EP0072873B1 - 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
EP0072873B1
EP0072873B1 EP81106517A EP81106517A EP0072873B1 EP 0072873 B1 EP0072873 B1 EP 0072873B1 EP 81106517 A EP81106517 A EP 81106517A EP 81106517 A EP81106517 A EP 81106517A EP 0072873 B1 EP0072873 B1 EP 0072873B1
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Prior art keywords
feedstocks
refining process
heavy
process according
alkaline earth
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German (de)
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EP0072873A1 (fr
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Kiyoshige Hayashi
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Priority to AT81106517T priority patent/ATE18253T1/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
    • 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 process for refining petroleum and the like by pyrolysing heavy feedstocks.
  • Heavy petroleum feedstocks are usually subjected to thermal cracking processes such as visbreaking, delayed coking and fluid coking and to catalytic processes such as hydrodesulfurization, hydrocatalytic cracking and fluid catalytic cracking, in order to produce intermediate or final products. Catalytic processes in particular give rise to troublesome difficulties.
  • the heavy feedstocks include crude oil or petroleum derived from coal, shale or tar sands and tar sand bitumen and may contain vacuum-distillation residues, topped petroleum residues, atmospheric or vacuum bottoms and heavy hydrocarbon fractions as a result of deasphalting or other preliminary treatment.
  • the heavy feedstocks may be rich in coke precursors, as is shown by the Conradson carbon-residue test.
  • Heavy petroleum feedstocks differ in composition and contain solid asphaltic fractions which are converted into coke upon heat treatment at temperatures higher than 400°C.
  • the amount of solid asphaltic fractions in vacuum residues is larger than in atmospheric residues.
  • crude oil containing a high percentage of vacuum residue for example Daqing crude petroleum and Minus crude petroleum, presents a greater problem of coke formation in refining, inevitably leading to an increase of the price of the final products, than does Middle East petroleum.
  • Canadian and Venezuelan tar sand bitumens also present the problem of high refining cost, because of their high vanadium and nickel contents. Ash and metal components of solid asphaltic fractions increase the coke formation.
  • the heavy feedstocks contain heavy metals, in particular vanadium and nickel in the form of organometallic complexes.
  • the metals are deposited on the catalysts and, in excess amounts, reduce the desirable catalytic activity and selectivity thereof, so that the hydrodesulfurization, fluid catalytic cracking, heavy oil cracking, hydrocracking and other catalytic reactions are adversely affected.
  • the metals act as catalysts for a dehydrogenation reaction, so that the formation of hydrogen and coke is promoted with resultant lower yield of desired petroleum products.
  • the heavy feedstocks In comparison with distillates such as petrol, kerosene and gas oil, the heavy feedstocks contain a large quantity of sulfur in the form of organosulfur complexes.
  • the organosulfur complexes are pyrolysed to H 2 S, free sulfur, mercaptans and sulfides, whilst polymerization and condensation reactions with formation of complex sulfur compounds and polyaromatic sulfur complexes occurs at the same time.
  • the free sulfur formed promotes petroleum breakdown and polymerization/condensation by radical reactions. As a result of polymerization/condensation, coke is formed in increasing amounts and the yield of liquid oil products is diminished, the coke thus formed smelling heavily of creosote.
  • Coke precursors, heavy metals and sulfur are contained in large quantities in asphaltenes forming an isopentane-insoluble component of the asphaltic fraction of the heavy feedstock.
  • the asphaltenes in the feedstock have very large molecules with fused aromatic ring structures and are dispersed in heavy oils in the form of a colloidal solution.
  • the asphaltenes tend to cause further polymerization/condensation reactions, forming cohesive product molecules.
  • the catalyst which may include zeolite, alumina, silica gel etc., used in the first stage acts as an accelerator for the formation of the solid asphaltic fractions.
