• 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:
    In a process for exothermic and heterogeneous synthesis, for example of ammonia, in which the synthesis gas is reacted in several catalytic beds (6, 7, 13) with axial-radial or only radial flow, said reaction gas is collected at the outlet from the last catalytic bed but one (7) and is transferred to a system for heat recovery (SAC) external to the reactor, and is re-introduced into the last catalytic bed (13).
    公开号:SU1632365A3
    申请号:SU894614489
    申请日:1989-06-26
    公开日:1991-02-28
    发明作者:Зарди Умберто；Пагани Джорждо
    申请人:Аммония Казале С.А. (Фирма)；Зарди Умберто；
    IPC主号:
    专利说明:

    The invention relates to a method for conducting exothermic heterogeneous synthesis, in which the reaction gas passes through a series of catalytic layers arranged one above the other separately and relative to each other and placed in a single reactor space, where the gas enters the next catalytic layer after passing through one catalytic layer.
    The aim of the invention is to increase the yield of the finished product and the productivity of the reactor.
    FIG. 1 shows a longitudinal section of the reactor; in fig. 2 - the same, with a radial course of gas.
    The reactor includes a housing 1, cassettes 2 with layers of catalyst 3-5.
    The reactor operates as follows.
    The source gas is fed into the reactor through its bottom part and passes from bottom to top through the space 6 between the inside of the wall of the housing 1 and the outside of the wall of the cassette 2, which allows reducing the minimum temperature. peraturu hull.
    The gas exiting the specified space in the upper-end of the cassette containing three catalytic layers fits into the tubes of the gas heat exchanger 7 located in the central part of the first catalytic layer 3 where it is preheated.
    the heat of the hot glow coming out of the first catalytic layer 3. The gas passes through the first catalytic layer 3 by a centripetal flow.
    After passing through the heat exchanger 7 along the external surfaces of the pipes, the hot gas enters the second catalytic layer 4 and passes through it in the form of an inward flow.
    The hot gas reacted in the second catalytic bed 4 is collected in cavity 8 and transferred
    After exiting the steam generator 10
    through the central pipeline 9, the gas enters the reactor through the pipe20
    25
    35
    axially positioned in relation to the reactor, directly to the steam generator 10, which is a system of pipe and shape, where part of the heat of reaction is removed to produce steam. The gas after the heat return returns directly to the reactor through the pipe 11, located outside the transfer pipe 9. The gas after the steam generator directly feeds the last catalytic layer 5, passing through it in the form of a flow directed radially outside.
    The hot reactor gas exiting Catalytic Layer 5 collects - Q with in the peripheral outer zone 12 of the catalytic layer and is again transferred to the central part of the reactor, passing through the space 13 of the double bottom 14 of the last catalytic layer. After that, the gas leaves the bottom of the reactor through line 15.
    In the reactor shown in FIG. 2, the gas passes through the catalytic layers of the axial-radial flow. ,,.
    The heat removal system according to the invention can be applied in reactors with catalytic beds in which the gas flows are completely radial. The system can also be used in reactors operating at lower pressures, in which space 6 is not provided, shown in FIG. 1, and the catalytic layers are in direct contact with the inner wall of the reactor body 1. In this case, the hot reactor gas exiting the catalytic layer 5 is again directed to the central part of the reactor through the space 13 formed between the bottom of the last catalytic station and the body.
    R this rrakpo (fig. 2) gas, coming out of the third on the reactor
    the wire 20 forming the space 19 and feeds the catalytic layer 5 through the space 21 formed by the closed bottom part 22 of the catalytic layer 5 and the bottom part 23 connected to the wall 17.
    The wall 17 in the upper part has a lid 24 which prevents the gas exiting the catalytic layer 4 from mixing with the gas feeding the catalytic layer 5. The gas from the catalytic layer 5 passes through the transfer pipe 9 and exits the reactor.
    权利要求:
    Claims (6)
    [1]
    1. A method for conducting an exothermic heterogeneous synthesis by passing a gas through a series of separate and consecutive catalytic layers placed
    in the same reactor volume, and removal of the finished synthetic gas, characterized in that, in order to increase the yield of the finished product, the gas emerging from the penultimate catalytic bed is removed from the reactor space, about 45 is passed through the outside of the steam generator and then introduced into the last catalytic layer, followed by removal from the reactor space.
    [2]
    2. A method according to claim 1, characterized in that the gas is passed through
    in the form of an axial radial or radial flow from the outside to the inside through the catalytic layers from the first to the last but one, and through the last layer - as a stream from the inside to the outside.
    [3]
    3. Reactor for carrying out exothermic heterogeneous synthesis,
    50
    323654
    layer 5 is fed into the steam generator through a space 16 formed between the wall of the cassette 2 and the new additional cylindrical wall 17 introduced next to the wall 18 for gas distribution, feeding the last catalytic layer 5 with a centripetal flow. After passing through the space 16, the gas passes through the space 19 and enters the U-shaped tubes of the steam generator 10.
    After exiting the steam generator 10
    5 gas enters the reactor through a pipe
    .
    the wire 20 forming the space 19 and feeds the catalytic layer 5 through the space 21 formed by the closed bottom part 22 of the catalytic layer 5 and the bottom part 23 connected to the wall 17.
    The wall 17 in the upper part has a lid 24 which prevents the gas exiting the catalytic layer 4 from mixing with the gas feeding the catalytic layer 5. The gas from the catalytic layer 5 passes through the transfer pipe 9 and exits the reactor.
