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EP0072873A1 - Procédé de raffinage pour enrichissement du rendement de distillation du pétrole lourd - Google Patents

Procédé de raffinage pour enrichissement du rendement de distillation du pétrole lourd Download PDF

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Publication number
EP0072873A1
EP0072873A1 EP81106517A EP81106517A EP0072873A1 EP 0072873 A1 EP0072873 A1 EP 0072873A1 EP 81106517 A EP81106517 A EP 81106517A EP 81106517 A EP81106517 A EP 81106517A EP 0072873 A1 EP0072873 A1 EP 0072873A1
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EP
European Patent Office
Prior art keywords
feedstocks
refining process
heavy
oil
process according
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EP81106517A
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German (de)
English (en)
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EP0072873B1 (fr
Inventor
Kiyoshige Hayashi
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Individual
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Priority to DE8181106517T priority Critical patent/DE3173881D1/de
Priority to EP81106517A priority patent/EP0072873B1/fr
Priority to AT81106517T priority patent/ATE18253T1/de
Publication of EP0072873A1 publication Critical patent/EP0072873A1/fr
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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
    • 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
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides

Definitions

  • the present invention relates to a petroleum refining process for taking measures to increase products extracted from petroleum feedstocks by means of pyrolysis.
  • the heavy feedstocks include atmuspnenc or vacuum bottoms, more specifically vacuum distillation residue and further contain topped petroleum residue, atmospheric or vacuum bottoms, heavy hydrocarbon fractions obtained by being subjected to deasphalting or other preliminary treatments, whole crude oils or petroleum derived from coal, shale or tar sands, and tar sand's bitumen.
  • the heavy feedstocks are rich in coke precursors as represented by the typically high Conradson carbon residue content thereof.
  • the heavy feedstocks When such heavy feedstocks are exposed to high temperatures as in a catalytic refining process, a quantity of coke undesirably formed on catalyst surfaces is increased to suffer a lowering of catalytic activity, and therefore, the conventional catalytic refining process entails the disadvantage of false economy because periodic regeneration of catalyst is frequently required.
  • the heavy feedstocks contain a high percentage of heavy metals being principally vanadium and nickel which exist in the form of organometallic complexes. By metals, if in excess, are adversaly affected hydrodesulfurization, fluid ccatalytic cracking, heavy oil cracking, hydrocracking and the other various catalytic reactions.
  • the metals are deposited on the catalysts thereby reducing desirable catalytic activity and selectivity thereof.
  • the metals act as catalysts for dehydrogenation reaction and consequently, hydrogen and coke formations are increased at the expense of desired petroleum products.
  • the heavy feedstocks contain a large quantity of sulfur in petroleum in its condensed state in comparison with distillate such as gasoline, kerosene and gas oil.
  • the sulfur contained in the form of organosulfur complex by the heavy feedstocks is pyrolyzed into H 2 S, free sulfur, mercaptan and sulfide, and at the same time, polymerisation and condensation are repeatedly carried out to be gradually turned into extremely complex sulfur compound and further into polyaromatic sulfur complex.
  • the free sulfur thus formed by the pyrolytic functions as the leading role to repeatedly continue a radical reaction of petroleum analysis and polymerisation/condensation.
  • coke is increasingly formed due to the polymerisation/condensation and instead, the yield of liquid oil products is diminished and the coke thus forced is heavily redolent of creosote.
  • Coke precursors, heavy metals and suflur are comprehended in great quantities so-called asphaltenes constituting a component of asphaltic fraction in the heavy feedstocks (insoluble component of isopentano).
  • the asphaltenes in the feedstocks are dispersed in heavy quality oils in the form of colloidal solution and show fused aromatic ring constructions with a very large molecules.
