• 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 system to obtain an optimal distribution of the synthesis gas in catalytic beds for heterogeneous reactions in gaseous phases is, according to the invention, formed by a set of gas distributors for each catalytic bed, one for the inlet of the gas in the catalytic beds and one for the outlet of the gas, each distributor being made up of two cylindrical walls coaxial one to the other and with the axis of the cylindrical pressure vessel, and both being permeable to gas. The wall of the distributors closest to the catalytic bed is the one with the largest cross section (more permeable to gas), whereas the other wall of each distributor presents: a) a smaller cross section with respect to the wall nearer to the catalyst, but still large enough in order to limit the pressure drop through the same at least equal and not higher than three times (preferably not higher than one time) the pressure drop in the catalytic bed itself (in the gas inlet distributor); b) a narrow cross section (low permeability) narrow enough to create a pressure drop of at least (preferably at least four times) the pressure drop of the catalytic bed (in the outlet gas distributor).
    公开号:SU1741600A3
    申请号:SU874202223
    申请日:1987-03-12
    公开日:1992-06-15
    发明作者:Зарди Умберто
    申请人:Аммониа Казале С.А. (Фирма)；Умберто Зарди (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for carrying out heterogeneous catalytic reactions with the distribution of synthesis gas in catalyst beds in high-pressure cylindrical apparatus with an internal cartridge with a catalyst, which contains at least two layers in which the catalyst is placed. It is a two-cylindrical-permeable for gas, coaxial to each other and the axis of the high-pressure apparatus, the gas passing through the cataric, lytic layers with inward or outward radial flow e, either an inward or outward axial-radial flow, is distributed through the gas inlet and exhaust manifolds.
    Reactors are known which consist of a cylindrical high-pressure apparatus with an internal cartridge with a catalyst disposed in at least two layers, each layer representing two cylindrical walls permeable to gas and coaxial to each other and the axes of the high-pressure apparatus. The gas passes the aforementioned catalytic beds with inward or outward radial flow or inward or outward axial-radial flow and is distributed through gas inlet and outlet manifolds. Each manifold can be represented by a central pipeline, a high-pressure coaxial machine, the wall of which is
    2
    (Ј o o
     WITH
    permeable to gas on the inner wall of the catalytic layer, or the air space between the cylindrical wall permeable to gas and the non-perforated solid wall (exhaust gas manifold), or a double wall permeable to gas, one part of which has a large 17
    neck surface area is in contact with the catalyst layer directly or through a wire mesh substrate of the catalyst, and the other has a cross section for gas that is significantly lower than the first cross section and provides a concentrated pressure differential at least equal to the pressure differential of the catalyst layer, which contributes to uniform distribution of gas along the entire axial length of the layer,
    The most widely used reactors use distributors with a catalyst bed, the inlet manifold of which is represented by a double wall permeable to gas, with an inner part that is closer to the catalyst bed and an outer part with a smaller cross section for the passage of gas in which there is a significant pressure drop (higher than the pressure drop of the catalyst bed), therefore, special devices must be used to impart gas to a high velocity from the outer wall the speed limiter is a consequence of the reduced cross section of the outermost wall), the direction parallel to the walls of the distributor avoiding a direct collision with the permeable inner wall, which could cause an uneven distribution of gas in this layer and damage to the catalyst.
    In the above-mentioned reactors, the exhaust manifold does not provide any concentrated pressure drop, a uniform distribution of gas in the catalyst bed is achieved due to the pressure drop in the outer wall of the intake manifold.
    The aforementioned reservoir design requires a very efficient seal of the upper receiver of the bed, which must have high mechanical strength to maintain a large pressure drop.

    ,
    ten
    15
    25
    741600
    in order to avoid a state where a part of the gas is bypassing the catalyst bed.
    The purpose of the invention is to increase the efficiency of the process by more uniform distribution of gas.
    According to the proposed method, the pressure drop is controlled on the outer walls of the inlet and outlet valves (one gas inlet distributor in the catalyst beds and one gas distributor for gas release, each of which is formed by two cylindrical walls coaxial to each other and axes of the high pressure cylindrical apparatus). each dispenser are permeable to gas), while living
    The 2Q section of the distributors is selected depending on the magnitude of the pressure drop in the catalyst bed. Preferably, the living section of the outer walls of the distributors is chosen depending on the pressure drop at the inlet distributor to a range exceeding the pressure drop in the catalytic layer 1 - Zraza, and at the output one at least 2 times.
    Alternatively, the living section of the outer walls is selected depending on the pressure drop on the outer wall of the outlet dilator, equal to at least the pressure drop on the outer wall of the inlet distributor, which is limited to 0.9 pressure drop in the catalytic layer
    The method can be applied in reactors with a gas flow in radial or
    40 axial-radial directions in the catalytic beds and carried out with a set of distributors, one of which admits gas to the catalyst beds, and the other
    4S releases gas, each distributor being composed of two cylindrical walls coaxial to each other and the axis of a high-pressure cylindrical apparatus, and both walls are 50 permeable to gas.
