• 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 STVA products from coal and to be used in coke chemistry. The installation consists of a reactor, a high-pressure separator (HW), pipelines, a vapor-gas stream (GWP) and ash ash from the high-pressure hub, high-pressure intermediate separators (SP), equipped with pipelines for the removal of the GWP, an H2-discharge unit equipped with a pipeline to discharge the circulating H2-containing gas. To ensure the reliability of the apparatus operating at high pressure, the reactor and the HW are made in the form of two bodies inserted one into the other with an annular cavity between them. This cavity is filled with pressure medium. The annular cavities are connected to a pipeline in which pipelines enter, leading off the GWP from the HS or from the PS or H2-containing gas from the hydrogen separation unit from the entrance to the compressor. This installation allows not to replace the medium in the annular cavity, since it does not receive high-boiling components, and, therefore, does not pitch. In addition, it improves the reliability of operation of the high-pressure unit in combination with effective pressure equalization through pipelines indirectly connected to the suction line of the circulation compressor, 4 sludge. O) 00 SP) about sd 00 gn
    公开号:SU1360589A3
    申请号:SU843758548
    申请日:1984-06-29
    公开日:1987-12-15
    发明作者:Воловски Эккард；Миртш Франк
    申请人:Рурколе Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a plant for the processing of coal, in particular to a plant for coal hydrogenation to produce fleshy products.
    Reactors of conventional coal hydrogenation plants have a ceramic lining in order to maintain external (carrier pressure) lining at a lower temperature. However, in these reactors, the porous lining can be destroyed during rapid depressurization of the reactor.
    For chemical reactions that take place at elevated pressures and temperatures, actors themselves, based on the principle of a bubble, justify themselves. To withstand high temperatures
    The high-pressure pump 2 is brought to a pressure of approximately 320 bar. Partially preheated in heat exchanger
    (, ke 3 hydrogenating gas at a pressure of 320 bar is supplied via line 4 to coal slurry, a three-phase mixture consisting of a solid phase (coal, catalyst based on 30 wt.%), coal
    10 levodorods and hydrogenating gas,
    heated in the heat exchanger 5 and the heater 6 to the temperature at the inlet of the reactor 430–460 ° C; the three-phase reaction mixture is allowed through line 7 to
    The 15 cut reactors 8 are hydrogenated and then fed via line 9 to the high pressure hot separator 10, where the bottom phase (high-boiling hydrocarbons and
    and chemical corrosion, internally about 20 solids), and from the upper part of the reactor, the reactor consists of a heat-resistant and corrosion-resistant material. The reaction pressure is transferred to the outer shell of the reactor, which is at a lower temperature. This is done by means of a gas or liquid support medium, which is located between the reactor shell / in the annular space and which transfers the internal pressure to the outer carrier shell and at the same time creates a differential between the inner and outer shell of the reactor. Thus, in comparison with a continuous wall reactor, it is possible to manufacture the inner and outer platings of the reactor relatively thin and, thus, cheap. An important prerequisite for the use of such reactors is the continuously provided pressure equalization between the internal cavity and the supporting medium in the annular cavity. This pressure equalization should also be provided for the unsteady reactor mode (commissioning, shutdown, loading), and for emergency modes (for example, Lenin's fast pressure release during an emergency temperature rise in the reactor).
    The purpose of the invention is to increase the reliability of the high pressure unit.
    FIG. 1-4 shows the proposed installation,
    PRI m-e 1. In the installation according to figure 1, the suspension of coal in recycled hydrocarbons along the line 1 pos
    The high-pressure pump 2 is brought to a pressure of approximately 320 bar. Partially preheated in heat exchanger
    ke 3 hydrogenating gas at a pressure of 320 bar is supplied via line 4 to the coal suspension, a three-phase mixture consisting of a solid phase (coal, catalyst based on 30 wt.%), coal
    hydrohydrogen and hydrogenation gas,
    heated in the heat exchanger 5 and the heater 6 to the temperature at the inlet of the reactor 430–460 ° C; the three-phase reaction mixture is allowed through line 7 to
    the hydrogenation reactors 8 are then fed via line 9 to the high-pressure hot separator 10, where 1 cubic phase is withdrawn from the bottom (high-boiling hydrocarbons and
    0
    five
    ti on line 12 - vapor phase (excess hydrogenating gas, reaction gases and vaporous hydrocarbons). The vapor-gas phase is partially cooled 5 (to about 240 ° C) in heat exchangers 5 and 3, as a result of which a part of the hydrocarbons condenses. In the high-pressure intermediate separator 13, both phases are separated from one another by lines 14 and 15.