  • the asphaltenes have a property of tending to cause further polymerisation/condensation reactions only by being subjected to heat treatment in a distillation process of oil refining and bring about cohesion.
  • any conventional measure comprises turning asphaltene in the feedstocks, which have been soluble on colloidal dis- person, into insoluble solid asphaltic fractions in such a manner that they are put on catalyst surfaces at a first stage and heated at the reaction temperature between 400°C and 510°C thereby to segregate and remove the fractions along with the catalysts from the feedstocks, and thereafter, subjecting the fractions thus segregated to hydrogenation reaction, hydrocracking reaction, fluid catalytic reaction and so on by using other catalysts at a second stage.
  • the characteristic clincher for a novel techique of a refining process resides what catalysts are used for adhering thereto and removing solid asphaltic fractions at the first stage.
  • the catalysts adopted at the first stage are generally used in a hydrogen current, and among them those sufferring a lowering of activity to remove the solid asphaltic fractions from the feedstocks are burnt with air and regenerated to recycle.
  • oxide and hydroxide in alkaline earth metals do not eat steel even at the high temperature in the range of from 400°C to 1000°C, and besides, even when they are exposed to great quantities of vapour at the foregoing temperature.
  • Oxide and hydroxide in alkaline metals are soluble in water and easy to be ionized, and on the other hand, only a small amount thereof can be dissolved in water even if dissolved and they has a little tendency toward ionization. There is a great difference between the alkaline metals and the alkaline earth metals though they fall under the category of basic compounds.
  • the inventor has been made a study of a petroleum refining process by using chemicals such as CaO and Ca(OH) 2 which do not eat steel even at a high temperature. As a result, the following has been found.
  • An object of the present invention is to provide a petroleum refining process for reducing the yield of coke and consequently, increasing the yield of middle oil, particularly distillation oil of good quality in pyrolyzing process for heavy quality oil.
  • Another object of the present invention is to remove various metals, particularly vanadium and nickel, which are contained in heavy feedstocks and have an effect of accelerating formation of solid asphaltic fractions.
  • Still another object of the present invention is to suppress appearence of hannful effect of increasing solid asphaltic fractions.
  • Still another object of the present invention is to increase the yield of refining distillates by condensing vanadium, nickel and sulfur to solid bodies and segregating the solid bodies from coke.
  • a petroleum refining process for increasing the yield of products extracted from heavy petroleum feedstocks by means of pyrolysis which is carried out by heating in a presence of vapour at the temperature in the range of from 350°C to 550°C a mixture which are obtained by uniformly adding oxides in alkaline earth metals or hydroxides, such as powdered CaO and Ca(OH) 2 or slurry dispersed in water to heavy petroleum feedstocks.
  • the single figure is a schematically explanatory diagram of one embodiment of a petroleum refining device according to the present invention.
  • the present invention relates to a petroleum refining process comprising staying, in a presence of vapour, a mixture which is obtained by adding 0.1 to 5 weight % of chemicals such as CaO and Ca(OH) 2 to 100 weight % of heavy petroleum feedstocks selected as raw materials while being heated at the final temperature in the range of from 400°C to 550°C thereby to cause a small amount of solid asphaltic fraction to be precipitated along with CaO and Ca(OH) 2 , permitting heavy metals to act upon CaO and Ca(UH) 2 thereby to be precipitated while the soild asphaltic fractions are precipitated, and also permitting H 2 S and free sulfur formed at the same temperature in the same reaction time to be precipitated as a result of a reaction on CaO and Ca(OH) 2 , whereby petroleum intermediates and final products of good quality which contain neither solid asphaltic fraction nor heavy metal can economically be produced with the increased yield due to the coprecipitation of the solid asphaltic fractions, heavy metals and free sulfur.
  • chemicals such as CaO and Ca(OH