    For carrying out the method according to the first embodiment, the living section of the outer walls of the distributors is chosen so that in the inlet gas distributor I, the outer wall is less permeable to gas than the inner wall closest to the catalyst to limit the pressure drop to one 30
    35
    55
    three times the pressure drop in the catalyst bed itself, and in the exhaust gas distributor, the permeability of the outer wall provides a pressure drop of 2 - k above the pressure drop in the catalyst bed. In the second embodiment, the living section of the outer walls of the distributors is chosen accordingly. distributor at least equal to the pressure drop on the outer wall of the inlet distributor, which is limited to 0.9 pressure drop in the catalytic layer
    Fig. 1 shows a cross section of a set of two catalytic beds with distributors providing a radial direction (to the center) of the gas flows; on the same, with the axial-radial direction of gas flows; in FIG. 3 the same, with opposite flow direction.
    FIG. schematically shows a set of two consecutive (one above the other) annular layers T and 2 with a radial (to the center) gas flow 3 in the layer, each of which is enclosed in a solid (non-perforated) cylindrical wall k and formed from two sets of distributors, one of which - external - consists of two coaxial gas-permeable cylindrical walls - the outer 5 and inner 6 (closest to the catalyst), and the inner wall 6 is more permeable to the gas than the outer wall 5, and the other is inner The inner (outlet) distributor consists of two coaxial cylindrical gas-permeable walls — an outer 7 and an inner 8; the inner (closest to the catalyst) wall 8 is more permeable to the gas than the outer wall 7 of the closed bottom 9 located in the limited space between wall 7 and the non-perforated wall 4, and the upper part (cover) 10, located in the confined space between the wall 8 and the non-perforated cylindrical wall, AND, being part of the means for. gas release.
     In this case, the walls of 5-8 reshade-lit fleet usually have an impenetrable
    ABOUT
    five
    for gas, the upper part 12. From figure 1 it can be seen that a larger amount of gas passes through the catalytic layers in the radial (to the center) flow in accordance with a large area of the living section of the distributors, and the rest (small) amount of gas passes through the catalytic layers in the axial flow in an enclosed area formed by the top 12, which are gas-tight
    Figure 2 shows a system with axially radial (to the center) gas flow through the catalyst, with the bottom part located in the zone bounded by walls 5 and 11, and the lid 10 is limited by walls k and 7 "Q 1, but with the opposite (from the center) radial direction of gas flow 3. In this embodiment, the function of the distributors 5 varies: the walls 7 and 8 become inlet, and the walls 5 and 6 - the outlet
    With a corresponding change in the direction of gas supply, the direction of radial flows in the system can also be changed in the same way.
    Example 1 In the ammonia synthesis reactor with two layers of catalyst (similar to figure 1) and an inwardly directed radial gas flow, the following operating conditions are realized: catalyst — irregular-shaped granules, 1.5–3 mm in size; hydraulic resistance (pressure drop) of gas in the catalyst bed, 0.015 kgf / cm2; the pressure drop on the wall 5 of the inlet distributor is 0.02 kgf / cm2 (the pressure drop on the wall 6 of the inlet distributor is insignificant and is not taken into account); the pressure drop on the wall 7 of the outlet distributor is 0.05 kgf / cm2 (the pressure drop on the wall 8 is insignificant).
    The excessive pressure on the cover 10 in the zone of the catalyst bed is negligible 0 (no compaction is required). The ratio of pressure drop on the walls of the distributors and in the catalyst bed is 1.3-1.3 °
    Example2. 8, an ammonia synthesis reactor, similar to that shown in Fig. 2, with three layers of an isatore bed and mainly with radial (to the center) gas flow and partially axial gas flow is carried out
    0
    the following operating conditions: catalyst - random-shaped granules, size 1.5 - 3 mm; gas pressure drop in the catalyst bed, 0.015 kg / / cm2; the pressure drop on the wall 5 of the inlet distributor is 0.015 kg / cm2 (the pressure drop on the wall 6 of the inlet distributor is negligible); the pressure drop on the wall 7 of the exhaust distributor is 0.06 kg / cm2 (the pressure drop on the wall 8 is negligible); ratio of pressure drops 1: 1:.
    Primer3 In the ammonia synthesis reactor of FIG. 3, a catalyst in the form of granules of 1.5–3 mm is used, with the pressure drop across the wall 7 of the inlet distributor 0.005 kg / cm 2, on the wall 5 of the outlet distributor 0.01 kg / cm 2, and the pressure differential in the catalyst bed with efm 0,015 kg / cm2o
    Here, the condition is satisfied that the pressure drop across the inlet distributor is less than the pressure drop across the outlet distributor and less than 0.9 pressure drop in the catalyst bed.
