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US20040238406A1 - Method for producing fuel distillates - Google Patents

Method for producing fuel distillates Download PDF

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Publication number
US20040238406A1
US20040238406A1 US10/486,028 US48602804A US2004238406A1 US 20040238406 A1 US20040238406 A1 US 20040238406A1 US 48602804 A US48602804 A US 48602804A US 2004238406 A1 US2004238406 A1 US 2004238406A1
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weight
oil
fraction
boiling point
slate
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Juri Kanataev
Mikhail Yulin
Evgeny Ruzhnikov
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/22—Non-catalytic cracking in the presence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils

Definitions

  • This invention relates to the field of oil refining industry and, more particularly, to methods for distillation of heavy still bottoms for producing fuel distillates by way of thermal conversion and hydrocracking with the use of donor-solvent processes.
  • the said mixture is subjected to thermal conversion (viscosity breaking) for obtaining the products having lower viscosity and reduced amounts of heavy metals.
  • thermal conversion viscosity breaking
  • Such stock and its distillates may be reprocessed into light fuel distillates by way of catalytic cracking.
  • the advantage of this process is its technological flexibility, i.e., by modifying the process parameters (temperature, pressure, volumetric rate, etc.) it is possible to achieve the maximum conversion and yield of the desired products.
  • thermal conversion or hydrocracking is used for mixtures containing heavy oil stock (fuel oil, tar oil, mixtures of Western Siberian oils, heavy oils from the Buzatchi and Mangyshlak fields), sapropelite - Leningrad, Baltic, sulfur shale or Kuzbass sapromixite 1-10% by weight, crude shale oil or its fraction 220-340° C., 1-10% by weight, or tetralin or its alkyl derivatives at elevated temperature and pressure with subsequent separation of fuel distillates.
  • the yield of fuel distillates is in the range of 55-60% by weight of the stock when using thermal conversion and up to 90% by weight of the stock when using hydrocracking.
  • distillates produced by way of thermal conversion or hydrocracking may be reprocessed for producing light motor fuels, including motor gasoline and diesel fuel.
  • Tetralin is produced by way of hydrogenising technical products containing condensed aromatic hydrocarbons, mainly naphthalene and its alkyl derivatives.
  • the process of producing tetralin and its alkyl derivatives is very expensive.
  • the final product is also relatively expensive.
  • the closest to this invention is a method of producing fuel distillates, which includes mixing residual oil stock with ground sapropelite and a liquid activating additive, homogenizing the obtained mixture and its thermal conversion or hydrocracking with subsequently separating the desired products (RU, A1 No. 2128207, 1999).
  • a hydrogenated fraction with the boiling point in the range of 300 to 400° C. is used in the amount of 1-5% by weight as the liquid activating additive.
  • the yield of fuel distillates is 55-60% by weight when using thermal conversion and up to 90% by weight when using hydrocracking.
  • the known solution is disadvantageous in that the use of a hydrogenised fraction with the boiling point 300 to 400° C. as the aromatic additive also increase the cost of the final products due to the fact that for its production the additional stage of distillation separation and further hydrorefining are necessary in order to ensure higher hydrogen-donor properties for the fraction with the boiling point 300 to 400° C.
  • the objective of this invention is to raise the efficiency of the method of refining heavy still bottoms, including reducing the cost of the final product.
  • the technical result of the invention is the elimination of using a hydrogenised fraction with the boiling point 300 to 400° C., while preserving the production capacity of the method.
  • the ground sapropelite before homogenization is activated mechanically in, at least, one disperser, as sapropelite a slate coal is used, which contains, in per cent by weight: 45-60% of the mineral part and 40-55% of the organic part, as the liquid activating additive the shale oil fraction is used with the boil-off limits 200 to 400° C. and containing hydrogen in the amount of at least 10.0% by weight, said slate coal and the shale oil fraction being taken in the quantities (% by weight of the stock) from 1 to 5 and from 1.0 to 6.0, respectively.
  • slate coals which contain, in grams per ton: molybdenum 3-15, nickel 20-35, cobalt 3-10, chrome 30-40, copper 15-40 and lead 5-20.