  • One of the importances of the present invention consists in a point tnat the solid asphaltic fractions, so-called "coke", formed by heating the heavy petroleum feedstocks at the temperature in the ranee ui from 400°C to 550°C is sharply reduced at length due to the reaction in a presence of the mixture of CaO and Ca(OH) 2 and vapour, and instead, the yield of liquid petroleum fractions, more particularly gas oil fraction is increased.
  • Heavy petroleum feedstocks are different in their components with a kind of the raw materials and contain solid asphaltic fraction which are turned to coke due to heat treatment at the temperature higher than 400°C.
  • the amount of solid asphaltic fractions in vacum residue is larger than that in atmospheric residue. Therefore, crude oil containing a high percentage of vacuum residue, for example, Daqing crude petroleum and Minus crude petroleum confronts a troublesome problem of the increased coke formation in petroleum refining in comparison with Middle Eastern crude petroleum and inevitably increases the prices of final products.
  • Canadian and Venezuelan tar sand bitumens will bring about far more troublesome problem from the standpoint of refining cost because vanadium and nickel contents thereof are extremely high.
  • the content of solid asphaltic fraction depends upon those of Conradson carbon residue and asphaltene, so that the solid asphaltic fractions are increased with the contents of Conradson carbon residue and asphaltene with the result that the yield of coke formed therefrom is increased. Also, ash and metal components constitute solid asphaltic fractions thereby increasing coke formation thus involved. Vanadium and nickel have an effect to accelerate dehydrogenation of petroleum hydrocarbon and consequently, the yield of carbonous matter is increased. When the least amounts of active carbon, activated alumina, silica gel, activated clay and acidic clay are added as addition compounds into the heavy feedstocks and the feedstocks with the addition compounds are heated, the reac- .
  • the catalyst including zeolite, alumina, silica gel, etc.
  • the formation of the solid asphaltic fractions is also accelerated by various metals such as vanadium and nickel, in the heavy feedstocks. Sulfur compounds are harmful more than metals. This is because as already mentioned above, bridging and polymerisation/condensation of tarry matter being heavy feedstocks, particularly hydrocarbon having a high boiling point are hastened due to free sulfur which is inevitably yielded in an instance by pyrolyzing sulfur compounds to form an extremely increased amount of coke.
  • the petroleum refining process according to the present invention entails a superior effect of heat treatment and thermal cracking by use of chemicals such as CaO and Ca(OH) 2 .
  • the reaction of CaO and Ca(OH) 2 necessitates coexistence of moisture, preferably steam.
  • Despit vacuum residue of Daqing crude petro- leu:.: without an addition compound can be conveyed in 1.5 kg/min at 50°C through pipelines by use of a pump having a fixed horsepower, residue with 1 to 3 % CaC can be conveyed in 2.0 to 2.1 kg/min under the same condition thereby carrying out transportation of oil ecconomically
  • the feature of the refining process according to the present invention is to maintain heavy feedstocks under the condition of strongly basic surface activation of Ca-ion at the temperature in the range of from 350°C to 550°C.
  • the amount of gas yielded by subjecting heavy feedstocks with an addition compounds of CaO and Ca(OM) 2 to heat treatment at the temperature in the range of from 400°C to 550°C under coexis- tance of water or steam is somewhat more than that in case of feedstocks without addition compound.
  • the component such as tar sand bitumen which contains a high percentage of metals such as vanadium and nickel is so treated that it reacts upon Ca-ion to be turned into a solid in a separatably form from liquid oil together with solid asphaltic fraction.
  • the chemicals of strongly basic alkalin earth compounds such as CaO and Ca(OH) 2 to be used for heavy feedstocks at the temperature in the range of from 400°C to 550°C in the petroleum refining process according to the present invention has satisfactory property of strongly basic surface activation of Ca-ion at the temperature in the range of from 400°C to 500°C.
  • the most of the characteristic features of the proseht invention consists in an increased yield of gas oil fraction as refining distillate and a reduction of coke formation.
