• 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:
    1503747 Alkylation apparatus UOP Inc 17 April 1975 [18 April 1974] 15842/75 Heading C5E [Also in Division Bl] In apparatus for acid catalysed alkylation reactions, reactants introduced through plurality of spray nozzles, e.g. 11, 12, 13 and connected to respective reactant inlets 19 and acid catalysts introduced from 9 are caused to pass upwardly in a serpentine path defined by baffles 10, heat being withdrawn by cooling coil 16. Thus, isobutane, 2 methyl butane, 2 methyl pentane, benzene, toluene and xylene, may be alkylated using C 3 -C 20 olefines. Catalysts may be hydrogen fluoride, phosphoric acid, aluminium chloride or boron fluoride.
    公开号:SU1099834A3
    申请号:SU752127182
    申请日:1975-04-18
    公开日:1984-06-23
    发明作者:Фрэнсиз Андерсон Роберт
    申请人:Юниверсал Ойл Продактс Компани (Фирма)；
    IPC主号:
    专利说明:


    with
    CX) 00: 4 f10 The invention relates to the construction of an apparatus for acid catalytic oxidation and can be used for the alkylation of hydrocarbons. A known apparatus comprising a housing within which an heat exchanging device is arranged axially, and in height in a checkerboard order reflector baffles lj are fixed. The disadvantage of this apparatus is that it is impossible to achieve contact between the acid and the reagents. Closest to the invention is an acid catalytic alkylation apparatus, comprising a vertically positioned housing with nozzles for supplying acid and discharging the reaction products, between which the device for injecting reagents, transverse partitions and heat exchanging device JJZJ are located along the height of the apparatus. A disadvantage of the known device is that it is impossible to intensify the process in it due to the counter-current movement of the phases. The aim of the invention is to intensify the process by providing countercurrent phase motion. In order to achieve this goal, an acid catalytic alkylation unit containing a vertically located case with ports for supplying acid and discharging reaction products, between which the device for injecting reagents, the transverse partitions and the heat exchanging device, are placed along the height of the apparatus, are placed in a checkered pore The reagent injection devices are installed above even or odd partitions and are made in the form of a multichannel nozzle, and the heat exchangers troystvo located along the axis of the apparatus. The drawing shows the device. The apparatus includes a housing 1, a lid 2, a bottom 3, inside the housing there is a y-squeeze-heat exchanging device 4 installed in the housing. In the lid 2 a separator is fixed on the partition 5, forming the inlet and outlet chambers for the heat carrier, the transverse partitions 6 are installed along the height of the housing placed in a staggered order, over which the devices 7 for injecting agents are arranged, made in the form of a multi-channel nozzle. The device works as follows. The refrigerant enters the upper part of the pipeline 8 and through the partition 5 is deflected and enters the heat exchanger 4 and exits the outlet chamber through the pipeline 9. The heat exchange device 4 shows a diagram of T1HF and can include several tubes or coils located inside the housing. Coolant, such as water, flows through conduit 8 at a rate sufficient to maintain a predetermined reaction temperature in the reaction chamber. The acid catalyst phase is supplied to housing 1 via conduit 10 and, being deflected from its original direction of movement by transverse partitions 6, passes in serpentine-like fashion through housing 1, exit from it through conduit 11. Partitions 6 to change the direction of flow are shown located inside housing 1 planes perpendicular to the longitudinal axis of the body. The transverse partitions 6 are substantially evenly distributed between the catalyst input through the pipeline 10 and the reaction product output through the pipeline 11 and have round segments like openings on opposite sides of the housing 1, whereby the flow of the catalyst phase deviates from one side to the other in a serpentine-like manner. Reagents from conduit 12 enter pipelines 13-16, from where they are then supplied through openings 17 for supplying reagents to units 7 for injecting reagents. The reactants are injected into the acid catalyst phase to form the acid-hydrocarbon dispersion in which the reaction takes place. The upward movement of the dispersion tends to prevent the separation of dispersed phases, and the multi-stage injection of reagents effectively enhances the dispersion of the phases at each stage. The acidic hydrocarbon dispersion, containing the acid catalyst, pea agents and reaction products, is discharged from housing 1 via conduit 11 and subjected to further processing steps, resulting in the reduction