СПОСОБ ПОЛУЧЕНИЯ КОМПОЗИЦИЙ КАТАЛИЗАТОРА ГИДРОКРЕКИНГА

Изобретение относится к способу получения селективного в отношении нафты катализатора гидрокрекинга, содержащего от 3 до 4,8 мас.% молибдена в расчете на металл и от 1,5 до 3 мас.% никеля в расчете на металл, который включает введение в тугоплавкий оксидный носитель, содержащий алюминийоксидный связующий компонент и компонент цеолита Y в количестве от 65 до 75 мас.% в расчете на общую массу катализатора, никеля и молибдена, находящихся в растворе, содержащем лимонную кислоту, где компонент цеолита Y имеет размер элементарной ячейки в диапазоне от 24,42 до 24,52 Å, молярное отношение диоксида кремния к оксиду алюминия (ДКОА) в диапазоне от 10 до 15 и площадь поверхности от 910 до 1020 м2/г. Также изобретение относится к способу гидрокрекинга углеводородного сырья, который включает контактирование сырья при повышенной температуре с каталитической композицией, полученной заявленным выше способом. Технический результат заключается в получении селективного в отношении нафты катализатора гидрокрекинга ...

IMPROVED FLUIDIZING GAS DISTRIBUTION DEVICE

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

Shutdown method of bubbling bed hydrotreating process

The invention discloses a start-up method for a fluidized-bed hydrogenation process. When a fluidized-bed hydrogenation device starts up, hot light distillate oil is pumped into a reaction without any catalyst to preheat the reactor; when the reactor is heated to a certain temperature, heavy oil feed containing dispersed catalysts is pumped into the reactor to further raise the temperature of the reactor; and then catalysts are added into the reactor through an online catalyst inlet pipe of the reactor; when the amount of the catalysts added into the reactor reaches a required storage amount of the catalysts, the catalysts are no longer added into the feed and the start0up of a device is complete and the device begins to operate normally. The start-up method simplifies start-up process, operates flexibly, ensures smooth start-up of the device and reduces operation cost.

Process of conversion catalytic of hydrocarbon mixtures containing of sulphur into products with less sulphur content and point of lower boiling

СПОСОБ ГИДРООБРАБОТКИ В КИПЯЩЕМ СЛОЕ

В реакторе кипящего слоя продукт реакции подвергают испарительному разделению высокого давления с последующим испарительным разделением среднего давления. Жидкость для поддержания кипящего слоя образуется при пропускании жидкости, полученной после разделения при высоком давлении, через эдуктор в жидкость, полученную после разделения при среднем давлении. Жидкость для поддержания кипящего слоя направляют в реактор для увеличения объема слоя катализатора до 110 - 200 об.% от объема неподвижного слоя катализатора. В результате такой рециркуляции поддерживают наилучший баланс давления, а уносимый катализатор и мелкие частицы катализатора вновь возвращаются в реактор и не попадают в другое оборудование. 4 з.п.ф-лы, 1 ил. .

ПРОЦЕСС ВО ВЗВЕШЕННОМ СЛОЕ С РЕЦИРКУЛЯЦИОННЫМ ЭДУКТОРОМ

В реакторе кипящего слоя продукт реакции подвергают испарительному разделению высокого давления с последующим испарительным разделением среднего давления. Жидкость для поддержания кипящего слоя образуется при пропускании жидкости, полученной после разделениям при высоком давлении, через эдуктор в жидкость, полученную после разделения при среднем давлении. Жидкость для поддержания кипящего слоя направляют в реактор для увеличения объема слоя катализатора до 11О-200 об. % от объема неподвижного слоя катализатора. В результате такой рециркуляции поддерживают наилучший баланс давления, а уносимый катализатор и мелкие частицы катализатора вновь возвращаются в реактор и не попадают в другое оборудование.

HYDRAULIC PROCESS OF CONVERSION

METHOD AND DEVICE FOR A PARTICLE REPLACING SYSTEM FOR COUNTER CURRENT CONTACT OF A GASEOUS ONE AND A LIQUID METAL CHARGE WITH A BULK MATERIAL BED.

IMPROVED FLUIDIZING GAS DISTRIBUTION DEVICE

DEMETALLIZATION CATALYST AND PROCESS FOR METALS- CONTAINING HYDROCARBON FEEDSTOCKS

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

MODERNIZED REACTOR OF A BOILING LAYER WITH SLIGHT POLLUTION OF SEDIMENT

PROCESS FOR the IMPROVEMENT OF the POINT Of FLOW OF PARAFFINIC LOADS WITH a CATALYST CONTAINING ZEOLITE IM-5

PROCESS FOR the IMPROVEMENT OF the POINT Of FLOW OF PARAFFINIC LOADS WITH a CATALYST CONTAINING ZEOLITE IM-5

L'invention concerne un procédé pour améliorer le point d'écoulement d'une charge comportant des paraffines de plus de 10 atomes de carbone, dans lequel la charge à traiter est mise au contact d'un catalyseur comprenant la zéolithe IM-5 et au moins un élément hydro-déshydrogénant, à une température comprise entre 170 et 500°C, une pression entre 1 et 250 bar et une vitesse volumique horaire entre 0,05 et 100 h-1, en présence d'hydrogène à raison de 50 à 2000 l/l de charge. Les huiles obtenues présentent de bons points d'écoulement et des indices de viscosité (VI) élevés. Le procédé est également applicable aux gazoles, et autres charges nécessitant la réduction de leur point d'écoulement.

METHOD AND DEVICE FOR TREATING AND SORTING AND RECYCLING OIL-CONTAINING EFFLUX CATALYST

Disclosed are a method for treating and sorting and recycling an oil-containing efflux catalyst, and a device for the method of treating and sorting and recycling an oil-containing efflux catalyst; the method for treating and sorting and recycling an oil-containing efflux catalyst comprises: (A) vortex-washing and on-line activation of an efflux catalyst; (B) vortex-rotation gas stripping of a catalyst solvent; (C) airflow acceleration sorting of the highly active catalyst; (D) vortex re-stripping and particle collection of the highly active catalyst; and (E) gas cooling, and condensation and removal of the solvent. The method for treating and sorting and recycling an oil-containing efflux catalyst has the advantages of a simple process, being easy to operate, a high oil-removal efficiency, and a high sorting efficiency of a highly active catalyst.

СПОСОБ ГИДРООБРАБОТКИ ДИСТИЛЛЯТОВ УГЛЕВОДОРОДНОГО СЫРЬЯ

Сырье углеводородного дистиллята обрабатывают водородсодержащим газом в кипящем слое частиц катализатора при определенных температуре и давлении с получением жидкого углеводородного продукта и непрореагировавшего водородсодержащего газа. Сырье и газ предварительно нагревают до определенных температур и давления и далее осуществляют теплообмен между различными потоками. Проводят раздельный теплообмен при высоком и низком давлениях для эффективного теплообмена при высоком давлении и снижения потребления топливного газа в нагревателях. Предусмотрена система постоянного контроля температуры сырьевых дистиллятов с учетом теплообмена.

ПРОЦЕСС ВО ВЗВЕШЕННОМ СЛОЕ С РЕЦИРКУЛЯЦИОННЫМ ЭДУКТОРОМ

В реакторе кипящего слоя продукт реакции подвергают испарительному разделению высокого давления с последующим испарительным разделением среднего давления. Жидкость для поддержания кипящего слоя образуется при пропускании жидкости, полученной после разделениям при высоком давлении, через эдуктор в жидкость, полученную после разделения при среднем давлении. Жидкость для поддержания кипящего слоя направляют в реактор для увеличения объема слоя катализатора до 11О-200 об. % от объема неподвижного слоя катализатора. В результате такой рециркуляции поддерживают наилучший баланс давления, а уносимый катализатор и мелкие частицы катализатора вновь возвращаются в реактор и не попадают в другое оборудование.

PROCEDURE FOR THE PROCESSING OF OLD OR WASTE PLASTICS

Process for processing used or waste plastic material

Container and process for the catalytic hydrocarbon transformation

PROCESS FOR THE IMPROVEMENT OF THE POINT OF LOAD DRAINING PARAFÍNICAS WITH A CATALYSER THE BASE OF ZEÓLITO IM-5

processo para hidroprocessamento de um óleo combustível

Process for manufacturing naphthenic base oils from effluences of fluidized catalytic cracking unit

REDUCED HOLDUP IN CATALYTIC REACTOR

A reactor for refining resid includes an elongated vertical vessel containing a bed of catalyst which is expanded or ebullated by a liquid/gas mixture. The mixture rises in an updraft through the bed and then is recirculated with an increased velocity by an ebullating pump. To reduce gas holdup of the ebullated bed and to promote a more uniform flow, the gas is entrapped by two cascaded stages of baffles which have an internal conical shape to guide, direct, and entrap the gas. One of these two stages has a shape which creates a countercurrent in the flowing liquid to deflect any catalyst particles which might otherwise be elutriated by the increased velocity.

Purification of the products of synthesis of hydrocarbons

[...]

HYDROGEN-ENRICHED FEEDSTOCK FOR FLUIDIZED CATALYTIC CRACKING PROCESS

PROCESS FOR PREPARING HYDROCRACKING CATALYST COMPOSITIONS

A process for the preparation of a naphtha-selective hydrocracking catalyst comprising of from 3 to 4.8 %wt of molybdenum, calculated as metal, and of from 1.5 to 3 %wt of nickel, calculated as metal, which comprises loading a refractory oxide support comprising an alumina binder component and a zeolite Y component in a content of from 65 to 75 wt% based on the total weight of the catalyst, with nickel and molybdenum in the presence of citric acid, wherein the zeolite Y component has a unit cell size in the range of from 24.42 to 24.52 Å, a SAR in the range of from 8 to 15, and a surface area of from 850 to 1020 m2/g.

Wallendes-Bettverfahren mit Zurückleitungseduktor

DISTILLATE HYDROGENATION PROCESS

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

... 1319314 Chemical contact process NIPPON OIL CO Ltd 19 June 1970 [21 June 1969] 29963/70 Heading B1F [Also in Division C5] A method of uniformly closely contacting solid particles with a less dense liquid and possibly a gas comprises separately introducing the solid particles and fluid into the lower portion of contact zone 5, whereby to cause substantially all of the solid particles introduced into the contact zone to move upwardly through the contact zone in intimate contact with the fluid and to pass into overflow zone 7, allowing the particles to pass from the overflow zone 7 into the settling zone 8 whereby to settle under the influence of gravity to form a layer of accumulated particles in the lower portion 11 of the settling zone, there being substantially no flow of fluid through the settling zone, recycling solid particles from the layer into the lower portion of contact zone 5, and withdrawing the fluid from the overflow zone 7 substantially free of solid particles. The method ...

Process of hydrogenation of petroleum oils

... A petroleum oil, with less than 1.0% sulphur and of which at least 10% boils above 900 DEG F., is passed in liquid slurry form with hydrogen rich gas through a reactor 9 containing a bed of 95% iron oxide/5% chromium oxide hydrogenation catalyst to effect desulphurization of not less than 80% and conversion of costituents boiling above 900 DEG F. to those boiling below 900 DEG F. of not less than 70%, the gas feed being not less than 6000 S.C.F. per barrel of oil, and recycling, either internally or externally of the reactor, maintaining an upward flow of not less than 60 gallons per minute per square foot of cross-section of the reactor to expand the reactor bed, a net effluent being removed from the reactor and treated in separator 16 to remove entrained catalyst. The recycling may exceed 10 volumes of liquid per volume of liquid feed at 1, and is effected on aslurry of catalyst and oil, by standpipe 30 and pump 32 inside the reactor and/or by recirculation line ...

METHOD AND APPARATUS FOR AN ON-STREAM PARTICLE REPLACEMENT SYSTEM FOR COUNTERCURRENT CONTACT OF A GAS AND LIQUID FEED STREAM WITH A PACKED BED

This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid at a rate insufficient to levitate the bed and with catalyst selected by a density, shape and size at a design feed rate of liquids and gas to prevent ebulation of the packed bed at the design feed rates. Catalysts are selected by measuring bed expansion in a large pilot plant run with hydrocarbon, hydrogen, and catalyst at the design pressures and flow velocities. The liquid and gas components of the feed flow into the bed in alternate annular rings across the full area of the bed. At the desired flow rate, such catalyst continually flows in a plug-like manner downwardly through the vessel by introducing fresh catalyst at the top of the bed by laminarly flowing such catalyst in a liquid stream on a periodic ...

СПОСОБ ПЕРЕРАБОТКИ ПЛАСТМАССОВОГО УТИЛЬСЫРЬЯ И ПЛАСТМАССОВЫХ ОТХОДОВ

Для получения химического сырья и компонентов жидкого топлива пластмассовое утильсырье и пластмассовые отходы деполимеризуют до перекачиваемой и летучей фаз. Летучую фазу разделяют на газовую фазу и конденсат, который подвергают стандартным нефтеперерабатывающим процессам, а перекачиваемую фазу подвергают жидкофазной гидрогенизации, газификации, швелеванию или сочетанию этих технологических операций. Деполимеризацию проводят без добавки водорода, предпочтительно при давлении 0,01-300,0 бар, преимущественно 0,1-100,0 бар, в частности 0,2-2,0 бар, при 150-470oC, преимущественно 250-450oС, и времени реакции 0,1-10,0, преимущественно 0,5-5,0 ч, и три потока продуктов отводят в количествах 15-85 мас.% деполимеризата, 10-80 мас.% конденсата, а также 5-20 мас. % газовой смеси, каждый в пересчете на исходную смесь пластмасс. 9 з.п. ф-лы, 2 табл., 3 ил.

Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoff

FLUIDIZING GAS DISTRIBUTION DEVICE

... "IMPROVED FLUIDIZING GAS DISTRUBUTION DEVICE" An improved device for distributing fluidizing gas to a bed of fluidized solids. The distribution device is arranged to maintain a bed of fluidized particles above a planar region of gas injection and allow withdrawal of solids from below the region of gas injection. The fluidizing gas is distributed to a bed of fluidized particles by a central dome and a series of horizontally extending branch pipes arranged about the periphery of the dome. In order to improve the structural integrity of the apparatus and the operation of the device, the horizontal branch pipes are attached to a knuckle region of the central dome by a series of extruded outlets that minimize stress concentrations in the branch pipe connection and locate outlet holes in the branch pipes at an elevation close to the outlet holes in the dome.

METHOD AND APPARATUS FOR ON-STREAM PARTICLE REPLACEMENT SYSTEM FOR COUNTER CURRENT CONTACT OF GAS AND LIQUID FEED STREAM WITH PACKED BED

This invention takes the advantage of circular ring path for alternate flow of gas and liquid to convey the fluids at a flow rate incapable of producing a boiling condition on catalyst bed. It takes also the advantage of the designed feeding rate for liquid and gas to choose the size, shape, and density of catalyst in order to prevent boiling on filling bed under the designed feeding rate of fluids. By said process, evenly distributed liquid hydrocarbon and hydrogen gas can be passed continuously through compacted filling bed of catalyst, and the full volume of reactor being filled with reactants is realized. The catalyst is chosen after measurement of expansion of bed layer when hydrocarbon, hydrogen, and catalyst are fed under designed pressure and flow rate in a large pilot test plant.

PROCESSING METHOD OF OLD OR WASTE ARTIFICIAL MASS

HYDROPROCESS FOR A HYDROCARBON STREAM FROM COAL TAR

A coal tar process is described. A coal tar stream is provided, and the coal tar stream is separated to provide a plurality of hydrocarbon streams. At least one of the hydrocarbon streams is hydroprocessed in a fluidized bed hydroprocessing zone with a catalyst to provide a gaseous volatile product and a solid heavy hydrocarbon product absorbed onto the catalyst. The gaseous volatile product is separated from the catalyst. The catalyst is regenerating by separating the absorbed heavy hydrocarbon product from the catalyst. The regenerated catalyst is recycled into the hydroprocessing zone.

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

UPFLOW CATALYTIC HYDROTREATING REACTOR

Catalyst structure and method of upgrading hydrocarbons in the presence of the catalyst structure

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material and any two or more metals loaded in the porous support structure selected from Ga, Ag, Mo, Zn, Co and Ce. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

VERFAHREN ZUR HERSTELLUNG EINES SCHWEFELARMEN TREIB- ODER HEIZOELS

VERFAHREN ZUR VERARBEITUNG VON ALT- ODER ABFALLKUNSTSTOFFEN

METHODE UND VORRICHTUNG FÜR EIN TEILCHENAUSWECHSELSYSTEM FÜR GEGENSTROMKONTAKT EINES GASFÖRMIGEN UND EINES FLÜSSIGEN EINSATZES MIT EINEM SCHÜTTGUTBETT.

Hydrogenation of Residuum

... 1,175,023. Hydrocracking HYDROCARBON RESEARCH Inc. 27 June, 1968, No. 30778/68. Heading C5E. A process of hydrogenating and hydrocracking a reduced crude having at least 25 volume per cent boiling above 975‹ F. comprises (a) passing said crude at a temperature in the range of 750‹ to 900‹ F. and at a pressure in the range of 1000 to 5000 p.s.i.g. together with at least 2500 SCF/BBL of hydrogen upwardly through a reaction zone in the presence of a hydrogenation type catalyst having a narrow size range, said range falling between # inch and 325 mesh (USS), whilst (b) the flow velocities of liquid and hydrogen upwardly through the catalyst are such as to expand the bed of catalyst at least 10% over the settled state volume and to maintain the catalyst in random motion in the liquid, and (c) the space velocity of the liquid is such as to accomplish more than 50% conversion of the 975‹ F. plus boiling components in the feed and to partially remove sulphur, (d) separating the effluent from the ...

Process for manufacturing naphthenic base oils from effluences of fluidized catalytic cracking unit

Disclosed is a method of manufacturing high quality naphthenic base oil by subjecting, as a feedstock, light cycle oil (LCO) and slurry oil (SLO) obtained through fluidized catalytic. cracking (FCC) to hydrotreating and dewaxing.

Improvements relating to expanded bed liquid prase hydrocarbon conversion processes and apparatus therefor

A fluidisable bed of catalyst particles is supported on a static bed consisting of 3 to 15 layers of spherical particles which are 10 to 15 times larger than the catalyst particles, a hydrocarbon liquid and if desired a gas being passed up through the stationary support particles to the catalyst bed for conversion. The gas may be introduced above the support bed, the liquid and gas being recycled. The catalyst comprises one or more metals having hydrogenating activity selected from Groups VIa and VIII of the Periodic Table, supported as an oxygen-containing refractory base, e.g. alumina, silica-alumina or an alumino-silicate. The spherical support particles may be of soda-glass.