  • the present invention aims at a continuous increase yield of middle oil, particularly gas oil, from heavy feedstocks as raw material by use of chemicals such as CaO and Ca(OH)2 But the increased yield of the middle oil is not accomplished only by desulfurization due to CaO and Ca(OH) 2 and solidification of metals such as vanadium and nickel. It is attained under coexistence of CaO and Ca(OH) 2 and water or steam and entails a large reduction of coke formation thus involved.
  • the additional interest of the present invention lies in that the yield of gas is slightly increased. It is unexpected that the yield of gas is increased, despite that of coke is reduced.
  • H 2 and C 3 - C 4 hydrocarbon are ascertained to be reduced and methane to be increased.
  • thermal cracking for taking measures to increase C 3 - 4 gaseous hydrocarbon and gasolinic hydrocarbon is preferentially carried out.
  • the thermal cracking is further promoted due to sulfur, metals and carbon. It is, however, anticipated that the thermal cracking being promoted due to sulfur, metals and carbon is suppressed when CaO and Ca(OH) 2 exist together, and in the meantime, the thermal cracking by which analysis is stopped is preferentially carried out when interrupted due to gas oil of high molecular weight and high boiling point.
  • heavy feedstocks of petroleum are not soiled by metals such as vanadium and nickel, sulfur, oxygen compounds and nitrogen compounds.
  • the yield of distillation fraction of widdle oil, particularly gas oil is to be increased at the temperature in the range of from 400°C to 550°C.
  • Solids of carboneus matters such as active carbon and soiled mesocarbon readily absorbs oxygen compounds on its surface and is soiled by metals, sulfur, oxygen compound and nitorgen compound, thereby reducing the yield of middle oil, particularly gas oil.
  • Heavy feedstocks 1 are inhaled by a pump 4 and mixed with slurry of milk of lime discharged from a vessel 2 by means of a pump 3, and the mixture thus obtained is forwarded into a heater 6 via a heat exchanger 5 and heated in the heater 6 while constantly keeping the output temperature at the desired temperature in the range of from 400°C to 550 °C. Thereafter, the mixture is fed into one of surge drums 7 and 8, thereby accumulating solid asphaltic fractions on the bottom of the surge drum.
  • Two surge drums are alternatively used so that, where the yield of the solid asphaltic fractions collected in one of surge drums reaches a certain quantity, a supply of the feedstocks to the one surge drum is discontinued and at the same time, the feedstocks begins to be supplied to the other surge drum.
  • the rest surge drum is purged with steam to remove- oil and gas collected therein
  • manhole covers disposed on the top and bottom of the rest surge drum are opened, and tnen, a hard solid body formed in the drum is quarried out by virtue of high pressure water being injected inside the drum tnrough the upper manhole thereof by means of a water jet cutter and the solid asphaltic fractions 10 is discharged through the lower manhole.
  • Each surge drum is provided on its lower portion with a steam blowing nozzle 9.
  • Steam to be injected inside the surge drum from the nozzle 9 contributes to mixing sufficiently the heavy feedstocks fed into the surge drum with Ca(OH) 2 to maintain the condition of strongly basic surface activiation of Ca-ion at an arbitrary temperatures in the range of from 400°C to 550 0 C, and to accelerating the reaction to solidify metals, sulfur, etc. while minimizing solid asphaltic fractions.
  • An oil inlet port may be disposed on any portion of the top, the side wall and the bottom of the surge drum. It is preferable to mount the oil inlet port between the top and the side wall thereof when the reaction temperature is relatively low.
  • the time for which heavy feedstocks is stayed at the surge drum may be controlled on the basis of the amount of steam supplied.
  • a foamed body yielded in the surge drum overflows and is fed into a distilling column 11 while solid asphaltic fractions and its pre- curson are fed thereinto.
  • a purpose to obtain a desired petroleum product by oil refining and a kind of raw materials enable determination on wheter solid asphaltic fractions is subjected to a segregation treatment in a settler 18 to obtain slurry-like fuel oil 20, or whether the feedstocks are to be recycled via a pipeline 21, in order to recover gas 14, gasoline 15 from the top of the distilling column 11, kerosine 16, gas oil 17 from the side portion thereof and clarified fuel oil 19 from the bottom thereof.
  • the yields of gas and gasoline are reduced, and at a higher temperature, the yield of coke is increased though a faster reaction is caused.
