• 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:
    A reactor is provided with at least one homogeneous bed of solid particles, especially of catalyst particles. To this end, the solid particles in the reactor are brought into a state of incipient fluidisation by means of a fluid stream, and the flow velocity of the fluid stream is then reduced or the fluid stream is interrupted and the particles are allowed to settle. A reactor suitable for carrying out the process has a supply tank (2) with a fluid inlet (13) at the bottom end, a fluid outlet (14) at the top end, an inlet (17) for the solid particles at the top end and an outlet (3) for the solid particles at the bottom end, and a line (6) which connects the outlet (3) for the solid particles to the top end of the reactor (1). <IMAGE>
    公开号:SU1072791A3
    申请号:SU752181496
    申请日:1975-10-15
    公开日:1984-02-07
    发明作者:Аренд Пегельс Абрахам；Ян Шеффер Хендрик
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В.(Фирма)；
    IPC主号:
    专利说明:


    rsD
    The invention relates to a method for filling reactors with one or several homogeneous layers of solid particles, in particular catalyst particles, and can be used in the hydrodesulfurization processes of natural oil fractions, such as crude oil or residues obtained by removing at least part of the volatile products from crude oil ,. A known method of filling the reactor with one or more homogeneous layers of solid particles with a diameter of 0.5-3 mm and a length of 3-7 mm by bringing the solid particles into a fluidized state with a fluid flow and their subsequent precipitation by reducing the flow rate or stopping by 1 hour. “The purpose of the invention is to more completely fill the reactor with homogeneous layers of solid particles, in particular catalyst particles. The goal is achieved by the fact that according to the method of filling the reactor with one or more homogeneous layers of solid particles with a diameter of 0.5-3 mm and a length of 3-7 mm by bringing the solid particles into a fluidized state by a liquid flow and their subsequent deposition by reducing the velocity flow or stopping of the feed, before the precipitation, the pseudation of the particles is carried out in the initial stage of the layer expansion less than 10. Under the fluidization, it is assumed that the solid particles are suspended in the liquid. By maintaining fluid flow, the precipitation of solid particles (they are in the fluidized bed) is prevented. The expansion of this layer means the percentage concentration at which the volume of the fluidized bed exceeds the volume of the layer formed by the fully settled catalyst particles. Initial fluidization means that the degree of expansion of the bed is small, i.e. below 10%, predbchtitelNO below 5%. The lower the expansion rate of the fluidized bed, the more complete is the reactor after the catalyst particles settle and, consequently, the less empty space in the reactor. The flow rate of the fluid flow which can be used to maintain the catalyst particles of this type, having certain sizes in the state of initial fluidization, must be determined in advance in experiments on models. It is possible to pre-fill an empty reactor with solid particles, and then introduce a stream of liquid into it in order to bring these particles to the state of initial fluidization. Filling the reactor with solid particles (for example, by means of a receiving funnel) takes a lot of time, moreover, a large degree of breakage of solid particles is observed. Therefore, it is preferable to introduce solid particles into the reactor in the form of isham in liquid. During the introduction of solid particles, which may or may not be in the form of sludge, the flow of fluid that causes these particles to the state of initial fluidization may be constant (or not constant). If the specified fluid flow is maintained during the introduction of solid particles (which is preferable), then the latter flow into the upper part of the reactor. Preferably, the reactor has one or more conical grids for solid particles, so that solids can be formed on each of them, and the grids are a central opening through which solids can descend when the reactor is to be emptied. The inclination of the gratings is preferable so that the solids can leave the reactor under the force of gravity when the reactor is to be emptied. According to the invention, during the filling of the reactor, the solid particles are brought to the initial fluidization state by means of a liquid stream. In order also to fill the space below the gratings, it is advantageous to lower the flow rate of the fluid one or several times for a short period of time after a short decrease in this velocity or a complete stop of the flow of fluid. An oil based fluid flow is preferred. Oil distillate fractions, in particular gas oil, are very suitable. Although it is possible to use fresh liquid each time in order to bring the solid particles into a state of initial fluidization, the same liquid can be used for recirculation. It is preferable to introduce a liquid stream in the lower part of the reactor at a desired rate and remove it from the upper part in a place beyond which solid particles cannot be in the liquid. When the reactor is filled with all the solid particles that need to be brought into the initial fluidization state, the flow rate of the liquid is reduced or stopped and the particles are allowed to settle. After the particles have settled, the liquid can
    be removed or replaced by another. In some cases, the same fluid that is used for fluidization can pass, at elevated temperature and / or pressure, through the already formed homogeneous layer of the catalyst in order to transfer the catalyst to the active form (for example, α-sulfided for catalyst desulfurization based on metals U1 and / or MP groups on the carrier).