    The vapor phase via line 14 is fed to cooler 16, where it is cooled to near ambient temperature (e.g., 40 ° C), thereby condensing the remaining hydrocarbons. The separation of the cooled hydrocarbons from the residual vapor-gas phase (hydrogenating gas, gaseous hydrocarbons, residual gases) is carried out in a high-pressure intermediate separator 17 on lines 18 and 19. During the washing stage 20, hydrocarbon gases (.) Are removed from the residual gas. lines 21, and the hydrogenating gases, after adjusting to a pressure of 320 bar from tank 22, by means of a compressor 23 and adding fresh hydrogen supplied via line 24 as a hydrogenating gas, are fed to the process via line 4.
    According to the invention, the solution of the task of providing the required pressure level in the internal tank of the reactors and the hot separator l is carried out by means of a pipe 25 between the upper part of the separator 13 and the annular spaces of the reactors and the hot separator. Pipeline 25 is a connecting pipe.
    five
    0
    and performs pressure equalization between the reservoirs connected by it. The condensation of hydrocarbons in the pipeline 25 is prevented by installing heaters or placing cooler 26 under the separator 13.
    The proposed placement of the pipeline between the top of the hot separator 10 and the intermediate parator 13, i.e. indirectly on the suction side of the compressor 23, due to the fact that during the hydrogenation of coal, the pressure loss between the reactors 8 and the separator 13 is relatively low (approximately 7 bar), so that without additional regulating means a sufficient and simultaneous equalization of pressure between the internal cavity and the annular reactor space. In the case of a pipeline between the pressure side of the compressor 23 and the annular spaces of the reactors and the hot separator, this does not occur, because a three phase blend (the hydrogenation of coal greatly increases the viscosity due to the swelling of the coal) there is a relatively large pressure drop (for example, 20 bar), which leads to the presence of excess pressure in
    annular space acting on the wall of the internal tank of the reactor. The indicated pressure drop values are characteristic for normal operation of the plant.
    In emergency cases, pressure drops in the reactors can occur (in the event of an emergency discharge when coal is hydrogenated, for example, from 300 to about 130 bar in 5 minutes). Sudden pressures in comparable intervals occur because, for example, when the reactor overheats, emergency pressure release is promptly turned on. While in normal operation (quasi-stationary mode), the proposed placement of the connecting pipework water in the internal tank of the reactor maintains a small pressure, with a sharp decrease in pressure (for example, during an emergency discharge) a small excess pressure in the annular space acts on the internal tank of the reactor. Thus, there is no one-sided high
    the loads on the inner tank, and the inner tanks of the reactors and the hot separator can be made relatively thin walled.
    The installation of FIG. 1 works as follows.
    The feed in the suspension process contains 100 kg of coal, 5 kg of catalyst based on iron oxide and 150 kg of recycled hydrocarbons and has a temperature and pressure of 320 bar.
    Use coal of the following characteristics.
    Technical and chemical analysis, wt.%:
    Carbon 77.1
    Hydrogen 4.3
    Nitrogen1,3
    Oxygen 3.8
    Sulfur0.9
    five
    0
    five
    0
    five
    0
    Humidity Ash content Sieve analysis May.%:
    um
    192
    96
    64
    48
    24
    sixteen
    eight
    2
    7.6. 5.0.
    the remainder
    on the screen:
    0.0 8.2
    19.8
    27.0
    51.7
    63.2
    80.0
    94.3
    Hydrogenating gas (consisting of 95 kg of circulating gas and 15 kg of fresh hydrogen) is added to this suspension. After heating in devices 5 and 6, a mixture of coal slurry with gas with a temperature and pressure of 302 bar is fed to the first reactor 8.
