+

WO2003010259A1 - Procede de fabrication de carburants distilles - Google Patents

Procede de fabrication de carburants distilles Download PDF

Info

Publication number
WO2003010259A1
WO2003010259A1 PCT/RU2001/000283 RU0100283W WO03010259A1 WO 2003010259 A1 WO2003010259 A1 WO 2003010259A1 RU 0100283 W RU0100283 W RU 0100283W WO 03010259 A1 WO03010259 A1 WO 03010259A1
Authority
WO
WIPO (PCT)
Prior art keywords
oil
shale
raw materials
κiπ
mass
Prior art date
Application number
PCT/RU2001/000283
Other languages
English (en)
Russian (ru)
Inventor
Juri Alekseevich Kanataev
Mikhail Konstantinovich Yulin
Evgeny Aleksandrovich Ruzhnikov
Original Assignee
Zakrytoe Aktsionernoe Obschestvo Nauchno-Proizvodstvennaya Kompaniya 'panjsher-Holding'
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Zakrytoe Aktsionernoe Obschestvo Nauchno-Proizvodstvennaya Kompaniya 'panjsher-Holding' filed Critical Zakrytoe Aktsionernoe Obschestvo Nauchno-Proizvodstvennaya Kompaniya 'panjsher-Holding'
Priority to GB0402417A priority Critical patent/GB2393731B/en
Priority to PCT/RU2001/000283 priority patent/WO2003010259A1/fr
Priority to CNB018236286A priority patent/CN1238471C/zh
Priority to US10/486,028 priority patent/US20040238406A1/en
Publication of WO2003010259A1 publication Critical patent/WO2003010259A1/fr

