• 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 the production of liquid fuels from coal and can be used in oil refining and coal chemistry. The purpose of the invention is to improve the quality of the target products and reduce the catalyst flow. The process is carried out by mixing coal with a solvent and a catalyst, followed by hydrogenating the resulting suspension, separating the obtained hydrogenation products in a hot separator into a vapor-gas stream and a liquid-solid phase. Then the vapor-gas stream is fed to catalytic hydrogenation with the release in the form of a liquid phase of the solvent, recycled for mixing with coal, and the vapor-gas phase, subjected to additional hydrogenation with condensation of the vapor-gas phase and the selection of the target products. By vacuum evaporation of the liquid-solid phase, a distillate is obtained that is recycled to the process. It is advisable to distill the vapor-gas phase before hydrogenation, with the release of the target liquid phase. The vapor-gas stream is first subjected to separation in a hot separator, and the separated liquid phase is recirculated for mixing with the hydrogenation products. The distillate separated from the liquid-solid phase is added to the vapor-gas stream directed to additional catalytic hydrogenation, or distilled is added to the hydrogenation products before separation and x in a hot separator, or the distillate is subjected to additional hydrogenation followed by recycling to the stage mix with coal and solvent slurry. These conditions reduce the content of basic nitrogen in the target fraction with. 20-320 C up to 6 mg / kg and phenolic oxygen up to 15 mg / kg. 3 hp f-ly, 5 ill. SO with O) 00 4 Yu
    公开号:SU1468427A3
    申请号:SU864027591
    申请日:1986-06-02
    公开日:1989-03-23
    发明作者:Воловски Экард；Леринг Райнер；Фридрих Франк；Штробель Бернд
    申请人:Рурколе Аг (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to a process for the calming of liquid products from coal and can be used in the coal chemical industry.
    The aim of the invention is to improve the quality of the target products and reduce the consumption of the catalyst.
    FIG. 1-5 are flowcharts for implementing the method.
    According to FIG. 1 The crushed coal supplied by LI 1, which may already contain the catalyst mass, is mixed with recycled liquid hydrocarbons (solvent) through line 2 until the slurry in the apparatus 3 is obtained. The mass ratio of coal (anhydrous) to solvent may be about 1: 0.8-1: 3, preferably 1: 1 and 1: 1.5. As a catalyst, compounds of iron, cobalt, nickel, tungsten, molybdenum, zinc or tin with oxygen or sulfur, usually on a carrier, as well as their mixtures, are usually used for hydrogenation. The suspension of coal is pumped through the pump 4 through the heater 5 into the reactor 6. Po. lines 7 sell hydrogenating gas consisting of circulating gas supplied through line 8 and fresh hydrogen supplied through line 9. The hydrogen content in the circulating gas must be more than 50 vol.% In addition, the circulating gas is supplied in different height in reactors 6, 10, and 11 (not shown) in the quantity necessary to provide temperature control. The total amount of circulating gas supplied by compressor 12 is 1-8 of them / k coal free from water and ash. The amount of fresh hydrogen is (depending on the consumption of hydrogen) 0.7-1.5 nm / kg coal. The coal slurry and the hydrogenation gas are heated in the preheater 5 and are subjected to hydration in the reactor 6 at 450-500 C and a pressure of more than 100 bar. Reactor 6 can consist of one or more tanks. In case the reactor is provided with a fluidized bed of catalyst, the coal slurry should not contain a catalyst mass. The hydrogenation product is fed through line 13 to hot cenajpaTop 14, in which, at 440-480 ° C, vapor and gases are separated from liquid and solid substances (waste slurry) and withdrawn through line 15. The waste slurry is expanded and fed into a vacuum an evaporator 16 for separating hydrocarbons contained therein. T-water through line 17 is usually used to produce hydrogen.
