• 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:
    Hydrocarbon-bearing substrate particles are pre-heated by heating the same with a solid heat-bearing medium by indirect counter-current flow using a series of heat transfer loops each containing a circulating heat transfer medium chosen such that the whole series permits a staged rise in temperature of the substrate particles and a staged drop in temperature of the solid heat-bearing medium. Preferably the heat transfer fluid in the loops circulates between the substrate and the hot spent substrate by means of the so-called thermosyphon effect. An apparatus for carrying out the method is described.
    公开号:SU1366063A3
    申请号:SU823424749
    申请日:1982-04-20
    公开日:1988-01-07
    发明作者:Khejnz Voetter；Khubrekht Korneliz Anton Meurs；Richard Chalz Darton；Radzhamani Krishna
    申请人:Shell Int Research；
    IPC主号:
    专利说明:

    The invention relates to a method for producing hydrocarbons from oil shale and allows to increase the yield of hydrocarbons. The shale is heated by passing it through several (from 2 to 10) zones. Hot waste shale is served in one or more zones in the direction perpendicular to the flow of inert gas entering the zones at a speed of 0.1-2.0 m / s. 8 tab. 7 il.
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    The invention relates to a method for producing hydrocarbons from oil shale.
    The purpose of the invention is to increase the yield of hydrocarbons "
    Fig "1 shows a diagram of the installation for the extraction of hydrocarbons from oil shale for the implementation of the proposed method; Fig.2 device (rotor) for the distillation of the slate; FIG. 3 shows a variant of the device for retort distillation of this method comprising a vessel with five compartments of retort distillation, the cross-sectional area of which and the height of each compartment respectively increase and decrease relative to the preceding compartment; figure 4 - the same .View from above; figure 5 is a variant of the device retort distillation, containing five compartments of the retort distillation, located in a row of three vessels, the second and third of which contain two compartments of the retort distillation; on Fig.6zona heating; Fig. 7 shows the heat transfer circuit of the heating zone "
    The preheating zone (FIG. 1) includes a row 1 of compartments for preheating fresh slate and a row 2 of compartments for cooling the hot spent substrate. Shale particles enter the device at ambient temperature through line 3 to row 1, containing five separate, but interconnected, compartments 4–8, in which the shale particles are maintained in a fluidized bed by supplying air through the supply pipe 9. Each compartment 4–8 Heated separately due to the transfer of heat from the coolant flowing through the heat exchange circuits 10-14, respectively. The heat exchange medium in each circuit is heated due to contact with the hot spent substrate, which is passed from the combustion zone through the supply line 15 to the row 2 of the hot spent shale. This series of spent hot slate also contains a series of five compartments 16–20, each of which contains the spent slate in a fluidized bed by supplying air from pipe 9. ' The direction of flow of hot waste shale through row 2 is anti-counterbolt to the direction of flow of fresh
    shale flowing through row 1, excluding the direct contact of fresh and spent shale, the temperature of which gradually rises. Cooled waste ate-. It is discharged through line 21. Water vapor and any other volatile materials released during preheating are discharged through line 22.
    • After passing through row 1, the heated slate is passed into a stripping column 23, in which all the air present in the slate,. 'in contact with the steam supplied through line 24. From the stripping column 23 the shale passes into the zone of retort' distillation. The vessel retort distillation (figure 2) contains five compartments (or zones). 25-29, each of which is provided with lower inlet openings 30-34, through which steam passes through line 35. The heated slate enters compartment 25 through inlet 36, and subsequently passes into other compartments through system 37-40 of partitions or overflows. In each of the compartments there is a distributor 41-45 to ensure uniform flow of steam to the fluidized shale particles. Each compartment contains a-. individual upper inlets ‘46-50 for passing hot exhaust shale fed through line 51 from the combustion zone to the fluidized bed of shale particles. Hydrocarbons released from shale particles, along with steam from each zone, pass through cyclone 52-57 to the product discharge line (not shown) · From the compartment 26, the shale particles pass through the overflow 58, through the Stripping column 59 to remove traces of the product, and from there to outlet 60.