    In the hot separator 10, the reaction product is separated into a head product and a bottom product, which is removed from the process. The latter consists of 21 kg of the solid phase (undissolved coal, catalyst, ash) and 92 kg of hydrocarbons at a temperature of 400 ° C and a pressure of 299 bar.
    The head product (299 bar) is cooled in heat exchangers 5 and 3 and subjected to hot separation in the steam generator 13 at a temperature of 240 ° C and a pressure of 292 bar per vapor-gas phase and condensed hydrocarbons (79 kg), which in line 15 serves for recycling.
    51360589b
    The gas-vapor mixture is cooled in tag-aid of the compressor 23 and adding
    exchanger 16 to about. Hydrocarbons condensed therewith (49 kg, 40 s, 287 bar) are fed through line-19 for processing, and gas hydrocarbons are sent to washing 20, where they are washed out, and hydrocarbons C.-Cv are removed through line 21 from the process.
    /. P.
    the fresh water supplied by line 24 of the genus as a hydrogenating gas, n, is fed to the process via line 4.
    According to the invention, the solution is to provide the required pressure level in the internal tank of the reactor and the hot separator.
    (25 kg, 40 C, 285 bar). After removal, the IQ is maintained through the pipeline.
    Neither 9 kg of gas in tank 22 residual gas is compressed to 320 bar and recirculated at the start of the process.
    Example2, In the installation according to
    but FIG. 2 the coal slurry in the recirculated air pressure equalizes 15.
    Hydrocarbons in line 1 are brought to a pressure of about 320 bar by means of a high-pressure pump 2. Hydrogenated 1 ° C gas partially heated in the heat exchanger 3 under a pressure of 320 bar is supplied via line 4 to the coal suspension. A three-phase mixture consisting of a solid phase (coal, catalyst based on May 30, Y,), coal,
    20
    between the tanks connected to them.
    The proposed placement of the pipeline between the top of the hot separator 10 and the separator 17, i.e. indirectly on. the suction side of the compressor 23, due to the fact that during the hydrogenation of coal, the pressure loss between the reactors 8 and the separator 17 is relatively low (example 35
    hydrogens and hydrogenation gas, but 12 bar), so that without additional heating in heat exchanger 5 and heater 6, at the inlet of the reactor 430–460 0 the three-phase reaction mixture is fed through line 7 through hydrogenation reactors 8 and then fed to a hot separator 10 high pressure according to LIRSHI 9, where the bottom of the bottom (high-boiling hydrocarbons and solids) is withdrawn from the bottom through line 11, and the vapor-gas phase (excess hydrogenating gas, reaction gases and vaporous hydrocarbons). The vapor-gas phase is partially cooled (approximately up to) in heat exchangers 5 and 3, as a result of which some hydrocarbons are condensed. In separator 13, both phases are separated from each other and diverted via lines 14 and 15.
    The vapor-gas phase is cooled by means of the cooler 16 to almost ambient temperature (for example, up to 40 s), thereby condensing
    This means that sufficient and simultaneous equalization of pressure is established between the internal cavity and the annular space.
    30 won the reactor. In the case of the presence of a pipeline between the pressure side of the compressor 23 and the annular spaces of the reactors and the hot separator, this does not occur, as due to the heating of the three-phase mixture (when the coal is hydrogenated, the viscosity increases greatly due to the swelling of the coal) pressure (e.g.
    40 20 bar), which leads to the presence of overpressure in the annular space acting on the wall of the internal tank of the reactor. The indicated pressure drop values are x
    45 factors for normal operation installation.
    In emergency cases, pressure drops may occur in reactors (in the event of an emergency discharge
    hydrocarbon residue. Separation of ox 50 P hydrogenation of coal, for example, from the hydrocarbons from the residual vapor-gas phase, (hydrogenation gas, gaseous hydrocarbons,
    300 to about 130 bar in 5 min. Sudden increases in pressure at comparable intervals do not occur, so
    flue gases) are produced in separations, such as, for example, when the reactor is overheated
    Torus 17 on lines 18 and 19. At stage 55 P, emergency flushing 20 of residual gas and pressure release is promptly started. At that time, as in line 23, hydrocarbon gases are operated for normal operation (quasi-stationary (p.; - C 4), and gas from the tank 22 after the mode) by means of the proposed expansion to 320 bar at the interconnection of the connecting pipe
    fresh feed supplied through line 24 as a hydrogenation gas is supplied to the process via line 4.
