US2844524A - Integration of coker with refinery - Google Patents

Integration of coker with refinery Download PDF

Info

Publication number
US2844524A
US2844524A US399036A US39903653A US2844524A US 2844524 A US2844524 A US 2844524A US 399036 A US399036 A US 399036A US 39903653 A US39903653 A US 39903653A US 2844524 A US2844524 A US 2844524A
Authority
US
United States
Prior art keywords
coking
coker
line
heavy
zone
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 - Lifetime
Application number
US399036A
Other languages
English (en)
Inventor
Jr Henry Ernst
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
Original Assignee
Exxon Research and Engineering Co
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
Priority to BE533993D priority Critical patent/BE533993A/xx
Application filed by Exxon Research and Engineering Co filed Critical Exxon Research and Engineering Co
Priority to US399036A priority patent/US2844524A/en
Priority to GB33969/54A priority patent/GB774924A/en
Priority to DEST9181A priority patent/DE1010218B/de
Application granted granted Critical
Publication of US2844524A publication Critical patent/US2844524A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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

Definitions

  • This invention relates to the coking of heavy petroleum residua in contact with hot fluidized solids and to a process particularly adapted for such coking.
  • the gas oil product from fluid coking is usually designated for further processing by catalytic cracking, the gas oil must be relatively free of catalystpoisoning impurities.
  • the fluid coking operation tends to volatilize ash materials, like the compounds of iron, nickel, chromium, and vanadium.
  • some heavy condensed ring aromatics of poor catalytic cracking quality are also passed over with the coker product. For these reasons, it is the prudent practice to fractionate the coker product to remove from the catalytic-feed stock heavy ends which contain these materials. Generally these heavy ends are recycled to the coker in order that all of the available hydrocarbon material in the ends can be converted to lighter, and hence more valuable, products.
  • the fluid coker receives topped crude that has been processed by atmospheric and vacuum distillation to remove naphthas and gas oils.
  • the gas oils contained in the ends can be substantially removed and sent to catalytic Patented July 22, 1958 processing and in this manner the economic drawbacks to the conventional mode of operation will be avoided. This new process is illustrated in the attached drawing which forms a part of this specification.
  • an object of this invention to provide an improved method for converting topped crude into high yields of napthas and gas oils suitable for further catalyic cracking. Another object is to devise a process for coking residuum oils in such a manner as to reduce the amount of gas oils recycled to the coker. A more specific object of this invention is to increase the efliciency and practicability of the fluid coking process by adroit treatment of fractionated recycled heavy ends from the coker eifluent. pear more clearly as this description proceeds.
  • the inventions objects are attained by processing a crude in the following manner:
  • the crude is first subjected to atmospheric and then to vacuum distillation to secure the virgin naphthas and gas oils for other operations.
  • the reduced crude is then sprayed into a conventional fluid coker.
  • the volatiles issuing from the coker are fractionated to obtain gas oils for catalytic cracking and heavy impurity containing ends.
  • the heavy ends are recycled, not to the coker, but to the vacuumv distillation zone where gasoils are removed from the ends before the ends are again subjected to pyrolysis.
  • the crude enters the process by a line 1 after being suitably heated to about'600" to 800 F. It is first fractionated in a conventional atmospheric fractionator 10 and separated into light gases, removed by line 2, a naphtha fraction, removed by line 3, a gas oil fraction, removed by line 4, and the topped crude bottoms, removed by line 21. The light gases, naphtha and gas oil are sent to other conventional refining steps not shown.
  • the topped crude, via lines 21 and 5 is transferred to a vacuum distillation chamber 20 j where further amounts of gas oil are separated and removed from the topped crude and passed by line 6 to line 4.
  • the vacuum crude produced is then transferred by line 7 to the fluid coking vessel 30 and sprayed into the dense fluidized bed of coke particles having a particle size of to 500 microns.
  • the fluidized bed can consist of other finely divided solids such as sand.
  • the coking vessel per se is not a part of this invention.
  • the coker consists of a coking vessel 30 and a solids heating or burning system shown herein as a transfer line burner 70.
  • a conventional fluid bed burner may be substituted for the transfer line burner, if desired, both types being well known. Either is entirely satisfactory for the present application.
  • the fluid coker is operated at about atmospheric pressure or a, little above, e. g., 0 to '50 p. s. i. g.
