• 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 residue or residue fraction left behind during vacuum distillation in a crude oil refinery is further processed, in that it undergoes thin-film short-path distillation at a higher temperature and under a fine vacuum. Raising the temperature leads to a rise in the feed rate and to an improvement in the distillate/residue ratio.
    公开号:SU1757443A3
    申请号:SU874202933
    申请日:1987-07-21
    公开日:1992-08-23
    发明作者:Каппенбергер Петер
    申请人:Бусс Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for processing the residue remaining after vacuum distillation in an oil refinery.
    After the last fractional distillation of oil at a refinery in a vacuum, the distillation residue contains those substances that do not evaporate to about 550 ° C (normal pressure). This distillation residue corresponds in general case to 25% of the crude oil loading. further processing can be carried out in practice by treating with solvents, for example, by deasphalting with propane. Due to this, the residue is divided into the first fraction containing solvent-soluble lubricating oils and waxes and a second fraction containing solvent-insoluble asphalts asphaltenes, etc. This results in a larger amount of the second fraction From the first fraction obtained by dissolving the first fraction, valuable non-flammable substances can be obtained, such as lubricating oils and waxes, or this fraction can be fed to the cracking unit to produce low boilers of products. The second fraction insoluble in the solvent or the precipitate can be used either for the production of bitumen or for months e as fuel for an oil refinery, or after admixing the lighter fraction to liquefaction, as
    N cl
    ,
    s
    СО CO
     WITH
    heavier fuel outside the refinery, for example for power plants,
    The processing of the residue by vacuum distillation with a solvent has various disadvantages and limitations. The solvent-insoluble, insoluble, low-value fraction containing asphalt often corresponds to more than half of the vacuum distillation residue, which in heavy grades of natural oil can be 40% or more of the amount of oil. This kind of large dollars exceeds the needs of the refinery fuel. With the second possibility of using the insoluble fraction, in the manufacture of bitumen, problems also arise, since asphaltenes and asphalts existing in natural colloidal oil and asphalts precipitate. However, the complete re-dispersion required for the production of Oithum is often no longer possible, so that a low-value product is obtained.
    In addition, as a result of treating the residue with a solvent, lubricating oils and waxes do not completely dissolve into the solution, on the contrary, high molecular weight components are transferred into the solution and are introduced into the first fraction, which is harmful to the final products then obtained, for example, leads to enhanced coking of the lubricating oils obtained.
    In addition, the use of a low boiling solvent requires special security measures, in particular, expensive equipment. Recovery of the solvent requires high energy costs and, due to the high solvent / residue ratio, is expensive.
    There is a method of molecular distillation of the remainder of an oil refinery, in which both the evaporation pressure and the temperature of the condensation surfaces are reduced. In order to improve the energy balance, the residue of vacuum distillation without any supply of energy is supplied for molecular distillation, so that the heat of evaporation of the charge, which has the temperature of the residue of vacuum distillation, is removed, which inevitably leads to cooling and, consequently, lower temperatures for molecules continuous distillation than with the aforementioned vacuum.
    There is a method of processing the residue of vacuum distillation at a refinery using molecular
    distillation.
    Distillation
    performed under vacuum from 1-10
    -2


    up to 50 mbar, feeding the raw material in the form of a thin film onto the evaporation surface. Turbulence is imparted to the film by mechanical means, such as brushes, to clean 5 bodies. Heat from the vacuum distillation preceding the molecular distillation is used for evaporation, so that the molecular distillation is carried out at a lower temperature than the preceding vacuum distillation.
    As a disadvantage of the method, it is possible to note the formation of a large amount of a low-value residue at molecular distillation and an insufficient amount of vitamin 15. When refining Middle Eastern oil, which is a valuable product with a high content of distillable components, 17% of the residue is formed. In addition, in a known way there is an indication of
    20 the need to suppress decomposition reactions, i.e. The process should be carried out only when the temperatures are permissible from the product point of view, i.e. keep the temperature low enough to prevent product decomposition and do not form deposits on the evaporator surface that prevent heat transfer.