    To obtain layers of solid particles that do not cause a strong pressure drop, when the liquid to be converted with these particles passes through the layer, it is preferable that the sizes of these particles remain within narrow limits.
    The presence of solid particles that are smaller than the sizes indicated and finely ground is undesirable, since they can interfere with the flow and, consequently, lead to a significant drop in pressure.
    In the production of catalyst particles, for example, by extrusion, during further handling (transport; pouring, etc.), crushing is usually observed, which results in the formation of smaller particles, despite the fact that some amount of pulverized material (finely ground particles) is always present
    Solids, whose dimensions lie within narrow limits, are introduced into the bed obtained by fluidization in a liquid, partially or completely consisting of particles, whose dimensions lie within narrow limits, as well as of particles that are smaller, until the particles having smaller sizes will not be assembled in the right-back layer. Interruption then fluidization, you can remove the top layer of settled particles having smaller sizes. It is very convenient to remove smaller particles with suction. During fluidization, which is convenient to perform in the supply tank. - (in a large, e.g. cylindrical vessel), dust particles usually do not settle, but are entrained in liquid and are carried away from the supply tank. Before returning the fluid for fluidization, it is good to remove the fine particles from the bottom of the supply tank again by filtration. Feed tanks can be used as space for storing solids. After particles are obtained in the supply tank, the dimensions of which lie within narrow limits, the reactor can be filled with them at any desired time, preferably in a sludge state.
    The operation of replacing solid particles in the reactor can be performed very quickly (within a few hours). The reactor is emptied and then filled from the supply tank with particles whose dimensions lie within narrow limits. Filling the reactor with solid particles that are not assembled together in advance in the supply tank in any way can take several days if
    0 large reactor. Preferably, the feed tank has a volume of the same order (or slightly larger) as the reactor.
    Solids are obtained by extrusion. BecbUjia particles with a diameter of 0.5-3 mm and a length are well suited. 3-7 mm.
    Such solids are suitable as catalyst particles, in
    0 particularly for a catalyst that can be used to remove metals and / or hydrodesulphurize crude natural oils or residues. They contain one or several U1 metals and / or VIII groups of the periodic system or their compounds on oxide carriers; in this case, catalyst particles consisting of one or several oxides and / or cobalt sulfides, nickel, molybdenum, and tungsten on a carrier consisting entirely of alumina and / or silica.
    Removal of metals and / or hydro5 desulfurization, for example, crude oil or residue can be produced in reactors with crude oil or residue can be produced in reactors under known conditions, namely at 385-445 s, pressure
    0 hydrogen 75-225 kg / cm and space velocity OJ5-5 weight. hours load for one part of the volume of the catalyst.
