US2777802A - Extractive distillation operation for preparation of catalytic cracking feed stocks - Google Patents

Extractive distillation operation for preparation of catalytic cracking feed stocks Download PDF

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Publication number
US2777802A
US2777802A US474477A US47447754A US2777802A US 2777802 A US2777802 A US 2777802A US 474477 A US474477 A US 474477A US 47447754 A US47447754 A US 47447754A US 2777802 A US2777802 A US 2777802A
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distillation
tower
catalytic cracking
metal contaminants
boiling
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US474477A
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English (en)
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Nick P Peet
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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Priority to NL100147D priority Critical patent/NL100147C/xx
Priority to NL202701D priority patent/NL202701A/xx
Priority to BE543301D priority patent/BE543301A/xx
Application filed by Exxon Research and Engineering Co filed Critical Exxon Research and Engineering Co
Priority to US474477A priority patent/US2777802A/en
Priority to GB34143/55A priority patent/GB782791A/en
Priority to FR1138469D priority patent/FR1138469A/fr
Priority to DEE11658A priority patent/DE1035296B/de
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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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting

Definitions

  • This invention concerns a novel erative to reduce the content present in catalytic cracking charge stocks.
  • the invention concerns the use of a novel refluxing agent in a distillation operation in a manner to cause removal of metal contaminants by the principles of extractive distillation.
  • the novel refluxing agent employed in accordance with this invention is a high molecular weight asphaltic material.
  • the feed stock to a catalytic cracking operation constitutes a so-called gas oil fraction of crude oil which boils in the range of about 400 to 800 F. or somewhat higher.
  • Portions of the gas oil boiling distillation process opof metal contaminants petroleum crude oil boiling above the range may be considered residual petroleum fractions.
  • Such residual fractions may be used as sources of asphalt, fuel, and other products which are of relatively low economic value. It, therefore, becomes attractive to develop means for successfully utilizing portions of the residual fractions of crude oil as catalytic cracking feed stock.
  • the gas oil distillate referred to would have a boiling range of about 700 to 1100 F.
  • metal contaminant carry over in the segregation of heavy distillate fractions is apparently due to two phenomena. First of all, it appears that the metal contaminants occur or are converted during distillation to the form of metal complexes. These complexes may generally be identified as large condensed ring substances. Some of these metal complexes and particularly nickel porphyrins are sufliciently volatile so as to be carried overhead at a temperature of about 1050 F. Consequently, when attempting to segregate heavy boiling gas oil fractions including components boiling above about 900 F., volatile metal contaminants are unavoidably obtained in the distillate product. It
  • the present invention is based on the discovery that certain high molecular weight condensed ring aromatic compounds are effective as solvents for the objectionable metal complexes present in crude oil. Consequently, by introducing these particular solvents into a distillation zone, by virtue of their high boiling character, metal contaminants can be removed from distillate fractions by the principles of extractive distillation.
  • the present invention therefore, concerns a technique by which certain high molecular weight condensed ring aromatic compounds are employed as an extractive distillation refluxing agent in the segregation of heavy oil fractions.
  • the extractive distillation refluxing agent to be employed may be defined as a high molecular Weight asphaltic material containing a low concentration of nickel compounds and particularly characterized by substantially no volatilization of nickel components at temperatures of about 1050 to 1300" F. at atmospheric pressure.
  • the high molecular weight asphaltic material referred to contains a large portion of condensed ring aromatic compounds believed to have more than about 15 rings in the molecule.
  • the asphaltic materials boil from about 1050" F. up to about 1400 F. and higher.
  • refluxing agents must contain a low concentration of metal contaminants, although some high boiling metal contaminants can be tolerated.
  • concentration of metal contaminants capable of volatilizing at temperatures below about 1300 F. should be less than about 2 to 5 pounds per 1000 barrels. In some cases, somewhat greater concentrations of higher boiling metal contaminants can be tolerated, the limitation relating to the possibility of entrainment in the particular distillation facilities available.
  • the extractive distillation refluxing agent can be derived from two potential sources.