    The device for retort distillation (fig. 3) contains five compartments or zones of retort distillation 25-29, and the cross-sectional area of each subsequent compartment is smaller, and the height of each subsequent compartment is larger than the area and height of the previous compartment.
    The heated slate enters compartment 25 through inlet 36 and
    consistently passes into the following
    compartments through the system 37-40 partitions or overflows (figure 2), Ugdevodo1366063
    four
    the genera released from the shale particles, together with the steam from each compartment, are passed through cyclones 5257 to the product in-line 61.
    From the compartment 29, shale particles pass through an outlet 62 to a stripping column (not shown) in order to remove the last traces of the product.
    A possible variant of the device for retort distillation (figure 5), containing five compartments or zones of retort distillation in a row of three separate vessels with widened upper parts, in which cyclones are installed. The second and third vessels are each divided into two compartments, respectively, by partitions 38 and 40.
    The first compartment of the retort distillation 25 has the largest cross-sectional area and the smallest height, while the second vessel contains two compartments 26 and 27 of the retort distillation with the same average cross-sectional area, and the height of both compartments is larger and the cross-sectional area is smaller in comparison with the first compartment 25 retort distillation.
    The third vessel contains two compartments 28 and 29 of the retort distillation, the heights of which are greater than the heights of the compartments 26 and 27 of the retort distillation in the second vessel, and the average cross-sectional area less than the average cross-sectional areas of the compartments of the retort distillation in the second vessel.
    All three vessels are interconnected by means of pipes 63 and 64.
    The heated slate enters compartment 25 through inlet 36 and passes into the second vessel, into its compartment 26 through pipe 63, and then through overflow 38 into the compartment 27, from which flows into the third vessel through pipe 9, into compartment 28 and then through overflow 40 into compartment 29 and, finally, through outlet 62 passes into a stripping column (not shown) to remove traces of the product. Stripping gas is fed through the inlets, and is evenly distributed in the compartments of the retort distillation through distributors. Hydrocarbons released from shale particles, along with the stripping gas, are passed through cyclones to the product in-line 61.
    The coke-bearing waste shale is then burned in the combustion zone. The slate particles from the stripping column 59 are passed upward by the flow
    $ air (figure 1), entering through line 65, through a vertical burner 66, where coke is partially burned, and from it into chamber 67 of combustion of the fluidized bed of the fluidized layer, in which the burning is completed. Hot spent shale is sent from the combustion chamber 67 in two streams. One stream is subjected to steam distillation through supply line 68, and passed through line 51 to the zone of retort distillation. The other stream is passed through the second cooling system 69 and the line 15 in a row 2 of the exhausted slate of the additional heating zone. Hot flue gases are used to generate steam in convection. battery and to heat the air when burning.
    On the heating circuit (Fig.6) row
    25 fresh slate is served in six separate compartments or zones, sequentially located 70-75, and a number of hot spent slate consists of seven separate compartments or zones
    30 76-82. Fresh slate is passed through line 83 to six consecutive compartments. Hot waste shale is passed through line 84 successively to compartments 76-82 and maintained in a fluidized bed state in each compartment by means of air supplied through line 85. Air from the compartments. 76 and 77 are passed into cyclone 86 and along line 87 as
    Drilling fluid for shale in the third row of fresh shale. Similarly, the air from the bays 78-82 is passed through a cyclone 88 and through line 89 as a fluidizing gas for shale.
    45 in the compartment 72 rows of fresh slate. The slate in compartment 70 is maintained in a fluidized state by fresh air supplied through line 90, and the slate in compartments
    5 θ 73, 72 and 75 are liquefied by steam supplied via line 91. Steam from compartments 73, 74 and 75, together with the water released from the shale, is passed into a cyclone 92, with one stream
    55 re-compress in compressor 93
    and return to line 91. Another stream is passed to the condenser (not
    shown). The resulting water
    can be used for cooling.
    five
    6
    The transfer of heat from the hot waste base to the fresh base is carried out by means of heat transfer circuits 94-100. The compartments 70 and 76 are connected by contour 94, the compartments 71 and 77 by contour '95, the compartments 72 and 78 by contour 96, compartments 74 and 81 by contour 99, and the compartments 75 and 82 by contour 100. The row 73 the fresh slate is associated with two compartments 79 and 80 of a row of hot spent slate, respectively, by contours 97 and 98.