Links

Classifications

    • 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

  • the yield of fuel distillates is 55-60m. % on raw materials ⁇ and thermoinvestment and up to 90m. % ⁇ and hydropacking.
  • the hydraulic process distillation and hydraulic distillation process it can be converted to light motor fuel, including automobile gasoline and diesel.
  • Methaline is obtained by hydration of technical products that contain condensed aromatic hydrocarbons, mainly, phthalin and its products.
  • the process of obtaining tetralin and its alkaline derivatives is very advantageous.
  • a positive product is also obtained and the final product.
  • the well-known method in the form of liquid activating additive, is the use of hydrated fraction with ⁇ . ⁇ i ⁇ . 300 - 400 ° ⁇ in the amount of 1 - 5 wt. %
  • the yield of fuel distillates is 55-60 wt. % ⁇ and thermal expansion and up to 90 wt. % ⁇ and hydropacking.
  • a well-known solution has a drawback, which is used in the quality of the added component of the hydrated fraction with ⁇ . ⁇ i ⁇ . 300-400 ° C also increases the cost of the end products in view of the fact that for its production an additional stage is necessary for highlighting the distillation and further cooling for the operation.
  • ⁇ i ⁇ . 300-400 ° C WITH HIGHER WATER PRODUCTS. Sufficiently high cost of hydrated fractions with ⁇ . ⁇ i ⁇ . 300-400 ° C supports the process of use in an inactive processing industry of a known method.
  • the objective of the present invention is to increase the efficiency of the process in order to process heavy inactive products, including the reduction of the output of the invention.
  • a non-technical result of the invention is the exclusion of the use of a hydrated fraction with ⁇ . ⁇ i ⁇ . 300 - 400 ° C when stored, the product is safe.
  • I use hot oil shales containing g / ⁇ : molybdenum 3-15, nickel 20-35, caliber 3-10, ⁇ m 30-40, copper 15-40 and lead 5-20.
  • the homogenization is carried out in a mixing device with a temperature of 80 - 10 ° ⁇ .
  • hot oil shale and mechanical activation are additionally crushed for sizes of 30-100 microns.
  • the chemical exposure is known to the type ⁇ -14 type equipment, as well as to the known disperse mixture (homogenizing mixture), the mixture is dispersed.
  • An optional embodiment of the invention is also available, while the mixture is also dual-homogenized.
  • the resulting mixture promotes mixing and intensive homogenization in order to equally distribute the added actives to the entire raw material volume.
  • P ⁇ nya ⁇ ie " ⁇ e ⁇ m ⁇ nve ⁇ siya" or gid ⁇ e ⁇ ing, is ⁇ lzuem ⁇ e in resort ⁇ m iz ⁇ b ⁇ e ⁇ enii, imee ⁇ ⁇ aditsi ⁇ nn ⁇ e value and v ⁇ lyuchae ⁇ ⁇ ivedenie in ⁇ n ⁇ a ⁇ ⁇ e ⁇ i ⁇ uem ⁇ g ⁇ sy ⁇ ya with v ⁇ d ⁇ d ⁇ m - 500-2000 ⁇ bem ⁇ v v ⁇ d ⁇ da or v ⁇ d ⁇ d ⁇ s ⁇ de ⁇ zhascheg ⁇ gas ⁇ i n ⁇ malny ⁇ usl ⁇ viya ⁇ ( ⁇ 0 ° C, ⁇ -0,1013 ⁇ Pa) for one volume of liquid raw materials at a pressure of 4.0-15.0 PSa, a volumetric speed of 1-3 hours "1 (an adjustable contact time of 20-90 min) and a temperature of 390-440 ° ⁇ .
  • ⁇ imalnymi usl ⁇ viyami ( ⁇ em ⁇ e ⁇ a ⁇ u ⁇ a, pressure, ⁇ bemnaya s ⁇ s ⁇ ) yavlyayu ⁇ sya Te, ⁇ i ⁇ y ⁇ ⁇ b ⁇ azue ⁇ sya ma ⁇ simaln ⁇ e ⁇ liches ⁇ v ⁇ tselev ⁇ g ⁇ ⁇ du ⁇ a not nablyudae ⁇ sya nezhela ⁇ eln ⁇ g ⁇ susches ⁇ venn ⁇ g ⁇ ⁇ s ⁇ l ⁇ zheniya, ⁇ s ⁇ benn ⁇ in ⁇ ubcha ⁇ y ⁇ echi and ⁇ ea ⁇ e.
  • Water-based products are also available in liquid form.
  • the direct catalytic effect on the reduction of compounds of raw materials and the products of its decay indicates a significant increase in the mineral content, which increases
  • oil shale which contains (wt.%): 45-60 mineral part and 40-55 mineral part.
  • shales containing g / ⁇ are used: molybdenum , 3-15, nickel 20-53, temperature 3-10, ⁇ m 30-40, copper 15-40 and lead 5-20.
  • the mineral part of the oil shale contains (wt.%):
  • any raw materials of a heavy type can be used - vacuum gas oil, heavy fuel oil, heavy oil, heavy oil, heavy oil, heavy oil, heavy oil, and heavy oil.
  • shale oil which consists of a fraction with a boiling range of 200–400 ° ⁇ and which contains at least
  • This oil is well-known - thermal oil shale with a solid transfer agent.
  • the well-known fine-grained oil shale is dried, it is heated to a furnace with a separate heating medium with a vapor-gas mixture.
  • the last, after its dry calculation, is spoiled with a mixture of solvents with the output of a heavy oil mist. Further, the vapor-gas mixture is cooled in the condensate with the output of the direct condensate of the heavy oil fraction in the product kachestvo.
  • the condensed part of the vapor-gas mixture is separated in the refined section with the release of the light oil fraction, which is discharged from the by-product.
  • the method ensures the production of valuable fractions from the oil shale with a low content of mechanical impurities and the optimization of the economic situation (“Waste and industrial waste”.
  • Distinctive feature obtained from the t.kip. 200-400 ° C is a shale oil, which, in its composition, contains a high amount of water (not less than 10 wt.%) Due to the fact that it is significantly These compounds are supplied with a 2-4-group of large hydrocarbon hydrocarbons (di-, tetra- and hexane-derivatives of phenylanthene, benzene, benzene, and benzene). Indicated function with ⁇ . ⁇ i ⁇ . 200-400 ° C of oil is a sufficiently efficient product of hydrogen and heat treatment and hydraulic processing of non-essential raw materials (non-productive).