  • slate coals are used, the mineral part of which contains, in per cent by weight: SiO 2 30-40 Cao 25-40 Na 2 O 0.3-3.0 Fe 2 O 3 5-10 MgO 1.5-5.0 P 2 O 5 0.1-0.7 Al 2 O 3 8-15 SO 3 1.5-5.0 TiO 2 0.5-0.7 K 2 O 2.0-5.0
  • homogenization is carried out in a mixer at the temperature from 80 to 100° C.
  • the mechanical-chemical treatment is carried out in the known apparatus of Desi-14 type as well as in known dispersers (homogenizers) and homo-mixers.
  • heavy oil stock (fuel oil, tar oil) is successively mixed with the liquid activating additive and sapropelite, where the sapropelite (slate coal) is preliminarily ground down to the particle size of 30 to 100 microns (preferably 50 to 100 microns).
  • the obtained mixture is mixed and intensively homogenized for the purpose of uniformly distribute the activating additives in the whole quantity of the raw stock.
  • the raw stock after such treatment may be subjected to thermal conversion or hydrocracking in less strict conditions in comparison to the known methods, namely: at the reactor temperatures from 415 to 440° C., the temperatures of the raw stock exiting the ftrnace from 450 to 490° C., the pressure from 4 to 10 MPa, the volumetric rate from 0.8/hour to 2.0/hour. But the most important aspect is that the processes of thermal conversion and hydrocracking are going without expensive catalysts.
  • the optimal conditions are those, at which the maximum quantity of the fmal product is obtained and no undesirable significant coke formation is observed, especially in the tube furnace and in the reactor.
  • the usual separation methods are evaporation at a reduced (in comparison to the reaction conditions) pressure, separation of the liquid products from the slime (concentrate of the solid products), which may be carried out by any known methods, e.g., centrifugation, filtration, etc, separation of the liquid and the vaporous products of the reaction, etc.
  • centrifuging with the application of a decanter centrifuge.
  • the liquid additive also possesses hydrogen-donor properties.
  • a certain catalytic impact on the transformation of the initial raw stock and the products of its decomposition is exerted by the mineral part of the additive, which consists, to a significant degree, of aluminosilicates and ferric salts.
  • a slate coal which contains the mineral part (45-60% by weight) and the organic part (40-55% by weight), is used as the sapropelite.
  • slate coals which contain (in grams per ton) molybdenum 3-15, nickel 20-53, cobalt 3-10, chrome 30-40, copper 15-40 and lead 5-20, are used.
  • the mineral part of slate coals contains, in per cent by weight: SiO 2 30-40 Cao 25-40 Na 2 O 0.3-3.0 Fe 2 O 3 5-10 MgO 1.5-5.0 P 2 O 5 0.1-0.7 Al 2 O 3 8-15 SO 3 1.5-5.0 TiO 2 0.5-0.7 K 2 O 2.0-5.0
  • the shale oil is used, which consists of the fraction with the boil-off limits of 200 to 400° C. and containing hydrogen in the amount of at least 10.0% by weight.
  • Such shale oil is produced by the known method, i.e., the heat treatment of slate coals with a solid heat carrier.
  • the fine-grained slate coal is dried and subjected to thermal destruction with a solid heat carrier with the formation of a gas-vapor mixture. The latter, after its dry cleaning, is sprayed with a condensate mixture, and the first condensate of the heavy fraction of oil is removed.
  • a specific feature of the thus obtained shale oil fraction with the boiling point from 200 to 400° C. is that its composition includes elevated quantities of hydrogen (at least 10% by weight) due to the presence of a significant quantity of hydroderivative polycyclic aromatic compounds. These compounds are represented by a group of 2-4-ring hydroaromatics (di-, tetra- and hexaderivatives of alkyl naphthalene, anthracene, phenanthrene, benzanthracene, pyren, fluoranthen, chrysene).
  • This fraction with the boiling point from 200 to 400° C. is a rather efficient donor of hydrogene at thermal conversion and hydrocracking of residual oil stock (preferably, tar oil).
  • the optimal content of hydrogen in shale oil with the boiling point from 200 to 400° C. should be at least 10% by weight. If the hydrogen quantity in shale oil is lowered to a value below 10% by weight, the yield of fuel distillates in the processes of thermal conversion and hydrocracking is significantly reduced. An increase of the hydrogen quantity in shale oil to a value above 12% by weight does not influence the yield of fuel distillates, but makes the final product more expensive.
