1505results about "Coke ovens" patented technology

The present invention relates to processes for preparing gaseous products, and in particular methane and / other value added gases such as hydrogen, via the catalytic hydromethanation of a carbonaceous feedstock in the presence of steam and syngas, wherein a hydromethanation reactor is combined with a syngas generator in a particular combination.

A hydrocarbon product stream having hydrocarbons with boiling points in the aviation fuel range is produced from renewable feedstocks such as plant and animal oils. The process involves treating a renewable feedstock by hydrogenating, deoxygenating, isomerization, and selectively hydrocracking the feedstock to produce paraffinic hydrocarbons having from about 9 to about 16 carbon atoms and a high iso / normal ratio in a single reaction zone containing a multifunctional catalyst, or set of catalysts, having hydrogenation, deoxygenation, isomerization and selective hydrocracking functions.

A premium synthetic lubricating oil base stock having a high VI and low pour point is made by hydroisomerizing a Fischer-Tropsch synthesized waxy, paraffinic feed wax and then dewaxing the hydroisomerate to form a 650-750° F.+ dewaxate. The waxy feed has an initial boiling point in the range of about 650-750° F., from which it continuously boils up to at least 1050° F. and has a T90-T10 temperature difference of at least 350° F. The feed is preferably hydroisomerized without any pretreatment, other than optional fractionation. The 650-750° F.+ dewaxate is fractionated into two or more base stocks of different viscosity.

The invention relates to iron coke for a blast furnace and a preparing method thereof. The iron coke comprises 5wt%-20wt% of iron ore powder and 80wt%-95wt% of mixed coal; the mixed coal is formed by mixing 25wt%-29wt% of one third of coking coal, 40wt%-44wt% of coking coal, 7wt%-11wt% of lean coal, 6wt%-10wt% of gas-fat coal and 12wt%-16wt% of fat coal; the iron ore powder and the mixed coal are mixed uniformly with water and tamped before entering the blast furnace, and are placed into the blast furnace when the temperature is 800 DEG C, the temperature is increased at the speed of 2 DEG C per minute to 3 DEG C per minute, the iron ore powder and the mixed coal are discharged from the blast furnace when the temperature is 950-1050 DEG C, and the iron coke is obtained by adopting a wet way of quenching the coke. According to the iron coke and the preparing method, the performance, the ratio, the particle size and the composition and the like of the iron ore powder and the mixed coal are optimized, and the strength and the reactivity of the iron coke can meet the requirement of the blast furnace process under the circumstance of not adding binding agents.

The present invention is coking blend method with gas coal, and different kinds of coking coal with required vitrinite reflectance distribution are blended. The blended coals include gas-fat coal 5-10 wt%, fat coal 5-20 wt%, 1 / 3 coking coal 30-45 wt%, coking coal 30-45 wt% and lean coal 10-18 wt%. The method of the present invention has reasonable utilization of the coking coal resource, accurate coal blending and high coke quality.

A process derived hydrogen donor solvent is used to increase the maximum resid conversion and conversion rate in an ebullated bed resid hydrocracker. The hydrogen donor solvent precursor is produced by hydroreforming reactions within the resid hydrocracker, recovered as the resin fraction from a solvent deasphalting unit, regenerated in a separate hydrotreater reactor, and recycled to the ebullated bed resid hydrocracker. The major advantage of this invention relative to earlier processes is that hydrogen is more efficiently transferred to the resin residual oil in the separate hydrotreater and the hydrogen donor solvent effectively retards the formation of coke precursors at higher ebullated bed resid hydrocracker operating temperatures and resid cracking rates.

A gasifier is disclosed combining a fixed bed gasification section where coarse fuel is gasified and an entrained flow gasification section where fine fuel is gasified. The fixed bed section includes upper and lower sections. Coarse fuel is devolatilized in the upper fixed bed section and subjected to elevated temperatures sufficient to crack and destroy tars and oils in the effluent gases. The entrained flow gasification section is disposed in a lower plenum adjacent the lower fixed bed section. A plurality of injection ports are configured to introduce oxygen, steam, or air into different sections of the gasifier to control temperature and operating conditions. Activated carbon may be formed in the upper fixed bed section and in the entrained flow section. The activated carbon may be used as a sorbent to remove pollutants from the effluent gases. The gasifier may be used with various coarse and fine fuel feedstocks.