  • the optimal water content in shale oil is supplied with oil.
  • 200-400 ° C should be no less than Yumas. % With a decrease in the amount of water in shale oil below Yumas. % noticeably decreases the yield of fuel distillations in the process of heat treatment and hydraulics.
  • the increase in the amount of water in shale oil is higher than 12 wt. % Practically do not affect the output of fuel distillates, but they do not end up.
  • the fraction of shale oil with a range of 200-400 ° ⁇ and containing at least 10.0 wt.% Of the water is included in the amount of 1.0 - 6.0 wt.% Of non-raw materials.
  • a good and good result is that it is possible to obtain and use oil or hydraulic products in the Czech Republic or in Finland However, in this and other cases, the output of light products will be significantly lower due to the result of that, in 9 The reactive system will not have the necessary quantity of hydraulic compounds that are equipped with non-aquatic properties.
  • the target fuel distillates for the separation of food products and hydraulics in conjunction with the invention are the usual widespread fuel activities:
  • the resulting fuel distillates may be processed into components of commercial fuels or into conventional fuels by conventional methods of processing.
  • a gasoline fraction can be doubled up for special catalytic converters with a petrol processing unit 82-93.
  • Diesel fraction after hydraulics can be used as a diesel fuel with a chain number of 48-50.
  • Conventional fuel products are the basic products of the process in accordance with the invention. They can be easily converted to consumer fuels, i.e.
  • the invention results in a result that does not result from obvious evidence from the prior art.
  • the installation diagram for the implementation of the required method is provided in the figure.
  • An open (combustible) oil shale with a size of 25–250 mm or a shale fines with a size of 0–25 mm from an iron wagon is empty for storage.
  • Warehouse for oil shale is available in the bunker for the purchase of oil shale 1.
  • hot oil shale for the storage of the oil in the bunker for oil oil shale 1
  • hot oil shale is fed to a crusher with a manual filter (2), where it is crushed to a size 10 particles 8mm.
  • the shale shredded up to 8 mm in size is fed into the “Nez-14” disembratement (3), where further shale is shredded up to a 1 mm particle size.
  • the “K ⁇ -14” demis- Disintegrator “Ez ⁇ -14” is equipped with a cyclone, air filter, manual filter, and a sockets.
  • the shredded slate is released to the vibrator with a working distance of 140 mb.
  • the entire shale grinding unit is equipped with protective equipment and protective equipment. It is intended for separating shale particles with sizes above 140 mk.
  • Raw materials are prepared by the following process. ⁇ Brass ⁇ A heated mixer, where a temperature of 80-100 C is maintained, or another stirring device (9), is used (if it is not emitted), First, the shale oil is supplied to the mixing apparatus (9), then the oil from the reservoir (8) and the slate are supplied through the dispenser (6). Processors for the supply of components of the raw material mixture carry out the operations of the stirring device in order to avoid sitting on the bottom of the oil shale.
  • the mixing device does not provide an efficient mixing of the 3 large-sized mixture, then it is more suitable for the large-scale mixing (hermetic). At this temperature, in the unit for the production of raw materials, it is necessary to maintain raw materials in the range of 80 -10 ° C to ensure the pumping is good.
  • the raw material heating furnace (14) has two sections ⁇ and B. In the section, they are maintained in the range of 380-400 ° ⁇ , and at the outlet from the furnace, 460-490 ° ⁇ is dependent on it. Partially converted raw materials are delivered to the lower part of the furnace from the furnace.
  • P ⁇ dacha v ⁇ d ⁇ d ⁇ s ⁇ de ⁇ lsascheg ⁇ gas (s ⁇ de ⁇ zhanie 80% water) is 1000–1500 nm 3 per m 3 of raw material.
  • on top of the hot unit go to the main fractions, growing up to 360-380 ° C, from below the hot unit ⁇ a ⁇ a ⁇ tsii, vy ⁇ i ⁇ ayuschie above 360-380 ° C in admixture with ⁇ vo ⁇ dymi ⁇ du ⁇ ami.
  • ⁇ e ⁇ ny ⁇ g ⁇ yacheg ⁇ se ⁇ a ⁇ a ⁇ a vmes ⁇ e with v ⁇ d ⁇ d ⁇ s ⁇ de ⁇ z haschim gaz ⁇ m ( ⁇ SG) ⁇ ydya sis ⁇ emu ⁇ lazhdeniya (17) in na ⁇ a ⁇ livae ⁇ sya se ⁇ a ⁇ a ⁇ e vys ⁇ g ⁇ pressure (18), wherein ⁇ is ⁇ di ⁇ ⁇ delenie ⁇ SG ⁇ gid ⁇ geniza ⁇ a. ⁇ SG is ideal for mixing with fresh water, and then on a circulating chamber (25).
  • the bottom product of the hot unit (such as sludge) is cooled by a coolant valve 20 and is cooled to an intermediate temperature (21)
  • Liquid (such as a liquid) is mixed with hydrogenation (a hot heater) and the mixture is used after heating in a furnace (24), which leads to a decrease in gas (water) radiation (26).
  • ⁇ i ⁇ . up to 180 C diesel fraction with ⁇ . ⁇ i ⁇ . 180-360 ° C, gas oil with ⁇ . ⁇ i ⁇ . 360-500 ° ⁇ and a residue that grows above 500 ° ⁇ (figure).
  • ⁇ ⁇ aches ⁇ ve ⁇ s ⁇ a ⁇ chn ⁇ g ⁇ ne ⁇ yan ⁇ g ⁇ sy ⁇ ya in ⁇ ivedenny ⁇ ⁇ ime ⁇ a ⁇ is ⁇ lzuyu ⁇ : gud ⁇ n mixture za ⁇ adn ⁇ sibi ⁇ s ⁇ i ⁇ ne ⁇ ey, ⁇ y imee ⁇ ⁇ a ⁇ a ⁇ e ⁇ is ⁇ i ⁇ u following: ⁇ l ⁇ n ⁇ s ⁇ - 984 ⁇ g / m 3, elemen ⁇ ny s ⁇ s ⁇ av, wt%: C, 86.8;.