    The drawing shows the proposed installation.
    five
    The installation contains a reactor 1, which can be filled with catalyst particles from the supply tank 2. The particles can leave the pit container through the pipeline 3 and, mixing with a liquid, for example, gas oil supplied through pipeline 4, they can flow into the upper part of the reactor 1 under by the action of the slurry pump 5 through the conduit 5 of the conductor 6. At the same time, the liquid can flow to the lower part of the reactor. Pipeline 8 serves to discharge the liquid through the top of the reactor. Through conduit 8, the fluid can flow to the re: Zervoir 9, which is reported by
    5 pipeline 10 with the atmosphere. On
    Soy 11 serves to supply fluid from reservoir 9 to conduits 4 and 7 through conduit 12. Pitaccid reservoir 2 includes a particle inlet 17 and a fluid inlet conduit 13 (which closes when reactor 1 is filled} through which, when closed, conduits 3 4 and 7, the fluid can be supplied from reservoir 9 to feed reservoir 2 via conduit 12 by pump 11. The upper part of feeder reservoir 2 is provided with an outlet conduit 14 through which fluid can be returned to recirculation reservoir 9. ground particles can be removed from the fluid in conduit 14 by means of a filtering device 15. The conduit 16 is located in the lower part of the supply tank and serves to completely remove or almost completely from the supply tank the liquid that can be made when it is; and the tank is filled with solid particles whose dimensions lie within narrow limits.
    . Example. Reactor 1 (height 23 m, diameter 3.2 m) is filled with 170 m of particles, the catalyst obtained during extrusion, medium diameter — 1.5 mm in diameter and 5 mm long. The catalyst particles come from the pit 2 tank 2 (height 26 m, diameter 3.2 m) through pipe 3, pump 5 and pipe 6 at a speed of 15 t / h using gas oil, which flows through pipe 4 at a speed of 223. Through the pipeline 7, the gas oil enters the reactor 1 at a speed of 7 mm / s in the reactor, so that the particles in the reactor are brought to the initial fluidization state. In the upper part of the reactor, the gas oil is returned to the tank 9 for recycling through conduit 8. When the required amount of catalyst particles in the reactor is in the state of initial fluidization, the flow rate of gas oil flowed through conduit 7 several times briefly. The gas oil supply is then interrupted and, if required, the gas oil present in the reactor is removed.
    Particles that are transported to the reactor from feed tank 2 are prepared as follows.
    The feed tank is filled with catalyst particles, for example, from the drums through the inlet port 17 Pulverized and smaller particles are removed by fluidizing the contents of the feed tank with gas oil, which enters through conduit 13 at a flow rate of 9 mm / s in the feed tank. The gas oil is discharged through line 14 in the upper part of the supply tank and passes into the tank 9 after filtration in the filter unit 15. After about 3 hours, the gas oil supply ends and the oil is removed from the supply tank. Smaller particles that have collected in the upper layer of the contents of the supply tank are then removed with a large vacuum cleaner.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR FILLING THE REACTOR with one or more homogeneous layers of solid particles with a diameter of 0.5-3 mm and a length of 3-7 mm by bringing the solid particles into fluidized state with a fluid flow and their subsequent deposition due to / by reducing the flow rate or stopping the flow, characterized in that, in order to more completely fill the reactor, before the deposition, the fluidization of the particles is carried out in the initial stage of expansion of the layer of less than 10%.
    类似技术:
    公开号 | 公开日 | 专利标题
    RU2635560C2|2017-11-14|Method of adsorption desulfurization of hydrocarbons and reactor apparatus for its implementation
    US4287088A|1981-09-01|Multi-stage fluidization and segregation of used catalyst fractions
    CN102292416B|2014-04-16|Systems and methods to remove liquid product and fines from a slurry reactor
    JP2935536B2|1999-08-16|Distillation tower reactor
    JP2001526587A|2001-12-18|Slurry hydrocarbon synthesis method by external product filtration
    US2726137A|1955-12-06|Process and apparatus for transfer of solid particles
    FI61040C|1982-05-10|ANORDING FOER UTFOERANDE AV ETT KONTINUERLIGT FOERFARANDE FOER KATALYTISK BEHANDLING AV KOLVAETEOLJOR
    SU1072791A3|1984-02-07|Method for filling reactor
    CN101842141A|2010-09-22|Magnetic separation combined with dynamic settling for fischer-tropsch processes
    CN101733045B|2012-04-18|Solid-liquid separation device and solid-liquid separation method for slurry bed reactor
    EP0008957B1|1983-01-26|Apparatus for transferring solids
    US3896026A|1975-07-22|Methods and apparatus for forming a dense phase catalyst transfer system
    EP0408669A1|1991-01-23|Improved method and apparatus for withdrawal of small catalyst particles in fcc systems.
