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
  • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
  • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
  • C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
  • C10G53/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
• • 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
  • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
  • C10G21/02—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
  • C10L5/00—Solid fuels
  • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
  • C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
  • C10L5/10—Methods of shaping, e.g. pelletizing or briquetting with the aid of binders, e.g. pretreated binders
  • C10L5/14—Methods of shaping, e.g. pelletizing or briquetting with the aid of binders, e.g. pretreated binders with organic binders
  • C10L5/16—Methods of shaping, e.g. pelletizing or briquetting with the aid of binders, e.g. pretreated binders with organic binders with bituminous binders, e.g. tar, pitch

Definitions

• the invention relates to a process for separating predominantly dissolved resinous substances from coal-derived heavy oils, in which two fluid fractions are obtained, one of which contains only a small proportion of toluene-insoluble substances (TI), and the other enriches the toluene-insoluble (TI) is, as well as the use of these fractions.
• TI toluene-insoluble substances
• the quinoline-insoluble solids (QI) present in the residues are undesirable for many processing processes and are therefore removed, if necessary, by mechanical separation processes.
• the separation effect is achieved either due to the particle size as in filtration or primarily due to the higher density of solids as in centrifugation. It is also known to agglomerate the solid particles by adding a promoter liquid so that they can be removed from the residues under the action of gravity by simply letting them settle (DE-PS-2 810 332).
• the almost QI-free residues are mainly used for the production of highly anisotropic carbons.
• the known processes aim to keep the loss of ⁇ -resins (TI - QI) as low as possible.
• This also has the advantage that the 0.1-rich residue is obtained as an easily manageable granulable solid (DE-OS-3 112 004) or as a non-sticky suspension (DE-OS-2 355 606).
• pitches with a high content of ⁇ -resins are required, which also have a not too low content of quinoline-insoluble.
• Additional ⁇ -resins can be produced in the heavy oils by a gentle thermal treatment, but a simultaneous generation of QI, which is not desirable, cannot be avoided. In addition, such thermal processes are very complex. Mechanical separation processes for TI concentration are not known.
• Hard pitches with a high QI content and a high coking residue are required for the production of abrasion-resistant, hard coke with a high bulk density, as are used, for example, for the carburization of steel and cast iron.
• Such hard pitches have hitherto been produced from normal pitches by thermal treatment and blowing with air and coked in horizontal chamber furnaces.
• pitches with a low TI content and a high Bureau of Mines Correlation Index are an excellent carbon black oil component.
• Methods for the production of such carbon black raw materials are described in the patents DE-2 547 679 and DE-2 560 019.
• the insoluble in toluene is removed in a high-speed centrifuge or with a very fine filter.
• this method appears to be of little use for technical implementation due to the small difference in density between the ⁇ -resins and the other pitch components suitable.
• This object is achieved according to the invention in that the content of toluene-insoluble (TI) in the heavy oil used, obtained from coal, with an aromatic solvent to less than 10 % By weight, preferably less than 5% by weight, and the mixture is mixed with a non-aromatic, organic solvent in a ratio of 1: 3 to 5: 1 and with stirring the heavy, TI-rich phase which settles with a peripheral speed of the stirrer of 0.5 to 6.0 m / s at a temperature between 50 and 200 ° C, preferably between 50 and 100 ° C under the influence of gravity with a clarification surface load of up to 1 t / m 2 h in a TI poor and a TI-rich fraction is separated.
• TI toluene-insoluble
• the amount used per unit of time in relation to the clarification area is referred to as the clarification area load.
• the aromatic solvent can be added to the heavy oil first or together with the non-aromatic solvent. Mixing is not a problem. For example, a static mixer can be used. Mixing in a centrifugal pump is also sufficient, however, if the solvent is metered in evenly before the pump.
• a solvent combination of methylnaphthalene oil and petrol has proven itself for heavy oils with a boiling point of about 300 ° C and above, but other solvent combinations such as xylene and n-heptane also serve the same purpose. For reasons of cost, however, fractions are preferred to pure substances.
• ratio of the container diameter (d) to the filling height (h) also has an influence on the removal of the toluene-insoluble.
• a ratio d / h 2 is particularly advantageous.
• the inventive method makes it possible to reduce the residues from the reprocessing of coal-derived heavy oils with reasonable effort and to partially process them into valuable products. This opens up new areas of application for these residues that were previously reserved for oils obtained by distillation.