  • ⁇ ⁇ aches ⁇ ve sa ⁇ eli ⁇ a is ⁇ lzuyu ⁇ : ⁇ yad ⁇ v ⁇ y ⁇ ibal ⁇ iys ⁇ y shale having the following ⁇ a ⁇ a ⁇ e ⁇ is ⁇ i ⁇ u wt%: ⁇ ⁇ - 46,70; C ⁇ 01 2 min -8.32; C ⁇ a ⁇ - 81.3; ⁇ ( ⁇ -9.25; ⁇ s - 0.28; 8 ", - 0.90; ⁇ ⁇ a - 3.0.
  • ⁇ ⁇ aches ⁇ ve zhid ⁇ y a ⁇ ivi ⁇ uyuschey d ⁇ bav ⁇ i is ⁇ lzuyu ⁇ slantsev ⁇ e masl ⁇ , s ⁇ s ⁇ yaschee of ⁇ a ⁇ tsii with ⁇ edelami vy ⁇ i ⁇ aniya 200-400 ° C, having the following ⁇ a ⁇ a ⁇ e ⁇ is ⁇ i ⁇ u: 995 ⁇ l ⁇ n ⁇ s ⁇ ⁇ g / m ⁇ aza ⁇ el ⁇ el ⁇ mleniya 1.5696, m ⁇ le ⁇ ulya ⁇ naya weight 290 s ⁇ de ⁇ zhanie as ⁇ al ⁇ en ⁇ v 3,8mas. %, elemental composition, wt. %: C-82.95, ⁇ -10.0; ⁇ - 0.56; 8-0.6; Stagnation temperature - minus 20 ° ⁇ , viscosity - 14.9 cSt and 50 ° ⁇ .
  • the process of temperature control or hydraulics of the appliance is either on or on installation with a volume of 6 liters or on a manual installation of 10.
  • the quantitatively edible and aromatic additives make up 0.5–6.0%, the quantitative gain is 0.5–5.0% of the total weight of the pulp.
  • Liquid products of the process are distilled at a fraction of ⁇ . ⁇ i ⁇ . up to 180 ° ⁇ , 180-360 ° ⁇ , 360-500 ° ⁇ and remains above 500 ° ⁇ .
  • Shale-free mixture for processes of thermal treatment or hydroprocessing is prepared by means of the subsequent mixing of non-volatile raw materials, especially in case of heavy oil. ⁇ i ⁇ . 200-400 ° C and ryadovo 13 oil shale. Mixing is carried out in a heated stirrer at a temperature of at least 85 ° ⁇ for 2.5 hours, and then the resulting mixture is homogenized in a dispersing device or on a device. By doing this, a mixture is not stratified over a long period of time.
  • EXAMPLE 1 The initial mixture is prepared by mixing a pot of 10 ⁇ , hot shale 0.2 ⁇ (mineral composition of the mineral part is 40 wt.%) And a fraction of the shale oil with ⁇ . ⁇ i ⁇ . 200-400 C with a water content of 10 wt. %, 0.3 ⁇ . Mixing is carried out in a heated mixer at a temperature of at least 85 ° C for 2.5 hours. Then the mixture promotes activation and homogenization. ⁇ e ⁇ m ⁇ nve ⁇ siyu vedu ⁇ ⁇ d pressure ⁇ Pa 3-5, ⁇ em ⁇ e ⁇ a ⁇ u ⁇ e 425-450 ° C ⁇ bemn ⁇ y s ⁇ s ⁇ i 1-2 hour "1.
  • EXAMPLE 2 The raw materials and conditions of the process are similar to those of Example 1, with the exception of the fact that the slate contained 45 wt. % of the mineral part.
  • the indicators of the process of heat transfer are given in the table ⁇ ° 1.
  • Example 3 The raw materials and conditions of the process of heat transfer are similar to the method
  • EXAMPLE 4 The raw materials and conditions of the thermoinvestment are similar to Example 1, with the exception of the fact that the slate contained 60 wt. % of the mineral part. The performance indicators of the process are listed in Table 1.
  • EXAMPLE 5 The raw materials and conditions of the process are similar to those of Example 1, with the exception of the fact that the slate contained 65 wt. % of the mineral part.
  • the performance indicators of the process are listed in Table 1.
  • Example 6 The starting raw material is prepared by mixing a 10 ton oil tank, 0.2 ton hot oil shale, and oil shale oil fraction with ⁇ . boiling 200 - 400 ° C and a water content of 10 wt. % 0.3 ⁇ . Mixing is carried out in a heated mixer at a temperature of at least 85 ° C for 2.5 hours. Then the mixture promotes activation and homogenization. At this time, the shale content is 0.5 mass. % 14 ⁇
  • the products obtained have the following characteristics: gasoline fraction with ⁇ . ⁇ i ⁇ . up to 180 ° C: index of application 1, 4216, elemental composition, wt.%: C 84, 53; ⁇ 13.75; 8 0.46; ⁇ 0.06; diesel ⁇ with ⁇ . ⁇ i ⁇ . 180-360 ° C: index of application 1, 4786; elemental composition, wt.%: C 85.89, ⁇ 12.26, 8 0.69, ⁇ 0.06 gas oil fraction with ⁇ . ⁇ i ⁇ . 360-500 ° C: index of application 1, 5211, elemental composition, wt.%: C 86.60, ⁇ 11.24, 8 1.29, ⁇ 0.21; left with t.kip.
  • EXAMPLE 8 The raw materials and conditions of the thermoinvestment are similar to Example 6, except for the shale content in the amount of 2.0 mass. % Thermostatic indicators are shown in Table 2.
  • EXAMPLE 9 The raw materials and conditions of the process are similar to those of Example 6, except for the addition of oil shale in the amount of 3.0 mass. % Indicators of the thermal process are given in Table 2.
  • EXAMPLE 10 The raw materials and conditions of the process are similar to those of Example 6, except for the addition of oil shale in the amount of 5.0 wt. % Thermostatic indicators are shown in Table 2.
  • EXAMPLE 11 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the amount of oil shale with ⁇ . ⁇ i ⁇ . 200-400 ° C - 0.5 wt.%.
  • the indicators of the process are given in Table 2.
  • Example 12 The raw materials and conditions of the process are similar to the example.
  • Example 14 The raw materials and conditions of the process are similar to those for the process.
  • EXAMPLE 15 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the amount of shale oil fractions with ⁇ . ⁇ i ⁇ . 200-400 ° C shale oil - 6.0 wt. % Indicators of the thermal process are given in Table 2.
  • EXAMPLE 16 The raw materials and conditions of the thermal process are similar to those of Example 6, with the exception of the quantity of hot oil shale - 2.0 wt. % Indicators of the thermal process are given in Table 2.
  • Example 17 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the quantity of fractions with ⁇ . ⁇ i ⁇ . 200-400 With shale oil - 3.0m. % Indicators of the thermal process are given in Table 2.
