• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A process for increasing the fuel yield of coal liquefaction products by extracting the asphaltenes, resins and aromatic compounds from said coal liquefaction products. This is accomplished by contacting said coal liquefaction products with a halogenated aliphatic solvent to form two phases, one containing tar and the other containing said solvent and the remainder of said coal liquefaction products, separating said phases from each other and treating said tar phase with a second solvent to recover asphaltenes, resins and/or aromatics in said tar phase. The resulting asphaltenes, resins and/or aromatics are suitable for upgrading to produce additional synthetic fuel.
    公开号:SU927125A3
    申请号:SU782678808
    申请日:1978-10-20
    公开日:1982-05-07
    发明作者:Анджело Параскос Джон
    申请人:Галф Рисерч Энд Дивелопмент Компани(Фирма)；
    IPC主号:
    专利说明:

    hydrogen is supplied to the liquefaction zone containing the hydrogenation catalyst. Hydrogen comes from the recirculation system and, if necessary, from an additional source. The product of the dilution of the coal obtained in the zone. liquefaction as a result of a conventional hydrogenation process, is transferred to a mixing zone along with trichlorofluoroethane. Trichlorofluoroethane and the liquefaction product coal containing tar and / or solid particles are thoroughly mixed and then transferred to a separation zone or hydrocyclone, where the liquefaction product, tar and solid particles are separated, forming the lower phase containing the carbon liquefying product without tar and and / or solid particles and trichlorofluoroethane and upper (once containing tar and / or solid particles, as well as some amounts of trapped trichlorfluoroethane. The lower phase is removed from the separation zone and transferred to the solvent purification zone, where from solvent is removed from the heat exchanger and removed from the heat exchanger. The oil product enters the collecting device, and part of the oil is returned to the suspension zone through the oil recirculation channel.The upper zone containing tar and / or solid particles and solvent is fed to the solvent purification zone, in which the solvent is cleaned of tar and / or solid products using a heat exchanger is returned to mixing with the products of coal liquefaction in the mixing zone.
    The tar and solids are transferred to the washing and extraction zone, where the second hydrocarbon solvent, for example benzene, hexane or cyclohexane, also enters. Here, asphaltenes, resins and aromatics fed to tar are recovered from tar. the cleaning zone of the second solvent, where, using a heat exchanger, the second solvent is freed from asphaltenes, resins and aromatic compounds and is fed into a collecting device. Asphaltenes, resins and aromatics are fed to the enrichment device. The remaining tar and solids can enter the gas production zone, where steam and free oxygen are also injected. In the gas receiving zone, free oxygen enters an exothermic reaction with tar and solid particles, which release carbon dioxide, carbon monoxide, nitrogen and methane gas, water vapor and heat. The vapor shifts the secondary reactions between the gases towards the evolution of hydrogen. The remaining tar and NHg enter the collecting device; hydrogen and other components are fed to the hydrogen enrichment zone, from where carbon monoxide, carbon dioxide, nitrogen and methane are transferred to a collecting device. Hydrogen to the zone of liquefaction coal.
    The yield of fuels ps1 emitted in the process of liquefying coal is increased by extracting asphaltenes, resins and aromatics from the tar-containing by-product obtained in the process of carbon liquefying Synthetic liquid fuels boiling in the range of 38.3 to 7 ° C, have a density of from 0.9 to 1.1, with a molecular ratio of carbon to hydrogen ranging from 1 to 0.66: 1. A typical example is a solvent oil derived from sub-bituminous coal, for example, high-carbon coal, containing an average oil with a boiling range from 190.5 to
    The table provides data on the composition and content of coal and other solid carbon-containing substances that can be used to obtain a liquid product recovered with trichlorofluoroethane in accordance with the proposed method of moisture absence).
    The presence of carbon and hydrogen in the carbonaceous material is mainly due to benzene compounds, multiring aromatic compounds, heterocyclic compounds, etc. Nitrogen is present mainly in chemical bonding with aromatics. Some sulfur and oxygen are in chemical bonds with aromatics. and part in chemical communication with neorga
    elements, such as iron and calcium.
