• 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:
    Oil shale containing relatively large quantities of alkaline carbonate minerals is retorted utilizing superheated water vapor at temperatures of from about 425 DEG C. to about 510 DEG C. Retorting with a sufficient carbon dioxide partial pressure effectively suppresses decomposition of the alkaline carbonates to obtain an environmentally acceptable retorted shale.
    公开号:SU1033006A3
    申请号:SU802890048
    申请日:1980-02-26
    公开日:1983-07-30
    发明作者:Дин Олред Виктор
    申请人:Маратон Ойл Компани (Фирма)；
    IPC主号:
    专利说明:

    00
    The invention relates to methods for obtaining organic materials from oil shale and can be used in the oil industry. A method for separating organic compounds from oil shale is known, including heating shale with steam to 25 510 ° C at a pressure of 7-103 kPa and the velocity of gaseous products 6 , 0-305 cm / s, removal of gaseous products obtained in the heating process, and the subsequent release of ti3 gaseous products of heating of hydrocarbons and carbon dioxide 111. Oil shale contains a large amount of rbonatov fishing alkali metal, e.g. magnesium carbonate and / or calcium carbonates. In the process of heating the shale with water vapor to 125-5 ° C, carbonates decompose, which comes with heat absorption, which leads to an increase in energy consumption for heating oil shale to secrete organic compounds The aim of the invention is to reduce energy costs by preventing carbonate decomposition in shale. This goal is achieved by the fact that according to the method of separating organic compounds from oil shale, including heating the shale in a retort with water vapor to 25-5 P (5 and pressure / -103 kPa and gaseous product velocity 10-305 cm / s, gas-discharge) obtained during the heating process and the subsequent release of hydrocarbons and carbon dioxide from the gaseous products, the heating is carried out in the presence of carbon dioxide. At the heating stage of the shale, carbon dioxide extracted from the gaseous heating products is supplied. The carbon dioxide is fed from the gaseous heating products to the upper and lower parts of the retor. The drawing shows an installation diagram for carrying out the proposed method. The method is as follows: The crushed and sieved combustible shale from the bunker 1 is fed to the closed bunker 2 where pressure kPa by flue gas supplied through the line}. 06 After reaching the required pressure and temperature in the hopper 2, the valve opens and the slate enters the heater 5, which is located between the closed a bunker 2 and a distillation column 6. Superheated steam is supplied to the preheater 5 through line 7 through valve 8 to heat the incoming oil shale to the water dew point at the operating distillation pressure. Water can be supplied to the preheater 5 through line 9 through valve 10. From the preheater 5, the slate enters the distillation column 6, to which superheated water is supplied through switchgear 11 from pipe 12. Upward moving superheated water vapor in countercurrent is in contact with combustible shale, which moves downward under the action of gravity. Superheated steam heats the oil shale to the temperature necessary for the pyrolysis of the organic components of the oil shale, at which shale oil, gases and solid residue are obtained. It is necessary that the heating temperature is in the range of + 50-85 ° C, preferably A50-i 70 C, pressure - in the range of 6.9-103 kPa. preferably 2 1-517 kPa, and the gas velocity is in the range of 10-508 cm / s, better. 10-305 cm / s, most preferably 25-203 cm / s. I From the preheater 5, partially condensed vapors and gases produced in the process of heating the shale are transferred from distillation column 6 via line 13 to heat exchanger Ik, where shale oil and steam are condensed, and then via line 15 to separator 16. Water vapor from heat exchanger 1 through line 17 is supplied to compressor 18, where it is compressed to a pressure equal to the pressure in the distillation column. Pressurized steam passes through the superheater 19, where its temperature is raised to, and through line 12 is fed to the distillation column 6. In the separator 16, non-condensed gases are separated from oil and water and through line 20 is fed to a separator 21 of carbon dioxide, which can constitute a suitable separator of the conventional type. The resulting gases contain a significant volume of carbon dioxide, for example volume. A suitable absorbing medium is introduced into the absorber 21, for example diethanolamine, which is in contact with the uncondensed product gases and selectively absorbs carbon dioxide from them. The remaining uncondensed bulk gases from the absorber 21 are fed through line 22 to the conventional treatment unit. The carbon dioxide enriched absorbing medium is transported from absorber 21 through line 23 to carbon dioxide trap 2k. . The trap 2 may be a conventional trap, for example a unit in which the solution is heated to a temperature sufficient to reduce the solubility of carbon dioxide in an absorbent medium and thus remove almost all. carbon dioxide from it. The absorbing medium from which carbon dioxide is released is recycled to the