  • EXAMPLE 18 The starting raw material is prepared by mixing a 7-, 5, t, risel with ⁇ . ⁇ i ⁇ . above 500 ° C - 2.5 ⁇ , hot oil shale - 0.2 ⁇ and oil shale - 0.3 ⁇ .
  • Mixing is carried out in a heated mixer at a temperature of at least 85 ° ⁇ , for
  • the mixture is activated or homogenized.
  • the content of the mineral part in the shale was - 40mass. %
  • EXAMPLE 19 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of the fact that the slate was 45 months old. % of the mineral part. The performance of the hydraulic process is shown in Table 3. EXAMPLE 20. The raw materials and conditions of the hydraulic process are similar.
  • Example 21 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of the fact that the slate contained a mass of 60%. % of the mineral part. Hydraulic process indicators are shown in Table 3.
  • EXAMPLE 22 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of the fact that the slate contained 65 wt. % of the mineral part. Hydraulic process indicators are shown in Table 3.
  • EXAMPLE 23 The raw materials and conditions of the hydroprocessing process are similar to Example 18, except for the shale content in the amount of 0.5 mass. % Hydration indicators are shown in Table 4.
  • EXAMPLE 24 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of shale formation in the amount of 1.0 mass. % The performance of the hydraulic process is shown in table 4.
  • Example 25 The raw materials and conditions of the hydraulic process are similar.
  • EXAMPLE 26 The raw materials and conditions of the hydroprocessing process are similar to Example 18, except for the shale content in the amount of 3.0 mass. % Hydration indicators are shown in Table 4.
  • EXAMPLE 27 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of shale formation in the amount of 5.0 mass. % Hydration indicators are shown in Table 4. 17 EXAMPLE 28. The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of the contraction of the oil shale of the fraction with ⁇ .kip. 200-400 ° C shale oil 0.5 wt. % The performance of the hydraulic process is shown in table 4. EXAMPLE 29. The raw materials and conditions of the hydraulic process are similar.
  • EXAMPLE 30 The raw materials and conditions of the hydration process are similar to Example 18, with the exception of the fraction with ⁇ . ⁇ i ⁇ . 200-400 ° C shale oil 2.0mass. % Hydration indicators are shown in Table 4.
  • EXAMPLE 31 The raw materials and conditions of the hydration process are similar to Example 18, with the exception of the fraction with ⁇ . ⁇ i ⁇ . 200-400 ° C shale oil 3.0mass. % Hydration indicators are shown in Table 4.
  • EXAMPLE 32 The raw materials and conditions of the hydraulic process are similar to Example 18, with the exception of the fraction with ⁇ . ⁇ i ⁇ . 200-400 ° ⁇ shale oil 6.0mass. % Hydration indicators are shown in Table 4.
  • EXAMPLE 33 The raw materials and conditions of the hydroprocessing process are similar to Example 18, with the exception of a bulk oil shale of 2.0 months. % The performance of the hydraulic process is shown in Table 4.
  • EXAMPLE 34 The raw materials and conditions of the hydraulic process are similar.
  • EXAMPLE 35 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the water content of oil shale from ⁇ . ⁇ i ⁇ . 200 - 400 C 8.0 mt. % Indicators of the process of heat transfer are given in Table 5.
  • EXAMPLE 36 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the presence of water in the oil shale with ⁇ . ⁇ i ⁇ . 200-400 ° C Yumas. % Indicators of the process of heat transfer are given in Table 5.
  • EXAMPLE 37 The raw materials and conditions of the process are similar to those of Example 6, with the exception of the water content of oil shale from ⁇ . ⁇ i ⁇ . 200 - 400 C 12mas. % Indicators of the process of heat transfer are given in Table 5.
  • Example 38 The raw materials and conditions of hydroprocessing of the process are similar to those of Example 18, with the exception of the combination of water and oil shale oil with ⁇ . ⁇ i ⁇ . 200-400 ° C 8.0m. % Hydration indicators are shown in Table 5.
  • EXAMPLE 39 The raw materials and conditions of the hydroprocessing process are similar to those of Example 18, with the exception of the presence of water containing oil shale from ⁇ . ⁇ i ⁇ . 200-400 ° C 10.0m. % Hydration indicators are shown in Table 5.
  • EXAMPLE 40 The raw materials and conditions of the hydroprocessing process are similar to those of Example 18, with the exception of the water content of shale oil fractions with ⁇ . ⁇ i ⁇ . 200-400 ° C 12.0m. %
  • the indicators of the hydroprocessing process are given in table 5.
  • Example 41 According to the method, the closest analogue to the patent
  • Example 42 In accordance with method - the closest analogue to the patent ⁇ 2128207, mix (wt.%): Good - 100.0; Baltic shale -2.0, in t.h. the mineral part is 1.3; shale tar-3.0; Waste water -2.5. Hydrocracking is carried out under the following conditions: temperature - 425 ° ⁇ , pressure - JuPa, volumetric speed 1.0 hour "1. Receive the following gas output - 0.5%; with a temperature of up to 180 ° ⁇ - 19.0; a fraction with a temperature of 180-360 ° ⁇ -63.0; a function with a temperature of 360-520 ° ⁇ - 11.0; it remains with ⁇ . kipip. above 520 C -1.5; koks on the mineral part of the sapropelite is 6.5.
  • Examples 11–15 illustrate the present invention, in other words, as a liquid liquid additive, an active fraction is used with ⁇ . ⁇ i ⁇ . 200-400 With oil shale.