DEMETALLIZATION CATALYST AND PROCESS FOR METALS- CONTAINING HYDROCARBON FEEDSTOCKS

A particulate synthetic catalyst material composed of substantially aluminum oxide promoted with 0.5-10 W % total metal and having total pore volume of 0.350-0.500 cc/gm for use in demetallization and hydroconversion processes for metals-containing hydrocarbon feedstocks. The catalyst material is preferably spherical shaped and provides a narrow differential size range having a particle equivalent diameter ratio range for larger to smaller particles of about 1.2-2.0, and a preferred nominal 12-18 mesh (U.S. Sieve Series) particle size range. The catalyst can be advantageously used in an ebullated bed reactor in a hydrodemetallization process for hydrocarbon feedstocks containing high metals concentration at reaction conditions of 780-850.degree.F temperature and 1000-3000 psig hydrogen partial pressure. Use of such synthetic catalyst results in improved reactor fluidization operations and low catalyst loss by attrition and carryover of fines from the reactor, and achieves improved results ...

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

GAS OIL HYDROPROCESS

A process for the hydroprocessing of a gas oil (GO) hydrocarbon feed to provide high yield of a diesel fraction. The process comprises a liquid-full hydrotreating reaction zone followed by a liquid-full hydrocracking reaction zone. A refining zone may be integrated with the hydrocracking reaction zone. Ammonia and other gases formed during the hydrotreatment are removed in a separation step prior to hydrocracking.

GAS OIL HYDROPROCESS COMPRISING A LIQUID-FULL HYDROTREATING REACTION ZONE FOLLOWED BY A LIQUID-FULL HYDROCRACKING REACTION ZONE

A process for the hydroprocessing of a gas oil (GO) hydrocarbon feed to provide high yield of a diesel fraction. The process comprises a liquid-full hydrotreating reaction zone followed by a liquid-full hydrocracking reaction zone. A refining zone may be integrated with the hydrocracking reaction zone. Ammonia and other gases formed during the hydrotreatment are removed in a separation step prior to hydrocracking.

Process for preparing hydrocracking catalyst compositions

A process for the preparation of a naphtha-selective hydrocracking catalyst comprising of from 3 to 4.8 %wt of molybdenum, calculated as metal, and of from 1.5 to 3 %wt of nickel, calculated as metal, which comprises loading a refractory oxide support comprising an alumina binder component and a zeolite Y component in a content of from 65 to 75 wt% based on the total weight of the catalyst, with nickel and molybdenum in the presence of citric acid, wherein the zeolite Y component has a unit cell size in the range of from 24.42 to 24.52 AA, a SAR in the range of from 8 to 15, and a surface area of from 850 to 1020 m2/g.

CATALYSEUR ET PROCEDE POUR L'HYDRODEMETALLISATION DE CHARGES D'HYDROCARBURES CONTENANT DES METAUX

L'INVENTION A POUR OBJET UN CATALYSEUR DE DEMETALLISATION POUR LES CHARGES DE PETROLE CONTENANT DES METAUX. LE CATALYSEUR DE L'INVENTION COMPREND DES PARTICULES CONSISTANT ESSENTIELLEMENT EN OXYDE D'ALUMINIUM ACTIVE PAR DES OXYDES DE METAUX CHOISIS PARMI LE CHROME, LE FER, LE MOLYBDENE, LE TITANE ET LE TUNGSTENE, LEDIT CATALYSEUR AYANT UNE TENEUR TOTALE EN METAUX D'ENVIRON 0,5-10 EN POIDS ET UN VOLUME DE PORES TOTAL D'ENVIRON 0,350 A ENVIRON 0,500CMG, LESDITES PARTICULES DE CATALYSEUR COMPRISES ENTRE 3 ET 97 CENTILES DE TOUTES LES PARTICULES AYANT UN RAPPORT DE DIAMETRE EQUIVALENT DES PARTICULES PLUS GROSSES AUX PARTICULES PLUS PETITES NE DEPASSANT PAS ENVIRON 2,0. APPLICATION: HYDRODEMETALLISATION ET HYDROCONVERSION CATALYTIQUES DE CHARGES DE PETROLE DONNANT DES OPERATIONS EN LIT FLUIDISE AMELIOREES AVEC DE FAIBLES PERTES DU CATALYSEUR PAR ATTRITION ET UN FAIBLE ENTRAINEMENT DE FINES HORS DU REACTEUR, AVEC UNE ELIMINATION DES METAUX DE 60-70 EN POIDS ET UNE HYDROCONVERSION DE 50-70 EN ...

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HYDROGEN-ENRICHED FEEDSTOCK FOR FLUIDIZED CATALYTIC CRACKING PROCESS

DISTRIBUTOR FOR IMPROVED GAS FLOWING

PURPOSE: To uniformly distribute gas to a bed to solid particles by using a molded connecting section having segments extending upward on an outer side in order to connect plate pipes to a knuckle part existing between a central dome and its supporting member. CONSTITUTION: The central part of the fluidized bed of the solid particles is provided with the perforated central dome 24 for distributing the gas, plural pieces of the radially and horizontally extending branch pipes 26 for distributing the gas in the annular region of the fluidized bed described above and a device which supports the dome 24 and the pipes 26 and carries the fluidizing gas to the inside of the dome 24 and the pipes 26. The doughnut-shaped knuckle 46 enclosing the periphery of the dome 24 is disposed at this device 40. A series of the branch pipe connecting parts 48 are formed at the knuckle 46 and respective branch pipe connecting sections 48 have the outlets communicating with the inside of the dome 24 and have ...

Hydrogenizing process of the organic compounds

CATALYST AND PROCESS FOR the HYDRODEMETALLISATION OF HYDROCARBON LOADS CONTAINING OF METALS

LIQUID-SOLID PARTICLE OR LIQUID-GAS-SOLID PARTICLE CONTACTING METHOD

DEVICE TO TRANSFER CATALYST FROM A LOW PRESSURE VESSEL TO A HIGH PRESSURE VESSEL AND PURGE THE TRANSFERRED CATALYST

An apparatus for the transfer of solid particulate matter from a low pressure system (30) to a high pressure system (40) is presented. The apparatus simplifies the particle transfer process, and is useful for systems where solid catalyst particles are cycled through a reactor and a regenerator.

IMPROVED DESULFURIZATION PROCESS

In a desulfurization process for the removal of organosulfur compounds from a hydrocarbon fluid stream (1), such as cracked-gasoline or diesel fuel wherein a bifunctional sorbent system (33) is employed, surface treatment of the bifunctional sorbent 40) during the use of same for desulfurization (10) results in an extension of the useful life of the bifunctional sorbent prior to the regeneration and reactivation (20) of same for further use in the desulfurization (10) of the hydrocarbon fluid stream (1).

REACTOR WITH COMBINED DYNAMIC FLOW SYSTEM FOR TREATING OIL AND DERIVATIVES THEREOF

The present invention describes a reactor (1) for treating oil and oil derivatives, which consists of a central body (2) with a countercurrent flow system interconnected to a plurality of lateral bodies (3) with a cocurrent flow system; also described is a method for treating oil and oil derivatives.

METHOD FOR CONVERTING A HEAVY HYDROCARBON FEEDSTOCK INCORPORATING SELECTIVE DEASPHALTING IN SERIES WITH RECYCLING OF A DEASPHALTED CUT

Wallendes-Bettverfahren mit Zurückleitungseduktor

Process and apparatus for contacting reactants with fluidized solid particles and the transfer of such particles

In contacting fluidized solid particles with reaction gases, the fluidized solid particles are circulated through a first vessel to a hopper and back to the first vessel, and some fluidized solids are passed periodically through a transfer line from the hopper to a second vessel and in the reverse direction by varying the pressure in the second vessel. In this way, constant fluidized bed depth and time of contact are maintained in the first vessel. The solids may be catalysts in a hydrocarbon cracking or hydrodesulphurization process; alternatively the solids may be heat transfer media or may react with the gases. In the apparatus shown, a residual hydrocarbon oil to be desulphurized enters at 30, together with hydrogen, and mixes with catalyst from pipe 26; after passage through two reaction zones 10a, 10b at 750-950 DEG F. and a pressure of 250-2000 lbs. per sq. inch, the gaseous products separate from the catalyst in hopper 16 and leave through line 20, and the catalyst ...

IMPROVED DESULFURIZATION PROCESS

REDUCED HOLDUP IN CATALYTIC REACTOR

A reactor for refining resid includes an elongated vertical vessel containing a bed of catalyst which is expanded or ebullated by a liquid/gas mixture. The mixture rises in an updraft through the bed and then is recirculated with an increased velocity by an ebullating pump. To reduce gas holdup of the ebullated bed and to promote a more uniform flow, the gas is entrapped by two cascaded stages of baffles which have an internal conical shape to guide, direct, and entrap the gas. One of these two stages has a shape which creates a countercurrent in the flowing liquid to deflect any catalyst particles which might otherwise be elutriated by the increased velocity.

PROCESS FOR PROCESSING USED OR WASTE PLASTIC MATERIAL

A process is disclosed for processing used or waste plastic materials in order to recover chemical raw materials and liquid fuel components by depolymerisation of the used materials, which are transformed into a pumpable and into a volatile phase. The volatile phase is separated into a gaseous phase and a condensate or condensable depolymerisation product, which are refined by standard usual procedures. The pumpable phase remaining once the volatile phase is separated is subjected to liquid phase hydrogenation, gasification, low temperature carbonisation or to a combination of said processes.

Fluidized bed hydrotreating catalyst and preparation method thereof

The invention relates to a fluidized bed hydrotreating catalyst and a preparation method thereof, and the preparation method comprises the following steps: preparing a suspension from alumina, aluminum hydroxide, an alkaline auxiliary agent and deionized water, and carrying out liquid grinding, hydrothermal reaction, washing and filtering to obtain a wet filter cake A; adding deionized water, a peptizing agent solution and a dispersing agent solution into the obtained wet filter cake A to prepare sol B with certain aluminum oxide content; injecting the sol B into a column containing oil on the upper layer and an alkaline solution on the lower layer for forming, and drying and roasting a formed substance to obtain a product spherical carrier C; and dipping the carrier in an active metal component, and directly roasting the carrier in a roasting furnace to obtain the fluidized bed hydrogenation catalyst. The catalyst has the characteristics of proper granularity, uniform particles, excellent ...

Catalyst for hydro-demetallisation and hydroconversion

METHOD FOR CONVERSION OF PETROLEUM STREAMS INCLUDING A STEP OF HYDROCRACKING IN EBULLATED BED SORTING SYSTEM INCORPORATING A CATALYST

L'invention concerne un procédé de conversion d'une charge hydrocarbonée comprenant les étapes suivantes : a) une étape d'hydrocraquage de ladite charge hydrocarbonée en présence d'hydrogène dans au moins un réacteur contenant un catalyseur supporté en lit bouillonnant avec un appoint en ledit catalyseur, b) une étape de soutirage d'au moins une partie du catalyseur utilisé à l'étape a) d'hydrocraquage, c) au moins une étape d'analyse de la teneur en un contaminant déposés sur les grains dudit catalyseur soutirés à l'étape b) de soutirage par une technique permettant une analyse grain par grain, d) au moins une étape de séparation desdits grains à la suite de l'étape c) d'analyse en au moins 2 fractions, l'une au moins contenant les grains de catalyseurs dont ladite teneur en contaminant est inférieure à un seuil de tri, dans lequel ledit appoint en catalyseur est constitué de grains de catalyseur frais et d'au moins une partie de ladite fraction obtenue à l'étape d) de séparation contenant ...

HYDROPROCESSING METHOD, OR AN APPARATUS RELATING THERETO

One exemplary embodiment can be a hydroprocessing method. The hydroprocessing method can include providing a feed and a stream including hydrogen to a vessel. The vessel may have a catalyst collector and an internal riser. Generally, a catalyst circulates within the vessel by at least partially rising within the internal riser.

GAS OIL HYDROPROCESS

A process for the hydroprocessing of a gas oil (GO) hydrocarbon feed to provide high yield of a diesel fraction. The process comprises a liquid-full hydrotreating reaction zone followed by a liquid-full hydrocracking reaction zone. A refining zone may be integrated with the hydrocracking reaction zone. Ammonia and other gases formed during the hydrotreatment are removed in a separation step prior to hydrocracking.

PROCESS AND CATALYST FOR REDUCING SULFUR IN HYDROCARBONS

Wirbelschichtverfahren mit wechselseitiger Foerderung von Festkoerperteilchen in fluidisiertem Zustand zwischen zwei Reaktionsbehaeltern oder einem Reaktionsbehaelter und einem Regenerator und Vorrichtung zur Durchfuehrung des Verfahrens

Fluid bed reactor used for gasoline desulfuration

The invention provides a fluid bed reactor used for gasoline desulfuration, which belongs to the field of petrochemical industry and is characterized in that an automatic back wash filter, a dust reduction machine, a catalyst bed, a backflow prevention distributor and an impact prevention distributor are arranged in a reactor, and the reactor is externally connected with a reductor and an acceptor. By utilizing the reactor, the filtering performance of the filter can be automatically and efficiently restored in time, thereby reducing the labor strength; catalyst particles are prevented from flowing back below the reactor, thereby enabling gas to be evenly distributed on the section of the whole reactor; the dust content of the gas is effectively reduced, thereby greatly reducing the load of the automatic back wash filter, effectively prolonging the operating period of the automatic back wash filter and reducing equipment investments and maintenance charges; the influent gas is prevented ...

Desulfurization of hydrocarbon streams

A process for desulfurizing a hydrocarbon stream which includes at least 100 ppmw sulfur in the form of organic sulfur compounds, and C4 -hydrocarbons. The hydrocarbon stream is contacted in the absence of added hydrogen with a fluidized bed of an acidic catalyst having a structure of ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-35, ZSM-48, MCM-22, MCM-36, MCM-49, zeolite Y, zeolite beta or mixtures thereof to convert the organic sulfur compounds to hydrogen sulfide. The catalyst contacts the hydrocarbon stream at a pressure of from 0.0 psig to about 400 psig, a temperature of from about 400° F. to about 900° F., and a weight hourly space velocity of from about 0.1 hr.-1 to about 10.0 hr.-1. Thereafter, the hydrogen sulfide is removed from the hydrocarbon stream.

Ebullating bed methods for treatment of biocomponent feedstocks

Processes are provided for producing a diesel fuel product having a sulfur content of 15 wppm or less (e.g., 10 wppm or less) from feed sources that include a biocomponent feedstock. The biocomponent feedstock can be initially co-processed with a mineral feed in a fluidized bed stage, such as an ebullating bed processing stage. Ebullating bed processing can mitigate the impact of the biocomponent feed on other hydrotreatment aspects of a diesel boiling range feed. Challenged biocomponent feeds can be handled by introducing the biocomponent feed into the ebullating bed reactor in a manner that reduces the fouling impact of the feed.

Process for improving the pout point of paraffinic feedstocks with zeolite IM-5 based catalyst

L'invention concerne un procédé pour améliorer le point d'écoulement d'une charge comportant des paraffines de plus de 10 atomes de carbone, dans lequel la charge à traiter est mise au contact d'un catalyseur comprenant la zéolithe IM-5 et au moins un élément hydro-déshydrogénant, à une température comprise entre 170 et 500ºC, une pression entre 1 et 250 bar et une vitesse volumique horaire entre 0,05 et 100 h-1, en présence d'hydrogène à raison de 50 à 2000 l/l de charge. Les huiles obtenues présentent de bons points d'écoulement et des indices de viscosité (VI) élevés. Le procédé est également applicable aux gazoles, et autres charges nécessitant la réduction de leur point d'écoulement.

Hydroumwandlungsverfahren

Katalysatortraeger

LOW SULPHUR FUEL OIL FROM HIGH METALS CONTAINING PETROLEUM RESIDUUM

... 1431728 Treating heavy oils HYDROCARBON RESEARCH Inc 19 June 1974 27260/74 Heading C5E Low sulphur fuel oil is produced from hydrocarbon residuum containing at least 50 p.p.m. of vanadium by contacting with hydrogen at 700-850‹ F. and 1000-3000 p.s.i.g. in a bed comprising a mixture of demetallization solids having a high porosity and low activity and a solid desulphurization catalyst of low porosity and high activity. In examples, Venezuelan light and heavy atmospheric residua are treated using a mixture of cobalt molybdate on alumina catalyst together with either activated bauxite or 95% alumina/5% silica.

NOVEL REACTOR WITH TWO FLUIDIZED REACTION ZONES WITH AN INTEGRATED GAS/SOLID SEPARATION SYSTEM

Method for filling fluidized bed reactor catalyst

An adsorption desulforization reaction device and a method for the adsorptive desulfurization

A boiling bed hydrogenation reaction system and fluidized bed hydrogenation process method

Verfahren zur Hydrierung mit hohem UEberfuehrungsgrad

SILBERTRAEGERKATALYSATOR

Method for improving flow point of paraffine material by using catalyst using zeolite IM-5 as main composition

SYSTEM, APPARATUS AND PROCESS FOR EXTRACTION OF BITUMEN FROM OIL SANDS

A separation process and system for extracting hydrocarbons from a mixture. In some embodiments, a process for separating a bitumen froth stream containing bitumen froth, water and fine solids into a bitumen enriched froth stream and a water and fine solids stream, comprises: (a) receiving the bitumen froth stream in a concentrator vessel, (b) distributing the bitumen froth stream in the concentrator vessel as a substantially uniform and generally horizontal flow of the bitumen froth stream at a first flow velocity, (c) slowing the bitumen froth stream to a second flow velocity, slower than the first flow velocity, in a separation region of the concentrator vessel to promote separation of the bitumen froth from the water and fine solids, and then (d) collecting a bitumen enriched froth stream and (e) collecting a separate water and fine solids stream. Related embodiments of systems and apparatus may also be provided. 1. A process for separating a bitumen froth stream containing bitumen froth , water and fine solids into a bitumen enriched froth stream and a water and fine solids stream , the process comprising:receiving the bitumen froth stream in a concentrator vessel;distributing the bitumen froth stream in the concentrator vessel as a substantially uniform and generally horizontal flow of the bitumen froth stream at a first flow velocity;slowing the bitumen froth stream to a second flow velocity, slower than the first flow velocity, in a separation region of the concentrator vessel to promote separation of the bitumen froth from the water and fine solids, the bitumen froth accumulating as a bitumen froth layer atop a water layer with the fine solids settling within the water layer;collecting the bitumen froth layer as the bitumen enriched froth stream; andcollecting the water layer and fine solids as the water and fine solids stream.2. The process of wherein the bitumen froth layer is continuously collected at an overflow outlet while the water layer and fine ...

