СПОСОБ И УСТАНОВКА ДЛЯ ОБРАБОТКИ СРЕД, ЗАГРЯЗНЕННЫХ ПОЛИХЛОРИРОВАННЫМ БИФЕНИЛОМ

Изобретение касается обработки сред, загрязненных полихлорированным бифенилом посредством объединения данной среды с жидкостью, содержащей один или несколько жидких углеводородов, с получением смеси среда/жидкость, акустической обработки данной смеси при аудиочастоте с целью экстракции полихлорированного бифенила из среды в жидкость, и обработки полученной жидкости натрийсодержащим щелочным металлом. Данный способ может включать дополнительные стадии для уменьшения размера частиц среды. После акустической обработки данную жидкость можно декантировать со среды и обработать отдельно натрийсодержащим щелочным металлом. Технический эффект - возможность мобильной обработки среды на месте загрязнения, эффективное разрушение загрязнений за минимальное количество стадий обработки 2 н. и 33 з.п. ф-лы, 4 ил., 13 табл.

СПОСОБ ДЕАСФАЛЬТИЗАЦИИ И ОБЕССЕРИВАНИЯ ТЯЖЕЛОЙ НЕФТИ С ПОЛУЧЕНИЕМ БИТУМНОГО ВЯЖУЩЕГО

Изобретение относится к области нефтедобычи и нефтепереработки, а именно к способу удаления смолисто-асфальтеновых веществ из тяжелой нефти, а также ее обессериванию. Способ деасфальтизации тяжелой нефти включает добавление к ней кремнийорганической жидкости, перемешивание, отделение смолисто-асфальтеновых веществ и отделение светлого продукта от кремнийорганической жидкости путем дистилляции, в котором в качестве кремнийорганической жидкости используют силиконовое масло, представляющее собой полидиметилсилоксан с молекулярной массой 1250-28000 г/моль, при следующем соотношении компонентов (мас.%): силиконовое масло 33-94; тяжелая нефть - остальное, а смолисто-асфальтеновые вещества отделяют декантацией с получением готового битумного вяжущего. Технический результат: более полное удаление смолисто-асфальтеновых веществ из тяжелой нефти при меньших энергетических затратах и возможности использования полученных смолисто-асфальтеновых веществ в качестве готового товарного продукта - битумного ...

СПОСОБ ПОЛУЧЕНИЯ ВЫСОКОИНДЕКСНЫХ КОМПОНЕНТОВ БАЗОВЫХ МАСЕЛ

Изобретение относится к способу получения высокоиндексных компонентов базовых масел, соответствующих группе II и III по API, и может быть применено в нефтеперерабатывающей промышленности для получения высокоиндексных компонентов базовых масел из непревращенного остатка гидрокрекинга с использованием процессов депарафинизации селективными растворителями и каталитической гидроочистки. Способ осуществляют путем каталитического гидрокрекинга нефтяного сырья при давлении не менее 13,5 МПа, температуре от 380 до 430°С, объемной скорости подачи сырья от 0,5 до 1,5 чсо степенью конверсии не менее 75% с получением непревращенного остатка гидрокрекинга, содержащего не менее 90% мас. насыщенных углеводородов, в том числе изопарафиновых углеводородов не менее 30% мас., с последующим его фракционированием и выделением целевых фракций, которые подвергаются депарафинизации селективными растворителями и гидроочистке, отличающийся тем, что после фракционирования выделяют три узкие целевые фракции, в качестве ...

СПОСОБ ПОЛУЧЕНИЯ КОТЕЛЬНОГО ТОПЛИВА

Способ получения котельного топлива, включающий вакуумную ректификацию прямогонного мазута, с получением утяжеленного гудрона и металлизированной фракции вакуумной ректификации, фракции вакуумного газойля с последующим висбрекингом утяжеленного гудрона с получением комбинированного продукта висбрекинга, при этом для получения котельного топлива смешивают гудрон утяжеленный, металлизированную фракцию вакуумной ректификации мазутов, смесь асфальта и экстракта производства масел, разбавитель - прямогонное дизельное топливо фракции 160-360°С, комбинированный продукт висбрекинга, характеризующийся тем, что в процессе вакуумной ректификации смесевого сырья дополнительно выделяют фракцию с температурой кипения 360-390°С и используют ее в качестве дополнительного компонента разбавителя котельного топлива, в котельное топливо дополнительно вводят фракцию каталитического газойля с температурой кипения 190-550°С, при следующем соотношении компонентов смешения в котельном топливе, мас. %: гудрон утяжеленный ...

УСТРОЙСТВО И СПОСОБ ДЛЯ ИЗВЛЕЧЕНИЯ ТЯЖЕЛЫХ УГЛЕВОДОРОДОВ ИЗ ПОТОКА РАСТВОРИТЕЛЯ

... 1. Устройство для удаления тяжелых углеводородов из потока растворителя, включающее:первый экстракционный узел и второй экстракционный узел;где первый экстракционный узел включает первую линию ввода воды, линию вывода потока растворителя и первую линию вывода тяжелых углеводородов;причем первая линия вывода тяжелых углеводородов соединена со вторым экстракционным узлом;где второй экстракционный узел включает вторую линию ввода воды, вторую линию вывода воды и вторую линию вывода тяжелых углеводородов;причем вторая линия вывода воды соединена с первой линией ввода воды; илиния ввода легких углеводородов соединена с первым экстракционным узлом, и дополнительно поток растворителя включает замкнутый поток растворителя, а система регенерации растворителя соединена с линией вывода потока растворителя.2. Устройство по п.1, в котором система регенерации растворителя включает двухступенчатую испарительную систему.3. Устройство для удаления тяжелых углеводородов из потока растворителя, включающее ...

МНОГОСТАДИЙНЫЙ ГИДРОКРЕКИНГ ОСТАТКОВ ПЕРЕГОНКИ

... 1. Способ повышения качества остатка перегонки углеводородов, включающийгидрокрекинг остатка на первой стадии реакции с образованием потока, выходящего с первой стадии;гидрокрекинг фракции деасфальтизированного масла на второй стадии реакции с образованием потока, выходящего со второй стадии;фракционирование потока, выходящего с первой стадии, и потока, выходящего со второй стадии, с извлечением, по меньшей мере, одной дистиллятной углеводородной фракции и остаточной углеводородной фракции;подачу остаточной углеводородной фракции в установку деасфальтизации растворителем с получением фракции асфальтенов и фракции деасфальтизированного масла.2. Способ по п. 1, где, по меньшей мере, рабочая температура либо рабочее давление на второй стадии реакции больше, чем рабочая температура и рабочее давление на первой стадии реакции.3. Способ по п. 1, где, по меньшей мере, часть асфальтенов в остатке подвергается гидрокрекингу на первой стадии реакции.4. Способ по п. 1, дополнительно включающий работу ...

СПОСОБ ПОЛУЧЕНИЯ СМАЗОЧНОГО БАЗОВОГО МАСЛА

... 1. Способ получения смазочного базового масла, имеющего содержание насыщенных веществ выше, чем 90 вес.% и индекс вязкости выше, чем 90, в котором используют в качестве исходного сырья продукты вакуумной дистилятной перегонки путем проведения следующих стадий:(a) обработки продуктов вакуумной дистилляции растворителем для экстракции, избирательным в отношении экстракции ароматических соединений из продуктов вакуумной перегонки,(b) смешивания экстрагированного масла, полученного на стадии (а), с сырьем, включающим более чем 50 вес.% воска или включающим более чем 80 вес.% парафинов и имеющим температуру текучести выше, чем 0°С,(c) гидроочистки смеси, полученной на стадии (b),(d) каталитической депарафинизации гидроочищенного масла, полученного на стадии (с), для получения смазочного базового масла, и(e) контактирования депарафинизированного масла с катализатором насыщения ароматических веществ.2. Способ по п.1, в котором сырьем, включающим более чем 50 вес.% воска на стадии (b), является ...

ЭКСТРАКЦИОННАЯ КОЛОННА И СПОСОБ ДЛЯ ЕЕ ИСПОЛЬЗОВАНИЯ

... 1. Противоточная колонна (1) экстрагирования жидкости жидкостью, выполненная с возможностью протекания в ней двух или более жидкостей (2) и содержащая внутри одной общей емкости (3)первый вход (41) для первого жидкого подаваемого потока (51),второй вход (42) для второго жидкого подаваемого потока (52),первый выход (61) для потока (71) продукта,второй выход (62) для потока (72) побочного продукта,секцию (8) перемешивания, включающую в себя средство (9) перемешивания,статическую секцию (10), включающую в себя насадку (11),необязательно коллектор (12) и/или распределитель (13),отличающаяся тем, что внутри общей емкости (3) находится только одна секция (8) перемешивания и только одна или две статические секции (10).2. Колонна (1) по п. 1, которая является, по существу, вертикальной, причем внутри общей емкости (3) находится только одна статическая секция (10), и причем секция (8) перемешивания предпочтительно расположена существенно выше статической секции (10).3. Колонна (1) по любому из п ...

Способ выделения ароматических углеводородов из их смесей с неароматическими

"VERFAHREN ZUR HERSTELLUNG VON KAELTEMASCHINENOELEN"

Verfahren zur Herstellung hochwertiger Schmieroele

Verfahren zur Herstellung naphthenischer Schmieroele

Verfahren zur extrahierenden Fraktionierung von Aromaten enthaltenden Kohlenwasserstoffgemischen

Improved process of distilling hydrocarbons

... 147,715. Standard Oil Co., (Assignees of Humphreys, R. E.). June 26, 1914, [Convention date]. Hydrocarbons, cracking.-High-boiling hydrocarbons, such as fuel oils, are treated to produce hydrocarbons of lower boiling-point such as gasolene by distilling them in a boiler 3 under a pressure of 4 to 22 atmospheres and passing the vapours, still under pressure, up inclined pipes 4 in which the heavier fractions condense and run back into the boiler. The lighter fractions are condensed in a condenser 7 in which the increased pressure may be retained or not. Specifications 29862/12 and 6593/14 are referred to.

Hydrocarbon Treating Process

... 1,156,838. Separating hydrocarbons. TEXACO DEVELOPMENT CORP. 4 Oct., 1966, No. 44363/66. Heading C5E. A method of treating a hydrocarbon oil comprising dicyclic aromatic hydrocarbons, monocyclic aromatic hydrocarbons, and non-aromatic hydrocarbons effecting separation of a first product fraction rich in said dicyclic aromatic hydrocarbons, a second product fraction rich in said monocyclic hydrocarbons and a third product fraction rich in said non-aromatic hydrocarbons comprises contacting said hydrocarbon oil with a solvent comprising furfural at selective conditions in a first contacting zone, effecting separation of a first extract-mix comprising said first product fraction and a first raffinate comprising monocyclic hydrocarbons and non-aromatic hydrocarbons, separating said first product fraction from said first extract mix, contacting said first raffinate with a solvent comprising furfural at conditions effecting extraction of aromatic hydrocarbons to the substantial exclusion of non-aromatic ...

Method of Separating Aromatic Hydrocarbons from Mixtures containing them.

... 1,160,520. Separating aromatic hydrocarbons. SOC. ITALIANA RESINE S.p.A. 28 Dec., 1966 [29 Dec., 1965], No. 58009/66. Heading C5E. Aromatic hydrocarbons are separated from liquid hydrocarbon mixtures by introducing the mixture into a multi-stage extractor at an elevated temperature countercurrent to an organic solvent selected from diethylene glycol, dipropylene glycol, a mixture of said glycols and sulpholane, withdrawing from the extractor an aromatic-rich liquid extract and a non-aromaticrich liquid raffinate, conveying said extract to a second multi-stage extractor, operating at lower temperature than the first, countercurrent to a saturated hydrocarbon mixture boiling at atmospheric pressure below 50‹ C., recovering from the second extractor a first liquid phase comprising organic solvent (which may be recycled) and which is substantially free from aromatic hydrocarbons, and a second liquid phase comprising aromatic and saturated hydrocarbons and which is substantially free from solvent ...

A process for improving synthetic lubricating oils

Synthetic lubricating - oils obtained as described below are improved by extraction with selective solvents, e.g. nitrobenzene, aniline, acetonitrile, benzonitrile, chlorinated ethers, esters of aliphatic alcohols liquid sulphur dioxide, liquefied propane or other normally gaseous aliphatic hydrocarbon or mixtures. Agents lowering the setting point may be added to the treated oils. The synthetic oils are those made by polymerization or condensation of the liquid olefines produced by cracking paraffin wax or fats or fatty oils, or by dehydrating alcohols obtained by hydrogenation of fats or fatty oils; the olefines may be mixed with mineral or tar oil fractions, or cracking or destructive hydrogenation products of coals, tars, or mineral oils; and high molecular condensation products of isobutylene may be added before, during, or after condensation. The extraction is effected by mixing and setting, or by countercurrent flow, suitably at -30 DEG C. to 50 DEG C. and if desired at increased ...

Washing oily solids

Oil residues are removed from contaminated solids, in particular from cuttings produced from drilling a borehole using an oil-based drilling fluid, by contacting the solids with a washing fluid which comprises carbon dioxide and cosolvent under conditions at which carbon dioxide is a supercritical fluid and the cosolvent is in solution in the supercritical carbon dioxide, and then separating washed solids from the washing fluid; wherein the washing fluid comprises at least 5% by volume of co-solvent which is one or more organic compounds with a Hildebrand solubility parameter in a range from 16 to 21 MPa1/2. The washing process may be applied to drilling cuttings produced offshore. The co-solvent may include at least one of a cycloaliphatic ring, an olefinic unsaturation, an ester group and an ether group, and may be d-limonene, α-pinene, methyl ester of soybean oil, cyclohexane or glyceryl palmitate.

A process for splitting up a liquid mixture into its components or groups of components

In separating a liquid mixture into its components A, B by a solvent S which dissolves A more readily than B the component A is obtained in any desired degree of purity by washing at uniform temperature the extract solution of A in S with a liquid which entirely or substantially consists of A. The extraction and the washing may both be in counter-current, and the washing liquid may be some of the extract from which the solvent S has been entirely or substantially removed, and the used washing liquid may be treated with the solvent S. The last operation is preferably effected when the washing liquid is of approximately the same composition as the initial liquid mixture AB and may advantageously be mixed with it. The solvent S may be completely miscible with component A, but when a high degree of purity is required it is essential that at the working temperature the solvent be only partially miscible with both A and B. Atmospheric, reduced, or increased pressure may be used. Mixtures of solids ...

Solvent Refining

... 1,153,116. Solvent-extracting oils. TEXACO DEVELOPMENT CORP. 7 Feb., 1968 [13 March, 1967], No. 6046/68. Heading C5E. A method of manufacturing a lubricating oil includes the steps of contacting a lubricating oil stock with a solvent comprising N-methyl- 2-pyrrolidone at a temperature of at least 50‹ F. and below the temperature of complete miscibility of said lubricating oil stock in N-methyl-2-pyrrolidone and at a dosage effective to dissolve at least 10% by volume of material from said lubricating oil stock whereby a refined lubricating oil stock is produced of improved viscosity index, improved thermal stability and improved oxidation stability. The process is applicable to paraffinic and naphthenic oils. Preferred temperatures are between 50‹ and 250‹ F. The process may be followed by de-waxing with toluene-MEK mixture and distillation.

A process for preparing fractions with a melting point lower than that of paraffin wax from liquid hydrocarbon mixtures

Liquid hydrocarbons free from paraffin wax are separated into (A) a fraction richer in straight chain saturated aliphatic hydrocarbons, of relatively higher M.P., and (B) a fraction richer in cyclic, unsaturated aliphatic, and/or branched chain saturated aliphatic hydrocarbons, of relatively lower M.P., by cooling in the absence of a diluent to below -20 DEG C., and at this temperature extracting the entirely or partially solid mass obtained with a solvent which is non-polar or has a dipole movement not exceeding 1,5 X 10<-18>, e.s.u., and which dissolves (B) more readily than (A). Fractions of decreasing M.P. can be obtained by repeating the process on the extract at successively lower temperatures, using the same or different solvents. The treatment of lubricating oils, gas oils, kerosenes, and gasolenes with low M.P. ethers, esters, gasolenes, toluene, and chlorinated hydrocarbons, e.g. ethylene chloride is specified. In an example, gas oil having an aromatic content of 40 per cent is ...

Improvements relating to processes for the fractional decomposition of hydrocarbon mixtures

Mineral oils are separated into fractions by flowing the oil on to a body of a solvent of lower specific gravity than the oil, and after standing, drawing off layer fractions which contain the desired final oil in admixture with lighter oils and solvent, and distilling these fractions to remove the solvent and the lighter oils at a temperature lower than the boiling range of the desired oil which is obtained as residue. A crude mineral oil is fed from a tank b to a column c about half full of benzine. The oil is distributed uniformly through a tubular cross h. After standing, insoluble matter is removed through a cock g and three fractions are drawn off through the 3rd, 6th, and 8th valves f. These fractions are freed from solvent and then distilled at 200 to 215 DEG C. under a reduced pressure of 50 to 60 mm. to remove light oils, leaving three lubricating-oil fractions. Specification 460,906 is referred to.

Improvements in apparatus for maintaining and controlling liquid levels

... 509,728. Automatic control systems. STANDARD OIL DEVELOPMENT CO. Aug. 25, 1938, No. 25047. Convention date, Dec. 27, 1937. [Class 38 (iv)] Fluid level.-The position of the interface between two substantially immiscible fluids having dissimilar electrical resistivities is maintained by means of a pair of electric contacts close together in the fluid at the level desired and a valve electrically operated in response to the variations in electrical resistance between the contacts occurring with change in interface level. The contacts may be in a side arm connected to the fluid container or in an outwardly extending portion of its wall; they may consist of the ends of units sealed through a glass side arm 1/16 of an inch apart, parallel wires close together, or the points of a sparking plug. Fig. 1, shows a system for controlling the level of the interface between two fluid phases (one of which may be a gas) such as the raffinate and extract phases in a solvent treating process comprising a ...

Improvements relating to processes for refining lubricating oils

... Crude lubricating-oil is topped to remove hydrocarbons devoid of lubricating properties, and is then fractionated by flowing the topped oil on to a body of solvent of lower specific gravity than the oil, and after standing, drawing off the layer fractions and removing solvent therefrom. The stratification may take place under atmospheric or higher pressure. For example, a topped mineral oil is fed from a tank b to a column c about half full of benzine. The oil is distributed uniformly through a tubular cross h. After standing, insoluble matter is removed through a cock g, and fractions are drawn off through the valves f, and p solvent is removed therefrom. The oil fractions obtained may be further treated with sulphuric acid, lime and fuller's earth. Specification 460,906 is referred to.

PROCESS FOR THE PREPARATION OF LUBRICATING OILS

Improvements in or relating to liquid-liquid countercurrent extraction of a liquid mixture

In the liquid-liquid countercurrent extraction of a liquid mixture with a selective solvent partially miscible therewith, additional selective solvent or extract phase is added at a point downstream from the point of introduction of the first solvent in an amount to maintain the specific gravity differential between the raffinate and extract phases at at least 0.2. The process may be used in the "Duo Sol" solvent extraction process wherein 2 immiscible solvents are flowing countercurrently. Liquid mixtures specified are petroleum fractions such as gasolines, naphthas, kerosenes, gas oils, e.g. catalytic cycle gas oil, and lubricating oils. Solvents referred to are nitrobenzene, liquid propane or sulphur dioxide, b ,b 1-dichloroethyl ether, phenols, furfural and liquid hydrogen fluoride. The process is described with reference to the Figure which shows an extraction zone, consisting of a contacting zone superimposed on a settling zone, containing contact masses to promote mixing.