  • the shale oil fraction with the boil-off limits of 200 to 400° C. and containing hydrogen in the quantity of at least 10% by weight is introduced in the quantity of 1.0 to 6.0% by weight of the oil stock.
  • a certain positive result may be also achieved when carrying out the processes of thermal conversion or hydrocracking in the presence either of a slate coal only or shale oil only.
  • the yield of light oil products would be significantly lower due to the fact that the reaction system would not have the necessary quantity of hydroaromatics possessing the hydrogen-donor properties.
  • the desired fuel distillates when separating the products of thermal conversion and hydrocracking in accordance with the invention, are common broad fuel fractions: the gasoline fraction boiling off within the limits of 40-180° C., the diesel fuel fraction boiling off within the limits of 180-360° C., and the gas-oil fraction boiling off within the limits of 360-500° C.; their properties and methods of use are well known to specialists in the field of oil refining.
  • the produced fuel distillates may be re-refmed into the components of commercial fuels or to commercial fuels by the usual methods of oil refining that are common in the industry.
  • the gasoline fraction may be subjected to hydrorefining on special catalysts for the production oof the gasoline component having the octane number 82-93 under study method.
  • the diesel fuel fraction after hydrorefining may be used as a commercial diesel fuel with the cetane number 48-50.
  • Such fuel fractions are the main products when carrying out the process in accordance with the invention. They may be easily re-refined into commercial fuels, i.e., this invention enables to get the result that is not obvious from the state of the art.
  • the slate coal is fed on the band conveyor to the crusher with the bag filter 2 , where it is crushed to the particle size of 8 mm.
  • the 8 mm slate coal particles is delivered to the “Desi-14” crusher 3 , where the slate coal is further crushed for obtaining particles having the size of 1 mm.
  • the crushed slate coal if fed via the discharging passage for the fmal grinding to the “Desi-14” disintegrator 4 , where it is ground to the particle size less than 100 microns.
  • the “Desi-14” disintegrator is equipped with a cyclone, an air filter, a bag filter and a star feeder.
  • the ground slate coal is fed via the discharging passage of the “Desi-14” disintegrator to the jigger screen with the mesh up to 140 microns, and then to the temporary storage bin 5 .
  • the complex for slate coal disintegration has the control panel with the protection and starting devices.
  • the jigger screen is designed for separating slate coal particles having the size more than 140 microns.
  • the slate coal ground to the particle size of 100 microns is fed to the section for raw stock preparation. This stage is very important for the whole chain of the production process.
  • the preparation of the raw stock is carried out as follows. To the heated mixer or another mixing device 9 , at which the temperatures of 80-100° C. is maintained, the shale oil from the tank 7 , the tar oil (or fuel oil) from the tank 8 and, last, the slate coal are fed by turns. First, to the mixing device 9 the shale oil is fed by the pump, then the tar oil from the tank 8 and the slate coal through the metering device 6 are fed.
  • the operations of feeding the three components of the raw stock mixture are carried out while operating the mixing device for the purpose of preventing sedimentation of slate coal to the bottom of the mixer. If the mixing device may not ensure the efficient mixing of the 3-component mixture, it is advisable to use the pump-dispensers 10 for more thorough mixing (homogenization). At this time the temperature in the section for raw stock preparation should be maintained at the level of 80-100° C. for ensuring the tar oil pumpability.
  • the prepared raw stock mixture is delivered to the back-up mixer 11 , from where it is fed by the raw stock high-pressure pump 12 to the heat exchanger 13 and from there—to the raw stock heating furnace 14 .
  • the furnace 14 has two sections—A and B.
  • the temperature in the section A is maintained within the limits of 380-400° C.
  • the temperature at the exit of the furnace is maintained at 460-490° C. depending on the type of treated raw stock.
  • the partially transformed raw stock is delivered to the lower part of the hollow non-heated reactor 15 , where the reactions of the raw stock hydrocracking go at the hydrogen pressure 6-10 MPa, the volumetric rate of 1.0-2.0/hour and the reactor-height temperatures of 425-450° C.
  • the hydrogen-containing gas (hydrogen content 80%) is fed in the quantity of 1,000-1,500 cubic meters per 1 cubic meter of the raw stock.