PROFITABLE METHOD FOR CARBON CAPTURE AND STORAGE

The present invention generally relates to a method for sequestering carbon dioxide. Biomass is converted into paraffinic hydrocarbons. The paraffinic hydrocarbons are steam cracked into olefins. The olefins are polymerized into non-biodegradable polyolefins. 1. A method comprising steam cracking paraffinic hydrocarbons into olefins , wherein the paraffinic hydrocarbons are derived from a biomass.2. The method of claim 1 , wherein the paraffinic hydrocarbons are produced by gasification followed by Fischer-Tropsch conversion3. The method of claim 2 , wherein the biomass is wood chips.4. The method of claim 1 , wherein the paraffinic hydrocarbons are produced by the hydrotreating of fatty acids and/or fatty acid esters.5. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are oils from plants.6. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are fats from animals.7. The method of claim 4 , wherein the fatty acids and/or fatty acid esters are oils from algae.8. The method of claim 7 , wherein the algae are grown in ponds and/or photo-bioreactors with COsupplied from stationary emission sources.9. The method of claim 8 , wherein the stationary emission source is a coal-fired power plant.10. The method of claim 1 , wherein the olefins comprise ethylene claim 1 , propylene claim 1 , butenes claim 1 , and butadiene.11. The method of claim 1 , wherein bio-derived hydrogen is produced as byproduct of steam cracking.12. The method of claim 1 , wherein bio-derived pyrolysis gasoline is produced as byproduct of steam cracking.13. The method of claim 12 , wherein the pyrolysis gasoline is used as motor gasoline blend stock.14. The method of claim 13 , wherein the pyrolysis gasoline is hydrogenated prior to use as motor gasoline.15. The method of claim 1 , wherein bio-derived fuel gas is produced as byproduct of steam cracking.16. The method of claim 1 , wherein the pyrolysis fuel oil yield is less than 1 wt % of the paraffinic ...

PROCESS FOR MAKING A DISTILLATE PRODUCT AND/OR C2-C4 OLEFINS

A process for making a distillate product and one or more C2-C4 olefins from a FCC feedstock containing a cellulosic material and a hydrocarbon co-feed is provided. 1. A process for making a distillate product and one or more C2-C4 olefins comprising:a) contacting a FCC feedstock with a FCC catalyst at a temperature of at least 400° C. in a riser reactor to produce a distillate product and a spent FCC catalyst, wherein the FCC feedstock comprises a cellulosic material and a hydrocarbon co-feed;b) separating at least a portion of the distillate product from the spent FCC catalyst;c) regenerating the spent FCC catalyst to produce a regenerated FCC catalyst;d) contacting an intermediate reactor feedstock with at least a portion of the regenerated FCC catalyst at a temperature of at least 500° C. in an intermediate reactor to produce one or more C2-C4 olefins and a used regenerated FCC catalyst;e) separating at least a portion of the one or more C2-C4 olefins from the used regenerated catalyst; andf) providing at least a portion of the used regenerated FCC catalyst as FCC catalyst in step a).2. The process of wherein the FCC feedstock comprises a hydrocarbon co-feed and at least one cellulosic material selected from the group consisting of a solid cellulosic material claim 1 , a pyrolysis oil derived from cellulosic material claim 1 , and a mixture thereof.3. The process of wherein the hydrocarbon co-feed comprises at least 8 wt % elemental hydrogen claim 1 , based on the total weight of the hydrocarbon co-feed on a dry basis.4. The process of wherein the hydrocarbon co-feed comprises in the range from at least 20 wt % to at most 100 wt % of at least one paraffin claim 1 , based on the total weight of the hydrocarbon co-feed.5. The process of wherein the combination of the cellulosic material and the hydrocarbon co-feed has an overall molar ratio of hydrogen to carbon (H/C) of equal to or more than 1.1 (1.1/1).6. The process of wherein the cellulosic material is a solid ...

Methods for Producing Hydrocarbon Products from Bio-Oils and/or Coal-Oils

The present invention relates to a method for producing a hydrocarbon product from coal and/or biomass comprising the following steps: converting the coal to a coal-oil and/or converting the biomass to bio-oil, optionally processing the coal-oil and/or bio-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the coal-oil and/or bio-oil; and using at least a portion of the coal-oil and/or bio-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product. 1. A method for producing a hydrocarbon product from coal comprising the following steps:converting the coal to a coal-oil by thermal or hydrothermal conversion;processing the coal-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the coal-oil; andusing at least a portion of the coal-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product.2. A method for producing a hydrocarbon product from biomass comprising the following steps:converting the biomass to bio-oil by thermal or hydrothermal conversion;processing the bio-oil in a hydroprocessing reaction to remove one or more of oxygen, nitrogen or sulfur from hydrocarbon compounds in the bio-oil; andusing at least a portion of the bio-oil as a feedstock in a cracking reaction to convert hydrocarbon compounds in the feedstock into a mixture of smaller hydrocarbon compounds comprising the hydrocarbon product.3. The method of claim 2 , wherein the feedstock is comprised of at least:(i) 50% of said bio-oil and said hydrocarbon product is at least a 50% renewable product;(ii) 75% of said bio-oil and said hydrocarbon product is at least a 75% renewable product; or(iii) 90% of said bio-oil and said hydrocarbon product is ...

METHOD OF PRODUCING DROP-IN DIESEL

Methods are disclosed for producing renewable diesel from hydrocarbon-containing feedstock using microwave energy and hydrotreatment. 1. A method for producing a fuel , comprising:forming pellets comprising at least one hydrocarbon-containing feedstock and at least one catalyst; crude oil;', 'biochar; and', [{'sub': '2', 'H;'}, 'CO; and', {'sub': '2', 'optionally, CO;'}], 'optionally, syngas comprising], 'depolymerizing said hydrocarbon-containing feedstock in the presence of said catalyst using high-frequency microwave energy at a temperature of about 275° C. and 350° C. to form a composition comprising{'sub': '2', 'reacting said crude oil with Hto remove impurities and to form an upgraded crude oil; and'}distilling said upgrading crude oil to form a phenol fraction and a diesel fraction.2. A method of claim 1 , further comprising:blending said diesel fraction with at least one additive.3. A method of claim 1 , further comprising:blending said diesel fraction with at least one fossil fuel.4. A method of claim 1 ,wherein said depolymerizing step is carried out at a temperature of about 280° C.5. A method of claim 1 ,wherein said pellets have a density sufficient to permit said depolymerizing step and said hydrotreating step without substantially mechanically degrading said pellets.6. A method of claim 1 , further comprising:drying said hydrocarbon-containing feedstock prior to forming said pellets.7. A method of claim 6 , further comprising:combusting at least a portion of said syngas in said drying step.8. A method of claim 1 , further comprising:recovering heat from said biochar to form a cooled biochar.9. A method of claim 8 , further comprising:storing said cooled biochar.10. A method of claim 1 , further comprising:storing said phenol fraction.11. A method of claim 1 ,wherein said phenol fraction comprises methoxyphenol.12. A method of claim 1 , further comprising:storing said diesel fraction.13. A method of claim 1 ,wherein said catalyst is a zeolite.14. A ...

METHODS AND SYSTEMS FOR PROCESSING BIOMASS MATERIAL

Embodiments of the present invention provide for production and recovery of volatile organic compounds and higher hydrocarbons from biomass material. One embodiment comprises contacting a solid component of a biomass material with a digestive solvent to form a digested biomass stream, and at least a portion of the digested biomass is further thermocatalytically treated to generate higher hydrocarbons. The solid component is generated by a method comprising introducing a biomass material to a compartment of a solventless recovery system, wherein the biomass material contains one or more volatile organic compounds; contacting the biomass material with a superheated vapor stream in the compartment to vaporize at least a portion of an initial liquid content in the biomass material; separating a vapor component and a solid component from the heated biomass material; retaining at least a portion of the gas component for use as part of the superheated vapor stream. 1. A method for processing a biomass material comprising:introducing a biomass material to a compartment of a solventless recovery system, wherein the biomass material contains one or more volatile organic compounds;contacting the biomass material with a superheated vapor stream in the compartment to vaporize at least a portion of an initial liquid content in the biomass material, said superheated vapor stream comprising at least one volatile organic compound;separating a vapor component and a solid component from the heated biomass material, said vapor component comprising at least one volatile organic compound;retaining at least a portion of the gas component for use as part of the superheated vapor stream;discharging the solid component from the solventless recovery system;contacting at least a portion of the solid component with a digestive solvent to form a digested biomass stream comprising carbohydrates;contacting the digested biomass stream with molecular hydrogen in the presence of a molecular hydrogen ...

Systems and Methods For Hydrotreating A Shale Oil Stream Using Hydrogen Gas That Is Concentrated From The Shale Oil Stream

Systems and methods for hydrotreating a liquid fraction of a shale oil stream using hydrogen gas that is concentrated from a gaseous fraction of the shale oil stream. The systems and methods include providing a portion of the gaseous fraction to a sorptive separation assembly and separating a concentrated hydrogen stream from the portion of the gaseous fraction within the sorptive separation assembly. The system and methods further include providing the concentrated hydrogen stream and the liquid fraction to a hydrotreater and reacting the concentrated hydrogen stream with the liquid fraction within the hydrotreater to produce the hydrotreated liquid stream. The systems and methods may include generating the shale oil stream within a subterranean formation using an in situ process, such as an in situ shale oil conversion process and/or providing a supplemental hydrogen stream to the hydrotreater. 1. A method of hydrotreating a liquid fraction of a shale oil stream with hydrogen gas concentrated from a gaseous fraction of the shale oil stream , the method comprising:separating the liquid fraction of the shale oil stream from the gaseous fraction of the shale oil stream;providing a portion of the gaseous fraction to a sorptive separation assembly;separating, in the sorptive separation assembly, a concentrated hydrogen stream from the portion of the gaseous fraction;providing the concentrated hydrogen stream and the liquid fraction to a hydrotreater; andreacting, in the hydrotreater, the concentrated hydrogen stream with the liquid fraction to produce a hydrotreated liquid stream.2. The method of claim 1 , wherein the method further includes generating the shale oil stream within a subterranean formation using at least one of a pyrolysis reaction claim 1 , an in situ pyrolysis reaction claim 1 , a shale oil retort process claim 1 , a shale oil heat treating process claim 1 , a hydrogenation reaction claim 1 , a thermal dissolution process claim 1 , and an in situ shale ...

METHOD FOR CONVERTING A HYDROCARBONACEOUS MATERIAL TO A FLUID HYDROCARBON PRODUCT COMPRISING P-XYLENE

The invention relates to a method for producing a fluid hydrocarbon product, and more specifically, to a method for producing a fluid hydrocarbon product via catalytic pyrolysis. The reactants comprise hydrocarbonaceous materials (e.g., biomass). The catalyst comprises a zeolite catalyst treated with a silicone compound. The product comprises p-xylene. 1. A method for producing a fluid hydrocarbon product comprising p-xylene from a hydrocarbonaceous material , comprising:feeding the hydrocarbonaceous material to a reactor;pyrolyzing within the reactor at least a portion of the hydrocarbonaceous material under reaction conditions sufficient to produce a pyrolysis product; andcatalytically reacting at least a portion of the pyrolysis product under reaction conditions in the presence of a zeolite catalyst to produce the fluid hydrocarbon product;the zeolite catalyst comprising pores with pore mouth openings and catalytic sites on the external surface of the catalyst, and an effective amount of a treatment layer derived from a silicone compound to reduce the size of the pore mouth openings and to render at least some of the catalytic sites on the external surface of the catalyst inaccessible to the pyrolysis product.2. The method of wherein catalytic sites are positioned in the pores near the pore mouth openings claim 1 , and the treatment layer renders at least some of the catalytic sites in the pores near the pore mouth openings inaccessible to the pyrolysis product.3. The method of or wherein the fluid hydrocarbon product comprises xylenes with a p-xylene selectivity in the xylenes of at least about 40% claim 1 , or at least about 45% claim 1 , or at least about 50% claim 1 , or at least about 55% claim 1 , or at least about 60% claim 1 , or at least about 65% claim 1 , or at least about 70% claim 1 , or at least about 75% claim 1 , or at least about 80% claim 1 , or at least about 85% claim 1 , or at least about 90%.4. The method of any of the preceding claims ...

HYDROPYROLYSIS OF BIOMASS FOR PRODUCING HIGH QUALITY LIQUID FUELS

A self-sustaining process for producing liquid fuels from biomass in which the biomass is hydropyrolyzed in a reactor vessel containing molecular hydrogen and a deoxygenating catalyst, producing a partially deoxygenated pyrolysis liquid, which is hydrogenated using a hydroconversion catalyst, producing a substantially fully deoxygenated pyrolysis liquid and a gaseous mixture comprising CO and light hydrocarbon gases (C-C). The gaseous mixture is reformed in a steam reformer, producing reformed molecular hydrogen, which is then introduced into the reactor vessel for hydropyrolizing the biomass. The deoxygenated liquid product is further processed to produce diesel fuel and gasoline. 1. (canceled)2. A process for a producing a liquid hydrocarbon-containing product from biomass , the process comprising:(a) pyrolyzing the biomass in the presence of hydrogen and a deoxygenation catalyst to provide a hydropyrolysis effluent comprising a partially deoxygenated hydropyrolysis product and char, and(b) hydroconverting the partially deoxygenated hydropyrolysis product in the presence of a hydroconversion catalyst to provide a hydroconversion effluent comprising the liquid hydrocarbon-containing product and a water-containing product,wherein deoxygenation in step (a) and hydroconversion in step (b) are carried out to an extent whereby the liquid hydrocarbon-containing product has sufficiently low oxygen content to be phase-separable from the water-containing product.3. The process of claim 2 , further comprising(c) separating the liquid hydrocarbon-containing product from the water-containing product by phase separation.4. The process of claim 3 , wherein claim 3 , following separation in step (c) claim 3 , the water-containing product contains less than 2000 ppm dissolved total organic carbon (TOC).5. The process of claim 3 , wherein the hydroconversion reactor effluent further comprises a gaseous mixture comprising CO and C-Chydrocarbons claim 3 , the process further ...

BIOMASS CONVERSION SYSTEMS PROVIDING INTEGRATED STABILIZATION OF A HYDROLYSATE USING A SLURRY CATALYST FOLLOWING BIOMASS PRETREATMENT AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with integrated catalytic reduction during digestion to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Such integrated catalytic reduction may be conducted using a slurry catalyst. Biomass conversion systems for performing integrated catalytic reduction can comprise: a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst; a pretreatment digestion unit that is not part of the fluid circulation loop and does not contain the slurry catalyst; and a solids transport mechanism operatively connecting the pretreatment digestion unit to the hydrothermal digestion unit. 1. A biomass conversion system comprising:a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit;a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst;a pretreatment digestion unit that is not part of the fluid circulation loop and does not contain the slurry catalyst; anda solids transport mechanism operatively connecting the pretreatment digestion unit to the hydrothermal digestion unit.2. The biomass conversion system of claim 1 , wherein the solids transport mechanism operatively connects the bottom of the pretreatment digestion unit to the top of the hydrothermal digestion unit.30. The biomass conversion system of claim claim 1 , wherein the solids transport mechanism is capable of conveying a biomass ...

BIOMASS CONVERSION SYSTEMS PROVIDING INTEGRATED STABILIZATION OF A HYDROLYSATE USING A SLURRY CATALYST AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with integrated catalytic reduction during digestion to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Such integrated catalytic reduction may be conducted using a slurry catalyst. Biomass conversion systems for performing integrated catalytic reduction can comprise: a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; and a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst. 1. A biomass conversion system comprising:a hydrothermal digestion unit that contains a slurry catalyst capable of activating molecular hydrogen;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; anda fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit, the catalytic reduction reactor unit also containing the slurry catalyst.2. The biomass conversion system of claim 1 , wherein the fluid circulation loop is configured to establish upward fluid flow in the hydrothermal digestion unit.3. The biomass conversion system of claim 1 , further comprising:a retention mechanism within the hydrothermal digestion unit that is operable to retain cellulosic biomass solids having a particle size of about 3 mm or above.4. The biomass conversion system of claim 1 , further comprising:a reaction product takeoff line in fluid communication with the fluid circulation loop, the reaction product takeoff line being located between the hydrothermal digestion unit and an outlet of the catalytic reduction reactor unit.5. The biomass conversion system of claim 4 , further comprising:a solids separation mechanism that is operatively ...

Integrated Oil Production and Upgrading Using Molten Alkali Metal

A method that combines the oil retorting process (or other process needed to obtain/extract heavy oil or bitumen) with the process for upgrading these materials using sodium or other alkali metals. Specifically, the shale gas or other gases that are obtained from the retorting/extraction process may be introduced into the upgrading reactor and used to upgrade the oil feedstock. Also, the solid materials obtained from the reactor may be used as a fuel source, thereby providing the heat necessary for the retorting/extraction process. Other forms of integration are also disclosed. 1. A method for upgrading an oil feedstock comprising:retorting oil shale to produce shale oil and shale gas;upgrading the shale oil using an alkali metal, wherein shale gas obtained from the retorting step is used as the reactant gas in the upgrading step.2. The method of claim 1 , wherein the shale gas comprises a quantity of hydrogen sulfide claim 1 , wherein the hydrogen sulfide is added to the shale oil during the upgrading step.3. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used to provide heat during the retorting step.4. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used as a feedstock in the retorting step.5. The method of claim 1 , wherein the upgrading step produces a solid material containing organic matter claim 1 , wherein this solid material is used during the retorting step.6. The method of claim 1 , wherein the upgrading step produces products a solid material claim 1 , wherein the solid material is used produce power for an electrolytic regeneration of the alkali metal.7. A method for upgrading a heavy oil or bitumen from oil sands comprisingheating the oil sands to cause the heavy oil or bitumen to flow, wherein a gas is also produced by this heating;upgrading the heavy oil or ...

BIOMASS CONVERSION SYSTEMS CONTAINING A MOVING BED CATALYST FOR STABILIZATION OF A HYDROLSATE AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids to form a hydrolysate may be conducted with in situ catalytic reduction to transform soluble carbohydrates in the hydrolysate into a more stable reaction product. Biomass conversion systems for performing such a transformation can comprise: a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit; an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit; a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; and a catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit. 1. A biomass conversion system comprising:a hydrothermal digestion unit that also contains a first catalyst capable of activating molecular hydrogen, the first catalyst being fluidly mobile within the hydrothermal digestion unit;an optional hydrogen feed line that is operatively connected to the hydrothermal digestion unit;a fluid circulation loop comprising the hydrothermal digestion unit and a catalytic reduction reactor unit that contains a second catalyst capable of activating molecular hydrogen; anda catalyst transport mechanism external to the hydrothermal digestion unit, the catalyst transport mechanism being capable of conveying at least a portion of the first catalyst to another location from a catalyst collection zone located within the hydrothermal digestion unit.2. The biomass conversion system of claim 1 , wherein at least a portion of the first catalyst is non-buoyant in a fluid phase.3. The biomass conversion system of claim 1 , wherein the ...