    The cooled waste slate is discharged along line 101. An embodiment of the heat transfer circuit based on the thermosyphon effect is possible (FIG. 7). Compartment 102 of the row of fresh shale is located above compartment 103 of the row of fresh slate. Heat transfer medium in liquid state passes from vessel 104 to compartment 103, where it evaporates due to heat transfer from the hot spent shale. Steam rises through the top of the vessel.
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    104 into compartment 102, where it is re-condensed due to heat transfer to fresh slate.
    И p and me R 1. Method (Fig.])
    five
    carry out continuously in the specified conditions. Each zone of the retort distillation has the same cross-sectional area and height.
    10 The initial composition of the slate, wt.%: Water 8; organic material 20.0; mineral substances 72.0, with a maximum diameter of 2 mm.
    Heating mode: fresh feed
    15 shale 58 kg / s; the initial temperature of shale particles is 25 ° C; the final temperature of the shale particles is 250 ° C.
    The mode of retort distillation: temperature of hot spent shale 700 ° С; feed rate of preheated dry shale 53 kg / s; steam flow rate of 0.5 n / s (at the upper part of the fluidized bed).
    25 Table 1 presents the distribution of steam, temperature and waste slate by zones.
    Table 1
    —— -------------- -------——— ——Η -------: ---— - ~ - —-- Zone Squarecross section Heightzones,m amountused Temperature, 0 Add hot waste n, m !ra, kg / s slate, kg / s 25 five 3.4 0.40 450 50 26 five 3.4 0.25 480 22 27 - five 3.4 0.59 480 2.5 28 five 3.4 0.74 480 1.1 29 five 3.4 0.82 480 0.5
    The total amount of steam used is 2.9 kg / s, the total number of rivers is -. hydrocarbons 7 kg / s.
    Combustion mode: supply to the vertical burner 122.1 kg / s, heat removed from the combustion chamber of the fluidized bed to maintain a temperature of 700 ° C 36 MW.
    Example 2. The process of Example 1 is repeated, and at least some zones have an area of 45 1
    the river section is smaller than the cross-sectional area of the previous zones. The heights of the zones are the same. And in this case, steam is injected to maintain the velocity of the flow in the upper part of the fluidized bed in each zone at a level of 0.5 m / s.
    The mode of retort distillation.
    Table 2 presents the distribution
    steam, temperature and exhaust
    of shale by zones.
    7
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    table 2
    Zone Square Height amount Tempera- Add transverse zones, using tour, ° C hot from th section m my couple, worked m 2kg / s slate, kg / s —---- ----------one ----: - -----— "and .—--——. “. and ------------ 25 five 3.4 0.40 450 50 26 five .3,4 0.25 482 22 27 3 3.4 0.25 482 2.0 28 2 3.4 0.25 482 0.9 29 1.8 3.4 0.25 482 0.6 -. G. - --— - - „---— g , ----
    The total amount of steam supplied is 1.4 kg / s, the total amount of hydrocarbons recovered is 6.4 kg / s.
    Example The method of example 1 is repeated with the difference that both the heights and the cross-sectional areas of some zones differ from the heights and cross-sectional areas of the previous zones. Ive
    In this case, steam is injected to maintain the flow rate in the upper part of the fluidized bed of each zone at a level of 0.5 m / s.
    . Retort distillation zone.
    Table 3 shows the distribution of steam, temperature and waste shale by zones.
    Table 3
    Zone Cross-sectional area, m 2 —————— Temperature, ° С Adding hot spent shale, kg / s Heightzones,m amountsteam used, kg / s 25 five 3.4 0.40 450 50 26 five 3.4 0.25 482 22 27 3 5.7 0.25 482 2.5 28 2 8.5 0.25 482 1.1 29 1.8 9.4 0.25 482 0.5
    The total amount of steam supplied is 1.4 kg / s, the total amount of recoverable hydrocarbons is 7 kg / s.