Process for production of lubricating oils

Naphthenic type lubricating oils are obtained by subjecting a mixed base lubricating oil distillate fraction to a solvent extraction and dewaxing treatment, the solvent extraction including the steps of extracting with an aromatic-selective solvent, for example, phenol, furfural, liquid SO2, nitrobenzene, and nitroparaffins, in a first stage to obtain a first extract phase, which extract phase is then separated into a second extract phase and a second raffinate phase, from which raffinate phase most of the paraffinic and aromatic compounds have been excluded, and hydrogenating the dewaxed second raffinate in the presence of a catalyst. The dewaxing step may either precede or preferably follow the solvent extraction. The separation of the first extract phase may be effected by at least one of the steps of cooling and injection of anti-solvent, for example water, if desired with concomitant extraction with an aromatic-selective solvent. The dewaxing may be effected by means of a solvent, ...

Process of solvent extraction of components aromatic of mixtures of hydrocarbons.

Process of solvent extraction sophisticated.

Process of aromatic hydrocarbon extraction per solvent.

PROCEDURE FOR EXTRACTING AROMATIC HYDROCARBONS FROM A COAL WATER MATERIAL MIXTURE

LIQUID HYDROCARBON MIXTURES WITH HIGH ONES IN ONE AND TWO-FULL OF SEEDS AROMATIC PORTIONS.

PROCEDURE FOR THE PRODUCTION OF PURE ONES AROMATICS.

VERTICAL LIQUIDLIQUID CONTACT COLUMN

PROCEDURE FOR THE PRODUCTION FROM PURE AROMATICS REFORMATBENZIN

Procedure for the separation of aromatic hydrocarbons

Process to prepare a process oil

Methods and systems for storing and transporting gases

A method and system of storing and transporting valuable gases comprising mixing the gases with liquid natural gas to form a mixture. The mixture is transported in vessel configured for cooling the mixture by boiling a portion of liquid natural gas. The transportation vessel is further configured to be cooled in the absence of valuable gases by a remaining portion of liquid natural gas. The method further comprises recycling liquid natural gas through the vessel for pre-cooling the vessel prior to loading the mixture of valuable gases and liquid natural gas.

Configurations and methods for gas condensate separation from high-pressure hydrocarbon mixtures

SOLVENT REFINING OF A PETROLEUM BASED OIL STOCK WITH N-METHYL2-PYRROLIDONE

LUBRICATING OILS BY SOLVENT EXTRACTION

Raffinate hydroconversion process

Optical fiber connector system

MULTISTAGE RESID HYDROCRACKING

Processes for upgrading resid hydrocarbon feeds are disclosed. The upgrading processes may include: hydrocracking a resid in a first reaction stage to form a first stage effluent; hydrocracking a deasphalted oil fraction in a second reaction stage to form a second stage effluent; fractionating the first stage effluent and the second stage effluent to recover at least one distillate hydrocarbon fraction and a resid hydrocarbon fraction; feeding the resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil fraction.

PROCESS FOR THE PREPARATION OF LUBRICATING OILS

A process for the preparation of lubricating oils with a viscosity index lower than 90, characterized in that two or more components prepared from waxy crude mineral oils are blended, which components have been selected from the following three groups: A. aromatic extracts from deasphalted residual lubricating oil fractions, which extracts have been subjected to a catalytic hydrogen treatment, B. aromatic extracts from distillate lubricating oil fractions, which extracts have been subjected to a catalytic hydrogen treatment, C. dewaxed gas oils having a 5% boiling point of at least 275.degree.C, it being understood that the lubricating oils are prepared, by blending one or more components selected from group C with one or more components selected from group A and/or with one or more components selected from group B.

EXTRACTIVE DISTILLATION

TREATMENT OF EXTRACTION SOLVENT TO REMOVE ACID CONTAMINANTS

A method for removing corrosive contaminants from a polar extraction solvent comprises adding water to the solvent to provide a mixture. Then the mixture is contacted with a basic ion exchanger resin to remove the corrosive contaminants. The solvent is recovered and may be reused.

PRINTING INK OIL

INTEGRATED PROCESS FOR BITUMEN RECOVERY, SEPARATION AND EMULSIFICATION FOR STEAM GENERATION

The invention relates to a process for splitting bitumen into two fractions and rendering a heavier bottom fraction as a useable emulsion fuel. The process is particularly effective in creating an alternate fuel to natural gas in a steam- based bitumen recovery process wherein bitumen is recovered from an underground reservoir.

PROCESS FOR BENZENE REDUCTION AND SULFUR REMOVAL FROM FCC NAPHTHAS

A process for the removal of sulfur compounds and benzene of a catalytica lly cracked petroleum naphtha comprising benzene, organic sulfur compounds a nd olefins, by fractionating the cracked naphtha into a relatively low boili ng range, olefinic, light catalytic naphtha (LCN) and an olefinic heavy cata lytic naphtha (HCN) which boils above the range of the LCN the boiling range s of the LCN and the HCN being defined by a cut point selected to maintain m ost of the benzene in the cracked naphtha in the LCN together with olefins i n the boiling range of the LCN. The LCN is subjected to an optional non-hydr ogenative desulfurization step followed by a fixed bed alkylation step in wh ich the benzene in the LCN is alkylated with the olefins contained in this f raction. The HCN is treated by a similar an alkylation step using the olefin s contained in this fraction to alkylate the sulfur compounds, forming alkyl ated products which boil above the gasoline boiling range. The LCN and HCN a re ...

REMOVAL OF ACIDIC IMPURITIES IN PROCESSES FOR SOLVENT EXTRACTION OF AROMATICS FROM NONAROMATICS

Corrosion of process equipment in a system for extraction of aromatic components from nonaromatic components by means of a selective solvent, for example tetraethylene glycol, is reduced by treating with anion exchange resin a stream composed mainly of water which has been used to wash residual solvent from the extracted aromatics.

Verfahren zur Trennung von naphthenische Öle, paraffinische Öle sowie Paraffin enthaltenden Produkten in einzelne Bestandteile in ununterbrochenem Arbeitsgang und unter Anwendung von Lösungsmitteln.

Appareil pour la mise en contact de deux liquides de densité différente d'une manière continue et à contre-courant.

Verfahren zur Zerlegung einer Mischung organischer Verbindungen

Procédé et installation d'extraction par solvant

Procédé de fabrication d'un produit dérivé de la gomme arabique.

Extraktionsverfahren

Lösungsmittelextraktionsverfahren

Procedimento per l'estrazione in fase liquida di idrocarburi aromatici da miscele li contengono

Procedimento per la separazione di idrocarburi aromatici da miscele con idrocarburi paraffinici e naftenici

Vorrichtung um zwei oder mehr Phasen in innige Berührung zu bringen

Verfahren zur Herstellung von Benzin hoher Oktanzahl

Procédé de fabrication d'une huile de lubrification

Liquid-liquid extraction column including two types of plates themselves.

La présente invention décrit une colonne dextraction liquide-liquide à plateaux perforés et déversoirs, présentant une majorité de plateaux dits «ouverts» et une minorité de plateaux dits «fermés», les deux types de plateaux différant par le degré de perforation. Application de ladite colonne au traitement de système liquide-liquide à coalescence variable au cours du temps. Lapplication est prévue pour lextraction de composés soufrés.

Liquid-liquid extraction column including two types of plates themselves.

La présente invention décrit une colonne d’extraction liquide-liquide à plateaux perforés et déversoirs, présentant une majorité de plateaux dits «ouverts» et une minorité de plateaux dits «fermés», les deux types de plateaux différant par le degré de perforation. Application de ladite colonne au traitement de système liquide-liquide à coalescence variable au cours du temps. L’application est prévue pour l’extraction de composés soufrés.

Liquid-liquid extraction column using trays provided with an element generator load loss.

La présente invention décrit une colonne d’extraction liquide-liquide à plateaux perforés (Po) et déversoirs, les plateaux étant de plus équipés d’un élément de friction additionnel (Pad) qui permet d’augmenter l’épaisseur de la couche coalescée et de garantir un écoulement à contre-courant des phases continue et dispersée. La colonne d’extraction est utilisée par exemple pour l’extraction de composés soufrés d’une phase hydrocarbure par une solution aqueuse de soude.

Liquid-liquid extraction column using trays provided with an element generator load loss.

La présente invention décrit une colonne dextraction liquide-liquide à plateaux perforés (P 0 ) déversoirs, les plateaux étant de plus équipés dun élément de friction additionnel (P ad ) qui permet daugmenter lépaisseur de la couche de coalescée et de garantir un écoulement à contre-courant des phases continue et dispersée.

СХЕМЫ И СПОСОБЫ СЕПАРАЦИИ КОНДЕНСАТА ГАЗА ИЗ УГЛЕВОДОРОДНЫХ СМЕСЕЙ ВЫСОКОГО ДАВЛЕНИЯ

Предполагаемые схемы и способы обработки газа используют орошаемый абсорбер, который получает жидкое и парообразное углеводородное сырье. Абсорбер дополнительно получает десорбирующую среду, которая по меньшей мере частично сформирована парообразной фракцией газов, отогнанных из стабилизатора, и также получает очищающую среду, которая по меньшей мере частично сформирована жидкой фракцией газов, отогнанных из стабилизатора. В наиболее предпочтительном случае отогнанный продукт абсорбера поддерживается при температуре вблизи или ниже точки росы сырья.

METHOD OF SEPARATING MULTICOMPONENT MIXTURES INTO FRACTIONS

SYSTEM AND METHOD FOR OBTAINING THE HIGH-QUALITY GASOLINE AS A RESULT OF THE CATALYTIC RECOMBINATION OF THE HYDROCARBON

SYSTEM AND METHOD FOR OBTAINING THE HIGH-QUALITY GASOLINE AS A RESULT OF THE CATALYTIC RECOMBINATION OF THE HYDROCARBON

УСТАНОВКА И СПОСОБ СЕПАРАЦИИ КОНДЕНСАТА ГАЗА ИЗ УГЛЕВОДОРОДНЫХ СМЕСЕЙ ВЫСОКОГО ДАВЛЕНИЯ

Предполагаемые схемы и способы обработки газа используют орошаемый абсорбер, который получает жидкое и парообразное углеводородное сырье. Абсорбер дополнительно получает десорбирующую среду, которая, по меньшей мере, частично сформирована парообразной фракцией газов, отогнанных из стабилизатора, и также получает очищающую среду, которая, по меньшей мере, частично сформирована жидкой фракцией газов, отогнанных из стабилизатора. В наиболее предпочтительном случае отогнанный продукт абсорбера поддерживается при температуре вблизи или ниже точки росы сырья.

СПОСОБ ПЕРЕРАБОТКИ КАТАЛИЗАТА

Способ переработки катализата, в котором он фракционируется на бензиновую, промежуточную и дизельную фракции. Промежуточная фракция индивидуально или вместе с фракцией газойля подвергается экстрактивной дистилляции с разделением фракций ароматических и неароматических углеводородов. Ароматические углеводороды фракционируются с получением бензиновой фракции, имеющей высокое октановое число, которая смешивается с бензиновой фракцией для того, чтобы повысить октановое число. Фракция, не содержащая ароматических углеводородов, перегоняется и получаемая газойлевая фракция смешивается с другой газойлевой фракцией для того, чтобы увеличить цетановое число. В отличие от предшествующего уровня техники способ по настоящему изобретению имеет низкие сырьевые индексы, низкие капитальные затраты, низкие эксплуатационные затраты и позволяет увеличить ассортимент выпускаемых продуктов.

COALESCER FOR CO-CURRENT CONTACTORS

Process of production of stable oils, in particular of oils of transformers, oils of turbines and lubricating oils, on the basis of the shale clay oil

Process of improvement of oils of lighting

Process of production of a suitable matter for the plasticization and the extention of synthetic plastic compositions, compositions obtained and aromtic fractions used

Process of separation of aromatic hydrocarbons of mixtures of hydrocarbons

Process for obtaining aromatic hydrocarbons per extraction of mixtures of hydrocarbons of a content of armoatic lower than 90%

Process of separation of a mixture by means of a selective solvent

Process of solvent extraction sophisticated

New process of aromatic hydrocarbon extraction

Improved method for distilling hydrocarbons

Catalytic process of reforming of mixtures of hydrocarbons

Process of aromatic hydrocarbon extraction

PROCEEDED OF REFINING OF FRACTIONS Of LUBRICATING OILS STRONG CONTENT OF AROMATIC HAS

Solvent dewaxing oils - by chilling using evaporating refrigerant

PROCESS FOR THE SEPARATION OF AROMATIC HYDROCARBONS FROM A MIXED HYDROCARBON FEEDSTOCK

Полочный экстрактор

Полезная модель относится к технике экстракции тяжелого нефтяного сырья, а именно к конструкции противоточных экстракционных колонн для сольвентной деасфальтизации (СДА) нефтяных остатков различными более легкими растворителями. Полочный экстрактор включает тарелки-перегородки в форме дисков с сегментными вырезами в центре и по краям и распределители потоков сплошной и дисперсной фазы, выполненные в виде съемных и разборных элементов насадки, при этом в конструкцию боковых полок добавлены скругления по внутренним краям элемента насадки, а полки, расположенные посередине, имеют округлую выпуклую форму со стороны стекания пленки дисперсной фазы, на поверхности полок добавлены шарообразные вкрапления, по краям в линию сделаны отверстия, прямолинейные кромки полок заменены на гребенчатые, а распределители входящих потоков представляют собой полутрубу с боковыми перфорированными стенками, соединенными с краями центральной полки элемента контактных устройств. Предложенная конструкция полочного экстрактора позволяет обеспечить эффективное диспергирование тяжелой фазы нефтяного сырья в сплошной фазе растворителя, минимизировать застойные зоны и увеличить межфазную поверхность контакта и скорости экстракции, а также упростить монтаж/демонтаж внутренних устройств для их эффективной очистки вне корпуса аппарата в случае небольших диаметров экстрактора. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 196 381 U1 (51) МПК B01D 11/04 (2006.01) C10G 21/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (52) СПК B01D 11/04 (2019.08); C10G 21/00 (2019.08) (24) Дата начала отсчета срока действия патента: 06.11.2019 Дата регистрации: 27.02.2020 Приоритет(ы): (22) Дата подачи заявки: 06.11.2019 (45) Опубликовано: 27.02.2020 Бюл. № 6 Адрес для переписки: 141700, Московская обл., г. Долгопрудный, Институтский пер., 9, МФТИ, отдел по интеллектуальной собственности (56) Список документов, цитированных в отчете о поиске: US 5500116 A1, 19.03.1996 ...

Multi-stage counter-current froth settler and method of use

A method for recovery of bitumen from a bitumen-containing froth utilizes solvent and a single, froth settling vessel having a plurality of internals therein. The froth is first diluted with enough solvent to reduce the viscosity of the froth and the diluted froth is added to the vessel above the internals. Additional of the solvent is added to the vessel, either below the internals, intermediate the internals or both and is flowed counter-current to the diluted froth which is flowing downwardly over the plurality of internals. A gradient of solvent concentration relative to hydrocarbon concentration is formed through the internals which act as multiple stages of separation. The product, being bitumen and other light components, are carried with the solvent to the top of the vessel. The heavier components such as water, solids and asphaltene aggregates fall to the bottom of the vessel by gravity. Where paraffinic solvents are used, the solvent to bitumen ratio for the initial dilution of the froth is kept below a ratio at which the asphaltenes are rejected. Substantially all of the asphaltene rejection occurs in the settling vessel as the solvent to bitumen ratio increases therein.

Method for predicting catalyst performance

Disclosed herein is a method involving the steps of: (a) precipitating an amount of polyaromatic compounds from a liquid sample of a first hydrocarbon-containing feedstock having solvated polyaromatic compounds therein with one or more first solvents in a column; (b) determining one or more solubility characteristics of the precipitated polyaromatic compounds; (c) analyzing the one or more solubility characteristics of the precipitated polyaromatic compounds; and (d) correlating a measurement of catalyst activity performance for the first hydrocarbon-containing feedstock sample with a mathematical parameter derived from the results of analyzing the one or more solubility characteristics of the precipitated polyaromatic compounds to predict catalyst performance of a catalyst in a refinery operation of the hydrocarbon-containing feedstock.

Controlling bitumen quality in solvent-assisted bitumen extraction

Described herein is a method of controlling bitumen quality in a process stream within a solvent-assisted bitumen extraction operation, for instance a hydrocarbon stream from a froth separation unit (FSU). Bitumen quality is a measure of the amount of selected contaminants in the process stream. Contaminants may include asphaltenes (comprising metal porphyrins), sulfur, and inorganic solids (comprising inorganic elements, e.g. Si, Al, Ti, Fe, Na, K, Mg, and Ca). First, the amounts of selected contaminants are measured. Next, these measured values are compared to maximum reference values. If one or more of these contaminants is higher than the maximum reference value, at least one variable of the solvent-assisted bitumen extraction is adjusted to improve bitumen quality.

Selective separation of heavy coker gas oil

Embodiments of the invention are directed to the improvement of the design of coker systems and processes in order to improve the yields and separation of heavy coker gas oils derived therefrom.

PROCESS OF REDUCING VISCOSITY OF HEAVY CRUDE OIL BY REMOVAL OF ASPHALTENE USING A PRECIPITATING AGENT

A process and system for reducing the viscosity of heavy and extra heavy crude oils, and more particularly to a process for reducing the viscosity of heavy and extra heavy crude oils by means of total or partial oil deasphalting using a precipitating agent in order to obtain an upgraded crude oil of lower viscosity that can be pumped without the use of diluents. The upgrading also includes a reduction in metals and sulfur associated with asphaltene removal. The process consists of relatively simple equipment such as static mixers and stirred tanks and operation temperature is low and pressure is moderate. 1. A method of reducing a viscosity of heavy and extra heavy crude oils at an oilfield site by partially removing asphaltenes to produce a pumpable upgraded oil , the method comprising:combining a heavy or extra heavy crude oil and a feed precipitant, wherein a volumetric precipitant to crude oil ratio is in a range from about 1 to about 2;precipitating and separating asphaltenes from the combination crude oil and precipitant;separating the precipitated asphaltenes to form an oil slurry comprising the asphaltenes and precipitant, and a liquid stream comprising precipitant and a remaining volume of the crude oil; andseparating the liquid stream to produce the upgraded oil and a first precipitant stream, wherein a yield of upgraded oil is about 90% by weight or more with respect to the heavy or extra heavy crude oil.2. The method of claim 1 , further comprising:washing the oil slurry with additional precipitant;separating the washed oil slurry to produce an asphaltenes stream and a second precipitant stream; anddrying the asphaltenes stream to produce a solid asphaltene product, and a third precipitant stream.3. The method of claim 2 , wherein at least one of the first claim 2 , second claim 2 , and third precipitant streams is recycled as feed precipitant.4. The method of claim 2 , wherein at least one of the first claim 2 , second claim 2 , and third precipitant ...

METHOD FOR TREATING HEAVY OIL

According to the invention, there is provided a method for treating heavy crude oil (HCO) which includes the steps of combining the HCO with an alkane containing solvent to form an HCO/solvent mixture, sonicating this mixture at audio frequency to precipitate asphaltenes from the HCO/solvent mixture, and separating the precipitated asphaltenes from the HCO/solvent mixture. 1. A method for treating heavy crude oil (HCO) comprising the steps of:a) combining said HCO with an alkane containing solvent to form an HCO/solvent mixture;b) sonicating said mixture at audio frequency to precipitate asphaltenes from the HCO/solvent mixture; andc) separating the precipitated asphaltenes from the HCO/solvent mixture.2. A method as in claim 1 , vacuum filtering the HCO/solvent mixture to remove precipitated asphaltenes.3. A method as in claim 1 , distilling the HCO-solvent mixture to remove solvent from the HCO/solvent mixture after removal of precipitated asphaltenes so as to create a deasphalted and solvent free synthetic crude oil (SCO).4. A method as in claim 1 , wherein the alkane contains solvent selected from the group consisting of pentane claim 1 , hexane and iso-octane.5. A method as in claim 1 , wherein the deasphalted HCO/solvent mixture is used as the feedstock for a chemical and/or biological oil upgrading process.6. A method as in claim 5 , wherein the chemical and/or biological process uses enzyme sources.7. A method as in claim 5 , wherein the chemical and/or biological process uses one or more oxidants in the presence of an acid.8. A claim as in claim 6 , wherein the enzyme source is soyabean husk.9. A claim as in claim 8 , wherein the enzyme is peroxidase.10. A claim as in claim 7 , wherein the acid is acetic acid.11. A claim as in claim 7 , wherein the oxidant is hydrogen peroxide combined with iron oxide.12. A method as in claim 1 , wherein the deasphalting time is 2 minutes (120 seconds) or less.13. A method as in claim 13 , wherein the deasphalting time is ...