METHODS, SYSTEMS, AND DEVICES FOR CONTINUOUS LIQUID FUEL PRODUCTION FROM BIOMASS

Methods, systems, and devices for continuous production of liquid fuels from biomass are provided. Some embodiments utilize a thermochemical process to produce a bio-oil in parallel with a thermochemical process to produce a hydrogen-rich synthesis gas. Both product streams may be fed into a third reaction chamber that may enrich the bio-oil with the hydrogen gas, for example, in a continuous production process. One product stream may include a liquid fuel such as diesel. Some embodiments may also produce other product streams including, but not limited to, electrical power generation and/or biochar. 1. A method of continuous liquid fuel production utilizing biomass , the method comprising:receiving one or more biomass feedstocks;utilizing a first portion of the one or more biomass feedstocks to produce synthesis gas from a first thermochemical process;utilizing a second portion of the one or more biomass feedstocks to produce bio-oil from a second thermochemical process; andgenerating a liquid fuel through combining the produced synthesis gas and the produced bio-oil.2. The method of claim 1 , wherein the first thermochemical process comprises:combining water with the first portion of the one or more biomass feedstocks to from a wet biomass feedstock;transferring the wet biomass feedstock to a reaction chamber; andheating the wet biomass feedstock within the reaction chamber such that the elements comprised by the wet biomass feedstock dissociate and react to form at least the synthesis gas.3. The method of claim 2 , where the elements comprises by the wet biomass feedstock dissociate and react through a non-oxidation reaction to form at least the synthesis gas.4. The method of claim 3 , wherein the non-oxidation reaction comprises a hydrous pyrolysis reaction.5. The method of claim 1 , wherein the synthesis gas comprises hydrogen gas.6. The method of claim 1 , wherein the one or more biomass feedstocks comprises at least cellulose claim 1 , lignin claim 1 , or ...

SYSTEM FOR MAKING RENEWABLE FUELS INCLUDING GASOLINE, DIESEL, AND JET FUEL

Multiple catalytic processing stations coupled with a system which produces volatile gas streams from biomass decomposition at discrete increasing temperatures or constant temperature. These catalytic processing stations can be programmed to maximize conversion of biomass to jet fuel components. The system may also include a processing station for subjecting biomass within the stations to at least one programmable starting temperature (T) and for incrementing an individual processing station temperature by programmable increments (ΔT) to produce a volatile and a non-volatile component. Further, methods for converting biomass and char to renewable jet fuel, diesel, and kerosene are disclosed. 1. A system for the conversion of biomass to diesel or jet fuel , comprising:a device containing a number of processing stations (N) and a series of catalysts;{'sub': 'start', 'each processing station capable of subjecting biomass within the station to at least one starting temperature (T) to produce a volatile and a non-volatile component;'}at least one catalyst reactor for receiving volatile components generated in each processing station; andwherein, the at least one catalyst reactor contains a catalyst selected from the group consisting of: dehydration catalysts, olefin oligomerization catalysts and hydrotreating catalysts.2. The system of claim 1 , further comprising additional catalyst reactors.3. The system of claim 2 , wherein the additional catalyst reactors are used in series.4. The system of claim 2 , wherein the additional catalyst reactors are used in parallel.5. The system of claim 1 , further comprising a temperature controller for incrementing an individual processing station temperature by increments (ΔT).6. The system of claim 1 , wherein the non-volatile component is a carbonaceous material.7. The system of claim 1 , further comprising a gasifier for converting the carbonaceous material to syngas.8. The system of claim 7 , further comprising a conduit from the ...

PYROLYSIS VAPOR RAPID FILTRATION AND CONVERSION TO FUEL

The present disclosure pertains to biomass pyrolysis processes and systems that decrease entrainment of char and other contaminants in the pyrolysis vapors by filtering the vapors in a heated container comprising a moving bed granular filter (MBGF), which in turn, comprises granular heat carrier. The granular heat carrier is heated within the MBGF and fed directly to the pyrolysis reactor, optionally along with filtered solids such as char. In certain embodiments, the MBGF additionally comprises at least one upgrading catalyst that contacts the vapors to produce a hydrocarbon mixture fungible with a petroleum-derived transportation fuel, a hydrocarbon transportation fuel component, or mixtures thereof. 1. A biomass pyrolysis process , comprising the steps of:(a) providing a heated container that encloses a moving bed granular filter, wherein the moving bed granular filter comprises a granular heat carrier;(b) heating the granular heat carrier in the heated container to produce a heated granular heat carrier that is conveyed to a pyrolysis reactor;(c) pyrolyzing a biomass feedstock in the pyrolysis reactor to produce pyrolysis vapors comprising a residual amount of entrained char particles, wherein rapid heating of the biomass feedstock is facilitated by contact with the heated granular heat carrier;(d) conveying the pyrolysis vapors out of the pyrolysis reactor and through the moving bed granular filter to separate at least a portion of the residual entrained char particles, thereby producing low-particulate pyrolysis vapors and a solid stream comprising char and the heated granular heat carrier of step (a).2. The process of claim 10 , further comprising contacting the low-particulate upgraded pyrolysis vapors with at least one upgrading catalyst within the heated container to produce a hydrocarbon mixture fungible with a petroleum-derived transportation fuel or a component thereof.3. The process of claim 1 , further comprising contacting the low-particulate ...

SYSTEM AND METHOD FOR MAKING RENEWABLE FUELS

Multiple catalytic processing stations enable a method for producing volatile gas streams from biomass decomposition at discrete increasing temperatures. These catalytic processing stations can be programmed to maximize conversion of biomass to useful renewable fuel components based on input feedstock and desired outputs. 1. A method for converting biomass to renewable fuels , comprising:providing a system containing a number of processing stations (N) in communication with a series of catalysts;heating a biomass within the stations at a starting temperature (Tstart) to produce a volatile and a non-volatile component, said biomass and said heating selected to provide volatile components of a predetermined composition; andsubjecting the volatile components of a predetermined composition generated in at least one station through the series of catalysts to produce at least one renewable fuel.2. The method of claim 1 , wherein said series of catalysts is selected based on said starting temperature.3. The method of claim 1 , wherein said series of catalyst is based on the biomass composition.4. The method of claim 3 , wherein the biomass is a lipid-rich biomass and the volatile components from the lipid-rich biomass is contacted with a dehydration catalyst to produce a product which on cooling to a temperature range of 1-20° C. produces a second volatile component claim 3 , a first renewable fuel and water.5. The method of claim 3 , wherein the biomass is a hemicellulose-rich biomass and a volatile components from the hemicellulose-rich biomass is contacted directly with an aromatization catalyst to produce a product which on cooling to a temperature of 0-5° C. produces a second volatile component claim 3 , a first renewable fuel and water.6. The method of claim 3 , wherein the biomass is a lignin-rich biomass and the volatile component from the lignin-rich biomass is contacted with a dehydration catalyst to produce a product which on cooling to 2-20° C. produces a ...

BIOMASS CONVERSION SYSTEMS HAVING A SINGLE-VESSEL HYDROTHERMAL DIGESTION UNIT/CATALYTIC REDUCTION REACTOR UNIT FOR INTEGRATED STABILIZATION OF A HYDROLYSATE AND METHODS FOR USE THEREOF

Digestion of cellulosic biomass solids may be conducted in a pressure vessel that contains both a hydrothermal digestion unit and a catalytic reduction reactor unit. Biomass conversion systems incorporating such a feature may comprise: a pressure vessel that comprises a first section comprising a hydrothermal digestion unit and a second section comprising a first catalytic reduction reactor unit that contains a first catalyst capable of activating molecular hydrogen; wherein the hydrothermal digestion unit and the first catalytic reduction reactor unit are in fluid communication with one another; a biomass feed mechanism that is operatively connected to the pressure vessel, the biomass feed mechanism being capable of introducing cellulosic biomass solids to the pressure vessel and also capable of withdrawing a reaction product from the first catalytic reduction reactor unit; and a hydrogen feed line that is operatively connected to the first catalytic reduction reactor unit. 1. A biomass conversion system comprising: 'wherein the hydrothermal digestion unit and the first catalytic reduction reactor unit are in fluid communication with one another;', 'a pressure vessel comprising a first section and a second section, the first section comprising a hydrothermal digestion unit and the second section comprising a first catalytic reduction reactor unit that contains a first catalyst capable of activating molecular hydrogen;'}a biomass feed mechanism that is operatively connected to the pressure vessel, the biomass feed mechanism being capable of introducing cellulosic biomass solids to the pressure vessel and also capable of withdrawing a reaction product from the first catalytic reduction reactor unit; anda hydrogen feed line that is operatively connected to the first catalytic reduction reactor unit.20. The biomass conversion system of claim , wherein the pressure vessel comprises an annular structure , with the first section comprising an outer portion of the annular ...

FORMATE-ASSISTED PYROLYSIS

The present invention provides, among other thing, methods for creating significantly deoxygenated bio-oils form biomass including the steps of providing a feedstock, associating the feedstock with an alkali formate to form a treated feedstock, dewatering the treated feedstock, heating the dewatered treated feedstock to form a vapor product, and condensing the vapor product to form a pyrolysis oil, wherein the pyrolysis oil contains less than 30% oxygen by weight. 1. A method comprisingproviding a feedstock;associating the feedstock with an alkali formate to form a treated feedstock;dewatering the treated feedstock;heating the dewatered treated feedstock to form a vapor product; andcondensing the vapor product to form a pyrolysis oil;wherein the pyrolysis oil contains less than 30% oxygen by weight.2. The method of claim 1 , wherein the feedstock is selected from the group consisting of cellulosic biomass claim 1 , wood claim 1 , wood waste claim 1 , lignin claim 1 , spent pulping/fractionation liquors claim 1 , algal biomass claim 1 , food waste claim 1 , sludges and municipal solid waste claim 1 , and mixtures thereof.3. The method of claim 1 , wherein the alkali formate is selected from the group consisting of calcium formate claim 1 , magnesium formate claim 1 , sodium formate claim 1 , potassium formate claim 1 , lithium formate claim 1 , zinc formate claim 1 , and mixtures thereof.4. The method of claim 1 , wherein the dewatered treated feedstock is heated to between about 200° C. and about 600° C.5. The method of claim 1 , wherein the dewatered treated feedstock is heated to between about 375° C. and about 500° C.6. The method of claim 1 , wherein the dewatered treated feedstock is heated for between about one second and about four hours.7. The method of claim 1 , wherein at least one of the associating claim 1 , dewatering claim 1 , heating and condensing steps is carried out at a pressure between about vacuum and about 10 bar.8. A method comprisingproviding ...

HYDROPYROLYSIS OF BIOMASS-CONTAINING FEEDSTOCKS

Various techniques are disclosed for pretreating municipal solid waste (MSW) and other biomass-containing feedstocks that may be of a poorer quality and consequently more difficult, or even impossible, to convert to higher value liquid products (e.g., transportation fuels) using conventional processes. Such conventional processes may otherwise be satisfactory for the conversion of the biomass portion of the feedstock alone. The pretreatment of biomass-containing feedstocks may generally include steps carried out prior to a hydropyrolysis step and optionally further steps, in order to change one or more characteristics of the feedstock, rendering it more easily upgradable. 1. A process for producing liquid products from a biomass-containing feedstock comprising the steps of:a) devolatilizing the feedstock in a pre-reactor vessel containing hydrogen and a solid bed material selected from the group consisting of a pretreating catalyst, a sorbent, a heat transfer medium, and mixtures thereof, to produce a pre-reactor vapor stream comprising entrained solid particles; andb) hydropyrolyzing at least a portion of the pre-reactor vapor stream in a hydropyrolysis reactor vessel containing hydrogen and a deoxygenating catalyst, producing a hydropyrolysis reactor output comprising at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char particles.2. The process of claim 1 , further comprising:c) removing substantially all of the char particles from the hydropyrolysis reactor output to provide a purified hydropyrolysis reactor vapor stream having a reduced char content; andd) hydroconverting at least a portion of the purified hydropyrolysis reactor vapor stream in a hydroconversion reactor vessel containing hydrogen and a hydroconversion catalyst, producing a hydroconversion reactor output; ande) recovering a substantially fully deoxygenated hydrocarbon liquid and a gaseous mixture from the hydroconversion reactor output.3. The process of claim ...

SYSTEMS FOR FUELS FROM BIOMASS

The present application generally relates to a system to prepare a fuel from a biomass and a petroleum fraction wherein a renewable fuel oil is obtained via pyrolysis, delivered to the injection point of a refinery system, and then co-processed with a petroleum fraction in the presence of a catalyst. 1. A system to prepare a fuel from a biomass and a petroleum fraction , comprising:a pyrolysis system for producing a renewable fuel oil from the biomass;a refinery system comprising a conversion unit to co-process the renewable fuel oil and the petroleum fraction as reactants in the presence of a catalyst;a delivery system to deliver the renewable fuel oil to an injection point of the conversion unit; anda control system to control the delivery of renewable fuel oil to the refinery system.2. The system of claim 1 , wherein the pyrolysis system is a rapid thermal processing system producing an unenriched renewable fuel oil.3. The system of claim 1 , wherein the pyrolysis system is co-located with the refinery system.4. The system of claim 1 , wherein the conversion unit comprises a fluidized catalytic cracker.5. The system of claim 4 , wherein the fluidized catalytic cracker comprises a retro-fitted fluidized catalytic cracker.6. The system of claim 5 , further comprising one or more modified injection ports through which the renewable fuel oil is injected into a riser of the fluidized catalytic cracker.7. The system of claim 6 , wherein at least one of the one or more modified injection ports comprises a modified nozzle.8. The system of claim 1 , wherein the conversion unit comprises a hydrotreating unit or a hydrocracking unit.9. The system of claim 1 , wherein the delivery system delivers 0.05-20 wt. % renewable fuel oil as a percentage of reactants.10. The system of claim 1 , wherein the delivery system comprises a storage tank and a pre-heater.11. The system of claim 1 , wherein the control system monitors and adjusts the addition of renewable fuel oil so as to ...

INTEGRATED PROCESS FOR THE PRODUCTION OF RENEWABLE DROP-IN FUELS

A process for producing renewable biofuels from biomass is provided wherein a bio-oil containing stream is hydrotreated in an integrated system which uses streams and components generated or obtained from the biomass treatment and conversion. 1. A process for producing a renewable fuel from biomass , the process comprising:(a) converting biomass in a biomass conversion unit in the presence of a biomass conversion catalyst and separating the converted biomass into a fluid phase and a solid phase;(b) separating the fluid phase into a non-condensable gas phase, a renewable bio-oil and process water;{'sub': '6', '(c) fractionating the renewable bio-oil into a water stream, a full range bio-naphtha stream and a topped bio-oil stream, wherein the topped bio-oil stream comprises Cor higher oxygenates;'}{'sub': 5', '6, '(d) molecularly recombining the oxygenates of Cor lower within the process water, the full range bio-naphtha stream and the water stream to produce a recovered organic stream (ROS) comprising Cor greater oxygenates and a clear aqueous stream;'}(e) forming a slurry catalyst mix from the ROS and a soluble hydroprocessing active phase;(f) feeding at least a portion of biomass conversion catalyst and the catalyst mix into a slurry-phase hydroprocessor reactor;(g) forming in the slurry-phase hydroprocessor reactor a solid-phase slurry dispersed catalyst comprising atomically dispersoids of the active phase onto a support comprising the biomass conversion catalyst;(h) feeding the topped bio-oil stream into the slurry-phase hydroprocessor reactor and subjecting the topped bio-oil stream to hydrogenation in the presence of the solid-phase slurry dispersed catalyst; and(i) obtaining renewable fuels originating from hydrogenated topped bio-oil stream.2. The process of claim 1 , wherein the soluble hydroprocessing active phase is an organometallic salt selected from the group of acetylacetonates claim 1 , naphthenates claim 1 , oxalates claim 1 , tartrates claim 1 , or ...

TORREFACTION REDUCTION OF COKE FORMATION ON CATALYSTS USED IN ESTERIFICATION AND CRACKING OF BIOFUELS FROM PYROLYSED LIGNOCELLULOSIC FEEDSTOCKS

A bio-oil production process involving torrefaction pretreatment, catalytic esterification, pyrolysis, and secondary catalytic processing significantly reduces yields of reactor char, catalyst coke, and catalyst tar relative to the best-case conditions using non-torrefied feedstock. The reduction in coke as a result of torrefaction was 28.5% relative to the respective control for slow pyrolysis bio-oil upgrading. In fast pyrolysis bio-oil processing, the greatest reduction in coke was 34.9%. Torrefaction at 275° C. reduced levels of acid products including acetic acid and formic acid in the bio-oil, which reduced catalyst coking and increased catalyst effectiveness and aromatic hydrocarbon yields in the upgraded oils. The process of bio-oil generation further comprises a catalytic esterification of acids and aldehydes to generate such as ethyl levulinate from lignified biomass feedstock. 1. A method for reducing coke deposition on a catalyst used in cracking of a pyrolysis oil vapor , the method comprising:(a) subjecting a biomass to torrefaction;(b) pyrolyzing the torrefaction-treated biomass, thereby generating a heated pyrolysis oil vapor;(c) catalytically esterifying the heated pyrolysis oil vapor or components thereof, thereby providing a heated pyrolysis oil vapor having a reduced acid and aldehyde content compared to a heated pyrolysis oil vapor not catalytically esterified; and(d) cracking the catalytically esterified heated pyrolysis oil vapor, thereby generating a bio-oil, wherein said cracking step comprises contacting the heated pyrolysis oil vapor with a second catalyst, and wherein said catalyst accumulates a reduced coke deposition compared to when the heated pyrolysis oil vapor is generated from a biomass not treated with torrefaction.2. The method of claim 1 , wherein in step (c) the heated pyrolysis oil vapor is contacted with an aqueous composition comprising at least one alcohol and a first catalyst selected to catalyze the esterification of at ...

METHOD FOR EXTRACTING BIOCHEMICAL PRODUCTS OBTAINED FROM A PROCESS OF HYDROTHERMAL CARBONIZATION OF BIOMASS

The invention relates to a method for extracting biochemical products obtained from a process of hydrothermal carbonization of biomass, which includes feeding an aqueous mixture of biomass from a preheating tube for the aqueous mixture of biomass to a vertical reactor with a predetermined level of floatation and an area for accumulation of steam and gases in the upper part thereof, wherein said method for extracting biochemical products is characterized in that it includes (a) heating the aqueous mixture of biomass to, or above, evaporation temperature in said vertical reactor and/or in a previous stage of preheating the aqueous mixture of biomass, increasing the generation of stream and/or gases at the predetermined flotation level of the vertical reactor, (b) extracting the steam and/or gases generated in the previous stage and accumulated in the upper part of the vertical reactor, and (c) cooling the gases and/or condensing the steam extracted in the previous stage at different levels of temperature and pressure. The invention likewise relates to the biochemical product obtainable from said method, as well as to a system for implementing said method. 1. Method for extracting biochemical products during a process of hydrothermal carbonization of biomass , comprising feeding an aqueous mixture of biomass from a preheating tube of the aqueous mixture of biomass to a vertical reactor with a defined level of flotation and an area for the accumulation of steam and gases in its upper portion , where said method for extracting biochemical products is characterized in that it comprises:(a) Heating the aqueous mixture of biomass up to or over the evaporation temperature in the same vertical reactor and/or in a prior preheating stage of the aqueous biomass mixture, increasing the generation of steam and/or gases at the set level of floatation of the vertical reactor.(b) Extracting the biochemicals alongside the steam and/or gasses generated in the previous stage, which ...