    Example4. The described heating zone (FIG. 5) operates continuously. The fresh oil shale supplied through line 83 is the same as in example 1, both in terms of composition and particle diameter. The heated particles of the oil shale leave the preheating zone through a line at a temperature of about 250 ° C. Hot spent shale at a temperature of about 700 ° C is injected through line 84 and passed a countercurrent to fresh combustible shale through a heating zone.
    It leaves the above-mentioned heating zone at a temperature reduced
    50 to about 80 ° C, through line 101.
    Hot spent slate is obtained from the fluidized bed burning chamber, in which the coke-carrying shale is burned with air as described for
    zones in FIG.
    Row of fresh slate: supply of slate 5.8 kg / s; initial temperature
    25 ° C.
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    Table A shows the temperature distribution by zones (compartments).
    Row of hot spent shale: shale feed 42 kg / s; initial temperature is 700 ° C.
    Table4
    Compartment | Temperature, C . 74 40 75 55 76 85 77  105 78 150 79 250 Table 5 presents the distribution temperature in zones (compartments). That blitz and 5. Compartment Temperature, ° С 87 566 86 461. 85 327 84 197 83 138 82 109 81 80
    Heat transfer circuits,
    Table 6 presents the temperature distribution, working pressure in 5 zones (compartments).
    Table
    Circuit Wednesday Workingtemperature, ° С Workingpressurebar 99 Methanol 65 .1,0 100 82 1.8 101 Water 112 1.5 102 - υ - 150 5.0 103 216 22 '104 300 90
    Example 5. The method of example 1 was reproduced, but with a decrease in the velocity of the gas leaving the surface of the layer to 0.1 m / s "
    Table 7 presents the distribution of steam, temperatures and waste
    ΊΟ
    shale by zones.
    Table 7
    ~ ——1 η ——— x —— η ———— - Mr. —————— η Zone Area- Height amount Tempera- Adding peppers zones, m is using tour, ° C burnable section, m 5bath whose reflection pair, kg / s bobby slate, kg / s - ------—--------- ------- ————- 25 25 0.7 0.38 450 50 26 25 0.7 0.24 480 22 27 25 0.7 0.56 480 2.5 28 25 0.7 0.7 480 1.1 29 25 0.7 0.77 480 0.5
    The total amount of steam added is 2.65 kg / s, the total amount of hydrocarbons produced is 7 kg / s.
    И p and measure 6. The method of example 1 was reproduced, but with an increase in the velocity of the gas leaving the surface of the layer to 2 m / s.
    Retort distillation zone.
    55 Table 8 shows the distribution of steam, temperatures and waste shale by zones.
    eleven
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    Table 8
    Zone Cross-sectional area, m Heightzones,m ' Amount of steam used, kg / s Temperature, ° С Add hot otrabotan ate ats, kg / s 25 1, 25 13.6 0.47 450 50 26 1.25 13.6 0.3 480 22 27 ' 1.25 13.6 0.7 480 2.6 28 1.25 13.6 0.88 480 1.2 29 1.25 13.6 0.97 480 0.6
    The total amount of steam supplied is 3.32 kg / s, the total amount of hydrocarbons produced is 7 kg / s. In the case when the velocity of the gas discharged from the surface of the layer is 1 m / s, the results are similar to the results at a speed of 0.5 m / s (example 1). The yield of hydrocarbons is also equal to 7 kg / s.
    Zones can be a series of separate, interconnected vessels or horizontal compartments, formed with the help of screens or overflows in one vessel of the appropriate form. The number of zones can be from 2 to 10.
    The residence time of the base in each zone may be the same or different in the range of 1-10 minutes. The diameter of the base supplied to the process, 0.5-5 mm. The cross-sectional area of the zones of retort distillation 0,752
    AO m, height varies within
    1.5-15 m.
