• 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:
    The invention relates to liquid hydrocarbon mixtures, in particular, a process for the production of raw materials for a reformer and diesel fuel, which can be used in coal chemistry and oil refining. The process is carried out by liquid-phase hydrogenation of a suspension of coal in a solvent at an elevated temperature and a pressure of 300 bar in a circulating hydrogen medium. The resulting products are separated with separation of the vapor-gas stream and the ash residue. The vapor-gas stream is cooled and the solvent and target oil are separated from it. The latter is mixed with H 2 , heated and fed to vapor phase hydrogenation, which is carried out at a pressure of 100-200 bar. The resulting products are separated to obtain the desired products, H 2 O and H 2 -containing gas, which is fed to the circulating hydrogen system. In this case, a mixture of fresh make-up hydrogen in the amount of 2500 nm 3 / t of oil and circulating hydrogen, purified from H 2 O, NH 3 , H 2 S, CO, CO 2 and C 1 -C 4 -hydrocarbons, is fed to vapor-phase hydrogenation, liquid-phase hydrogenation is fed the fraction remaining after separation of the target products and water from the vapor-phase hydrogenation products after intermediate compression to a pressure of 300 bar. For the preferred implementation of the method, it is necessary: a) to divide the total stream of fresh hydrogen into two streams, of which the first is mixed with the raw material fed to vapor phase hydrogenation, and the second is used as a cooling gas during vapor phase hydrogenation b) to use part of the circulating H 2 -containing gas of liquid-phase hydrogenation as a cooling gas during vapor-phase hydrogenation c) part of the cooled waste H 2 -containing gas with vapor-phase hydrogenation circulate as a cooling gas for vapor-phase hydrogenation g) hydrogenation products to be cooled during heat exchange with the oil supplied to the vapor-phase hydrogenation e) the circulating H 2 -containing gas of liquid-phase hydrogenation, together with the suspension of coal in the solvent, is heated by heat exchange with the vapor-gas stream of liquid-phase hydrogenation. The method allows to reduce the pressure of liquid-phase and vapor-phase hydrogenation by 50-200 bar and reduce the consumption of hydrogen. 5 hp f-ly, 2 ill.
    公开号:SU1563596A3
    申请号:SU853942405
    申请日:1985-08-02
    公开日:1990-05-07
    发明作者:Делер Вернер；Мерц Лудвиг；Фронерт Хайнц；Укерманн Бернд；Грезер Ульрих；Янковски Альфонс；Воловски Экард；Тамм Ханс-Фридрих；Вилцок Норберт
    申请人:Феба Ель Энтвиклюнгс-Гезельшафт Мбх (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for the production of raw materials for the installation of reforming and diesel fuel, and may find application in the oil refining and coal chemical industries.
    The aim of the invention is to reduce the pressure of the liquid phase and vapor phase hydrogenation while reducing the consumption of hydrogen.
    FIG. 1 and 2 is a diagram of an installation for carrying out the proposed method,
    Note e. 1. About 50 t / h of coal oil is directed through line 1 and through heat exchanger 2, then mixed with 1250 m2 / h of fresh hydrogen supplied through line 3} and then the mixture is directed through heat exchanger 4 at a pressure of 100 bar and 340 ° C to a steam reactor 5, in which there is a fixed catalyst bed based on Al, Mo, Ni oxide. The vapor phase hydrogenation temperature is 400 ° C. The coal oil supplied via line 1 contains 0518 t / h of light oil with a boiling point below 200 ° C and 0.32 t / h of average oil with a boiling point above- 200 ° C. Fresh hydrogen supplied via line 3 contains 99.5% by volume H2.
    The original coal oil supplied to the vapor phase hydrogenation is characterized by the following data:
    Elemental analysis, wt.%: C 86.01 H 9.96; K 1.00, S 0.03, O 3.0.
    Boiling point by fraction, wt.%: Less than 200 ° C 35.4; 200-325 ° C 60.4; above 325dS 4.2.