PROCESS TO PRODUCE BIOFUELS FROM BIOMASS

A process for producing biofuels from biomass is provided by removing sulfur compounds and nitrogen compounds from the biomass by contacting the biomass with a digestive solvent to form a pretreated biomass containing soluble carbohydrates and having less than 35% of the sulfur content and less than 35% of the nitrogen content, based on untreated biomass on a dry mass basis, prior to carrying out aqueous phase reforming and further processing to form a liquid fuel. 1. A system comprising: a digester that receives a biomass feedstock and a digestive solvent operating under conditions to effectively remove nitrogen compounds and sulfur compounds from said biomass feedstock and discharges a treated stream comprising a carbohydrate having less than 35% of the sulfur content and less than 35% of the nitrogen content based on untreated biomass feedstock on a dry mass basis; an aqueous phase reforming reactor comprising an aqueous phase reforming catalyst that receives the treated stream and discharges an oxygenated intermediate stream , wherein a first portion of the oxygenated intermediate stream is recycled to the digester as at least a portion of the digestive solvent; and a fuels processing reactor comprising a condensation catalyst that receives a second portion of the oxygenated intermediate stream and discharges a liquid fuel.2. A system comprising: a digester that receives a biomass feedstock and a digestive solvent operating under conditions to effectively remove nitrogen , phosphorus and sulfur compounds from said biomass feedstock and discharges a treated stream comprising a carbohydrate having less than 35% of the sulfur content and less than 35% of the nitrogen content based on untreated biomass feedstock on a dry mass basis; an aqueous phase reforming reactor comprising an aqueous phase reforming catalyst that receives the treated stream and discharges an oxygenated intermediate , wherein a first portion of the oxygenated intermediate stream is recycled to ...

CATALYTIC PYROLYSIS USING UZM-39 ALUMINOSILICATE ZEOLITE

A new family of coherently grown composites of TUN and IMF zeotypes has been synthesized and shown to be effective catalysts for catalytic pyrolysis of biomass. These zeolites are represented by the empirical formula. 3. The process of wherein the hydrocarbons produced include aromatic compounds and the selectivity to aromatic compounds within the condensable portion of the pyrolysis gases is greater than 33% by weight.4. The process of wherein the hydrocarbons produced include aromatic compounds and the selectivity to aromatic compounds within the condensable portion of the pyrolysis gases is greater 50% by weight.5. The process of wherein the hydrocarbons produced include aromatic compounds and the yield of aromatic compounds is greater than 2% by weight based upon the biomass.6. The process of wherein the hydrocarbons produced include aromatic compounds and the yield of aromatic compounds is greater than 3% by weight based upon biomass.7. The process of wherein the pyrolysis conditions include a temperature from about 300° C. to about 800° C.8. The process of wherein the catalyst is in a fluidized state.9. The process of wherein the contacting a carbonaceous biomass feedstock with a microporous crystalline zeolitic catalyst is carried out using a catalyst-to-carbonaceous biomass feedstock ratio of about 0.1 to about 200.10. The process of wherein the coherently grown composite of TUN and IMF zeotypes is thermally stable up to a temperature of greater than 600° C.11. The process of wherein the coherently grown composite of TUN and IMF zeotypes has a micropore volume as a percentage of total pore volume of greater than 60%.12. The process of wherein the microporous crystalline zeolitic catalyst comprises the heat transfer medium of a fast pyrolysis process.13. The process of further comprising regenerating the catalyst after contacting with the feedstock to form a regenerated catalyst and recycling the regenerated catalyst to the contacting step.15. The process of ...

PROCESS FOR PRODUCING TRANSPORTATION FUELS FROM OIL SANDS-DERIVED CRUDE

Disclosed are processes for extracting deasphalted crude oil from oil sand. Deasphalted crude oil can be extracted using a hydrocarbon recycle solvent stream having specified Hansen blend parameters, with the oil sand being contacted with the hydrocarbon recycle solvent stream in a contact zone of a vessel to separate not greater than 80 wt % of the bitumen present on the oil sand. The separated bitumen is considered a deasphalted crude oil stream, since it has an asphaltenes content substantially lower than that of the total bitumen initially present on the oil sand. The deasphalted crude oil stream can be treated using a hydrotreating catalyst or catalytic cracking catalyst to produce transportation fuel. 1. A process for treating deasphalted crude oil extracted from oil sand , comprising:supplying a hydrocarbon recycle solvent stream to a contact zone of a vessel, wherein the recycle solvent has a Hansen dispersion blend of not greater than 16, a Hansen polarity blend of less than 1 and a Hansen polarity blend of less than 2;supplying a feed stream of oil sand to the contact zone of the vessel, wherein the oil sand is comprised of at least 4 wt % total bitumen, based on total weight of the supplied oil sand;contacting the oil sand with the hydrocarbon recycle solvent in the contact zone of the vessel to separate not greater than 80 wt % of the bitumen present on the oil sand;removing at least a portion of the hydrocarbon solvent and the separated bitumen from the contact zone of the vessel;separating the hydrocarbon solvent from the separated bitumen to produce the hydrocarbon recycle solvent stream and a deasphalted crude oil stream, wherein the deasphalted crude oil stream has an ASTM D7169 5% distillation point of from 400° F. to 700° F., an asphaltenes content of not greater than 10 wt %, a Conradson Carbon Residue (CCR) of not greater than 15 wt % and sulfur content of not greater than 4 wt %, andtreating the deasphalted crude oil stream with a hydrotreating ...

Feedstock Conversion To Fuel On High Pressure Circulating Fluidized Bed

There is provided a process and systems for producing fuels via pyrolysis of carbonaceous feedstock under pressure and temperature in an efficient manner using a circulating fluidized bed with catalyst(s). The pressure and temperature are selected to provoke supercritical conditions, and pyrolysis, hydropyrolysis, hydrotreating, and optionally reforming treatment of the carbonaceous feedstock is carried out simultaneously in one reactor on a recirculating fluidized bed containing catalysts. 1. A process for the production of fuel comprising ,(a) providing in a reaction vessel a carbonaceous feedstock, a lift gas mixture of inert gas components, hydrogen, a fluidized bed of inert particulate solids and a hydrogenation catalyst; 'wherein the pyrolyzing comprises simultaneous pyrolysis, hydropyrolysis and hydrotreating of the carbonaceous feedstock to form said fuel.', '(b) pyrolyzing the carbonaceous feedstock to form fuel product components under temperature and pressure so as to establish supercritical conditions of temperature and pressure of at least one component of the carbonaceous feedstock, lift gas, hydrogen, water or fuel product;'}2. The process of wherein a hydrocarbon is present in said reaction vessel and said simultaneous pyrolysis claim 1 , hydropyrolysis and hydrotreating further includes simultaneous reforming wherein said hydrocarbon is reacted with water to form carbon monoxide and hydrogen.3. The process of wherein the reaction vessel is at a temperature of at least 647° K and a pressure of at least 22.1 MPa.4. The process of wherein said carbonaceous feedstock has a water content of 0% by weight to 97% by weight.5. The process of wherein the carbonaceous feedstock has a residence time is said reaction vessel of less than or equal to 5.0 seconds.6. The process of wherein said fuel has an oxygen level of less than or equal to 1000 ppm claim 1 , a nitrogen level of less than or equal to 15 ppm and a sulfur content of less than or equal to 3000 ppm.7 ...

CATALYTIC PROCESS FOR CO-PROCESSING OF CELLULOSIC BIOMASS AND HEAVY PETROLEUM FUELS

Disclosed herein is an economically viable co-process for converting biomass to liquid biohydrocarbon fuels and for upgrading heavy deteriorate petrol-oils to high value transportation fuels. In the process, cellulose, hemi-cellulose and lignin, which are composed of ligno-cellulosic biomass, are converted to the bio-hydrocarbons (alkanes and aromatics) that are currently derived almost exclusively from fossil fuels. The resulted hydrocarbon liquid can be separated against their boiling points for gasoline, diesel and heavy oils. The heavy oils can then cracked into lower molecular weight hydrocarbons. Meanwhile, the co-processed heavy petro-fuels are partially converted into lower molecular weight hydrocarbons that fall in the boiling point range of gasoline and diesel. 1. A process for co-processing of lignocellulosic biomass and heavy petroleum fuels , comprising:mixing lignocellulosic biomass, heated heavy petroleum fuels and a metal oxide based catalyst in a mixer to produce a mixture;{'sub': 2', '2, 'flowing the mixture to a reactor maintained at a pressure in a range from about 101 kPa to about 10 kPa and maintained at a temperature in a range from about 200° C. to about 450° C. and applying external forces to the mixture to produce longitudinal waves and shear stress in the mixture wherein responsively adiabatically erupting bubbles accompanied by high temperature and pressure are produced, and wherein in-situ hydrogen is generated, and wherein lignocellulosic biomass depolymerizes thereby generating a variety of free radicals and intermediates, wherein the free radicals and intermediates react with hydrocarbon molecules in the heavy petroleum fuels such that large hydrocarbon molecules are cracked into smaller hydrocarbon molecules, and a combination of intermediate with hydrocarbon molecules and in which oxygen is eliminated in the form of CO, COand HO;'}withdrawing gaseous products from the reactor to a distillation unit;flowing remaining solids and ...

PROCESS FOR PYROLYSIS OF COAL

A process for pyrolyzing a coal feed is described. The coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is fractionated into at least a pitch stream. The pitch stream is hydrogenated, and the hydrogenated pitch stream is recycled into the pyrolysis zone. The hydrocarbon stream may be processed further by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, and transalkylation. 1. A process comprising:pyrolyzing a coal feed into a coal tar stream and a coke stream in a pyrolysis zone;separating the coal tar stream into at least a pitch stream;hydrogenating the pitch stream; andrecycling the hydrogenated pitch stream into the pyrolysis zone.2. The process of wherein hydrogenating the pitch stream comprises contacting the pitch stream with a hydrogenation catalyst consisting of metal selected from the group consisting of Group VI metals (Cr claim 1 , Mo claim 1 , W) claim 1 , Group VII metals (Mn claim 1 , Tc claim 1 , Re) claim 1 , or Group VIII metals (Fe claim 1 , Co claim 1 , Ni claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Os claim 1 , Ir claim 1 , Pt) and combinations thereof supported on an inorganic oxide claim 1 , carbide or sulfide support claim 1 , including AlO claim 1 , SiO claim 1 , SiO—AlO claim 1 , zeolites claim 1 , non-zeolitic molecular sieves claim 1 , ZrO claim 1 , TiO claim 1 , ZnO claim 1 , and SiC.3. The process of wherein hydrogenating the pitch stream takes place at a temperature between about 250° C. and about 500° C.4. The process of wherein the hydrogenation takes place at a pressure between about 1.72 MPa (about 250 psig) and about 20.7 MPa (about 3 claim 1 ,000 psig).5. The process of wherein separating the coal tar stream further provides a hydrocarbon stream.6. The process of further comprising:recovering at least one product from the hydrocarbon stream.7. The process of further comprising:feeding additional coal feed into the pyrolysis zone; ...

HYDROTREATING PROCESS AND MULTIFUNCTION HYDROTREATER

A multifunction hydrotreater includes a particulate removal zone having a particulate trap to remove particulate contaminants from a coal tar stream and a demetallizing zone including a demetallizing catalyst to remove organically bound metals from the departiculated stream. The demetallizing zone is positioned after the particulate removal zone. The hydrotreater also includes a hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallization zone, which includes at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream. 1. A multifunction hydrotreater comprising:a particulate removal zone comprising a particulate trap to remove particulate contaminants from a coal tar stream;a demetallizing zone comprising a demetallizing catalyst to remove organically bound metals from the de-particulated stream, the demetallizing zone positioned after the particulate removal zone; anda hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone comprising at least one hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst to provide a hydrotreated coal tar stream, the hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation zone positioned after the demetallizing zone.2. The multifunction hydrotreater of claim 1 , wherein said hydrodesulfurization claim 1 , hydrodenitrogenation claim 1 , and hydrodeoxygenation zone comprises:a first zone comprising a first hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst; anda second zone comprising a second hydrodesulfurization, hydrodenitrogenation, and hydrodeoxygenation catalyst.3. The multifunction hydrotreater of claim 2 , wherein each of said first and second catalysts includes one or more of a nickel-molybdenum catalyst claim 2 , a cobalt-molybdenum catalyst claim 2 , a nickel-tungsten catalyst claim 2 , and a nickel-cobalt-molybdenum catalyst.4. The ...

NEEDLE COKE PRODUCTION FROM HPNA RECOVERED FROM HYDROCRACKING UNIT

A process for the treatment of a hydrocracking unit bottoms stream containing heavy poly-nuclear aromatic (HPNA) compounds and/or a fresh hydrocracking feedstock stream containing HPNA precursors to produce coke. The HPNA and/or HPNA precursors are removed from the hydrocracking unit bottoms stream and/or a fresh hydrocracking feedstock stream by solvent washing, and the HPNA and/or HPNA precursors are subjected to delayed coking for the production of coke. 1. A process for the treatment of a hydrocracking unit bottoms stream containing heavy poly-nuclear aromatic (HPNA) compounds and/or a fresh hydrocracking feedstock stream containing HPNA precursors to produce coke , the process comprising:a. contacting the hydrocracking unit bottoms stream and/or the fresh hydrocracking feedstock stream with an effective amount of adsorbent material in an adsorption unit to produce an adsorbent laden with HPNA compounds and HPNA precursors and an adsorbent treated hydrocarbon stream;b. washing the adsorbent laden with HPNA compounds and HPNA precursors with one or more solvents to extract the HPNA compounds and HPNA precursors and produce a solvent effluent stream;c. recovering and introducing the solvent effluent stream from the adsorption unit into a separation unit;d. recovering the one or more solvents from the separation unit for re-use as the one or more solvents;e. recovering the HPNA compounds and HPNA precursors from the separation unit;f. subjecting the HPNA compounds and HPNA precursors to a delayed coking process for the formation of needle, anode, or fuel grade coke.2. The process of claim 1 , wherein the contacting is with the hydrocracking unit bottoms stream claim 1 , and the process produces needle coke.3. The process of claim 1 , wherein the contacting is with the fresh hydrocracking feedstock stream claim 1 , and the process produces fuel coke.4. The process of claim 1 , wherein the contacting is with the hydrocracking unit bottoms stream and/or fresh ...

Liquid Fuel Production Process and Apparatus Employing Direct and Indirect Coal Liquefaction

A method and apparatus for producing liquids from coal including diesel and jet fuel blends and BTX in which the coal feed is converted to liquids in a DCL reactor, the produced liquids are upgraded and separated into, naphtha and DCL jet or diesel blend stock streams, the C3/180-350° F. stream is converted in a Fischer Tropsch reactor to produce a highly paraffinic diesel or jet fuel blend stock and the DCL and Fischer Tropsch blend stocks are blended in controlled ratios to produce premium diesel or jet fuels meeting applicable specifications. 1. A method for producing liquids from feed coal , comprising the steps of:a) supplying feed coal to a direct coal liquefaction (DCL) reactor and operating such reactor in a catalytic process for converting at least 50% of the supplied feed coal on a moisture and ash free (MAF) basis to coal liquids;b) upgrading coal liquids produced in step a to produce C3/180-400° F. and distillate blend stock streams;c) converting C3/180-400° F. produced in step b to syngas;d) converting syngas produced in step c by a Fischer Tropsch (F-T) process to predominately paraffinic liquids;e) upgrading the liquids produced in step d to produce a distillate blend stock stream and lighter products; andf) blending distillate blend stock streams produced in steps b and e to produce a liquid fuel or fuel blend stock.2. The method of wherein the stream being converted in step c is a C3/180-350° F. stream.3. The method of further including the step of recycling the lighter products produced in step e to be converted into syngas and used as a feed to the F-T process.4. The method of wherein the ratio of distillate blend stock produced by step b that is blended in step f with the distillate blend stock produced by step e is between 2 and 12 to 1 and the blended distillate fuel produced in step (f) is a diesel fuel or diesel fuel blend stock having a Cetane Number of greater than 47.5. The method of wherein the ratio of distillate blend stock produced by ...

Process, Method, and System for Removing Heavy Metals from Oily Solids

Oil is recovered from a mercury containing oily solids by mixing the solids with at least a treating agent selected from selected from flocculants, sulfidic compounds, demulsifiers, and combinations thereof, and optionally a solvent, forming a mixture. The mixture is then separated to recover a first phase containing treated oil having less than 50% of the original amount of mercury in the oily solids, and a second phase containing treated solids having a reduced concentration of mercury. The oily solids are selected from drilling muds; oily sediments coating inside of pipelines; sediment deposits on crude oil tanks, vessels, and separators; surface coating on equipment; slop oil from upstream operations; oily solids from heavy oil processing operations; solids recovered from processes for removing mercury from hydrocarbon materials; spill clean-up materials; and mixtures thereof. 1. A process to recover oil from oily solids containing a first amount of mercury and first concentration of mercury , the process comprising:mixing the oily solids containing mercury with a treating agent in an amount from 0.001-10 wt % based on weight of the oily solids, forming a mixture, wherein the treating agent is selected from flocculants, sulfidic compounds, demulsifiers, and combinations thereof;separating the mixture to recover a first phase containing treated oil having less than 50% of the first amount of mercury and a second phase containing treated solids having a second amount of mercury, wherein the second amount of mercury is less than the first amount.2. The process of claim 1 , wherein the first concentration of mercury in the oily solids is greater than 50% meta-cinnabar as determined by Reitveld XRD refinement.3. The process of claim 1 , the recovered treated oil has a mercury concentration of less than 100 ppbw.5. The process of claim 4 , further comprising separating the mixture of treated oil and solvent to recover treated oil having less than 50% of the first ...

TWO STAGE PROCESS FOR PRODUCING RENEWABLE BIOFUELS

A process for treating bio-oil or pyrolysis oil used to produce renewable biofuel. In a first stage, solids and/or organic reactive molecules within the feedstream are reduced without substantially deoxygenating the organic reactive molecules in the feedstream. The resulting feedstream is then introduced into a second hydrotreatment stage to produce deoxygenated bio-oil or pyrolysis oil. 1. A process for treating bio-oil or pyrolysis oil used to produce renewable biofuel , the process comprising:(a) introducing a feedstream containing bio-oil or pyrolysis oil to a first stage and reducing solids and/or organic reactive molecules within the feedstream in the first stage without substantially deoxygenating the organic reactive molecules in the feedstream;(b) introducing the feedstream having reduced solids and/or reduced organic reactive molecules to a second stage, wherein the second stage is a hydrotreatment stage, and further wherein the temperature in the second stage is greater than the temperature in the first stage and the pressure in the first stage is less than or equal to the pressure in the second stage and producing deoxygenated bio-oil or pyrolysis oil in the second stage.2. The process of claim 1 , wherein the first stage is a hydrotreatment stage.3. The process of claim 2 , wherein the first stage and the second stage are housed within the same hydrotreater reactor.4. The process of claim 1 , in which the entire liquid and gaseous effluent from the first stage is passed through to the second stage.5. The process of claim 3 , wherein the pressure in the hydrotreater reactor is from about 1 claim 3 ,500 psig to about 2 claim 3 ,000 psig.6. The process of claim 1 , wherein the first stage and the second stage are housed in different reactors.7. The process of claim 6 , wherein the feedstream is heated by an exothermic reaction upon entry into the hydrotreater of the second stage.8. The process of claim 2 , wherein the feedstream prior to entry into the ...