The invention relates to an improvement method of needle coke used refined aromatic hydrocarbon oil. The improvement method of the needle coke used refined aromatic hydrocarbon oil comprises the following steps: taking oil rich in aromatic hydrocarbon, heating the oil to 400-490 DEG C by a heating furnace, introducing the oil into a polymerization tower, taking the material at the bottom of the polymerization tower and introducing the material into a flash tower, taking the flashed material at the bottom of the flash tower, cooling the material to the room temperature, introducing the material into a gas-liquid separator, controlling the vacuum degree in the gas-liquid separator to be 5-10kpa, taking the material at the bottom of the gas-liquid separator, and enabling the material to flow into a refined aromatic hydrocarbon oil buffering tank to prepare the raw material which is refined aromatic hydrocarbon oil for producing needle coke. The improvement method of the needle coke used refined aromatic hydrocarbon oil is simple in process; the oil rich in aromatic hydrocarbon with low content of aromatic hydrocarbon in domestic oil refining plant is processed, the content of the aromatic hydrocarbon is increased; the prepared refined aromatic hydrocarbon oil is applicable to production of the needle coke.

This invention relates to a novel integrated hydroconversion process for converting heavy atmospheric or vacuum residue feeds and also converting and reducing impurities in the vacuum gas oil liquid product. This is accomplished by utilizing two residue hydroconversion reaction stages, two vapor-liquid separators, and at least two additional distillate ebullated-bed hydrocracking / hydrotreating reaction stages to provide a high conversion rate of the residue feedstocks.

A process for producing a hydrocarbon from biomass. A feed stream having free fatty acids, fatty acid esters or combinations thereof is provided. The feed stream is heated in the presence of a first catalyst to produce a partially hydrodeoxygenated stream. The partially hydrodeoxygenated stream is heated in the presence of a second catalyst to produce an effluent stream containing the hydrocarbon.

The invention relates to a heavy oil processing method by combining thermal cracking and gasification. A raw material is conducted to a reactor from the bottom of a gas-solid separation region, is dispersed into oil drops through an atomizer; a lightweight component of the oil drop is volatilized to form oil gas in the falling process of the oil drops in a thermal cracking region; a heavy component is condensed to form coke, wherein the oil gas carries out thermal cracking reaction; coke particles drop into a gasification region and carry out gasification reaction at a temperature of between 800 and 1,600 DEG C to generate synthetic gas; one part of residual fine coke particles drop into an ash hopper to form clinker; the other part of the residual fine coke particles and the generated gas flow upwards together, are contacted with the descending liquid drops and carry out heat exchange; gas phase and coke in the gas-solid separation region of the upper part of the rector are separated; the separated fine coke particles re-drop into the thermal cracking region and the gasification region and continuously react; and the separated gas phase flows out of the rector, enters a subsequent separation system and is separated into synthetic gas, dry gas, liquid gas, gasoline, diesel, oil slurry and other products. The method has high gasification efficiency and reasonable utilization of heat energy and reduces energy consumption.

The present invention relates to hydrocarbons and particularly to the manufacture of hydrocarbon components suitable as aviation fuels or jet fuels and as blending stocks for aviation fuels. The process comprises the stages, wherein in the first stage an oil feed of biological origin and hydrogen gas are subjected to conditions sufficient to effect hydrodeoxygenation in the presence of a hydrodeoxygenation catalyst to yield n-paraffins;in the second stage the n-paraffins and hydrogen gas are subjected to conditions sufficient to effect isomerisation in the presence of an isomerisation catalyst to yield isoparaffins and separating fractions; andrecycling the fraction boiling at a temperature above 200° C. under atmospheric pressure obtained from the second stage to reisomerisation, where isomerisation is effected in the presence of an isomerisation catalyst.

