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WO1993022399A1 - Procede permettant d'obtenir des distillats de combustibles - Google Patents

Procede permettant d'obtenir des distillats de combustibles Download PDF

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Publication number
WO1993022399A1
WO1993022399A1 PCT/RU1992/000177 RU9200177W WO9322399A1 WO 1993022399 A1 WO1993022399 A1 WO 1993022399A1 RU 9200177 W RU9200177 W RU 9200177W WO 9322399 A1 WO9322399 A1 WO 9322399A1
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WO
WIPO (PCT)
Prior art keywords
temperature
products
raw materials
mixture
mass
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/RU1992/000177
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English (en)
Russian (ru)
Inventor
Alexandr Borisovich Vol-Epshtein
Mark Borisovich Shpilberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mezhdunarodny Biznes-Tsentr 'alfa'
Original Assignee
Mezhdunarodny Biznes-Tsentr 'alfa'
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 Mezhdunarodny Biznes-Tsentr 'alfa' filed Critical Mezhdunarodny Biznes-Tsentr 'alfa'
Publication of WO1993022399A1 publication Critical patent/WO1993022399A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10G1/02—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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils

Definitions

  • the original non-raw material or its distillate part 30 may be processed into light non-processed products by means of catalytic conversion.
  • the indicated method is used, for example, bituminous coal with a particle size of 20-2000 ⁇ .
  • the ratio of liquid products to the mass of coal is 1.5–20: 1, respectively.
  • the selected fraction of liquid in- products for the purpose of obtaining cleaned sulfur and the smallest substances of the distillates is controlled by a hydroprocessor or a separator.
  • the yield of light distillates at the indicated method is 35.2 ⁇ of the total mass of raw materials or $ 38.7 of the mass of residual non-raw materials. ⁇
  • the minimum amount of liquid wastewater (temperature of boiling 345 ° ⁇ ) is provided for the indicated method
  • the process of thermal kreking is preferential to separate diesel fractions with an acceleration of 200–300 ° C. - 35 It is expedient to declare * the process of thermal kreking to be carried out at a temperature of 390-440 ° C with a pressure of ⁇ ⁇ 3-8 PSa for 20-90 minutes (that takes about 1 to 3 ).
  • the inventive methods provide for the reduction of thermal cracking under known conditions, including excretion of raw materials at a temperature of 8-4 ° C.
  • a prerequisite for operating the process is: temperature 390-440 ° C, pressure 3-8 ⁇ Pa, for 20-90 minutes (volumetric rate 0.7-3.0 hours "1 ).
  • thermocoupling use a mixture containing residual non-solid raw materials and other solid fuels - sappelite.
  • Inventory of quick non-ferrous raw materials can be used any kind of raw materials such as food, for example, fuel oil, hood, heavy oil (Malta) and others.
  • - 5 any other combustible fossil fuels, such as schists, sulphurous schists, gas mixtures and others, may be used.
  • the initial mixture also contains liquid gasification product of sapropelite.
  • Liquid gasification products of a gas smelter are a product of its processing in a gas generator and, in the case of using shale, they are called a shale oil.
  • ⁇ ⁇ aches ⁇ ve d ⁇ lni ⁇ eln ⁇ g ⁇ sy ⁇ ev ⁇ g ⁇ ⁇ m ⁇ nen ⁇ a m ⁇ gu ⁇ by ⁇ is ⁇ lz ⁇ va- us ⁇ a ⁇ sm ⁇ la itself, and ⁇ a ⁇ b ⁇ lee uz ⁇ aya ⁇ ⁇ em ⁇ e ⁇ a ⁇ u ⁇ e ⁇ i ⁇ eniya ⁇ a ⁇ tsiya e ⁇ y sm ⁇ ly gazi ⁇ i ⁇ atsii sa ⁇ eli ⁇ a, na ⁇ ime ⁇ , ⁇ a ⁇ tsiya with ⁇ em ⁇ e ⁇ a ⁇ u ⁇ y ⁇ i ⁇ eniya 220-340 ° C.
  • the saprotite is a liquid, the gas product of gasification of the sapropelite (shale gum) - or it is at a temperature of 220–320 g per cent, is A decrease in the content of the sapelite is lower than the declared value of 2 wt. $ Reduces the yield of the target product, an increase of more than 10 wt.
  • a preferred embodiment of the claimed method is a recirculation process in a dedicated process. - 6 - whole fractions with a boiling point of 200-370 ° ⁇ in the amount of 10-20 $ from the rest of the stock of non-heavy raw materials. This saves the need for process technology (reduce the temperature of the original mixture).
  • Targeted fuel distillates obtained from the separation of products from thermal processing are the usual methods that are used in the sale of conventional fuel products:
  • the resulting fuel distillates may be converted to commercial fuel or diesel fuel components.
  • a gasoline fraction may be doubled up with a gasoline component or hydraulics (easy hydraulics) with the following.