    According to the invention, the solution is to ensure the required pressure in the internal tank of the reactors and the hot separator
    27 between the upper part of the separator 17 and the annular spaces of the reactors and the hot separator. Pipeline 27 is a connecting pipe.
    0
    between the tanks connected to them.
    The proposed placement of the pipeline between the top of the hot separator 10 and the separator 17, i.e. indirectly on. the suction side of the compressor 23, due to the fact that during the hydrogenation of coal, the pressure loss between the reactors 8 and the separator 17 is relatively low (example
    but 12 bar), so without the extra
    This means that sufficient and simultaneous equalization of pressure is established between the internal cavity and the annular space.
    out the reactor. In the case of the presence of a pipeline between the pressure side of the compressor 23 and the annular spaces of the reactors and the hot separator, this does not occur, as due to the heating of the three-phase mixture (when the coal is hydrogenated, the viscosity increases greatly due to the swelling of the coal) pressure (e.g.
    20 bar), which leads to the presence of overpressure in the annular space acting on the wall of the internal tank of the reactor. The indicated pressure drop values are x
    For normal operation, the installation works.
    In emergency cases, pressure drops may occur in reactors (in the event of an emergency discharge
    P hydrogenation of coal, for example, with
    300 to about 130 bar in 5 min. Sudden increases in pressure at comparable intervals do not occur, so
    Yes, a small pressure is maintained in the internal tank of the reactor, with a sharp decrease in pressure (for example, during an emergency discharge) a small excess pressure in the annulus acts on the internal tank of the reactor. Since this way does not occur one-sided
    high load on the internal reservoir, the internal tanks of the reactors and the hot separator can be made relatively thin walled.
    Installation. In FIG. 2, it works as follows.
    The suspension supplied to the process contains 100 kg of coal, 5 kg of catalyst based on iron oxide and 150 kg of recycled hydrocarbons and has a temperature of 170 ° C and a pressure of 320 bar,
    Hydrogenating gas (consisting of 95 kg of circulating gas and 15 kg of fresh hydrogen) is added to this suspension. After heating in apparatus 5 and 6, a mixture of coal slurry with gas with a temperature of 450 C and pressure, 302 bar is fed to the first reactor 8.
    In the hot separator, the reaction product is separated into a head product and a bottom product withdrawn from the process. The latter consists of 21 kg of solid phase (insoluble coal, catalyst, ash) and 92 kg of hydrocarbons at a temperature of 400 ° C and a pressure of 299 bar.
    The head product (460 ° C, 299 bar) is cooled in heat exchangers 5 and 3 and subjected to hot separation in the separator 13 at a temperature of 240 ° C and a pressure of 292 bar per vapor-gas phase and condensed hydrocarbons (79 kg), which in line 15 serves for recycling.