A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone and a hydrotreating zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated solvent deasphalting, hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises: charging the crude oil to a solvent deasphalting zone with an effective amount of solvent for producing a deasphalted and demetalized oil stream and a bottom asphalt phase; charging the deasphalted and demetalized oil stream and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream.

The present invention is directed to the upgrading of heavy petroleum oils of high viscosity and low API gravity that are typically not suitable for pipelining without the use of diluents. The method comprises introducing a particulate heat carrier into an up-flow reactor, introducing the feedstock at a location above the entry of the particulate heat carrier, allowing the heavy hydrocarbon feedstock to interact with the heat carrier for a short time, separating the vapors of the product stream from the particulate heat carrier and liquid and byproduct solid matter, collecting a gaseous and liquid product mixture comprising a mixture of a light fraction and a heavy fraction from the product stream, and using a vacuum tower to separate the light fraction as a substantially bottomless product and the heavy fraction from the product mixture.

A device and method are provided for manipulating petroleum, non-conventional oil and other viscous complex fluids made of hydrocarbons that comprise enforcement of fluid in a multi-stage flow-through hydrodynamic cavitational reactor, subjecting said fluids to a controlled cavitation and continuing the application of such cavitation for a period of time sufficient for obtaining desired changes in physical properties and / or chemical composition and generating the upgraded products. The method includes alteration of chemical bonds, induction of interactions of components, changes in composition, heterogeneity and rheological characteristics in order to facilitate handling, improve yields of distillate fuels and optimize other properties.

An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil is provided to produce olefinic and aromatic petrochemicals. Crude oil and hydrogen are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity. Hydroprocessed effluent is thermally cracked in the presence of steam to produce a mixed product stream, which is separated. Hydrogen from the mixed product stream is purified and recycled to the hydroprocessing zone, and olefins and aromatics are recovered from the separated mixed product stream.

Applicants have developed a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen gas, while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor. A portion of the unconverted oil is then converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, products, hydrogen, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. Additional oil may be added at the interstage feed inlet, possibly in combination with slurry. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

A process for upgrading a hydrocarbon feedstock containing waxy components and having an end boiling point exceeding 650° F., which includes contacting the feedstock at superatmospheric hydrogen partial pressure with an isomerization dewaxing catalyst that includes ZSM-48 and contacting the feedstock with a hydrocracking catalyst to produce an upgraded product with a reduced wax content. Each catalyst is present in an amount sufficient to reduce the cloud point and the pour point of the feedstock at a conversion of greater than about 10%, and an overall distillate yield of greater than about 10% results from the process.

A method for producing biofuels is provided. A method of making biofuels includes dewatering substantially intact algal cells to make an algal biomass, extracting neutral lipids from the algal biomass, and esterifying the neutral lipids with a catalyst in the presence of an alcohol. The method also includes separating a water soluble fraction comprising glycerin from a water insoluble fraction comprising fuel esters and distilling the fuel esters under vacuum to obtain a C16 or shorter fuel esters fraction, a C16 or longer fuel ester fraction, and a residue comprising carotenoids and omega-3 fatty acids. The method further includes hydrogenating and deoxygenating at least one of (i) the C16 or shorter fuel esters to obtain a jet fuel blend stock and (ii) the C16 or longer fuel esters to obtain a diesel blend stock.

A process for producing a hydrocarbon from biomass. A feed stream having free fatty acids, fatty acid esters or combinations thereof is provided. The feed stream is heated in the presence of a first catalyst to produce a partially hydrodeoxygenated stream. The partially hydrodeoxygenated stream is heated in the presence of a second catalyst to produce an effluent stream containing the hydrocarbon.

A process is provided that is directed to a steam pyrolysis zone integrated with a hydroprocessing zone including residual bypass to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises separating the crude oil into light components and heavy components; charging the light components and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering a combined stream of pyrolysis fuel oil from the separated mixed product stream and heavy components from step (a) as a fuel oil blend.

