WO1999021639A1

WO1999021639A1 - Pressure swing adsorption process for separation of gas

Info

Publication number: WO1999021639A1
Application number: PCT/CN1998/000251
Authority: WO
Inventors: Jiaping Zhang; Hao Yang
Original assignee: Jiaping Zhang; Hao Yang
Priority date: 1997-10-24
Filing date: 1998-10-23
Publication date: 1999-05-06
Also published as: AU9619098A

Abstract

The invention relates to the pressure swing adsorption (PSA) process for separating or purifying one or more gas component from a feed gas mixture, so as to overcome the disadvantages such as low utilization ratio of adsorbent, high investment in system, insufficient recovery of product gas and high operational cost in prior art. M empty tanks are used in PSA system to avoid or reduce direct bed-to-bed pressure equalization and reduce restriction in operation between adsorbent beds. Thus, it is possible to reasonably arrange process flow so that with sufficient times to equalize pressure, adsorption is simultaneously carried out in more adsorbent beds. There are longer periods for regeneration. These result in higher utilization ratio of adsorbent and less dimension of equipments, pipes or valves. Finally, investement and operational cost decreased.

Description

变压吸附气体分离方法 Pressure swing adsorption gas separation method

发明领域 Field of invention

本发明涉及变压吸附气体分离方法，即一种改进的变压吸附气体分离或纯化方法。混合气体的组分分离和纯化的变压吸附法，是在较高压力下吸附容量大、在较低压力下吸附容量小的特性，由吸附塔吸附与解吸交替运行，从而是一种使气体分离和纯化循环进行的方法。吸附在较高压力下进行；解吸在较低压力或使用不易吸附组分冲洗或真空下进行，或者在二者甚至三者均需要的条件下进行解吸，有时还需要伴以加热。本说明书仅采用通常所说的冲洗变压吸附或真空变压吸附的方法来说明本发明。技术背景 The present invention relates to a pressure swing adsorption gas separation method, that is, an improved method for pressure swing adsorption gas separation or purification. The pressure swing adsorption method for separating and purifying the components of a mixed gas has the characteristics of large adsorption capacity at a higher pressure and small adsorption capacity at a lower pressure, and the adsorption tower and the desorption tower operate alternately, thereby making the gas Separation and purification cycle. Adsorption is carried out at a higher pressure; desorption is carried out at a lower pressure, or rinsed with a component that is not easily adsorbed or under vacuum, or under the conditions required by both or even three, and sometimes accompanied by heating. This specification uses only the so-called flushing pressure swing adsorption or vacuum pressure swing adsorption methods to illustrate the present invention. technical background

现有技术对于小型变压吸附 (PSA)制氮气或氧气的装置，通常采用两个吸附塔为一组交替吸附来取得产品。在这类装置中，当其中一个吸附塔处于吸附状态时，另一个吸附塔则处于再吸附准备过程。再吸附准备过程包括降压、冲洗、升压步骤。降压过程中，吸附剂中吸附的气体解吸，吸附剂恢复吸附能力。冲洗过程、抽空过程或抽空沖洗过程 (以下称再生过程），是为了使吸附剂更进一步得到解吸，并使吸附剂中易吸附的气体组分降低到某一浓度，以利于下一个吸附循环时，易吸附气体组分不会很快逸出吸附塔，由此使气体组分分离度提高。由于原料空气易得，上述两个吸附塔的再生过程中，一般不会对吸附塔吸附的有用气体以及死空间的有用气体作回收。两塔工作状态与时间的关系见表 1。表 1 二塔一进工艺

In the prior art, for a small-scale pressure swing adsorption (PSA) device for producing nitrogen or oxygen, two adsorption towers are usually used as a set of alternating adsorption to obtain products. In such a device, when one of the adsorption towers is in an adsorption state, the other adsorption tower is in a re-adsorption preparation process. The resorption preparation process includes steps of depressurization, flushing, and boosting. During the depressurization process, the gas adsorbed in the adsorbent is desorbed, and the adsorbent recovers the adsorption capacity. The washing process, evacuation process, or evacuation washing process (hereinafter referred to as the regeneration process) is to further desorb the adsorbent and reduce the easily adsorbable gas components in the adsorbent to a certain concentration, which is beneficial to the next adsorption cycle The easily adsorbable gas components will not escape the adsorption tower quickly, thereby improving the gas component separation. Due to the availability of raw air, the useful gas adsorbed by the adsorption tower and the useful gas in the dead space are generally not recovered during the regeneration of the two adsorption towers. The relationship between the working status and time of the two towers is shown in Table 1. Table 1 Two towers and one process

