• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 优先权
    • 专利摘要:
    The invention relates to methods for adsorptive separation of gas mixtures used to produce a nitric mixture in the production of ammonia and hydrogen-rich fractions from petroleum gases and allowing an increase in the degree of separation of gases. The gas mixture of the three components is passed under increased pressure through the adsorbent layer and the stream enriched with the component with the lowest adsorption capacity is withdrawn. Then the pressure is reduced to an intermediate value, washed with a component with an average adsorption capacity in countercurrent to the direction of adsorption with the outlet from the flow layer enriched with the component with the highest adsorption capacity. The pressure is reduced to the lowest desorption pressure when the flow of residual desorbed gas flows in two directions: coinciding with the direction of adsorption in the layer section, which has absorbed the component with the highest adsorption capacity, and opposite in the area that absorbed the component with average adsorption capacity. At the lowest pressure, additional flushing is possible. The pressure is then increased to adsorption pressure. The method allows to obtain a nitrogen-hydrogen mixture containing 85% hydrogen. 1 hp f-ly, 4 ill. cl
    公开号:SU1722209A3
    申请号:SU864027875
    申请日:1986-08-01
    公开日:1992-03-23
    发明作者:Висснер Франк；Болькарт Альфред
    申请人:Линде Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for the adsorption separation of gas mixtures and can be used to produce a nitric mixture suitable for the synthesis of ammonia, or the separation of oil and gas gases into a hydrogen-rich fraction and a fraction of higher hydrocarbons. The invention can be used on installations containing, for example, from up to 1.2 adsorbers.
    The purpose of the invention is to increase the degree of separation.
    Figure 1 and 2 shows a diagram of the method of adsorption; Fig. 3 shows an installation for carrying out the method; figure 4 - scheme of the method.
    EXAMPLE 1 A gas mixture consisting of three components A, B, B is separated in an installation operating on the principle of using different pressures in separate stages. In this case, component B with the highest adsorption capacity is completely adsorbed, component B with an average adsorption capacity is partially adsorbed, and the flow of the target product containing component A with the lowest adsorption capacity and part of component B is diverted during the adsorption stage
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    at the output end of the adsorber. After the end of the adsorption stage, the zone adjacent to the inlet portion of the adsorber contains the adsorbed component B, and the next zone contains at least partially component B. In addition, component A is also contained in the adsorber mainly in the hollow spaces between the particles of the adsorbent. At the end of the adsorption stage, the pressure of the adsorption pressure, for example 25 bar, is firstly reduced, with the gas containing components A and B being withdrawn directly against the direction of adsorption. The gas released in this continuous flow depressurization is removed at several stages, the pressure of the adsorbers is first equalized and then the gas is used to rinse the other adsorbers. After reaching the final pressure, e.g. 4 bar, from the other adsorber, in which a direct depressurization stage occurs at that moment, wash gas is supplied to the outlet end of the adsorber, and a gas stream enriched with desorbed components is withdrawn at the inlet end. Rinsing at an intermediate pressure is continued until the largest part of component B is washed out of the adsorber, after which countercurrent depressurization of the adsorber to the lowest working pressure, for example 1.5 bar, is carried out. Then, at this pressure, it is preferable to further flush the gas withdrawn from the other adsorber, and the regeneration can be completed at this stage. After flushing is completed, the pressure in the adsorber is increased by conventional methods by equalizing the pressure, if necessary in several stages with adsorbers in which pressure must be removed, as well as by injecting the crude or target gas to achieve adsorption pressure.
    Since component B is adsorbed by the adsorbent and the gas released during the continuous discharge of pressure in other adsorbers contains relatively large amounts of component B, it is recommended to remove desorbed components from the middle zone of the adsorber during the second washing, As a result, the adsorber section is prevented from absorbing which is almost completely free of component B.
    Figure 1 and 2 shows the scheme of the method of adsorption using three adsorbers. Adsorber 1, in which, after the end of the adsorption stage, can be carried out
    Several stages of a continuous depressurization are connected to the adsorber 2 during the operation. In adsorber 2, flushing is performed simultaneously. After the end of washing II, the connection between the adsorbers is shut off and in the adsorber 2 pressure is released countercurrently to the direction of adsorption (step III). During this operation in the adsorber I, further continuous depressurization can be carried out, or it can remain in the state reached after the completion of operation I. This depends on the conditions of the adsorption process. After finishing in the adsor5 a bank 2 of the countercurrent depressurization III, it is again connected to the adsorber 1, in which further directing depressurization IV is carried out and which supplies the flushing gas for flushing at the lowest working pressure V to the adsorber 2 While after the end of washing V in the adsorber 2, the pressure is again increased in the usual way, in the adsorber 1 after the termination of operation IV, an intermediate pressure is reached, at which the first washing is carried out with gas evolved during continuous discharge detecting adsorber 3, which just is performed in step I. Then AD0 sorber 1 is carried out until the discharge pressure of the low working pressure (ill step), after which it was washed gas adsorber 3 which flows straight-through pressure relief IV. In this example
    5, both washing steps are carried out with a gas released from the same adsorber under direct-flow depressurization. However, it is possible to use gases from various sorbers for carrying out these steps.