HIGH PRESSURE FEEDING SYSTEM FOR A LIQUID-BASED BIOMASS TO LIQUID REACTOR

The present disclosure provides methods to transfer a pressurized slurry of plant-based biomass into a reactor vessel. The methods allow for the transfer of practical-sized pieces of biomass in a slurry pressurized to above about 300 psi. 1. A method for transferring a slurry of plant-based biomass into a reactor vessel , the method comprising:providing plant-based biomass, wherein the biomass is made up of discrete pieces, wherein at least 20% of the discrete pieces have a greatest dimension of at least about ⅛ inch;combining a transport fluid with the biomass to form a pre-reaction slurry, wherein the pre-reaction slurry has a first weight ratio of fluid to biomass;pressurizing the pre-reaction slurry to a pressure above about 300 psi;removing at least a portion of the transport fluid from the pressurized pre-reaction slurry in a pre-reactor vessel to form a pressurized concentrated slurry with a second weight ratio of fluid to biomass, wherein the first weight ratio of fluid to biomass is greater than the second weight ratio of fluid to biomass;combining a reaction fluid from a reactor vessel with the pressurized concentrated slurry to form a pressurized reaction slurry; andtransferring the pressurized reaction slurry from the pre-reactor vessel into the reactor vessel, wherein the pressurized reaction slurry is received at the reactor vessel at a pressure above about 300 psi.2. The method of claim 1 , further comprising producing a reaction product comprising a liquid bio-oil product in the reactor vessel claim 1 , wherein the temperature in the reactor vessel is at least about 250° C. and the pressure in the reactor vessel is at least 300 psi.3. The method of claim 1 , wherein the biomass comprises cellulose claim 1 , hemicellulose claim 1 , lignin claim 1 , or a combination thereof.4. The method of claim 1 , wherein during the combining of the transport fluid with the biomass to form a pre-reaction slurry claim 1 , the transport fluid has a maximum temperature ...

Process for Extracting Lycopene

A process for extracting lycopene, comprising the following steps: pressing and dehydrating tomato pomace which is the by-products of tomato processing production, then drying it to control the water content in the range from 10% to 20%; crushing the dried tomato pomace, and separating tomato skins and tomato seeds by air blast process, granulating the separated tomato skins and extracting them, then purifying by removing impurity from the extracted lycopene with active carbon. The process uses the by-products of tomato production as raw material, thus increasing the utilization ratio of tomatoes; the way of separating the seeds and skins after dehydrating and drying can save water and reduce the discharge of pollutant; the addition of antioxidant in the process of drying avoids the impact of high temperature on lycopene; extracting after granulating the tomato skins significantly increases the extracting efficiency; treating the extracting solution with active carbon effectively can remove the pesticide residues, impurities, odor etc., and thus increase the quality of lycopene. 1. A process for extracting lycopene , comprising the following steps:a) dehydrating the raw material containing lycopene;b) drying the dehydrated raw material containing lycopene in the presence of antioxidant;c) coarsely crushing the dried raw material containing lycopene;d) separating the coarsely crushed raw material containing lycopene by air blast process, and taking the portion of raw material with a less relative density;e) finely crushing the portion of raw material with a less relative density obtained after separation step and granulating it;f) subjecting the resulting granules to extraction with organic solvent;g) treating the resultant of extraction with active carbon and filtering, then concentrating the filtrate to obtain lycopene product.2. The process for the extraction of lycopene according to claim 1 , wherein the raw material containing lycopene is tomato pomace ...

GREEN FLUID CATALYTIC CRACKING PROCESS

A process and apparatus for co-processing a hydrocarbon feedstock and a renewable biomass feedstock are described. Solid particles of biomass are introduced into the riser reactor zone and mixed with catalyst. The hydrocarbon feed stock is also introduced into the riser reactor zone. The solid particles of biomass react in the presence of the catalyst and are converted into oxygenated hydrocarbons, while the hydrocarbon reacts in the presence of the catalyst to form hydrocarbon products having a lower boiling point than the feedstock. 1. A process for co-processing a hydrocarbon feedstock and a renewable biomass feedstock comprising:introducing a lift gas into a fluid catalytic cracking riser reactor zone;introducing a catalyst into the riser reactor zone at a point downstream of where the lift gas is introduced;injecting solid particles of the biomass feedstock into the riser reactor zone;introducing the hydrocarbon feedstock into the riser reactor zone;mixing the solid particles of the biomass feedstock with the catalyst, the solid particles of the biomass feedstock reacting in the presence of the catalyst to form biomass products comprising gas, vapor, and char, and the gas and vapor biomass products further reacting in the presence of the catalyst to form oxygenated hydrocarbon products;mixing the hydrocarbon feedstock with the catalyst, the hydrocarbon feedstock reacting in the presence of the catalyst to form hydrocarbon products having a lower boiling point than a boiling point of the hydrocarbon feedstock; andrecovering the oxygenated hydrocarbon products, the hydrocarbon products, or both;wherein the solid particles of biomass feedstock are injected into the riser reactor zone at a point upstream of where the hydrocarbon feedstock is introduced and at or downstream of the point where the catalyst is introduced, or at a point downstream of where the hydrocarbon feedstock and the catalyst are introduced.2. The process of wherein the solid particles of biomass ...

PROCESS FOR CONVERTING A SOLID BIOMASS MATERIAL

A process for converting a solid biomass material comprising: a) providing a solid biomass material; b) contacting a feed comprising the solid biomass material and a petroleum-derived hydrocarbon composition, which petroleum derived hydrocarbon composition has a C7-asphaltenes content of equal to or more than 1.0 wt %, based on the total weight of the petroleum-derived hydrocarbon composition, co-currently with a source of hydrogen in one or more ebullating bed reactors comprising a catalyst at a temperature in the range from 350° C. to 500° C. to produce a reaction product. 1. A process comprising:a) providing a solid biomass material; andb) contacting a feed comprising the solid biomass material and a petroleum-derived hydrocarbon composition, which petroleum derived hydrocarbon composition has a C7-asphaltenes content of equal to or more than 1.0 wt %, based on the total weight of the petroleum-derived hydrocarbon composition, co-currently with a source of hydrogen in one or more ebullating bed reactors comprising a catalyst at a temperature in the range from 350° C. to 500° C. to produce a reaction product.2. The method of further comprising:c) fractionating the reaction product obtained in step b) into two or more product fractions and separating one or more product fraction(s) having a final boiling point of equal to or less than 370° C. at 0.1 MPa.3. The method of further comprising:d) upgrading the one or more product fraction(s) having a final boiling point of equal to or less than 370° C. at 0.1 MPa in one or more hydrocarbon conversion processes to produce one or more upgraded product fraction(s) having a final boiling point of equal to or less than 370° C. at 0.1 MPa;4. The method of further comprising:e) blending the one or more upgraded product fraction(s) having a final boiling point of equal to or less than 370° C. at 0.1 MPa with one or more other components to prepare a liquid fuel composition.5. The process of claim 2 , wherein the liquid fuel ...

ENZYMATIC DEPOLYMERIZATION AND SOLUBILIZATION OF CHEMICALLY PRETREATED COAL AND COAL-DERIVED CONSTITUENTS

Use of chemical pretreatment agents on the subsequent enzymatic conversion of coal is described. As an example, fungal manganese peroxidase (MnP) produced by the agaric white-rot fungus , where the enzyme MnP has little effect on the untreated coal controls, was investigated. The nature of pretreatment agents and their applied concentrations were found to have significant impact on subsequent enzymatic conversion of coal. Four agents were investigated: HNO, catalyzed HO, KMnO, and NaOH. Hydrogen peroxide was found to generate the greatest quantity of total organic carbon from the coal samples employed. Combined chemical and enzymatic treatment of coal is appropriate for enhanced depolymerisation of coal and coal-derived constituents and results in chemically heterogeneous and complex liquefaction products like humic and fulvic acids, which will have important ramifications in the generation of liquid and gaseous fuels from coals as nonpetroleum-derived fuel alternatives. 1. A method for depolymerizing and solubilizing coal and coal-derived constituents , comprising:treating the coal with an aqueous solution comprising at least one oxidizing agent, forming thereby treated coal and coal-derived constituents; andexposing the treated coal and coal-derived constituents to an aqueous solution comprising at least one enzyme effective for reacting with coal and coal-derived constituents.2. The method of claim 1 , wherein the at least one oxidizing agent is chosen from potassium permanganate and hydrogen peroxide.3. The method of claim 1 , wherein the at least one enzyme comprises peroxidase enzymes.4. The method of claim 3 , wherein the peroxidase enzymes comprise manganese peroxidase.5. The method of claim 4 , wherein the manganese peroxide is generated from fungus comprising white rot fungus.6Phlebia radiata, Clitocybula duseniiBjerkandera adusa. The method of claim 5 , wherein the white rot fungus is chosen from and claim 5 , and mixtures thereof.7Paecilomyces variotii.. ...

Process for Converting Biomass to Aromatic Hydrocarbons

The present invention provides methods, reactor systems, and catalysts for increasing the yield of aromatic hydrocarbons produced while converting biomass to hydrocarbons. The invention includes methods of using catalysts to increase the yield of benzene, toluene, and mixed xylenes in the hydrocarbon product. 1. A method for producing aromatic hydrocarbons , the method comprising:(a) processing a raw feedstock to form an intermediate feedstock;(b) converting the intermediate feedstock to a feedstock stream comprising an alcohol, a carboxylic acid, or combinations thereof;{'sub': 'eff', '(c) conditioning the feedstock stream to provide an oxygenate mixture having a H:Cratio of between 0.8 and 1.8; and'}(d) exposing the oxygenate mixture to a condensation catalyst to produce aromatic hydrocarbons.2. The method of claim 1 , wherein the intermediate feedstock comprises oxygenated hydrocarbons claim 1 , alkanes claim 1 , alkenes claim 1 , COmolecules claim 1 , hydrogen claim 1 , synthesis gas claim 1 , or combinations thereof.3. The method of claim 1 , wherein the converting step (b) comprises fermentation claim 1 , hydrogenolysis claim 1 , hydrolysis claim 1 , pyrolysis claim 1 , aqueous phase reforming claim 1 , alcohol synthesis claim 1 , Fisher-Tropsch synthesis claim 1 , steam reforming claim 1 , partial oxygenation claim 1 , or combinations thereof.4. The method of claim 1 , wherein step (b) comprises the steps of:fermenting the intermediate feedstock with one or more species of microorganism to form a fermentation broth comprising alcohols or carboxylic acids;removing the alcohols or carboxylic acids from the fermentation broth to provide the feedstock stream; andpurifying the feedstock stream prior to exposing the oxygenate mixture to the conditioning catalyst.5. The method of claim 1 , wherein the raw feedstock is biomass claim 1 , natural gas claim 1 , coal claim 1 , or petroleum.6. The method of claim 1 , wherein the processing step (a) comprises sugar ...

PRODUCING IMPROVED UPGRADED HEAVY OIL

A method is provided to produce a clean resid from a heavy hydrocarbon, the method including the steps of: feeding a heavy hydrocarbon to a conversion unit to convert at least a portion of the heavy hydrocarbon to lighter products and producing a resid, the resid comprising at least ten percent by weight components having true boiling points greater than 380° C. and further comprising at least some asphaltenes; contacting the resid with a naphtha to produce a mixed naphtha and resid, the naphtha comprising paraffin having from four to twelve carbons, the ratio of naphtha to resid high enough to result in precipitation of at least a portion of the asphaltenes in the resid; and separating a reject stream comprising asphaltenes and at least some solids from the resid to form a clean resid. 1. A method to produce a clean resid from a heavy hydrocarbon , the method comprising the steps of:feeding a heavy hydrocarbon to a conversion unit to convert at least a portion of the heavy hydrocarbon to lighter products and producing a resid, the resid comprising at least ten percent by weight components having true boiling points greater than 380° C., and the resid further comprising at least some asphaltenes;contacting the resid with a naphtha to produce a mixed naphtha and resid, the naphtha comprising paraffin having from four to twelve carbons, the ratio of naphtha to resid high enough to result in precipitation of at least a portion of the asphaltenes in the resid; andseparating a reject stream comprising asphaltenes and at least some solids from the resid to form a clean resid.2. The method of claim 1 , wherein the heavy hydrocarbon comprises bitumen and the conversion unit is a hydrocracker.3. The method of claim 1 , wherein subsequent to separation of the reject stream from the resid claim 1 , at least a portion of the naphthais removed from the clean resid.4. The method of claim 3 , wherein at least a portion of the removed naphthais recycled as naphtha.5. The method of ...

DEMULSIFIER INJECTION SYSTEM FOR FROTH TREATMENT PRODUCT QUALITY ENHANCEMENT

A method of improving the quality of diluted bitumen product in a bitumen froth treatment process is provided comprising: adding a demulsifier to bitumen froth to produce a mixture of bitumen froth and demulsifier, wherein the demulsifier is added at a dosage sufficient to reduce bitumen water content in the diluted bitumen product; subjecting the mixture of bitumen froth and demulsifier to a mixing energy input of greater than about 100 J/kg; adding a hydrocarbon diluent to the mixed mixture of bitumen froth and demulsifier to produce a diluent diluted bitumen froth; and subjecting the diluent diluted bitumen froth to a separation process to produce the diluted bitumen product. In one embodiment, demulsifier is first added to naphtha to form a demulsifier-diluent mixture which is then added to bitumen froth to form a diluted bitumen froth prior to subjecting the diluted bitumen froth to a mixing energy input of greater than about 100 J/kg. 1. A method of improving the quality of diluted bitumen product in a bitumen froth treatment process comprising:adding a demulsifier to bitumen froth to produce a mixture of bitumen froth and demulsifier, wherein the demulsifier is added at a dosage sufficient to reduce water content in the diluted bitumen product;subjecting the mixture of bitumen froth and demulsifier to a mixing energy input of greater than about 100 J/kg;adding a hydrocarbon diluent to the mixed mixture of bitumen froth and demulsifier to produce a diluent diluted bitumen froth; andsubjecting the diluent diluted bitumen froth to a separation process to produce the diluted bitumen product.2. The method of claim 1 , wherein the active chemical concentration of the demulsifier is about 35%.3. The method of claim 2 , wherein the dosage of the demulsifier ranges from about 1 ppm to about 50 ppm.4. The method of claim 1 , wherein the demulsifier comprises a polyglycol claim 1 , a polyglycol ester claim 1 , an ethoxylated alcohol or amine claim 1 , an ethoxylated ...

METHOD AND SYSTEM OF UPGRADING HEAVY OILS IN THE PRESENCE OF HYDROGEN AND A DISPERSED CATALYST

Methods and systems are provided for pretreating a heavy oil feed to a hydrocracker, such as a slurry hydrocracker to partially convert the stream and/or to convert catalyst precursors in the stream to catalytically active particles by hydrodynamic cavitation. 1. A method of upgrading a heavy oil comprising:subjecting a stream of heavy oil to hydrodynamic cavitation to produce a partially converted stream; andhydrocracking hydrocarbons of at least a part of the partially converted stream in the presence of a hydrogen containing gas and a dispersed catalyst or absorbent.2. The method of claim 1 , further comprising injecting a portion of the hydrogen containing gas into the stream of heavy oil prior to subjecting the stream of heavy oil to hydrodynamic cavitation.3. The method of claim 2 , wherein the portion of the hydrogen containing gas is provided prior to hydrodynamic cavitation is provided at a rate of 1-500 scf/B.4. The method of claim 1 , further comprising injecting the catalyst or absorbent into the stream of heavy oil so as to produce a stream of heavy oil with the catalyst or absorbent dispersed therein prior to hydrodynamic cavitation.5. The method of claim 4 , wherein the dispersed catalyst is present in the heavy oil at a catalyst concentrations from about 50 wppm to about 30 claim 4 ,000 wppm.6. The method of claim 1 , further comprising injecting a catalyst precursor into the stream of heavy oil so as to produce a stream of heavy oil with the catalyst precursor dispersed therein prior to hydrodynamic cavitation.7. The method of claim 6 , wherein the catalyst precursor is selected from the group consisting of a metal sulfate claim 6 , metal oxides claim 6 , organometallic compounds that thermally decompose to form solid particulates with catalytic activity claim 6 , and combinations thereof.8. The method of claim 6 , wherein the catalyst precursor is selected from a group consisting of phosphomolybdic acid claim 6 , moly-octanoate claim 6 , moly- ...

Rapid pyrolysis processing system and method

The present invention relates to a rapid pyrolysis system which is implemented in a non-catalytic disk flow form to obtain bio-oil using solid dry matter of biomass waste such as food waste, livestock manure, agricultural forest waste and the like as raw materials, and to a method thereof. According to the present invention, a silo supplies solid dry matter of biomass waste at a predetermined amount; an extruder is supplied with the solid dry matter of the biomass waste to extrude the same, and removes air included in the solid dry matter of the biomass waste; a reactor generates char and a vapor phase product by rapidly pyrolyzing the solid dry matter of the biomass waste having the air removed therefrom; a char rapid cooler rapidly cools the char, and a char storage stores the char rapidly cooled in the char rapid cooler; a condenser condenses the vapor phase product to generate bio-oil, and a bio-oil storage stores the bio-oil; the condenser discharges incondensable biogas which has not been condensed; and a biogas compressor compresses the biogas, and a biogas storage tank stores the biogas compressed by the biogas compressor.

Integrated process for the conversion of feedstocks containing coal into liquid products

Integrated process for the conversion of feedstocks containing coal into liquid products by the joint use of at least the following seven process units: coal liquefaction (CL), flash or distillation of the product obtained from the liquefaction (F), extraction with a solvent to remove the ashes (SDAsh), distillation to separate the solvent (RS), hydroconversion with catalysts in slurry phase (HT), distillation or flash of the product obtained from the hydroconversion (D), deasphalting with a solvent (SDA).

Method for producing coking binder

Method of producing ferro-coke through low temperature dry distillation

PURPOSE: A method for manufacturing ferro-coke using dry distillation at a low temperature is provided to effectively recycle ore dust, sludge, and remet generated from a FINEX process. CONSTITUTION: A method for manufacturing ferro-coke using dry distillation at a low temperature includes: a step of preparing a coal blend by blending coking coal(210) for manufacturing coke with at least one of fine iron ores(208) as sintering materials of which the average grain size is below 100 micrometers(excluding 0 micrometer), ore dust, sludge, and remet generated from a FINEX process; a step of manufacturing coke by dry-distilling the coal blend at a temperature of 900 to 1000 deg. C; and a step of maintaining the temperature at the upper side inside a dry quenching facility(214) fed with the coke between 1000 and 1050 deg. C by injecting air, and quenching in a nitrogen atmosphere.