  • Composition of the indicated additive in the range of 11–15 is 0.5; 1.0; 2.0; 3.0 and 6.0 wt. % based on good.
  • the total yield of fractions with ⁇ . ⁇ i ⁇ . up to 180 ° ⁇ , 180-360 ° ⁇ and 360-500 ° ⁇ have a maximum in the amount of 68.5-70.7 (under conditions of 13 and 14).
  • the yield of the target products is slightly higher (74.5% by weight under conditions of Example 15).
  • introduce a fraction of shale oil with ⁇ . ⁇ i ⁇ . 200-400 ° C and containing at least 10.0 wt. % of residual non-raw materials is in the range of 1.0 - b, 0mass. % on raw materials.
  • EXAMPLE 16 illustrates the use of the present invention in the process of thermoanalysis of good in case of only oil shale in the vicinity of 2.0. % on good.
  • the temperature range (up to 180 ° C, 180-360 ° C, 360-500 ° C) under conditions of 16 is 57.8 mass. % based on good.
  • EXAMPLE 17 demon- strates the indicators of the process of the sale of the good when used in the form of bulk additives - active - fractions with ⁇ . ⁇ i ⁇ . 200 - 400 ° C shale oil with a water content of 10.0 wt. %
  • the yield of targeted products under conditions of Example 17 is 47.9 mass. % based on good.
  • Table 3 shows the following. With an increase in the mineral content in the shale from 40 to 50 wt. % of production and hydroprocessing of the house, the output of the target products increases from 84.5m. % (under condition 18) to 93.7 (under conditions 20), and the increase in the share of the mineral part in the shale is up to mass.
  • s ⁇ avnenie ⁇ gid ⁇ e ⁇ ingu ⁇ ⁇ ime ⁇ am 18, 20 and 21 ⁇ azyvayu ⁇ d ⁇ s ⁇ izhenie ⁇ e ⁇ niches ⁇ g ⁇ ⁇ ezul ⁇ a ⁇ a nas ⁇ yascheg ⁇ iz ⁇ b ⁇ e ⁇ eniya on account ⁇ imeneniya g ⁇ yucheg ⁇ shale s ⁇ de ⁇ lsaniem mine ⁇ aln ⁇ y chas ⁇ i in g ⁇ yuchem shale in ⁇ liches ⁇ ve 45-60 wt.
  • composition 40 and 65mas. % of the mineral part in oil shale in the process of hydroprocessing of the reservoir does not ensure the achievement of the technical result.
  • Examples 23-27 illustrate the present invention, as a result of a third-party additive-activation, and when the appliance is hydraulically used, it is fire-proof.
  • the content of the specified slate in paragraphs 23-27 is 0.5; 1.0; 2.0; 3.0; 5.0.
  • the total yield of the fractions with ⁇ . ⁇ i ⁇ . up to 180 ° C, 180-360 ° C and 360-500 ° C have a maximum of 93.7 wt. % of the good for grades 25 and 26.
  • the oil shale is kept in the amount of 5.0 months. %, the yield of fuel distillation in nils than at 2.0 and 3.0 mass. % on good.
  • Examples 28-32 demon- strate the present invention, in fact, as a liquid supplement, the oil is activated and the oil is hydrated using a slurry.
  • Composition of the indicated supplement in examples 28-32 is equal to 0.5; 1.0; 2.0; 3.0 and 6.0 mass. % in terms of raw materials.
  • the total yield of fractions with ⁇ . ⁇ i ⁇ . up to 180 ° ⁇ , 180-360 ° ⁇ and 360-500 ° ⁇ have a maximum in the amount of 92.3-93, 7mass. % (under conditions of ⁇ primes 30 and 31).
  • the yield of the target products is slightly higher (95.7% by weight, given the condition of 32), but the increase of 3 percent results in the separation of the fraction from ⁇ . ⁇ i ⁇ . 200-400 ° C of shale oil is produced due to insignificant increase in the yield of the target products due to the significant loss of oil due to oil shale.
  • introduce a fraction of shale oil with ⁇ . ⁇ i ⁇ . 200-400 ° C with a water content of at least 10.0 wt. % of the rest of the non-ferrous raw materials follows in the amount of 1.0-6.0 wt. % on raw materials.
  • EXAMPLE 33 illustrates the use of the present invention in the process of hydrotherapy only for oil shale in the amount of 2.0 months. % on good.
  • the output of the reaction (up to 180 ° ⁇ , 180-360 ° ⁇ , 360-500 ° ⁇ ) under conditions of 33 is 63.6 mass. % based on good.
  • EXAMPLE 34 demon- strates the indicators of the hydraulic process of the hood when used in the form of a liquid additive-fraction - with ⁇ . ⁇ i ⁇ . 200 - 400 ° C shale oil in the amount of 3.0 wt. % on good.
  • the yield of targeted products under conditions of 34 is 57.7m. % based on good.
  • EXAMPLES 35, 36, 37 illustrate the present invention with a thermocouple, in addition to a liquid additive, it is used in the process.
  • ⁇ i ⁇ . 200 - 400 ° ⁇ of shale oil which is contained in its composition 8.0; 10.0 and 12 wt. % WATER.
  • the content of water in shale oil is in oil. 35 of them is 8.0 months. %, in ⁇ prime 36-1 ⁇ mass. %, in ⁇ imer 37-12 wt. %% Of 3 fractions (up to 180 ° ⁇ , 180-360 ° ⁇ , 360-500 ° ⁇ ) under conditions of 36 is 77.5 wt. % ⁇ good.
  • Reduction of water content of oil shale oil up to 8.0 mass. % in the case of an example of 35 leads to a decrease in the yield of target fractions up to 61.3 mass. % ⁇ good.
  • EXAMPLES 38, 39, 40 illustrate the present invention by hydroprocessing the good, in addition to the quality of the liquid additive, use the fraction with ⁇ . ⁇ i ⁇ . 200 - 400 ° ⁇ of shale oil, which is contained in its composition 8.0; 10.0; 12.0 wt. % WATER.
  • the yield of 3 fractions (up to 180 ° ⁇ , 180-360 ° ⁇ , 360-500 ° ⁇ ) under conditions of Example 39 is 92.2 wt. % ⁇ good. With this, the yield of gas from the gas phase was 1.0 wt. % ⁇ raw materials.
  • the present invention ensures that there is no loss of technical results, which does not result in an obvious result. 29 Intended use
  • the most successful invention can be used in the process of processing fuel distillates, which are a raw material for motor vehicles.