    Invention Formula
    1. A method for conducting an exothermic heterogeneous synthesis by passing a gas through a series of separate and consecutive catalytic layers placed
    in one reactor volume, and removal of the finished synthesis gas, characterized in that, in order to increase the yield of the finished product, the gas exiting from the penultimate catalytic bed is removed from the reactor space, is passed through an external steam generator and then introduced into the last catalytic layer, followed by removal from the reactor space.
    2. A method according to claim 1, characterized in that the gas is passed through
    in the form of an axial radial or radial flow from the outside to the inside through the catalytic layers from the first to the last but one, and through the last layer - as a stream from the inside to the outside.
    3. Reactor for carrying out exothermic heterogeneous synthesis,
    5163
    including a housing in which an internal gas heat exchanger and baskets for catalytic beds are installed, located outside and connected to the housing by means of an outlet nozzle of a steam generator, characterized in that, in order to increase productivity, it is equipped with means for accumulating hot gas, from the second to last catalytic layer, a means to return the gas after the heat is taken in the steam generator to the inside of the housing for reaction in the last catalytic layer and the means to remove the gas collected the periphery of the last catalytic bed from the bottom of the reactor.
    [4]
    4. The reactor according to claim 3, which is also distinguished by the fact that the means for storing hot gas after the first catalytic layer is made in the form of a pipeline installed along the axis of the reactor, the lower end of the reactor is passed coaxially through the outlet of the steam generator, located perpendicular to the axis of the reactor, while providing a second pipeline, coaxial and external to the first pipeline.
    [5]
    5. Reactor on PP. 3 and 4, characterized in that the lower tritichesky basket is made with a double bottom, the space of which serves to collect and remove gas collected from the periphery of the last catalytic bed.
    [6]
    6. Reactor on PP. 4 and 5, characterized in that it is provided with an additional wall, which forms a channel with the wall of the cassette for gas distribution in the last catalytic bed.
    Fiel
    W outlet
    FIG. 2
    类似技术:
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    US3050377A|1962-08-21|Converter
    US4942022A|1990-07-17|Catalytic reactor
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    RU2588617C1|2016-07-10|Method for exothermic and endothermic catalytic processes for partial conversion of hydrocarbons and reactor set therefor
    KR810000264B1|1981-03-26|Radial-flow reactor for the synthesis of ammonia with production of high thermal-level system
    DE3374928D1|1988-01-28|Horizontal ammonia converter
    ES8305593A1|1983-05-01|Reactor for heterogeneous catalytic synthesis
    同族专利:
    公开号 | 公开日
    ES2030940T5|1996-03-16|
    CN1014032B|1991-09-25|
    EP0355303A1|1990-02-28|
    EP0355303B1|1992-04-01|
    CA1337735C|1995-12-19|
    DE68901115D1|1992-05-07|
    JPH0248032A|1990-02-16|
    CN1039539A|1990-02-14|
    US5152977A|1992-10-06|
    ES2030940T3|1992-11-16|
    EP0355303B2|1995-12-20|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    PL83843B1|1972-05-10|1976-02-28|Instytut Nawozow Sztucznychpo|
    IN165082B|1985-05-15|1989-08-12|Ammonia Casale Sa|
    CH670400A5|1986-03-13|1989-06-15|Ammonia Casale Sa|
    DE3783220T2|1986-11-03|1993-04-29|Ammonia Casale Sa|METHOD FOR REDUCING ENERGY NEEDS IN MULTIPLE UNIT REACTORS FOR HETEROGENEOUS SYNTHESIS AND RELATED REACTORS.|
    US4867959A|1986-11-20|1989-09-19|Santa Fe Braun, Inc.|Process for synthesizing ammonia|CH678286A5|1989-03-09|1991-08-30|Ammonia Casale Sa|
    AT198426T|1993-10-29|2001-01-15|Ammonia Casale Sa|METHOD FOR RETROFITTING A HETEROGENIC EXOTHERMAL SYNTHESIS REACTOR|
    US5427760A|1994-02-22|1995-06-27|Brown & Root Petroleum And Chemicals|Axial-radial reactors in the braun ammonia synloop with extrnal heat sink|
    US5948239A|1997-03-12|1999-09-07|Abb Lummus Global Inc.|Process for obtaining distillate fuel products using a multi-bed catalytic reactor|
    CN1170769C|1998-10-30|2004-10-13|霍尔多托普索埃公司|Process and converter for preparation of ammonia|
    CN103435006B|2013-08-20|2015-04-08|湖南安淳高新技术有限公司|High-CO high-conversion-rate isothermal shift reactor|
    DE102014219274A1|2014-09-24|2016-03-24|Siemens Aktiengesellschaft|Power plant for the production of energy and ammonia|
    US9751773B1|2017-02-07|2017-09-05|Hunan Anchun Advanced Technology Co., Ltd.|Ammonia synthesis system and method|
    CN109850918A|2018-12-17|2019-06-07|福州大学化肥催化剂国家工程研究中心|A kind of reactors for synthesis of ammonia and technique|
    CN109821355B|2019-03-15|2021-11-05|东北大学|Radial flow pressure swing adsorption bed and use method thereof|
    法律状态:
    2010-08-20| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: MM4A Effective date: 20080627 |
    优先权:
    申请号 | 申请日 | 专利标题
    CH245788|1988-06-27|
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