• 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:
    1504816 Feedstock for delayed coking processes CONTINENTAL OIL CO 18 June 1976 [25 Aug 1975] 25437/76 Heading C5E A delayed coking process for producing premium coke from petroleum-derived feedstock comprises the following feedstock pre-treatment steps: (a) preselecting a desired BMCI value (a defined function of boiling point and API gravity) for the feedstock, (b) determining the BMCI of the feedstock before charging it to the delayed coker, and (c) adjusting the BMCI of the feedstock, prior to charging it to the coker, to the preselected desired value. The adjustment of the BMCI may be by distillation, blending, or cracking of the feedstock.
    公开号:SU865132A3
    申请号:SU762373647
    申请日:1976-06-17
    公开日:1981-09-15
    发明作者:Х.Кеглер Вильям
    申请人:Континентал Ойл Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the production of coke, namely to methods for delayed coking. A method of slow coking is known, including heating the crude oil to a temperature of coking and subsequent aging at the indicated temperature i. The disadvantage of this method is the production of coke with a high linear thermal expansion coefficient (CTE), i.e. obtaining low quality coke due to the fact that the implementation of this method does not preliminarily determine the properties of the raw material. The purpose of the invention is to improve the quality of coke. This goal is achieved by the fact that according to the method of delayed coking, which includes heating the crude oil to the coking temperature and subsequent aging at the specified temperature, the crude oil has a correlation index of 95-130. The best quality of coke (with the lowest coefficient of thermal expansion coefficient of CTE) is obtained from the feedstock, which has a defined limit of aromatic concentrations, characterized by the value of correlation efficiency (IC), which is proportional to the content of aromatic compounds in the raw material and can be calculated by the formula 48640 IC 473d: 4. 456.8 + T kip -evolmetric average T PIP boiling point, C; , 20 - density of the raw material at, is related to the density of water at 4 ° C. The volumetric average temperature can be calculated using the formula T-) + Td -t- Tj + T. - - - -, T. temperature at the distillate 10% by volume; 30% by volume; 50% by volume; 70 vol. %; 90% by volume. The temperatures at the distillate of 10 vol.%, Vol.% And so on are summed up and za, are divided by five. In those cases, for example, in the case of thermal cracking resins), when full distillation is always possible, instead of the average boiling point, the boiling point is determined by distillation at 50%, which closely correlates with the average volumetric boiling point and is found in almost all layers 1a x within three values of IC. Most coking plants use a moderate or large amount of product recycled by passing the overhead from the coke drum into the recycle. a coke plant, where these overheads, as well as fresh raw materials fed into the system, are fractionated to produce a residual product, which is the kiln charge for the operation of the pot. In these cases, the IC value of the furnace load is a more significant factor in the quality of coke than the IC value of the feedstock entering the system and may change due to a change in the process conditions in the distillation column. Therefore, when the feedstock and the recycled product are fed into a distillation column, and the residual product of the distillation column is used as the furnace charge, the IC value of the furnace charge may be a better indicator of the quality of coke than the IC value of the fresh raw material. The term “raw materials” means the kiln loading, and not the fresh raw material supplied to the S system. The drawing shows a graph of the dependence of the KTR obtained coke from Ik feedstock. The points of the curve are determined using a wide variety of raw materials. The most likely value of IC, providing the highest quality coke with CTE 5.0 X C and below, is in the range of 95-130. As the IC value moves away from the specified limit in any direction, the prospects for obtaining coke with CTE 5.0 X or below becomes more and more distant. When the feedstock analyzed prior to coking has an IR value of 95 - 130 and, in particular, 110 - 115, it can be fed directly to coking and it is possible to produce higher coke quality. If the Hc value of the feedstock is outside these limits, then some regulation of this feedstock is necessary in order to ensure the greatest possibility of obtaining coke with a CTE of 5.0x or less. Such regulation of the IC value of the raw material can be carried out in one of the ways, for example by mixing. Thermal cracking can be the most effective way to control the IC value, especially when it is less than 95. Distillation and mixing can be the most practical ways to control the IC raw material value within the required limits if this raw material size is more than 130. After this adjustment it is necessary that the re-determination of the value of the initial raw material is carried out before loading into the coke oven to ensure that it is within the specified limits. Experiments have been carried out in a pilot coke plant using different types of feedstock, which are regulated in various ways. (Determining the relationship between the IC of this raw material and the CTE of the produced coke. Example 1. A mixture of thermally cracked recycle gas oil and liquid catalytically cracked decanted oil is coked 50-50 wt.