  • 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 more harmful than metals, because of the above-mentioned polymerization/condensation reactions forming tarry matter. Hydrocarbons having high boiling points, in particular, are converted to coke by free sulfur, which is inevitably formed in the pyrolysis of sulfur compounds. Even when the reaction is carried out in the presence of hydrogen, the harmful action of sulfur is not to be neglected.
  • alkali metal hydroxides and carbonates such as NaOH, Na 2 C0 3 and the like attack steel at temperatures above 400°C.
  • oxides and hydroxides of alkaline earth metals do not attack steel even at the high temperatures in the range of 400°C to 1000°C at which they are exposed to great quantities of steam at the same temperatures.
  • the oxides and hydroxides of alkali metals are soluble in water and easily ionized, whereas only small amounts of alkaline earth metals can be dissolved in water and they have little tendency to ionize in solution. thus, there is a difference between the alkali metals and the alkaline earth metals, although they are all basic compounds.
  • the document US-A-3,707,462 describes a method of converting a sulfur-containing heavy' petroleum feedstock by passing the feedstock into a first bed of fluidized particles containing calcium oxide or a precursor thereof at a temperature between 500°C and 600°C to convert the feedstock to vapours of reduced sulfur content and to carbonaceous material of increased sulfur content which deposits on the particles, recovering the vapours from the first bed and transferring particles from the first bed to a second bed in which the particles are fluidized at a temperature of 800°C to 1000°C in a gas containing oxygen to remove the carbonaceous deposits on the particles at least partially and to react at least some of the sulfur present in the carbonaceous deposits with the calcium oxide to form calcium sulfide, recovering the gases from the second bed, transferring some of the particles from the second bed to the first bed and transferring particles from the second bed to a lower zone of a third bed in which the particles are fluidized at a temperature of 1000°C to 1100°C in an oxygen-containing gas, whereby at least
  • the document US-A-3,707,459 describes a process for the thermal treatment of a hydrocarbon residue feed having Conradson carbon numbers between 5 and 40 by heating the residue under a pressure sufficient to maintain the residue in the liquid phase and at a temperature between 371°C and 482°C in the presence of a free radical acceptor such as an acyclic hydrocarbon and/or a mild alkali using one or more , stages.
  • a free radical acceptor such as an acyclic hydrocarbon and/or a mild alkali using one or more , stages.
  • the free radical acceptor in the form of a solid may be slurried with the hydrocarbon feed.
  • the alkaline material may be any mild alkali such as sodium carbonate etc., although calcium oxide is preferred.
  • the above object is achieved by a process for refining petroleum and the like by pyrolysing heavy feedstocks which includes pre-heating the feedstocks mixed together with alkaline earth metal oxides or hydroxides or an aqueous slurry thereof, maintaining the pre-heated feedstocks in a soaking drum for 1 second to 30 minutes at a temperature of 350°C to 550°C and a pressure of 98 to 196 kPa-gauge in the presence of water or steam, and then continuously segregating gas and residue from the feedstocks in a distilling column while precipitating and solidifying asphaltenes, heavy metals and sulfur whilst maintaining strongly basic conditions by the presence of alkaline earth metal ions.
  • alkaline earth metal oxides or hydroxides such as powdered CaO and Ca(OH) 2 or a water-dispersed slurry thereof
  • the yield of products extracted from the heavy petroleum feedstocks is increased.
  • an increase of the amount of solid asphaltic fractions is suppressed and vanadium, nickel and sulfur are deposited in the form of solid bodies which may be removed from the coke.
  • a mixture obtained by adding to heavy petroleum feedstocks, selected as raw materials, 0.1 to 5% by weight, based on the amount of heavy petroleum feedstocks, of alkaline earth oxides or hydroxides such as CaO and Ca(OH) z is heated and maintained in the presence of vapour at a temperature in the range of 400°C to 550°C, thus causing only a small amount of solid asphaltic fraction to be precipitated and permitting heavy metals as well as H z S and free sulfur formed at the same temperature within the same reaction time to react with the alkaline earth oxide or hydroxide and to be precipitated.