Carbon Dioxide Fractionalization Process

A process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, separating the light hydrocarbon stream into a carbon dioxide-rich stream and a carbon dioxide-lean stream, and feeding the carbon dioxide-lean stream into a hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process compared to the processing capacity of the hydrocarbon sweetening process when fed the hydrocarbon feed stream. Included is an apparatus comprising a first separation unit that receives a hydrocarbon feed stream containing carbon dioxide and produces a heavy hydrocarbon stream and a light hydrocarbon stream, and a second separation unit that receives the light hydrocarbon stream and produces a carbon dioxide-rich stream and a carbon dioxide-lean stream, wherein the apparatus is configured to feed the carbon dioxide-lean stream to a physical solvent, membrane, or carbon dioxide recovery process.

Method of Processing a Bituminous Feed Using Agglomeration in a Pipeline

The present disclosure relates to a method of processing a bituminous feed. The bituminous feed is contacted with an extraction liquor to form a slurry. The slurry is then flowed through a pipeline. A bridging liquid is added to the slurry to assist agglomeration. Agitation is also used to assist agglomeration. The result is an agglomerated slurry comprising agglomerates and a low solids bitumen extract. The agglomerates are then separated from the low solids bitumen extract. Performing the agglomeration in a pipeline as opposed to in a conventional agitating vessel may provide certain advantages, such as improved sealing in order to contain the potentially flammable mixture of oil sands slurry from the atmosphere, production of smaller and more uniform agglomerates due to improved mixing of the bridging liquid into the oil sands slurry, and the flexibility to have a long residence time for the extraction and agglomeration processes.

BITUMEN PROCESSING AND TRANSPORT

Methods for preparing, converting, and/or transporting bitumen are provided. Asphaltene prills, prilling processes, and converted bitumen suitable for transport are disclosed. One method for preparing bitumen for transport comprises: separating asphaltene from the bitumen to generate a deasphalted oil and asphaltene; separating the asphaltene into a first asphaltene fraction and a second asphaltene fraction, the first asphaltene fraction being less soluble in deasphalted oil and the second asphaltene fraction being more soluble in deasphalted oil; and forming an asphaltene prill comprising an inner core comprising the second asphaltene fraction and an outer layer comprising the first asphaltene fraction. Asphaltene prills disclosed herein may comprise an inner core comprising an asphaltene fraction having more solubility in deasphalted oil, and an outer layer comprising an asphaltene fraction having less solubility in deasphalted oil. Methods for the transport of bitumen via a pipeline are disclosed. 1. A method for preparing or converting bitumen for transport , the method comprising:separating asphaltene from the bitumen to generate a deasphalted oil and asphaltene;separating the asphaltene into a first asphaltene fraction and a second asphaltene fraction, the first asphaltene fraction being less soluble in deasphalted oil and the second asphaltene fraction being more soluble in deasphalted oil; andforming an asphaltene prill comprising an inner core comprising the second asphaltene fraction and an outer layer comprising the first asphaltene fraction.2. The method of claim 1 , further comprising the step of:adding one or more hollow portions to the asphaltene prill to control the density of the asphaltene prill.3. The of claim 2 , wherein the one or more hollow portions are added to the inner core of the asphaltene prill.4. The method of claim 1 , further comprising the step of:combining the asphaltene prill with the deasphalted oil to form a slurry suitable for ...

Process for Mercury Removal

A predictive tool is provided for estimating the mercury content of hydrocarbons to be produced from a wellbore in a newly investigated subterranean hydrocarbon producing formation based on the mercury content of an inorganic sample recovered from the wellbore. The mercaptans content of liquid hydrocarbons and/or the hydrogen sulfide content of natural gas produced from the formation may also be used to enhance the prediction. Based on the predicted value, a mercury mitigation treatment may be provided to mitigate the mercury content of hydrocarbons produced from the formation. 1. A method for producing hydrocarbons having reduced mercury content from a newly investigated production zone in a subterranean formation , comprising: a mercury content of at least one inorganic matrix sample from each of the plurality of hydrocarbon production zones;', 'a mercaptans content of at least one liquid crude oil sample from each the plurality of production zones;', 'a hydrogen sulfide content of at least one natural gas sample from each of the plurality of production zones;, 'providing a knowledge base of data from a plurality of hydrocarbon production zones, the data correlating a mercury content of a hydrocarbon produced from each of the plurality of production zones with at least one ofevaluating the knowledge base of data using at least one measured value from a newly investigated production zone, the measured value selected from the group consisting of a mercury content of an inorganic matrix sample from the newly investigated production zone, a mercaptans content of a liquid crude oil sample from the newly investigated production zone, and a hydrogen sulfide content of a natural gas sample from the newly investigated production zone as inputs to the knowledge base;predicting the mercury content of the hydrocarbon to be produced from the newly investigated production zone; andproviding a mercury mitigation treatment for removing at least a portion of the mercury from the ...

Supercritical Water Separation Process

A supercritical water separation process and system is disclosed for the removal of metals, minerals, particulate, asphaltenes, and resins from a contaminated organic material. The present invention takes advantage of the physical and chemical properties of supercritical water to effect the desired separation of contaminants from organic materials and permit scale-up. At a temperature and pressure above the critical point of water (374° C., 22.1 MPa), nonpolar organic compounds become miscible in supercritical water (SCW) and polar compounds and asphaltenes become immiscible. The process and system disclosed continuously separates immiscible contaminants and solids from the supercritical water and clean oil product solution. The present invention creates a density gradient that enables over 95% recovery of clean oil and over 99% reduction of contaminants such as asphaltenes and particulate matter depending on the properties of the contaminated organic material. 1. A process for treating a feedstock comprising:delivering a feedstock and supercritical water into a hydrothermal separation vessel, said hydrothermal separation vessel including an upper separation zone, a mid-level mixing zone, and a bottom concentration zone, wherein the feedstock and supercritical water are fed separately into the mixing zone to form a mixture, said mixing zone providing sufficient shear and mixing to cause dissolution of any soluble components of the feedstock into the supercritical water;maintaining a temperature and pressure within the hydrothermal separation vessel to achieve a vertical density gradient therein such that the separation zone exhibits a lower density than the concentration zone to form a product stream and a stream containing insoluble components; andremoving the product stream from the separation zone and the stream containing insoluble components from the concentration zone.2. The process of claim 1 , wherein any components present in the feedstock that are ...

Supercritical Water Separation Process

A supercritical water separation process and system is disclosed for the removal of metals, minerals, particulate, asphaltenes, and resins from a contaminated organic material. The present invention takes advantage of the physical and chemical properties of supercritical water to effect the desired separation of contaminants from organic materials and permit scale-up. At a temperature and pressure above the critical point of water (374° C., 22.1 MPa), nonpolar organic compounds become miscible in supercritical water (SCW) and polar compounds and asphaltenes become immiscible. The process and system disclosed continuously separates immiscible contaminants and solids from the supercritical water and clean oil product solution. The present invention creates a density gradient that enables over 95% recovery of clean oil and over 99% reduction of contaminants such as asphaltenes and particulate matter depending on the properties of the contaminated organic material. 1. A process for separating contaminants from a contaminated feedstock comprised of:combining a contaminated feedstock and supercritical water to form a supercritical water and feedstock solution in a hydrothermal separation vessel, said hydrothermal separation vessel including an upper separation zone and a bottom concentration zone;maintaining a temperature and pressure within the hydrothermal separation vessel to achieve a vertical density gradient therein such that the separation zone of the hydrothermal separation vessel exhibits a lower density than the concentration zone of the hydrothermal separation vessel, to cause the contaminants to separate from the solution in the separation zone and to form a product stream;removing the product stream from the separation zone of the hydrothermal separation vessel; andremoving the contaminants from the concentration zone of the hydrothermal separation vessel.2. The process of claim 1 , wherein the separation zone is maintained at a pressure greater than 22.1 MPa ...

PROCESS FOR CONVERTING A FEEDSTOCK CONTAINING PYROLYSIS OIL

The invention relates to a process for converting a feedstock comprising pyrolysis oil and a heavy hydrocarbon-based feedstock, with: 1. Process for converting a first feedstock comprising pyrolysis oil obtained from a steam cracking unit and a second heavy hydrocarbon-based feedstock , said process comprising the following steps:a) a step of hydroconverting said feedstocks in at least one reactor, in the presence of hydrogen and of at least one hydroconversion catalyst, with the reactor being fed with the first feedstock at a feed temperature T1 of between 80 and 200° C. and with the second feedstock at a feed temperature T2 greater than 250° C., producing a hydroconverted liquid effluent;b) a step of separating at least a portion of the hydroconverted liquid effluent obtained from step a) into at least a naphtha fraction, a gas oil fraction, a vacuum gas oil fraction and an unconverted residue fraction;c) a hydrocracking step in a fixed-bed reactor in the presence of a catalyst for hydrocracking at least a portion of the vacuum gas oil fraction obtained from step b), producing a hydrocracked liquid effluent;d) a step of fractionating at least a portion of the hydrocracked liquid effluent obtained from step c) into a naphtha fraction, a gas oil fraction and an unconverted vacuum gas oil fraction;e) a step of steam cracking of at least a portion of the naphtha fraction obtained from step d) and optionally of a portion of the unconverted vacuum gas oil fraction obtained from step d) to obtain a steam-cracked effluent;f) a step of fractionating at least a portion of the steam-cracked effluent obtained from step e) into an ethylene fraction, a propylene fraction, a butadiene and C4 olefin fraction, a pyrolysis gasoline fraction and a pyrolysis oil fraction;g) a step in which at least a portion of the pyrolysis oil fraction obtained from step f) is sent into the hydroconversion step a).2. Process according to claim 1 , characterized in that claim 1 , in step g) claim 1 ...

FORMING ASPHALT FRACTIONS FROM THREE-PRODUCT DEASPHALTING

Systems and methods are provided for using a three-product deasphalter to produce advantageous combinations of deasphalted oil, resin, and rock. The desaphalted oil, resin, and rock can then be further combined, optionally with other vacuum gas oil fractions produced during the distillation that generated the feed to the three-product deasphalter, to produce a product slate of improved quality while also maintaining the quality of the resulting asphalt product and reducing or minimizing the amount of lower value products generated. The additional “resin” product from the three product deasphalter can be generated by sequential deasphalting, by using a resin settler to separate resin from the deasphalted oil, or by any other convenient method. 1. A method for processing a heavy oil fraction , comprising:separating a vacuum gas oil fraction and a vacuum resid fraction from a heavy oil feed;{'sub': '4+', 'performing solvent deasphalting using a Csolvent under first solvent deasphalting conditions on at least a portion of the vacuum resid fraction to produce a first deasphalted oil and a first deasphalter residue, the effective solvent deasphalting conditions producing a yield of first deasphalted oil of 50 wt % or more of the feedstock;'}performing solvent deasphalting on at least a portion of the first deasphalted oil under second solvent deasphalting conditions to form a second deasphalted oil and a second deasphalter resin, the second solvent deasphalting conditions comprising lower lift deasaphlting conditions than the first solvent deasphalting conditions;forming a product slate from at least a portion of a) the vacuum gas oil fraction, b) the first deasphalter residue, c) the second deasphalted oil, and d) the second deasphalter resin, the product slate comprising an asphalt fraction and one or more fuels feeds, lubricant feeds, or a combination thereof, a volume of the product slate comprising 95 vol % or more of a combined volume of the vacuum gas oil fraction ...

Production of High Quality Base Oils

A process for creating higher quality and lower quality base oils from used lubricating oils and crude oils, wherein the higher quality base oils may be either Group III or Group II and the lower quality base oils may be either Group II or Group I. Vacuum gas oils produced from used lubricating oils and from crude oils are processed via two or more process steps, including solvent extraction, solvent or catalytic or iso dewaxing, and hydrotreating. Such process enables efficient conversion and operation of refineries formerly capable only of making Group I base oils, even as their ability to make heavier base oils, waxes, and bright stocks is preserved, substantially to the same extent as such products had been made prior to undertaking the conversion. 1. A method for making base oil , the method comprising steps of:blending together (a) vacuum gas oil made from crude oil (“CO-VGO”) and (b) vacuum gas oil made from used lubricating oil (“UO-VGO”) to form a blended VGO (“Blended VGO”); andprocessing the Blended VGO by means of at least two of solvent extraction, dewaxing, and hydrotreating to make a base oil.2. A method for making base oil by solvent extraction , de-waxing , and hydrotreating , the method comprising steps of:processing vacuum gas oil made from crude oil (“CO-VGO”) during a first period of time by at least two of solvent extraction, dewaxing, and hydrotreating to make at least one first base oil; andprocessing vacuum gas oil made from used lubricating oil (“UO-VGO”) during a second period of time by at least two of solvent extraction, dewaxing, and hydrotreating to make at least one second base oil.3. The method of wherein the UO-VGO is processed by hydrotreating prior to processing by solvent extraction.4. The method of wherein the UO-VGO is processed by solvent extraction prior to processing by hydrotreating.5. The method of wherein at least a portion of the effluent produced after processing the UO-VGO by hydrotreating is then processed by solvent ...

IMPROVEMENTS IN IN SITU UPGRADING VIA HOT FLUID INJECTION

The invention relates to systems, apparatus and methods for integrated recovery and in-situ (in reservoir) upgrading of heavy oil and oil sand bitumens. The systems, apparatus and methods enable enhanced recovery of heavy oil in a production well by introducing a hot hydrocarbon fluid from a mobile reservoir into the production well under conditions to promote hydrocarbon upgrading. The methods may further include introducing hydrogen and a catalyst together with the injection of the hot fluid into the production well to further promote hydrocarbon upgrading reactions. In addition, the invention relates to enhanced oil production methodologies within conventional oil reservoirs. 1. An apparatus for processing hydrocarbons , the apparatus comprising:an injection well, the injection well being configured to inject fluid into a subterranean reservoir;a recovery well, the recovery well being configured to recover fluid from the subterranean reservoir; andan injection well connector configured to receive heavy hydrocarbon fluid from a mobile surface reservoir and deliver the received heavy hydrocarbon fluid to the injection well to be injected into the subterranean reservoir for processing such that the fluid recovered from the subterranean reservoir via the recovery well has a different composition to the heavy hydrocarbon fluid injected via the injection well.2. The apparatus according to claim 1 , wherein the mobile surface reservoir forms part of an oil tanker ship.3. The apparatus according to claim 1 , wherein the apparatus forms part of an offshore oil rig.4. The apparatus according to claim 1 , wherein the heavy hydrocarbons comprise one or more of: bunker fuel; and fuel number 6.5. The apparatus according to claim 1 , wherein the apparatus comprises a pre-mixer configured to mix the heavy fraction with additional injection fluids and to inject the mixed fluids into the injection well.6. The apparatus according to claim 1 , wherein the injection well is ...

PROCESS FOR SELECTIVE CASCADE DEASPHALTING

The invention describes a process for the deasphalting of a heavy feedstock by liquid/liquid extraction, said process comprising at least two stages of deasphalting in series carried out on the feedstock to be treated making it possible to separate at least one fraction of asphalt, at least one fraction of heavy deasphalted oil, referred to as heavy DAO and at least one fraction of light deasphalted oil, referred to as light DAO, at least one of said stages of deasphalting being carried out by means of a mixture of at least one polar solvent and at least one apolar solvent, said stages of deasphalting being implemented under the subcritical conditions of the mixture of solvents used. 1. Process for the deasphalting of a heavy feedstock by liquid/liquid extraction , said process comprising at least two stages of deasphalting in series carried out on the feedstock to be treated , making it possible to separate at least one fraction of asphalt , at least one fraction of heavy deasphalted oil , referred to as heavy DAO and at least one fraction of light deasphalted oil , referred to as light DAO , at least one of said stages of deasphalting being carried out by means of a mixture of at least one polar solvent and at least one apolar solvent , the proportions of said polar solvent and said apolar solvent in the mixture of solvents being adjusted according to the properties of the feedstock treated and according to the desired yield of asphalt and/or the quality of the deasphalted oil , said stages of deasphalting being implemented under the subcritical conditions of the mixture of solvents used.3. Process according to claim 2 , in which the deasphalted oil phase originating from stage a) is previously subjected to at least one stage of separation in which the deasphalted oil is separated from the mixture of solvents or at least one stage of separation in which the complete deasphalted oil referred to as complete DAO is separated only from the apolar solvent.4. Process ...

Optimal asphaltene conversion and removal for heavy hydrocarbons

The invention provides improved apparatus and method for producing a pipeline-ready or refinery-ready feedstock from heavy, high asphaltene crude, comprising a pre-heater for pre-heating a process fluid to a design temperature at or near the operating temperature of a reactor; moving the process fluid into the reactor for conversion of the process fluid by controlled application of heat to the process fluid in the reactor so that the process fluid maintains a substantially homogenous temperature to produce a stream of thermally affected asphaltene-rich fractions, and a stream of vapour. The stream of vapour is separated into two further streams: of non-condensable vapour, and of light liquid hydrocarbons. The thermally affected asphaltene-rich fraction is deasphalted using a solvent extraction process into streams of heavy deasphalted oil liquid, and concentrated asphaltene, respectively. The deasphalted oil liquid and the light liquid hydrocarbons produced are blended to form a pipeline or refinery -ready feedstock.

Process Stream Decontamination Systems and Methods

A decontamination system for decontaminating at least one contaminant in a process stream. Decontaminant liquid is dispersed into the process stream using atomization. A controller detects contaminant levels in the process stream and adjusts the flow of decontaminant fluid into the process stream in response.

Enhanced methods for solvent deasphalting of hydrocarbons

Improvements to open-art Solvent Deasphalting (SDA) processes have been developed to reduce capital and operating costs for processing hydrocarbon streams are provided whereby open art SDA scheme is modified to include appropriately placed mixing-enabled precipitators (MEP's) to reduce solvent use requirements in an asphaltene separation step and to increase overall reliability for SDA processes, particularly suitable for Canadian Bitumen. When integrated with a mild thermal cracker, the improved SDA configuration further improves crude yield to be pipeline-ready without additional diluent and for use to debottleneck existing facilities such as residue hydrocrackers and coking units.

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker. 1. A process for converting whole crudes , the process comprising:separating a whole crude into at least a medium boiling fraction and a high boiling residue fraction;separating the high boiling fraction in a solvent deasphalting unit to produce a deasphalted oil fraction and a pitch fraction;converting the medium boiling fraction and the deasphalted oil fraction into one or more stream crackable products to produce a hydrotreated effluent;feeding the hydrotreated effluent to a steam cracker to convert hydrocarbons therein into one or more light olefins.2. The process of claim 1 , wherein the medium boiling fraction has two or more of the following properties:a 5% boiling point temperature in the range from about 130° C. to about 200° C.;a 95% boiling point temperature in the range from about 400° C. to about 600° C.;a hydrogen content in the range from about 12 wt % to about 14 wt %;a BMCI in the range from about 5 to less than 50;an API gravity of in the range from about 10° to about 40°;a sulfur content in the range from about 1000 ppm to about 10000 ppm;a nitrogen content in the range from about 1 ppm to about 100 ppm;a viscosity, measured at 40° C., of greater than 1 cSt;less than 5 wt % MCRT; andless than 50 ppm total metals.3. The process of claim 1 , wherein the high boiling residue fraction has two or more of the following ...