  • it is suitable to maintain the interior of the surge drum at a lower tempera- t ure , preferably in the range of from 400°C to 500°C so as to increase the yield of distillate such as middle oil and gas oil of good quality, which is adapted to reduce the yield of coke and gas.
  • middle oil of good quality (kerosine 16 and gas oil 17) from raw material for hydrocracking and FCC, therefore, recycling the majority of percipitate oil on the bottom of the distilling column through the pipeline 21 so as not to collect fuel oil 19. It may be attempted that the yield of the distillate thus obtained is increased so that gas oil having a high boiling point by returning settler 18 to a rcboiler (combined with a second heater) and the fuel oil 19 to the distilling column 11.
  • Residual substance of atmospheric distillate (mixed Middle Dastern crude petroleum) of specific gravity of 0.9429 (15/4°C), 2.6 weight % of sulfur content, 5 g/100g of bromine value, and the composition (by elution chromatography) of 50.0% mixed paraffin and olefine hydrocarbons, 45.6% mixed aromatic hydrocarbon and diene synthesis, 1.6% resin and 2.8% the others, and showing initial boiling point (IBP) at 225°C, 10% at 340°C, 20% at 375°C, 30% at 470°C by ASTM distillation test was used as raw material.
  • IBP initial boiling point
  • the raw material was fed into a pressure vessel at the temperature of from 450°C to 470°C and the pressure of 5kg/cm 2 -gauge and subjected to a coking treatment for 20 hours with the result that a product consisting of 28.2 weight % of cracked gas, 25,2 weight % of mixed coke and cracked oil; whose distillate is of 36.4 weight % below 250°C, 10.2 wreight % at 250 - 350°C, namely, 46.6 weight % of coked extract oil in all total were yielded.
  • the distillate below 250°C is of specific gravity of 0.7756(15/4°C), and consists of 0.50 weight % of sulfur content, 17.7 weight % of aromatic hydrocarbon, 26.1 weight % of olefine hydrocabon, 56.1 wheight % of saturation hydrocarbon, and shows IBP at 60°C, 10% at 108°C, 20% at 129°C, 50% at 175°C.
  • coking treatment was carried out in the same condition as described above except that 3 weight % of calcium hydroxide having particle size less than 100 mesh, preferably 4 - 8 ⁇ m, is added in the form of water slurry to the raw material with the result tnat a product consisting of 13.3 weight % of cracked gas, 12.0 weight % of coke and cracked oil of 13.2 weight % distillation below 250°C, 22.3 weight % at 250 ° C to 350 °C, 39.2 weight % above 350°C, namely, 74.7 weight % of coked distillation oil in all total was yielded.
  • the distillation below 250°C is of specific gravity of 0.753 (15/4°C), and consists of 0.56 weight % of sulfur content, and the composition (by elution chromatograph) of 42.4% aromatic hydrocarbon, 4.8 % olefine hydrocarbon, 52.8% saturation hydrocarbon; whose distillation at 250°C - 350°C is of specific gravity of 0.871 (15/4°C) and 25.6 g/lOOg of bromine value, and consists of 1.63 weight % of sulfur content, and whose distillation above 350°C is of specific gravity of 0.941 (15/4°C) and 8 g/100g of bromine value and consists of 2.37 weight % of sulfur content; and coke was of 1.86 weight % of sulfur content.
  • Tables 2, 3 and 4 are set out the results of experiments which were carried out by use of heavy feedstocks represented in Table 1 in conformity with the operating sequence illustrated in the accompanying flow sheet under such a condition that the surge drum is maintained at the temperature of from 490°C to 530°C to confirm the effect of addition of CaO having particle size less than 100 mesh, preferably 4 - 8 ⁇ m in its average size.
  • the addition of CaO contributes to increasing the yield of light oil (gas oil) by a large quantity and further to solidifying, within coke, sulfur contained by the feedstocks.
  • combustible sulfur is obtained by subjecting SO 2 which is obtained by burning the coke containing sulfur at 800 C, to a quantitation analysis
  • solidified sulfur is obtained by subjecting S0 3 which is obtained by burning the coke at 1500°C, to a quantitation analysis.
  • the sum content of the combustible sulfur and solidified sulfur is represented as 100 per cent, in Tables.
  • sulfur is appearently, remarkably solidified. This is extremely important for a refining process. When the yielded coke is burnt to be gasfied or used as fuel, it does not generate sulfur compounds at the temperature below 800°C, and thereby gas thus exhausted is clean.