    The aim of the invention is to increase the yield of the distillate, as well as to increase the efficiency of the process by increasing the feed rate, due to the fact that a smaller amount of high viscosity residue is formed, which, due to its low
    35 flow rate reduces feed rate.
    Thus, due to the formation of a smaller amount of material that slows down the rate of nutrition, it increases.
    40 The goal is achieved by the method of processing the residue of vacuum distillation at a refinery by thin-layer molecular distillation under vacuum conditions at a constant residual pressure of (3.5–5) mbar when the material to be distilled is distilled to the evaporation surface in the form of a film, which is attached a turbo-blnostnost brush cleaner with a separate output of the resulting distillate and a concentrated
    50 residues, the evaporation surface being heated by countercurrently supplying the heat carrier to a temperature that is 44-143 ° C higher than the temperature that the remainder of the vacuum pumping has.
    55 It is preferable to carry out the process so that the evaporation surface temperature is above 350 ° C.
    It was unexpectedly discovered that due to the increase in energy costs
    the cost-effectiveness of thin-layer molecular distillation of the residue of vacuum distillation increases significantly, i. e. that the deteriorating energy balance gives an economic improvement. The increase in energy costs occurs in accordance with the invention as a result of an increase in the temperature of molecular distillation compared with the temperature of the residue of vacuum distillation.
    In accordance with the extraction method of the prior art, the separation was carried out using a non-polar solvent based on polarity, i.e. chemical structure of substances. Using the known methods of molecular distillation, the separation of the residue of vacuum distillation is carried out on the basis of the boiling point of the existing substances. In accordance with the invention, due to the high temperature, valuable products which, in accordance with the prior art, would remain in a less valuable residue, are obtained in the form of a distillate. Therefore, in accordance with the invention, not only a quantitative advantage is achieved due to a larger quantity of valuable product, but also a different kind of composition of fractions is obtained and due to this other qualitative advantages. More important than an improvement in the distillate / residue ratio, is that, due to the higher temperature, the loading rate per unit time and evaporation surface can be increased several times. Due to this, the efficiency of the method is extremely improved.
    The difference of the so-called C / H-ratios, i.e. the ratio of carbon and hydrogen between the distillate and the residue is greatly increased by the method in accordance with the invention
    In addition, in accordance with the invention, a sharp reduction in processing time is provided with a very small variation, i.e. greater uniformity is ensured.
    A higher temperature allows for simultaneous removal without any problems of residue enriched with high-molecular substances.
    The lubricating oils obtained in accordance with the invention can be used without additives in the same manner as lubricating oils, which are prepared according to conventional vacuum distillation methods, and brought to the desired viscosity with the aid of expensive additives. In addition, the distillate is practically free of metal-containing components, as a result of which there is no problem in cracking with the base of impurity-sensitive catalysts in order to obtain low-grade materials. In addition, in accordance with the invention, polyaromatic substances remain in the residue, which additionally improves the quality of the distillate and stabilizes the colloidal asphaltenes in the residue.
    In this case, as compared with the installation of machinery, not only does the amount of asphalt-containing fraction decrease, i.e. of the residue of thin-layer molecular distillation, so that its full use as a fuel is possible.
    5, but it also changes qualitatively due to the fact that it can be immediately dispersed in the production of bitumen. This property can, among other things, be related to the higher content of polar components. In addition, when processing varieties of natural oil with a high content of wax, the residue is practically free of wax. Thin layer molecular distillation
    5 or its instrumentation in the technology of production processes is known and was used mainly to obtain improved cleaning of heat and steam substances to avoid them.
    0 thermal decomposition. In contrast, in accordance with the invention, thermal decomposition is even desirable, since thanks to this more valuable distillate is obtained, and possibly in a minor
    5 as long as the vacuum is maintained.
    Thanks to the method according to the invention, the last distillation residue at the refinery, which boils
    0 at about 550 ° C (at normal pressure), distillation is available with quantitative and qualitative advantages. In this case, products of a new composition with partially new properties are obtained.
    Subsequently, in accordance with the invention, of heavy varieties of natural oil, which have about 50% or more of the vacuum distillation residue and therefore
    0 commercially acceptable points of view, distillates in quantity can be obtained, as in the distillation of conventional varieties of natural oil, so that they are now also suitable for use.
