• 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:
    The process flow of the ammonia synthesis gas is continuously passed through at least three catalyst beds and the synthesis gas is reacted in the beds. In the heat exchangers disposed between each catalyst bed, the intermediate reaction of the partially reacted synthesis gas exiting the catalyst bed by heat exchange and recovery of the product ammonia-rich product effluent, Here, the process flow is the first raw material flow of the preheated synthesis gas through indirect heat exchange during the intermediate cooling of the partially converted synthesis gas before introduction into the first catalyst bed, and the two of the preheated synthesis gas by indirect heat exchange with the product effluent. Obtained by combining the first raw material stream and the third raw material stream of the synthesis gas to control the temperature of the process flow, where the first raw material flow is through heat exchangers located between the beds to cool the partially converted synthesis gas. A process for producing ammonia under high temperature and high pressure in a continuously passing ammonia reactor.
    公开号:KR19980081579A
    申请号:KR1019980014173
    申请日:1998-04-21
    公开日:1998-11-25
    发明作者:에릭앤드리어스갬
    申请人:죠르지오지롤라；할도르톱세아크티에셀스카브；
    IPC主号:
    专利说明:

    Method for producing ammonia and reactor
    The present invention relates to a method and a reactor for producing ammonia from a synthesis gas consisting of nitrogen and hydrogen by passing the synthesis gas through a large number of catalyst beds with intermediate cooling of the synthesis gas partially converted between the catalyst beds. In particular the invention relates to an improved process of this type and to the ammonia reactor used in the process, in which the cooling of the partially converted syngas is by indirect heat exchange with a single stream of fresh syngas.
    U. S. Patent No. 4,181, 701 discloses an ammonia reactor having a top and bottom catalyst bed and one of the beds equipped with a central heat exchanger. The process flow of the synthesis gas is divided into the raw material flows in the reactor, that is, the shell flow that cools the reactor shell, the exchange flow that cools the central heat exchanger, and the bypass to finally control the temperature of the process flow. Obtained by combining the flows.
    Moreover, indirect cooling of partially converted ammonia synthesis gas in a reactor having two or more catalyst beds is known in the art and commonly applied in the industry.
    Thus, the synthesis gas is indirectly cooled while passing fresh synthesis gas to the heat exchangers between the catalyst beds in a large number of separate streams. These flows are introduced through separate pipe connections installed in the reactor shell. The biggest drawback of the known ammonia production process of intermediate cooling of partially converted syngas in a heat exchanger between a large number of beds with separate gas streams is the need for a large number of inlet devices and complicated piping in the ammonia reactor. will be.
    It is therefore an object of the present invention to provide a process for the production of ammonia wherein intermediate cooling of partially converted synthesis gas in two or more catalyst beds is provided wherein the gas is cooled between catalyst beds by an indirect heat exchanger without the above drawbacks of known processes. It is.
    According to the above object, the present invention provides a method for producing ammonia under high temperature and high pressure in an ammonia reactor consisting of continuously passing the process flow of the ammonia synthesis gas into at least three catalyst beds and reacting the synthesis gas in the beds. to provide.
    This method intermediately cools the partially reacted synthesis gas exiting the catalyst bed by heat exchange in heat exchangers disposed between each catalyst bed and recovers the ammonia-rich product effluent, where the process flow is introduced into the first catalyst bed. The first raw material flow of the preheated synthesis gas through indirect heat exchange, the second raw material flow of the preheated synthesis gas by indirect heat exchange with the product effluent during the intermediate cooling of the partially converted synthesis gas, and the temperature of the process flow Obtained by combining the third feed stream of the synthesis gas to be controlled, where the first feed stream is passed continuously through heat exchangers located between the beds to cool the partially converted synthesis gas.
    A further object of the present invention is to use the method of the present invention having a simplified inlet and piping for the distribution of fresh syngas as a cooling medium in indirect heat exchange with partially reacted syngas between each catalyst bed. It is to provide an ammonia reactor for.
    Thus, the ammonia reactor according to the invention consists of a first, second and last catalyst bed which is arranged vertically at least about the coaxial axis and connected sequentially in a cylindrical pressure shell,
    An intermediate heat exchanger disposed between each catalyst bed for intermediate cooling of the ammonia synthesis gas partially converted from the catalyst bed by indirect heat exchange with the first feed stream of the fresh ammonia synthesis gas;
    A feed-effluent heat exchanger disposed at the outlet of the last catalyst bed to cool the ammonia product effluent stream by indirect heat exchange with a second feed stream of the ammonia synthesis gas;
    An inlet device for introducing the first raw material flow and an inlet device for introducing the second raw material flow into the reactor;
    An inlet device for introducing a third stream of fresh ammonia synthesis gas into the reactor;
    A device for passing the first, second and third feed streams to the top catalyst bed; And
    A device for coupling raw material flows to the process flow prior to introducing the process flow into the top catalyst bed,
    Here, the device for passing the first raw material flow is a passage for connecting the intermediate heat exchangers sequentially and for passing the first flow from the inlet device to the device for continuously combining the raw material flow through the intermediate heat exchanger. It is composed.