  • First of all in the case of those petroleum crude oils having remarkably low content of total metal contaminants or remarkably low content of volatile metal contaminants, it is possible to segregate suitably high molecular weight asphaltic material for the purposes of t 's invention. This, however, is the exceptional case since the asphaltic materials of the character required when derived from the average or typical crude oil contain prohibitively high concentrations of metal contaminants.
  • the refluxing agent can also be a synthetic, high molecular weight asphaltic material derived from cracking operations.
  • a desirable source of the refluxing agent free from metal contaminants is secured from thermal tar obtained in conventional refinery operations, particularly when cracking distillate stocks.
  • Such a tar may be obtained by distilling the products from a thermal cracking unit.
  • the objective is to remove the greatest possible portion of constituents boiling below about I050 F. This is best conducted by carrying out the distillation as a vacuum flashing process although alternatively a deasphalting process may be used to segregate the desired asphaltic fraction.
  • the refluxing agent to be employed can be derived from virgin or thermally cracked stocks by distillation or deasphalting
  • the preferred source of the refluxing agent is from :catalytically cracked products.
  • the highest boiling fractions of catalytically cracked feed stocks are conventionally designated as cycle oil and/ or clarified oil.
  • Such fractions include high molecular weight condensed ring aromatic compounds which may be designated as synthetic asphalts formed during the catalytic cracking operation. These materials are particularly effective in the practice of this invention and can be recovered from cycle oil or a clarified oil by vacuum flashing or deasphalting processes. It is also attractive to obtain the refluxing agent from thermal tars derived from catalytically cracked stock.
  • synthetic asphaltic materials are injected into the distillation zone for segregating heavy boiling gas oil fractions in proportions of about 1% to 50% based on the hydrocarbon vapor rate at the portion of the distillation zone at which the refluxing agent is injected.
  • the lower limit of the amount of refluxing agent to be used is determined by the concentration of metal contaminants in the stock distilled coupled with a consideration of the degree of contaminant removal required in the distillate product. In general, however, it is preferred to employ amounts of refluxing agent in the range of about 2% to about 20% and particularly about 5% based on the hydrocarbon vapor rate in the distillation operation.
  • the refluxing agent In order to secure the desired contaminant removal from heavy distillate products, it is essential that the refluxing agent be brought into the distillation tower at a point somewhat below the side stream withdrawalpoint of the highest boiling distillate product.
  • the refluxing agent must be brought into intimate contact with upflowing hydrocarbon vapors in the distillation tower.
  • the refluxing agent must be deposited over at least one plate in the distillation tower and preferably a greater number of plates ideally providing at least one theoretical stage of contacting of the vapors.
  • the refluxing agent together with extracted metal contaminants can be removed from the distillation tower at a lower side stream withdrawal point or, alternatively, the refluxing agent can be withdrawn together With the bottoms product of the distillation tower.
  • Fig. 1 diagrammatically illustrates application of the present invention to a vacuum distillation operation
  • Fig. 2 shows the application ofthe invention in a coking process
  • Fig. 3 shows the application of the invention to a combination distillation and cracking operation
  • Fig. 4 illustrates the invention when employed in a combination coking and cracking operation
  • Fig. 5 shows the invention when used in a combination distillation coking and cracking operation.
  • Fig. l the invention is illustrated in its basic application to a distillation tower.
  • the numeral I identifiies a distillation tower for the segre gation of oil fractions of a petroleum crude oil.
  • Tower 1 can particularly constitute a vacuum still operated at pressures of about 25 mm. to 250 mm. of mercury.
  • a petroleum oil is generally subjected to preliminary fractionation in an atmospheric distillation tower providing a bottoms fraction constituting reduced crude oil boiling above about 600 F.
  • Such a reduced crude oil can be brought into tower 1 through line 2 at temperatures of about 600 to 850 F.
  • the reduced crude oil undergoes a flashing operation in the lowest portion of the vacuum distillation tower so that light portions of the reduced crude are carried overhead in vaporform and the heaviest boiling fractions are carried downwardly toward the bottom of the tower.
  • the lightest boiling fractions can be removed from line 3 but successively higher boiling fractions can be removed from side stream withdrawals 4, 5 and 6.