A process for hydrocracking biomass, and the hydrocarbons produced therefrom. A feed stream having free fatty acids, fatty acid esters, or combinations thereof is contacted with a first catalyst under hydrogen pressure and heat. The hydrocarbon product stream which is comprised predominantly of n-paraffins is separated into heavy and light fractions. The heavy fraction is contacted with a second catalyst under hydrogen pressure and heat to produce an effluent stream which is combined with the light n-paraffin fraction to form a unique middle distillate product useful as a diesel or jet fuel.

A drying and upgrading device for lignite and a technological method thereof, relating to the lignite efficient utilization field. The invention comprises a chamber dryer for the lignite, a fluidized-bed pyrolysis device, a combustion device for the pyrolysed gas, and other adjuvant devices. The dried lignite is fed into the pyrolysis device, volatiles and liquid products are extracted, the volatiles are sent into the combustion device to be burnt to generate fume and steam, the fume and a part of the steam are sent into the drying device to serve as the drying media. The rest steam is sent into the pyrolysis device to provide the heat source for the pyrolysis. A chain conveying method and a method of chamber drying / discharge of the fume and the steam are adopted for the drying device. Two different steams with different temperatures are generated in the combustion device and used for drying and pyrolysis of the lignite respectively. Compared with the prior technology, the device and the method provided by the invention have the advantages of safe and reliable operation, reasonable design, steady running in the large-scale application, and capability of improving the comprehensive utilization rate of the lignite.

Applicants have developed a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil, hydrogen, and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is separated internally, within one of more of the reactors, to separate only the converted oil and hydrogen into a vapor product while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor as a liquid product. A portion of the unconverted oil is then converted to lower boiling point hydrocarbons in the next reactor, once again creating a mixture of unconverted oil, hydrogen, converted oil, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. The oil may alternately be partially converted, leaving a concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

A divided wall column can allow for fractionation of multiple streams while maintaining separate product qualities. Effluents from multiple stages of a reaction system can be processed in a single divided wall column. The divided wall column can produce multiple cuts from each separated area, as well as at least one output from a common area. At least one reaction stage can advantageously have a continuous liquid phase environment.

A dual riser FCC process for converting C3 / C4-containing feedstocks to aromatics. First and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) in a dual-riser FCC unit with a gallium enriched catalyst to make an effluent rich in ethylene, propylene and aromatics. The first riser (2) is operated at less severe conditions than the second riser (4) and can receive a relatively heavy feed such as gas oil. The feed to the second riser (4) includes propane, for example LPG, propane recycle from the C3 splitter (72), etc. The FCC catalyst can include gallium to promote aromatics formation.

A process for the production of very high quality base oils optionally with simultaneous production of high quality middle distillates comprises the stages for hydrotreatment, preferably hydrocracking, on Y or beta zeolite, and atmospheric distillation. The effluent is subjected to a catalytic dewaxing on the ZSM-48 catalyst. The process then comprises a hydrofinishing stage for hydrogenating the aromatic compounds, preferably on a catalyst that comprises at least one noble metal of group VIII, chlorine and fluorine, and the stages of atmospheric and vacuum distillation. The hydrofinishing stage is conducted at a temperature lower by 20-200° C. than the catalytic dewaxing stage.

The instant invention is directed to a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen, while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor where a portion of the unconverted oil is converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, converted oil, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

The present invention is one kind of coke coal blending ratio and coking process. The coke coal consists of fat coal 20-23 weight portions, coking coal 50-55 weight portions, 1 / 3 coking coal 15-20 weight portions, and lean coal 8-12 weight portions. The compounded coal has the quality including ash content 9-10 %, sulfur content 0.65-0.73 %, volatile component 24-26 %, G value 83-88, Ymm of 16-20, and Xmm of 20-30. The quality parameters, vitrinite reflectances and microscopic ingredients of the said four kinds of coal are specifically defined. During the coking process, the mixed coal material is sintered at 1200 deg.c for not less than 16 hr. The present invention can obtain coke with high strength.