  • petroleum intermediates and final products of good quality which contain neither solid asphaltic fractions nor heavy metals can be produced economically with increased yield, particularly of the gas oil fraction.
  • the reaction of CaO and Ca(OH) 2 necessitates the presence of moisture, preferably steam.
  • the presence of steam remarkably reduced the yield of coke, so that the amount of extracted oils, mainly kerosene and gas oil fractions, increased by about 12 to 15%.
  • the required amount thereof is at least 3-8 times and at most 10-30 times the amount of CaO and Ca(OH) 2 .
  • No foaming of the feedstock occurs at temperatures in the range of 200°C to 550°C when only CaO or Ca(OH) 2 are mixed with the feedstock.
  • foaming of the mixtures occurs; the extent of foaming depending upon the kind of crude petroleum.
  • a vacuum residue of Daqing crude petroleum foams far more strongly than an atmospheric residue of Minus crude petroleum.
  • the foaming is caused by the strongly basic surface-active effect of CaO and Ca(OH) 2 in the presence of water or steam which reduces the viscosity and interfacial tension of the heavy feedstocks mixed with 1 to 3% of water.
  • heavy feedstocks are maintained at a temperature in the range of 350°C to 550°C in the presence of strongly basic surface-active ions such as Ca-ions, the presence of water being necessary.
  • the amount of gas yielded by subjecting the heavy feedstocks with added CaO or Ca(OH) 2 to heat treatment at a temperature in the range of 440°C to 550°C in presence of water or steam is somewhat more than in the case of feedstocks without additives.
  • the vacuum residue of Murban/Oman crude petroleum is treated at 530°C, 60 to 66 I/kg of gas are produced in presence of 3% Ca(OH) z , whereas only 50 to 52 I/kg of gas are yielded without the additive.
  • the components of cracked gas are 6 mol % of hydrogen, 29 mol % of methane and 11.0 mol % of C 3 -hydrocarbon, whereas without the additive the components are 8 mol % of hydrogen, 25 mol % of methane and 13.3 mol % of C 3 -hydrocarbon.
  • vacuum residue of Daqing crude petroleum is treated at 530°C, 37 to 44 1/kg of gas are yielded using 3% of Ca(OH) 2 as additive and when it is treated at 490°C, 20 to 24 I/kg of gas are yielded using 1 % of Ca(OH) z , whereas 16 to 23 I/kg of gas are yielded without the additive.
  • Components such as tar sand bitumen, which contain a high percentage of metals such as vanadium and nickel, react with the calcium ions and form a solid which is separable together with the solid asphaltic fraction from the liquid oil.
  • the metal ions of the basic alkaline earth compounds used in accordance with the present invention provide a strongly basic surface-active effect at temperatures in the range of 400°C to 550°C.
  • middle oil particularly gas oil
  • the increased yield of middle oil, particularly gas oil, aimed at by the present invention results not only from the desulfurization of the feedstocks and the depositing of metals such as vanadium and nickel caused by the alkaline earth compound, but also from the joint presence of the alkaline earth compound and water or steam.
  • thermal cracking which increases the amounts of C 3 to C 4 gaseous hydrocarbons and gasolinic hydrocarbons preferentially occurs.
  • the thermal cracking is further promoted by sulfur, metals and carbon. It is to be expected that this promotion will not take place in the presence of the alkaline earth metals, whereas thermal cracking which increases the amounts of gasolinic hydrocarbons will occur preferentially.
  • the yield of the distillation fraction of middle oil, particularly gasoline oil from extremely pure heavy feedstocks which are not contaminated by metals such as vanadium and nickel and by sulfur, oxygen compounds and nitrogen compounds is greater at a temperature in the range of from 400°C to 550°C.
  • Carbonaceous solids such as active carbon and solid mesocarbon readily absorb oxygen compounds on their surfaces and are contaminated by metals, sulfur, oxygen compounds and nitrogen compounds, thus reducing the yield of middle oil, particularly gas oil.