  • Ordinarily the heaviest fractions of the reduced crude are'subjected to a steam stripping operation in the bottom of the distillation tower utilizing steam injected through line 7.
  • the stripped products constituting residual crude oil are then withdrawn through bottoms withdrawal 8.
  • Table I data are presented in Table I illustrating the amount of metal contaminants typically present in reduced crude derived from a variety of sources.
  • columns 1, 2, 3, 4 and 5, respectively, show the characteristics of residua derived from a mixture of Gulf Coast and West Texas crudes, a West Texas crude, a Panhandle crude, a Hawkins crude and a Lagunillas crude.
  • a synthetic asphaltic material of the character identified is brought into distillation tower 1 through line 9 at an introduction point somewhat below the lowest side stream withdrawal point.
  • the synthetic asphalt is introduced in quantities of about 1% to 50% by weight based on the volume of hydro carbon gases flowing upwardly through the portion of the distillation tower at which the synthetic asphalt is introduced. Since the synthetic asphalt, as identified, is a high boiling'material, it is present in liquid phase in distillation tower 1. Contact with upflowing hydrocarbon vapors results in selective extraction of metal contaminants and, in addition, the'synthetic asphalt serves to prevent entrainment of liquid portions "of the residual oil present in tower 1.
  • the synthetic asphaltic material can be withdrawn from distillation tower 1 through lower side stream Withdrawal or, alternatively, the asphaltic material may be allowed to pass downwardly through the tower for removal with residuum through line 8.
  • the synthetic asphaltic material containing extracted metallic contaminants is then discarded from the system and finds use as a fuel.
  • the synthetic asphaltic material may be subjected to severe flashing conditions, permitting removal of high boiling gas oil rich in metal contaminants as overhead product and withdrawal of a purified synthetic asphaltic material as a bottoms product which can be recycled to tower 1.
  • the invention is illustrated as applied to the distillation of products subjected to a coking operation in order to obtain heavy boiling products suitable for catalytic cracking.
  • the numeral designates a coking reactor in which residual portions of petroleum oil are contacted with coke particles at temperatures of about 800 to 1000 F. in order to secure conversion to lighter boiling constituents.
  • the coking operation conducted in zone 2% may be of any desired type and can constitue, for example, a fluidized operation in which coke particles are maintained as a fluid bed in accordance with the principles of fluidized solids contacting. Residual oil introduced into coking zone 20 through line 21 undergoes conversion permitting removal of a product stream through line 22 including gases, intermediate liquid fractions, and unconverted residual fractions.
  • Coke can be withdrawn periodically from zone 20 through line 23.
  • the products of the coking process removed through line 22 are then introduced to a distillation zone 24.
  • the distillation may be either atmospheric or vacuum distillation but preferably constitutes vacuum distillation of the character referred to in connection with Fig. 1. successively higher boiling portions of the feed are removed from still 24 through lines 25, 26,. 27 and 28. Uncoverted portions of the residual stock originally fed to the coking process can be removed as a bottoms product through line 29 and can be recycled to the process.
  • a synthetic asphaltic material is introduced to distillation zone 24 through line 30 at a point somewhat below the side stream withdrawal of the highest boiling distillate product.
  • This distillate product will include heavy gas oil suitable for catalytic cracking.
  • the injected synthetic asphaltic material can be removed from the tower 24 through a lower side stream Withdrawal 31 or, alternatively, the asphaltic material may be permitted to remain in the bottoms product of the fractionator.
  • the process of Fig. 2 is a particularly valuable process for upgrading residual stocks to catalytic cracking feed material.
  • the coking step of the process serves to remove a-substantial portion of metal contaminants the coking feed stock. These metal contaminants are deposited on the coke solids employed and/or produced in the process; consequently, by using the process of this invention in combination with this effect, heavy gas oil feed stocks having extremely low content of metal contaminants can be obtained for catalytic cracking feed stoc
  • Fig. 3 fllustrates the application of this invention to a fractionator of the character employed in the so-called combination distillation cracking operation. As illustrated by Fig. 3, fractionation of catalytically cracked products can be carried out in the same distillation tower in which a crude oil is fractionated.
  • the terial can be removed from a lower total product from catalytic reactor "18 may bepassed through line 32 for introduction near the bottom portion of the fractionator 33.