Method of producing liquid hydrocarbons from coal

Pyrolysis system and pyrolysis method of bitumen

The present invention relates to a raw bituminous material pyrolysis system and a pyrolysis method thereof. According to an embodiment of the present invention, the raw bituminous material pyrolysis system includes: a storage tank storing raw bituminous materials; a pyrolysis reactor which receives the raw bituminous materials from the storage tank and decomposes the raw bituminous materials into pyrolysis gas and inorganic byproducts through a pyrolysis operation; a first separator which receives the pyrolysis gas generated in the pyrolysis reactor and separates solids included in the pyrolysis gas; a second separator which receives the pyrolysis gas separated from the solids in the first separator to separate the pyrolysis gas into gas products and liquid products; a third separator which receives liquid products separated by the second separator and separates oil from the liquid products; a combustor which receives the oil separated by the third separator and the gas products separated by the second separator to combust the gas products and oil to provide a heat source needed for the pyrolysis of the raw bituminous materials to the pyrolysis reactor; a first refiner which receives the inorganic byproducts decomposed in the pyrolysis reactor through the pyrolysis operation and recovers calcium oxide (CaO) from the inorganic byproducts by refining the inorganic byproducts; and a second refiner which receives the residual liquid products left after separating the oil in the third separator and refines the residual liquid products to recover aromatic hydrocarbon substances from the residual liquid products.

Complex method of converting coal containing raw material into liquid products

FIELD: mining. SUBSTANCE: invention refers to complex method of converting coal containing raw material into liquid products by means of combined implementation of at least following seven process blocks: liquation of coal (CL), instantaneous evaporation or rectification of product produced from liquation (IE), extraction with dissolvent for removal of non-combustible substances (ED), rectification for separation of dissolvent (SD), conversion with hydrogenation with catalyst in suspension phase (CH), rectification or instantaneous evaporation of product produced with conversion with hydrogenation (R), and de-asphalting with solvent; the method is characterised with following: it consists of phases - directing raw material containing coal to one or more, than one, stage (CL) of direct liquation of coal at presence of suitable catalyst of hydrogenation in disperse phase, and also at presence of hydrogen or hydrogen and H 2 S, - directing flow containing product obtained from reaction of coal liquation to one or more, than one, stage (IE) of instantaneous evaporation or rectification producing gaseous flow and liquid flow,- directing liquid flow to stage (ED) of extraction with dissolvent, which results in producing non-soluble flow consisting of mineral substance present in raw material and of not-reacted coal and liquid flow consisting of produced liquefied coal and applied dissolvent, - directing liquid flow consisting of liquefied coal and applied dissolvent to one or more stages of rectification to separate in essence dissolvent contained in liquid flow, which is returned to stage (ED) of extraction with dissolvent; - mixing liquid flow in essence consisting of liquefied coal and at least part of flow containing pyrobitumens produced in block of de-asphalting with suitable catalyst in disperse phase and directing obtained mixture to reactor of hydro-processing (CH) supplying hydrogen or mixture of hydrogen and H 2 S into it, - not necessary directing flow ...

Patent DE303992C

Process for coking or carbonizing carbonaceous materials at low temperature

PROCESS FOR IMPROVING THE QUALITY OF COKE COAL HAVING INSUFFICIENT COKEFIING POWER

PROCEDE POUR AMELIORER LA QUALITE DE CHARBONS A COKE POSSEDANT UN POUVOIR COKEFIANT INSUFFISANT. ON UTILISE UN AGENT D'AMENDEMENT DE CHARBONS A COKE QUI EST OBTENU EN ELIMINANT PAR DISTILLATION ENTRE 2 ET 20 DE COMPOSANTS A BAS POINT D'EBULLITION D'UN SOUS-PRODUIT DU CHARBON FORTEMENT AROMATIQUE OBTENU PAR DESINTEGRATION DE CHARBON BROYE ETOU DE MATIERES PREMIERES CARBONEES ANALOGUES, AVEC UNE COMBINAISON DE MELANGES D'HYDROCARBURES PROVENANT DU CHARBON ET DU PETROLE EN TANT QUE SOLVANT, DANS DES CONDITIONS DE TEMPERATURE ET DE PRESSION ELEVEES, ON AJOUTE LE PRODUIT ANALOGUE AU BRAI AINSI OBTENU, POSSEDANT UN POINT DE RAMOLLISSEMENT (SUIVANT KRAMER-SARNOW) COMPRIS ENTRE 90 ET 160C, DANS UNE PROPORTION DE 1 A 20 EN POIDS A DES CHARBONS POSSEDANT UN POUVOIR COKEFIANT INSUFFISANT, ET ON PROCEDE A LA COKEFACTION DU MELANGE. PROCESS FOR IMPROVING THE QUALITY OF COKE COAL HAVING INSUFFICIENT COKEFIING POWER. A COKE AMENDING AGENT IS USED WHICH IS OBTAINED BY DISTILLING BETWEEN 2 AND 20 OF LOW POINT COMPONENTS OF A HIGHLY AROMATIC COAL BY-PRODUCT OBTAINED BY DESINTEGRATION OF BROKEN COAL AND / OR RAW MATERIALS ANALOGUE CARBONES, WITH A COMBINATION OF HYDROCARBON MIXTURES FROM COAL AND OIL AS A SOLVENT, AT HIGH TEMPERATURE AND PRESSURE CONDITIONS, ADDED TO THE PIT OBTAINED WITH POINTS OF RAMOL -SARNOW) COMPRISED BETWEEN 90 AND 160C, IN A PROPORTION OF 1 TO 20 BY WEIGHT TO COAL HAVING AN INSUFFICIENT COKETING POWER, AND THE COKEFACTION IS MADE.

Ferrous coke manufacturing process

LIQUEFACTION OF COAL

PROCESS FOR IMPROVING THE QUALITY OF COKE COAL HAVING INSUFFICIENT COKEFIING POWER

LIQUEFACTION OF CHARCOAL

L'INVENTION A TRAIT A LA LIQUEFACTION DU CHARBON. DANS UNE LIQUEFACTION EN DEUX ETAPES DANS LAQUELLE DU CHARBON, DE L'HYDROGENE ET UN SOLVANT DE LIQUEFACTION SONT MIS EN CONTACT DANS UNE PREMIERE ZONE DE LIQUEFACTION THERMIQUE 13, CELA ETANT SUIVI DU RECUEIL D'UN LIQUIDE SENSIBLEMENT EXEMPT DE CENDRE ET D'UN COURANT POMPABLE DE MATIERE INSOLUBLE, QUI COMPREND DU LIQUIDE 454C, LE LIQUIDE SENSIBLEMENT EXEMPT DE CENDRE ETANT AMELIORE ENSUITE DANS UNE DEUXIEME ZONE DE LIQUEFACTION THERMIQUE 52, LE SOLVANT DE LIQUEFACTION POUR LA PREMIERE ETAPE COMPREND LE COURANT POMPABLE DE MATIERE INSOLUBLE PROVENANT DE LA PREMIERE ETAPE DE LIQUEFACTION, ET DU LIQUIDE 454C PROVENANT DE LA DEUXIEME ETAPE DE LIQUEFACTION. ON REDUIT AINSI LA QUANTITE DE MATIERE NECESSAIRE EN PROVENANCE DE LA DEUXIEME ETAPE POUR LA PREPARATION DU SOLVANT DE LIQUEFACTION DE LA PREMIERE ETAPE. THE INVENTION RELATES TO THE LIQUEFACTION OF COAL. IN A TWO-STAGE LIQUEFACTION IN WHICH COAL, HYDROGEN AND A LIQUEFACTION SOLVENT ARE PUT INTO CONTACT IN A FIRST THERMAL LIQUEFACTION ZONE 13, FOLLOWING THE COLLECTION OF A LIQUID SENIALLY FREE OF ASH AND INSOLUBLE MATERIAL PUMPABLE CURRENT, WHICH INCLUDES 454C LIQUID, THE SENSITIVELY ASH-FREE LIQUID IS IMPROVED THEN IN A SECOND THERMAL LIQUEFACTION ZONE 52, THE LIQUEFACTION SOLVENT FOR THE FIRST STEP THAT IS FREE OF ASH BEING IMPROVED THEN IN A SECOND THERMAL LIQUEFACTION ZONE 52, THE LIQUEFACTION SOLVENT FOR THE FIRST PURPOSE OF THE FIRST STEP IN THE FIRST PURPOSE OF THE FIRST PURPOSE OF THE FIRST PURPOSE OF THE MAIN LIQUEFACTION, AND 454C LIQUID FROM THE SECOND LIQUEFACTION STAGE. THUS REDUCES THE QUANTITY OF MATERIAL NECESSARY FROM THE SECOND STEP FOR THE PREPARATION OF THE LIQUEFACTION SOLVENT OF THE FIRST STEP.

Advanced process for the manufacture of metallurgical coke

Manufacture of town gas without special coal

Union on liquefied petroleum gas tank, has screws which engage in holes tapped in collar forming fixing point around opening in tank

The union (6) has holes for screws (12) which engage in holes (5) tapped in a collar (4) forming a fixing point around an opening (3) in the tank. A washer (13) placed between the head of each screw and the union is made of a material which is rigid at ambient temperature and which melts or becomes elastic at higher temperatures of the order of 120 deg C. The annular union carries a valve or other equipment such as filling (7) and user connections. Each washer is a disc of thickness between 0.5 and 1 mm. The washer is made of metal, preferably a quaternary eutectic metal alloy and in particular an alloy of one third by weight bismuth, one third lead and one third tin.

Process for the carbonization and gasification of peat, lignite, sapropel and similar bituminous fuels

Method for catalytic conversion of kerogen shale oil

本发明涉及一种油母页岩油催化转化的方法，该方法包括：将油母页岩油从流化床反应器的下部送入流化床反应器中与来自油母页岩油上方的催化转化催化剂接触并由下至上逆流进行催化转化反应；从流化床反应器顶部得到的反应油气送出流化床反应器，从流化床反应器底部得到的待生催化剂送出流化床反应器后进行汽提和再生，再生所得再生催化剂作为催化转化催化剂返回流化床反应器进行催化转化反应。本发明方法的油母页岩油转化率高，总液收高，汽油选择性好。

Process for coal hydrogenation incorporating a refining step

PROCESS FOR THE PRODUCTION OF COKE

PROCEDE POUR LA PRODUCTION DE COKE, EN PARTICULIER DE COKE SIDERURGIQUE ET DE COKE DE FONDERIE, UN MELANGE DE CHARBONS DE DEPART QUI PRESENTE UNE DUREE DE COKEFACTION PREDETERMINEE POUR LA COKEFACTION DANS DES CHAMBRES DE CARBONISATION ETANT REALISE A PARTIR D'UN OU DE PLUSIEURS CHARBONS DE DEPART, ET LE MELANGE DE CHARBONS DE DEPART ETANT COMPACTE DANS LES CHAMBRES DE CARBONISATION D'UN FOUR A COKE, COKEFIE DANS CELUI-CI ET DETOURNE EN TANT QUE GATEAU DE COKE EN FONCTION DE LA DUREE DE COKEFACTION. AU MELANGE DE CHARBON DE DEPART EST AJOUTE DE L'ALUMINIUM EN GRAINS DANS UNE PROPORTION DE PLUS DE 0,3 EN POIDS, ET DE PREFERENCE DANS UNE PROPORTION DE PLUS DE 2,5 EN POIDS. APRES UNE DUREE DE CUISSON INFERIEURE D'AU MOINS 5 A LA DUREE DE COKEFACTION, LE GATEAU DE COKE EST DEFOURNE. PAR RAPPORT A LA DUREE DE COKEFACTION, LA DUREE DE CUISSON PEUT ETRE REDUITE JUSQU'A 30. PROCESS FOR THE PRODUCTION OF COKE, IN PARTICULAR STEEL COKE AND FOUNDER COKE, A MIXTURE OF STARTING COALS WHICH HAS A PREDETERMINED COKEFACTION DURATION FOR COKEFACTION IN CARBONIZATION CHAMBERS BEING CARRIED OUT FROM OR FROM SEVERAL CHARBONS STARTING, AND THE MIXTURE OF STARTING COALS BEING COMPACT IN THE CARBONIZATION CHAMBERS OF A COKE OVEN, COKEFIES IN THE COKE AND BYPASS AS A COKE CAKE DEPENDING ON THE COKEFACTION DURATION. TO THE STARTING COAL MIXTURE IS ADDED GRAIN ALUMINUM IN A PROPORTION OF MORE THAN 0.3 BY WEIGHT, AND PREFERentially IN A PROPORTION OF MORE THAN 2.5 BY WEIGHT. AFTER A COOKING TIME AT LEAST 5 LESS THAN THE COKEFACTION TIME, THE COKE CAKE IS DEFURRED. IN RELATION TO THE COKEFACTION TIME, THE COOKING TIME CAN BE REDUCED UP TO 30.

Coke production method

Process for the distillation of coal and other solid fuels

Adding aluminium to improve the production of coke

Method of producing hydrocarbons from coal

Nach der Erfindung wird eine sehr vorteilhaftere Hydriergasführung in Kohleverflüssigungsanlagen dadurch erreicht, daß das in nachfolgenden Raffinationsstufen anfallende wasserstoffreiche Gase nicht in Kreislauf- und Überschußgas aufgeteilt wird, sondern als Gesamtmenge dem Frischwasserstoff der Hydrierung zugeführt wird.

Process for the catalytic hydrogenation of coal

The invention relates to a process for the catalytic hydrogenation of coal in a combined coal and heavy-oil chamber, the pasting of the coal with oil, originating from petroleum and/or coal, and with a hydrogenation catalyst, and the hydrogenation taking place at 10-30 MPa and 693-763 K, and the bottom product from the hot separator, after admixture of the distillation residue from the coal stripper distillation, being distilled in vacuo and the vacuum distillate, having a boiling range of 573-803 K under normal pressure, preferably 623-753 K, and a Conradson number of at most 0.2% by mass, being reacted in a second hydrogenation stage over fixed-bed catalysts at a pressure of 5-30 MPa and a temperature of 613-743 K and a feed rate of 0.5-3.5 volumes/volume x hour. The catalyst used has a high geometrical surface area/volume ratio of at least 50 cm<-1> and a pore volume of at least 0.5 cm<3>/g and also a specific surface area of at least 100 m<2>/g.

Process for destroying, or preventing the formation of ammonia during the coking of coal

746,697. Coking coal. BERGWERKSGES. HIBERNIA AKT.-GES. Feb. 17, 1954 [May 8, 1953], No. 4690/54. Classes 55(1) and 55(2). In the coking of coal in coke or like ovens in order to destroy or prevent the formation of ammonia during coking, the upper stratum of the coal in the coking chamber is superficially wetted with a suspension of a metal oxide catalytic contact mass. Suitable oxides are those of iron, aluminium, zinc, magnesium, manganese copper and nickel. In an example an oven containing 20 tons of coal was superficially wetted with a suspension of 2À4 kg. of ferric oxide containing 33À14 per cent iron, the layer thickness of the contact mass increasing towards the rising pipe of the oven. In comparison with a second oven containing untreated charge of coal 95 per cent of the ammonia was destroyed in the oven containing the treated charge.

Low temperature fuel treatment process

Reduction of dust emission in charging coke ovens with hot coal - by applicn of an aq binder

Reduction of dust emission during charging of coke ovens with hot coal, by mixing with 0.05-0.1 wt.% of an aq. binder soln. of 30-70% concn. Air pollution and collection of coal dust in the collector main and tar sepn. plant are reduced. The binder shows a prolonged agglomerating effect on the fine coal particles, and is readily dispersed over the coal. The binder soln. is a sulphite waste liquor and contains up to 1% wetting agent. It is pref. mixed with 10-50 times the quantity of crude coal tar to form an emulsion, which assists dispersion over the coal and improves the binding action.

TWO-STAGE PROCESS FOR COAL HYDROPYROLYSIS

A kind of civilian clean coke and its production method

一种民用洁净焦炭包括主要质量指标如下：发热量≥5700kcal/kg、灰分≤23%、挥发分≤5%、灰熔点≥1280℃、抗碎强度≥75%、固硫率≥95%、着火温度≤420℃、反应性≥40%、比表面=15～35m 2 /g。本发明具有易点火、火焰长、升温速度快、燃烧持续时间长脱硫效果好的优点。

Method for manufacturing additives and method for manufacturing coke unsing the same

본 발명은 코크스 제조를 위한 원료탄에 첨가되는 첨가제의 제조 방법으로서, 석탄을 마련하는 과정, 석탄과 혼합될 용매를 마련하는 과정, 석탄과 용매를 혼합하는 과정, 석탄과 용매가 혼합된 혼합물을 대상으로 액화 추출 반응시키는 과정 및 액화 추출 반응을 종료한 후, 액화된 용해분과 액화되지 않은 불용분을 회수하는 과정을 포함한다. 따라서, 발명의 실시형태들에 의하면, 석탄 특히, 자원이 풍부하고 가격이 저렴한 미점탄을 이용하여 코크스의 강도 향상을 위한 첨가제를 제조한다. 따라서, 첨가제 제조를 위한 비용을 줄일 수 있는 정점이 있다. 그리고, 원료탄으로 미점탄을 사용하더라도, 본 발명에 따른 첨가제에 의해 점결성을 확보할 수 있다. 이에, 배합탄에 포함되는 미점탄의 함량을 증대시킬 수 있는 장점이 있다. The present invention relates to a method for producing additives for coke production, comprising the steps of preparing coal, preparing a solvent to be mixed with coal, mixing coal and solvent, mixing a mixture of coal and solvent And recovering the liquefied and un-liquefied insoluble components after completion of the liquefaction extraction reaction. Therefore, according to the embodiments of the present invention, an additive for enhancing the strength of coke is produced using coal, particularly, a resource-rich and low-cost tin-coat. Thus, there is a peak that can reduce the cost for producing the additive. Also, even when the unbaked charcoal is used as the coking coal, the additive according to the present invention can ensure the integrity. Accordingly, there is an advantage in that the content of tin coals contained in the blend can be increased.

Integrated process for the conversion of feedstocks containing coal into liquid products

Integrated process for the conversion of feedstocks containing coal into liquid products by the joint use of at least the following seven process units: coal liquefaction (CL), flash or distillation of the product obtained from the liquefaction (F), extraction with a solvent to remove the ashes (SDAsh), distillation to separate the solvent (RS), hydroconversion with catalysts in slurry phase (HT), distillation or flash of the product obtained from the hydroconversion (D), deasphalting with a solvent (SDA).