%. Additional portions of the initial mixture are subjected to thermal cracking under conditions of different hardness. The obtained cracking resins are subjected to coke The Ik value of the initial mixture is 102., and in both of the obtained resins, the Ik values are 148 and 125. Higher values of the Ic of the resins are obtained under more severe conditions in the cracking unit. The physical properties of the initial mixture are presented below. , 0269 Temperature at the distillation, s, - at, vol.%: - 5.10338 20360 30. 377 40389 50402 60417 70451 80 454 90488 95531 End point, ° С 531 Carbon residue according to Conradson, wt.% 1.7 Sulfur content wt.% 1.1, Viscosity, cSt, with C :. 3844.9 5418.8 99 .4.6i Ик102 Conditions for the occurrence of two different processes of thermal cracking (non-optimal mode) are presented in Table. 1. The properties of thermal cracking resins obtained under the specified process conditions are presented in, table. 2. | | From tab. 2 that the highest value of PjK is obtained in a rezul (Tate of a higher temperature of thermal cracking, which is likely caused by an increase in the intensity of the condensation-polymerization process. The initial mixture and two thermal cracking resins are subjected to coking in the experimental the coking plant has the following nominal process conditions (which provide the highest quality coke) listed below: Feed rate, kg / h4.53 Recirculation rate, g / h4.53 Furnace outlet temperature, C454 Overpressure at the furnace exit, kgf / cm 7 Excessive pressure in the drum, kgf / cm - 1.75 Drum surface temperature, C510 Drum bottom upper temperature, s 510 Duration of the process, h8 Total recirculation time, min10 Duration of the material under heating, h 2 Duration of treatment water vapor, 1 Goat h; mixed feed rate (total raw materials / fresh raw materials) 2 Table 3 presents the outputs of coking products and the quality data of coke obtained from three types of raw materials. The feedstock with the value of IR 102 is the initial mixture of catecically cracked liquid decanted oil and gas oils; the other two types of feedstock are resins obtained in a thermal cracking unit. For each case of operation of the coke plant, the values of the raw material and the furnace load of the furnace are presented. The difference in these two quantities for each kiln operation is related to the raw material mixed with recycled oil before entering the kiln. The smallest KTP of coke is obtained in the case of use, raw material with a magnitude of IR 125. This raw material undergoes thermal cracking under relatively soft conditions. A more severe thermal cracking mode leads to the production of raw materials with a higher Ic value (148). The initial mixture (with the value of Ik.102) and the raw material with a high value4, Ik h148) provide coke of lower quality (with a higher KTP}.) In addition, the raw material with a rare Ic can be thermocratically cracked to produce cracked raw material, having an optimal value of IC, which ensures the optimum quality of coke under the conditions of the coking plant. However, the feedstock cannot simply be cracked to almost the maximum degree, since more severe conditions Cracking results in a raw material having an IR value above the optimal limit, ensuring coke production with a low KTR value. EXAMPLE 2 The stirring effect of the clarified raw oil with a high content of paraffins, various amounts of thermal cracking resin is determined, having a high IR value (148), obtained according to example 1. These mixtures are subjected to coking under constant operating conditions in a coke installation as in example 1. Physical properties of two types of coking feedstock four mixtures obtained from this raw material are shown in Table. 4. As can be seen from the table. 4, four dimensions and two types of raw materials have IR values from 23 (with a high content of paraffins) to 148 (with a high Kim content of aromatic hydrocarbons) .. The resulting yields of coking products and the quality of coke are presented in Table. 5. From table. 