    Example1). In example 3, the pressure drop across the wall 7 of the inlet distributor is 0.075 kg / cm2 and is approximately equal to the pressure drop across the wall 5 of the outlet distributor. The pressure drop in the catalyst bed is 0.015 kg / cm2.
    Formula ie br
    ET

    e ni
    权利要求:
    Claims (3)
    [1]
    1. The method of carrying out heterogeneous catalytic reactions in cylindrical
    s
    0
    five
    0
    five
    0
    a high-pressure apparatus by pre-distributing by means of inlet and outlet distributors, each of which is formed by two coaxial cylindrical walls, and the subsequent passage of gas through at least two catalyst layers placed in the cartridge between two coaxially permeable gas permeable walls, radially or axially - a radial flow, characterized in that, in order to increase the efficiency of the process by more uniform distribution of the gas, the pressure drop regulate on the external walls of the inlet and outlet distribution, of the dividers, the living cross section of which is chosen depending on the magnitude of the pressure drop in the catalyst bed.
    [2]
    2, the method according to claim 1, characterized in that the living section of the outer walls of the distributors is chosen depending on the pressure drop at the inlet distributor to a range exceeding the pressure drop in the catalytic layer — 1-3 times, and at the inlet no less than than
    2 - k times.
    [3]
    3. The method according to claim 1, o t-l and h and y with the fact that the living section of the external walls of the distributors is chosen depending on the pressure drop on the external wall of the output distributor, equal to at least the pressure drop on the external wall inlet distributor, which is limited to 0.9 pressure drop in the catalytic hollow
    FI.2.
    Fa 3
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    同族专利:
    公开号 | 公开日
    CN1017970B|1992-08-26|
    EP0237888A2|1987-09-23|
    IN169405B|1991-10-12|
    CN87102931A|1987-10-21|
    CA1283525C|1991-04-30|
    CH670400A5|1989-06-15|
    EP0237888B1|1991-06-26|
    DE3770959D1|1991-08-01|
    EP0237888A3|1988-05-04|
    ES2022177B3|1991-12-01|
    US4849206A|1989-07-18|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DK119652B|1964-09-11|1971-02-08|Topsoe H|Reactor for performing gas phase reactions by passing a gas mixture through a bed filled with catalyst particles.|
    AT273054B|1964-09-11|1969-07-25|Haldor Frederik Axel Topsoe|Reactor for carrying out reactions in the gas phase|
    AT299981B|1970-04-21|1972-07-10|Chemie Linz Ag|Device for achieving uniform gas distribution in catalytic converter layers with radial flow in reactors for catalytic, exothermic high-pressure syntheses, preferably ammonia synthesis|
    US3944394A|1974-10-31|1976-03-16|Phillips Petroleum Company|Apparatus suitable for carrying out catalytic process|
    FR2365370B1|1976-09-22|1979-01-12|Charbonnages Ste Chimique|
    US4341737A|1979-05-22|1982-07-27|The Lummus Company|Apparatus for carrying out catalytic exothermic and endothermic high-pressure gas reactions|
    FR2460707B1|1979-07-13|1986-09-05|Ammonia Casale Sa|SYNTHESIS REACTOR, IN PARTICULAR FOR THE CATALYTIC SYNTHESIS OF AMMONIA AND METHANOL|
    IT1141102B|1980-11-28|1986-10-01|Ammonia Casale Sa|AXIAL-RADIAL REACTOR FOR HETEROGENEOUS SYNTHESIS|
    DE3171985D1|1981-04-15|1985-10-03|Uop Inc|Improved screen for collection and distribution of process streams and assembly of such screens|CH670578A5|1987-03-25|1989-06-30|Ammonia Casale Sa|
    ES2030940T5|1988-06-27|1996-03-16|Ammonia Casale Sa|PROCESS AND REACTOR FOR EXOTHERMAL HETEROGENOUS SYNTHESIS WITH SEVERAL CATALYTIC BEDS AND WITH EXTERNAL HEAT RECOVERY.|
    EP1818094A1|2006-02-13|2007-08-15|Ammonia Casale S.A.|Wall system for catalytic beds of synthesis reactors|
    EP2014356A1|2007-07-04|2009-01-14|Ammonia Casale S.A.|Wall system for catalytic beds of synthesis reactors and relative manufacturing process|
    CN105080434B|2014-04-18|2018-02-27|新特能源股份有限公司|A kind of catalytic reactor, system, the method for silicon tetrachloride catalytic hydrogenation|
    BR112019005684A2|2016-09-23|2019-06-11|Casale S A|catalytic axial-radial flow chemical reactor with two catalyst layers|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CH1025/86A|CH670400A5|1986-03-13|1986-03-13|
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