    5 The method according to the invention can be implemented using known devices for thin-layer molecular distillation. These devices are located after the last stage.
    vacuum distillation, oil refinery. The temperatures at the thin-layer molecular distillation are higher, and the pressure is lower by about a factor of up to 1СГ3 than at the preceding vacuum distillation. For the intended vacuum, in which a large volume of vapor is formed, the evaporation and condensation surfaces should as close as possible to each other. In general, this is achieved due to coaxial evaporation and condensation zones. Preferred are vertically arranged evaporation surfaces and condensation surfaces. The loaded material is uniformly distributed over the upper part of the heating surface and transferred to a turbulent state, which is maintained until the material under its own weight of the sheet leaves the heating surface and moves downwards. Due to this, the material heated over the entire heating surface immediately flows to the surface of the liquid, and the low boiling fraction is evaporated.
    Several units for thin-layer molecular distillation can be arranged in series or in parallel.
    Example 1. Non-distillable to a temperature of 530 ° C (the indication of the temperature is related to normal pressure) the residue from the vacuum distillation stage is fed to a thin-layer molecular distillation unit. The operating parameters were as follows: a vacuum residue temperature of 272 ° C, a loading rate of 13.1 kg / h, a pressure of 4.5 mbar, a heating temperature of 351 ° C. the cooling temperature is 103 ° C, the distillation rate is 6.5 kg / h, the fraction of distillate is 40.6 wt.%.
    The residue is continuously fed by means of a pump to the inlet of the evaporator and distributed evenly along the inner surface by means of a distribution ring. Then, the rotor brushes of the cleaner, which move along the evaporation surface, capture the material and feed the turbulent film to the heating surface. A wave front (frontal wave) is formed in front of the rotor brushes.
    The throughput and the amount of distillate were significantly increased due to an increase in the heating temperature, which can be primarily explained by the evaporation of high molecular weight substances.
    Tables 1 and 2 compare the data of other examples. Tests in examples 1-5
    was carried out, taking into account the increase in the share of distillate, and in examples 6-10 - taking into account the increase in download speed.
    Table 2 presents the results.
    analysis for Example 5. which is considered indicative.
    When conducting these tests, you dreamed that you were immediately able to achieve speed
    0 passes 225 kg / h-m, which guarantees the economic use in the scale of the refinery.
    Figure 1 shows a simplified process flow diagram for the distillation of an oil refinery; FIG. 2 shows an installation for implementing the method.
    According to Fig. 1, natural quality oil 1 of medium quality is fed to a distillation unit 2 operating at normal pressure. After evaporation, approximately 50% of the original natural oil is removed from the installation as separated fractions 3,4,5. The residue 6 is fed to another vacuum-operated distillation unit 7, from which approximately 25% of the natural oil is withdrawn as fractions 8, 9 and 11. Then, the non-distilled residue 12 is fed for further processing in accordance with the invention, i.e. .
    0 for thin-layer molecular distillation 13. This produces a distillate of 14 and a distillable residue of 15. A distillate of 14 can be fed or to a cracking unit to produce a low mole fraction of starchy products
    5 or separated further into lubricating oil and wax. The residue 15 is used as fuel in a refinery or is processed into tar.
    The installation shown in FIG. 2 is for
    0 implementation of the method has a loading tank 21 with a stirrer 22. The position M represents the motors related to individual devices. Loading tank 21 with an equipped
    A feed pump 23 of the pipeline 24 is connected to the molecular evaporator 25, which in turn is connected to the residue collector 26 and the distillate collector 27. Next to the molecular evaporator 25
    0, two low-temperature traps 28 and 29, one after the other, are connected. A rotor-slot vacuum pump 31 is located between the low-temperature traps 28 and 29, after the second low-temperature
    5, a rotor-slit vacuum pump 32 is located, and then a lamellar vacuum pump 33 is installed.
    The residue of the vacuum distillation stage fed to the loading tank 21 by means of the pump 23 is fed through a pipeline
    24 into molecular evaporator 25 where it is separated into distillate and residue by evaporation, and the separated fractions are trapped in collections 26 and 27 (a small amount of volatile components that are known under the conditions that could be formed as a result of thermal decomposition into molecules evaporator 25, trapped separately in low-temperature traps 28 and 29).