    Examples of solid carbonaceous materials that can be processed
    in accordance with the invention, the enriched products obtained from them are anthracite, bituminous and sub-bituminous, brown and other types of coal. The relative amount of solvent and solid carbonaceous matter may vary, but it is required that the solvent be sufficient to ensure the conversion of most of the solid carbonaceous substance In the reaction vessel. The ratio of the weight of the solvent to the weight of the solid carbonaceous material may lie in the range from 0.6: 1 to 9: 1, but | in a preferred embodiment, from 1: 1 to 4: 1. Best results are achieved when this ratio is 2: 1. The weight ratio of solvent to solid carbonaceous material may be used, exceeding 1, but this does not give additional advantages when dissolving or suspending a solid. It is not advisable to introduce an excessive amount of solvent, since additional energy is required for the subsequent separation of the solvent. Any solvent capable of extracting asphaltenes, resins and aromatics, for example benzene, toluene, n-hexane or cyclohexyl, and mixtures thereof can be used. Under asphaltenes, there are clusters of condensation polyaromatics containing heteroatomic compounds and forming large micellar structures, their molecular weight is from 200 to 25,000, and in the preferred embodiment from 500 to 5000. More specifically, asphaltenes can be characterized by a high number of condensates. polycyclic aromatic rings containing, in addition, naphthalene and paraffin side
    Rials, as well as other types of coal products, are examples of solid coal-containing materials that can be processed in accordance with
    according to the invention, for the preparation of enriched products therefrom. Instead of solid carbonaceous materials, other coal-bearing shales and tar-containing chains can be processed. The structure of condensation polycyclic aromatic rings can usually contain small amounts of other elements,; example, sulfur, nitrogen and / or oxygen atoms and heavy metals (vanadium, nickel, etc.). Anthracite, bituminous and sub-bituminous coals, brown coal mathepasi, from which similar liquid hydrocarbons are obtained. Example. Coal suspension containing crushed Bighlorn coal I, 8 kg; anthracene oil 33.76 kg and crushed hydrogenation catalyst 1, kg, including Ni 3.8%, Ti 5, and Mo Q, kl, deposited on an alumina base, together with hydrogen are subjected to hydrogetization at 398.88 ° C and pressure kg / cm for 0.75 hours, as a result of which a coal liquefaction product is obtained, containing liquid coal 9.6 kg, tar 116, 4+ kg and 2.5 kg of solid particles. Trichlorotrifluoroethane (2 kg) is added to the liquefying carbon product and the resulting mixture is stirred for 5 minutes. The mixture is then allowed to separate into an upper phase containing tar, solids and some trapped trichlorotrifluoroethane, and a lower phase containing liquid coal and trichlorotrifluoroethane. After separation of the two phases, there is essentially no tar or solid particles in the lower phase. iInsoluble tar and solids are extracted using a second solvent, for example benzene, toluene, n-hexane or cyclohexane, and mixtures thereof. About 10.30 kg of additional synthetic fuel is obtained from tar and solid particles. From the foregoing, it is evident that almost all the solid particles in the coal liquefaction product are separated from the resulting synthetic liquid fuel, the yield of which increases.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of producing liquid synthetic fuel from coal-slurry products suspended in a solvent, characterized in that, in order to increase the yield of the target product, the suspended carbon dilution products are mixed with trichlorofluoroethane to form an upper phase containing tar, and
    the lower phase, containing trichlorofluoroethane and the remaining products of carbon dilution, followed by separation of the resulting phases and treating the tar-containing phase with hydrocarbon solvents to isolate the desired yield.
    Sources of information taken into account in the examination 1. US patent number, class. 20810, published, 10/20/77 (prototype).