    The vapors from the evaporation stage are condensed in the heat exchanger 18 and fed to the collector 19. The liquid phase obtained in the same way is either fed through line 20 to prepare coal slurry, or by pump 21 is added 22 to the vapor-gas phase of the hot separator 14. It is possible to withdraw some of the liquid phase on line 20, and the rest to file on line
    22c the vapor-gas phase of the hot separator 14. The temperature of the mixture is controlled in the heat exchanger 23 before entering the reactor 10. The latter at the entrance to the reactor is 350-420 ° C. In reactors 10 and 11 catalysts are used, which are usually used in the processing of hydrocarbon fractions of coal and oil . In this case, the same or different catalysts can be used in reactors 10 and 11 in order to achieve the best results, for example, for a given coal or the corresponding target product regarding the degree of refining, saturation, cleavage and consumption of hydrogen.
    The vapors and gases leaving the reactor 10 are cooled in the heat exchanger 24 so that such an amount of solvent is constantly condensed that is consumed in the preparation of coal slurry. This solvent, by expansion, is withdrawn from intermediate separator 25 and recycled through line 2 to mixer 3. The required temperature before intermediate separator 25 is 250 to 350 seconds.
    Temperature of vapors and gases from the intermediate separator
    23 through line 26, is increased by heat exchange and, if necessary, additional regulation (refrigerator or heater 27) to the inlet temperature of the reactor 11 (350-420 s) containing a fixed catalyst bed. By cooling to a temperature below 50 ° C in the heat exchanger 28, liquid products are separated from the vapor-gas mixture in the cold separator 29, which are withdrawn along line 30. In addition, water containing ammonia and hydrogen sulfide formed during hydrogenation is condensed. It is diverted along line 31.
    A gas mixture consisting mainly of hydrogen and hydrocarbon gases is withdrawn from the head of the cold separator 29. The latter also contains hydrogen sulphide, ammonia and a small amount of carbon oxides. In the installation 32 for flushing the gas under high pressure, this gas is purified to the necessary degree and enriched with hydrogen. By means of the compressor 12, the circulating gas is recirculated to the process.
    The implementation of the method according to FIG. 2 differs from that described in that the lead product of intermediate separator 25 discharged through line 26 is cooled from heat exchanger 33 so that the secondary fraction is withdrawn from additional intermediate separator 34 through line 35 (boiling point is 185-325 ° C). This additional intermediate separator 34 may be (like a distillation column) provided with packing or other elements to increase the accuracy of the separation process. The 17 17ars removed from the head of the separator or column 34 and gases are heated in the heat exchanger 27 to the inlet temperature of the reactor 11 (350-420 ° C). At the same time, a product consisting of a light fraction (boiling end 185 s) 5 which can be directly reformed is withdrawn from the cold separator 29.
    The implementation of the method according to
    1468427
    ten
    Hydrogenation is carried out in the catalyst containing re-heated Pe 42 at 350-420 s and at about the same pressure as in other reactors. In this case, hydrogen is added to the overhead product in an amount of 0 5. All products 45 coming out of the reactor 42 are added to the coal suspension under pressure in front of the preheater 5. In this connection, the solid content in the slurry coal produced in the mixer 1 is increased compared to the 15 other forms of the process. Unused hydrogen in the reactor 42 can be completely used to hydrogenate the coal slurry. Therefore, the amount of feed on line 9 of fresh hydrogen can be responsibly reduced.
    Example 1. In the installation according to FIG. 1 I mix 126 kg of anhydrous gas-flame gas (120 kg / h, excluding ash and ash content) with 5 kg of dry catalyst mass based on iron oxide and 134 kg / h of recirculated solvent, and the resulting suspension 30 together with 650 hydrogenating ha (the amount of gas refers to normal conditions), consisting of 150 m- / h of fresh hydrogen and 500 m of circulating gas (with
    20
    25
     FIG. 3 differs from that of FIG. 1 gg of hydrogen (60 vol.%) Is passed through the fact that reactor 6 is distilled from the evaporator 16. The pressure in the reactor 6 is pumped through the line 36 to 40.0 Sh, and the temperature 37 to mix with the hot products
    reactor 6 before entering the hot separator 14.