    Heating temperatures for thin-layer molecular distillation may be higher than those indicated in the exemplary embodiment. Temperatures of 350 ° C or higher are preferred.
    权利要求:
    Claims (1)
    [1]
    Claim 1. Method of processing residue of vacuum distillation at a refinery by thin-layer molecular
    distillation under vacuum conditions at a constant residual pressure of (3.5-5) -10 mbar with the material to be distilled being fed to the evaporation surface, heated by countercurrent coolant supply, in the form of a film, which is given turbulence with the help of brushes of a cleaner, with by reasoning the output of the distillate and the concentrated residue,
    characterized in that, in order to increase the yield of the distillate and increase the efficiency, the process is carried out at an evaporation surface temperature exceeding the temperature
    the residue is vacuum distillation, at 44-143 ° C.
    2 The method according to claim 1 is different from the fact that the temperature of the evaporation surface is above 350 ° C.
    Table 1
    table 2
    Fig 2
    Table 3
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    同族专利:
    公开号 | 公开日
    DE3790412D2|1988-08-25|
    SE8800953D0|1988-03-16|
    GB2202458B|1990-06-13|
    JPH07110948B2|1995-11-29|
    FI881371A|1988-03-22|
    DE3790412C1|1999-11-11|
    CN1017253B|1992-07-01|
    CN87105188A|1988-02-03|
    WO1988000493A1|1988-01-28|
    AR243223A1|1993-07-30|
    FI881371A0|1988-03-22|
    AU591574B2|1989-12-07|
    SE8800953L|1988-03-16|
    FI85339C|1992-04-10|
    UA12649A|1997-02-28|
    EP0276240B1|1992-02-26|
    NL8720324A|1988-06-01|
    CH666901A5|1988-08-31|
    FI85339B|1991-12-31|
    GB8806834D0|1988-05-25|
    MX168940B|1993-06-15|
    AU7644387A|1988-02-10|
    IN167907B|1991-01-05|
    BR8707398A|1988-09-13|
    GB2202458A|1988-09-28|
    JPH01500439A|1989-02-16|
    EP0276240A1|1988-08-03|
    SE459498B|1989-07-10|
    US4925558A|1990-05-15|
    ES2004449A6|1989-01-01|
    CA1287593C|1991-08-13|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE3122650A1|1981-06-06|1982-12-23|Leybold-Heraeus GmbH, 5000 Köln|Process and apparatus for mineral oil distillation|
    DE3122652A1|1981-06-06|1982-12-23|Leybold-Heraeus GmbH, 5000 Köln|METHOD AND DEVICE FOR SHORT-WAY DISTILLATION|
    EP0189610A1|1984-12-19|1986-08-06|Shell Internationale Researchmaatschappij B.V.|Process and apparatus for the short-path vacuum distillation of a liquid hydrocarbon mixture|CH684057A5|1992-11-30|1994-07-15|Buss Ag|Methods for further processing the vacuum residue in a crude oil refinery.|
    CN1044568C|1994-02-17|1999-08-11|天津大学|Distillation method for thermal sensitive material with simultaneous prodn. of light and heavy impurities|
    US6699385B2|2001-10-17|2004-03-02|Chevron U.S.A. Inc.|Process for converting waxy feeds into low haze heavy base oil|
    US20050051463A1|2003-09-09|2005-03-10|Chevron U.S.A. Inc.|Production of high quality lubricant bright stock|
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    CA2797282A1|2010-04-23|2011-10-27|Regenerative Sciences Patents Limited|Method and system for hydrocarbon extraction|
    CN101892073B|2010-07-28|2013-03-27|广州市浩立生物科技有限公司|Method for extracting base oil from cutting line oil|
    KR102167583B1|2014-06-30|2020-10-19|코오롱인더스트리 주식회사|Method of manufacturing petroleum resin with improved odour|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CH2954/86A|CH666901A5|1986-07-23|1986-07-23|METHOD FOR PROCESSING THE RESIDUE RESULTING FROM A PIPELINE REFUELY IN VACUUM DISTILLATION.|
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