Hydrogen gas distribution in coal liquefaction plants

A wall is covered with a facade formed from sheet metal panels. Each panel (40) has its lower edge (44) bent inwards (45) at right angles then downwards (47) and finally outwards. The narrow flange (48) is embedded in a sealing strip 852) which is fixed to the wall (56). The upper edge of each panel 840) is bent inwards to form the flange (49) and then inwards at 45 deg. to form the narrow flange (51) which is also embedded in the sealing strip (52) so that the ingress of water is prevented. The side flanges of the panel (40) are narrower than the bottom flanges so that a ventilation gap is formed on the side of each panel.

Patent JPS5945711B2

Sulfur component directional removal method for coking by high-sulfur coking coal blending

本发明涉及一种高硫炼焦煤配煤炼焦的硫分定向脱除方法，是在高硫炼焦煤中加入其质量25～50wt%的供氢添加剂，再以添加有供氢添加剂的高硫炼焦煤等质量替换炼焦基础配煤中5～15wt%的低硫炼焦煤，得到由供氢添加剂、高硫炼焦煤和炼焦基础配煤组合成的改性炼焦配煤进行炼焦，利用炼焦过程中供氢添加剂分解产生的富氢活性基进行原位内部供氢，使改性炼焦配煤中的硫更多的以含硫气体的形式释放，降低焦炭中的硫含量，在保证焦炭质量的前提下，合理利用劣质高硫炼焦煤资源，节约优质稀缺炼焦煤资源，降低焦炭生产成本。

Improved method of refining coal by short residence time hydrodi sproportionation to form a novel coal derived fuel system

본 발명은 짧은 체류시간 가수불균등화 반응에 의해 석탄을 정련하여 유체상 연료 시스템과 유용한 조생성물의 슬레이트를 생성시키는 개선된 방법에 관한 것이다. The present invention is directed to an improved process for refining coal by short residence time hydro disproportionation reactions to produce slate of fluid phase fuel systems and useful crude products. 다른 양태에 있어서, 본 발명은 짧은 체류시간 부분 액황에 의해 액체 탄화수소를 많이 생성하는 동시에 유용한 수소를 전환시키는 개선된 방법에 관한 것이다. In another aspect, the present invention is directed to an improved process for converting useful hydrogen while producing large amounts of liquid hydrocarbons by short residence time partial liquid sulfur. 이제 짧은 체류시간 가수불균등화(SRT-HDP) 공정은 저압 및 높은 휘발 온도에서 기체 생성 및/또는 축합반응을 일으키지 않으면서 보다 빠른 가열속도로 수행할 수 있음을 금방 알수 있다. 본 발명에 따라서 휘발성 물질-함유 탄소상 물질의 입자를 고형 유기물질을 급속하게 분해 및 휘발시키기에 유효한 속도로 가열한다. 분해 반응은 고형 유기 물질을 탄화수소 분획과 자유 래디칼로 휘발되며 이들은 탄소상 입자로 방출된다. 이와 같이 휘발된 탄화수소 분획은 분획의 수소화와 자유 래디칼 수소 캡핑을 촉진시키는데 유효한 수소화 온도에서 수소 공여체 다량 함유 기체 감소 대기와 밀접하게 접촉시킨다. 가수균열이 일어나지만(수소화 온도에 따라), 수소화 온도와 수소화 체류시간은 열 가수균열과 기화를 감소시키도록 선택한다. It can be readily seen that the short residence time hydro- disproportionation (SRT-HDP) process can be carried out at a higher heating rate without causing gas formation and / or condensation reactions at low pressures and high volatilization temperatures. According to the invention, particles of volatile-containing carbonaceous material are heated at a rate effective to rapidly decompose and volatilize the solid organic material. The decomposition reaction volatilizes the solid organic material into hydrocarbon fractions and free radicals, which are released as carbonaceous particles. This volatilized hydrocarbon fraction is in intimate contact with a gas-reducing atmosphere containing a large amount of hydrogen donor at a hydrogenation temperature effective to promote hydrogenation of the fraction and free radical hydrogen capping. Although hydrocracking occurs (depending on the hydrogenation temperature), the hydrogenation temperature and hydrogenation residence time are chosen to reduce ...

Improvement of the coke quality of coals with insufficient coking properties

Method of producing coke

1. СПОСОБ ПОЛУЧЕНИЯ КОКСА путем смешени  угольной шихты с добавкой и коксовани  полученной смеси, отличающийс  тем, что, с целью сокращени  времени коксовани{1 , в качестве добавки используют алюминий в количестве 0,3-2,5 мас.%. 2.Способ по п. 1, отличающийс  тем, что алюминий используют в зернистом виде. 3.Способ по п. 1, отличающийс  тем, что алюминий используют в виде тонких обрезков из алюминиевой пленки и/или алюминиевого листа. 4.Способ по п. 1, отличающийс  тем, что алюминий используют в виде порошка. (Л ИЗОБРЕТЕНИЯ ir 1. A method for producing a coke by mixing a coal charge with an additive and coking the mixture obtained, characterized in that, in order to reduce the coking time {1, aluminum is used as an additive in an amount of 0.3-2.5 wt.%. 2. A method according to claim 1, wherein aluminum is used in a granular form. 3. A method according to claim 1, characterized in that aluminum is used in the form of thin scraps of aluminum film and / or aluminum sheet. 4. A method according to claim 1, wherein aluminum is used in the form of a powder. (L INVENTIONS ir

Improvements in the distillation of coal

446,412. Materials for making gas and coke. ROBERTS, A., 20, Reydon Avenue, Wanstead, and SMITH, C. W., Bush House, Aldwych, both in London, [Representatives of ROBERTS, A. A.], and HACKFORD, J. E., 150, Southampton Row, London. July 26, 1934, Nos. 21833/34, 28427/34, 11785/35, 16011/35, and 18990/35. [Class 55 (ii)] Boric acid, sodium borate, or calcium borate is added to coal before distillation, with or without a soluble salt of a strong acid with a monovalent base, such as sodium or potassium chloride, or sodium sulphate or phosphate. The boron compound, which has a boiling point not exceeding 400‹ C., is used in quantity not more than 2 per cent by weight of the coal ; and the quantity of boron compound together with soluble salt does not exceed 4 per cent by weight of the coal. In an example, 0À5 per cent of borax with 0À5 per cent sodium chloride is used. The coal and added material may be charged into hot or cold retorts. Specifications 446,616 and 446,617, are referred to.

Method of producing liquid products from coal

Изобретение касаетс  производства жидкого топлива из угл  и может найти применение в нефтепереработке и углехимии. Цель изобретени  - повышение качества целевых продуктов и снижение ра схода катализатора. Процесс ведут смешением угл  с растворителем и катализатором, последующей гидрогенизацией полученной суспензии, разделением полученных продуктов гидрировани  в гор чем сепараторе на парогазовый поток и жидко-твердую фазу . Затем парогазовый поток подают на каталитическое гидрирование с выделением в виде жидкой фазы растворител , рециркулируемого на смешение с углем, и парогазовой фазы, подвергаемой дополнительному гидрированию с конденсацией парогазовой фазы и выделением целевых продуктов. Вакуумным испарением жидкотвердой фазы получают дистилл т, рециркулируемый в процесс. Целесообразно парогазовую фазу перед гидрированием дистиллировать с выделением целевой жидкой фазы . Парогазовый поток сначала подвергают разделению в гор чем сепараторе и выделенную жидкую фазу рецирку- лируют на смешение с продуктами гидрировани . Дистилл т, вьщеленный из жидкотвердой фазы, добавл ют к парогазовому потоку, направл емому на дополнительное каталитическое гидрирование , либо дистилл т добавл ют к продуктам гидрировани  перед раз делением и х в гор чем сепараторе, либо дистилл т подвергают дополнительному гидрированию с последующим рециркулированием на стадию смешени  с суспензией угл  и растворител . Эти услови  позвол ют снизить содержание основного азота в целевой фракции с . 20-320 С до 6 мг/кг и фе- нольного кислорода до 15 мг/кг. 3 з.п. ф-лы, 5 ил. СО с О) 00 4 Ю The invention relates to the production of liquid fuels from coal and can be used in oil refining and coal chemistry. The purpose of the invention is to improve the quality of the target products and reduce the catalyst flow. The process is carried out by mixing coal with a solvent and a catalyst, followed by hydrogenating the resulting suspension, separating the obtained hydrogenation products in a hot separator ...

Method of producing metallurgical coke

1343691 Coking coal NIPPON KOKAN KK 10 May 1971 [11 May 1970] 14081/71 Heading C5E A method of making metallurgical coke comprises carbonizing in a coke oven a coal to which has been added pieces, wire-like or band-like in form, of a metallic or non-metallic material. Examples include steel, stainless steel, copper, scrap metal, carbon fibres and carbon-rich synthetic resin. The material should have a width or diameter in the range 0À1 to 0À8 mm. and a length in the range 2 to 150 mm., and should comprise 0À01 to 0À5% by weight of the coal.

LIQUEFACTION OF COAL

DANS UNE LIQUEFACTION EN DEUX ETAPES, LE RESIDU A POINT D'EBULLITION SUPERIEUR A 454C PROVENANT DE LA SECONDE ETAPE EST EMPLOYE DANS LA FORMULATION DU SOLVANT DE LIQUEFACTION DE LA PREMIERE ETAPE. IN A TWO-STAGE LIQUEFACTION, THE RESIDUE WITH A BOILING POINT GREATER THAN 454C FROM THE SECOND STAGE IS USED IN THE FORMULATION OF THE FIRST STAGE LIQUEFACTION SOLVENT.

PROCEDURE FOR MANUFACTURING COOK

Process for process setting and heat recovery in the sump (bottom) phase hydrogenation of coal with integral gas phase hydrogenation

The process-relevant process parameters for the sump (bottom) phase hydrogenation of coal with integral gas phase hydrogenation, under conditions of economical heat recovery from the total system, are set as follows: in spite of increasing soiling of the slurry heat exchanger and increasing deactivation of the gas phase catalyst, the process-relevant temperatures of the intermediate separator and of the gas phase reactor are set in a defined manner by means of the head condenser (cooler) after the sump (bottom) hydrogenation and the head cooler (condenser) before the intermediate separator, and the waste heat of the sump (bottom) phase products is partially recovered via heating of the gas phase feedstock and resupplied to the slurry heating.

COAL LIQUEFATION PROCEDURE

Delayed coking process for producing free-flowing coke using an overbased metal detergent additive

A delayed coking process for making substantially free-flowing coke, preferably shot coke. A coker feedstock, such as a vacuum residuum, is heated in a heating zone to coking temperatures then conducted to a coking zone wherein volatiles are collected overhead and coke is formed. An overbased alkaline earth metal detergent additive is added to the feedstock prior to it being heated in the heating zone, prior to its being conducted to the coking zone, or both.

Method for manufacturing additives

본 발명은 코크스 제조를 위한 원료탄에 첨가되는 첨가제의 제조 방법으로서, 석탄 및 산성 용액을 마련하는 과정, 석탄과 산성 용액를 혼합하여, 석탄을 전처리하는 과정, 전처리된 석탄을 유기 용매와 혼합하여, 액화 추출 반응시키는 과정 및 액화 추출 반응을 종료한 후, 액화된 용해분을 회수하여 건조하는 과정을 포함한다. 따라서, 본 발명의 실시형태들에 의하면, 첨가제 제조를 위한 원료인 석탄을 산성 용액에서 전처리함으로써, 점결성을 가지는 유기 성분의 추출이 용이해 지며, 종래와 같이 액화 추출 반응을 유도하기 위하여 고온, 고압 조건으로 조성하고, 수소(H) 가스를 투입할 필요가 없다. 따라서, 고온, 고압으로 조성하고, 수소(H) 가스를 투입하기 위한 비용 및 시간을 절약할 수 있으며, 이로 인해 전체적인 첨가제의 생산율을 향상시킬 수 있는 효과가 있다. The present invention relates to a method for producing an additive to be added to coke for coke production, comprising the steps of preparing coal and an acidic solution, mixing coal and an acidic solution, pretreating the coal, mixing the pretreated coal with an organic solvent, And a step of recovering and drying the liquefied solute after completion of the liquefaction extraction reaction. Therefore, according to the embodiments of the present invention, it is possible to facilitate extraction of organic components having a cohesive property by pretreating coal, which is a raw material for producing additives, in an acidic solution, And it is not necessary to add hydrogen (H) gas. Therefore, it is possible to reduce the cost and time required for the introduction of the hydrogen (H) gas, and to improve the overall production rate of the additive.

Process for the production of diesel fuel from coal middle oil

Bei einem Verfahren zur Herstellung eines Dieseikraftstoffes, bei dem ein kohlestämmiges Mittelöl als Vorprodukt für die nachfolgende Weiterbehandlung in einer Raffinations- und Hydrocrackstufe unter Gewinnung des Dieseikraftstoffes gewonnen wird durch a) hydrierende Kohleverflüssigung in Anwesenheit von prozeßstämmigem Anreiböl (Anmaischöl), wasserstoffhaltigem Kreislaufgas und feinteiligem Katalysator (Sumpfphase), b) Abtrennen der nicht verflüssigten Feststoffe aus der Sumpfphase in einem Heißabscheider bei etwa den gleichen Temperaturen und Drücken wie im Verflüssigungsreaktor, c) Kondensieren des dampfförmigen Kopfproduktes des Heißabscheiders in einem Zwischen- und einem Kaltabscheider unter gleichzeitiger Rückgewinnung des Kreislaufgases, wird - bei gleichbleibender Gesamtölausbeute aus der Kohle - der Mittelölanteil und insbesondere der als Dieselkraftstoff verwendbare Anteil des Mittelöls dadurch erhöht, daß d) das Kondensat aus dem Zwischen- und aus dem Kaltabscheider einer unter atmosphärischem Druck arbeitenden Destillationskolonne zugeführt und dort in die vier Siedeschritte Schnitt I unter 180 °C siedend, Schnitt II zwischen 180 und 250 °C siedend, Schnitt III zwischen 250 und 350 °C siedend und Schnitt IV über 350 °C siedend zerlegt wird sowie e) die Schnitte II und IV als Anreiböl, der Schnitt I als weiterzuverarbeitendes Kohleleichtöl und der Schnitt III als Vorprodukt für die nachfolgende Weiterbehandlung unter Gewinnung des Dieselkraftstoffes verwendet werden. In a process for the production of a diesel fuel in which a carbon-derived medium oil as a preliminary product for the subsequent further treatment in a refining and hydrocracking stage to obtain the diesel fuel is obtained by a) hydrogenating coal liquefaction in the presence of process-derived grinding oil (mashing oil), hydrogen-containing cycle gas and finely divided catalyst (Bottom phase), b) separating the non-liquefied solids from the bottom phase in a hot separator at about the same ...

Improved desulfurization process

A system which circulates fluidizable solid particles through a fluidized bed reactor, a fluidized bed regenerator, and a fluidized bed reducer to thereby provide for substantially continuous desulfurization of a hydrocarbon- containing fluid stream and substantially continuous regeneration of the solid particles is disclosed.

Direct coal liquefaction method

oisture- and ash-free coking coal is micronized and admixed with a recycle oil, whereafter it is rapidly hydrogenated and one portion of the residue of the fractional distillation of the hydrogenation product is sent to hydrotreating, together with hydrogen. Conventional catalysts can be used both for the hydrogenation and the hydrotreating.A gaseous fraction, consisting of water vapour, hydrogen sulphide, ammonia and Cl-C4 hydrocarbon is obtained along with gasoline.Gasoil can be obtained together with gasoline.

Improved Process of Increasing the Calorific Value of Fuel and Apparatus therefor.

23,080. Verity, J. W., and Lewis, F. C., [Higgins, E. B., partly]. April 20, 1911. Fuel such as coal, slack, coke, or peat is subjected in the presence of moisture and at ordinary temperature to the action of halogens, especially chlorine; or compounds of halogens with each other, such as iodine chloride; or compounds with hydrogen and oxygen, such as hypochlorous acid; or oxygen compounds of chlorine, such as the peroxide, to increase the calorific value and remove mineral or other impurities. The treatment may be with a solution of the reagent, by soaking, spraying, or percolation, or by a counter-current arrangement; or the reagent may act upon the moist fuel; or the reagent may be liberated electrolytically in the fuel, placed adjacent to or forming an anode which may be stationary or moving.

METHOD FOR REDUCING PRESSURE IN COKE OVENS

PROCEDE POUR REDUIRE LA PRESSION DANS LES FOURS A COKE. SELON CE PROCEDE, ON DISPERSE STATISTIQUEMENT DANS LE CHARBON DES FLOCONS FORMES D'UNE MATIERE QUI NE PASSE PAS PAR UNE PHASE PLASTIQUE DE MANIERE A FORMER DES PASSAGES DE GAZ TRAVERSANT LES COUCHES PLASTIQUES DU COKE EN FORMATION. CES FLOCONS ONT DE PREFERENCE UNE EPAISSEUR D'ENVIRON 3,2 A 19MM ET UNE LONGUEUR ET UNE LARGEUR D'ENVIRON 25 A 127MM. ON UTILISE DE PREFERENCE DE LA SCIURE, OU BIEN DE LA PATE A PAPIER, DES JOURNAUX, DES DECHETS MENAGERS OU AGRICOLES. ON OBTIENT AINSI LA SUPPRESSION DE LA POINTE DE PRESSION EN COURS DE COKEFACTION SANS REDUIRE LA QUALITE DU COKE. PROCESS FOR REDUCING PRESSURE IN COKE OVENS. ACCORDING TO THIS PROCESS, FLAKES FORMING FROM A MATERIAL WHICH DOES NOT GO THROUGH A PLASTIC PHASE ARE STATISTICALLY DISPERSED IN THE COAL, SO AS TO FORM GAS PASSAGES THROUGH THE PLASTIC LAYERS OF THE COKE IN FORMING. THESE SNOWFLAKES PREFERRED A THICKNESS OF ABOUT 3.2 TO 19MM AND A LENGTH AND WIDTH OF APPROXIMATELY 25 TO 127MM. SAWDUST IS PREFERREDLY USED, OR PAPER PULP, NEWSPAPERS, HOUSEHOLD OR AGRICULTURAL WASTE. THUS IS OBTAINED THE REMOVAL OF THE PRESSURE POINT DURING COKEFACTION WITHOUT REDUCING THE QUALITY OF THE COKE.

Improvements in the manufacture or processing of coke and the manufacture of coke gas

Multistage process for the direct liquefaction of coal

oisture- and ash-free coking coal is micronized and admixed with a recycle oil, whereafter it is rapidly hydrogenated and one portion of the residue of the fractional distillation of the hydrogenation product is sent to hydrotreating, together with hydrogen. Conventional catalysts can be used both for the hydrogenation and the hydrotreating.A gaseous fraction, consisting of water vapour, hydrogen sulphide, ammonia and Cl-C4 hydrocarbon is obtained along with gasoline.Gasoil can be obtained together with gasoline.