  • synthetic zeolite is used in practice for the catalytic cracking to produce gas oil.
  • a refining process carried out at temperatures in the range of 400°C to 550°C using chemicals such as CaO or Ca(OH) 2 and a certain quantity of water or steam may be used with any kind of heavy feedstock as raw material.
  • "Unclear pyrolysis” which brings about a remarkable reduction in the yield of middle oil, particularly gas oil, is thereby suppressed.
  • the pyrolysis of heavy feedstocks is kept in a clear condition.
  • the present invention is further illustrated with the aid of the Figure showing a flow sheet for the pyrolysis of heavy feedstocks.
  • a heavy feedstock 1 is mixed with a slurry of milk of lime supplied from a vessel 2 by means of a pump 3 whilst being conveyed into a heater 6 via a heat exchanger 5.
  • the mixture is heated in the heater 6, keeping the output temperature constant in the range of 400°C to 550°C.
  • the mixture is fed into one of two surge drums 7 and 8 which are used as soaking drums. Solid asphaltic fractions are accumulated on the bottom of the surge drum 7 or 8.
  • the two surge drums 7 and 8 are used alternately, so that when a certain quantity of solid asphaltic fractions has collected in the surge drum 7, the supply of the feedstock to the surge drum 7 may be discontinued and at the same time the feedstock may be supplied to the other surge drum 8, whilst the surge drum 7 is purged with steam to remove oil and gas collected therein. Covers disposed on the top and at the bottom of the surge drum 7 are opened, the hard solid body formed in the surge drum 7 is removed with a high pressure water jet injected through the upper opening and the solid asphaltic fraction 10 is discharged through the lower opening. Each of the surge drums 7 and 8 is provided at its lower.portion with a steam blowing nozzle 9.
  • the steam which is injected into the surge drum 7 or 8 from the nozzle 9 serves to mix the heavy feedstock with Ca(OH) z , so that calcium ions may be formed on the'surface of the Ca(OH) 2 and strong basic surface activity may be maintained at a temperature in the range of 350°C to 550°C.
  • the steam also serves to accelerate the deposition of metals, sulfur etc. in solid form, whilst minimizing the formation of solid asphaltic fractions 10.
  • An oil inlet port may be disposed on any portion of the top, side wall or bottom of the surge drums 7 and 8. It is preferable to mount the oil inlet port between the top and the side wall of each surge drum 7 and 8 for relatively low reaction temperatures.
  • the position of the oil inlet port is determined by the quality and quantity of the solid asphaltic fractions deposited within and adhering to the surge drums 7 or 8.
  • the residence time of the heavy feedstock in the surge drum 7 or 8 may be controlled on the basis of the amount of steam supplied. When a large amount of steam is supplied or a specific raw material is used, the foam formed in the surge drum 7 or 8 overflows and is fed into a distilling column 11, while solid asphaltic fractions and their precursors are fed therein.
  • the kind of raw materials and the desired petroleum product determine whether solid asphaltic fractions are subjected to segregation treatment in a settler 18 to obtain slurry-like fuel oil 20, or whether the feedstock is to be recycled via a pipeline 21, in order to recover gas 14 and petrol 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 reference numerals 12 and 13 denote a heat exchanger and a gas-liquid separator, respectively.
  • middle oil of good quality (kerosine 16 and gas oil 17) from raw material for hydrocracking and fluid catalytic cracking
  • the major portion of oil from the bottom of the distilling column 11 is recycled through the pipeline 21 without collecting fuel oil 19. It may be attempted to increase the yield of the distillate to include gas oil having a high boiling point by returning the fuel oil 20 from the settler 18 to a reboiler combined with a second heater and by returning the fuel oil 19 to the distilling column 11.
  • the raw material was fed into a pressure vessel at a temperature of 450°C to 470°C and a pressure of 490 kPa-gauge and subjected to a coking treatment of 20 hours to obtain a product consisting of 28.2% by weight of cracked gas, 25.2% by weight of mixed coke and cracked oil, the distillate of which contained 36.4% by weight boiling below 250°C and 10.2% by weight boiling at 250°C to 350°C, making a total of 46.6% by weight of coked extract oil.