  • the gaseous coker products pass upward through the coker and through a gas-solids separator or cyclone 40 where entrained fines are removed and returned to the fluidized bed by line 13. The hot products are then transferred to a fractionation zone 60 through line 14.
  • Coke is removed from the coker by line 8 in order that the pseudo-liquid level of the particles can be maintained at the desired height and in order to remove the coke particles that have increased beyond a fluidizable size because of the carbon deposition.
  • the coke particles flow down standpipe 8 by gravity and are engaged by a stream of air from line 9, the air being supplied by a source not shown, and are pneumatically conveyed up- Further objects and advantages will apward in the transfer line burner 70.
  • the conveying air supports a partial combustion of the entrained coke particles in the transfer line burner. This burning adds heat to the remaining or unburned coke particles which are thereafter recycled.
  • the coke particles after their partial combustion, are separated from the flue gas formed during the combustion, in a gas-solids separator 50.
  • the separated solids pass downward to the coker by line 11.
  • the flue gas is removed by line 15 from "the separator and may be utilized for its heat value elsewhere.
  • the coke returned in line 11 to the coker may be in excess of the amount needed and a drawoff can be made of this excess by line 12.
  • Standard operating conditions are contemplated for the coker in order that large proportions of gas oils may be produced to serve as catalytic cracking stock.
  • the fluidized bed density will be about 20 to 60 lbs. per cu. ft., the superficial fluidizing velocity about 0.5 to 7 ft./sec., the coking temperature about 900 to 1050 F., the hydrocarbon vapor residence time about to 30 seconds, and the operating pressure about or slightly above atmospheric.
  • a fluidizing gas such as steam is added through one or more inlet lines, one of which is shown at 31.
  • the coker efiiuent is separated into the desired products by a fractionator 60. As illustrated, only three fractions are separated but a more selective fractionation can be made.
  • Uncondensed gases are removed from the fractionator by line 16 and passed to line 2 where they are removed from the process.
  • the desired gas oil in cluding some gasoline fractions is removed by line 17 and blended with the gas oil from the initial distillation stage in line 4.
  • the mixture of gas oils then can be sent to catalytic cracking, storage or other operations as desired.
  • the coker gas oil can be kept separate from the virgin gas oil and separately treated.
  • the bottoms fraction is removed from the fractionator by line 18 and is passed to line 5 where it enters the vacuum distillation zone as has been before indicated. Although it is not contemplated, a portion of the recycled bottoms can be passed to the coker via lines 19 and 7. This will depend upon specific operating conditions and economics.
  • Virgin naphtha 375 F. B. Pt 7,000 bbl./ day.
  • Virgin gas oil 375 to 1,l00 F.
  • B. Pt. (including some 1000 1100 coker material) 19,000 bbL/day.
  • Coker gas oil 250 to 1,000 F.
  • Topped crude boiling above 860' F. (to vac. distillation) 9,000 bbL/day. Recycled bottoms, boiling above 1000 F 1,370 bbL/day. Vacuum crude, boiling above 1100 F. (to coker) 3,800 bbl./day Vacuum crude, boiling above (net virgin).
  • a process of coking residual oils which comprises admixing a topped crude from an atmospheric distillation Zone with a recycled impurity containing bottoms fraction, separating the resulting mixture in a vacuum distillation zone into a light product fraction substantially free from impurities and a heavy tar boiling above 1050 F. containing the bulk of said impurities, subjecting said heavy tar to conditions of coking of a temperature in the range of 900 to 1050 F.
  • a process of coking residual oils which comprises admixing a topped crude feed from an atmospheric distillation zone with a recycled impurity containing bottoms fraction, separating the resulting mixture in a vacuum distillation zone into a light product fraction substantially free from impurities and a heavy tar containing the bulk of said impurities, subjecting said heavy tar to conditions of coking of a temperature in the range of above 900 to 1050 F.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)
  • Coke Industry (AREA)
US399036A 1953-12-18 1953-12-18 Integration of coker with refinery Expired - Lifetime US2844524A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BE533993D BE533993A (en:Method) 1953-12-18
US399036A US2844524A (en) 1953-12-18 1953-12-18 Integration of coker with refinery
GB33969/54A GB774924A (en) 1953-12-18 1954-11-23 Thermal cracking of heavy petroleum oils
DEST9181A DE1010218B (de) 1953-12-18 1954-12-16 Verfahren zur Gewinnung wertvoller Produkte aus Rohoelen durch Destillation und thermische Umsetzung

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US399036A US2844524A (en) 1953-12-18 1953-12-18 Integration of coker with refinery

Publications (1)

Publication Number Publication Date
US2844524A true US2844524A (en) 1958-07-22

Family

ID=23577872

Family Applications (1)