此表及后面表中符号意义如下： The meanings of the symbols in this table and the following tables are as follows:

A: 吸附 A: Adsorption

L: 降压、均压（或 P ) 结束后逆向或顺向降压， L: Reverse or forward pressure reduction after pressure reduction, equalization (or P),

1-NL: 第一次均压降至第 n次均压降， 1-NL: the first pressure equalization drops to the nth pressure equalization,

NR-1R: 第 n次均压升至第一次均压升， NR-1R: The nth equalizing pressure rise to the first equalizing pressure rise,

P:冲洗解吸时表示沖洗气流出，抽空解吸时表示 RR， P: indicates flushing air flow when flushing and desorbing, RR when flushing and desorbing,

PP: 抽空解吸或冲洗解吸或冲洗置换 PP: Evacuation or Rinsing Desorption or Rinsing Replacement

PPl-PPn: 冲洗解吸或冲洗置换或第一***至第 n***抽空解吸 FR:用非吸附相气或原料气或可与吸附相气混合之气最终升压 PPl-PPn: Flushing desorption or flushing replacement or evacuation and desorption of the first system to the nth system FR: Final pressure increase with non-adsorption phase gas or raw material gas or a gas that can be mixed with adsorption phase gas

RR: 隔离时间段（吸附塔保持前一状态） RR: Isolation period (adsorption tower remains in the previous state)

由于不回收降压过程流出的有用气体，对于原料气不易获得，或附加值高的原料气，上述流程不宜使用。为了回收降压过程流出的有用气体，通常采用两个以上的吸附塔一起工作，在吸附塔降压解吸过程中，设有吸附塔与吸附塔之间的一次或多次均压步驟，使降压解吸迓程: 出的 ¾用气体 Since the useful gas flowing out of the depressurization process is not recovered, it is not easy to obtain the raw material gas or the raw material gas with high added value, so the above process is not suitable for use. In order to recover the useful gas from the depressurization process, more than two adsorption towers are usually used to work together. In the desorption and desorption process of the adsorption tower, one or more pressure equalization steps between the adsorption tower and the adsorption tower are provided to reduce the pressure. Pressure desorption process: out of the gas

约原料和能量。以非吸附相作为产品时，还用降压过程流出的非吸附相气体直接冲洗需要再生的吸附塔，可以提高吸附剂吸附能力。常见的多塔变压吸附流程，举例如表 2-表 9所示：表 2 三塔一进一均工艺 About raw materials and energy. When the non-adsorbed phase is used as a product, the non-adsorbed phase gas flowing out of the depressurization process is also used to directly flush the adsorption tower that needs to be regenerated, which can improve the adsorption capacity of the adsorbent. The common multi-tower PSA process is shown in Table 2 to Table 9:

A 1L PP L 1R FR A 1L PP L 1R FR

1R FR A 1L PP L 1R FR A 1L PP L

1L PP L 1R FR A 表 3 四塔一进二均工艺

1L PP L 1R FR A Table 3 Four towers, one inlet and two equalization processes

表 4 五塔一进三均工艺

Table 4 Five towers one into three

表 5 六塔二进三均工艺

Table 5 Six-tower two-entry and three-average processes

表 6 七塔二进三均工艺

Table 6 Seven towers two into three

表 7 八塔二进三均工艺

Table 7 Eight-tower two-in-three-thin process

表 8 九塔三进四均工艺 Table 8.

表 9 十塔四进四均工艺

Table 9 Process

综观上述流程不难发现，吸附***的吸附塔数越多，可以实现的均压次数越多，就能越多地回收吸附塔均压降阶段流出的有用气体和能量。

Looking at the above process, it is not difficult to find that the more the number of adsorption towers in the adsorption system, the more equalization times that can be achieved, and the more useful gas and energy flowing out of the adsorption tower during the pressure drop stage can be recovered.

但表 2-9 所列变压吸附流程由于均压是在吸附塔之间直接进行，各塔的动作时间互相制约。对于任一流程而言，要保证吸附剂具有充足的再生时间，又增加均压次数，则不能增加同时进气的吸附塔数；或既增加均压次数，又增加同时进气吸附塔塔数，就难以保证吸附剂再生过程具有充足的时间，结果限制了吸附剂的利用率。 However, since the pressure swing adsorption processes listed in Table 2-9 are performed directly between the adsorption towers, the operation time of each tower is restricted. For any process, ensure that the adsorbent If there is sufficient regeneration time and the number of equalizing pressures is increased, the number of simultaneous adsorption towers cannot be increased; or if the number of equalizing pressures and the number of simultaneous intake adsorption towers are increased, it is difficult to ensure that the adsorbent regeneration process has sufficient As a result, the utilization of the adsorbent is limited.