    The implementation of the method according to FIG. 4 differs from that of FIG. 3 in that the vapor-gas phase of the hot separator 14 through line 38 is fed to an additional hot separation to the separator 39. The resulting vapors and gases are discharged through line 40, and the waste gas is fed to collector 19 through line 41.
    An embodiment of the method according to FIG. 5 differs from that described in FIG. 1 by the fact that an additional reactor 42 is installed outside the co-gas cycle. In this form of operation, hydrogen or hydrogen-containing gas supplied via line 43 is added to the head product of the vacuum evaporator 16 and then heated in the heat exchanger-heater 44 and sub-70 ° C. Steam temperature the space of the hot separator 14 is kept at 440 ° C. The effluent from the hot separator 14 is subjected to evaporation by expansion under. At the same time, 24 kg / h of distillate with t, kip are obtained. 320-45-40 C, which is added to the recycled solvent without further processing. All the head products of the hot separator 14 are passed through. through the reactor 10, containing 80 kg 50, a fixed catalyst bed of nickel sulphides (2.4 wt.% Ni) and molybdenum (10 wt.% Mo) on alumina and silicon dioxide (mass ratio 9: 1) as a nose 55 tel. The average temperature of the catalyst is, and the pressure is 40.0 Sha. The outgoing products are cooled to 275 C. At the same time, 110 kg / h of solvent are obtained, which is from 1468427
    ten
    Hydrogenation is carried out in a reactor containing a fluidized bed of a catalyst 42 at 350-420 s and at about the same pressure as in other reactors. In this case, hydrogen is added to the overhead product in an amount of 0.5-5. All products 45 coming out of the reactor 42 are added to the coal suspension under pressure in front of the preheater 5. In this connection, the solid content in the coal suspension produced in the mixer 1 is increased compared to the other 5 forms of the process. The unused hydrogen in the reactor 42 can be fully used to hydrogenate the coal slurry. Therefore, the amount of fresh hydrogen supplied through line 9 can be reduced accordingly.
    Example 1. In an installation according to FIG. 1 x 126 kg of anhydrous gas-flame coal (120 kg / h, excluding water and ash content) are mixed with 5 kg of dry catalyst mass based on iron oxide and 134 kg / h of recirculated solvent, together with 650 hydrogenation gas (the amount of gas refers to normal conditions) consisting of 150 m- / h of fresh hydrogen and 500 circulating gas (containing
    0
    five
    g of hydrogen (60 vol.%) is passed through reactor 6. The pressure in reactor 6 is 40.0 Sha, and the temperature
    gg of hydrogen (60 vol.%) is passed through reactor 6. The pressure in reactor 6 is 40.0 Sh, and the temperature
    470 C. The temperature in the vapor space of the hot separator 14 is maintained at 440 ° C. The waste slurry leaving the hot separator 14 is subjected to evaporation by expansion under. At the same time, 24 kg / h of distillate with t, kip are obtained. 320-540 ° C, which is added to the recycled solvent without further processing. All the head products of the hot separator 14 are passed through. through the reactor 10, containing 80 kg of 0, a fixed catalyst bed of nickel sulphides (2.4 wt.% Ni) and molybdenum (10 wt.% Mo) on alumina and silicon dioxide (mass ratio 9: 1) as a nose 5 tel. The average temperature of the catalyst is, and the pressure is 40.0 Sha. The outgoing products are cooled to 275 ° C. In this way, 110 kg / h of solvent is obtained, which is removed from the intermediate separator 25 and combined with the solvent supplied via line 20. The recycled solvent thus obtained contains 38% by weight of a heavy fraction with a boiling point. 325-440 ° C and 62 wt.% Average fraction with BP. 185-325 s. Intermediate Separator Head Products 25
     14684278
    154 kg / h of solvent, which is removed from intermediate separator 25. This solvent is continuously recycled to the coal slurry preparation stage. It consists of 30 wt.% Of the heavy fraction with b.p. 325-385 C and 70 wt.% Average fraction