absorber 21 via line 25. The extracted carbon dioxide-containing gas, which is essentially carbon dioxide, is transported via line 2b. A substantial portion of the gas containing carbon dioxide is discharged through line 27 and introduced into the distillation column 6 directly above the quench zone of water in its lower part. Compressor 28 may be used to provide sufficient pressure of carbon dioxide-containing gas to enter it into the distillation column through lines 2b and 27. The introduction of carbon dioxide-containing gas into the upper part of the shale preheater 5 and near the lower end of the distillation column 6 does not only provide relatively uniform distribution of g of gas in the distillation column and Nodogrev body, but also serves as a barrier gas for the preheater and the distillation column, thereby minimizing the leakage of produced gas through the 3 | valve between the heater and the closed hopper and the lower end of the distillation column. Carbon dioxide has sufficient partial pressure to effectively prevent the decomposition of carbonates of alkali metals contained in combustible shales. 064 The oil obtained in the heating process is cooled to the water dew point by injecting water supplied through line 29 through switchgear 30. When contacted with water, hot oil vapor is generated, which passes to the top of the distillation column, cools the resulting shale oil and at the same time increasing the temperature in the distillation column. The processed shale is crushed using a roller crusher 31 in the presence of water supplied through line 32. To form a slurry suitable for transport by pumping, the slurry from tank 33 through pump 3 through line 35 is fed to a shale extractor. Example: Two identical cylindrical samples of combustible shale from the formation of the Zelena River, having a high content of calcium and dolomite, are heated in an atmosphere of H20 CA} and in atmosphere (B). The ratio between carbon dioxide and water vapor inside the retort is approximately 0.350, 7 moles of COP per mole of water vapor. Preferably from the amount of water vapor circulating through the retort. is C0. After that, the residual carbon of the oil shale OJ distilled is used with. Injecting air into the vapor gas. The samples are first weighed and then weighed continuously during distillation and oxidation by recording the heat balance at a temperature of about i482c. The results of these measurements are given; us 8 table. The relative difference in weight loss calculated in these measurements is the direct result of the decomposition of alkali metal carbonate. From a comparison of measurements A and B, it is clear that testing B in an atmosphere having a partial pressure of carbon dioxide leads to effective prevention of carbonate decomposition at low temperature. Thus, the proposed method effectively prevents the decomposition of alkaline meth. Carbonate during the distillation of combustible shale at using overheated
    water vapor at temperatures of approximately 25–510 ° C, which reduces energy consumption and also solves the problem of carbonate decomposition by introducing a significant portion of the distilled gas in the recycle to ensure sufficient partial carbon dioxide pressure, while the cost of introducing the necessary carbon dioxide is minimal.
    Reference level
    权利要求:
    Claims (3)
    [1]
    1. METHOD FOR ISOLATING ORGANIC COMPOUNDS FROM OIL SHEETS, including heating the shale in the retort with water vapor to 425 “510 ° С at a pressure of 7 ~ 1034 kPa and velocity, gaseous products 10-305 cm / s, removal of gaseous products obtained during heating, and the subsequent separation from the gaseous products of hydrocarbons and carbon dioxide, characterized in that, in order to reduce energy consumption by preventing decomposition of carbonates in the shale, heating is carried out in the presence of carbon dioxide.
    [2]
    2. The method according to claim 1, characterized in that at the stage of heating the shale serves carbon dioxide isolated from gaseous heating products *
    [3]
    3. The method according to claim 2, characterized in that the carbon dioxide extracted from the gaseous products of heating is fed into the upper and lower parts of the retort.
    Vhm ί
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    同族专利:
    公开号 | 公开日
    US4243511A|1981-01-06|
    引用文献:
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    US4404083A|1981-08-17|1983-09-13|Standard Oil Company|Fluid bed retorting process and system|
    EP0097163A1|1981-12-24|1984-01-04|Commonwealth Scientific And Industrial Research Organisation|Process for the recovery of oil from shale|
    US4449994A|1982-01-15|1984-05-22|Air Products And Chemicals, Inc.|Low energy process for separating carbon dioxide and acid gases from a carbonaceous off-gas|
    US4502942A|1983-04-25|1985-03-05|The University Of Akron|Enhanced oil recovery from western United States type oil shale using carbon dioxide retorting technique|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/023,852|US4243511A|1979-03-26|1979-03-26|Process for suppressing carbonate decomposition in vapor phase water retorting|
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