  • Crude oil is brought into fractionator 33 at an intermediate portion of the tower through line 34.
  • Light boiling fractions of the catalytic cracking products rise upwardly in vapor form through the distillation zone, serving as an effective stripping agent for heavy portions of the crude oil.
  • other stripping gases may be brought into tower 33 through other side stream introduction points.
  • Such stripping agents can constitute light naphtha fractions derived from other refining processes, such as a reforming process.
  • the necessary heat input for the distillation operation is supplied by a reboiler circuit indicated by numeral 36.
  • Distillate products including fractions of both the crude oil and the catalytically cracked products are withdrawn from the tower through lines 37, 28, 39 and 49. Operation of still 33 can be adjusted so that the product withdrawn through line 40 will constitute a gas oil suitable for catalytic cracking.
  • the distillate products are processed to minimize the presence of metal contaminants by introduction of a synthetic asphaltic material of the character described through line 41. This mapoint in the tower through line 42 after contact with upflowing vapors or, alternatively, the synthetic asphaltic material may be permitted to pass downwardly through the tower for re moval with residual oil through line 43.
  • Fig. 3 The process of Fig. 3 is particularly attractive in providing a distillation process for segregating a heavy gas oil for catalytic cracking which can be conducted at atmospheric pressures.
  • the use of this invention as described in this figure is particularly attractive in providing heavy boiling gas oils of low metal content suitable for catalytic cracking.
  • this figure diagrammatically illustratesapplication of the invention to the distillation of the products of a coking operation when con-. ducted in combination with a cracking reaction.
  • a high boiling residual fraction of crude oil containing metal contaminants is introduced to a coking reactor 45 through line 46.
  • the coking process may be of the character identified in connection with Fig. 2.
  • the hydrocarbon products. of the coking process are removed through line 47 for introduction to a sembbing tower 48 which is essentially a distillation zone in which the total coke products which have been converted during coking are removed overhead through line 49.
  • catalytic cracking reactor 50 The products of catalytic cracking are then passed through line 5-1 to distillation tower 52.
  • Still 52 is preferably a vacuum distillation tower permitting segregation of light boiling products through lines 53, 54, 55 and 56 and segregation of a heavy catalytic tar through line 57.
  • This tar will constitute a synthetic asphaltic material which can be recycled through line 57 to scrubbing tower 48 for contact with the coke products. Portions of the residual stock originally fed to the coking zone together with the synthetic asphaltic material are removed from scrubbing tower 48 through line 58 for recycle to the coking operation.
  • Fig. 4 illustrates a process having the advantages of Fig. 2 by employing a combination of coking, catalytic cracking and fractionation.
  • the process of Fig. 4 provides an integrated process for production of a suitable extractive distillation refluxing agent and use of this agent to effectively upgrade residual stock for catalytic cracking.
  • Fig. 5 illustrates a somewhat different combination of distillation, coking and cracking.
  • Fractionation zone 66 of Fig. 5 is similar to fractionation zone 33 of Fig. 3: and constitutes a combination fractionator in which both crude oil and products of catalytic cracking are subjected to fractionation. in the Harboretillationzone.
  • a crude oil isintroduced' into distillation zone 60 through line 61 together with the total products of a catalytic cracking zone brought into the tower through line 62.
  • Distillate products of varying boiling ranges are withdrawn from tower 60 through Withdrawal lines 31, 82, 83, 84 and 85.
  • the product of line 85 may constitute a gas oil fraction adaptable for catalytic cracking.
  • synthetic asphaltic material is brought into tower 60 through line 66. Residual fractions are removed from distillation zone 60 through line 67 together'with the synthetic asphaltic material introduced to the tower.
  • Fig. 5 provides a combination of the processes of Figs. 2, 3 and 4 which provides an attractive application for the present invention.
  • a particular feature of the process of Fig. 5 is the manner in which a high molecular weight asphaltic material is essentially used in a two-stage contacting operation to eliminate metal contaminant content of a catalytic cracking feed. This occurs in combination with the elimination of metal contaminants achieved in a coking operation so the process is well adapted for providing the highest quality catalytic cracking feed stock.
  • distillation process is a vacuum distillation process.
  • a process as in claim 6 wherein the distillation process is an atmospheric distillation process.
  • distillation process is a high pressure distillation-stripping process.