    with bp 205-325 C. Vapors and gases, vys so kip. 205-325 C. Couples and gases, you
    passed through reactor 11 containing Q coming from the upper part of intermediate separator 25, passing through reactor 11 also containing 80 kg of a fixed bed of catalyst based on nickel (2.4 wt.% Ni) and molybdenum
    15 (9.8 wt.% Mo) deposited on alumina. The temperature of the catalyst is on average 390 C. By cooling the ducts to
    20 to 29 get 55 kg / h of a clear product consisting of 40% by weight of light fraction with mp. 20-185 C and 60 wt.% Of the average fraction with so kip. 185-325 s. After 1 month the product is still
    25 is colorless. This product contains 6 mg / kg of basic nitrogen and less than 15 micron / kg of phenolic oxygen. Light fraction contains less
    thirty
    80 kg of a fixed catalyst bed consisting of molybdenum sulphides (9.8% by weight of Mo) and nickel (2.4% by weight of Ni) on alumina as a carrier. The average temperature of the catalyst is, and the pressure is 40.0 MPa. Due to cooling to 20 ° C, 65 kg / h (54 wt.% Free of water and ash coal) are condensed from the reaction products; the clear product is exhausted from the cold separator 29. The product has a boil. 20-320 ° C and contains 20 mg / kg of basic nitrogen and 50 mg / kg of phenolic oxygen. After storage for 1 month without access of air and light, the product has a slightly yellow color.
    Example 2. In the apparatus according to FIG. 1, 105 kg of dry gas-flame coal (100 kg / h excluding water and ash content) are mixed with 4 kg / h of dry iron oxide catalyst and 154 kg / h of recycled solvent every hour. This coal suspension, together with 625 hydrogenation gas consisting of 125 m / h of fresh hydrogen and 500 m / h of circulating gas (containing 80% by volume of hydrogen), is passed through reactor 6 with a capacity of 200 liters. The pressure in the reactor 6 is 30.0 MPa, and the temperature is 470 ° C. In the hot separator 14, the temperature is maintained at 440 ° C. The waste slurry 45 leaving the hot separator 14 is subjected to evaporation by an expansion of 1 year by vacuum. In this way, 21 kg / h of distillate are obtained. 320-430 ° C, which is fed to the point before the inlet of the reactor 10. In addition, the entire product of the hot separator 14 is passed through the JQ 10 reactor. The reactor 10 contains 80 kg of a fixed catalyst bed based on nickel
    (2.3 wt.% Ni) and molybdenum (9.4 wt.% 55 basic Mo) deposited on alumina. The average oxygen temperature of the catalyst is 1 month without. By cooling the 10 products leaving the reactor to 290 ° C, half-exiting the reactor to 20 ° C in a cold separator
    than 2 mg / kg of nitrogen.
    35
    40
    Example 3. Example 2 is repeated in the installation of FIG. 2 with the difference that the vapors discharged at 290 C from the head of the intermediate separator 25 and gases are cooled to 170 C and fed to the distant part of the packed column 34 with 25 theoretical plates (at a load of 20 l / h). From the cube of the column, 33 kg / h of the average fraction with so-called bale are removed by expansion. 185-325 C. The vapors and gases escaping from the upper part of the column at 160 C are heated and passed through the reactor 11. Reactor 11 contains 50 kg of a fixed catalyst bed based on nickel (2.4 wt.% Ni) and molybdenum (9, 8 wt.% Mo) deposited on alumina. The average temperature of the catalyst bed is maintained at 375 ° C. The products leaving the reactor are cooled to. In the cold separator 29, 22 kg of the light fraction are obtained every hour, b.p. 20-185 C.
    The middle fraction contains 0.06 wt.% Of nitrogen and less than 0.1 wt.%. After storage for air and light, the product has a yellow, straw-like color. No precipitate formation was observed on oxide. The temperature of the catalyst was 390 ° C.
    leaving the reactor about 20 ° C in a cold separator
    more
    than 2 mg / kg of nitrogen.