  • the gas-vapor flow is directed to the heat exchanger 13 and further to the hot separator 16 , where the temperatures of 270-320° C. and the pressure 10 MPa are maintained.
  • the fractions boiling off up to the temperatures of 360-380° C. mainly escape at the top part of the hot separator, and the fractions boiling off at the temperatures above 360-380° C. together with the solid products escape at the lower part of the hot separator.
  • the upper flow in the hot separator together with the hydrogen-containing gas after passing through the cooling system 17 is accumulated in the high-pressure separator 18 where the hydrogen-containing gas is separated from the hydrogenate.
  • the hydrogen-containing gas is fed for mixing with fresh hydrogen and then to the recirculation compressor 25 .
  • the hydrogenate from the high-pressure separator passes to the low-pressure separator 19 and further via the pipeline to the accumulating tank for further refining.
  • the product from the lower part of the hot separator goes via the baffle valve 20 to the cooler 21 for cooling and is transported via the pipeline to the decanter centrifuge 22 for separating the liquid products from the solid ones.
  • the liquid products are mixed with the hydrogenate (the top part of the hot separator), and the mixture is fed, after heating in the furnace 24 to the cracking fractionator 26 for distillation in order to produce the gasoline fraction with the boilin g point up to 180° C., the diesel fuel fraction with the boiling point 180-360° C., the gas-oil fraction with the boiling point 360-500° C. and the residue (recycle) boiling off at temperatures above 500° C.
  • the solid products are collected in the receiver 23 and then are supplied to the bitumen production facilities for producing bitumens used in the road construction or are used as the raw stock for extracting vanadium, nickel and rare-earth metals from them.
  • the tar oil from the mixture of Western Siberian oils is used, which has the following characteristics: density—984 kg/m 3 , elemental composition, in % by weight: C—86.8; H—10.86; S—1.5; N—0.3 (oxygen and impurities—the rest to 100.0), viscosity—28.0 sSt, coking ability—10.0% by weight, asphaltenes—9.3% by weight, boil off at temperatures lower 500° C.—24.5% by weight, contains vanadium—140 g/t, nickel—70 g/t.
  • the as-received Baltic slate coal is used, which has the following characteristics, in % by weight: A d —46.70; CO d 2 min —8.32; C daf —81.3; H daf —9.25; N daf —0.28; S d t —0.90; W d —3.0.
  • the liquid activating additive the shale oil is used, which consists of the fraction with the boil-off limits of 200-400° C. and has the following characteristics: density—995 kg/m 3 , refraction index—1.5696, molecular weight—290, asphaltenes content—3.8% by weight, elemental composition, in % by weight: C—82.95, H—10.0, S—0.6; pour point—minus 20° C., viscosity—14.9 sSt at 50° C.
  • the process of thermal conversion or hydrocracking of tar oil is carried out either in a continuous-flow plant with a 6 L reactor or in an industrial plant with a 10 m 3 reactor.
  • the conditions of thermal conversion are: temperature 425-450° C., pressure (of nitrogen, intrinsic hydrocarbon gases, hydrogen-containing gas) 3-5 MPa, volumetric rate 1.0-2.0/hour, gas recirculation 600-800 L per 1 L of the raw stock.
  • the conditions of hydrocracking are: temperature 425-450° C., pressure (of hydrogen or hydrogen-containing gas) 6.0-10.0 MPa, volumetric rate 1.0-2.0/hour, gas recirculation 1,000-1,500 L per 1 L of the raw stock.
  • the quantity of the liquid aromatic additive is 0.5-6.0%, the quantity of sapropelite is 0.5-5.0% of the tar oil weight.
  • the slate coal and oil mixture for the processes of thermal conversion or hydrocracking is prepared by successively mixing the residual charge stock, in particular tar oil, the fraction of shale oil with the boiling point 200-400° C. and as-received slate coal.
  • the mixing is carried out in a heated mixer at the temperature not lower than 85° C. for 2.5 hours, and then the prepared mixture is subjected to homogenization in a disperser device or in a process activation plant.
  • the base mixture was prepared by mixing 10 t of tar oil, 0.2 t of slate coal and 0.3 t of the shale oil fraction with the boiling point 200 to 400° C. and the hydrogen content of 10% by weight. The mixing was carried out in a heated mixer at a temperature not lower than 85 ° C. for 2.5 hours. Then the mixture was subjected to activation and homogenization. In this example the slate coal content was 0.5% by weight.
