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
  • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
• • 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
  • C10G1/065—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 in the presence of a solvent

Definitions

• the invention relates to the separation of liquid products from the hot separator residues of the bottom or combined bottom and gas phase hydrogenation of coal, heavy oil, bitumen and similar starting products, such as residues from top or vacuum distillation of crude oil.
• the mixture After passing through a preheater, the mixture is passed from below through a reactor system in which hydrocracking reactions take place at temperatures between 250 and 550 ° C, preferably 380-480 ° C, which lead to the cleavage of large molecules and their partial desulfurization, denitrification and deoxygenation .
• Disposable catalysts are preferably used as catalysts.
• these are, for example, molybdic acid, tin oxalate / ammonium chloride, Bayer mass and lux mass.
• catalysts are used which contain catalytically active metal compounds, for example tungsten, molybdenum, lead, tin, chromium, cobalt and nickel, in particular iron, on a carrier such as active carbon or in particular coke.
• the catalysts are used in amounts of up to 10% by weight, based on the starting product, in particular 1 to 6% by weight.
• the reaction mixture passes into a hot separator, from the top of which gaseous and vaporous reaction products, from the foot of unreacted feed, asphaltenes, catalyst and a certain amount of heavy and medium oil are drawn off as hot sludge.
• the hot separator which can also consist of a system of several separators connected in series, is operated at temperatures which are up to 100 K, preferably 20 to 40 K below the reactor temperature.
• the gaseous or vaporous products drawn off at the top of the hot separator are either regulated in a cold relaxation system and fed to further processing, or are passed under reaction pressure from a short distance from above into a system of reactors in which the gaseous or vaporous products are carried by fixed bed catalysts desulphurized, denitrified, deoxygenated and split (cf. W. Urban “Petroleum processing in the Scholvener 300 at combi hydrogenation chamber" in Petroleum and Coal, 8 (1955), pp. 780 - 782).
• the products of this "combi-hydrogenation" are regulated by a cold separator system and sent for further processing.
• the liquid product yield of the bottom or combined bottom and gas phase hydrogenation is increased in that part of the liquid constituents are separated from the base product of the hot separator with the aid of process gases and stripped.
• the process gas is passed through the product at temperatures between 20 and 300 ° C., preferably 50 to 200 ° C. and a pressure between 10 and 300 bar, preferably 50 to 200 bar.
• Any gas obtained in the process preferably a fraction enriched by washing from the process gas and containing methane, ethane, propane, butanes and pentanes, in particular high contents of propane, butane and / or pentane, can be used as stripping gas.
• the treatment of the hot sludge with the process gases expediently takes place continuously in that a pressure vessel coupled to the hot separator system is charged from above with the hot sludge and from below with the process gases.
• the weight ratio of hot blowdown: process gases is 1:10, preferably 1: 3, the throughput is 0.2 to 2.0 m 3 , preferably 0.3 to 0.6 m 3 blowdown per m 3 pressure vessel volume and per hour.
• the stripping gas can be removed from the entrained constituents of the hydrogenation residue by reducing the pressure to 100 to 1 bar, preferably 70 to 30 bar or increasing the temperature by 20 up to 150 K, preferably 50 to 100 K or a combination of both measures, for example a temperature increase of 20 to 70 K with a pressure reduction to 100 to 50 bar.
• the liquid products are refined or split in the gas phase reactor; in the case of coal hydrogenation, they serve as asphaltene-free mashing oil components.
• the stripping gas can be used again for separation after pressure increase by means of a compressor or a fan or after cooling.
• the solid-containing residue, enriched in metals and asphaltenes, from the treatment of the hot sludge with the process gases is removed from the process by the gas pressure via a lock system and can be fed to gasification, in order to cover the hydrogen requirement of the hydrogenation process.
• This hot sludge was placed in a downstream 5 l container with fittings for gas and liquid distribution at 200 bar and 150 ° C with 4.8 kg / h of a propane-butane mixture (propane: butane weight ratio 3: 2). treated.
• the gaseous product was let down to 40 bar, 0.9 kg / h of a liquid product with a boiling point of 520 ° C. separating.
• the product was free of asphaltenes and metals, its H / C ratio was 1.3; the sulfur content was 1.5% by weight.
• the solids in the residue were enriched to 28% by weight; the residue contained all metals that had been introduced into the process with the oil and the single-use catalyst.

Landscapes

• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Life Sciences & Earth Sciences (AREA)
• Wood Science & Technology (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Compositions Of Macromolecular Compounds (AREA)
• Working-Up Tar And Pitch (AREA)

Applications Claiming Priority (2)

Publications (3)

Family

ID=6134663

Family Applications (1)

Country Status (4)

Families Citing this family (1)

Family Cites Families (2)

• 1981
  • 1981-06-13 DE DE19813123535 patent/DE3123535A1/de not_active Withdrawn
• 1982
  • 1982-06-03 NO NO821844A patent/NO162864C/no unknown
  • 1982-06-11 DE DE8282105119T patent/DE3276003D1/de not_active Expired
  • 1982-06-11 EP EP82105119A patent/EP0068231B1/fr not_active Expired
  • 1982-06-11 CA CA000405046A patent/CA1171013A/fr not_active Expired

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