    The gas-vapor mixture is cooled in the heat exchanger 16 to approximately 40 ° C, the hydrocarbons condensed during this process (49 kg, 40 ° C, 287 bar.) Are fed through line 19 for processing, and the gas hydrocarbons are fed to washing 20, where they are washed out and discharged through 21 of the process hydrocarbons C, -0 (25 kg 40 ° C, 285 bar). After removing 9 kg



    gas in vessel 22 residual gas hedgehog-water 28 between the suction pipe is washed up to 320 bar and is recirculated to the house of compressor 23 and annular pro-process, II p and me 3,
    In the installation in accordance with FIG. 3, the coal suspension in the recirculating
    reactor and hot separator spaces. Pipeline 28 is connective and provides alignment
    Hydrocarbons in line 1 are brought to a pressure of about 320 bar by means of a high-pressure pump 2. The hydrogenation gas partially heated in the heat exchanger 3 under a pressure of 320 bar is supplied via line 4 to the coal slurry. A three-phase mixture consisting of a solid phase (coal, catalyst
    five
    Q
    0
    Q mash based
    30 wt.% Fe, jOg),
    hydrocarbons and a hydrogenating gas are heated in a heat exchanger 5 and heater 6 to a temperature at the inlet of the reactor 430–460 ° C. The three-phase reaction mixture is fed through line 7 through hydrogenation reactors 8 and then fed through line 9 to a hot high-pressure separator IO, where from the bottom, behind line 11, the bottom phase is withdrawn (high-boiling hydrocarbons and solids), and from the top of the line 12 is the vapor-gas phase (excess hydrogenating gas, reaction gases and vaporous hydrocarbons), 5 the vapor-gas phase is partially cooled (approximately up to 240 ° c) in heat bmennikah 5 and 3, whereby the corner portion condensed levodorodov, In separator 13 the two phases are separated from one another by lines 14 and 15,
    The vapor-gas phase is cooled to near ambient temperature (for example, before) by means of the cooler 16, thereby condensing the remainder of the hydrocarbons. The separation of the cooled hydrocarbons from the residual vapor-gas phase (hydrogenating gas, gaseous hydrocarbons, residual gases) is carried out in the separator 17 through lines 18 and 19. At the washing stage 20, the hydrocarbon gases (c.-C 4) are removed from the washing stage 20 After a pressure of 320 bar is brought to pressure from tank 22, a compressor 23 is added and fresh hydrogen supplied through line 24 is added as a hydrogenation gas to line 24,
    five
    0
    five
    According to the invention, the solution of the problem of providing the required pressure level in the internal tank of the reactor and the hot separator is carried out by means of pipelines.
    water 28 between the suction piping house of the compressor 23 and the annular pro-
    reactor and hot separator spaces. Pipeline 28 is connective and provides alignment
    51360589
    pressure build-up between connected
    im reservoirs.
    The proposed placement of the pipeline between the upper part of the hot separator 10 and the suction side of the compressor 23 is due to the fact that when hydrogen is hydrogenated, the pressure loss of the NIN between reactors 8 and separator 10 is relatively low (about 15 bar), so that without additional regulating means establish sufficient and simultaneous pressure equalization between the internal cavity and the annular space of the reactor. In the case of a pipeline between the pressure side of the compressor 23 and the annular spaces and reactors and a hot separator, this does not happen, as a result of; heating a three-phase mixture (the hydrogenation of coal greatly increases the viscosity due to swelling of the coal) there is a relatively sharp pressure drop (for example, 2D bar), which leads to the presence of overpressure in the annular space acting on the wall of the internal tank of the reactor. The specified values of the pressure drop are characteristic for the 1-normal mode of operation of the installation,
    In emergency cases, in reactors, abrupt pressure drops can occur (in the event of an emergency discharge during coal hydrogenation, for example, from 300 to about 130 bar in 5 minutes). Sharp higher pressures in a comparable interval: do not occur, because, for example, When the reactor is overheated, emergency pressure relief is switched on in a timely manner, while during normal operation (quasi-stationary mode), the proposed placement of the connecting pipe in the internal tank of the reactor maintains a small pressure with a sharp decrease Pressure (for example, in the event of an emergency discharge) has a slight overpressure in the annular space on the internal tank of the reactor. Since this does not result in a one-sided high load on the internal tank, the internal tanks of the reactors and the hot separator can be made relatively thin-walled.
    The installation of FIG. 3 works as follows.
    ten
    0
    five
    0
    five
    0
    0
    five
    0
    five
    The suspension supplied to the process contains 100 kg of coal, 5 kg of catalyst based on iron oxide and 150 gr of recycled hydrocarbons and has a temperature of 170 ° C and a pressure of 320 bar.
    Hydrogenating gas (consisting of 95 kg of circulating gas and 15 kg of fresh hydrogen) is added to this suspension. After heating in devices 5 and 6, a mixture of coal with gas with a temperature and pressure of 302 bar is supplied to the first reactor 8,
    In the hot separator, the reaction product is separated into a head product and a bottom product withdrawn from the process. The latter consists of 21 kg of the solid phase (insoluble coal, catalyst, ash) and 92 kg of hydrocarbons at a temperature of 400 ° C and a pressure of 299 bar.