    1 is a schematic cross-sectional view of an ammonia reactor in accordance with certain embodiments of the present invention.
    The invention is explained in more detail in the following description with reference to the drawings, in which Figure 1 shows in schematic form a cross-sectional view of an ammonia reactor according to a particular embodiment of the invention.
    When operating the invention, fresh ammonia syngas 2 is introduced into an ammonia reactor 4 constructed in accordance with a particular embodiment of the invention. Syngas is introduced into three separate feed streams 6, 8 and 10 through inlets 16, 18 and 20 installed in the shell 12 of the reactor.
    The reactor 4 is composed of a top catalyst bed 24, a central catalyst bed 26 and a bottom catalyst bed 28 in a shell. Heat exchangers 30 and 32 between beds 24 and 26 and between beds 26 and 28 cool the partially diverted process flow 37 leaving the beds 24 and 26. To be arranged. A heat exchanger 34 disposed downstream of the lowermost catalyst bed 28 is used to cool the product effluent 38 exiting the bed 28.
    Fresh syngas is transported to bed 24 in process flow 36 and partially converted in bed 24. The partially converted syngas is then passed continuously through beds 26 and 28 in process flow 37. Nitrogen and hydrogen pass through the beds to exothermically react to form ammonia and the resulting effluent 38 is rich in ammonia. The product effluent 38 is cooled in the heat exchanger 34 by indirect cooling with the raw material stream 8 before being recovered from the reactor via the outlet 40.
    As mentioned above, the reaction between hydrogen and nitrogen is exothermic in the catalyst beds and the temperature of the process flow is raised. For thermodynamic reasons, the temperature of process flow 37 must be lowered prior to introduction into beds 26 and 28. Thus, it is cooled in the heat exchangers 30 and 32 by indirect heat exchange with the raw material stream 6 which is sequentially passed through the heat exchangers 32 and 30.
    By passing through the heat exchanger the feed streams 6 and 8 are preheated by indirect heat exchange as described above. The preheated raw material streams are then combined with the process stream upstream of the top catalyst bed 24. The temperature of process flow 36 before it is introduced to bed 24 is controlled by adding cold raw material flow 10.
    The process of the present invention, which intermediately cools the gas partially converted between the catalyst beds, passes a large number of catalyst beds into a synthesis gas of nitrogen and hydrogen to produce ammonia, thereby reducing the number of inlets and simplifying the piping. It saves reactor manufacturing cost and time and facilitates application to other processes.
    权利要求:
    Claims (2)
    [1" claim-type="Currently amended] In the method for producing ammonia under high temperature and high pressure in an ammonia reactor,
    The process flow of the ammonia synthesis gas is continuously passed through at least three catalyst beds and the synthesis gas is reacted in the beds.
    In the heat exchangers disposed between each catalyst bed, the intermediate reaction of the partially reacted synthesis gas exiting the catalyst bed by heat exchange and recovery of the product ammonia-rich product effluent,
    Here, the process flow is the first raw material flow of the preheated synthesis gas through indirect heat exchange during the intermediate cooling of the partially converted synthesis gas before introduction into the first catalyst bed, and the two of the preheated synthesis gas by indirect heat exchange with the product effluent. Obtained by combining the first raw material stream and the third raw material stream of the synthesis gas to control the temperature of the process flow, where the first raw material flow is through heat exchangers located between the beds to cool the partially converted synthesis gas. Passing continuously.
    [2" claim-type="Currently amended] Consists of a first, second and last catalyst bed which is arranged vertically and connected sequentially at least about the cavity axis in a cylindrical pressure shell,
    An intermediate heat exchanger disposed between each catalyst bed for intermediate cooling of the ammonia synthesis gas partially converted from the catalyst bed by indirect heat exchange with the first feed stream of the fresh ammonia synthesis gas;
    A feed-effluent heat exchanger disposed at the outlet of the last catalyst bed to cool the ammonia product effluent stream by indirect heat exchange with a second feed stream of the ammonia synthesis gas;
    An inlet device for introducing the first raw material flow and an inlet device for introducing the second raw material flow into the reactor;
    An inlet device for introducing a third stream of fresh ammonia synthesis gas into the reactor;
    A device for passing the first, second and third feed streams to the top catalyst bed; And
    A device for coupling raw material flows to the process flow prior to introducing the process flow into the top catalyst bed,
    Here, the device for passing the first raw material flow is a passage for connecting the intermediate heat exchangers sequentially and for passing the first flow from the inlet device to the device for continuously combining the raw material flow through the intermediate heat exchanger. The ammonia apparatus characterized by the above-mentioned.