    US4836914A|1989-06-06|Method for removing iron content in petroleum series mineral oil therefrom
    IL28626A|1971-08-25|Process and apparatus for clarifying contaminated liquids
    US5098230A|1992-03-24|Method for withdrawing a particulate solid from a packed, fluidized bed
    US2726136A|1955-12-06|Solid particle transfer process and apparatus
    US3409411A|1968-11-05|Apparatus for separating solids and loading reactor vessel
    US5238659A|1993-08-24|Moving granular bed dust removal and reaction apparatus
    US3825116A|1974-07-23|Particle disengaging and fines removal
    US2347747A|1944-05-02|Suspended catalyst technique
    CN102232008A|2011-11-02|Method and system for handling slurries of varying liquid rates and solids content
    CN103540342A|2014-01-29|Fluidized bed reactor applied to adsorption desulfurization and application thereof
    JPH1024232A|1998-01-27|Catalyst packing method and catalyst packing device
    JPS605214A|1985-01-11|Method and apparatus for removing crude oil sludge
    同族专利:
    公开号 | 公开日
    JPS5164475A|1976-06-03|
    DK463475A|1976-04-18|
    CH618104A5|1980-07-15|
    AU501353B2|1979-06-21|
    FR2330450A1|1977-06-03|
    AR208931A1|1977-03-15|
    CA1039249A|1978-09-26|
    FR2330450B1|1981-04-30|
    DK146757B|1983-12-27|
    IT1043395B|1980-02-20|
    AU8574775A|1977-04-21|
    BE834258A|1976-04-07|
    GB1523796A|1978-09-06|
    NL7413636A|1976-04-21|
    BR7506738A|1976-08-17|
    US4022255A|1977-05-10|
    NO146310B|1982-06-01|
    DK146757C|1984-06-04|
    DE2546244A1|1976-04-29|
    JPS596689B2|1984-02-14|
    ZA756528B|1976-09-29|
    NO753476L|1976-04-21|
    ES441790A1|1977-09-01|
    SE7511565L|1976-04-20|
    NO146310C|1982-09-08|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2902434A|1954-04-29|1959-09-01|Kellogg M W Co|Method of starting up a reforming process|
    US3392110A|1965-09-02|1968-07-09|Mobil Oil Corp|Method for the utilization of highly active hydrocarbon conversion catalysts|
    US3398085A|1965-09-14|1968-08-20|Hydrocarbon Research Inc|Catalyst addition and withdrawal process|NL8802570A|1988-10-18|1990-05-16|Eskla Bv|METHOD FOR START-UP, RESPECTIVE DEPARTMENT OF AN APPARATUS FOR OPERATING PHYSICAL AND / OR CHEMICAL PROCESSES, AND A SYSTEM FOR IT.|
    FR2812824B1|2000-08-10|2003-05-30|Total Raffinage Distribution|NOVEL METHOD FOR THE UNIFORM LOADING OF SOLID PARTICLES INTO AN ENCLOSURE|
    GB0115243D0|2001-06-21|2001-08-15|Kvaerner Process Tech Ltd|Method|
    US7560076B2|2004-08-18|2009-07-14|Geno Llc|Conversion of nitrogen dioxideto nitric oxide |
    US7618594B2|2004-08-18|2009-11-17|Geno Llc|Conversion of nitrogen dioxideto nitric oxide |
    FR2950822B1|2009-10-01|2012-02-24|Inst Francais Du Petrole|DEVICE FOR LOADING CATALYST PARTICLES IN TUBES HAVING AN ANNULAR AREA|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL7413636A|NL7413636A|1974-10-17|1974-10-17|PROCEDURE FOR FILLING A REACTOR WITH SOLID PARTICLES.|
    [返回顶部]