    类似技术:
    公开号 | 公开日 | 专利标题
    US4079005A|1978-03-14|Method for separating undissolved solids from a coal liquefaction product
    US3617513A|1971-11-02|Coking of heavy feedstocks
    SU927125A3|1982-05-07|Process for producing synthetic liquid fuel
    US4119523A|1978-10-10|Processes for the production of deashed coal
    US4028219A|1977-06-07|Process for the production of deashed coal liquifaction products
    CA1149303A|1983-07-05|Coal extraction process
    US3796650A|1974-03-12|Coal liquefaction process
    US3705092A|1972-12-05|Solvent extraction of coal by a heavy oil
    US3850738A|1974-11-26|Bituminous coal liquefaction process
    US4561964A|1985-12-31|Catalyst for the hydroconversion of carbonaceous materials
    US3813329A|1974-05-28|Solvent extraction of coal utilizing a heteropoly acid catalyst
    US4846963A|1989-07-11|Ionic liquefaction process
    US4094766A|1978-06-13|Coal liquefaction product deashing process
    US4551224A|1985-11-05|Coal liquefaction process
    US4081358A|1978-03-28|Process for the liquefaction of coal and separation of solids from the liquid product
    US4338182A|1982-07-06|Multiple-stage hydrogen-donor coal liquefaction
    US4396491A|1983-08-02|Solvent extraction of oil shale or tar sands
    US3909390A|1975-09-30|Coal liquefaction process
    US4032428A|1977-06-28|Liquefaction of coal
    SU904530A3|1982-02-07|Method of separating tar and solid particles from coal liquflyed products
    US3755136A|1973-08-28|System for removing solids from coal liquefaction reactor effluents
    US4472263A|1984-09-18|Process for solvent refining of coal using a denitrogenated and dephenolated solvent
    US4099932A|1978-07-11|Conversion of solid fuels to fluid fuels
    US4461694A|1984-07-24|Coal liquefaction process with enhanced process solvent
    US4040957A|1977-08-09|Separation of insoluble material from coal liquefaction product by use of a diluent
    同族专利:
    公开号 | 公开日
    NL7815039A|1979-10-31|
    EP0001675A2|1979-05-02|
    ZA785241B|1979-09-26|
    AU3957778A|1980-03-13|
    JPS5470303A|1979-06-06|
    CS207724B2|1981-08-31|
    EP0001675A3|1979-05-16|
    GB2041398B|1982-07-07|
    GB2041398A|1980-09-10|
    AU518252B2|1981-09-24|
    FR2433041A1|1980-03-07|
    DD139133A5|1979-12-12|
    DE2857225A1|1980-05-08|
    BR7806681A|1979-07-03|
    US4133740A|1979-01-09|
    CA1119544A|1982-03-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2616607C1|2016-06-21|2017-04-18|Акционерное общество "Всероссийский научно-исследовательский институт по переработке нефти" |Synthetic oil production method|GB475723A|1935-05-23|1937-11-24|Edeleanu Gmbh|Improvements relating to the refining of hydrocarbon oils|
    US2223184A|1936-08-15|1940-11-26|William E Currie|Splitting up of extracts obtained from solid carbonaceous materials|
    US2453543A|1948-04-09|1948-11-09|Ernest J Schabelitz|Process of treating bituminous coal|
    US2631982A|1951-03-09|1953-03-17|Allied Chem & Dye Corp|Process for treating tar|
    US2871181A|1955-06-15|1959-01-27|Consolidation Coal Co|Method of removing finely divided solid particles from hydrocarbonaceous liquids|
    US3598717A|1968-06-25|1971-08-10|Universal Oil Prod Co|Method for liquefying coal|
    US3583900A|1969-12-29|1971-06-08|Universal Oil Prod Co|Coal liquefaction process by three-stage solvent extraction|US4257869A|1979-08-17|1981-03-24|Electric Power Research Institute|Liquefaction of acid treated coal|
    US4298451A|1980-02-25|1981-11-03|The United States Of America As Represented By The United States Department Of Energy|Two stage liquefaction of coal|
    FR2502636B1|1981-03-27|1983-06-24|Sumitomo Metal Ind|
    JPH0676585B2|1982-12-28|1994-09-28|三菱化成株式会社|Hydrogenation method of solvent refined coal|
    BR8504611A|1985-09-20|1987-04-28|Petroleo Brasileiro Sa|PROCESS TO SEPARATE WATER AND SOLIDS FROM FUELS, IN PARTICULAR FROM SHALE OIL|
    FR2594839B1|1986-02-26|1988-11-04|Inst Francais Du Petrole|PROCESS FOR THE FRACTIONATION OF SOLID ASPHALTS|
    JPH0717913B2|1988-05-31|1995-03-01|日本褐炭液化株式会社|Liquefaction method of coal|
    US6717021B2|2000-06-13|2004-04-06|Conocophillips Company|Solvating component and solvent system for mesophase pitch|
    US20080256852A1|2007-04-20|2008-10-23|Schobert Harold H|Integrated process and apparatus for producing coal-based jet fuel, diesel fuel, and distillate fuels|
    BRPI0915321A2|2008-06-15|2016-11-01|Craig Nazzer|process for separating solids from beneficial or harmful liquids by vaporization|
    EP3103858A1|2015-06-08|2016-12-14|L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude|Method for washing organic liquids with a liquid comprising flurohydrocarbons|
    RU2629559C1|2016-10-24|2017-08-30|Российская Федерация, от имени которой выступает Государственная корпорация по атомной энергии "Росатом"|Additive to fuel|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/844,456|US4133740A|1977-10-21|1977-10-21|Process for increasing the fuel yield of coal liquefaction products by extraction of asphaltenes, resins and aromatic compounds from said coal liquefaction products|
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