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. A system for converting whole crudes and other heavy hydrocarbon streams to produce olefins , the system comprising:a separation unit for separating a whole crude into at least a light boiling fraction, a medium boiling fraction, and a high boiling residue fraction;a solvent deasphalting unit for deasphalting the high boiling residue fraction and producing a deasphalted oil fraction and a pitch fraction;a conditioning system for destructively hydrogenating the medium boiling fraction and the deasphalted fraction to produce a hydrotreated effluent;a steam cracker unit for converting the hydrotreated effluent and the light boiling fraction into one or more light olefins and a pyrolysis oil.14. (canceled)15. (canceled)16. (canceled)17. The system of claim 13 , wherein the conditioning system for hydrotreating the medium boiling fraction and the deasphalted oil fraction comprises:a first hydroprocessing unit for hydroprocessing the medium boiling fraction; anda second hydroprocessing unit for hydroprocessing the deasphalted oil fraction.18. The system of claim 13 , further comprising a flow line for diverting the deasphalted oil fraction to the first hydroproces sing unit.19. The ...

Carbon Dioxide Fractionalization Process

A method comprises separating a hydrocarbon feed stream having carbon dioxide into a heavy hydrocarbon stream and a light hydrocarbon stream. The light hydrocarbon stream is separated into a carbon dioxide-rich stream and a carbon dioxide-lean stream. At least a portion of the carbon dioxide-lean stream is fed to a hydrocarbon sweetening process. Another method comprises receiving a hydrocarbon feed stream that comprises 30 molar percent to 80 molar percent carbon dioxide. A heavy hydrocarbon stream is separated from the hydrocarbon feed stream, wherein the heavy hydrocarbon stream comprises at least 90 molar percent C hydrocarbons. A carbon dioxide-rich stream is separated from the hydrocarbon feed stream, wherein the carbon dioxide-rich stream comprises at least 95 molar percent carbon dioxide. 1. A process comprising:receiving a hydrocarbon feed stream comprising carbon dioxide;separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream;separating the light hydrocarbon stream into a carbon dioxide-rich stream and a carbon dioxide-lean stream; andfeeding the carbon dioxide-lean stream into a hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process compared to the processing capacity of the hydrocarbon sweetening process when fed the hydrocarbon feed stream.2. The process of wherein the hydrocarbon sweetening process comprises:absorbing at least some of the carbon dioxide from the carbon dioxide-lean stream with a solvent;separating the solvent from the carbon dioxide-lean stream; andreleasing at least some of the carbon dioxide from the solvent by lowering the pressure of the solvent.3. The process of wherein the hydrocarbon sweetening process comprises: separating at least some of the carbon dioxide from the carbon dioxide-lean stream using a membrane.5. The process of wherein the hydrocarbon feed stream contains from about 30 percent to about 80 percent carbon ...

Method for cavitation-assisted refining, degumming and dewaxing of oil and fat

A method for degumming and/or refining crude oil containing impurities involving mixing the crude oil with degumming agents, i.e., water or acid, and subjecting the mixture to flow-through, hydrodynamic cavitation processing. The cavitational processing transfers impurities in the crude oil to a water phase for easier separation. The water phase may be separated from the oil phase by commonly available separation methods.

Process for conversion of residue employing de-asphalting and delayed coking

The present invention relates to resid processing, particularly related to conversion of resid material with maximum recovery of lighter hydrocarbons. The invented process utilizes a novel scheme for integration of solvent de-asphalting and delayed coking processes to maximize the residue conversion to valuable products, with cleaner quality of middle distillates and fuel oil products, in comparison with other integrated solvent de-asphalting and delayed coking schemes. This process also has an additional flexibility to vary the recycle quantity, without impacting fractionator operation of the delayed coking section, which further enhances the product recovery and achieves maximum conversion of the resid feedstock, with minimum impact on liquid product properties.

PROCESSES FOR DESALTING CRUDE OIL UNDER DYNAMIC FLOW CONDITIONS

Presented is a process for desalting crude oil. The process includes mixing a partially dehydrated crude oil, comprising less than 10 vol. % water and at least one water-extractable contaminant, with an aqueous wash fluid. A water-in-oil emulsion is formed. The water-in-oil emulsion is introduced into a first coalescence zone defined by a first vessel. The first vessel is configured to apply an electric field to the emulsion. The water-in-oil emulsion is broken within the first coalescence zone in the presence of the electric field under dynamic flow conditions to form a partially desalted crude oil and a non-emulsified aqueous salt solution. The partially desalted crude oil and the non-emulsified aqueous salt solution are then separated from one another under the dynamic flow conditions to yield a separated, partially desalted crude oil comprising less than 1 vol. % water. 1. A process , comprising:providing a partially dehydrated crude oil that comprises less than 10 vol. % water and a water-extractable contaminant;mixing an aqueous wash fluid with the partially dehydrated crude oil and forming a water-in-oil emulsion;introducing the water-in-oil emulsion into a first coalescence zone defined by a first vessel, wherein the first vessel is configured to apply a first electric field to the water-in-oil emulsion and to break the water-in-oil emulsion within the first coalescence zone in the presence of the first electric field and under a dynamic flow condition; andyielding from the first coalescence zone a partially desalted crude oil, comprising residual emulsified water of less than 1 vol. % water, and a non-emulsified aqueous salt solution.2. The process of claim 1 , wherein the process further comprises:introducing the partially desalted crude oil into a second coalescence zone defined by a second vessel configured to simultaneously apply a second centrifugal force and a second electric field to the partially desalted crude oil to convert the residual emulsified ...

Process and apparatus for two-stage deasphalting

Solvent deasphalting (SDA) in series is used to extract deasphalted oil from heavier hydrocarbons in series. Instead of stripping the pitch material of solvent in the second stage which can stick in the pitch stripper and inhibit flow, a dryer is used to vaporize solvent for recycle to the second SDA unit and produce pitch solids.

Carbon Dioxide Fractionalization

A method comprises separating a hydrocarbon feed stream having carbon dioxide into a heavy hydrocarbon stream and a light hydrocarbon stream. The light hydrocarbon stream is separated into a carbon dioxide-rich stream and a carbon dioxide-lean stream. At least a portion of the carbon dioxide-lean stream is fed to a hydrocarbon sweetening process. Another method comprises receiving a hydrocarbon feed stream that comprises 30 molar percent to 80 molar percent carbon dioxide. A heavy hydrocarbon stream is separated from the hydrocarbon feed stream, wherein the heavy hydrocarbon stream comprises at least 90 molar percent C 3+ hydrocarbons. A carbon dioxide-rich stream is separated from the hydrocarbon feed stream, wherein the carbon dioxide-rich stream comprises at least 95 molar percent carbon dioxide.

Process for producing propylene and a low-sulfur fuel oil component

A process for producing propylene and a low-sulfur fuel oil component, comprising the steps of contacting a heavy feedstock oil with a solvent for extraction separation to obtain a deasphalted oil and a deoiled asphalt; contacting the deasphalted oil and optionally a light feedstock oil with a catalytic conversion catalyst for reaction to obtain a reaction product comprising propylene; separating the reaction product to obtain a catalytic cracking distillate oil, and subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low-sulfur hydrogenated distillate oil, wherein the low-sulfur hydrogenated distillate oil and/or the deoiled asphalt is suitable for use as a fuel oil component. The process allows the conversion of saturated hydrocarbons in the heavy feedstock into propylene, eliminates the use of saturated hydrocarbons in the fuel oil component, and thus has better economic and social benefits.

Recovery of aliphatic hydrocarbons

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid hydrocarbon feedstock stream, which comprises aliphatic hydrocarbons and additionally comprises aromatic hydrocarbons and/or polar components, said process comprising the steps of: feeding the liquid hydrocarbon feedstock stream to a first column; feeding a first solvent stream which comprises an organic solvent to the first column at a position which is higher than the position at which the liquid hydrocarbon feedstock stream is fed; contacting at least a portion of the liquid hydrocarbon feedstock stream with at least a portion of the first solvent stream; and recovering at least a portion of the aliphatic hydrocarbons by liquid-liquid extraction of aromatic hydrocarbons and/or polar components with organic solvent, resulting in a stream comprising recovered aliphatic hydrocarbons and optionally organic solvent and a bottom stream from the first column comprising organic solvent and aromatic hydrocarbons and/or polar components.

Selective series-flow hydroprocessing system

Aromatic extraction and hydrocracking processes are integrated to optimize the hydrocracking units design and/or performance. By processing aromatics-rich and aromatic-lean fractions separately, the hydrocracking operating severity and or catalyst reactor volume requirement decreases.

FOULING REDUCTION IN SUPERCRITICAL EXTRACTION UNITS

A residual petroleum fraction feed is subjected to a deasphalting process by solvent extraction using a light paraffinic solvent with recovery of the solvent under supercritical process conditions. Fouling is reduced by the injection of an aromatic stream into the DAO-solvent stream from the extractor in order to provide a degree of solvency for residual asphaltenes in the DAO-solvent stream which otherwise would tend to precipitate in the heat exchanger used to create the supercritical conditions for the solvent. The aromatic solvent stream which, by its aromatic character, has solvency properties for the asphaltene components remaining in the DAO-solvent stream, is selected to have a boiling point above the boiling point of the solvent so that it does not contaminate the process solvent when the solvent is recovered in the solvent recovery section of the unit. 1. A residual oil deasphalting process which comprises:(i) contacting a petroleum fraction containing asphaltenes with a light paraffinic solvent for the non-asphaltene portion of the oil to produce a solution of deasphalted oil in the solvent and an asphaltenes fraction,(ii) passing the deasphalted oil solution through pressurization and heating steps to bring the solvent to a supercritical condition to cause a phase separation between a solvent-depleted solution of the deasphalted oil in the solvent and a phase comprising substantially solvent,(iii) separating the solvent-depleted solution of the deasphalted oil from the substantially solvent phase,(iv) recovering the deasphalted oil from the solvent-depleted solution, and(v) mixing an aromatic oil having a boiling point above the boiling point of the solvent and solvency properties for residual asphaltene components in the first solution into the first solution prior to the heating step.2. A process according to in which the light paraffinic solvent comprises a Cto Cparaffin.3. A process according to in which the light paraffinic solvent comprises butane. ...

APPARATUS AND A METHOD FOR WASHING OF HYDROCARBON PRODUCT VAPOR

An apparatus and a method for washing hydrocarbon product vapor are disclosed. The apparatus comprises housing, a first wash zone at a predefined cross-section of the housing for receiving the hydrocarbon product vapor, a plurality of injection units located within the first wash zone at predetermined intervals of the length of the housing for receiving wash oil. The injection units inject oil droplets formed from the received wash oil to contact the vapor and obtain a primary washed hydrocarbon vapor within the first wash zone. Further, a second wash zone is located above and in fluid communication with the first wash zone for receiving the primary washed hydrocarbon vapor. One or more spray headers receive wash oil and spray oil droplets formed from the received wash oil to contact with the primary washed hydrocarbon vapor, thereby forming a secondary washed hydrocarbon vapor. 1. An apparatus for washing hydrocarbon product vapor , the apparatus comprising:a housing; 'a plurality of injection units located at predetermined intervals of a length (L) of the first wash zone adapted to inject oil droplets to contact the hydrocarbon product vapor to form a primary washed hydrocarbon vapor; and', 'a first wash zone formed within the apparatus at a predefined cross-section of the housing and adapted to receive hydrocarbon product vapor, wherein the first wash zone comprises 'one or more spray headers adapted to spray oil droplets to contact the primary washed hydrocarbon vapor to form a secondary washed hydrocarbon vapor.', 'a second wash zone located above and in fluid communication with the first wash zone within the predefined cross-section of the housing, the second wash zone adapted to receive the primary washed hydrocarbon vapor from the first wash zone, wherein the second wash zone comprises2. The apparatus as claimed in claim 1 , wherein the predetermined intervals of the length (L) of the location of the plurality of injection units across the first wash zone is ...

Deterring Aggregation of Asphaltenes by Resins

Provided herein are methods of inhibiting the aggregation of asphaltenes, as well as methods of identifying appropriate aggregation inhibitors for asphaltenes. 1. A method of selecting an aggregation inhibitor for an asphaltene , the method comprising:defining a classical force field describing an internal geometry and a charge distribution of the asphaltene;calculating an equilibrium aggregate size distribution of the asphaltene by thermal equilibration;calculating an equilibrium aggregate size distribution of the asphaltene in the presence of a potential aggregation inhibitor by thermal equilibration;wherein a decrease in the equilibrium aggregate size in the presence of the potential aggregation inhibitor indicates that the potential aggregation inhibitor is a suitable aggregation inhibitor for the asphaltene.2. The method of claim 1 , wherein the aggregation inhibitor comprises a natural resin claim 1 , a synthetic resin claim 1 , or a combination thereof.3. The method of claim 1 , wherein the aggregation inhibitor comprises a petroleum resin.4. The method of claim 1 , wherein a decrease of at least 10% claim 1 , at least 25% claim 1 , or at least 50% in the equilibrium aggregate size in the presence of the potential aggregation inhibitor indicates that the potential aggregation inhibitor is a suitable aggregation inhibitor for the asphaltene.5. The method of claim 1 , wherein when the decrease in the equilibrium aggregate size in the presence of the potential aggregation inhibitor is at least 10% claim 1 , at least 25% claim 1 , or at least 50% claim 1 , the potential aggregation inhibitor is selected as a suitable aggregation inhibitor for the asphaltene.6. The method of claim 1 , wherein the method comprises:defining a classical force field describing an internal geometry and a charge distribution of the asphaltene;calculating an equilibrium aggregate size distribution of the asphaltene by thermal equilibration;calculating an equilibrium aggregate size ...

Apparatus and process for separating asphaltenes from an oil-containing fuel

An apparatus for separation of asphaltenes from an oil-containing fuel, has a mixing element for intensive mixing of the oil-containing fuel with a solvent to form a solution supersaturated with asphaltenes, a vessel for reducing the oversaturation by depositing the asphaltenes out of the supersaturated solution, a growth zone formed within the vessel for growth of asphaltene particles present via the asphaltenes separated out of the supersaturated solution, and a classifying unit connected in terms of flow to the vessel for separation of the asphaltene particles grown in the growth zone in terms of their particle size, wherein the vessel is formed and set up such that a stream containing asphaltene particles circulates between the mixing element and the growth zone of the vessel. A corresponding process has a stream containing asphaltene particles that circulates between the mixing element and the growth zone of the vessel.

SYSTEM FOR UPGRADING RESIDUUM HYDROCARBONS

A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system. 1. A system for upgrading residuum hydrocarbons , the system comprising:a first ebullated bed hydroconversion reactor system for contacting a residuum hydrocarbon fraction and hydrogen to produce a first effluent;a second ebullated bed hydroconversion reactor system for contacting a deasphalted oil fraction and hydrogen to produce a second effluent; anda first fractionation unit to fractionate the first effluent and the second effluent to recover one or more hydrocarbon fractions comprising a vacuum residuum fraction;a solvent deasphalting unit to solvent deasphalt the vacuum residuum fraction to produce the deasphalted oil fraction and an asphalt fraction;a third ebullated bed hydroconversion reactor system for contacting the asphalt fraction and hydrogen to produce a third effluent; anda second fractionation unit to fractionate the third effluent to recover one or more hydrocarbon fractions.2. The system of claim 1 , wherein the fractionation unit is fluidly coupled to at least one of the solvent deasphalting unit claim 1 , a vacuum distillation system ...

Process to upgrade partially converted vacuum residua

Processes for upgrading partially converted vacuum residua hydrocarbon feeds are disclosed. The upgrading processes may include: steam stripping the partially converted vacuum residua to generate a first distillate and a first residuum; solvent deasphalting the first residuum stream to generate a deasphalted oil and an asphaltenes fraction; vacuum fractionating the deasphalted oil to recover a deasphalted gas oil distillate and a heavy deasphalted residuum; contacting the first distillate and the deasphalted gas oil distillate and hydrogen in the presence of a first hydroconversion catalyst to produce a product; contacting the heavy deasphalted residuum stream and hydrogen in the presence of a second hydroconversion catalyst to produce an effluent; and fractionating the effluent to recover a hydrocracked atmospheric residua and a hydrocracked atmospheric distillate

BITUMEN PROCESSING AND TRANSPORT

Methods for preparing, converting, and/or transporting bitumen are provided. Asphaltene prills, prilling processes, and converted bitumen suitable for transport are disclosed. One method for preparing bitumen for transport comprises: separating asphaltene from the bitumen to generate a deasphalted oil and asphaltene; separating the asphaltene into a first asphaltene fraction and a second asphaltene fraction, the first asphaltene fraction being less soluble in deasphalted oil and the second asphaltene fraction being more soluble in deasphalted oil; and forming an asphaltene prill comprising an inner core comprising the second asphaltene fraction and an outer layer comprising the first asphaltene fraction. Asphaltene prills disclosed herein may comprise an inner core comprising an asphaltene fraction having more solubility in deasphalted oil, and an outer layer comprising an asphaltene fraction having less solubility in deasphalted oil. Methods for the transport of bitumen via a pipeline are disclosed. 1. A converted bitumen comprising:asphaltene prills, the asphaltene prills comprising an asphaltene inner core comprising an asphaltene fraction that is more soluble in deasphalted oil and an asphaltene outer layer comprising an asphaltene fraction that is less soluble in deasphalted oil; anddeasphalted oil.2. The converted bitumen of claim 1 , wherein the deasphalted oil is visbroken deasphalted oil.3. The converted bitumen of claim 1 , wherein the asphaltene prills further comprise at least one hollow portion.4. The converted bitumen of claim 3 , wherein the at least one hollow portion is in the inner core of the asphaltene prills.5. The converted bitumen of claim 1 , wherein the converted bitumen further comprises one or more additional diluents.6. An asphaltene prill comprising:an inner core, the inner core comprising an asphaltene fraction having a first solubility in deasphalted oil; andan outer layer, the outer layer comprising an asphaltene fraction having a ...

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING STEAM CRACKING AND CONVERSION OF NAPHTHA INTO CHEMICAL RICH REFORMATE

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and conversion of naphtha to chemical rich reformate. Feeds to the mixed feed steam cracker include light products from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Chemical reformate from straight run naphtha streams is used as an additional feed to the aromatics extraction zone and or the mixed feed steam cracker. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from the vacuum gas oil hydroprocessing zone. 121.-. (canceled)22. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a gas oil hydroprocessing (GOHP) zone operable to receive and treat vacuum gas oil from the first VDU fraction and produce a first GOHP fraction ...

Properties of Hydroprocessed Base Oils

Solvent extraction is applied to a hydrotreated base oil to create at least one higher quality product stream and at least one lower quality product stream, wherein the at least one higher quality product stream includes an improvement over the hydrotreated base oil in at least one of viscosity index, low temperature properties, volatility, and oxidation stability relative to that of the feedstock. 1. A method comprising the step of applying to a hydrotreated base oil a solvent treatment comprising at least one solvent to produce at least one first base oil , and one or more additional base oils , wherein the at least one first base oil has a higher paraffinic content than occurred in the hydrotreated base oil.2. The method of wherein the hydrotreated base oil feedstock is derived from one of a crude oil feedstock and a used lubricating oil feedstock.3. The method of wherein the hydrotreated base oil has been hydrotreated under a pressure of at least 600 psig.4. The method of claim 1 , further comprising a step of utilizing in the solvent treatment at least one of a preferentially selective paraffinic solvent claim 1 , and at least one of a preferentially selective solvent for at least one of aromatic claim 1 , polar claim 1 , and naphthenic constituents.5. A method for controlling at least one of volatility and viscosity of a base oil product by applying to a hydrotreated base oil feedstock a solvent treatment in which a first base oil is created that has a VI that is greater than that of the hydrotreated base oil feedstock and a further fractionation step comprising no less than two of:a. removal of solvent from the raffinate from which the first base oil was made,b. volatility of the first base oil that is at least one of (1) less than or equal to 15% or (2) less than or equal to 13%, in each case as measured by ASTM D-5800, andc. viscosity of the first base oil that is less than that of the hydrotreated base oil feedstock.6. The method of wherein the ...