of the alkylated product. Heat generated during the reaction is absorbed by the cooling agent and removed by means of heat exchange 4 to such an extent that pre-determined temperature conditions for the reaction are maintained. The reagent injecting devices 7 are horizontal tubes having multiple spreading nozzles which form a phenoid-like spray in the downstream direction. The lower device 7 is made in the form of an annular tube and there are interconnected tubes intersecting in the form of an X. The annular tube is provided with multiple spray nozzles that spray liquid trickles downwards in the form of a cone. During the alkylation process, the reagents used are ideally combined to produce a hydrocarbon as the main product, the carbon content of which is equal to the sum of carbon atoms of the olefin and alkylating agent and which is known as monoalkylate. A suitable alkylating reagent can be a unsaturated hydrocarbon having a tertiary carbon atom, such as isobutane or higher homologous isobutane, such as 2-methylbutak, 2-methylpentane, and the like. Other useful alkylating agents include benzene, toluene, xylene, naphthenes, phenols, cresols, amines, and the like. Unsaturated (olefin) reagents that can be used with benefit include hydrocarbons with 3–20 carbon atoms in the molecule, halo alkyls, alcohols, alkyl sulfates, alkyl phosphate, etc. Mono-olefins are preferred, such as propene and butenes. Alkylation of paraffinic reagent with olefin occurs more effectively in the presence of an acid catalyst. Hydrohalic acids as well as other inorganic acids, such as phosphoric acid, aluminum chloride, boron fluoride and others, are suitable catalysts for preferred catalysts. The conditions for the alkylation reaction maintained in the reaction chamber include the reaction temperature O - and a pressure of 1-40 atm. The reaction temperature is one of the most important conditions, since it has a significant effect on the quality of the alkylation product. A temperature range of 80-100 ° C is preferred. The pressure does not have such an important effect on product quality and should be sufficient to maintain all hydrocarbons and acid catalyst in a liquid state. The volume ratio of acid catalyst to hydrocarbon, taking into account cooling during the reaction, is maintained within 0.5: 1 -2: 1 With a ratio lower than 0.5: 1, the efficiency of the process is significantly reduced, as undesirable reactions and the incompleteness of the desired reactions. There is also no increase in the yield of alkylate or an improvement in its quality with an increase in the ratio of more than 2: 1. It is also desirable to maintain a high ratio of the molar concentration of isoparaffin or aromatic hydrocarbon to the molar concentration of the olefin involved in the reaction to obtain high quality monoalkylate. The limits of this ratio are wide enough, about 6: 1 - 20: 1 with a preferred working interval of about 8: 1 - 16: 1. The proposed apparatus improves the quality of the alkylation product in comparison with known installations for carrying out an alkylation reaction by providing a better acid-hydrocarbon dispersion therein. A better dispersion improves the function of reducing the heat of the acid phase, also improves the homogeneity of the ratio of acid to hydrocarbon in the whole volume of the reaction chamber and reduces the fluoride content in the alkylate. The acid phase acts as a lowering of the reaction temperature, adsorbing the heat generated during exothermic alkylation reactions. Better dispersion increases the area of heat transfer and eliminates the appearance of hot spots inside the reaction chamber, which contribute to the appearance of undesirable reactions and undesirable by-products. Such side products remain mainly in the product and reduce the quality of the alkylate. Better dispersion improves the constancy of the ratio of acid to hydrocarbon throughout the reactor by reducing agglomeration (accumulation of individual phases). The fluoride content in the alkylation product is reduced if the co-tact between and partially pr-reacted hydrocarbons is improved, and this is more effectively achieved by extending the period of maintaining Persian acid-hydrocarbon dis-i.
    权利要求:
    Claims (1)
    [1]
    APPARATUS FOR ACID-CATALYTIC ALKYLATION, containing a vertically located case with nozzles for supplying acid and removal of reaction products, between which are devices for injecting reagents, transverse partitions and a heat exchanger located along the height of the apparatus, which requires intensification the process by providing countercurrent movement of the phases, the transverse partitions are staggered, devices for injecting reagents are installed over even or odd orodkami and formed as a multi-channel nozzle, a heat-exchanger device laid along the machine axis.