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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)
US474477A 1954-12-10 1954-12-10 Extractive distillation operation for preparation of catalytic cracking feed stocks Expired - Lifetime US2777802A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
NL100147D NL100147C (enEXAMPLES) 1954-12-10
NL202701D NL202701A (enEXAMPLES) 1954-12-10
BE543301D BE543301A (enEXAMPLES) 1954-12-10
US474477A US2777802A (en) 1954-12-10 1954-12-10 Extractive distillation operation for preparation of catalytic cracking feed stocks
GB34143/55A GB782791A (en) 1954-12-10 1955-11-29 Improved extractive distillation operation for preparation of catalytic cracking feed stocks
FR1138469D FR1138469A (fr) 1954-12-10 1955-11-30 Préparation de charges de cracking catalytique
DEE11658A DE1035296B (de) 1954-12-10 1955-12-09 Verfahren zur Gewinnung von Beschickungen fuer die katalytische Crackung

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BE (1) BE543301A (enEXAMPLES)
DE (1) DE1035296B (enEXAMPLES)
FR (1) FR1138469A (enEXAMPLES)
GB (1) GB782791A (enEXAMPLES)
NL (2) NL202701A (enEXAMPLES)

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2884369A (en) * 1955-03-01 1959-04-28 Exxon Research Engineering Co Removal of metal contaminants from a hydrocarbon feed
US2901413A (en) * 1955-04-26 1959-08-25 Exxon Research Engineering Co Combination deasphalting, coking, and catalytic cracking process
US2906690A (en) * 1955-05-16 1959-09-29 Exxon Research Engineering Co Conversion of hydrocarbons
US2911353A (en) * 1955-11-08 1959-11-03 Exxon Research Engineering Co Treatment of a metal-contaminated heavy gas oil with non-adsorbent carbon particles
US2913395A (en) * 1957-03-04 1959-11-17 Union Oil Co Coking process
US2941928A (en) * 1957-04-17 1960-06-21 Standard Oil Co Coking apparatus for hydrocarbon oils
US2943995A (en) * 1958-04-15 1960-07-05 Sun Oil Co Two stage heavy oil coking process
US2956004A (en) * 1958-03-25 1960-10-11 Standard Oil Co Removing metal contaminants from feeds
US2963416A (en) * 1957-10-09 1960-12-06 Gen Carbon And Chemical Corp Coke production from petroleum stocks
US2963423A (en) * 1958-12-31 1960-12-06 Exxon Research Engineering Co Preparation of catalytic cracking feed stocks
US3065165A (en) * 1959-11-24 1962-11-20 Exxon Research Engineering Co Thermal cracking of hydrocarbons
US3085062A (en) * 1959-12-10 1963-04-09 Shell Oil Co Extractive distillation of lubricating oil stock
US3096273A (en) * 1960-08-05 1963-07-02 Kellogg M W Co Recovery of hydrocarbons
US3162593A (en) * 1962-03-21 1964-12-22 Tidewater Oil Company Fluid coking with cracking of more refractory oil in the transfer line
DE1209687B (de) * 1958-09-06 1966-01-27 Exxon Research Engineering Co Verfahren zum Entasphaltieren von aus oberhalb 480íµ siedenden Komponenten bestehenden Erdoelfraktionen
US3717569A (en) * 1971-01-22 1973-02-20 Standard Oil Co Method for increasing a refinery's capacity for processing metals-containing residual-type hydrocarbons
US4497705A (en) * 1983-08-17 1985-02-05 Exxon Research & Engineering Co. Fluid coking with solvent separation of recycle oil
US4528088A (en) * 1983-11-30 1985-07-09 Exxon Research And Engineering Co. Coking with solvent separation of recycle oil using coker naphtha and solvent recovery
US4530755A (en) * 1983-10-31 1985-07-23 Exxon Research And Engineering Co. Coking with solvent separation of recycle oil using coker naphtha
US4534854A (en) * 1983-08-17 1985-08-13 Exxon Research And Engineering Co. Delayed coking with solvent separation of recycle oil