Method and Apparatus for Recovering Synthetic Oils from Composite Oil Streams

A method for recovering synthetic oils from a feed stream, the method comprising separating at least a portion of the non-synthetic oil constituents from a commingled stream to produce a partially purified synthetic oil stream and one or more contaminant streams. Extracting at least a portion of the synthetic oil from the partially purified synthetic oil stream to produce a synthetic oil stream and a second contaminant stream.

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING DELAYED COKING OF VACUUM RESIDUE

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a delayed coker unit to produce coker naphtha, which is hydrotreated and passed as additional feed to aromatics extraction zone and/or the mixed feed steam cracker, and coker gas oil range intermediates as additional feed to the gas oil hydroprocessing zone. 119.-. (canceled)20. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a delayed coking zone operable to receive and convert the second VDU fraction comprising vacuum residue into a coker naphtha stream, a coker gas oil stream and petroleum coke;a distillate hydroproces sing (DHP) zone operable to receive and convert middle ...

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM RESIDUE CONDITIONING AND BASE OIL PRODUCTION

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feed to the gas oil steam cracker in certain embodiments includes gas oil range intermediates from the vacuum residue hydrocracking zone. In addition, a base oil production center is integrated to provide base oils product used for production of synthetic lubes or corresponding lube oil feedstocks 129.-. (canceled)30. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a gas oil ...

INTEGRATED PROCESS FOR SOLVENT DEASPHALTING AND GAS PHASE OXIDATIVE DESULFURIZATION OF RESIDUAL OIL

The invention is an integrated process for treating residual oil of a hydrocarbon feedstock. The oil is first subjected to solvent deasphalting then gas phase oxidative desulfurization. Additional, optional steps including hydrodesulfurization, and hydrocracking, may also be incorporated into the integrated process. 1. An integrated process for removing metals and sulfur from a residual oil feedstock , comprising:(i) deasphalting said residual oil feedstock in a first vessel, in the presence of a paraffinic solvent, to produce a gas, asphalt and deasphalted oil (DAO);(ii) separating said gas, asphalt and DAO from each other and also from said paraffinic solvent;(iii) moving said DAO to a second vessel containing an oxidative desulfurization (ODS) catalyst;{'sub': '2', '(iv) contacting said DAO and ODS catalyst with a gaseous oxidizing agent, to form SO, a second gas, and a liquid in a gaseous ODS process to remove additional sulfur in said DAO;'}(v) separating any gas and liquid produced in (iv) from each other;(vi) removing a portion of said gas of (v) from total gas, leaving a remainder;(vii) recycling said remainder to said second vessel, and;(viii) subjecting the liquid to hydrodesulfurization (HDS) with hydrogen and an HDS catalyst.2. (canceled)3. The method of claim 1 , further comprising subjecting the liquid to hydrocracking in the presence of hydrogen and a hydrocracking catalysts.4. An integrated process for removing metals and sulfur from a residual oil feedstock claim 1 , comprising:(i) deasphalting said residual oil feedstock in a first vessel, in the presence of a paraffinic solvent, to produce a gas, asphalt and a deasphalted oil (DAO);(ii) subjecting said DAO to hydrodesulfurization (HDS) in a second vessel, in the presence of an HDS catalyst, to produce a first liquid and a first;{'sub': '2', '(iii) contacting said first liquid with an ODS catalyst and a gaseous oxidizing agent to form a second gas, a second liquid product and SO;'}(iv) separating ...

SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING VACUUM RESIDUE HYDROPROCESSING

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include one or more naphtha fractions from hydroprocessing zones within the battery limits, including vacuum residue hydrocracking, within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include gas oil range intermediates from the vacuum gas oil hydroprocessing zone and the vacuum residue hydrocracking zone. 120.-. (canceled)21. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a distillate hydroprocessing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the second DHP fraction is used for diesel fuel production;a steam cracking zone comprising a mixed feed steam cracking (MFSC) zone operable to receive and thermally crack naphtha from the first ADU fraction and a C6-C9 ...

PROCESS AND SYSTEM FOR CONVERSION OF CRUDE OIL TO PETROCHEMICALS AND FUEL PRODUCTS INTEGRATING SOLVENT DEASPHALTING OF VACUUM RESIDUE

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a solvent deasphalting unit to produce deasphalted oil as additional feed to the gas oil hydroprocessing zone. 118.-. (canceled)19. An integrated system for producing petrochemicals and fuel products comprising:an atmospheric distillation unit (ADU) operable to receive and separate a feed, and discharge a first ADU fraction comprising naphtha, a second ADU fraction comprising at least a portion of middle distillates from the feed, and a third ADU fraction comprising atmospheric residue;a vacuum distillation unit (VDU) operable to receive and separate the third ADU fraction, and discharge a first VDU fraction comprising vacuum gas oil and a second VDU fraction comprising vacuum residue;a solvent deasphalting zone operable to receive and separate the second VDU fraction comprising vacuum residue into a deasphalted oil phase and an asphalt phase;a distillate hydroproces sing (DHP) zone operable to receive and convert middle distillates from the second ADU fraction into a first DHP fraction and a second DHP fraction, wherein the first DHP fraction comprises naphtha and the ...

Apparatus for removing a contaminant from a solvent separation process

The invention is a process and apparatus for removing a contaminant from an aromatic selective solvent. A feed stream comprising an aromatic hydrocarbon and a non-aromatic hydrocarbon is contacted with the aromatic selective solvent in an extractive distillation zone to produce a raffinate stream comprising the non-aromatic hydrocarbon, and a rich solvent stream comprising the aromatic hydrocarbon and the solvent. The rich solvent stream is separated in a second distillation zone to produce an extract stream comprising the aromatic hydrocarbon, and a lean solvent stream comprising the contaminant and the aromatic selective solvent. At least a portion of the lean solvent stream is washed with a non-aromatic hydrocarbon to produce a clean solvent stream, at least a portion of which is passed to at least one of the extractive distillation zone and the second distillation zone.

STEAM DILUENT GENERATOR

A method for using untreated produced water to generate steam and simultaneously producing diluents is disclosed. The method includes a combustion process for generating steam for hydrocarbon recovery using untreated water and, an optional process for recovering combustion byproducts to assist in hydrocarbon recovery or solvent injections. Specifically, a novel combustion method and a double-tube heat exchanger are used to generate steam while minimizing or eliminating water treatment steps and boiler fouling. Low value pitch, also known as asphalt, is used for combustion fuel. In addition to the steam generation, byproducts of the combustion process can be utilized in solvent injections or as a diluent. 1. A steam generator for steam assisted oil recovery , comprising:a) a solvent de-asphalting unit (SDA) for generating hot pitch and de-asphalted oils (DAO), said SDA having an outlet for removing said hot pitch and an outlet for removing said DAO;b) a fluid bed combustion boiler having at least one inlet for introducing said hot pitch and at least one inlet for introducing air, wherein said hot pitch and said air feed the combustion process, said fluid bed combustion boiler further comprising a solid media capable of capturing metals and oxide byproducts of said combustion process; andc) a double tube heat exchanger passing through said fluid bed combustion boiler, wherein a clean steam under pressure flows through the outer tube and oilfield produced water flows through inner tube of said heat exchanger.2. The steam generator in claim 1 , further comprising a fractionator and vessel for mixing said DAO with low boiling compounds from said fractionator.3. The steam generator in claim 2 , wherein said mixtures is separated into a makeup solvent stream and a diluent by a solvent splitter.4. An apparatus for generating steam claim 2 , solvent claim 2 , and diluents for steam assisted oil recovery to produce heavy oil claim 2 , comprising:a) a solvent de-asphalting ...

APPARATUSES AND METHODS FOR ENERGY EFFICIENT SEPARATIONS INCLUDING REFINING OF FUEL PRODUCTS

In various aspects, methods and apparatuses for liquid-liquid extraction are provided. In certain aspects, an emulsion can be formed by combining a feed stream, an extractant, and a surfactant. The feed stream comprises a plurality of distinct components including a first component to be removed therefrom. The feed stream may be selected from a group consisting of: a hydrocarbon feed stream and an azeotrope. Then, a portion of the first component is extracted from the feed stream (or emulsion) by contact with a superoleophobic and hygroscopic membrane filter that facilitates passage of the first component and extractant through the superoleophobic and hygroscopic membrane filter. A purified product is collected having the portion of the first component removed. Such methods are particularly useful for refining fuels and oils and separating azeotropes and other miscible component systems. Energy-efficient, continuous single unit operation apparatuses for conducting such separation techniques are also provided. 1. A method of liquid-liquid extraction comprising:creating an emulsion by combining a feed stream, an extractant, and a surfactant, wherein the feed stream comprises a first component that is a contaminant or impurity present at an initial amount and the feed stream is selected from a group consisting of: a non-polar feed stream and an azeotrope comprising the non-polar feed stream;removing a portion of the first component from the emulsion by contacting the emulsion with a first side of a superoleophobic and hygroscopic membrane filter to facilitate passage of the first component and the extractant through the superoleophobic and hygroscopic membrane filter to a second side of the superoleophobic and hygroscopic membrane filter; andcollecting a purified product having the portion of the first component removed.2. The method of claim 1 , wherein the removing the portion of the first component by contacting includes gravity-feeding the emulsion to the first ...

HIGH CAPACITY TRAY FOR LIQUID-LIQUID TREATING

The present disclosure relates to an improved sieve tray assembly for a liquid-liquid treating column. The tray is a modular design with inlet and outlet downcomer assemblies that are mounted flush to or raised above the sieve deck upper surface. The raised downcomer assemblies provide increased surface area for light liquid upflow perforations and enhanced liquid-liquid contacting capacity and efficiency. 1. A sieve tray assembly , comprising:a sieve deck comprising a plurality of perforations;an inlet downcomer assembly coupled to the upper surface of said perforated sieve deck;an outlet downcomer assembly coupled to the upper surface of said perforated sieve deck; andan outlet downcomer pipe coupled to the outlet downcomer assembly;wherein the inlet and outlet downcomer assemblies lie outside the plane of the sieve deck.2. The sieve tray assembly of claim 1 , wherein at least one of the inlet downcomer assembly and outlet downcomer assembly further includes a riser that is positioned on the sieve deck and supports at least one of the inlet downcomer assembly and outlet downcomer assembly above the sieve deck upper surface.3. The sieve tray assembly of claim 2 , wherein the sieve deck surface area situated below either or both of the riser-equipped downcomer assemblies comprises a plurality of perforations.4. The sieve tray assembly of claim 1 , further comprising a support ring coupled to the sieve deck along a lower sieve deck surface circumferential edge.5. A liquid-liquid contacting column claim 1 , comprising a plurality of sieve tray assemblies claim 1 , wherein each sieve tray assembly comprises:a sieve deck comprising a plurality of perforations;an inlet downcomer assembly coupled to the upper surface of the perforated sieve deck;an outlet downcomer assembly coupled to the upper surface of the perforated sieve deck; andan outlet downcomer pipe coupled to the outlet downcomer assembly;wherein radially outer portions of the inlet and outlet downcomer ...

METHODS TO DECONSTRUCT ASPHALTENE IN PETROLEUM PRODUCTS

A method of chemically changing extra-heavy/heavy crude oil into lighter crude oil and incrustation deposits in the down well casing's perforation using a chemical formulation under the following condition: 1) a working solution comprising heavy naphtha mixed with the chemical formulation is added to extra-heavy/heavy crude oil at ambient temperature by circulating through a centrifugal pump until the conversion of the heavy crude oil to lighter crude oil is complete and the crude oil is ready for transportation through pipeline or other means; or 2) thermal energy and equivalent to the normal pressure present, is artificially duplicated, at the down well location of perforations to contact the asphaltene incrustations with the formulation without dilution with naphtha or the energy imparted by a centrifugal pump. 1. A method of chemically changing extra heavy and heavy crude oil into lighter crude oil , comprising adding an amount of a chemical formulation comprising a primary chemical and secondary , tertiary and quintenary chemicals , effective to result in an increase in the American Petroleum Institute (API) gravity of the crude oil , wherein the primary chemical is attracted to the resin present in the crude oil , and is acting alone or in concert with other chemicals , to allow the aromatic and saturate components present in the bulk of the crude oil to migrate across the resin that encapsulates the asphaltene , and to react with the asphaltene so as to deconstruct the asphaltene back into its aromatic and saturate building block materials.2. The method according to claim 1 , wherein the primary chemical is selected from the group consisting of transdermal chemicals used as carriers to deliver vitamins or other materials across human skin to the collagen that lies below the skin.3. The method according to claim 1 , wherein the primary chemical is selected from the group consisting of transdermal chemicals that have a flash point of greater than 200° F. with ...

SYSTEM AND METHOD FOR SOLVENT DE-ASPHALTING

A de-asphalting system for solvent de-asphalting including a desasphalter and a controller. The deasphalter defines a contacting zone and a separation zone. The contact zone contacts a feed, including asphaltenes, and a solvent to form a mixture, where the contacting of the feed and the solvent causes at least a portion of the asphaltenes to precipitate out of the mixture. The contacting is disposed at an operating temperature. The separation zone separates the mixture into a de-asphalted oil-comprising material fraction (“S+PDAO”) and a asphaltene-rich material fraction. The asphaltene-rich material fraction includes the precipitated asphaltenes. The controller controls at least one operating parameter of the deasphalter based on at least on a refractive index of the S+PDAO phase. The operating parameter is selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the mass of precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the mass of the solvent to the mass of the feed. 1. A method for solvent de-asphalting comprising:selecting a solvent based on RI; andcontacting the selected solvent with a feed including asphaltenes to effect de-asphalting.2. A de-asphalting system for solvent de-asphalting comprising: a contacting zone for contacting a feed, including asphaltenes, and a solvent to form a mixture, wherein the contacting of the feed and the solvent causes at least a portion of the asphaltenes to precipitate out of the mixture, the contacting disposed at an operating temperature; and', 'a separation zone to separate the mixture into a de-asphalted oil-comprising material fraction (“S+PDAO”) and a asphaltene-rich material fraction, the asphaltene-rich material fraction including the precipitated asphaltenes; and, 'a deasphalter, the deasphalter defininga controller for controlling at least one operating parameter of the deasphalter based on at least on a refractive index of ...

INTEGRATED PROCESS FOR PRODUCING ANODE GRADE COKE

The invention relates to processes for producing anode grade coke from whole crude oil. The invention is accomplished by first deasphalting a feedstock, followed by processing resulting DAO and asphalt fractions. The DAO fraction is hydrotreated or hydrocracked, resulting in removal of sulfur and hydrocarbons, which boil at temperatures over 370° C., and gasifying the asphalt portion in one embodiment. This embodiment includes subjecting hydrotreated and/or unconverted DAO fractions to delayed coking. In an alternate embodiment, rather than gasifying the asphalt portion, it is subjected to delayed coking in a separate reaction chamber. Any coke produced via delayed coking can be gasified. 124-. (canceled)25. A method for producing anode grade coke , comprising:(i) solvent deasphalting a hydrocarbon feedstock to produce an asphalt fraction and a deasphalted oil (DAO) fraction, in a first reaction chamber;(ii) processing said DAO fraction and asphalt fraction in separate, second, third, and fourth reaction chambers;(iii) hydrocracking said DAO fraction to remove sulfur and nitrogen therefrom and distill any hydrocarbons contained in said DAO fraction which have a boiling point over 370° C., in a series of multiple chambers;(iv) subjecting any hydrotreated or unconverted DAO fraction to delayed coking in a third chamber, and(v) gasifying said asphalt fraction via combining it with oxygen and steam, in said fourth reaction chamber, to produce hydrogen therefrom.26. The method of claim 25 , further comprising gasifying any coke produced in step (iv).27. The method of claim 25 , comprising introducing any hydrogen produced in said third reaction chamber into said second reaction chamber.28. The method of claim 25 , wherein said hydrocarbon feedstock is crude oil and said solvent deasphalting comprises mixing said crude oil with a paraffinic solvent containing C-Ccarbon atoms claim 25 , at a temperature and a pressure below critical temperature and critical pressure of ...

METHOD AND DEVICE FOR SEPARATING ASPHALTENES FROM AN ASPHALTENE-CONTAINING FUEL

A method for separating asphaltenes from an asphaltene-containing fuel, wherein fuel is supplied to a separation unit in which a sub-stream with low-boiling fuel components of the fuel is separated. After separation of the sub-stream the fuel is supplied to a deasphalting unit in which asphaltenes contained in the fuel are separated by a solvent. After the separation of the asphaltenes from the fuel, the solvent is separated therefrom in a solvent recovery unit. The separated solvent is circulated back into the deasphalting unit, and a solvent fraction is obtained from the sub-stream that has been separated from the fuel, which is supplied to the deasphalting unit in addition to the solvent recirculated from the solvent recovery unit. A device is adapted for separating asphaltenes from an asphaltene-containing fuel. 121.-. (canceled)22. A method for separating asphaltenes from an asphaltene-containing fuel , the method comprising:supplying the fuel to a separation unit, in which a substream comprising low-boiling fuel components is separated from the fuel,supplying the fuel, after separation of the substream, to a deasphalting unit, in which asphaltenes contained in the fuel are separated by a solvent, wherein the solvent, after separation of the asphaltenes from the fuel in a solvent recovery unit, is separated therefrom,recircuating the separated solvent to the deasphalting unit,obtaining a solvent fraction from the substream separated from the fuel, which, in addition to the solvent recirculated from the solvent recovery unit, is supplied to the deasphalting unit,supplying the substream depleted in the separating unit comprising low-boiling fuel components to a high-performance turbine,supplying the deasphalted fuel purified by the deasphalting unit to a standard turbine, andwhen the turbine-specific heavy metal tolerance limit of the vanadium component in the deasphalted fuel in the standard turbine is exceeded, adding low-boiling fuel components to the ...

Apparatus and process for producing light olefins by catalytic and steam cracking

The present invention relates to an NCC process and an apparatus for producing light olefins and aromatics, wherein the fraction comprising ethane and/or propane (12) from the cracking effluent is sent at least partly into a steam cracking furnace (19), fed with steam (20), to produce a steam cracking effluent (21) comprising ethylene and/or propylene.

Processing a hydrocarbon stream using supercritical water

A bitumen stream is upgraded by heating to near-critical or super-critical conditions in the stream. The bitumen stream may be from a water-based extraction process, an in situ bitumen recovery process, or a solvent-based bitumen extraction process. To achieve an appropriate feed stream composition, water and/or clay may be added. The clay offers a catalytic effect. To achieve an appropriate feed stream composition, water may alternatively be removed.

INTEGRATED MULTI-STAGE SOLVENT DEASPHALTING AND DELAYED COKING PROCESS TO PRODUCE HIGH QUALITY COKE

Process embodiments for producing high grade coke and fuel grade coke from residual oil comprises: introducing the residual oil and a first paraffinic solvent having a carbon number Cto a first solvent deasphalting unit to produce a high quality deasphalted oil (HQDAO) fraction and a first asphalt fraction; passing the HQDAO fraction to a delayed coker to produce green coke; passing at least a portion of the first asphalt fraction and a second paraffinic solvent carbon number of Cto a second solvent deasphalting unit to produce a low quality deasphalted oil (LQDAO) fraction and a second asphalt fraction; and passing the LQDAO fraction to the delayed coker to produce the fuel grade coke. 1. A system for producing green coke and fuel grade coke from residual oil comprising:{'sub': 'n', 'a first solvent deasphalting unit configured to produce a high quality deasphalted oil (HQDAO) fraction and a first asphalt fraction from the residual oil and a first paraffinic solvent having a carbon number C;'}{'sub': 'n+1', 'a second solvent deasphalting unit downstream of the first solvent deasphalting unit, the second solvent deasphalting unit being configured to produce a low quality deasphalted oil (LQDAO) fraction and a second asphalt fraction from the first asphalt fraction and a second paraffinic solvent having carbon number of C; and'}a delayed coker in fluid communication with the first solvent deasphalting unit and the second solvent deasphalting unit, wherein the delayed coker is configured to produce green coke from the HQDAO fraction and is configured to produce fuel coke from the LQDAO fraction.2. The system of claim 1 , further comprising an adsorption column disposed downstream of the first solvent deasphalting unit and upstream of the delayed coker.3. The system of claim 2 , where the adsorption column comprises at least one packed column.4. The system of claim 1 , further comprising a first hydrotreater disposed downstream of the first solvent deasphalting unit ...