    The vapor phase hydrogenation waste stream from the vapor phase reactor 5 through line 6 is cooled in heat exchanger 2. In the high pressure separator 7, 0.49 ton / h of raffinate withdrawn through the pressure reducer is removed through line 8. This raffinate is then distilled further for 0,245 t / h of light oil with boiling point up to 200 ° С for use as a raw material for the reforming process and for 0,245 t / h of mazut or
    with fuel oil temperature a penalty above 200 ° C. The light raffinate oil 9 as a raw material for the reforming process is characterized by a content of N S, O less than 1 mg / kg for each element and has a density of 0.78 g / m 3.
    ten
    15
    20
    25


    ;
    .
    - " but
    635964
    The medium raffinate oil 10 is light fuel oil with a calorific value of 42 mJ / kg. Wastewater is discharged via line 11 and 1000 m5 of gaseous residual gas is separated through line 12, which, after being compressed in compressor 13, is introduced into a circulating gas flow directed to line 14.
    The residual gas of vapor-phase hydrogenation discharged through line 12 contains hydrogen in the amount of 97.8% by volume.
    The circulating gas is supplied through an appropriate compression stage of the compressor 15 for liquid phase hydrogenation.
    The pulp obtained from ground coal with a fraction withdrawn from the effluent stream, after being compressed by compressor 16 and after being mixed with compressed circulating gas through line 17, and heat exchanger 18 is then heated in an oven 19 during heat exchange with the liquid stream free from ash residues hydrogenation and supplied to the liquid-phase hydrogenation in the reactor 20 at a pressure of 300 bar. Then the product leaving the liquid phase reactor
    20, passes through a hot separator
    21, from which the solid-containing stream is discharged via line 22 to further processing. The stream, which does not contain solid particles of products, from the top of the hot separator 21, after cooling in the heat exchanger 18, is passed through heat exchange with the initial pulp through an intermediate separator 23, from which the
    on line 24, an oil fraction for pulping. The gaseous stream leaving the separator 23 in the cooler 25 is cooled from 50 ° C to room temperature and passed through the separating device 26, where the waste water is separated through line 27, and the gaseous stream through line 28 through the scrubber 29 when the waste water is removed. gas via line 30 is fed to circulating gas, line 14, and the resulting coal oil is separated, which, after partial pressure reduction, is supplied via throttle valve 31 to line 1, as mentioned above, to gas-phase hydrogenation. The amount of residual gas of liquid phase hydrogenation (line 29) is 3,960 Nm3 / h, and
    thirty
    35
    40
    45
    55
    contains the following components, vol.%: hf 80.5, C, C2, (3, C4 16.0; CO, CO2 2.5; N7 1.0; H2S, NH3 - traces. The amount of flow 14 is 4 647 m / h, and the flow 30 313.
    Example2. FIG. 2, designations are introduced: 30 — high pressure off-gas flow lines for controlling the partial pressure of hydrogen (exhaust flow); 32 is a line for supplying cooling gas from a liquid phase hydrogenation circulation system to a vapor phase reactor; 33 — Line for vapor-phase hydrogenation; 34 is a vapor phase gas compressor for hydrogenation; 35 - lines of the cooling gas vapor-phase hydrogenation.
    The temperature of the liquid phase hydrogenation is 480 ° C and the vapor phase hydrogenation is 400 ° C, the vapor phase hydrogenation pressure is 200 bar.
    The feedstock (line 1) is 50 tons / h and contains 18 tons / h of light oil with boiling points below 200 ° C and 32 tons / h of average oil having boiling levels above 200 ° C.
    Fresh hydrogen (line 3) 126700 Nm3 / h (99.5% H2 by volume).
    Circulating gas gas phase (line 33) 41700 Nm3 / h (97.8% of Er by volume).
    The off-gas of the gas phase (line 12) is 105000 nm3 / h (97.8% H2 by volume).
    Hydrogen in the raw gas phase is 50000 Nm3 / h (99.0% K7 by volume).
    The cooling gas in the gas phase (line 35) is 118400 Nm3 / h (99.0% H2 by volume).
    Refined oil (line 8) (boiling range above 200 ° C) 49.0 t / h.
    Hydrogenating off-gas in the liquid phase (line 29) 31300 (80.5% K by volume; C ,, C, C3, Cf 16.0% by volume; CO, Cf 2.5% by volume; N 1.0 % by volume; Hg8, NH, traces).