    5 Q
    5 basic oxygen, 1 month without
    five
    0
    Example 3. Example 2 is repeated in the installation of FIG. 2 with the difference that the vapors discharged at 290 C from the head of the intermediate separator 25 and gases are cooled to 170 C and fed to the distant part of the packed column 34 with 25 theoretical plates (at a load of 20 l / h). From the cube of the column, 33 kg / h of the average fraction with so-called bale are removed by expansion. 185-325 C. The vapors and gases escaping from the upper part of the column at 160 C are heated and passed through the reactor 11. Reactor 11 contains 50 kg of a fixed catalyst bed based on nickel (2.4 wt.% Ni) and molybdenum (9, 8 wt.% Mo) deposited on alumina. The average temperature of the catalyst bed is maintained at 375 ° C. The products leaving the reactor are cooled to. In the cold separator 29, 22 kg of the light fraction are obtained every hour, b.p. 20-185 C.
    The middle fraction contains 0.06 wt.% Of nitrogen and less than 0.1 wt.%. After storage for air and light, the product has a yellow, straw-like color. No precipitate formation was observed.
    is. The light fraction contains 1 mg / kg titrated nitrogen and oxygen each. After storage for 1 month, it remains light.
    Example 4. In the installation according to FIG. 3 through the reactor 6 with a capacity of 20C, hourly, at a pressure of 35.0 MPa, 100 kg of gas-flame coal (excluding water and ash) are passed together with 4 kg / h of dry iron oxide catalyst and 154 kg / h of recirculating solvent. In addition, 550 circulating gas (65% by volume of hydrogen) and 125 fresh hydrogen are introduced. The products leaving the reactor are fed to hot separator 14, where, b.p. 440 sec from is divided into liquid waste slurry and a vapor-gas stream removed from the head. From the waste sludge from the hot separator 14, distillation in the evaporator is 16–20 kg / h of the liquid phase, b.p. 330-440 s. After condensation B of the cooler 18, the liquid phase is fed to the collector 19, from which, using a pump 36, it is fed via line 37 to the products leaving the reactor.
    The head products of the hot separator 14 are passed at 390 ° C through the 50 liter of the 10 non-mobile catalyst layer based on nickel (2.3 May.% Ni) and molybdenum (9.4% by weight of Co) deposited on clay. - land After cooling to 275 ° C in the intermediate separator 25, 154 kg / h of solvent s-b.p. 200-385 ° C used to obtain a coal slurry. The overhead stream from intermediate separator 25 is heated to З90 s and at 400 ° C is passed through 80 liters of cobalt-based fixed bed catalyst (3 wt.% Co) and molybdenum (10, B wt.% Mo) contained in reactor 11, deposited on alumina. After cooling the product of the reactor 11 from the cold separator 29, 54 kg / h of product were withdrawn with a bp. 40-315 s, containing 15 µg / kg of nitrogen and 20 mg / kg of phenolic oxygen. It consists of 45 wt.% Light fraction (boiling up to 185 C) and 55 wt.% Of the middle fraction. After storage for 1 month, the initially clear product has a slightly yellow color.
    Example 5. In the installation according to FIG. 4 through the reactor 6 with a capacity of 200 liters hourly passed at
    ten
    25
    about t
    46842710
    and a pressure of 280 bar 100 kg of flame coal (excluding water and ooli), together with 4 kg / h of a dry catalyst based on iron oxide and 154 kg / h of recycled solvent. In addition, 550 circulating gas (80% by volume of hydrogen) and 125 m / h of fresh hydrogen were introduced. The products leaving the reactor are fed to a hot separator 14, where at 450 ° C they are separated into liquid waste slurry and a vapor-gas stream removed from the head. This stream is passed through after 15 subsequent additional hot separator 39.
    From the waste slurry of the hot separator 14 is distilled off in the evaporator 26 18 kg / h of the liquid phase, b.p. 340-20 C. This liquid phase is combined with waste slurry (2 kg / h, bp 330-420 C, contains 1 wt.% Solids) of additional hot separator 39 and is fed through line 37 to the exit reactor products
    thirty
    35
    40
    45
    50
    55
    before feeding to the hot separator 14.