Method

The present invention provides a steam-based method and system for recovering and processing a hydrocarbon mixture from a subterranean formation. The method comprises: (i) injecting steam into said formation to mobilise said hydrocarbon mixture; (ii) recovering said mobilised hydrocarbon mixture, wherein said mobilised hydrocarbon mixture comprises water and hydrocarbon; (iii) separating said hydrocarbon mixture to produce separated water and separated hydrocarbon, wherein a diluent is added to said mobilised hydrocarbon mixture prior to said separation; (iv) deasphalting said separated hydrocarbon to produce a deasphalted hydrocarbon and asphaltenes; (v) combusting said asphaltenes in an oxycombustion process to generate steam and/or energy and C0 2 ; and (vi) injecting said steam produced in step (v) into said formation and/or applying said energy produced in step (v) to generate steam and injecting said steam into said formation; wherein said method is at least partially self-sufficient in terms of steam generation and said method is at least partially self-sufficient in terms of diluent.

Supercritical water upgrading process to produce high grade coke

Embodiments of a process for producing high grade coke from crude oil residue include at least partially separating, in a solvent extraction unit, the crude oil residue into a deasphalted oil (DAO)-containing stream and an asphaltene containing-stream, producing a pressurized, heated DAO-containing stream, where the pressurized, heated DAO-containing stream, mixing a supercritical water stream with the pressurized, heated DAO-containing stream to create a combined feed stream, introducing the combined feed stream to an upgrading reactor system operating at supercritical temperature and pressure to yield one or more upgrading reactor output streams comprising upgraded product and a slurry mixture, where the slurry mixture comprises sulfur and one or more additional metals. The process also may include calcining the slurry mixture at a temperature of from 700° C. to 1900° C. to produce a product stream comprising the high grade coke.

RAPID ESTIMATION OF FEED POTENTIAL FOR BASE OIL FORMATION

Methods are provided for rapidly characterizing a feedstock being considered for lubricant base oil production in order to determine the viscosity index potential of the feedstock. It has unexpectedly been discovered that the DDVI value for a feedstock at a specified pour point can be predicted based on a) the feed distillate residual wax content at a temperature as determined by Differential Scanning Calorimetry, such as the feed distillate residual wax content at a temperature corresponding to the specified pour point temperature; b) the feed distillate refractive index; c) the feed distillate kinematic viscosity at a temperature, such as kinematic viscosity at 100° C.; and d) the distillate volume-averaged boiling point. Based on this unexpected correlation, the VI potential of a feedstock can be determined based on measurement of properties that can be performed on a time scale corresponding to one or a few days using a few milliliters of feedstock. 1. A method for determining feedstock quality for lubricant base oil production , comprising:determining a wax content of a distillate feedstock fraction by differential scanning calorimetry;obtaining a characteristic boiling point, a characteristic viscosity, and a refractive index for the distillate feedstock fraction;calculating a distillate dewaxed viscosity index (DDVI) at a DDVI-temperature for the distillate feedstock fraction based on the determined wax content and at least two of the obtained characteristic boiling point, the obtained characteristic viscosity, and the obtained refractive index, the calculated DDVI being at least 0 at the DDVI-temperature; andprocessing the feedstock to form a lubricant base oil having a viscosity index of at least 80 and a pour point of 0° C. or less.2. The method of claim 1 , wherein the DDVI-temperature is −9° C.3. The method of claim 1 , wherein the wax content of the distillate feedstock fraction is determined based on the relationship W=ΔH/A(T) claim 1 , where W is the ...

METHOD FOR TREATING A HYDROCARBON FEEDSTOCK COMPRISING A DEASPHALTING STEP AND AN ASPHALT CONDITIONING STEP

The invention relates to a process for treating a hydrocarbon-based feedstock, comprising a) a step of extracting the feedstock, b) a step of separating the fraction comprising de-asphalted oil, c) an optional step of injecting a withdrawal flux into the fraction comprising asphalt, d) an optional step of separating the fraction comprising asphalt and solvent or solvent mixture obtained from the extraction step a), e) an optional step of injecting a withdrawal flux into the asphalt fraction alone or as a mixture with a withdrawal flux obtained from step d) and an integrated step of conditioning the asphalt fraction obtained from steps a) and/or c) and/or d) and/or e), in solid form, performed in successive or simultaneous substeps. 1. Process for treating a hydrocarbon-based feedstock containing hydrocarbons with a content of C7 asphaltenes of at least 1% by mass relative to the feedstock , an initial boiling point of at least 340° C. , and a final boiling point of at least 600° C. , said process comprising the following steps:a) a step of extracting the feedstock using a solvent or a solvent mixture making it possible to obtain, on the one hand, at least one fraction comprising asphalt and solvent or solvent mixture, and, on the other hand, at least one fraction comprising de-asphalted oil and solvent or solvent mixture,b) a step of separating the fraction comprising de-asphalted oil and solvent or solvent mixture obtained from the extraction step a), making it possible to separate the de-asphalted oil from the solvent or solvent mixture introduced into the extraction step a),c) an optional step of injecting a withdrawal flux into the fraction comprising asphalt and solvent or solvent mixture obtained from the extraction step a),d) an optional step of separating the fraction comprising asphalt and solvent or solvent mixture obtained from the extraction step a), optionally as a mixture with the withdrawal flux introduced during the optional step c), making it ...

Integrated desulfurization and denitrification process including mild hydrotreating and oxidation of aromatic-rich hydrotreated products

Reduction of sulfur-containing and nitrogen-containing compounds from hydrocarbon feeds is achieved by first contacting the entire feed with a hydrotreating catalyst in a hydrotreating reaction zone operating under mild conditions to convert the labile organosulfur and organonitrogen compounds. An extraction zone downstream of the hydrotreating reaction zone separates an aromatic-rich fraction that contains a substantial amount of the remaining refractory organosulfur and organonitrogen compounds. The aromatic-lean fraction is substantially free of organosulfur and organonitrogen compounds, since the non-aromatic organosulfur and organonitrogen compounds were the labile organosulfur and organonitrogen compounds which were initially removed by mild hydrotreating. The aromatic-rich fraction is oxidized to convert the refractory organosulfur and organonitrogen compounds to oxidized sulfur-containing and nitrogen-containing hydrocarbon compounds. These oxidized organosulfur and organonitrogen compounds are subsequently removed.

PROCESS TO REMOVE ASPHALTENE FROM HEAVY OIL BY SOLVENT

Embodiments of the disclosure produce a method and system for deasphalting a hydrocarbon feed. The hydrocarbon feed and a first solvent is combined using a Taylor-Couette mixer to form a mixed stream. The mixed stream and a second solvent are introduced to an extractor to produce a first deasphalted oil stream and a pitch stream. The first deasphalted oil stream is introduced to a solvent recovery unit to recover the first solvent and the second solvent via a recovered solvent stream and to produce a second deasphalted oil stream. 1. A method for deasphalting a hydrocarbon feed , the method comprising the steps of:combining the hydrocarbon feed and a first solvent using a Taylor-Couette (TC) mixer to form a mixed stream, wherein the hydrocarbon feed comprises asphaltenes;introducing the mixed stream and a second solvent to an extractor to produce a first deasphalted oil stream and a pitch stream, wherein the first deasphalted oil stream is substantially in the absence of the asphaltenes, wherein the pitch stream comprises the asphaltenes; andintroducing the first deasphalted oil stream to a solvent recovery unit to recover the first solvent and the second solvent via a recovered solvent stream and to produce a second deasphalted oil stream, wherein the second deasphalted oil stream is substantially in the absence of the first solvent and the second solvent.2. The method of claim 1 , wherein the hydrocarbon feed is selected from the group consisting of: an atmospheric residue fraction claim 1 , a vacuum residue fraction claim 1 , and combinations thereof.3. The method of claim 1 , further comprising the steps of:pressurizing the hydrocarbon feed to a pressure ranging between 2 MPa and 4 MPa; andheating the hydrocarbon feed to a temperature ranging between 150 deg. C. and about 350 deg. C.4. The method of claim 1 , further comprising the step of:pressurizing the first solvent to a pressure ranging between 2 MPa and 4 MPa.5. The method of claim 1 , wherein the first ...

Solvent recovery system below supercritical conditions

A system and process for solvent recovery after sonic treatment of heavy oil feedstocks is disclosed. The system avoids supercritical variations. The separation process involves solvent selection and use of a proprietary sonic reactor. The solvent recovery process may include pressure variations to solvent materials in order to obtain separation from of solvents from separated asphaltenes or deasphalted oil at high temperatures. The applied pressure variations allow the separation to occur avoiding supecritical states in the solvent materials.

METHOD AND APPARATUS FOR PRODUCING UNCONVENTIONAL OIL AT SHALLOW DEPTHS

An oil production well is drilled into a kerogenous chalk source rock comprising (i) type IIs kerogen and (ii) shallow naturally-occurring unconventional oil derived from the type IIs kerogen that is resident within pore space of the source rock. In some embodiments, the production well is drilled at a location where the geothermal gradient is at least 3 degrees C. per 100 m is present at or near the production well. It is believed that the presence of this geothermal gradient accelerated maturation of the type IIs kerogen of the source rock to convert a portion of the type IIs kerogen into the unconventional oil. In some embodiments, the shallow production well is non-vertical. In some embodiments, at depths that are shallow and within the source rock, the production well is cased and perforated. Oil from the source rock may be produced via the production well and the shallow-depth perforated locations thereof. 1. A method of unconventional oil production comprising:a. drilling a production well into a kerogenous chalk source rock comprising (i) type IIs kerogen and (ii) shallow naturally-occurring unconventional oil derived from the type IIs kerogen that is resident within pore space of the source rock;b. at shallow depths of at most 2 kilometers and within the source rock, casing and perforating the production well; andc. producing the shallow naturally-occurring unconventional oil from the source rock via the production well.2. The method of wherein a location at which the production well is drilled is selected in accordance with a geothermal gradient.3. The method of any preceding claim wherein the production well is drilled at a location where the geothermal gradient is at least 3.0 degrees Celsius per 100 meters claim 1 , or at least 3.5 degrees Celsius per 100 meters claim 1 , or at least 4.0 degrees Celsius per 100 meters.4. The method of any preceding claim wherein the unconventional oil and at least some of the perforations of the production well are ...

METHODS AND SYSTEMS FOR PROCESSING CELLULOSIC BIOMASS

Separation of a product of digestion of cellulosic biomass solids may be challenging due to the various components contained therein. Methods and systems for processing cellulosic biomass, particularly a reaction product of a hydrothermal reaction containing lignin-derived products, such as phenolics, comprise providing the reaction product of a further processing (such as condensation reaction) to a non-aqueous stream to at least part precipitate the lignin and removing the precipitated lignin. 1. A method comprising:heating cellulosic biomass solids, molecular hydrogen, a catalyst capable of activating molecular hydrogen, and a digestion solvent in a reactor in a first reaction zone to produce a first reaction product;optionally providing at least a portion of the first reaction product to a gas separator unit to recover a vapor fraction comprising compounds with a normal boiling point of 100 degrees C. or lower before providing it to the separation zone;providing at least a portion of the first reaction product to a separation zone comprising a liquid-liquid phase separation unit or a liquid-liquid extraction unit to recover an aqueous stream and a non-aqueous stream, wherein the aqueous stream comprises a major portion of water in said portion of the first reaction product;providing the aqueous stream to an aqueous stream separation zone to recover light compounds from at least a portion of the aqueous phase in an overhead fraction, wherein the overhead fraction comprises a major portion of compounds with a normal boiling point of less than 150 degrees C. in said portion of the aqueous stream;providing to a further processing zone at least one of a portion of the vapor fraction, at least a portion of the aqueous phase overhead fraction, and/or at least a portion of the distillate overhead fraction to provide a higher hydrocarbon product;providing at least a portion of the higher hydrocarbon product to the non-aqueous stream to precipitate at least a portion of ...

MULTI-STAGE RESID HYDROCRACKING

Processes and systems for upgrading resid hydrocarbon feeds are disclosed. The process system may operate in two different operating modes, maximum conversion and maximum quality effluent. The process system may be reversibly transitioned between the different operating modes. The system has the ability to reversibly transition between the two modes without shutting down the system or losing production. 1. A process for upgrading resid , comprising:feeding hydrogen and a resid hydrocarbon to a first ebullated bed reactor containing a first hydrocracking catalyst;contacting the resid and hydrogen in the presence of the hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the resid;separating a product from the first reactor into a first gas phase and a first liquid phase product;feeding hydrogen and a deasphalted oil hydrocarbon fraction and a vacuum distillate hydrocarbon fraction to a second ebullated bed reactor containing a hydrotreating catalyst;contacting the deasphalted oil hydrocarbon fraction, the vacuum distillate hydrocarbon fraction and hydrogen in the presence of the hydrotreating catalyst at conditions of temperature and pressure to hydrotreat at least a portion of the deasphalted oil hydrocarbon fraction and the vacuum distillate hydrocarbon fraction;separating a product from the second reactor into a second gas phase and a second liquid phase product;separating the second liquid phase product into a second reactor effluent and a residual fluid catalytic cracking (RFCC) feed;fractionating the first liquid phase product and the second reactor effluent to form at least one distillate hydrocarbon fraction, the vacuum distillate hydrocarbon fraction, and at least one resid hydrocarbon fraction; andfeeding the at least one resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil hydrocarbon fraction.2. The process of claim 1 , wherein the fractionating ...

INTEGRATED PROCESS FOR PRODUCING ANODE GRADE COKE

The invention relates to processes for producing anode grade coke from whole crude oil. The invention is accomplished by first deasphalting a feedstock, followed by processing resulting DAO and asphalt fractions. The DAO fraction is hydrotreated or hydrocracked, resulting in removal of sulfur and hydrocarbons, which boil at temperatures over 370° C., and gasifying the asphalt portion in one embodiment. This embodiment includes subjecting hydrotreated and/or unconverted DAO fractions to delayed coking. In an alternate embodiment, rather than gasifying the asphalt portion, it is subjected to delayed coking in a separate reaction chamber. Any coke produced via delayed coking can be gasified. 1. A method for producing anode grade coke , comprising:(i) solvent deasphalting a hydrocarbon feedstock to produce an asphalt fraction and a deasphalted oil (DAO) fraction, in a first reaction chamber;(ii) processing said DAO fraction and asphalt fraction in separate, second, third, and fourth reaction chambers;(iii) hydrocracking said DAO fraction in said second reaction chamber to remove sulfur and nitrogen therefrom and to distill any hydrocarbons contained in said DAO which have a boiling point over 370° C. wherein said second reaction chamber is a fixed bed, ebullated bed, or slurry bed chamber;(iv) subjecting any hydrotreated or unconverted DAO fraction to delayed coking in a third chamber, and(v) gasifying said asphalt fraction via combining it with oxygen and steam, in said fourth reaction chamber, to produce hydrogen therefrom.2. The method of claim 1 , further comprising gasifying any coke produced in step (iv).3. The method of claim 1 , comprising introducing any hydrogen produced in said third reaction chamber into said second reaction chamber.4. The method of claim 1 , wherein said hydrocarbon feedstock is crude oil and said solvent deasphalting comprises mixing said crude oil with a paraffinic solvent containing C-Ccarbon atoms claim 1 , at a temperature and a ...

ADDITIVES FOR SUPERCRITICAL WATER PROCESS TO UPGRADE HEAVY OIL

A method of upgrading a petroleum feedstock, the method comprising the steps of introducing a disulfide oil, a water feed, and a petroleum feedstock to a supercritical water upgrading unit, and operating the supercritical water upgrading unit to produce a product gas stream, a product oil stream, and a used water stream. 1. A system for upgrading a petroleum feedstock , the system comprising:a disulfide oil unit, the disulfide oil unit is operable to produce a disulfide oil from a disulfide oil unit feed, where the disulfide oil comprises disulfides, wherein the disulfides comprise sulfur-containing compounds of the form Ci-SS-Cj, where C refers to carbon, where S refers to sulfur, where i is selected from 1, 2, 3, 4, 5, and 6, where j is selected from 1, 2, 3, 4, 5, and 6, wherein the disulfide oil comprises a total sulfur content of greater than 30% by weight;a supercritical water upgrading unit, the supercritical water upgrading unit operable to produce a product gas stream, a product oil stream, and a used water stream, wherein a supercritical water reactor of the supercritical water upgrading unit is operated at a temperature between 380 deg C. and 600 deg C. and a pressure in the range between 3203 psig and 5150 psig.2. The system of claim 1 , where the supercritical water upgrading unit comprises:a petroleum mixer, the petroleum mixer operable to mix the disulfide oil and a petroleum feedstock to produce a mixed petroleum stream;a petroleum pump, the petroleum pump operable to increase a pressure of the mixed petroleum stream to produce a pressurized petroleum stream;a petroleum heater, the petroleum heater operable to increase a temperature of the pressurized petroleum stream to produce a hot petroleum stream;a mixer, the mixer operable to mix the hot petroleum stream and a supercritical water stream to produce a mixed feed;a supercritical water reactor, the supercritical water reactor operable to produce a modified stream, where conversion reactions occur ...

INTEGRATED SOLVENT DEASPHALTING, HYDROTREATING AND STEAM PYROLYSIS SYSTEM FOR DIRECT PROCESSING OF A CRUDE OIL

A system is provided integrating a steam pyrolysis zone integrated with a solvent deasphalting zone and a hydrotreating zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. 1. An integrated solvent deasphalting , hydrotreating and steam pyrolysis system for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the system comprising:a solvent deasphalting zone having a deasphalted and demetalized oil stream outlet and a bottom asphalt outlet;a catalytic hydroproces sing zone in fluid communication with the deasphalted and demetalized oil stream outlet of the solvent deasphalting zone, the catalytic hydroprocessing zone having inlet for receiving a mixture of the deasphalted and demetalized oil stream and hydrogen recycled from a steam pyrolysis product stream effluent, and make-up hydrogen as necessary, and an outlet for discharging a hydroprocessed effluent, the catalytic hydroprocessing zone including a reactor operating under conditions effective to produce a hydroprocessed effluent; a thermal cracking convection section with an inlet in fluid communication with the hydroprocessing zone outlet, and an outlet, and', 'a thermal cracking pyrolysis section having an inlet in fluid communication with the outlet of the convection section and the light fraction outlet, and a pyrolysis section outlet;, 'a thermal cracking zone including'}a quenching zone in fluid communication with the pyrolysis section outlet, the quenching zone having an outlet for discharging an intermediate quenched mixed product stream and an outlet for discharging quenching solution;a product separation zone in fluid communication with the quenching zone outlet, and the product separation zone having a hydrogen outlet, one or more olefin product outlets and one or more pyrolysis fuel oil outlets; anda hydrogen purification zone in fluid communication with the product separation zone hydrogen outlet, the ...