    权利要求:
    Claims (2)
    [1]
    Claim
    [2]
    2θ A method of producing hydrocarbons from oil shale, which includes heating a shale with a particle size of up to 5 mm in a fluidized bed to a temperature of the order of 400 ° C hot ^ worked
    25th shale temperature of about 700 ° C, the flow into the layer from the bottom up to the inert oxygen-free gas, which is vapor / recirculated gas produced in
    30 process, removal of hydrocarbons produced with an inert gas, removal from a layer of spent oil shale, heating it by burning in a separate stage and feeding to the stage of heating shale, characterized in that, in order to increase the yield of hydrocarbons, the shale is heated by passing it through several zones in which hot waste shale is fed to one or several of these zones, the flow of inert gas is fed at a speed of 0.12 m / s, and the flow of shale particles is fed in the transverse direction relative to the gas flow.
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    同族专利:
    公开号 | 公开日
    NZ200354A|1985-07-31|
    FR2504548A1|1982-10-29|
    TR21195A|1983-12-08|
    LU84098A1|1983-04-13|
    US4419215A|1983-12-06|
    MA19455A1|1982-12-31|
    AU543593B2|1985-04-26|
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    SE8202468L|1982-10-23|
    AU8284282A|1982-10-28|
    BE892912A|1982-10-20|
    EG15722A|1986-06-30|
    DE3214616A1|1982-12-30|
    ZA822675B|1983-02-23|
    SE448999B|1987-03-30|
    ATA153582A|1983-12-15|
    AT375384B|1984-07-25|
    CA1189811A|1985-07-02|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2285276A|1939-11-24|1942-06-02|Standard Oil Dev Co|Shale oil distillation|
    US2581041A|1947-11-14|1952-01-01|Standard Oil Dev Co|Utilization of heat of finely divided solids|
    US2697688A|1949-11-30|1954-12-21|Standard Oil Dev Co|Distillation of oil-bearing minerals|
    SE307931B|1962-06-12|1969-01-27|Oil Shale Corp|
    DE1909263C3|1969-02-25|1974-04-25|Metallgesellschaft Ag, 6000 Frankfurt|Method and device for the smoldering of fine-grained bituminous substances that form a powdery smoldering residue|
    US3929615A|1973-06-01|1975-12-30|American Gas Ass|Production of hydrocarbon gases from oil shale|
    US4052293A|1975-10-10|1977-10-04|Cryo-Maid Inc.|Method and apparatus for extracting oil from hydrocarbonaceous solid material|
    US4088562A|1975-11-19|1978-05-09|Twenty Farms, Inc.|Method and apparatus for processing oil shale|
    US4210491A|1976-11-01|1980-07-01|Tosco Corporation|Method and apparatus for retorting a substance containing organic matter|
    US4110192A|1976-11-30|1978-08-29|Gulf Research & Development Company|Process for liquefying coal employing a vented dissolver|
    SE427578B|1978-06-21|1983-04-18|Stal Laval Turbin Ab|FUEL DRYING PLANT|
    US4260371A|1979-07-20|1981-04-07|Shale Oil Science & Systems, Inc.|Modular heat exchange apparatus|US4464247A|1983-10-13|1984-08-07|Standard Oil Company |Horizontal fluid bed retorting process|
    GB8501921D0|1985-01-25|1985-02-27|Shell Int Research|Supply of hot solid particles to retorting vessel|
    US5196260A|1988-11-19|1993-03-23|Ciba-Geigy Corporation|Process for the treatment of fibrous materials with modified organopolysiloxanes and the materials|
    US20030070317A1|2001-10-15|2003-04-17|Anderson George E.|Apparatus and method for removing solvent from particulate|
    KR20110051248A|2008-08-12|2011-05-17|슈빙 바이오셋|Closed loop drying system and method|
    US8262866B2|2009-04-09|2012-09-11|General Synfuels International, Inc.|Apparatus for the recovery of hydrocarbonaceous and additional products from oil shale and sands via multi-stage condensation|
    GB201406538D0|2014-04-11|2014-05-28|Thermtech Holding As|Method of treating a material|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB8112490|1981-04-22|
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