Application Number Title Priority Date Filing Date
US399036A Expired - Lifetime US2844524A (en) 1953-12-18 1953-12-18 Integration of coker with refinery

Country Status (4)

Country Link
US (1) US2844524A (en:Method)
BE (1) BE533993A (en:Method)
DE (1) DE1010218B (en:Method)
GB (1) GB774924A (en:Method)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3487006A (en) * 1968-03-21 1969-12-30 Lummus Co Direct pyrolysis of non-condensed gas oil fraction
US4137149A (en) * 1977-06-29 1979-01-30 Exxon Research & Engineering Co. Slurry hydrogen treating processes
US4551232A (en) * 1983-02-09 1985-11-05 Intevep, S.A. Process and facility for making coke suitable for metallurgical purposes
US4592830A (en) * 1985-03-22 1986-06-03 Phillips Petroleum Company Hydrovisbreaking process for hydrocarbon containing feed streams
US20170253809A1 (en) * 2016-03-06 2017-09-07 David Ledo Perez Solid Residue Separation: A New Way of Transporting and Processing Heavy Feedstocks

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2543884A (en) * 1947-08-12 1951-03-06 Standard Oil Dev Co Process for cracking and coking heavy hydryocarbons
US2598058A (en) * 1950-01-06 1952-05-27 Universal Oil Prod Co Continuous conversion and coking of heavy liquid hydrocarbons

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2561334A (en) * 1948-01-22 1951-07-24 Lummus Co Method of hydrocarbon conversion to lower boiling hydrocarbons and coke

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2543884A (en) * 1947-08-12 1951-03-06 Standard Oil Dev Co Process for cracking and coking heavy hydryocarbons
US2598058A (en) * 1950-01-06 1952-05-27 Universal Oil Prod Co Continuous conversion and coking of heavy liquid hydrocarbons

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3487006A (en) * 1968-03-21 1969-12-30 Lummus Co Direct pyrolysis of non-condensed gas oil fraction
US4137149A (en) * 1977-06-29 1979-01-30 Exxon Research & Engineering Co. Slurry hydrogen treating processes
US4551232A (en) * 1983-02-09 1985-11-05 Intevep, S.A. Process and facility for making coke suitable for metallurgical purposes
US4592830A (en) * 1985-03-22 1986-06-03 Phillips Petroleum Company Hydrovisbreaking process for hydrocarbon containing feed streams
US20170253809A1 (en) * 2016-03-06 2017-09-07 David Ledo Perez Solid Residue Separation: A New Way of Transporting and Processing Heavy Feedstocks
US10421914B2 (en) * 2016-03-06 2019-09-24 David Ledo Perez Solid residue separation: a new way of transporting and processing heavy feedstocks

Also Published As

Publication number Publication date
GB774924A (en) 1957-05-15
BE533993A (en:Method)
DE1010218B (de) 1957-06-13

Similar Documents

Publication Publication Date Title
EP0191207B1 (en) Process for improving product yields from delayed coking
US4213848A (en) Fluid coking and gasification process
US2768127A (en) Improved residual oil conversion process for the production of chemicals
US2573906A (en) Multistage catalytic conversion of bituminous solids
US2436160A (en) Cracking of hydrocarbon oils with
US2598058A (en) Continuous conversion and coking of heavy liquid hydrocarbons
US2690990A (en) Production of motor fuels from heavy hydrocarbon oils in a two stage conversion process with inert solids
US3093571A (en) Method and apparatus for treating shale
US4816136A (en) Low severity fluid coking
US2416608A (en) Catalytic conversion of oils
US4295956A (en) Fluid coking process
US3238271A (en) Cracking of hydrocarbons to gaseous olefines
US2844524A (en) Integration of coker with refinery
US1972944A (en) Treatment of hydrocarbon oils and coal
US2863823A (en) Combination transfer line and fluid bed coking system
US5176819A (en) Coking process with hot solids recycled to the stripping zone
US4552649A (en) Fluid coking with quench elutriation using industrial sludge
US2853434A (en) Two stage coking of residua feeds in unitary reactor
US3661767A (en) Fluid coking-steam cracking combination process
US1986593A (en) Treatment of hydrocarbon oils and coal
US5658455A (en) Fluidized bed coking process
US3144400A (en) Fluid coking process
US4426277A (en) Low severity fluid coking process
US2899376A (en) Liquid phase - boo
US2879221A (en) Hydrocarbon oil conversion process