UPGRADING CHALLENGED FEEDS AND PITCHES PRODUCED THEREFROM

A method for producing pitch can include: hydroprocessing a challenged feed from a refinery operation to produce a hydroprocessed product; distilling the hydroprocessed product to yield one or more upgraded fractions and a resid fraction; and solvent deasphalting the resid fraction to yield a deasphalted oil stream and a hydroprocessed pitch stream. The resultant pitch can have a micro carbon residue (MCR) of 50 wt % or greater, a solubility in toluene of 95 wt % or greater, and a softening point of 200° C. or less. The pitch can optionally be fluxed with a fluxing solvent. 1. A method comprising:hydroprocessing a challenged feed from a refinery operation to produce a hydroprocessed product;distilling the hydroprocessed product to yield one or more upgraded fractions and a resid fraction; andsolvent deasphalting the resid fraction to yield a deasphalted oil stream and a hydroprocessed pitch stream.2. The method of further comprising:blending the challenged feed with a co-feed and/or hydroprocessing solvent before hydroprocessing.3. The method of further comprising:performing the hydroprocessing in the presence of hydrogen.4. The method of claim 1 , wherein products consist of the one or more upgraded fractions claim 1 , the deasphalted oil stream claim 1 , and the hydroprocessed pitch stream claim 1 , and wherein the pitch is 1 wt % to 35 wt % of the total product.5. The method of claim 1 , wherein the pitch has a softening point of 50° C. to 200° C.6. The method of claim 1 , wherein the pitch has a T10 distillation point of 800° F. (427° C.) to 1300° F. (704° C.).7. The method of claim 1 , wherein the pitch has a T50 distillation point of 1000° F. (538° C.) to 1500° F. (815° C.).8. The method of claim 1 , wherein the pitch has a micro carbon residue (MCR) of 50 wt % to 95 wt %.9. The method of claim 1 , wherein the pitch has a solubility in toluene of 95 wt % to 100 wt %.10. The method of claim 1 , wherein the pitch has comprises 0.1 wt % to 15 wt % saturated ...

CONVERSION OF CRUDE OIL INTO LOWER BOILING POINT CHEMICAL FEEDSTOCKS

Methods and systems of producing chemical feedstocks from crude oil can include: introducing a fraction of crude oil into a catalytic hydrovisbreaker reactor, wherein the crude oil fraction is dealkylated after introduction; introducing a product stream from the catalytic hydrovisbreaker reactor and a solvent into a solvent de-asphalter unit; and introducing de-asphalted oil from the unit into a two-stage hydrocracker to produce the chemical feedstocks. The crude oil fraction can be atmospheric residue or vacuum residue. The chemical feedstocks can include C gases, C-Cgases, naphtha, BTX, and gas oil. The chemical feedstocks can be used to produce olefins and polymers. 1. A method of producing chemical feedstocks from crude oil comprising:introducing a fraction of crude oil into a catalytic hydrovisbreaker reactor, wherein the crude oil fraction is dealkylated after introduction;introducing a product stream from the catalytic hydrovisbreaker reactor and a solvent into a solvent de-asphalter unit; andintroducing de-asphalted oil from the unit into a two-stage hydrocracker to produce the chemical feedstocks.2. The method according to claim 1 , further comprising introducing crude oil into an atmospheric pipe still claim 1 , wherein the crude oil fraction is atmospheric residue.3. The method according to claim 1 , further comprising introducing atmospheric residue into a vacuum pipe still claim 1 , wherein the crude oil fraction is vacuum residue.4. The method according to claim 1 , further comprising introducing a micro-catalyst precursor and a source of hydrogen into the catalytic hydrovisbreaker reactor with the crude oil fraction claim 1 , wherein the micro-catalyst precursor comprises one or more elements or compounds that are oil-soluble claim 1 , capable of forming a sulfide claim 1 , and capable of transferring hydrogen atoms to crude oil fraction radicals.5. The method according to claim 4 , wherein the one or more elements or compounds are selected from ...

INTEGRATED SOLVENT DEASPHALTING AND STEAM PYROLYSIS SYSTEM FOR DIRECT PROCESSING OF A CRUDE OIL

A system is provided integrating a steam pyrolysis zone integrated with a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. 1. An integrated solvent deasphalting and steam pyrolysis system for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the system comprising:a solvent deasphalting zone having a deasphalted and demetalized oil stream outlet and a bottom asphalt outlet; a thermal cracking convection section with an inlet in fluid communication with the deasphalted and demetalized oil stream outlet of the solvent deasphalting zone, and an outlet, and', 'a thermal cracking pyrolysis section having an inlet in fluid communication with the outlet of the convection section and the light fraction outlet, and a pyrolysis section outlet;, 'a thermal cracking zone including'}a quenching zone in fluid communication with the pyrolysis section outlet, the quenching zone having an outlet for discharging an intermediate quenched mixed product stream and an outlet for discharging quenching solution; anda product separation zone in fluid communication with the quenching zone outlet, and having a hydrogen outlet, one or more olefin product outlets and one or more pyrolysis fuel oil outlets.2. The integrated system of claim 1 , further comprising:a first compressor zone having an inlet in fluid communication with the quenching zone outlet discharging an intermediate quenched mixed product stream and an outlet discharging a compressed gas mixture;a caustic treatment unit having an inlet in fluid communication with the multi-stage compressor zone outlet discharging a compressed gas mixture, and an outlet discharging a gas mixture depleted of hydrogen sulfide and carbon dioxide; anda second compressor zone having an inlet in fluid communication with the caustic treatment unit outlet, and an outlet for discharging compressed cracked gas;a dehydration zone having ...

INTEGRATED HYDROTREATING, SOLVENT DEASPHALTING AND STEAM PYROLYSIS SYSTEM FOR DIRECT PROCESSING OF A CRUDE OIL

A system is provided integrating a steam pyrolysis zone with a hydrotreating zone and a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. 1. An integrated hydrotreating , solvent deasphalting and steam pyrolysis system for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the system comprising:a catalytic hydroprocessing zone having inlet for receiving the crude oil feedstream and hydrogen recycled from a steam pyrolysis product stream effluent, and make-up hydrogen as necessary, and an outlet for discharging a hydroprocessed effluent, the catalytic hydroprocessing zone including a reactor operating under conditions effective to produce a hydroprocessed effluent;a solvent deasphalting zone in fluid communication with the hydroprocessed effluent outlet of the catalytic hydroprocessing zone having an inlet for receiving the hydroprocessed effluent and an outlet for a deasphalted and demetalized oil stream and an outlet for a bottom asphalt; a thermal cracking convection section with an inlet in fluid communication with the deasphalted and demetalized oil stream outlet, and an outlet, and', 'a thermal cracking pyrolysis section having an inlet in fluid communication with the outlet of the convection section and the light fraction outlet, and a pyrolysis section outlet;, 'a thermal cracking zone including'}a quenching zone in fluid communication with the pyrolysis section outlet, the quenching zone having an outlet for discharging an intermediate quenched mixed product stream and an outlet for discharging quenching solution;a product separation zone in fluid communication with the intermediate quenched mixed product stream outlet, and having a hydrogen outlet, one or more olefin product outlets and one or more pyrolysis fuel oil outlets; anda hydrogen purification zone in fluid communication with the product separation zone hydrogen outlet, the ...

Fluid compositions and methods for using cross-linked phenolic resins

A cross-linked phenolic resin demulsifier may be added to a water-in-oil emulsion having at least one foulant therein. The demulsifier may separate at least a portion of the foulant(s) from the water-in-oil emulsion, and the separated foulant(s) may be removed from the water-in-oil emulsion. In a non-limiting embodiment, the amount of the demulsifier present in the water-in-oil emulsion may range from about 0.1 ppm to about 50,000 ppm.

System and Method for Reducing Mutagenicity in Petroleum Aromatic Extracts

System and method for reducing mutagen levels contained within a volume of petroleum aromatic extracts. The petroleum aromatic extracts are mixed with at least one solvent. This produces a mixture. Once mixed, some of the petroleum aromatic extracts dissolve. Others settle in the mixture. The petroleum aromatic extracts that have settled on the mixture are removed from the mixture and are ready for use. The mixture is heated to evaporate the solvent from the mixture. The evaporated solvent can be recaptured and reused. The residuum of the mixture contains petroleum aromatic extracts that can be partially recovered using traditional hydroprocessing techniques. 1. A method of reducing mutagen levels contained within petroleum aromatic extracts , said method comprising the steps of:refining a petroleum oil, therein producing a byproduct of petroleum aromatic extracts having a first level of mutagenic compounds;mixing said petroleum aromatic extracts with at least one solvent to produce a mixture, wherein said at least one solvent is selected from a group consisting of ketones, acetone, nitriles and acetonitrile;resting said mixture to enable some of said petroleum aromatic extracts to settle;removing said petroleum aromatic extracts that have settled from said mixture, wherein said petroleum aromatic extracts removed from said mixture have a second level of mutagenic compounds that is lower than said first level of mutagenic compounds.2. The method according to claim 1 , wherein removing said petroleum aromatic extracts that have settled from said mixture leaves a residual solution claim 1 , wherein said method further includes evaporating said at least one solvent from said residual solution.3. The method according to claim 2 , wherein evaporating said at least one solvent from said residual solution produces a residuum of aromatic extracts.4. The method according to claim 3 , further including hydroprocessing said residuum of aromatic extracts.5. The method according ...

SEPARATION METHOD AND ASSEMBLY FOR PROCESS STREAMS IN COMPONENT SEPARATION UNITS

A method for removing contaminants from an process stream that includes the use of reticulated material to filter the process stream. The reticulated material also facilitate process stream flow distribution in process units. The reticulated material can be packed with a void space between a substantial number of the reticulated material that can be varied to enhance filtration and flow distribution. The method of filtering also provides a method of removing contaminants leaving process equipment. The methods can be used on a variety of process streams and process equipment. The reticulated material can include ceramics, metallic materials, and chemical vapor deposition elements. The reticulated material can be of various shapes and sizes, and can also be catalytically active. 1. A method of removing contaminants from a contaminated process stream comprising:a) providing a plurality of randomly packed reticulated elements within a process unit, wherein the reticulated elements are sized such that there is a significant and varied void space therebetween, and wherein the entire depth of the randomly packed reticulated elements is capable of filtering contaminants from the process stream; and(b) contacting the contaminated process stream with the reticulated elements to filter contaminants from the contaminated process stream on a surface of the reticulated elements while allowing the process stream to pass through the significant and varied void space between the reticulated elements to produce a substantially decontaminated process stream.2. The method of claim 1 , wherein the reticulated elements comprise a plurality of disk-shaped elements.3. The method of claim 2 , wherein the disk-shaped elements have a diameter of about 11/2 inches.4. The method of claim 1 , wherein the reticulated elements comprise a plurality of monoliths.5. The method of claim 4 , wherein the monoliths have a width and a length of about 11/2 inches.6. The method of claim 1 , wherein the ...

SEPARATION METHOD AND ASSEMBLY FOR PROCESS STREAMS IN COMPONENT SEPARATION UNITS

A method for removing contaminants from a process stream that includes the use of reticulated material to filter the process stream. The reticulated material also facilitate process stream flow distribution in process units. The reticulated material can be packed with a void space between a substantial number of the reticulated material that can be varied to enhance filtration and flow distribution. The method of filtering also provides a method of removing contaminants leaving process equipment. The methods can be used on a variety of process streams and process equipment. The reticulated material can include ceramics, metallic materials, and chemical vapor deposition elements. The reticulated material can be of various shapes and sizes, and can also be catalytically active. 1. A method of removing contaminants from a contaminated process stream comprising:a) providing a plurality of randomly packed reticulated elements within a process unit, wherein the reticulated elements are sized such that there is a significant and varied void space therebetween, and wherein the entire depth of the randomly packed reticulated elements is capable of filtering contaminants from the process stream; and(b) contacting the contaminated process stream with the reticulated elements to filter contaminants from the contaminated process stream on a surface of the reticulated elements while allowing the process stream to pass through the significant and varied void space between the reticulated elements to produce a substantially decontaminated process stream.2. The method of claim 1 , wherein the reticulated elements comprise a plurality of disk-shaped elements.3. The method of claim 1 , wherein the reticulated elements comprise a plurality of monoliths.4. The method of claim 1 , wherein the depth of the randomly packed reticulated elements within the process unit is at least six inches.56. The method of claim claim 1 , wherein the depth of the randomly packed reticulated elements ...

COMBINED PROCESS TO PRODUCE BOTH A PIPELINEABLE CRUDE AND CARBON FIBER FROM HEAVY HYDROCARBON

An integrated process that is operated to create both a higher value pipelineable crude and a higher value carbon fiber product from a lower value common heavy hydrocarbon feedstock where the feedstock is processed in a thermal reactor followed by a solvent deasphalting unit with the liquids being gathered and processed to reduce olefins for pipeline transport and the solids are processed to generate a marketable carbon fiber product with any gases generated throughout the entire process reused in the process or sold. 1. An integrated process operated to produce both a pipelineable crude product and a carbon fiber product from a heavy hydrocarbon feedstock , where the heavy hydrocarbon feedstock is processed in a thermal reactor and some of the product from the thermal reactor is treated in a solvent deasphalting unit , with produced liquids being collected and mixed and further processed to reduce olefins , to produce a liquid crude stream for pipeline transport , and with asphaltene solids produced from the solvent deasphalting unit further processed into a carbon fiber product , and where gases generated at any portion of the entire process are reused in the process or sold , the process comprising:a. introducing the heavy hydrocarbon feedstock into a heater and raising the heavy hydrocarbon feedstock temperature to a desired temperature range below the cracking temperature of the heavy hydrocarbon feedstock of 600-660° F. to produce a heated heavy hydrocarbon feedstock;b. sending the heated heavy hydrocarbon feedstock for processing to a near atmospheric thermal reactor operating at an elevated uniform bulk liquid temperature of 700-790° F. for an in-reactor residence time of (1 min to 7 hours) to create and produce a vaporized lighter heavy hydrocarbon stream and a heavier liquid hydrocarbon stream;c. condensing the lighter heavy hydrocarbon stream produced from the reactor in step b) to produce a condensed lighter heavy hydrocarbon stream;d. saturating olefins ...

OIL SANDS EXTRACTION

A process for the separation of inorganic material from unconditioned oil sands is described. The process include the steps of (a) contacting unconditioned oil sands with a light aliphatic solvent being capable of dissolving bitumen and dispersing asphaltenes present in the oil of unconditioned oil sands; under conditions permitting dispersion of the asphaltenes, to thereby produce a mass; wherein the light aliphatic solvent being selected from the group consisting of pentane, hexane, iso-hexane, neo-hexane, heptane and mixtures thereof; (b) agglomerating a significant portion of fines and coarse inorganic material from said mass obtained in step (a) and dissolving a significant portion of bitumen in the solvent, wherein the amount of solvent is adjusted to maintain dispersion of the asphaltenes, and (c) separating the agglomerated inorganic material and non-agglomerated coarse inorganic material from said mass to obtain a slurry of organic material comprising dissolved bitumen, dispersed asphaltenes and non-agglomerated fines. 151-. (canceled)52. A process for the separation of inorganic material from unconditioned oil sands , the process comprising:(a) contacting unconditioned oil sands with a light aliphatic solvent being capable of dissolving bitumen and dispersing asphaltenes present in the oil of unconditioned oil sands; under conditions permitting dispersion of the asphaltenes, to thereby produce a mass; wherein the light aliphatic solvent being selected from the group consisting of pentane, hexane, iso-hexane, neo-hexane, heptane and mixtures thereof;(b) agglomerating a significant portion of fines and coarse inorganic material from said mass obtained in step (a) and dissolving a significant portion of bitumen in the solvent, wherein the amount of solvent is adjusted to maintain dispersion of the asphaltenes, and(c) separating the agglomerated inorganic material and non-agglomerated coarse inorganic material from said mass to obtain a slurry of organic ...

Separation of solid asphaltenes from heavy liquid hydrocarbons using novel apparatus and process ("ias")

An apparatus and process is provided for improved asphaltene separation from heavy hydrocarbon or bitumen with low process complexity through mass transfer using solvent and counter-current flows, with three sections: an upper DAO/solid-asphaltene separation zone, a middle solvent mixing and segregation zone, and a bottom clarification zone. Solvent mixed with heavy hydrocarbon forms a process feed introduced to the process vessel's upper zone and exposed to counter-current solvent removing DAO from solid asphaltene particles in the feed, the particles fall through the middle zone and are mixed with introduced solvent, which introduced solvent segregates DAO-rich solution in the upper zone (for extraction from that zone) from solvent-rich mixtures in the middle mixing and lower clarification zones. Solvent flows and precipitate movement are controlled to optimize mass transfer in process, resulting in high DAO recovery and dry, solid asphaltene product.

Methods for upgrading of contaminated hydrocarbon streams

A method of upgrading a heteroatom-containing hydrocarbon feed by removing oxidized-heteroatom contaminants is disclosed. The method includes contacting the oxidized-heteroatom-containing hydrocarbon feed with a caustic and a selectivity promoter, and removing the heteroatom contaminants from the heteroatom-containing hydrocarbon feed.

FISCHER-TROPSCH SYNTHESIS USING MICROCHANNEL TECHNOLOGY AND NOVEL CATALYST AND MICROCHANNEL REACTOR

The disclosed invention relates to a process for converting a reactant composition comprising Hand CO to a product comprising at least one aliphatic hydrocarbon having at least about 5 carbon atoms, the process comprising: flowing the reactant composition through a microchannel reactor in contact with a Fischer-Tropsch catalyst to convert the reactant composition to the product, the microchannel reactor comprising a plurality of process microchannels containing the catalyst; transferring heat from the process microchannels to a heat exchanger; and removing the product from the microchannel reactor; the process producing at least about 0.5 gram of aliphatic hydrocarbon having at least about 5 carbon atoms per gram of catalyst per hour; the selectivity to methane in the product being less than about 25%. The disclosed invention also relates to a supported catalyst comprising Co, and a microchannel reactor comprising at least one process microchannel and at least one adjacent heat exchange zone. 1. A process for converting a reactant composition comprising Hand CO to a product comprising at least one aliphatic hydrocarbon having at least about 5 carbon atoms , the process comprising:flowing the reactant composition through a microchannel reactor in contact with a Fischer-Tropsch catalyst to convert the reactant composition to the product, the catalyst comprising Co supported on a support, the microchannel reactor comprising a plurality of process microchannels containing the catalyst;transferring heat from the process microchannels to a heat exchanger; andremoving the product from the microchannel reactor;the process producing at least about 0.5 gram of aliphatic hydrocarbon having at least about 5 carbon atoms per gram of catalyst per hour;the selectivity to methane in the product being less than about 25%; andflowing a regenerating fluid through the process microchannels in contact with the catalyst.2. The process of wherein each process microchannel has an internal ...

ASPHALTENE CONVERSION, SEPARATION, REMOVAL AND TRANSPORT PREPARATION FOR HEAVY HYDROCARBONS

A process to convert asphaltenes found in heavy hydrocarbon sources, remove the converted solid asphaltene portion from the hydrocarbon source at operating conditions and to prepare the separated solid asphaltenes for easier handling, storage or bulk transport, with a minimal amount of heavy hydrocarbon remaining with the asphaltenes to serve as an inherent binder for larger and robust formed solid asphaltene pieces. 116.-. (canceled)17. An agglomerated solid asphaltene product comprising: asphaltene particles; and', 'residual resin in an amount ranging between 2 wt % and 10 wt % of the solid asphaltene particulate,, 'a solid asphaltene particulate obtained from a hydrocarbon feedstock, the solid asphaltene particulate comprisingwherein the residual resin acts as an indigenous binder to enable agglomeration of the solid asphaltene particulate to form the agglomerated solid asphaltene product, andwherein the solid asphaltene particulate has a softening point above pyrolysis temperatures at atmospheric pressure.18. The agglomerated solid asphaltene product of claim 17 , wherein the solid asphaltene particulate has a melting point above pyrolysis temperatures at atmospheric pressure.19. The agglomerated solid asphaltene product of claim 17 , wherein the amount of residual resin ranges between 2 wt % and 6 wt % of the solid asphaltene particulate.20. The agglomerated solid asphaltene product of claim 17 , wherein no extraneous binder is used to obtain the agglomerated solid asphaltene product claim 17 , and the amount of residual resin is sufficient to agglomerate the solid asphaltene particulate.21. The agglomerated solid asphaltene product of claim 17 , wherein an extraneous binder is added to the solid asphaltene particulate in an amount of less than 10 wt % of the solid asphaltene particulate.22. The agglomerated solid asphaltene product of claim 17 , comprising less than 2 wt % of un-agglomerated asphaltene particles.23. The agglomerated solid asphaltene product of ...