• the inventive method is explained in more detail on the basis of a few discontinuous exemplary embodiments, without being limited thereto.
• the process can also be carried out continuously with the same result, the mixture of heavy oil and solvents preferably being fed into the agitator tank in the region of the phase interface.
• the sewage treatment area load is 0.15 t / M 2 h.
• the settling process with stirring at 60 ° C is complete after one hour.
• the two fractions are discontinuously distilled at a top pressure of 93 mbar up to a top temperature of 90 ° C. in order to recover the solvents.
• the residues left are 26.3 parts by weight of a low-TI fraction in which there are still 0.2% by weight of toluene but no methanol, and 13.8 parts by weight of a TI-rich fraction in the no solvent residues can be detected.
• the analysis data are shown in the table.
• the TI-poor fraction has a Bureau of Mines Correlation Index of 175 and is used as a soot raw material.
• the coke yield based on the pitch residue (normal pitch) is 62% by weight.
• the mixture After being left to sit for 2 hours with stirring at 73 ° C., the mixture separated into a light and a heavy phase. At 100 mbar head pressure and a bottom temperature of up to 288 ° C., 25 parts by weight of the upper phase and 1 part by weight of solvent are distilled off from the lower phase. In this way, 6 parts by weight of a TI-rich and 4 parts by weight of a TI-poor fraction are obtained, the analysis data of which are listed in the table.
• the 6 parts by weight of the TI-rich fraction are mixed with 3 parts by weight of coal pitch normal pitch with the same analysis data as the pitch to be extracted and processed by gentle helmet distillation to form electrode binders.
• a binder with a softening point of 90 ° C. (K.-S.) a QI content of 10.2% by weight, a ⁇ -resin content of 25.3% by weight, an ash content of 0.28% by weight and a coking residue (Conradson) of 52.6% by weight.
• the phase separation is completed within one hour. 24 parts by weight of solvent and tar oils are distilled off from the light phase at a top pressure of 100 mbar and a bottom temperature of up to 350 ° C. The remaining 5 parts by weight of distillation residue are almost free of Ql and contain only 1.3% by weight of ⁇ -resins. The softening point is 62 ° C (K.-S.) and the coking residue is 43.1% by weight. The residue is used as an impregnating agent in graphite electrodes for steel production.
• 0.5 part by weight is distilled off from the 4 parts by weight of the heavy phase at a top pressure of 100 mbar and a bottom temperature of up to 370.degree.
• the residue with a softening point of 90 ° C (K.-S.) and a coking residue (Conradson) of 54.3% by weight has an ash content of 0.3% by weight and a QI content of 9.5 % By weight and a ⁇ -resin content of 26.7% by weight and is used as an electrode binder.
• a coal-based product from which the ash constituents or the quinoline-insoluble matter has at least partially been removed can also be used as the heavy oil. It is known to reduce the ash content in heavy oils by centrifugation, and to at least partially remove the quinoline-insoluble by filtering, separating or allowing accelerated settling. In particular, methods for removing the quinoline-insoluble by letting the promoter accelerate settling can be combined well with the inventive method.
• Example 2 20 parts by weight of normal pitch coal pitch as in Example 2 are mixed with 9 parts by weight of methylnaphthalene oil (boiling range 235 to 245 ° C) and 9 parts by weight of kerosene (boiling range 250 to 300 ° C) in a tip-top container with a reflux condenser for 3 hours with stirring 250 ° C thermally treated. The mixture is then cooled to 180 ° C. by pumping over a cooler. After one hour without stirring, a QI-rich fraction (20% by weight of the mixture) has settled on the bottom and is drained off.
• methylnaphthalene oil oil
• kerosene boiling range 250 to 300 ° C
• Example 2 A normal pitch as in Example 2 is used. The extraction is carried out as in this example, but without stirring. There is no flowable heavy phase. The material that settles out can neither be loosened nor melted completely and must therefore be removed mechanically.
• Example 2 The test is carried out as described in Example 2, with the exception that only 5 parts by weight of white spirit are used.
• the TI content of the solvent-free TI-low fraction is 3.9% by weight.
• the material is not suitable as a soot oil component.

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• Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• General Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Materials Engineering (AREA)
• Life Sciences & Earth Sciences (AREA)
• Environmental & Geological Engineering (AREA)
• General Life Sciences & Earth Sciences (AREA)
• Geochemistry & Mineralogy (AREA)
• Geology (AREA)
• Working-Up Tar And Pitch (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Coke Industry (AREA)

Applications Claiming Priority (2)

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• 1983
  • 1983-09-29 DE DE19833335316 patent/DE3335316A1/de not_active Withdrawn
• 1984
  • 1984-05-15 DE DE8484200689T patent/DE3475919D1/de not_active Expired
  • 1984-05-15 EP EP84200689A patent/EP0135943B1/de not_active Expired
  • 1984-07-19 ZA ZA845600A patent/ZA845600B/xx unknown
  • 1984-08-06 US US06/637,934 patent/US4582591A/en not_active Expired - Lifetime
  • 1984-09-28 JP JP59202097A patent/JPS6092389A/ja active Granted

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