    The head products of the additional hot separator 39 are passed at 380 ° C. through 80 liters of fixed bed catalyst in the reactor 10 based on nickel (2.3% by weight Ni) and molybdenum (9.4% by weight Mo) deposited on alumina. After cooling to 280 ° C in the intermediate separator 25, 154 kg / h of the solvent used to prepare the coal slurry is obtained. The overhead stream from intermediate separator 25 is heated to 390 ° C and, with 80 liters of cobalt-based catalyst (3.0% by weight of Co) and molybdenum (10.8% by weight of Mo) deposited on the alumina. After cooling the products of the reactor 11 from the cold separator 29, 54 kg / h of product were withdrawn with a bp. 20-315 С, containing 10 mg / kg of basic nitrogen - and 15 mg / kg of phenolic oxygen. It consists of 45 wt.% Light fraction (boiling up to 185 C) and 55 wt.% Of the average fraction. After storage for 1 month, the initially clear product has a slightly yellow color.
    Example 6. In the installation according to FIG. 5 conducted experiment using low bituminous coal. At the same time, 109 kg / h of anhydrous coal (100 kg / h of carbon without water content
    and ashes) - mixed with 4 kg / h of catalyst based on iron oxide and 87 kg / g of 1 circulating solvent, and the resulting suspension is continuously fed by pump 4 to preheater 5. Before the preheater .5, 150 circulating gas containing 85% by volume is supplied hydrogen. In addition, before the preheater 5, hot liquid and gaseous products removed from the reactor 42 are added to the coal slurry. The reactor 42 contains 25 kg of a fixed catalyst bed based on nickel (2.4 wt.% Ni) and molybdenum (9.4 wt.% Mo) deposited on alumina as a carrier. In the reactor 42, all the product obtained by evaporation by expansion with a boil. 320-430 C (25 kg / h, if necessary, after saturation with hydrogen sulfide) are treated with 125 m / h of fresh hydrogen at 385 ° C and a pressure of 152 bar. The reactor 6 with a capacity of 200 l is operated at 45 ° C and pressure of 15.0 Mlla. In the hot separator 14, the hydrogenation products are separated at 450 ° C into liquid waste sludge and a stream of vapors and gases, which after cooling to 370 ° C are passed through reactor 10 with 80 kg of a fixed bed of catalyst based on tungsten sulfides (20% by weight W) and nickel (3.0 wt.% Ni) on alumina as a carrier. The pressure in the reactor is 15.0 MPa, and the temperature is 390 ° C. The products of the reactor 10 are cooled to 330 ° C. From the subsequent intermediate separator 25, 87 kg / h having a boil. 195-370 ° C mixture of medium and heavy fractions used to prepare coal slurry.
    The vapor-gas head product of the intermediate separator 25 is heated from 330 to Z70 s and passed through reactor 11 with 80 kg of a fixed bed of catalyst based on nickel (2.4 wt.% Ni) and molybdenum (9.8 wt. Mo) deposited on alumina. At the same time, they operate at a pressure of 15.0 MPa and a temperature. After cooling the reaction products to 20 ° C, 56.5 kg / h of product consisting of 40% by weight of the light fraction with a boil out of the cold separator 29 is withdrawn. 20-185 ° C and 60% by weight of the middle fraction with a bp. 185-325 ° C. The content of basic nitrogen is 8 mg / kg, and the content of phenol oxygen
    0
    five
    0
    five
    0
    five
    0
    five
    0
    five
    about 15 mg / kg. After storage for 1 month without access of air and light, the product remains bright.
    Example 7 (comparative). Example 2 is repeated, with the difference that the hydrogenation in the reactor 10 is carried out on 160 kg of catalyst and the vapor-gas phase removed from the intermediate separator 25 is fed to the liquid products and the circulating gas from it. At this, 55 kg / h of product is obtained, consisting of 36% by weight of the light fraction with mp. 20-185 C and 64 wt.% Of the average fraction with BP. 185-325 0. The nitrogen content is 100 mg / kg.