Apparatus and Method Related to Carbon Dioxide Removal

In accordance with the present invention, disclosed herein is an apparatus and method for removing CO 2 from products by using a first acid gas absorber and a second acid gas absorber, which are both a part of a single acid gas removal unit.

APPARATUSES AND METHODS FOR ENERGY EFFICIENT SEPARATIONS INCLUDING REFINING OF FUEL PRODUCTS

In various aspects, methods and apparatuses for liquid-liquid extraction are provided. In certain aspects, an emulsion can be formed by combining a feed stream, an extractant, and a surfactant. The feed stream comprises a plurality of distinct components including a first component to be removed therefrom. The feed stream may be selected from a group consisting of: a hydrocarbon feed stream and an azeotrope. Then, a portion of the first component is extracted from the feed stream (or emulsion) by contact with a superoleophobic and hygroscopic membrane filter that facilitates passage of the first component and extractant through the superoleophobic and hygroscopic membrane filter. A purified product is collected having the portion of the first component removed. Such methods are particularly useful for refining fuels and oils and separating azeotropes and other miscible component systems. Energy-efficient, continuous single unit operation apparatuses for conducting such separation techniques are also provided. 1. A method of liquid-liquid extraction comprising:creating an emulsion by combining a feed stream, an extractant, and a surfactant, wherein the feed stream comprises a first component present at an initial amount and the feed stream is selected from a group consisting of: a hydrocarbon feed stream and an azeotrope;removing a portion of the first component from the emulsion by contacting the emulsion with a first side of a superoleophobic and hygroscopic membrane filter to facilitate passage of the first component and the extractant through the superoleophobic and hygroscopic membrane filter to a second side of the superoleophobic and hygroscopic membrane filter; andcollecting a purified product having the portion of the first component removed.2. The method of claim 1 , wherein the removing the portion of the first component by contacting includes gravity-feeding the emulsion to the first side of the superoleophobic and hygroscopic membrane filter at ambient ...

Production of hydrocarbon product and selective rejection of low quality hydrocarbons from bitumen material

Methods are described for the production of a hydrocarbon product and selective rejection of low quality hydrocarbons from a bitumen-containing material, where product quality, production yield, processing input requirements, and environmental benefits are assessed for selecting a candidate method for deployment. The methods facilitate selection and deployment of sustainable hydrocarbon production operations rather than focusing on maximizing volumetric yield of hydrocarbons.

Method for Producing Base Lubricating Oil from Oils Recovered from Combustion Engine Service

A method for producing ILSAC GF5 or higher compatible oils from used oil, comprising separating material having a boiling point less than about 350° F. from recovered oil to produce de-volatized fraction and light oil fraction. Separating material with a boiling point greater than about 350° F. and less than about 650° F. from the de-volatized oil fraction to produce fuel oil fraction and heavy oil fraction. Separating material with a boiling point greater than about 1200° F. from the heavy oil fraction to produce partially purified oil fraction and residual fraction. Treating the partially purified oil fraction to separate it into purified oil fraction and contaminant fraction. Hydrogenating the contaminant fraction to remove predetermined compounds, further saturating the fraction and thereby creating a saturated oil fraction. Fractionating the saturated oil stream to produce one or more of naphtha fraction, diesel oil fraction and base oil fraction. 1. A method for efficiently producing a high yield of ILSAC GF5 or higher compatible oils from the recovery and upgrade of oil derived from modern electric , hybrid , turbocharged , and high efficiency gasoline and diesel engines , the method comprising:a) separating at least a portion of material having a boiling point less than about 350° F. from recovered oil to produce a de-volatized oil fraction and a light oil fraction;b) separating at least a portion of material with a boiling point greater than about 350° F. and less than about 650° F. from the de-volatized oil fraction to produce a fuel oil fraction and a heavy oil fraction;c) separating at least a portion of material with a boiling point greater than about 1200° F. from the heavy oil fraction to produce a partially purified oil fraction and a residual fraction;d) treating the partially purified oil fraction to separate it into a purified oil fraction and a contaminant fraction;e) hydrogenating the contaminant fraction to remove predetermined compounds, ...

REMOVAL OF POLYNUCLEAR AROMATICS FROM SEVERELY HYDROTREATED BASE STOCKS

Adsorbents for aromatic adsorption are used to improve one or more properties of base stocks derived from deasphalted oil fractions. The adsorbents can allow for removal of polynuclear aromatics from an intermediate effluent or final effluent during base stock production. Removal of polynuclear aromatics can be beneficial for improving the color of heavy neutral base stocks and/or reducing the turbidity of bright stocks. 1. A method for making lubricant base stock , comprising:performing solvent deasphalting, under effective solvent deasphalting conditions on a feedstock having a T5 boiling point of 370° C. or more and a T50 of 510° C. or more, the effective solvent deasphalting conditions producing a yield of deasphalted oil of 40 wt % or more of the feedstock;hydroprocessing at least a portion of the deasphalted oil under first effective hydroprocessing conditions to form a hydroprocessed effluent, the at least a portion of the deasphalted oil having an aromatics content of 60 wt % or more, the hydroprocessed effluent comprising a sulfur content of 300 wppm or less, a nitrogen content of 100 wppm or less, or a combination thereof;{'sub': 5', '5, 'separating, from the hydroprocessed effluent, at least a fuels boiling range fraction, a first fraction comprising polynuclear aromatics and having a Tdistillation point of at least 370° C., and a second fraction having a Tdistillation point of at least 370° C., the second fraction having a higher kinematic viscosity at 100° C. than the first fraction;'}hydroprocessing at least a portion of the first fraction under second effective hydroprocessing conditions, the second effective hydroprocessing conditions comprising catalytic dewaxing conditions, to form a twice-hydroprocessed effluent comprising a 370° C.+ portion having a first kinematic viscosity at 100° C.; andi) exposing the at least a portion of the first fraction, prior to the hydroprocessing under second effective hydroprocessing conditions, to an adsorbent under ...

PROCESS FOR THE TREATMENT OF REFINERY PURGE STREAMS

The present invention relates to a process for the treatment of refinery purge streams, containing a hydrocarbon component in slurry phase having a boiling point higher than or equal to 140° C., characterized by the presence of quantities of asphaltenes higher than or equal to 5% by weight and characterized by the presence of a solid content higher than or equal to 5% by weight. The process provides that said purge be mixed with a suitable fluxing agent according to appropriate ratios and under certain conditions, forming a suspension with a content higher than or equal to 10% by weight of compounds having a boiling point TbP lower than or equal to 350° C. After mixing, the suspension is sent to a liquid/solid separation step which operates under suitable conditions, separating a solid phase containing a residual organic component and a solid component, called cake, and a liquid phase containing residual solids. The solid phase obtained is cooled to below 60° C., including the upper extreme, forming a granular solid which is stored and maintained at a temperature lower than or equal to 60° C. 1. A process for the treatment of refinery purge streams , the process comprising:a) withdrawing a refinery purge stream comprising a hydrocarbon component in slurry phase having a boiling point higher than or equal to 140° C., characterized by the presence of quantities of asphaltenes higher than or equal to 5% by weight and characterized by the presence of solid contents greater than or equal to 5% by weight;{'sub': 'bp', 'b) mixing said purge, at a temperature higher than or equal to 100° C., with a mixture of hydrocarbons or fluxing agent, having a total content of aromatic compounds ranging from 50% to 70% by weight, and an initial boiling point equal to or higher than the temperature at which the mixing is carried out, so as to form a suspension with a content higher than or equal to 10% by weight of compounds having a boiling point Tlower than or equal to 350° C.;'}c) ...

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker 1. A system for converting whole crudes and other heavy hydrocarbon streams to produce olefins and/or aromatics , the system comprising:a first integrated separation device configured for separating a hydrocarbon feedstock comprising the whole crudes into at least a light boiling fraction, a medium boiling fraction, and a high boiling residue fraction;a first conditioning unit, comprising a resid hydrocracking system, configured for hydrocracking the high boiling residue fraction and pyrolysis oil to produce a hydrocracked effluent;a second integrated separation device configured for separating the hydrocracked effluent to produce a fuel oil fraction and a partially conditioned fraction;a second conditioning unit configured for destructively hydrogenating the medium boiling fraction and the partially conditioned fraction to produce a steam cracker feedstream;a steam cracker configured for converting hydrocarbons in the steam cracker feedstream into one or more light olefins and the pyrolysis oil.2. The system of claim 1 , further comprising a flow line configured for feeding the light boiling fraction to the steam cracker.3. The system of claim 1 , further comprising an integrated hydrotreater configured for converting the fuel oil fraction into an ultra-low sulfur fuel oil stream.4. The system of claim 3 , wherein the integrated ...

Method for Producing Base Lubricating Oil from Waste Oil

A method for recovering base oil from waste lubricating oil by separating base oil range constituents from a waste lubricating oil mixture, thereafter separating higher quality base oil constituents and lower quality base oil constituents from the base oil recovered from the waste lubricating oil mixture and thereafter treating the lower quality base oil constituents to produce marketable base oil. The total base oil produced from a waste lubricating oil mixture by this process is greater than the quantity producible by previous processes using only base oil separation from the waste lubricating oil mixture or processes which use only treatment of the base oil recovered from the waste lubricating oil mixture to produce the product base oil. 1. A method for separating a liquid stream comprising a plurality of constituents of varied boiling points by flash distillation in at least one distillation zone comprising at least one flash distillation vessel to produce at least one overhead stream and at least one bottom stream , the method comprising:a) passing the liquid stream into a heated liquid layer contained in a flash distillation vessel and producing an overhead stream and a bottom stream and having up to one theoretical plate;b) heating the bottom stream to a selected temperature and passing a portion of the heated bottom stream to the flash distillation vessel to maintain the heated liquid layer at a selected temperature and at a selected level in the flash distillation vessel in a lower portion of the vessel;c) heating the heated liquid layer in the flash distillation vessel at a temperature sufficient to flash a portion of the liquid feed stream to the flash distillation vessel thereby producing the bottom stream and the overhead stream;d) passing at least a portion of the distillate overhead stream out of the distillation vessel.2. The method of wherein a plurality of flash distillation vessels are used.3. The method of wherein at least one of the flash ...

MEMBRANE-BASED WASHING AND DEACIDIFICATION OF OILS

Membrane-based method of washing and deacidification of oils, wherein a stream of oil is conveyed from an oil reservoir along one side of porous hydrophobic membrane, and washing aqueous solution is conveyed along another side of this membrane. The membranes form hollow fibers, and their total surface area and porosity are large enough for efficient removal of fatty acids, water, ions and hydrophilic organic impurities from oil. Membrane pore size is small enough, so that hydrodynamic mixing of oil and aqueous solution does not take place. Additional stabilization of oil/water meniscus in the pores is achieved by transmembrane pressure difference. 1. A membrane-based oil washing process to remove an excess of emulsified water , metal ions , water-soluble colored and smelly impurities , and fatty acids , comprising:a hollow fiber membrane module through which a flow of an oil solution and a flow of an aqueous solution are separated by one or more membranes of the hollow fiber membrane module.2. The membrane-based oil washing process of claim 1 , wherein the oil solution flows outside of one or more fibers of the hollow fiber membrane module and the aqueous solution flows inside the one or more fibers.3. The membrane-based oil washing process of claim 1 , wherein the oil solution and the aqueous solution are pumped in a recirculation mode from respective source vessels through the hollow fiber membrane module and then back to the respective source vessels.4. The membrane-based oil washing process of claim 1 , wherein both the oil solution and the aqueous solution flow in the same direction in a horizontal module claim 1 , thus minimizing changes of transmembrane pressure difference in the hollow fiber membrane module.5. The membrane-based oil washing process of claim 1 , wherein the membrane is porous and is made of hydrophobic polymer material claim 1 , so that the membrane pores of the one or more membranes are filled with oil.6. The membrane of claim 5 , wherein ...

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker

INTEGRATED MULTI-STAGE SOLVENT DEASPHALTING AND DELAYED COKING PROCESS TO PRODUCE HIGH QUALITY COKE

Process embodiments for producing high grade coke and fuel grade coke from residual oil comprises: introducing the residual oil and a first paraffinic solvent having a carbon number Cto a first solvent deasphalting unit to produce a high quality deasphalted oil (HQDAO) fraction and a first asphalt fraction; passing the HQDAO fraction to a delayed coker to produce green coke; passing at least a portion of the first asphalt fraction and a second paraffinic solvent carbon number of Cto a second solvent deasphalting unit to produce a low quality deasphalted oil (LQDAO) fraction and a second asphalt fraction; and passing the LQDAO fraction to the delayed coker to produce the fuel grade coke. 1. A process for producing green coke and fuel grade coke from residual oil comprising:{'sub': 'n', 'introducing the residual oil and a first paraffinic solvent having a carbon number Cto a first solvent deasphalting unit to produce a high quality deasphalted oil (HQDAO) fraction and a first asphalt fraction;'}passing the HQDAO fraction to a delayed coker to produce green coke;{'sub': 'n+1', 'passing at least a portion of the first asphalt fraction and a second paraffinic solvent carbon number of Cto a second solvent deasphalting unit to produce a low quality deasphalted oil (LQDAO) fraction and a second asphalt fraction; and'}passing the LQDAO fraction to the delayed coker to produce the fuel grade coke.2. The process of claim 1 , wherein the HQDAO fraction is passed to the delayed coker and produces green coke during a first period claim 1 , and the LDQDAO fraction is passed to the delayed coker and produce fuel grade coke during a second period claim 1 , wherein the first period occurs before the second period claim 1 , or the first period occurs after the second period.3. The process of claim 1 , wherein the HQDAO fraction and the LQDAO fraction are passed to the delayed coker simultaneously.4. The process of claim 1 , further comprising calcining the green coke to produce anode ...

PROCESS FOR PRODUCING HIGH QUALITY COKE IN DELAYED COKER UTILIZING MIXED SOLVENT DEASPHALTING

Process embodiments for producing green coke from residual oil comprise introducing residual oil and a solvent mixture into a mixing vessel to produce a feed mixture, the solvent mixture comprising at least one paraffinic solvent with a carbon number from 3 to 8 and at least one aromatic solvent, where the solvent mixture comprises from 0.1 to 10% by volume of aromatic solvent and 90 to 99.9% by volume of paraffinic solvent, passing the feed mixture to a solvent deasphalting unit to produce a deasphalted oil (DAO) fraction and an asphalt fraction, and passing the DAO fraction to a delayed coker to produce the green coke and a delayed coker effluent. 1. A process for producing green coke from residual oil comprising:introducing residual oil and a solvent mixture into a mixing vessel to produce a feed mixture, the solvent mixture comprising at least one paraffinic solvent with a carbon number from 3 to 8 and at least one aromatic solvent, where the solvent mixture comprises from 0.1 to 10% by volume of aromatic solvent and 90 to 99.9% by volume of paraffinic solvent;passing the feed mixture to a solvent deasphalting unit to produce a deasphalted oil (DAO) fraction and an asphalt fraction; andpassing the DAO fraction to a delayed coker to produce the green coke and a delayed coker effluent.2. The process of claim 1 , further comprising passing the delayed coker effluent to a fractionator unit claim 1 , where the fractionator unit separates the delayed coker effluent into separate fractionater output streams comprising: solvent and light naphtha; heavy naphtha; light coker gas oil; heavy coker gas oil; and unconverted bottoms oil.3. The process of claim 2 , further comprising recycling the solvent and light naphtha back to the mixing vessel.4. The process of claim 2 , where the solvent has a final boiling point of up to 100° C.5. The process of claim 2 , further comprising recycling the unconverted bottoms oil back to one or more of the mixing vessel and the delayed ...

METHOD AND DEVICE FOR PREPARING A VANADIUM-CONTAINING COMBUSTIBLE

A method and a device for preparing a vanadium-containing combustible in a de-asphalting device. In this way, a vanadium-containing combustible is supplied to a de-asphalting unit via a supply line in a de-asphalting device, wherein the vanadium-containing combustible supplied into the de-asphalting unit forms a first mass flow and a substantially de-asphalted combustible is discharged from the de-asphalting unit via a discharge line. A bypass line is connected to the supply line, wherein, via the bypass line, a second mass flow of the vanadium-containing combustible is directed past the de-asphalting unit in parallel to the first mass flow and supplied to the discharge line, such that a combined mass flow is formed in the discharge line. 112.-. (canceled)13. A method for preparing a vanadium-containing combustible , provided for combustion in a gas turbine , in a deasphalting device , the method comprising:feeding a vanadium-containing combustible by way of an infeed line to a deasphalting unit, wherein the vanadium-containing combustible fed into the deasphalting unit forms a first mass flow;discharging a substantially deasphalted combustible from the deasphalting unit by way of a discharge line;wherein a bypass line is connected to the infeed line;directing a second mass flow of the vanadium-containing combustible by way of the bypass line in a manner parallel with the first mass flow past the deasphalting unit and feeding to the discharge line, wherein a merged mass flow is formed in the discharge line;wherein a control valve is disposed in the infeed line, and the bypass line is connected to the control valve;measuring an exit concentration of vanadium in the combustible in the merged mass flow by a measuring device disposed in the discharge line; andcontrolling a ratio between the first mass flow and the second mass flow by the control valve so as to proceed from the exit concentration of vanadium measured in the merged mass flow;wherein the ratio between the ...

CATALYTIC CRACKING FRACTIONATION AND ABSORPTION STABILIZATION SYSTEM, AND ENERGY SAVING METHOD THEREOF

The present invention provides a catalytic cracking fractionation and absorption-stabilization system, and energy saving method thereof; the present invention is to arrange a waste heat refrigerator of the main fractionating tower, a waste heat refrigerator of rich gas and a waste heat refrigerator of stabilizer in a catalytic cracking fractionation and absorption-stabilization system so as to utilize low temperature waste heat at the top of a main fractionating tower, rich gas, stable gasoline, intermediate heat exchange flow of an absorber of the system as a refrigerator driving heat source; in order to cool naphtha and circulating gasoline to a low temperature lower than 40° C., control low temperature operations of the absorber and reduce the heat load of a desorber and a stabilizer, and the heat extracted by the refrigerators is cooled by cooling water with a higher temperature so as to reduce the consumption of the cooling water. In addition, developed residual pressure generating units and waste heat generating units coordinate to convert medium and low pressure of the dry gas and low-grade waste heat of other products in the system into electric energy that can be conveyed into a grid, therefore the electricity consumption of a dry gas compressor can be supplemented, and the operation cost of the system is reduced to the minimum. 112830318212112191032183435. A catalytic cracking fractionation and absorption-stabilization system of an oil refinery , wherein heat is extracted from the top of a main fractionating tower () by a waste heat refrigerator to serve as a refrigerator driving heat source after heat extraction so as to cool naphtha; rich gas () at the top of the main fractionating tower enters into a compressor for compression , the compressed rich gas is mixed with rich gasoline () discharged from the bottom of an absorber and desorbed gas () discharged from the top of a desorber , and the mixture enters into a gas-liquid separation tank () to reduce ...

Multistage resid hydrocracking

Processes for upgrading resid hydrocarbon feeds are disclosed. The upgrading processes may include: hydrocracking a resid in a first reaction stage to form a first stage effluent; hydrocracking a deasphalted oil fraction in a second reaction stage to form a second stage effluent; fractionating the first stage effluent and the second stage effluent to recover at least one distillate hydrocarbon fraction and a resid hydrocarbon fraction; feeding the resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil fraction.