    The head product (460 ° С, 299 bar) is cooled in heat exchangers 3 and 3 and subjected to hot separation in separator 13 at a temperature of 240 ° C and a pressure of 292 bar per vapor-gas phase and condensed hydrocarbons (79 kg), which are fed to line 15 recycling
     The steam-gas mixture is cooled in a heat exchanger 16 to approximately 40 ° C, the hydrocarbons condensed during this process (49 kg, 40 ° C, 287 bar) are fed, according to f- NII 19 for processing, and the gas hydrocarbons are fed to the washing 20 where they are washed out and discharged through line 21: hydrocarbons from the process (25 kg, 40 ° C, 285 bar). After removal of 9 kg of gas in the vessel 22, the residual gas is compressed to 320 bar and is recycled to the start of the process,
     Example 4 In the installation according to FIG. 4, the suspension of coal in recycled hydrocarbons in line 1 is brought to a pressure of about 320 bar by means of a high-pressure pump 2. The hydrogenation gas, partially heated in the exchanger 3, under a pressure of 320 bar is fed via a line 4 to the coal suspension. A three-phase mixture consisting of a solid phase (coal, catalyst based on 30 wt.% FeiOj), hydrocarbons and a hydrogenating gas is heated in a heat exchanger 5 and heater 6 to the temperature at the inlet of the reactor 430-460 ° C. The three-phase reaction mixture is fed through line 7 through the hydrogenation reactor 8
    and then supplied via line 9 to the high-pressure hot separator 10, where the bottom phase is withdrawn from the bottom along line 11 (high boiling hydrocarbons and solids), and from the top of the line 12 vapor gas phase 4 is stored (excess hydrogenating gas , reaction gases and vaporous hydrocarbons). The vapor-gas phase is partially cooled (approximately up to 240 s) in heat exchangers 5 and 3, as a result of which some hydrocarbons are condensed. In separator 13, both phases are separated from one another by lines 14 and 15,
    The vapor-gas phase is cooled to near ambient temperature (for example, to 40 ° C) by means of the cooler 16. thereby condensing the remainder of the hydrocarbons. The separation of the cooled hydrocarbons from the residual vapor – gas phase (hydrogenating gas, gaseous hydrocarbons, residual gases) is carried out in a separator 17 along lines 18 and 19. At the washing stage 20, hydrocarbon gases () are removed from line 21, and gas from the tank 22, after adjusting to a pressure of 320 bar using a compressor 23 and adding fresh hydrogen supplied through line 24 as a hydrogenating gas, it is fed to the process via
    According to the invention, the solution of the problem of providing the required pressure level in the internal tank of the reactors and the hot separator is carried out by means of a pipe 29 connected directly to the upper part of the separator 10,
    The proposed placement of the pipeline between the upper part of the hot separator 10 and the upper part of the first reactor, t, e, indirectly to the suction side of the compressor 23, allows the hydrogen loss of pressure between the reactors 8 and the separator 10 to be reduced to 1–2 bar), so that without additional regulating means establish a sufficient and simultaneous pressure equalization between the internal cavity and the annular space of the reactor. In the case of a pipeline between the pressure side of the compressor 23 and the annular spaces of the reactors and the hot separator, this does not occur, since
    due to the heating of the three-phase mixture (when the coal is hydrogenated, the viscosity increases greatly due to the swelling of the coal) a relatively large pressure drop occurs (for example, 20 bar), which leads to the presence of excess pressure in the annular space acting on the wall
    Q internal reactor tank. The indicated pressure drop values are characteristic for normal operation of the plant.
    In emergency situations in reactors
    5, abrupt pressure drops can occur (in the event of an emergency release during coal hydrogenation, for example, from 300 to about 130 bar in 5 minutes). . Sharp pressure increases compared
    0 myyh intervals do not occur, so
    as, for example, in case of overheating of the reactor, emergency pressure relief is promptly activated. While in normal operation (quasistadionary
    5 mode) by means of the proposed placement of the connecting pipe and in the internal tank of the reactor, a small pressure is maintained, with a sharp decrease in pressure (for example,
    0 measures in case of emergency discharge) a slight overpressure in the annular space acts on the internal tank of the reactor. Since in such a way one-sidedly high load on the inner tank does not occur, the inner tanks of the reactor and the hot separator are of the kind (at the same time, they can be made relatively thin-walled).