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2219345A (en) * 1938-01-26 1940-10-29 Standard Oil Co Combination cracking
US2312445A (en) * 1940-05-13 1943-03-02 Robert F Ruthruff Catalytic combination process
US2334306A (en) * 1942-11-18 1943-11-16 Texas Co Cracking hydrocarbon oils
US2349603A (en) * 1943-07-02 1944-05-23 Texas Co Combination catalytic and thermal cracking
US2541795A (en) * 1947-06-18 1951-02-13 Sinclair Refining Co Catalytic cracking of hydrocarbons
US2644785A (en) * 1950-06-03 1953-07-07 Standard Oil Dev Co Combination crude distillation and cracking process

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2219345A (en) * 1938-01-26 1940-10-29 Standard Oil Co Combination cracking
US2312445A (en) * 1940-05-13 1943-03-02 Robert F Ruthruff Catalytic combination process
US2334306A (en) * 1942-11-18 1943-11-16 Texas Co Cracking hydrocarbon oils
US2349603A (en) * 1943-07-02 1944-05-23 Texas Co Combination catalytic and thermal cracking
US2541795A (en) * 1947-06-18 1951-02-13 Sinclair Refining Co Catalytic cracking of hydrocarbons
US2644785A (en) * 1950-06-03 1953-07-07 Standard Oil Dev Co Combination crude distillation and cracking process

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2884369A (en) * 1955-03-01 1959-04-28 Exxon Research Engineering Co Removal of metal contaminants from a hydrocarbon feed
US2901413A (en) * 1955-04-26 1959-08-25 Exxon Research Engineering Co Combination deasphalting, coking, and catalytic cracking process
US2906690A (en) * 1955-05-16 1959-09-29 Exxon Research Engineering Co Conversion of hydrocarbons
US2911353A (en) * 1955-11-08 1959-11-03 Exxon Research Engineering Co Treatment of a metal-contaminated heavy gas oil with non-adsorbent carbon particles
US2913395A (en) * 1957-03-04 1959-11-17 Union Oil Co Coking process
US2941928A (en) * 1957-04-17 1960-06-21 Standard Oil Co Coking apparatus for hydrocarbon oils
US2963416A (en) * 1957-10-09 1960-12-06 Gen Carbon And Chemical Corp Coke production from petroleum stocks
US2956004A (en) * 1958-03-25 1960-10-11 Standard Oil Co Removing metal contaminants from feeds
US2943995A (en) * 1958-04-15 1960-07-05 Sun Oil Co Two stage heavy oil coking process
DE1209687B (de) * 1958-09-06 1966-01-27 Exxon Research Engineering Co Verfahren zum Entasphaltieren von aus oberhalb 480íµ siedenden Komponenten bestehenden Erdoelfraktionen
US2963423A (en) * 1958-12-31 1960-12-06 Exxon Research Engineering Co Preparation of catalytic cracking feed stocks
US3065165A (en) * 1959-11-24 1962-11-20 Exxon Research Engineering Co Thermal cracking of hydrocarbons
US3085062A (en) * 1959-12-10 1963-04-09 Shell Oil Co Extractive distillation of lubricating oil stock
US3096273A (en) * 1960-08-05 1963-07-02 Kellogg M W Co Recovery of hydrocarbons
US3162593A (en) * 1962-03-21 1964-12-22 Tidewater Oil Company Fluid coking with cracking of more refractory oil in the transfer line
US3717569A (en) * 1971-01-22 1973-02-20 Standard Oil Co Method for increasing a refinery's capacity for processing metals-containing residual-type hydrocarbons
US4497705A (en) * 1983-08-17 1985-02-05 Exxon Research & Engineering Co. Fluid coking with solvent separation of recycle oil
US4534854A (en) * 1983-08-17 1985-08-13 Exxon Research And Engineering Co. Delayed coking with solvent separation of recycle oil
US4530755A (en) * 1983-10-31 1985-07-23 Exxon Research And Engineering Co. Coking with solvent separation of recycle oil using coker naphtha
US4528088A (en) * 1983-11-30 1985-07-09 Exxon Research And Engineering Co. Coking with solvent separation of recycle oil using coker naphtha and solvent recovery

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DE1035296B (de) 1958-07-31
FR1138469A (fr) 1957-06-14
NL202701A (enEXAMPLES)
GB782791A (en) 1957-09-11
NL100147C (enEXAMPLES)
BE543301A (enEXAMPLES)

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