    The refined light oil (line 9) has a boiling range below 185 ° C, 24.5 tons / hour are produced. This oil satisfies the quality of the raw material for the reformer and has a nitrogen content of less than 1 ppm and a density of 0.78 g / m3.
    The cooling gas from the circulating liquid phase hydrogenation system is fed to the reactor 5 (via line 32)
    only in cases of necessity. Therefore, under normal conditions, the amount of this gas is 0. The composition of this gas stream basically corresponds to the composition of the hydrogen-containing gas in the liquid-phase hydrogenation circuit with 85% by volume of hydrogen.
    According to the scheme of Example 2, the flow of line 30 (exhaust gas) is 31300 nm / h. Its composition corresponds to the composition of the flow line 29, containing 80.5% by volume of hydrogen. The rest is inert.
    5 and organic gases.
    The stream of line 14, which is composed of the streams of lines 29 and 12 minus the stream of line 30, contains 85 vol.% Of hydrogen. Stream composition
    0 lines 29 and 30 are identical.
    In quantitative terms, the flux of line 14 is 470000 nm / h, the flux of line 12 is 105000 nm3 / h and the flux of line is 30 31000 nm3 / h. From here they calculate
    5 flow rate for the flux line 29,396,000 Nm3 / h.
    The raw coal oil undergoing gas phase hydrogenation is first preheated in heat exchanger 2 in countercurrent with 5 products leaving the gas phase reactor. This use of heat means an improvement in thermal efficiency. The final heating, together with hydrogenating hydrogen from line 5, is carried out in heater 4 to a temperature of 385 ° C at the vapor phase hydrogenation 5 required at the inlet of the reactor.
    0
    权利要求:
    Claims (6)
    [1]
    1. The method of obtaining raw materials for the installation of reforming and diesel
    5 fuel from coal by liquid-phase hydrogenation of a suspension of coal in a solvent at elevated temperature and pressure in the circulating hydrogen medium, subsequent separation of liquid-phase hydrogenation products with separation of the vapor-gas stream and ash residue, cooling the vapor-gas stream, separation of the solvent and left-oil oil from it, mixing the latter with hydrogen, heating and feeding to vapor-phase hydrogenation, separating the products of vapor-phase hydrogenation to obtain the desired products, water s
    five
    and hydrogen-containing gas and supplying it to a circulating hydrogen system, characterized in that, in order to reduce pressure and hydrogen consumption, liquid-phase hydrogenation is carried out at a pressure of 300 bar vapor — at a pressure of 100-200 bar, the total amount of hydrogen is fed to the process for vapor-phase hydrogenation, at In this case, purified hydrogen mainly from ammonia, hydrogen sulfide, CO, C0, j, and Ct-C4 hydrocarbons is fed to vapor-phase hydrogenation as circulating hydrogen mixed with fresh make-up hydrogen, taken in the amount of 2500 nm / ton m la, and circulating hydrogen in liquid-phase hydrogenation is fed fraction remaining after separation of the desired products and water from the hydrogenation products of PA-rofaznoy after intermediate compression to the pressure liquid-phase hydrogenation.
    [2]
    2. The method according to claim 1, about tl and h a-y and i, so that the total stream of fresh hydrogen is divided into two streams, of which the first stream is mixed with the raw material fed to the vapor-phase hydrogenation, and the second
    the current is used as a cooling gas during vapor phase hydrogenation.
    [3]
    3. A method according to claim 1, characterized in that a part of the circulating hydrogen-containing gas of liquid-phase hydrogenation is used as a cooling gas during vapor-phase hydrogenation.
    [4]
    4. A method according to claim 1, characterized in that a portion of the cooled spent hydrogen-containing gas after vapor-phase hydrogenation is circulated as a cooling gas to vapor-phase hydrogenation
    [5]
    5. A method according to claim 1, characterized in that the vapor-phase hydrogenation products are cooled during heat exchange with the oil supplied to the vapor-phase hydrogenation.
    [6]
    6. A method according to claim 1, characterized in that the circulating hydrogen-containing gas of liquid-phase hydrogenation, together with the suspension of coal in the solvent, is heated by heat exchange with a vapor-gas stream of liquid-phase hydrogenation.