    When the invention is carried out according to the scheme shown in Fig. 2, the washing stages at the lowest working pressure are eliminated, as a result of countercurrent
    5, pressure relief III is already undergoing sufficient desorption.
    The circuit according to Fig. 1 is generally simplified due to the fact that operations IV and V. do not occur.
    0 Example 2. In the installation of Fig. 3, consisting of successively included adsorbers 1-5, containing an active carbon layer as an adsorbent, the gas mixture of the composition (vol.%) Is subjected to separation:
    5 53 hydrogen (component with the lowest adsorption capacity), 30 nitrogen (component with an average adsorption capacity) and 17 carbon dioxide (component with the highest adsorption capacity), which in an amount of 100 Nm3 / h is fed by
    lines 6. As a result of carrying out the process according to the mode described below and shown in Fig. 4, 54.6 Nm3 / h of the target product containing 7 hydrogen and nitrogen in a volume ratio of 85:15 (carbon dioxide content is less than 0 , 01 vol.%), 30.8 nm / h of the composition gas flow (volume%) discharged through line 8: 13.4 hydrogen, 38.3 nitrogen and 48.3 carbon dioxide, 14.6 nm3 / h discharged lines 9 of the gas flow composition (vol.%): 16.9 hydrogen, 68.5 nitrogen and 18.7 carbon dioxide. Pos. 10 in fig.3 is designated a flow meter.
    The process according to the scheme of Fig. 4 is carried out in the installation of Fig. 3 as follows.
    After adsorption, indicated by BP, which is carried out at a pressure of 35 bar for 3.3 minutes, a four-stage pressure reduction is carried out, the first stage of pressure reduction, indicated by pos.1, is carried out to 23 bar within 30 seconds. The gas released in this process is used to carry out the indicated position. And the second stage of pressure increase (from 12 to 23 bar) in the adsorber passing through the indicated position Sh. The first stage of pressure increase (from 1.5 to 12 bar). Indicated poses. IV second stage of pressure reduction is carried out up to 12 bar for 30 seconds. The gas released in this process is used to carry out the first stage of pressure increase (stage III). At the designated nos.V of the third stage of pressure reduction (from 12 to 4 bar for 2 minutes), gas is released, which is used to carry out the adsorber’s labeled repetitive washing of the adsorber, marked as nos.VII, the fourth stage of pressure reduction (from 4 up to 3.5 bar for 1.3 minutes). At the countercurrent washing stage VI, a carbon dioxide-rich fraction is withdrawn from line 8. After the countercurrent washing VI is completed, side-stream II is withdrawn from the nitrogen-enriched fraction withdrawn from the process by line 9. At this stage, indicated by pos. VIII, the adsorber pressure is reduced to 1.5 bar for 0.8 minutes. Then the pressure is again increased to 23 bar in the manner described above. Subsequent pressurization in the adsorber to adsorption pressure (35 bar) is carried out at the designated position of the IX stage for 2.8 minutes with the aid of a portion of the desired product. Taking into account the hydrogen content in the initial mixture and in the target product, the hydrogen yield is 87.5%.
    If the above-described adsorption process is carried out in accordance with a known method, then 60.1 Nm3 / h of the desired product is obtained with a volume ratio of hydrogen and nitrogen of 75:25 (the content of carbon dioxide is less than 0.01% by volume) and 39.9 nm3 / h fractions of the composition (vol.%): 20 hydrogen, 37.4 nitrogen and 42.6 carbon dioxide.
    The yield of hydrogen is only 85%.
    As follows from example 2, the described method allows to obtain a nitric mixture containing 85% of hydrogen,
    against 75% of hydrogen in the known method, which indicates an increase in the degree of separation.
    权利要求:
    Claims (2)
    [1]
    1. A method of separating a gas mixture consisting of a component with the highest capacity for adsorption, a component with the lowest capacity for adsorption and a component with a medium capacity for adsorption, including passing the gas mixture under increased pressure through an adsorbent bed with diversion of the stream enriched with the component with the lowest capacity to adsorption, pressure reduction
    in the adsorbent layer to an intermediate pressure between the adsorption pressure and the lowest desorption pressure, washing the component of the initial gas mixture with a subsequent decrease in pressure to the
    low desorption pressure with removal from the adsorbent layer of residual gas to be desorbed and pressure increase to adsorption pressure, characterized in that, in order to increase the degree of separation, washing is carried out by a component with an average adsorption capacity fed countercurrently to the direction of adsorption, with removal from the layer adsorbent of the stream enriched with the component with the highest capacity for adsorption, and the subsequent decrease in pressure is carried out when the flow of residual desorbed gas flows in the direction coinciding with the direction Niemi adsorption on the bed section
    adsorbent, absorbed the component with the highest capacity for adsorption, and in the direction opposite to the direction of adsorption in the area of the layer of adsorbent that absorbed the component with average ability to adsorption.
    [2]
    2. A method according to claim 1, characterized in that at the lowest desorption pressure an additional washing is carried out.
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    引用文献:
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    GB1437600A|1972-05-17|1976-05-26|Boc International Ltd|Gas separation|
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    JPS5537293B2|1976-02-18|1980-09-26|
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