Landscapes

  • 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)

Abstract

L'invention concerne un procédé de fabrication de carburants distillés et peut s'utiliser dans l'industrie de transformation du pétrole pour fabriquer des carburants pour moteur et des carburants pour moteurs à réaction. Selon l'invention, toutes les matières premières pétrolières résiduelles (mazout, goudron, pétroles lourds) sont mélangées à des schistes combustibles comprenant 45 - 60 % en poids de parties minérales et 40 - 55 % en poids de parties organiques, avec une fraction ayant une température d'ébullition 200 - 400 °C contenant pas moins de 10,0 % en poids d'hydrogène, dont la teneur s'élève à 1,0 - 6,0 % du poids. Le mélange est ensuite soumis à l'homogénéisation dans un mélangeur à une température égale ou supérieure à 80°; on procédé ensuite à la thermoconversion ou à l'hydrocraquage. A partir des produits de thermoconversion ou d'hydrocraquage on obtient des carburants distillés (essence, carburant diesel, gasoil sous vide).
PCT/RU2001/000283 2001-07-12 2001-07-12 Procede de fabrication de carburants distilles WO2003010259A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
GB0402417A GB2393731B (en) 2001-07-12 2001-07-12 Method for producing fuel distillates
PCT/RU2001/000283 WO2003010259A1 (fr) 2001-07-12 2001-07-12 Procede de fabrication de carburants distilles
CNB018236286A CN1238471C (zh) 2001-07-12 2001-07-12 生产燃料馏出物的方法
US10/486,028 US20040238406A1 (en) 2001-07-12 2001-07-12 Method for producing fuel distillates

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/RU2001/000283 WO2003010259A1 (fr) 2001-07-12 2001-07-12 Procede de fabrication de carburants distilles

Publications (1)

Publication Number Publication Date
WO2003010259A1 true WO2003010259A1 (fr) 2003-02-06

Family

ID=20129635

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/RU2001/000283 WO2003010259A1 (fr) 2001-07-12 2001-07-12 Procede de fabrication de carburants distilles

Country Status (4)

Country Link
US (1) US20040238406A1 (fr)
CN (1) CN1238471C (fr)
GB (1) GB2393731B (fr)
WO (1) WO2003010259A1 (fr)

Families Citing this family (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
US8647398B2 (en) * 2010-10-22 2014-02-11 Kior, Inc. Production of renewable biofuels
US8936714B2 (en) * 2012-11-28 2015-01-20 Uop Llc Process for producing diesel

Citations (5)