  • the distillate below 250°C had a specific gravity of 0.7756 (15/4°C), consisted of 0.50% by weight sulfur, 17.7% by weight aromatic hydrocarbons, 26.1% by weight olefine hydrocarbons, 56.1 % by weight saturated hydrocarbons and had an initial boiling point at 60°C, 10% at 108°C, 20% at 129°C, 50% at 175°C, 90% at 234°C and 95% at 246°C.
  • the distillate in the temperature range of 250°C to 350°C had a specific gravity of 0.8509 (15/4°C), an average molecular weight of 200, a bromine value of 16 g/100 g and contained 1.47% by weight of sulfur.
  • the coke obtained had a sulfur content of 4.5% by weight.
  • Coking treatment was carried out in accordance with the present invention under the same conditions as described above, except that 3% by weight of calcium hydroxide having a particle size less than 100 mesh, preferably 4 to 8 pm, was added in the form of an aqueous slurry to the raw material, with the result that a product was obtained, consisting of 13.3% by weight of cracked gas, 12.0% by weight of coke and cracked oil containing 13.2% by weight distilling below 250°C, 22.3% by weight distilling from 250°C to 350°C and 39.2% by weight distilling above 350°C, making a total of 74.7% by weight of coke distillation oil.
  • the distillate boiling below 250°C had a specific gravity of 0.783 (15/4°C), a sulfur content of 0.56% by weight and a composition, determined by elution ch-romatography, of 42.4% aromatic hydrocarbons, 4.8% olefine hydrocarbons and 52.8% saturated hydrocarbons.
  • the distillate at 250°C to 350°C had a specific gravity of 0.871 (15/4°C), a bromine value of 25.6 g/100 g and contained 1.63% by weight of sulfur.
  • the distillate above 350°C had a specific gravity of 0.941 (15/4°C), a bromine value of 8 g/100 g arid a sulfur content of 2.37% by weight.
  • the coke had a sulfur content of 1.86% by weight.
  • Tables 2, 3 and 4 are set out the results of experiments carried out by using the heavy feedstocks indicated in Table 1 in accordance with the operating sequence illustrated by the Figure.
  • the surge drums 7 and 8 were maintained at temperatures of 490°C to 530°C to confirm the effect of adding CaO having a particle size of less than 100 mesh, preferably an average size of 4 to 8 pm.
  • the addition of CaO increases the yield of light oil (gas oil) and the deposition of sulfur from the feedstock in solid form in coke.
  • Combustible sulfur was determined by subjecting SO z , which was obtained by burning the coke at 800°C, to quantitative analysis.
  • Solidified sulfur was determined by subjecting S0 3 , which was obtained by burning the coke at 1500°C to quantitative analysis.
  • the sum of the contents of combustible sulfur and solidified sulfur is represented as 100% in the Tables.
  • the amount of solidified sulfur is remarkable. This is extremely important for a refining process.
  • the coke product is burned to be gasified or used as a fuel, it does not generate sulfur compounds at temperatures below 800°C and the waste gas is clean.
  • the vanadium is deposited in the coke when CaO is used and is almost removed from the heavy oil. On the contrary, when no additive is used, a larger quantity of vanadium remains in the heavy oil.
  • the vanadium In a refining process it is important for the vanadium to be deposited in the coke arid not to remain in the heavy oil, so that the heavy oil may be used as fuel for gas turbines and Diesel engines. It is to be noted that the light oil and the heavy oil obtained by the process of the present invention do not lower the activity of conventional catalysts. Thus, the process of the present invention can replace the conventional preliminary processes for treating heavy oils and tar sand bitumen which use hydrogen and catalysts causing troublesome difficulties.

