Converter for ammonia synthesis

专利摘要:
Ammonia converter for radial flow through two catalyst beds has a central heat exchanger mounted centrally in one of the beds. The process stream of synthesis gas is obtained by combining inside the converter separate feed streams: a shell stream serving to cool the converter shell, an exchange stream serving to cool the central heat exchanger, and a by-pass stream for final adjustment of the temperature of the process stream. The process stream passes in succession radially through the first catalyst bed in inwards direction through the central heat exchanger for being cooled, and radially through the second catalyst bed.
公开号:SU1037831A3
申请号:SU772461107
申请日:1977-03-09
公开日:1983-08-23
发明作者:Фредерик Аксель Топсее Хальдор；Анреас Гам Эрик
申请人:Хальдор Топсее А/С (Фирма)；
IPC主号:

专利说明:

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The invention relates to an ammonia synthesis envelope and can be used to implement ammonia synthesis methods at elevated pressure and temperature. Ammonia synthesis converters are known in the art and contain two or more separate catalyst layers in the building. The catalyst or between its layers is placed intermediate heat exchangers, which serve to maintain the optimal synthesis mode by cooling the reaction gas containing ammonia with cold synthesis gas supplied to the converter or other cooling agent Tl. The disadvantage of this type of envelope design is mainly the complication of the equipment and the increase in its size, since the built-in heat exchangers require a considerable amount of additional space for their placement. Other well-known technical solutions aimed at maintaining the optimal mode of ammonia synthesis consist in the fact that in the converter containing two or more catalyst layers, inlets are made between the layers to supply cold synthetic gas. The converter is closest to the one proposed. synthesis of ammonia, including a body with several inputs of synthesis gas, two annular catalyst layers with a radial distribution of the raw materials, located vertically one below the other and symmetrically to the central axis and having annular external e and inwardly of the gas flow passages, the intermediate tubular heat exchanger located along the central axis of the tube space of which is connected to one of the gas inlets and the preliminary heat exchanger Cs. The disadvantage of this converter is dilution of the reaction gas with unreacted synthesis gas, which leads to a decrease in the concentration of ammonia in the gases emitted from the converter, an increase in the volume of gases recirculated to the converter, and an increase in energy costs in the process of ammonia production. The purpose of the invention is to reduce energy costs by increasing the concentration of ammonia in the gases leaving the converter and reducing the volume of gases recirculated to the converter. This is achieved by the fact that a gas collector is made inside the converter to integrate all synthesis gas streams fed to the converter, connected to the outer annular channel of the first catalyst bed along the gas flow with the tube space of the intermediate heat exchanger and the preliminary heat exchanger. The preferred embodiment includes an input-synthesis gas in the pref: {: itelny teplomemnik in the form of an annular channel along the inner wall of the housing. FIG. 1 shows an embodiment of a converter with an integrated pre-heat exchanger; FIG. 2 - 4 - versions of NIN without integrated pre-heat exchanger. Converter for ammonia synthesis (figure 1) includes a housing 1 with inputs of synthesis gas 2-4, two layers of catalyst 5 and 6 with a radial distribution of raw materials, located vertically one below the other and symmetrically relative to the central axis and having external annular channels 7 and 8, internal gas channels 9 and 10, an intermediate heat exchanger 11, the tube space of which is connected to the gas inlet 3, and a preliminary heat exchanger 12. Inside the converter there is a gas manifold 13 connected to the annular channel 7 of the layer 5, with the tube space a intermediate heat exchanger X pre-heat exchanger 12. Channel 14 for supplying synthesis gas to the preliminary heat exchanger 12 is made annular and connected to the input of synthesis gas 2. According to FIG. 2, the converter is made without an integrated pre-heat exchanger 12, the annular channel 14 is connected to the intermediate heat exchanger 11, which therefore eliminates the gas inlet 3. In FIG. 3, the arrangement of the intermediate heat exchanger 11, which is located at the level of the second catalyst bed b, is changed, therefore the length of the supply gas channel is reduced, and the annular channel 10 is made with the help of partition 15. In FIG. 4 first in the course of the gas. The catalyst bed 5 is located above the bed and on the same level as the intermediate heat exchanger 11, which somewhat simplifies the design of the converter by eliminating the partition 16 shown in FIG. 2 and 3. The operation and operation principle of the converter is as follows. The process stream of synthesis gas, which passes through the layers of the ca-, Talis.ator, is formed in the collector 13 by combining all the syngas streams fed to the converter. These streams are fed through inlets 2-9 or 2 and 4, depending on the version used. In this case, one of the streams is always supplied along the internal stack of the housing through channel 14.
In this case, one of the streams is always fed into the collector 13 through the inlet 2 and the annular channel 14, and the other stream through the inlet 4 directly into the collector 13.
When using options with three streams, the third stream is fed into the tubes of the intermediate heat exchanger 11 through the input of FIGS. 1 and 4. In this case, the gas from the channel 14 passes to the collector 13 either directly or through the preliminary heat exchanger 12, where it is mixed with the synthesis gas stream, the output the heat from the tubes of the heat exchanger 11 and the gas supplied through the inlet 4. Further, the combined gas flow passes through the annular channel 7,
The catalyst bed 5, the annular channel 9, gets into the annular space of the heat exchanger 11, where it is cooled by gas passing inside the tubes, the annular channel 10 passes through, the second catalyst layer. 6, the annular channel 8 and out of the converter in the particular case (figure 1 through the tubes of the preliminary heat exchanger 12.
In the case of using two-flow variants, when the preliminary heat exchanger is excluded from the converter design, the gas flow from the channel 14 is directed to the tubes of the intermediate heat exchanger to cool the intermediate flow of the reaction gas leaving the first catalyst layer 5 through the channel 9. Further movement of the combined The flow of gas does not differ from that described above.
2
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权利要求:
Claims (1)
[1]
AMMONIA SYNTHESIS CONVERTER, comprising a housing with several synthesis gas inlets, several annular catalyst layers with a radial distribution of raw materials arranged vertically one below the other and symmetrically relative to the central axis and having annular external and internal gas channels, an intermediate tubular heat exchanger located along the central axis, the tube space of which is connected to one of the gas inlets, characterized in that, in order to reduce energy costs by increasing the concentration a MIAK in gases extending from the converter and to reduce the amount of gases recirculated to the converter within the converter is formed a gas manifold for combining all fed into the converter syngas streams, coupled with the outer annular channel of the first downstream gas catalyst bed, with the tubular space of the intermediate heat exchanger. ' *
10.37831

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法律状态:

优先权:

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申请号 | 申请日 | 专利标题

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GB9452/76A|GB1574723A|1976-03-10|1976-03-10|Apparatus for the synthesis of ammonia|

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