    After storage for 1 month, the initially clear product has a yellow color.
    Comparison of the results of examples 2 and 7 shows that the product obtained by a known method has the worst quality, despite the fact that the hydrogenation stage in the reactor 10 is carried out at the same catalyst consumption as the total consumption in the described method (80 kg in the reactor 10 and 80 kg in the reactor 11).
    Example 8 (comparative). Example 2 is repeated, with the difference that the hydrogenation in the reactor 10 is carried out on 180 kg of catalyst and the vapor-gas phase withdrawn from the intermediate separator 25 is fed to the separation of liquid products and circulating gas from it. In this way, 55 kg / h of product is obtained, consisting of 35% by weight of the light fraction with mp. 20-185 C and 65 wt.% Of the average fraction with BP. 185-325 0. The nitrogen content is 90 mg / kg. After storage for 1 month, the initially clear product has a yellowish color.
    权利要求:
    Claims (3)
    [1]
    1. A method for producing a liquid pro-. of coal by mixing coal with
     31
    a solvent and a catalyst, subsequent hydrogenation of the resulting suspension, separation of the obtained hydrogenation products in a hot separator to the vapor-gas flow and the liquid solid phase, supplying the vapor-gas flow to catalytic hydrogenation followed by separation from the hydrogenation products in the form of a liquid phase solvent, recycled to the offset coal, and the vapor-gas phase of the target products with the subsequent precipitation from it by condensation of the target products and the circulating gas of the evolution from the liquid-solid phase of a vacuum evaporation of the distillate and its recirculation into the process, in particular, so that, in order to improve the quality of the target products and reduce the consumption of the catalyst, the vapor-gas phase is subjected to additional catalytic hydrogenation.


    14
    [2]
    2. Process according to claim 1, characterized in that, before hydrogenation, the vapor-gas phase is subjected to
    additional distillation with the release of the liquid phase as the desired product.
    [3]
    3. The method according to claim 1, differing from that with the fact that the vapor – gas flow
    subjected to additional separation in the hot separator and the resulting liquid phase is recycled for mixing with the hydrogenation products.
     A method according to claim 1, distinguishing between Yuk and the fact that the distillate, injected from the liquid-solid phase, is added to the vapor-gas stream before additional catalytic hydrogenation or to the hydrogenation products before separation of the latter in a hot separator, or subjected to additional hydrogenation and recycle mix: e with coal slurry and
    solvent.
    Phie.1
    FIG. 2
    12
    f (yo
    / 5 / JS
    7
    /
    and L-
    /
    Compiled by N. Koroleva Editor S. Pekar Tehred L. Serdyukova Proofreader M, Sharoshi
    Order 1220/59
    Circulation 446
    VNIIPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology of the USSR 113035, Moscow, Zh-35, Raushsk nab. 4/5
    Production and publishing plant Patent, Uzhgorod, st. Gagarin, 101
    Fi.Ts
    12
    FI.5
    Subscription
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    同族专利:
    公开号 | 公开日
    EP0209665B1|1988-10-12|
    EP0209665A1|1987-01-28|
    US4741822A|1988-05-03|
    JPS62285983A|1987-12-11|
    DE3660919D1|1988-11-17|
    AU581990B2|1989-03-09|
    JPH0784597B2|1995-09-13|
    ZA864365B|1986-12-09|
    AU8658089A|1987-12-03|
    DE3519830C2|1993-07-22|
    DE3519830A1|1986-12-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    DE2654635B2|1976-12-02|1979-07-12|Ludwig Dr. 6703 Limburgerhof Raichle|Process for the continuous production of hydrocarbon oils from coal by cracking pressure hydrogenation|
    US4330391A|1976-12-27|1982-05-18|Chevron Research Company|Coal liquefaction process|
    US4338182A|1978-10-13|1982-07-06|Exxon Research & Engineering Co.|Multiple-stage hydrogen-donor coal liquefaction|
    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|
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    申请号 | 申请日 | 专利标题
    DE3519830A|DE3519830C2|1985-06-03|1985-06-03|
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