    类似技术:
    公开号 | 公开日 | 专利标题
    US10464818B2|2019-11-05|Process for producing ammonia synthesis gas
    KR100547540B1|2006-03-23|Synthesis gas production by steam reforming using catalyzed hardware
    EP0504471B1|1994-08-31|Autothermal steam reforming process
    US7220505B2|2007-05-22|Autothermal reformer-reforming exchanger arrangement for hydrogen production
    EP0026057B1|1984-03-14|Synthesis reactor and processes
    US4904455A|1990-02-27|Production of synthesis gas using convective reforming
    AU2003248392B2|2010-06-17|Process and apparatus for the preparation of synthesis gas
    SU1215617A3|1986-02-28|Method of producing methane-containing gas
    KR960014902B1|1996-10-21|Reformation in a plate-fin exchanger
    US5180570A|1993-01-19|Integrated process for making methanol and ammonia
    EP0503482B1|1994-07-27|Autothermal steam reforming process
    RU2398733C2|2010-09-10|Converter system with maximum reaction speed for exothermic reactions
    DK167864B1|1993-12-27|Procedure and reactor system for reforming carbon hydroids during heat exchange
    US4618451A|1986-10-21|Synthesis gas
    KR890001963B1|1989-06-05|Apparatus and method for reforming hydrocarbons
    US7547332B2|2009-06-16|Apparatus for the preparation of synthesis gas
    US4152407A|1979-05-01|Process and apparatus for exothermic reactions
    AU597362B2|1990-05-31|Process and apparatus for the production of synthesis gas
    AU2004205368B2|2008-09-18|Methanol synthesis
    CA1327271C|1994-03-01|Autothermal production of synthesis gas
    US4180543A|1979-12-25|Ammonia synthesis reactor having parallel feed to plural catalyst beds
    CA1181571A|1985-01-29|Ammonia production process
    US6433029B1|2002-08-13|Methanol synthesis
    US4337170A|1982-06-29|Catalytic steam reforming of hydrocarbons
    US5181937A|1993-01-26|Apparatus for production of synthesis gas using convective reforming
    同族专利:
    公开号 | 公开日
    AU732110B2|2001-04-12|
    SK283645B6|2003-11-04|
    CN1202457A|1998-12-23|
    JP4093632B2|2008-06-04|
    DK44497A|1998-10-22|
    PL190731B1|2005-12-30|
    PL325910A1|1998-10-26|
    CA2235294C|2007-02-06|
    SK50098A3|1998-11-04|
    MX9802989A|1998-12-31|
    EA199800315A1|1998-10-29|
    DK173023B1|1999-11-15|
    CA2235294A1|1998-10-21|
    DE69806436T2|2003-01-16|
    EP0873972A2|1998-10-28|
    DE69806436D1|2002-08-14|
    KR100533345B1|2006-01-27|
    CZ293679B6|2004-06-16|
    EP0873972B1|2002-07-10|
    CZ121598A3|1998-11-11|
    CN1107028C|2003-04-30|
    UA45422C2|2002-04-15|
    ID20192A|1998-10-22|
    AT220387T|2002-07-15|
    JPH10310423A|1998-11-24|
    NO981764L|1998-10-22|
    NO321774B1|2006-07-03|
    EP0873972A3|1998-12-23|
    EA000611B1|1999-12-29|
    US6015537A|2000-01-18|
    AU6282898A|1998-10-22|
    TW422816B|2001-02-21|
    NO981764D0|1998-04-20|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    法律状态:
    1997-04-21|Priority to DK199700444A
    1997-04-21|Priority to DK444/97
    1997-04-21|Priority to DK0444/97
    1998-04-21|Application filed by 죠르지오지롤라, 할도르톱세아크티에셀스카브
    1998-11-25|Publication of KR19980081579A
    2006-01-27|Application granted
    2006-01-27|Publication of KR100533345B1
    优先权:
    申请号 | 申请日 | 专利标题
    DK199700444A|DK173023B1|1997-04-21|1997-04-21|Process and reactor for producing ammonia|
    DK444/97|1997-04-21|
    DK0444/97|1997-04-21|
    [返回顶部]