    S9
    Joint venture with>
    类似技术:
    公开号 | 公开日 | 专利标题
    RU2136358C1|1999-09-10|Method and device for temperature monitoring | and method for catalytic dehydrogeneration of hydrocarbons
    SU1099834A3|1984-06-23|Apparatus for acid and catalytical alkylation
    US2491618A|1949-12-20|Catalytic contacting apparatus
    US2720447A|1955-10-11|Contacting apparatus
    US6106789A|2000-08-22|Alkylation reactor with internal acid cooling zones
    US3133128A|1964-05-12|Contacting of fluids
    EA006358B1|2005-12-29|Flow distributor for an alkylation reactor or heat exchanger
    US7947232B2|2011-05-24|HF alkylation reactor
    US3212860A|1965-10-19|Method of and apparatus for contacting immiscible fluids
    US3501536A|1970-03-17|Alkylation with spiralling flow path of reactants and alkylate
    US3006739A|1961-10-31|Apparatus for contacting immiscible fluids
    US3108048A|1963-10-22|Apparatus for contacting of different density fluids
    US3249649A|1966-05-03|Catalytic alkylation
    US20160167012A1|2016-06-16|Ionic liquid reactor with heat exchanger
    JP3080403B2|2000-08-28|Turbulence process and production of monoalkyl aromatic hydrocarbons
    US3982903A|1976-09-28|Alkylation reaction chamber
    JP2678385B2|1997-11-17|Process for catalytic dimerization, codimerization or oligomerization of olefins by the use of self-regulating fluids
    US9000249B2|2015-04-07|Alkylation unit and process
    CA2007987A1|1990-08-22|Alkylation catalyst isolation
    US4000212A|1976-12-28|Unitary acid-hydrocarbon reactor in hydrocarbon alkylation
    US3469949A|1969-09-30|Alkylation apparatus forming an upwardly spiralling flow path of reactants
    US3160673A|1964-12-08|Hydrocarbon alkylation process
    US3426095A|1969-02-04|Process and apparatus for conducting a plurality of alkylation reactions within a single reactor
    US3914110A|1975-10-21|Alkylation reaction cooler
    US4024200A|1977-05-17|Countercurrent flow reaction chamber for plural stages of HF alkylation
    同族专利:
    公开号 | 公开日
    CA1051809A|1979-04-03|
    IT1035339B|1979-10-20|
    FR2267996A1|1975-11-14|
    FR2267996B1|1979-07-13|
    JPS50148302A|1975-11-27|
    RO64346A|1979-05-15|
    JPS5542048B2|1980-10-28|
    AR210327A1|1977-07-29|
    ES436486A1|1977-01-01|
    GB1503747A|1978-03-15|
    BR7502350A|1976-02-17|
    IN144650B|1978-06-03|
    US3914111A|1975-10-21|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2700768C1|2018-06-25|2019-09-20|Общество с ограниченной ответственностью "МилИнвест" |Sulfuric alkylation reactor|US2855449A|1954-03-12|1958-10-07|Phillips Petroleum Co|Method of and apparatus for the acid-catalyzed alkylation of hydrocarbons|
    US3006739A|1958-12-03|1961-10-31|Phillips Petroleum Co|Apparatus for contacting immiscible fluids|
    US3150934A|1960-01-14|1964-09-29|Texaco Inc|Apparatus for effecting fluidfluid contact|
    US3212860A|1962-03-23|1965-10-19|Phillips Petroleum Co|Method of and apparatus for contacting immiscible fluids|
    US3249649A|1963-02-28|1966-05-03|Phillips Petroleum Co|Catalytic alkylation|
    US3501536A|1969-02-26|1970-03-17|Universal Oil Prod Co|Alkylation with spiralling flow path of reactants and alkylate|
    US3560587A|1969-04-14|1971-02-02|Universal Oil Prod Co|Hydrogen fluoride alkylation with reaction cooler and reaction soaker vessels|
    US3607970A|1969-04-25|1971-09-21|Universal Oil Prod Co|Process for producing high octane alkylated hydrocarbons substantially free of alkyl fluoride compounds|
    US3705017A|1970-11-27|1972-12-05|Universal Oil Prod Co|Apparatus for a catalytic reaction|US3982903A|1974-04-18|1976-09-28|Universal Oil Products Company|Alkylation reaction chamber|
    US4024200A|1974-12-16|1977-05-17|Uop Inc.|Countercurrent flow reaction chamber for plural stages of HF alkylation|
    US4420462A|1982-03-22|1983-12-13|Clyde Robert A|Catalytic heat exchanger|
    JPH0577761B2|1985-04-09|1993-10-27|Hiroshi Yoshihara|
    US5227556A|1990-04-17|1993-07-13|The Dow Chemical Company|Turbulent flow process, monoalkyl aromatic production process and reactor for such process|
    DE102005049457A1|2005-10-15|2007-05-16|Degussa|Device for carrying out chemical reactions|
    US7947232B2|2006-12-07|2011-05-24|Exxonmobil Research & Engineering Company|HF alkylation reactor|
    US8747783B2|2009-06-24|2014-06-10|Uop Llc|Acid alkylation system and process for controlling temperature in a settler|
    US20110060178A1|2009-09-04|2011-03-10|Nafis Douglas A|Slurry column gasoline alkylation using gas phase olefin injection|
    FR3008627B1|2013-07-19|2017-02-24|Arkema France|THERMAL CONVERSION TANK USED IN ACETONE CYANOHYDRIN AMIDIFICATION PROCESS|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05462071|US3914111A|1974-04-18|1974-04-18|Alkylation reaction chamber|
    [返回顶部]