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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)
EP81106517A 1981-08-21 1981-08-21 Procédé de raffinage pour enrichissement du rendement de distillation du pétrole lourd Expired EP0072873B1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
DE8181106517T DE3173881D1 (en) 1981-08-21 1981-08-21 Refining process for producing increased yield of distillation from heavy petroleum feedstocks
EP81106517A EP0072873B1 (fr) 1981-08-21 1981-08-21 Procédé de raffinage pour enrichissement du rendement de distillation du pétrole lourd
AT81106517T ATE18253T1 (de) 1981-08-21 1981-08-21 Raffinationsprozess zur ausbeutesteigerung von destillaten aus schweren erdoeleinsaetzen.

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Application Number Priority Date Filing Date Title
EP81106517A EP0072873B1 (fr) 1981-08-21 1981-08-21 Procédé de raffinage pour enrichissement du rendement de distillation du pétrole lourd

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EP0072873A1 true EP0072873A1 (fr) 1983-03-02
EP0072873B1 EP0072873B1 (fr) 1986-02-26

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AT (1) ATE18253T1 (fr)
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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2141379C1 (ru) * 1996-04-23 1999-11-20 Российский государственный университет нефти и газа им.И.М.Губкина Катализатор для пиролиза углеводородного сырья
WO2013019335A1 (fr) * 2011-07-29 2013-02-07 Saudi Arabian Oil Company Procédé de cokéfaction retardée utilisant des matières adsorbantes
US11427782B2 (en) 2018-07-20 2022-08-30 Neste Oyj Purification of recycled and renewable organic material
US11499104B2 (en) 2018-07-20 2022-11-15 Neste Oyj Purification of recycled and renewable organic material
US11624030B2 (en) 2018-07-20 2023-04-11 Neste Oyj Production of hydrocarbons from recycled or renewable organic material
US11655422B2 (en) 2018-07-20 2023-05-23 Neste Oyj Purification of recycled and renewable organic material
US11981869B2 (en) 2018-07-20 2024-05-14 Neste Oyj Purification of recycled and renewable organic material

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2001291563A1 (en) 2000-09-18 2002-04-02 Ensyn Group, Inc. Products produced from rapid thermal processing of heavy hydrocarbon feedstocks
US7572365B2 (en) 2002-10-11 2009-08-11 Ivanhoe Energy, Inc. Modified thermal processing of heavy hydrocarbon feedstocks
US7572362B2 (en) 2002-10-11 2009-08-11 Ivanhoe Energy, Inc. Modified thermal processing of heavy hydrocarbon feedstocks
US9707532B1 (en) 2013-03-04 2017-07-18 Ivanhoe Htl Petroleum Ltd. HTL reactor geometry

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3707462A (en) * 1970-01-27 1972-12-26 Exxon Research Engineering Co Conversion of heavy petroleum feedstocks
US3707459A (en) * 1970-04-17 1972-12-26 Exxon Research Engineering Co Cracking hydrocarbon residua
GB1307543A (en) * 1970-05-21 1973-02-21 Exxon Research Engineering Co Thermal cracking process
GB1576720A (en) * 1975-12-19 1980-10-15 Standard Oil Co Catalytic cracking with reduced emission of noxious gases

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3707462A (en) * 1970-01-27 1972-12-26 Exxon Research Engineering Co Conversion of heavy petroleum feedstocks
US3707459A (en) * 1970-04-17 1972-12-26 Exxon Research Engineering Co Cracking hydrocarbon residua
GB1307543A (en) * 1970-05-21 1973-02-21 Exxon Research Engineering Co Thermal cracking process
GB1576720A (en) * 1975-12-19 1980-10-15 Standard Oil Co Catalytic cracking with reduced emission of noxious gases

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2141379C1 (ru) * 1996-04-23 1999-11-20 Российский государственный университет нефти и газа им.И.М.Губкина Катализатор для пиролиза углеводородного сырья
WO2013019335A1 (fr) * 2011-07-29 2013-02-07 Saudi Arabian Oil Company Procédé de cokéfaction retardée utilisant des matières adsorbantes
JP2014523955A (ja) * 2011-07-29 2014-09-18 サウジ アラビアン オイル カンパニー 吸着材を用いるディレードコークス化プロセス
US9023192B2 (en) 2011-07-29 2015-05-05 Saudi Arabian Oil Company Delayed coking process utilizing adsorbent materials
US11427782B2 (en) 2018-07-20 2022-08-30 Neste Oyj Purification of recycled and renewable organic material
US11499104B2 (en) 2018-07-20 2022-11-15 Neste Oyj Purification of recycled and renewable organic material
US11624030B2 (en) 2018-07-20 2023-04-11 Neste Oyj Production of hydrocarbons from recycled or renewable organic material
US11655422B2 (en) 2018-07-20 2023-05-23 Neste Oyj Purification of recycled and renewable organic material
US11981869B2 (en) 2018-07-20 2024-05-14 Neste Oyj Purification of recycled and renewable organic material

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Publication number Publication date
DE3173881D1 (en) 1986-04-03
ATE18253T1 (de) 1986-03-15
EP0072873B1 (fr) 1986-02-26

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