5, it is clear that coke of the highest quality is obtained from each mixture, while coke with an unacceptable high KTP is obtained from each furnace charge as an unmixed raw material. The mixture with the minimum content of thermal cracking resin (40), with the initial value of IC 61 and the IC value of the furnace 82 load, provides coke with an acceptable CTE value, but the coke yield is much lower than if the raw material is used with an IC value of 95 - .130. There may be some types of coking feedstock when the limit of IC values between 95 and 130 is not the desired optimal limit. In these cases, another predefined limit may be specified, and the present invention is broader; its aspects include regulating the coking operation by first selecting the limit of IC values, ensuring the achievement of the desired result, controlling the IC value of the raw material and adjusting the IC value of the raw material in the specified pre-set limit. This may be the case when the coke yield does not have a large building, and the KTR of the coke plays the main role. Then, for this situation, the value of IC should be pre-selected outside the 95-130 limit. It is also possible that some types of coking feedstock have values of IH beyond the limit of 95-130, which provide optimal results. In such a case, the present invention includes the steps of preselecting the required limit for the value of the raw material Ic, determining the value of the raw material Ic and adjusting the value of the raw material Ic, if it is not within the preselected limit. It is not possible to precisely name the low KTP value of coke obtained from a feedstock with an IC in the range of 95–130, but the IC value can be quickly determined for a given feedstock, since the average boiling point and density of the feedstock is the qs factor which almost always can be determined for any 5p® ukta stream or feedstock in the process of refining. In addition, SUYETVA link between the IC and the original coking duel for this type of 5Hp or mixtures of this raw material. However, the F® that the IR of the feedstock is g is the predefined limit of 95130; It does not guarantee that the CTE value of the resulting coke is less than 5.0x10 / C. The CTE of the produced coke is also a function of the coking conditions, and in some cases a certain type of feedstock, even if it has the required IR value, cannot provide top quality coke, regardless of the conditions of "Koksovani. However, even in this case, the CTE of coke will be minimal for this type of feedstock if the raw IC is in the required limit, i.e. Some types of feedstock, even if they have the required Ic value, do not provide the highest quality coke. However, the regulation of the IC value to the specified limit optimizes the possibilities of obtaining higher quality coke, and this is a more perfect method of quality control in comparison with the known ones. Raw materials that do not provide the possibility of obtaining higher quality coke usually have a high content of asphaltenes. The optimal raw material for obtaining superior quality is such a raw material that has an IR value of 95-130. Example 3. Consider the condition when the raw material does not provide the possibility of obtaining top quality coke, however, it carried out the process according to the invention. the minimum value of KTP of coke is reached as a result of coking of the raw material, which was subjected to preliminary regulation in order to bring the value of Ic of this raw material to the required limit. In this example, mixtures of residual oils of vacuum distillation (with different content of diluted stripped tar) with coking gas oil of the highest quality are used. Oilsgoe oil is a poor raw material for obtaining coke of the highest quality. Even after mixing with the pyrolysis resin of aromatic hydrocarbons, top quality coke is not obtained. However, mixtures having an IC value in the specified limit result in coke production with a lower CTE value than the feedstock having an IC value outside the specified limit. The properties of the raw material for coking used in this example are given in table. 6. The outputs of the coking product and the characterization of coke are presented in t abl. 7 The exact reason for the connection between the initial value Ik of the raw material and the CTE of the coke produced has not been established. However, it exists and is valuable in the implementation of the coking process to produce top quality coke having a minimum CTE value. In some cases, the only difference between this process and the usual coking process is the analysis of the value of the feedstock IC before it is supplied to the coking unit. For example, if the IC value of the feedstock is 95-130, then this raw material must be supplied directly to the coking operation without much adjustment, and one can expect an optimum quality of the product to be obtained. The most likely case is when the Ic value of the feedstock is not within the required limit and can be regulated by such methods, KciK hermetic cracking, with the aim of increasing Ic, or mixing, with the aim of reducing Ic, or in some other way ( or by methods), for example, by distillation, regulation of conditions in a distillation column of a coking plant, etc. The present invention provides a simple and reliable method for determining whether a coke feedstock has the optimum potential to produce the highest quality coke from it, Si also allows you to determine which parameters need to be adjusted in order to obtain an optimal coke yield.