    Priority points:
    04.08.84- on PP. 1 and 6;
    04.05.85 - on PP, 2-5.
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    同族专利:
    公开号 | 公开日
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    PL254799A1|1986-06-17|
    CN1003375B|1989-02-22|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3652446A|1969-11-17|1972-03-28|Exxon Research Engineering Co|Combination process for liquefaction of coal and catalytic cracking of selected fractions thereof|
    US3755137A|1971-03-24|1973-08-28|Hydrocarbon Research Inc|Multi-stage ebullated bed coal-oil hydrogenation and hydrocracking process|
    US3892654A|1974-03-04|1975-07-01|Us Interior|Dual temperature coal solvation process|
    US4045328A|1976-07-23|1977-08-30|Exxon Research And Engineering Company|Production of hydrogenated coal liquids|
    US4048054A|1976-07-23|1977-09-13|Exxon Research And Engineering Company|Liquefaction of coal|
    US4189371A|1976-08-20|1980-02-19|Exxon Research & Engineering Co.|Multiple-stage hydrogen-donor coal liquefaction process|
    US4111788A|1976-09-23|1978-09-05|Hydrocarbon Research, Inc.|Staged hydrogenation of low rank coal|
    US4123347A|1976-12-22|1978-10-31|Exxon Research & Engineering Co.|Coal liquefaction process|
    US4330391A|1976-12-27|1982-05-18|Chevron Research Company|Coal liquefaction process|
    US4330389A|1976-12-27|1982-05-18|Chevron Research Company|Coal liquefaction process|
    US4222844A|1978-05-08|1980-09-16|Exxon Research & Engineering Co.|Use of once-through treat gas to remove the heat of reaction in solvent hydrogenation processes|
    US4159236A|1978-05-12|1979-06-26|Gulf Oil Corporation|Method for combining coal liquefaction and gasification processes|
    US4338182A|1978-10-13|1982-07-06|Exxon Research & Engineering Co.|Multiple-stage hydrogen-donor coal liquefaction|
    US4452688A|1979-09-04|1984-06-05|Electric Power Research Institute|Integrated coal liquefication process|
    US4300996A|1979-12-26|1981-11-17|Chevron Research Company|Three-stage coal liquefaction process|
    US4410414A|1980-01-18|1983-10-18|Hybrid Energy Systems, Inc.|Method for hydroconversion of solid carbonaceous materials|
    US4322283A|1980-09-04|1982-03-30|Exxon Research & Engineering Co.|Coal conversion in the presence of added hydrogen sulfide|
    US4485008A|1980-12-05|1984-11-27|Exxon Research And Engineering Co.|Liquefaction process|
    US4400263A|1981-02-09|1983-08-23|Hri, Inc.|H-Coal process and plant design|
    DE3105030A1|1981-02-12|1982-09-02|Basf Ag, 6700 Ludwigshafen|METHOD FOR THE CONTINUOUS PRODUCTION OF HYDROCARBON OILS FROM COAL BY PRESSURE HYDROGENATION IN TWO STAGES|US4569749A|1984-08-20|1986-02-11|Gulf Research & Development Company|Coal liquefaction process|
    US4795841A|1987-04-02|1989-01-03|Elliott Douglas C|Process for upgrading biomass pyrolyzates|
    DE3741105C2|1987-12-04|1990-01-04|Veba Oel Entwicklungs-Gesellschaft Mbh, 4650 Gelsenkirchen, De|
    US20090232725A1|2007-11-23|2009-09-17|Sherman Aaron|Flow rate of gas in fluidized bed during conversion of carbon based material to natural gas and activated carbon|
    WO2009067266A1|2007-11-23|2009-05-28|Robert Walker|Apparatus and method for converting carbonacious material containing hydrogen deficient carbon into diesel fuel|
    US9688934B2|2007-11-23|2017-06-27|Bixby Energy Systems, Inc.|Process for and processor of natural gas and activated carbon together with blower|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3428783A|DE3428783C2|1984-08-04|1984-08-04|
    DE3516084|1985-05-04|
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