• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    1523210 Start-up and shut-down procedures for hydroprocessing reactors CITIES SERVICE RESEARCH & DEVELOPMENT CO 10 Dec 1976 [17 Dec 1975] 51746/76 Heading C5E A start-up or shut-down procedure for an upflow ebullating bed reactor comprises circulating an initial charge of light oil and hydrogen through the reactor and progressively replacing the light oil by the heavy oil feed as the reactor temperature is increased (or vice versa for shut-down) with the ratio of light oil to heavy oil feed and the temperature being altered in a correlation such that the viscosity and density of the changing feed are maintained within + 20% of the starting viscosity and - 10% of the starting density during start up (or within -20% of the starting viscosity and + 10% of the starting density during shut down) whilst the liquid is pumped at constant rate to circulate in the reactor and ebullate the bed. The charge of catalyst in the reactor is initially heated by passage of hot gas.
    公开号:SU795500A3
    申请号:SU762434651
    申请日:1976-12-17
    公开日:1981-01-07
    发明作者:С.Джеймс Льюис
    申请人:Ситиз Сервис Рисерч Энд Дивелопменткомпани (Фирма)；
    IPC主号:
    专利说明:

    (54) WAY OF REACTOR START
    one
    The invention relates to methods for starting a reactor with a fluidized bed of a catalyst for the hydrotreatment of heavy oil residues and can be used in the refining industry.
    Methods are known for starting a reactor with a fluidized bed of a catalyst for hydrotreating heavy oil residues 1 and 21.
    Closest to the invention is a method for launching a fluidized bed reactor for hydroprocessing heavy oil residues 3j. The heated gas is passed through a catalyst reactor, then a light oil fraction and a hydrogen-containing gas are circulated and the light fraction is gradually replaced with a feedstock.
    The proc, ess is carried out with a constant increase in temperature. The conversion or hydrogenation rate is controlled by increasing the reactor temperature and the space velocity. Thus, it is necessary to constantly change the flow rate of the liquid phase and regulate the gas flow rate.
    The aim of the invention is to increase the efficiency of the process.
    This goal is achieved by the described method of starting a reactor with a fluidized bed of a catalyst for hydrotreating heavy oil residues by passing heated gas through a reactor with a catalyst, then circulating through the reactor while gradually increasing the temperature of the light oil fraction
    and a hydrogen-containing gas supplied at a constant rate and maintained during the subsequent gradual replacement of the light oil fraction with the feedstock of the rate of the circulating
    the liquid phase is constant by feeding the liquid phase with the fluctuation of viscosity and density at a given temperature value within +10 and ± 5%, respectively, of their initial values for a light oil fraction
    at the temperature of the beginning of its circulation. When carrying out the process by the described method, there is no need to change the feed rate of the liquid
    phase and gas flow control. In the examples below, the same equipment is used. The steps of loading the catalyst and passing through the reactor with the heated gas catalyst OM are of the same type. On odi-naky data on the supply of hydrogen-containing gas, the circulating light oil fraction (LMF) and the feedstock — heavy gas oil (TG). The characteristics of the oil fraction and heavy gas oil are given below. Mean boiling point, C J Density, g / cm at 15.56 ° C Viscosity, P, at 99, Viscosity, P, at 0.205 0.48 Example 1. In a reactor with a boiling-bed reactor at operating temperature and pressure, a light oil fraction begins to be supplied to the catalyst. PeajcTop is filled up to a working urn and it is created: an expanded catalyst slSy. Maintain a constant gas supply; At time T + 22 h (T is the conditionally accepted initial value of time), the circulation rate of the light oil fraction is increased by 33%.
    For this example, the temperature is.
    The increasing (relative) viscosity from -5 d5 from baseline to decreasing with density from +5 to -5% from baseline is a consequence of changes in the composition of the mixture and the tera time.
    In this case, the superficial velocity of the liquid in the reactor remains approximately the same {calculated by the formula given below.