    Process conditions
     one
    Process
    Feed rate
    kg / h
    Recycling rate
    kg / h
    Outlet temperature
    coil, C
    Overpressure in
    coil, kgf / cm
    The temperature in the evaporative drum, with:
    top part
    base
    The temperature in the distillation column, s, (top)
    Reboiler temperature
    with
    Reflux number of distillation column
    Ud. weight, g / cm Temperature at distillation, s, at.
    five
    ten
    20
    thirty
    40
    table 2
    1.1338 1.0785
    317 348 369 385 396
    50
    60
    70 80 90 95 End Point, C
    Conradson carbon residue, weight
    Sulfur content, wt.%
    Viscosity, cSt, when, “C:
    409 431 449 477
    993 (534) 1061 (572) 572
    Table 3
    Coke (e content
    6% volatile)
    Coke quality
    Non-Finished (Green) Coke:
    Volatile yield, wt.% Calcined coke:
    Kerosene density,
    Graphitized KTP electrode, 10 / С Clarified oil, wt.% Thermal cracking resin, wt.% Od. weight, g / cm 1.1338 0.8927 0.9676 The temperature at the distillate, s, at, vol. %:
    Continuation of table 3
    26.7 40.1
    7,8
    7.5
    2.12 2.12 4.8 6.4
    Table 4 100 60, 100 - 40 3 25 40 60 70 75, 0086 1,0466 1,0623
    carbon residue
    according to Conradson, VV.% 12.0 0.1
    sulfur,
    1.27 0.12 148 23
    148
    23 145
    37
    ,
    0.15
    0.03
    0.16 0.00
    5.8 12.1
    2.6 12.8
    7.4 18.2
    43.8 52.0 40.1
    4.9
    and cop:
    7,8
    9.8
    0.60
    :
    blueu, 2,12
    2.13 2.12 2.12 2.12 v 2.12
    electrol, loVc
    6.411.7 4.23.44.74.0
    Continuation of table 4
    3,44,17.38,5
    0.71 0.96 1.06 1.11 6183105112
    Table 5
    6183105112
    8298113126
    0,050,080,070,10
    0,110,110,090,10
    8.57.9., 6
    74,968,965,964,0
    16,423,027,229,2.
    8.8. 6.39.58.0
    1.01 1.00 1.11.09
    Initial raw materials:
    Residual, weight%
    Otbesenenna sm wt.%
    but
    Beam, weight, .g / cm,
    The temperature at the distillate, With, when, about,%:
    table 6
    50
    thirty
    70
     100
    50 11448 10793 10327
    fresh (oven load)
    Outputs of products, wt.%:
    N.
    Hjs
    Sf up to 204 - 343С from and above. Coke quality
    Uneven (green
    coke:
    Volatile yield, wt.%
    Sulfur content, wt.% Calcined coke:
    Kerosene density, g / cm
    权利要求:
    Claims (1)
    [1]
    Graphite Electro KtP, 16 1 ° 0. DETAILED DESCRIPTION A method for delayed coking, including heating oil to a coking temperature and subsequent aging at a specified temperature, is different. so that with. to improve the quality of the coke, oil table 7
    117
    153
    94 105
    144 122
    0.10
    0.10
    1.15 0.07 0.04 0.10 4.7 6.0 7.9
    41,8
    48.3
    55.5 53.4 36.4
    45.5
    6.4
    6.9
    6.7
    2.12 2.11
    2.11
    8.1
    7.4
    8.5 raw materials have a correlation index of 9555.Sources of information taken into account during the examination 1. Kazmin G, I. and others. Refineries USA. M., 1962, p. 158-170.