  • the resulting products had the following characteristics: the gasoline fraction with the boiling point up to 180 ° C.: refraction index 1.4216; elemental composition, in % by weight: C 84.53, H 13.75, S 0.46, N 0.06; the diesel fuel fraction with the boiling point 180-360 ° C.: refraction index 1.4786, elemental composition, in % by weight: C 85.89, H 12.26, S 0.69, N 0.06; the gas-oil fraction with the boiling point 360-500 ° C.: refraction index 1.521 1: elemental composition, in % by weight: C 86.60, H 11.24, S 1.29, N 0.21; the residue with the boiling point above 500 ° C.: density 1,011 kg/m 3 , elemental composition, in % by weight: C 88.18, H 9.48, S 1.70, N 0.64.
  • the base mixture was prepared by mixing 7.5 t of tar oil, 2.5 t of recycle with the boiling point above 500° C., 0.2 t of slate coal and 0.3 t of the shale oil. The mixing was carried out in a heated mixer at a temperature not lower than 85° C. for 2.5 hours. Then the mixture was subjected to activation and homogenization. In this example the mineral part content of the slate coal was 40% by weight.
  • the resulting liquid products were subjected to centrifuging for separating the solid components.
  • the hydrogenate was distilled into fractions having the boiling point up to 180° C. (gasoline), 180-360° C. (diesel fuel), 360-500° C. (gas-oil) and the residue with the boiling point above 500° C.
  • the residue with the boiling point above 500° C. was returned as the recycle for hydrocracking, being mixed with the base tar oil.
  • the resulting products had the following characteristics: the fraction with the boiling point up to 180° C.: refraction index 1.4728; elemental composition, in % by weight: C 86.25, H 12.20, S 1.26, N 0.07; the fraction with the boiling point 180-360° C.: refraction index 1.728, elemental composition, in % by weight: C 86.25, H 12.20, S 1.26, N 0.07; the fraction with the boiling point 360-500° C.: refraction index 1.5305: elemental composition, in % by weight: C 85.95, H 11.13, S 1.86, N 0.31; the residue with the boiling point above 500° C.: density 1,000 kg/m 3 , coking ability 6.5%, asphaltenes content 6.3%, vanadium content 300 g/t, nickel content 130 g/t; elemental composition, in % by weight: C 88.08, H 9.50, S 1.70, N 0.62.
  • the prepared mixture contained, in % by weight: tar oil -100.0, Baltic slate coal—2.0, including the mineral part—1.3; shale oil—3.0.
  • the thermal cracking was carried out in then following conditions: temperature—425° C., pressure—4 MPa, volumetric rate—1.0/hour.
  • the following yield was achieved, counting on tar oil, in % by weight: gas—7.8, water—1.0, the fraction with the boiling point 180-360° C.—42.9, the fraction with the boiling point 360-520° C.—15.1, the residue with the boiling point above 520° C.—22.5, coke on the mineral part of sapropelite—3.7.
  • the prepared mixture contained, in % by weight: tar oil—100.0, Baltic slate coal—2.0, including the mineral part—1.3; shale oil—3.0; hydrogen consumption—2.5.
  • the thermal cracking was carried out in then following conditions: temperature—425° C., pressure—10 MPa, volumetric rate—1.0/hour.
  • the technical result of the invention may not be achieved due to lowering in the yield of the desired product.
  • Exceeding the 5% limit of the slate coal content does not result in an increase in the desired product yield, but only contributes to rise in the cost of the final product of the tar oil thermal conversion process. due to ineffective consumption of slate coal.
  • slate coal should be added to tar oil in the amounts of 1.0-5.0% by weight with respect of the raw stock.
  • the quantity of the liquid activating additive should be 1.0-6.0% by weight, counting on the tar oil.
  • Examples 11-15 illustrate this invention in which the shale oil fraction with the boiling point 200-400° C. is used as the liquid activating additive.
  • the content of the said additive in Examples 11-15 is (in % by weight), respectively, 0.5, 1.0, 2.0, 3.0, and 6.0 counting on tar oil.