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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)

Claims (8)

1. Procédé pour le raffinage du pétrole et des produits similaires par pyrolyse de charges lourdes, comprenant essentiellement le préchauffage de la charge lourde mélangée à un oxyde ou un hydroxyde d'un métal alcalino-terreux, ou à une boue aqueuse de cet additif, le maintien de la charge préchauffée, dans un réacteur (réservoirs-tampons (7, 8)), pendant 1 seconde à 30 minutes à une température de 350 à 550°C et sous une pression de 196 kPa efficaces en présence d'eau ou de vapeur d'eau et la séparation continue du gaz et du résidu de la charge dans une colonne de distillation avec précipitation et solidification des asphaltènes, des métaux lourds et du soufre et maintien de conditions de traitement fortement basiques par la présence des ions dudit métal alcalino-terreux.
2. Procédé de raffinage selon la revendication 1, caractérisé en ce que la charge est chauffée à une température comprise dans l'intervalle de 400 à 500°C dans un four et que la charge préchauffée est maintenue dans le réacteur (réservoirs-tampons (7) et (8)) pendant un temps de séjour de 1 seconde à 10 minutes, suivi de la distillation de ladite charge.
3. Procédé de raffinage selon la revendication 1, caractérisé en ce que l'oxyde de métal alcalino-terreux est l'oxyde de calcium CaO.
4. Procédé de raffinage selon la revendication 1, caractérisé en ce que l'hydroxyde de métal alcalino-terreux est l'hydroxyde de calcium Ca(OH)2.
5. Procédé de raffinage selon la revendication 1, caractérisé en ce qu'une chambre de cokéfaction retardée est utilisée comme réacteur (réservoirs-tampons (7) et (8)).
6. Procédé raffinage selon la revendication 1, caractérisé en ce qu'une chambre de cokéfaction sur lit fluidisé est utilisée comme réacteur (réservoirs-tampons (7) et (8)).
7. Utilisation du procédé de raffinage selon la revendication 1 pour réduire la teneur en vanadium ou en nickel des huiles lourdes produites pour les turbines à gaz et les moteurs Diesel.
8. Utilisation du procédé de raffinage selon la revendication 1 pour produire des charges pour le craquage catalytique sur lit fluidisé et l'hydrocraquage.
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
AT81106517T ATE18253T1 (de) 1981-08-21 1981-08-21 Raffinationsprozess zur ausbeutesteigerung von destillaten aus schweren erdoeleinsaetzen.
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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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 EP0072873A1 (fr) 1983-03-02
EP0072873B1 true EP0072873B1 (fr) 1986-02-26

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7270743B2 (en) 2000-09-18 2007-09-18 Ivanhoe Energy, Inc. Products produced form 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

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KR101703398B1 (ko) 2011-07-29 2017-02-22 사우디 아라비안 오일 컴퍼니 흡착제 물질을 활용한 지연 코킹 공정
FI128069B2 (en) 2018-07-20 2024-04-24 Neste Oyj Cleaning of recycled and renewable organic material
FI128115B2 (en) 2018-07-20 2024-08-20 Neste Oyj Cleaning of recycled and renewable organic material
FI128911B (en) 2018-07-20 2021-03-15 Neste Oyj Purification of recycled and renewable organic material
FI128174B (en) 2018-07-20 2019-11-29 Neste Oyj Purification of recycled and renewable organic material
FI128121B (en) 2018-07-20 2019-10-15 Neste Oyj Production of hydrocarbons from recycled or renewable organic material

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1280375A (en) * 1970-01-27 1972-07-05 Exxon Research Engineering Co Conversion of heavy hydrocarbon 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
CA1110567A (fr) * 1975-12-19 1981-10-13 Iacovos A. Vasalos Craquage catalytique a degagement reduit de gaz nocifs

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7270743B2 (en) 2000-09-18 2007-09-18 Ivanhoe Energy, Inc. Products produced form 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

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ATE18253T1 (de) 1986-03-15
EP0072873A1 (fr) 1983-03-02
DE3173881D1 (en) 1986-04-03

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