    类似技术:
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    同族专利:
    公开号 | 公开日
    NO761996L|1977-02-28|
    JPS5226501A|1977-02-28|
    NO148294C|1983-09-14|
    CA1076049A|1980-04-22|
    GB1504816A|1978-03-22|
    ES450966A1|1977-08-16|
    AU1518976A|1978-01-05|
    SE7606553L|1977-02-26|
    FR2322192A1|1977-03-25|
    DE2626622A1|1977-03-03|
    DE2626622C2|1985-02-21|
    US4043898A|1977-08-23|
    FR2322192B1|1980-02-08|
    IT1065957B|1985-03-04|
    ZA763516B|1977-05-25|
    DK257776A|1977-02-26|
    BE843144A|1976-12-20|
    NO148294B|1983-06-06|
    NL7605082A|1977-03-01|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    US3412009A|1967-03-15|1968-11-19|Continental Oil Co|Process for producing carbon black oil|
    DE1671304B2|1967-03-28|1976-05-13|DELAYED COOKING PROCESS FOR THE SIMULTANEOUS PRODUCTION OF TWO DIFFERENT GRADE OF PETROL COCKS|
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    US4518486A|1980-12-24|1985-05-21|The Standard Oil Company|Concurrent production of two grades of coke using a single fractionator|
    US4490244A|1982-09-29|1984-12-25|Great Lakes Carbon Corporation|Production of premium grade petroleum coke|
    JPH0250154B2|1984-09-12|1990-11-01|Nippon Kokan Kk|
    US4737261A|1984-10-05|1988-04-12|International Coal Refining Company|Process for the production of premium grade needle coke from a hydrotreated SRC material|
    US4698147A|1985-05-02|1987-10-06|Conoco Inc.|Short residence time hydrogen donor diluent cracking process|
    NZ217510A|1985-09-12|1989-09-27|Comalco Alu|Process for producing high purity coke by flash pyrolysis-delayed coking method|
    US4720338A|1986-11-03|1988-01-19|Conoco Inc.|Premium coking process|
    US5158668A|1988-10-13|1992-10-27|Conoco Inc.|Preparation of recarburizer coke|
    US5143597A|1991-01-10|1992-09-01|Mobil Oil Corporation|Process of used lubricant oil recycling|
    US6048448A|1997-07-01|2000-04-11|The Coastal Corporation|Delayed coking process and method of formulating delayed coking feed charge|
    US20020179493A1|1999-08-20|2002-12-05|Environmental & Energy Enterprises, Llc|Production and use of a premium fuel grade petroleum coke|
    US6168709B1|1998-08-20|2001-01-02|Roger G. Etter|Production and use of a premium fuel grade petroleum coke|
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    US8372264B2|2006-11-17|2013-02-12|Roger G. Etter|System and method for introducing an additive into a coking process to improve quality and yields of coker products|
    US8206574B2|2006-11-17|2012-06-26|Etter Roger G|Addition of a reactor process to a coking process|
    US8361310B2|2006-11-17|2013-01-29|Etter Roger G|System and method of introducing an additive with a unique catalyst to a coking process|
    US9011672B2|2006-11-17|2015-04-21|Roger G. Etter|System and method of introducing an additive with a unique catalyst to a coking process|
    EP2336267B1|2008-09-09|2017-04-05|JX Nippon Oil & Energy Corporation|Process for producing needle coke for graphite electrode and stock oil composition for use in the process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/607,728|US4043898A|1975-08-25|1975-08-25|Control of feedstock for delayed coking|
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