• 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:
    In the process for the hydroconversion of heavy and residual oils, spent and waste oils mixed with sewage sludges in a typical liquid-phase hydrogenation with hydrogen-containing gases with addition of a finely ground material, this additive preferably has a large internal surface area. …<??>Industrial and also municipal sewage sludges frequently contain problematic constituents which preclude disposal by application to fields in agriculture or landfill or by combustion and pyrolysis processes. …<??>The additive is added in two different grain size ranges, in such a way that a part of the additive is a fine-grained fraction having a grain size of 90 mu m or less and another part is a coarse-grain fraction of a grain size from 100 mu m to 2000 mu m, preferably 100 to 1000 mu m, and that the process is carried out at a weight ratio of the feed oils and the sewage sludges used of 10 : 1 to 1 : 1.5. …<??>The process is used for converting the vacuum residue from a Venezuelan heavy oil with addition of 2% by weight of lignite coke as an additive and admixing of 10% by weight of sewage sludge in a liquid-phase hydrogenation to obtain, in particular, useful liquid products and extensive conversion of the organic fractions of the sewage sludge.
    公开号:SU1739853A3
    申请号:SU884356701
    申请日:1988-10-27
    公开日:1992-06-07
    发明作者:Кречмар Клаус；Мерц Людвиг；Ниманн Клаус
    申请人:Феба Ель Энтвиклюнгсгезельшафт, Мбх (Фирма)；
    IPC主号:
    专利说明:


    Yo
    The invention relates to a method for hydrogenating the conversion of a mixture of residual oils and purified sludge and can be used in the petrochemical industry.
    Methods are known for processing clarified spam by burning and pyrolysis.
    The closest to the invention is the method of hydrogenating the conversion of a mixture of residual oils and purified sludge in the liquid phase at a partial pressure of hydrogen of 150-2.0 bar, temperature 400-450 ° C, hydrogen: oil 1000-5000 nm3 / t liquid and solid starting products in the presence of coke brown coal additive l. The amount of additive is
    2 wt.% Of the total amount of liquid
    and solid starting materials.
    However, the degree of conversion is insufficient. (E)
    The purpose of the invention is to increase the degree of conversion. ". QQ
    The goal is achieved by the fact ff | that according to the method of hydrogenating the Јe} version of the mixture of residual oils and purified sludge in the liquid phase at a partial hydrogen pressure of 150
    200 bar, temperature 400 - 490 ° С, hydrogen: oil ratio 1000 - 5000 Nm3 / t of liquid and solid initial products in the presence of an additive - coke of brown coal in the amount of 2 wt.% From the total amount of liquid and solid initial products, additive used in the form of two fractions - a fraction with a grain size of 90 mm and a fraction with a grain size of 1UO - 1000 mm with the process at a mass ratio of residual oil: purified sludge equal to 9: 1.
    The method is carried out as follows.
    A high pressure pump transports the oil, respectively, a mixture of oil with a solid substance, including an additive, to the high pressure section of the installation. The circulating gas and fresh hydrogen are heated and admixed, for example, to the residual oil in the high pressure compartment. The reaction mixture is passed, for using the reaction heat of the reaction products, through the regenerator battery and heater and then into the reactors. A reactor system consists, for example, of three vertical hollow tube reactors connected in series, which operate with flow upwards. Here conversion takes place at temperatures of 400 - 490 ° C and a partial pressure of hydrogen t50 - -200 bar. Due to the supply of cold gas, the quasi-isothermal nature of the operation of reactors is possible.
    In connected hot separators, which operate at approximately the same temperature as the reactors, the unconverted portion of the used heavy oils residual oils, as well as solids, is separated from the gaseous under the process conditions of the reaction products. The bottom product of the hot sep parator is choked stepwise.
    After intensive cooling and condensation, the gas and liquid are separated in a cold high pressure separator. The liquid product is throttled and can be recycled further in conventional refinery processes.
    Gaseous reaction products, including Cj-Cd-gases, are released from the gas. Hydrogen in the form of circulating gas is returned to the process.
    PRI me R. In a continuously operating unit for hydrogenation with three successively connected vertical liquid-phase reactors, the residue of vacuum distillation of a heavy oil is converted with the addition of 2 wt.% Brown coal coke consisting of a fraction less than 90 mm in an amount of 90 wt.% And a fraction more than 90 mm into a coke.
    1739853f
    10 wt.% and 10 wt.% clarified sludge (dried to a residual moisture content of less than 2%, milled and sieved to less than 80 mm) in the presence of
    1.5 m3 of hydrogen per 1 kg of residue and with a partial pressure of hydrogen of 190 bar. In order to achieve a 90% by weight conversion of the residue, the average temperature in the series-connected liquid-phase reactors is set at 465 ° C. The specific capacity is 0.5. (500 ° С +)
    The vacuum residue used in the process has the following element
    five
    Nye composition, wt.%:
    C H
    S
    N
    ABOUT
    On
    Sa
    Hi
    V
    weights.m.d.
    84,60
    10.41
    3.19
    0.80
    0.5
    6 ppm
    76 ppm 76 ppt
    The content of asphaltenes is (according to Condranson) wt%, coke (according to Condranson) 17.56 wt.%, Fractions 200 ° С 0 wt.%; 200 - 350 ° C 0 wt.%; 350 - 500 ° C 3.1 500 ° C 96.9% by weight.
    Used sludge has the following elemental composition, wt.%:
    C34,4
    II2,9
    S0.7
    Fe2,5
    Ash53.0
    Water10.0
    This sludge is generated during the treatment of domestic and industrial wastewater in a sewage treatment plant.