  • the diesel fraction may be hydraulically cleaned with the receipt of diesel fuel or its component;
  • the reactive fuel fraction may be hydraulically cleaned and hydraulically cleaned and converted to other propellants.
  • Example I Consumables are mixed for a little more than 400 g.
  • the used raw materials have the following characteristics:
  • Partitioning is carried out in a 2-liter rotating autoclave with a pressure of 8 Sha, a temperature of 425 ° C at a constant speed of 1 hour. Received liquid products are suitable for filtration to separate solid components.
  • Example 3 The process is similar to that described in Example I. TM bruiseI ⁇ elsuyu_syergye analogue I; the oil shale is in the amount of 5% of the mass of mud. The results of ⁇ -20 pessa are given in the table below. The resulting products have a similar behavior to the I method. . Example 3.
  • Example II The process is similar to Example I. Use the same raw materials as Example I, the original mixture is mixed at a temperature of 70 ° C to 10 ° C, which is free of shale. The results of the process are shown in the table below. The resulting products have the same properties as Example I. Example 4. 30 The process is similar to I. Uses raw materials that are analogous to that used. Oh good. The results of the process are given in the table below. Selected products have the same properties as Example I. 35 Example 5.
  • Example 6 The resulting products are similar to those described in Example I. Example 6.
  • Example 9 The process is similar to that described in Example I. They use a raw, analogous method to I, and the product is supplied with a gas by-product at a rate of 220 g. Process results are presented in the table below. Received products have products similar to those described in the example. Example 9.
  • Example I The process is similar to that described in Example I. 30 They use a raw, analogous method to I, which is used for the gasification of the product with a 220 The results of the process are presented in the table below. The resulting products have the same characteristics as those described in - 35 Example I.
  • Example II The process is similar to that described in Example I. They use a raw, analogous method to Example I, with the tempera- - 10 - The acidification rate of 220-340 ° ⁇ is taken in the amount of 1.0 $ from the weight of the unit. The results of the process are given in the table below. The products obtained have the same characteristics as described in Example I. Example II.
  • Example 14 The process is similar to that described in Example I, but at a temperature of 440 ° ⁇ . The results of the process are given in the table below. The resulting products have the same characteristics as Example I. Example 14.
  • Example 15 The process is carried out similarly as described in Example I, but within 20 minutes. The results of the process are given in the table below. The resulting products have the same characteristics as Example I. Example 15.
  • Example 16 The process is similar to that described in Example I, but for 90 minutes. The results of the process are given in the table below. The resulting products have characteristics similar to that of Example I. - II - Example 16.
  • Example 17 The process is similar to that described in Example I, but at a pressure of 10 PSa. The results of the process are given in the table below. The resulting products have charcoal-5 products, similar to Example I. Example 17.
  • Example 18 The process is similar to that described in Example I, but at a pressure of 3 Pa. The results of the process are given in the table below. The resulting products have the characteristics of 10 products, similar to Example I. Example 18.
  • Example 19 The process is carried out in the same way as in Example 3.
  • the original mixture is cooked at a temperature of 60 -00 ° ⁇ .
  • the process will recycle the diesel fraction with a boiling point of 200-370 ° ⁇ 15 in the amount of 10 $ from the weight of the bucket.
  • the results of the process are given in the table below.
  • the resulting products have characteristics similar to those of Example I.
  • Example 19
  • Example 3 The process is carried out in the same way as in Example 3.
  • the original 20 mixture is cooked at a temperature of 50-90 ° ⁇ .
  • the process recycles diesel fraction with a boiling point of 200-370 ° C in the amount of $ 20 from the bucket mass.
  • the results of the process are given in the table below.
  • the products obtained have the same characteristics as in Example I. 25 Example 20.
  • the thermal cracking of this oil is mixed with soft brown coal ( ' ⁇ 0 $ from the net mass) at a temperature of 486 ° C, a pressure of 4 Pa and a time of 90 minutes.