  • the total yield of the fractions with the boiling points up to 180 ° C., 180-360 ° C., and 360-500 ° C. is in its maximum at 68.5-70.7 (in the conditions of Examples 13 and 14).
  • the liquid additive content of 6.0% by weight the desired products yield is slightly higher (74.5% by weight in the conditions of Example 15).
  • Exceeding the 6% content limit of the fraction with the boiling point 200-400 ° C. results only in a significant rise in the cost of the final product due to ineffective consumption of shale oil.
  • the shale oil fraction with the boiling point 200-400 ° C. with its hydrogen content not less than 10.0% by weight should be added to the residual oil stock in the amount of 1.0-6.0% by weight, counting on the raw stock.
  • Example 16 illustrates the use, while carrying out the tar oil thermal conversion process according to this invention, of slate coal only in the amount of 2.0% by weight, counting on tar oil.
  • the yield of the three fractions (boiling points up to 180 ° C., 180-360 ° C., 360-500 ° C.) in the conditions of Example 16 is 57.8% by weight, counting on tar oil.
  • Example 17 illustrates the parameters of the tar oil thermal conversion process, in which the shale oil fraction with the boiling point 200-400 ° C. and hydrogen content of 10.0% by weight is used as the liquid activating additive.
  • the desired products yield in the conditions of Example 17 is 47.9% by weight, counting on tar oil.
  • Examples 23-27 illustrate this invention, in which slate coal is used as the solid activating additive at hydrocracking of tar oil.
  • the tar oil content in Examples 23-27 is (in % by weight): 0.5, 1.0, 2.0, 3.0, 5.0.
  • the total yield of the fractions with the boiling points up to 180° C., 180-360° C., and 360-500° C. is in its maximum at 93.7% by weight, counting on tar, for Examples 25 and 26.
  • the slate coal content of 5% by weight the fuel distillates yield is lower than at that of 2.0 and 3.0% by weight counting on tar oil.
  • the technical result of the invention may not be achieved due to lowering in the yield of the desired products.
  • Exceeding the 5% limit of the slate coal content does not result in an increase in the desired product yield, but only contributes to rise in the cost of the final product of the tar oil hydrocracking process due to ineffective consumption of slate coal.
  • slate coal should be added to tar oil in the amounts of 1.0-5.0% by weight with respect of the raw stock.
  • the quantity of the liquid activating additive should be 1.0-6.0% by weight, counting on the tar oil.
  • Examples 28-32 illustrate this invention in which the shale oil fraction with the boiling point 200-400° C. and the hydrogen content not less than 10.0% by weight is used as the liquid activating additive at hydrocracking of tar oil.
  • the content of the said additive in Examples 28-32 is, respectively, 0.5, 1.0, 2.0, 3.0, and 6.0 in % by weight, counting on the raw stock.
  • the total yield of the fractions with the boiling points up to 180° C., 180-360° C., and 360-500° C. is in its maximum at 92.3-93.7 (in the conditions of Examples 30 and 31).
  • the shale oil fraction with the boiling point 200-400° C. with its hydrogen content not less than 10.0% by weight should be added to the residual oil stock in the amount of 1.0-6.0% by weight, counting on the raw stock.
  • Example 33 illustrates the use, while carrying out the hydrocracking process according to this invention, of slate coal only in the amount of 2.0% by weight, counting on tar oil.
  • the yield of the three fractions (boiling points up to 180° C., 180-360° C., 360-500° C.) in the conditions of Example 33 is 63.6% by weight, counting on tar oil.
  • Example 34 illustrates the parameters of the tar oil hydrocracking process, in which the shale oil fraction with the boiling point 200-400° C. is used, as the liquid activating additive, in the amount of 3.0% by weight, counting on the tar oil.
  • the desired products yield in the conditions of Example 34 is 57.7% by weight, counting on the tar oil.
  • Examples 35, 36, 37 illustrate this invention in respect of tar oil thermal conversion, in which the shale oil fraction with the boiling point 200-400° C. and with the hydrogen content of 8.0, 10.0 and 12% by weight is used as the liquid activating additive.
  • the hydrogen content of the tar oil in Example 35 is 8.0% by weight, in Example 36-10% by weight, in Example 37-12% by weight.
  • the total yield of the fractions with the boiling points up to 180° C., 180-360° C., and 360-500° C. is 77.5% by weight, counting on tar oil, in the conditions of Example 36.