    The following are the conditions for conducting hydrogenation conversion in the presence and absence of clarified sludge,
    0
    The temperature of the liquid phase, C Consumption t - e yellow oil,
    The costs of clarified sludge,
    BUT
    with clarified slime
    465
    0.482
    0.054
    AT
    without bleached sludge
    465
    0.528
    1.5 0.5 280 250
    1.5
    0.5
    280
    250
    25
    learn the following re
    AB
    with clarification- without clarified sludge
    30 7.6 7.6
    5,579,7
    7.0 2.2
    90.2 90.0 70
    the way is carried out of the sludge having ab, wt.%:
    35
    40
    45
    The slurry contains 52.62 wt.% Ash and has the following characteristics:
    True density, g / cm31,89
    Bulk density, g / cm30,44
    Porosity, ml / 110.62
    The yield of liquid products (oil) is 75.5 wt.% (Calculated on the amount of the original oil + clarified sludge). These products have the following composition, vol.%: Up to 200 ° C 22, 200 - 250 ° C 39, above 350 ° C 39.
    The use of an additive in the form of 2 fractions eliminates the process of foaming the contents of the reactors, leading to a decrease in conversion
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of hydrogenating the conversion of a mixture of residual oils and purified sludge in the liquid phase with a partial pressure of hydrogen of 150-200 bar, temperature of 400-490 ° C, hydrogen: oil ratio 1000-5000 Nm3 / ton of liquid and solid starting products in the presence of brown coal coke , taken in an amount of 2% by weight of the total amount of liquid and solid starting products, characterized in that, in order to increase the conversion level, the additive is used in the form of two fractions - a fraction with a grain size of 90 mm and / fraction with a grain size of 100- 1000 mm and the process is carried out and the weight ratio of the residual oil: refined slurry is 9: 1.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1739853A3|1992-06-07|Method of hydrogenation-conversion of residual oils and purified slime mixture
    US4781796A|1988-11-01|Apparatus for the conversion of sludges
    US5114541A|1992-05-19|Process for producing solid, liquid and gaseous fuels from organic starting material
    US5292442A|1994-03-08|Process for disposing of sewage sludge
    US4145274A|1979-03-20|Pyrolysis with staged recovery
    US4052173A|1977-10-04|Simultaneous gasification of coal and pyrolysis of organic solid waste materials
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    US5217625A|1993-06-08|Process for disposing of sewage sludge
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    US5264009A|1993-11-23|Processing of sewage sludge for use as a fuel
    US5188739A|1993-02-23|Disposal of sewage sludge
    GB2073239A|1981-10-14|Coal extraction process
    US4054492A|1977-10-18|Process for treating bituminous or oil-containing material using dry distillation
    Bridle1982|Sludge derived oil: wastewater treatment implications
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    EP0545683B1|1996-07-03|Disposal of sewage sludge
    US4839021A|1989-06-13|Treatment of petroleum derived organic sludges and oil residues
    US4463210A|1984-07-31|Production of chemical feedstock by the methanolysis of wood
    US3733187A|1973-05-15|Process for converting solid wastes to pipeline gas
    同族专利:
    公开号 | 公开日
    NO884896L|1989-05-05|
    EP0314992A2|1989-05-10|
    US5064523A|1991-11-12|
    DD283417A5|1990-10-10|
    DE3737370C1|1989-05-18|
    EP0314992A3|1990-01-17|
    NO884896D0|1988-11-03|
    引用文献:
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    USRE29156E|1971-11-30|1977-03-22|Black Clawson Fibreclaim, Inc.|Fuel by-products of municipal refuse|
    US4206032A|1978-03-17|1980-06-03|Rockwell International Corporation|Hydrogenation of carbonaceous materials|
    US4396786A|1980-10-27|1983-08-02|Johnson Matthey Public Limited Company|Method for producing fuel oil from cellulosic materials|
    DE3100899A1|1981-01-14|1982-08-05|Basf Ag, 6700 Ludwigshafen|METHOD FOR DRAINING MINERAL OIL CONTAINERS WITH RECOVERY OF THE OIL PART|
    US4370221A|1981-03-03|1983-01-25|Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Energy, Mines And Resources|Catalytic hydrocracking of heavy oils|
    DE3221411A1|1982-06-05|1983-12-08|Veba Oel Entwicklungsgesellschaft mbH, 4660 Gelsenkirchen-Buer|METHOD FOR HYDROGENATING HEAVY OIL, BITUMEN AND THE LIKE|
    CA1225062A|1983-09-13|1987-08-04|Trevor R. Bridle|Processes and apparatus for the conversion of sludges|
    DE3412536A1|1984-04-04|1985-10-31|Fried. Krupp Gmbh, 4300 Essen|METHOD FOR PRODUCING HYDROCARBONS FROM CLEANING SLUDGE|
    DE3442506C2|1984-11-22|1987-04-16|Union Rheinische Braunkohlen Kraftstoff Ag, 5000 Koeln, De|
    NO861708L|1985-06-07|1986-12-08|Kraftwerk Union Ag|PYROLYSIS PLANT.|
    DE3634275A1|1986-10-08|1988-04-28|Veba Oel Entwicklungs Gmbh|METHOD FOR HYDROGENATING CONVERSION OF HEAVY AND RESIDUAL OILS|
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    US5824731A|1996-10-23|1998-10-20|Rondy & Co., Inc.|Thermoplastic carbon black concentrates containing reclaim carbon black|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3737370A|DE3737370C1|1987-11-04|1987-11-04|Process for the hydroconversion of heavy and residual soils, waste and waste allogols mixed with sewage sludge|
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