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)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Un procédé, qui permet d'obtenir des distillats de combustibles, consiste à procéder au craquage thermique d'un mélange contenant un produit huileux résiduel et un minéral combustible solide, la sapropélite, à une température allant de 390 à 490 °C et à une pression pouvant atteindre 8 MPa, puis à extraire le produit désiré. On ajoute au mélange initial un produit liquide découlant de la gazéification de la sapropélite ou une fraction de ce produit qui est doté d'un point d'ébullition allant de 220 à 340 °C.
PCT/RU1992/000177 1992-04-30 1992-09-25 Procede permettant d'obtenir des distillats de combustibles Ceased WO1993022399A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SU5040714 RU2009162C1 (ru) 1992-04-30 1992-04-30 Способ получения топливных дистиллятов
RU5040714 1992-04-30

Publications (1)

Publication Number Publication Date
WO1993022399A1 true WO1993022399A1 (fr) 1993-11-11

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ID=21603497

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Application Number Title Priority Date Filing Date
PCT/RU1992/000177 Ceased WO1993022399A1 (fr) 1992-04-30 1992-09-25 Procede permettant d'obtenir des distillats de combustibles

Country Status (2)

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RU (1) RU2009162C1 (fr)
WO (1) WO1993022399A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997019149A1 (fr) * 1995-11-20 1997-05-29 Sergei Vladimirovich Trifonov Installation de craquage thermique de petrole brut

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2132355C1 (ru) * 1998-09-25 1999-06-27 Андриенко Владимир Георгиевич Способ получения жидких продуктов из тяжелых нефтяных остатков
RU2155796C1 (ru) * 1999-06-11 2000-09-10 Научно-исследовательский институт химии при Саратовском государственном университете им. Н.Г. Чернышевского Способ обогащения топливных сланцев

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3870621A (en) * 1973-07-30 1975-03-11 Exxon Research Engineering Co Residuum processing
US4404091A (en) * 1981-10-26 1983-09-13 Mobil Oil Corporation Treatment of shale oils
US4544479A (en) * 1980-09-12 1985-10-01 Mobil Oil Corporation Recovery of metal values from petroleum residua and other fractions

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3870621A (en) * 1973-07-30 1975-03-11 Exxon Research Engineering Co Residuum processing
US4544479A (en) * 1980-09-12 1985-10-01 Mobil Oil Corporation Recovery of metal values from petroleum residua and other fractions
US4404091A (en) * 1981-10-26 1983-09-13 Mobil Oil Corporation Treatment of shale oils

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997019149A1 (fr) * 1995-11-20 1997-05-29 Sergei Vladimirovich Trifonov Installation de craquage thermique de petrole brut
WO1997019148A1 (fr) * 1995-11-20 1997-05-29 Bryson, Julian Raffinage du petrole et des produits petroliers

Also Published As

Publication number Publication date
RU2009162C1 (ru) 1994-03-15

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