* 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
GB2071133A (en) * 1980-03-04 1981-09-16 Coal Industry Patents Ltd Cracking process
RU2009166C1 (ru) * 1992-04-30 1994-03-15 Международный бизнес-центр "Альфа" Способ получения топливных дистиллятов
RU2128207C1 (ru) * 1998-05-22 1999-03-27 Региональная общественная организация инвалидов - Патриотическое объединение инвалидов войны в Афганистане и воинов-интернационалистов "Панджшер" 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 (5)

* 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
GB2071133A (en) * 1980-03-04 1981-09-16 Coal Industry Patents Ltd Cracking process
RU2009166C1 (ru) * 1992-04-30 1994-03-15 Международный бизнес-центр "Альфа" Способ получения топливных дистиллятов
RU2128207C1 (ru) * 1998-05-22 1999-03-27 Региональная общественная организация инвалидов - Патриотическое объединение инвалидов войны в Афганистане и воинов-интернационалистов "Панджшер" Способ получения топливных дистиллятов
RU2132354C1 (ru) * 1998-09-25 1999-06-27 Андриенко Владимир Георгиевич Способ получения жидких продуктов из тяжелых нефтяных остатков

Also Published As

Publication number Publication date
GB2393731A8 (en) 2004-08-26
CN1238471C (zh) 2006-01-25
CN1545547A (zh) 2004-11-10
GB2393731B (en) 2005-02-16
US20040238406A1 (en) 2004-12-02
GB2393731A (en) 2004-04-07
GB0402417D0 (en) 2004-03-10

Similar Documents

Publication Publication Date Title
RU2547826C2 (ru) Способ гидропереработки тяжелой и сверхтяжелой нефти и нефтяных остатков
US6660157B2 (en) Heavy oil hydrocracking process with multimetallic liquid catalyst in slurry bed
AU2005266712B2 (en) A process for direct liquefaction of coal
RU2385346C2 (ru) Способ обработки с использованием водорода и система для обогащения тяжелой нефти с использованием коллоидного или молекулярного катализатора
RU2541324C2 (ru) Добавка для процесса гидропереработки и способ ее получения и применения
US5064523A (en) Process for the hydrogenative conversion of heavy oils and residual oils, used oils and waste oils, mixed with sewage sludge
CN102471054A (zh) 从炼厂气高剪切生产增值产品
EP4408956A1 (fr) Procédé de valorisation d'huiles hautement oléfiniques issues de la pyrolyse de déchets plastiques
CA1134304A (fr) Decendrage de la houille par agglomeration au petrole
WO1999061560A1 (fr) Procede de production de distillats de carburants
WO2004094562A1 (fr) Procede de recyclage de dechets caoutchouteux
CN108745026B (zh) 一种适应于焦化法处理清罐污泥的均质预处理系统和方法
WO2003010259A1 (fr) Procede de fabrication de carburants distilles
US20140209513A1 (en) System and process for coal liquefaction
CN105038853B (zh) 一种利用fcc油浆和煤共炼制油的方法
CA1322746C (fr) Hydrocraquage de petrole lourd en presence de coke de petrole sous-produit de la cokefaction de petrole lourd
RU2288940C1 (ru) Способ термохимической переработки тяжелых нефтяных остатков
CN108456550B (zh) 一种外循环式反应装置和煤油共炼方法
EP0020656A1 (fr) Procede de liquefaction du charbon utilisant des mineraux etrangers
CA1155411A (fr) Methode d'hydrogenation de la houille
US4764270A (en) Simultaneous upgrading of tar sand bitumen and coal by corefining
EP0020663A1 (fr) Procede de liquefaction du charbon avec un systeme ameliore de recyclage de la boue
US4421632A (en) Process for hydrogenation of coal
US4098583A (en) Method of removing ash components from high-ash coals
CN116328663A (zh) 一种浆态床反应器、劣质油浆态床加氢裂化系统及方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BY CA CH CN CR CU CZ DE DK DM EE ES FI GB GD GE GH GM HR HU ID IN IS JP KE KG KP KR KZ LC LK LR LT LU LV MA MD MG MK MN MW NO NZ PL PT RO RU SD SE SG SI SK TJ TM TR TT TZ UA UG US UZ VN YU

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ UG ZW AM AZ BY KG KZ MD TJ TM AT BE CH CY DE DK ES FI GB GR IE IT LU MC NL PT SE BF CF CG CI CM GA GN GW ML MR NE TD TG

ENP Entry into the national phase

Ref document number: 0402417

Country of ref document: GB

Kind code of ref document: A

Free format text: PCT FILING DATE = 20010712

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 223/DELNP/2004

Country of ref document: IN

WWE Wipo information: entry into national phase

Ref document number: 0402417.0

Country of ref document: GB

WWE Wipo information: entry into national phase

Ref document number: 2004/01109

Country of ref document: ZA

Ref document number: 200401109

Country of ref document: ZA

WWE Wipo information: entry into national phase

Ref document number: 20018236286

Country of ref document: CN

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWE Wipo information: entry into national phase

Ref document number: 10486028

Country of ref document: US

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP

点击 这是indexloc提供的php浏览器服务，不要输入任何密码和下载