  • Raising the hydrogen content of the shale oil fraction to 12% by weight in the conditions of Example 37 does not result in a significant increase in the desired fractions yield (the desired fractions yield in the conditions of Example 37 is 80.8% by weight) and contributes only to rise in the cost of the final product due to ineffective consumption of shale oil.
  • the quantity of the added shale oil with the boiling point 200-400° C. and the hydrogen content of 10-12% by weight should be 1.0-6.0% by weight.
  • Examples 38, 39, 40 illustrate this invention in respect of tar oil hydrocracking, in which the shale oil fraction with the boiling point 200-400° C. and with the hydrogen content of 8.0, 10.0 and 12% by weight is used as the liquid activating additive.
  • the total yield of the fractions with the boiling points up to 180° C., 180-360° C., and 360-500° C. is 92.2% by weight, counting on tar oil, in the conditions of Example 39, while the hydrogen consumption from the gaseous phase was 1.0% by weight of the raw stock.
  • Raising the hydrogen content of the shale oil fraction to 12% by weight in the conditions of Example 40 does not result in a significant increase in the desired fractions yield (the desired fractions yield in the conditions of Example 40 is 92.3% by weight).
  • the quantity of the added shale oil fraction with the boiling point 200-400° C. and the hydrogen content not less than 10% by weight should be 1.0-6.0% by weight.
  • This invention may be most successfully utilized in oil refining for producing fuel distillates, which are raw stock for the production of motor fuels and jet engine fuels.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US10/486,028 2001-07-12 2001-07-12 Method for producing fuel distillates Abandoned US20040238406A1 (en)

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PCT/RU2001/000283 WO2003010259A1 (fr) 2001-07-12 2001-07-12 Procede de fabrication de carburants distilles

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7984566B2 (en) * 2003-10-27 2011-07-26 Staples Wesley A System and method employing turbofan jet engine for drying bulk materials
US20140109470A1 (en) * 2010-10-22 2014-04-24 Kior, Inc. Production of renewable biofuels
US20140144809A1 (en) * 2012-11-28 2014-05-29 Uop Llc Process for producing diesel

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4035281A (en) * 1976-03-05 1977-07-12 Mobil Oil Corporation Production of fuel oil
US6190537B1 (en) * 1998-05-22 2001-02-20 Zakrytoe Aktsionernoye Obschestove “Panjsher- Holding” Method for producing fuel distillates

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2071133B (en) * 1980-03-04 1983-07-27 Coal Industry Patents Ltd Cracking process
RU2009166C1 (ru) * 1992-04-30 1994-03-15 Международный бизнес-центр "Альфа" Способ получения топливных дистиллятов
RU2132354C1 (ru) * 1998-09-25 1999-06-27 Андриенко Владимир Георгиевич Способ получения жидких продуктов из тяжелых нефтяных остатков

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4035281A (en) * 1976-03-05 1977-07-12 Mobil Oil Corporation Production of fuel oil
US6190537B1 (en) * 1998-05-22 2001-02-20 Zakrytoe Aktsionernoye Obschestove “Panjsher- Holding” Method for producing fuel distillates

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7984566B2 (en) * 2003-10-27 2011-07-26 Staples Wesley A System and method employing turbofan jet engine for drying bulk materials
US20140109470A1 (en) * 2010-10-22 2014-04-24 Kior, Inc. Production of renewable biofuels
US8968670B2 (en) * 2010-10-22 2015-03-03 Kior, Inc. Production of renewable biofuels
US20140144809A1 (en) * 2012-11-28 2014-05-29 Uop Llc Process for producing diesel
US8936714B2 (en) * 2012-11-28 2015-01-20 Uop Llc Process for producing diesel
US20150119614A1 (en) * 2012-11-28 2015-04-30 Uop Llc Process for producing diesel
US9284498B2 (en) * 2012-11-28 2016-03-15 Uop Llc Process for producing diesel

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GB2393731A8 (en) 2004-08-26
CN1238471C (zh) 2006-01-25
CN1545547A (zh) 2004-11-10
GB2393731B (en) 2005-02-16
WO2003010259A1 (fr) 2003-02-06
GB2393731A (en) 2004-04-07
GB0402417D0 (en) 2004-03-10

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