    0 Installation of this scheme works as follows.
    Supplied suspension contains 100 kg of a catalyst based on iron oxide and 150 kg
    5 recycled hydrocarbons and has a temperature of 170 ° C and a pressure of 320 bar,
    Hydrogenating gas (consisting of 95 kg of circulating gas and 15 kg of fresh hydrogen) is added to this suspension. After heating in devices 5 and 6, a mixture of coal slurry with gas with a temperature of 450 C and a pressure of 302 bar is fed to the first reactor 8.
    In the hot separator, the reaction product is separated into a head product and a bottom product withdrawn from the process. The latter consists of 21 kg of solid phase.
    five
    0
    five
    13
    (undissolved coal, catalyst, ash) and 92 kg of hydrocarbons at a temperature and pressure of 299 bar.
    The head product (, 299 bar) is cooled in heat exchangers 5 and 3 and subjected to hot separation in the steam generator 13 at a temperature of 240 ° C and a pressure of 292 bar per vapor-gas phase and condensed hydrocarbons (79 kg), which are fed via line 15 for processing.
    The gas-vapor mixture is cooled in the heat exchanger 16 to approximately 40 ° C. The hydrocarbons dented at the same time (49 kg, 287 bar) are fed through line 19 for processing, and the gas hydrocarbons are fed to the washing 20, where they are washed out and drained through 21 from the process of hydrocarbons (25 kg, 40 C, 285 bar). After removal of 9 kg of gas in the vessel 22, the residual gas is compressed to 320 bar and is recycled to the start of the process.
    Thus, in the proposed installation, the compensation medium in the annular cavity is not replaced, osmol-NIN is not observed, because high-boiling components do not enter the medium, which increases the reliability of the high pressure unit in combination with efficient pressure equalization through pipelines
    one







    14
    connected to the suction line of a circulating, cooling compressor.
    权利要求:
    Claims (1)
    [1]
    Formula invented and
    An apparatus for producing liquid products from coal, consisting of a reactor, a high-pressure hot separator
    pressure, pipelines, effluent, vapor – gas flow and ash flow from. hot separators, high-pressure intermediate separators fitted with steam-exhaust pipelines
    the call of the streams, the block of release of hydrogen-containing gas, supplied with a conduit for the withdrawal of hydrogen circulating hydrogen, a compressor, circulating hydrogen-containing gas,
    characterized in that, in order to increase the reliability of operation of high-pressure apparatuses, the reactor and the high-pressure hot separator are made in the form of two buildings.
    inserted one into the other with an annular cavity between them, filled with a medium under pressure, the annular cavities are connected to the pipeline, which includes the pipelines, the output -
    vapor – gas stream from a hot separator or from intermediate separators or hydrogen containing gas, from a hydrogen separation unit from the entrance to the compressor.
    fs / g /
    fig.g
    efjus3
    22
    f3
    2
    Editor M.Petrova
    Compiled by N. Kirillov
    Tehred M. Hodanich: Proofreader G. Reshetnik
    Order 6166/57
    Circulation 463 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, F-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, Projecto st., 4
    jieL
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    同族专利:
    公开号 | 公开日
    PL146013B1|1988-12-31|
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    EP0134894A2|1985-03-27|
    EP0134894B1|1988-09-14|
    DE3323885A1|1985-01-03|
    EP0134894A3|1986-06-04|
    US4555325A|1985-11-26|
    BR8403222A|1985-06-11|
    AU568859B2|1988-01-14|
    JPH0624621B2|1994-04-06|
    CA1231656A|1988-01-19|
    DE3473993D1|1988-10-20|
    PL248359A1|1985-04-24|
    AU2959384A|1985-01-24|
    ZA844752B|1985-05-29|
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    申请号 | 申请日 | 专利标题
    DE3323885A|DE3323885A1|1983-07-02|1983-07-02|METHOD FOR THE PROCESS ENGINEERING OF THERMAL AND PRESSURE-LOADED MULTI-PHASE REACTORS, SPECIFICALLY HYDRATING REACTORS IN THE SUMMING PHASE|
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