    ,,
    v-
    where V is the superficial velocity of the liquid in the reactor, l / m min; about - the density of wetted catalyst particles, g / cm;
     liquid density,, is the viscosity of the reaction liquid, cP;
    CS is a constant value depending on the characteristics of the raw material.
    The procedure for stopping the reactor is similar to the start-up procedure. The supply of heavy feedstocks is gradually ceased and a light mass fraction is fed instead. The feed rate of the liquid phase is adjusted so that a 35% expansion of the layer at the start is achieved. At time T + 25 h, the delivery of heavy gas oil begins with the supply of 12.5% TG and 87.5% LMF. At time T + 26 h, the composition of the feed mixture is changed and 25% TG and 75% LMF are fed. At time T + 27 h, the composition of the feed mixture is 37.5% TG and 62.5 LMF. At time T + 28 h, the composition of the feed mixture is 50% TG and 50% LMF. At this time, catalyst transfer has been observed due to excessive expansion. Permanently 2. Set a constant gas flow rate and a constant flow rate of the liquid phase. These values are adjusted so that a 35% expansion of the layer at the start is achieved. This table below shows how the relatively constant viscosity and density of the feed stream are maintained by gradually replacing the circulating light. raw oil fraction with increasing temperature. This makes launching smooth and quick.
    权利要求:
    Claims (3)
    [1]
    1. US Patent 3244617, cl. 208-143, published 1966.
    [2]
    2. US patent 3491017, cl. 208-108, published. 1970.
    [3]
    3. US patent number 3491018,
    cl. 208-108, published. 1970 (prototype).
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    同族专利:
    公开号 | 公开日
    JPS5276306A|1977-06-27|
    DE2655259C3|1982-10-28|
    FR2335583B1|1982-06-18|
    DE2655259B2|1981-06-04|
    FR2335583A1|1977-07-15|
    DE2655259A1|1977-06-30|
    CA1069453A|1980-01-08|
    US4053390A|1977-10-11|
    GB1523210A|1978-08-31|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3244617A|1963-06-11|1966-04-05|Cities Service Res & Dev Co|Start-up of a hydrogenation-hydrocracking reaction|
    US3271301A|1964-02-03|1966-09-06|Cities Service Res & Dev Co|Hydrogenation process|
    US3281352A|1965-06-04|1966-10-25|Hydrocarbon Research Inc|Process for hydrogenation in the presence of a high boiling oil|
    US3642613A|1970-06-19|1972-02-15|Universal Oil Prod Co|Black oil conversion process startup procedure|
    US3733476A|1972-05-30|1973-05-15|Texaco Development Corp|Means and method for automatically controlling the hydrogen to hydrocarbon mole ratio during the conversion of a hydrocarbon|
    DE2351774A1|1973-10-16|1975-04-24|Exxon Research Engineering Co|Electronic quality control of processed product - comparing measured electric parameter simulating viscosity with set desired value|US4898663A|1988-11-25|1990-02-06|Texaco Inc.|Method for controlling sedimentation in an ebullated bed process|
    US5156733A|1989-03-29|1992-10-20|Texaco Inc.|Method for controlling sedimentation in an ebulated bed process|
    US5258116A|1992-03-23|1993-11-02|Mobil Oil Corporation|Method for reducing turnaround time of hydroprocessing units|
    CN101418232B|2007-10-26|2012-08-29|中国石油化工股份有限公司|Shutdown method of bubbling bed hydrotreating process|
    CN101418231B|2007-10-26|2012-04-04|中国石油化工股份有限公司|Shutdown method of bubbling bed hydrotreating process|
    BR102018011146A2|2018-05-30|2019-05-28|Nc Engenharia, Industria E Comercio Ltda|DEVICE FOR DRAINAGE AND SEALING OF MIST ELIMINATORS|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/641,394|US4053390A|1975-12-17|1975-12-17|Start-up procedure for a residual oil processing unit|
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