steam may be introduced into the separator through pipe 5. Vapours at a temperature between 600 DEG and 850 DEG F. leave the separator through pipe 7, and are fed to the lower part of reactor 74, which contains a fluidized bed of hot, finely-divided contact material. If necessary, the vaporous feed can be heated further before being fed to reactor 74, by by-passing some or all of it through furnace 9. The liquid from separator 4 passes through pipe 15 into vacuum tower 16 (which can have two, three or more plates) maintained at an absolute pressure of 1 to 6 lbs./square inch by means of pump 20. Vapours leave the head of tower 16 at a temperature between 550 DEG and 775 DEG F., and are condensed in condenser 18. The condensate is collected in tank 19. Part of the condensate may, if desired, be pumped to the top of tower 16 as reflux; and an upper side stream from tower 16 may be pumped, via a condenser, to separator 4. Liquid from tank 19 is pumped as liquid feed to reactor 74 via pipe 22. Residual material at a temperature between 600 DEG and 800 DEG F. is withdrawn from the base of tower 16 through pipe 23, and is utilized to heat the liquid flowing to reactor 74 through pipe 22, by means of heat-exchanger 28. In an alternative procedure, the liquid feed may be preheated by heat-exchange with the vapours leaving the head of tower 16. If desired, additional heating (up to 800 DEG F.) of the liquid feed is effected by by-passing some or all of it through furnace 29. The liquid feed is sprayed into the upper part of reactor 74 through a nozzle 79. The conversion products are withdrawn from the reactor through pipe 80. Contaminated contact materials passes down standpipe 75, and is lifted in a fluidized state through conduit 76 to regenerator 70 by oxidizing gas introduced via valve 77. The regenerated catalyst withdrawn from the regenerator is brought to the desired contact temperature by means of heat-exchanger 73 in standpipe 71, and is then returned to reactor 74 through conduit 72 by means of carrying gas such as steam, flue gas or gaseous hydrocarbons, supplied via valve 73. In another embodiment, the regenerated catalyst is conveyed to the reactor by means of the vapours from separator 4; and the liquid feed from tank 19 is introduced into the stream before it reaches the reactor. The products withdrawn from the top of the reactor may be passed into a flash tower, the distillate from which is passed on to further recovery operations, while the liquid bottoms are recycled to the reactor. In the product recovery system, material boiling above gasoline may be recovered as recycle oil by fractionation. Part of the recycle oil may be employed for cutting back the bottom product from tower 16 to a fuel oil of suitable viscosity. The remainder may be recycled to furnace 2. Specification 593,778 is referred to.
GB22192/51A 1950-12-15 1951-09-21 Hydrocarbon conversion process Expired GB708956A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US708956XA 1950-12-15 1950-12-15

Publications (1)

Publication Number Publication Date
GB708956A true GB708956A (en) 1954-05-12

Family

ID=22098009

Family Applications (1)

Application Number Title Priority Date Filing Date
GB22192/51A Expired GB708956A (en) 1950-12-15 1951-09-21 Hydrocarbon conversion process

Country Status (1)

Country Link
GB (1) GB708956A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115491232A (en) * 2022-10-13 2022-12-20 陕西延长石油(集团)有限责任公司 Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy and poor-quality residual oil

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115491232A (en) * 2022-10-13 2022-12-20 陕西延长石油(集团)有限责任公司 Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy and poor-quality residual oil
CN115491232B (en) * 2022-10-13 2024-01-23 陕西延长石油(集团)有限责任公司 Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy inferior residual oil

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