Doshi在美国专利 US 4 , 340 , 398中公开了一种采用三个或多个吸附塔的变压吸附法，其中降压流出气不是从吸附塔出口端直接输送到另外的吸附塔，而是先输送到空罐，然后再将空罐中的气体输送到另外的吸附塔用于升压。但在流程中未安排多塔同时吸附，吸附剂利用率仍不高。 Doshi discloses a pressure swing adsorption method using three or more adsorption towers in U.S. Patent No. 4,340,398, in which the depressurized effluent gas is not directly sent from the exit end of the adsorption tower to another adsorption tower, but instead The gas is sent to the empty tank, and then the gas in the empty tank is sent to another adsorption tower for pressurization. However, no simultaneous adsorption of multiple columns was arranged in the process, and the utilization rate of the adsorbent was still not high.

中国专利申请公开 CN 1156637A公开了一种采用一个或一个以上的带折流板的外部气体贮槽，用于贮存在吸附塔降压过程中流出的气体，使不会出现返混现象，再用该气体经吸附塔出口端对吸附塔进行吹扫、均压和升压。这样流进塔的产品气纯度逐步增高，有利于提高产品的纯度和收率。但也没有安排使更多吸附塔同时处于吸附状态，由此吸附剂利用效率提高的幅度有限。 Chinese Patent Application Publication CN 1156637A discloses one or more external gas storage tanks with baffles, which are used to store the gas flowing out during the depressurization process of the adsorption tower, so that the phenomenon of back mixing does not occur. This gas is used to purge, equalize, and pressurize the adsorption tower through the exit end of the adsorption tower. In this way, the purity of the product gas flowing into the tower is gradually increased, which is beneficial to improving the purity and yield of the product. However, there are no arrangements for more adsorption towers to be in the adsorption state at the same time, so the improvement of the utilization efficiency of the adsorbent is limited.

中国专利申请公开 CN 1175474A描述了一种 N塔 (N≥5)的真空变压吸附工艺，其特点是采用 N - 2个吸附塔同时进行吸附，如此增加了吸附剂的吸附时间比。但是，由于其限制了解吸时间比，吸附剂的再生效果不好，因而吸附剂的实际利用效率并没有得到有效的提高。此外，该工艺仅有一次均压，对高压力吸附工艺的吸附塔流出气不能进行有效的直接回收，因此气体回收率受到限制。另外，由于真空泵不能直接对塔连续抽空，因而抽空效率不高。 Chinese Patent Application Publication CN 1175474A describes a vacuum pressure swing adsorption process with N towers (N≥5), which is characterized in that N-2 towers are used for simultaneous adsorption, which increases the adsorption time ratio of the adsorbent. However, due to its limitation on the absorption time ratio, the regeneration effect of the adsorbent is not good, so the actual utilization efficiency of the adsorbent has not been effectively improved. In addition, the process has only one pressure equalization, and the direct discharge of the effluent gas from the adsorption tower of the high-pressure adsorption process cannot be effectively recovered, so the gas recovery rate is limited. In addition, since the vacuum pump cannot directly evacuate the tower directly, the evacuation efficiency is not high.

中国专利申请公开 CN 1160598A公开了《六塔真空变压吸附气体分离工艺》的方法，吸附塔数量只限于 6 , 并且只能是真空变压吸附，同时处于吸附状态的塔数为 2(即塔数的 1/3), 吸附剂利用率不够高。 Chinese Patent Application Publication CN 1160598A discloses the method of "six-tower vacuum pressure swing adsorption gas separation process". The number of adsorption towers is limited to six, and it can only be vacuum pressure swing adsorption, and the number of towers in the adsorption state at the same time is two (that is, the tower 1/3), the utilization rate of the adsorbent is not high enough.

由上述内容不难理解，本领域迫切需要开发一种能够克服上述先有技术中存在的缺陷的气体的变压吸附分离方法。本发明的目的 It is not difficult to understand from the foregoing that there is an urgent need in the art to develop a pressure swing adsorption separation method of a gas that can overcome the defects in the prior art. Object of the invention

本发明旨在解决已有技术存在的吸附剂利用效率低、 ***设备投资高、有效气体回收率不够高和运行成本高的问题。 The present invention aims to solve the problems of low adsorbent utilization efficiency, high system and equipment investment, insufficient effective gas recovery rate, and high operating cost in the prior art.

本发明提供一种变压吸附气体分离方法，依照该方法，可以完全依据吸附剂特性，确定吸附塔数量为 2 ~ 24的任意数目，同时处于吸附状态的吸附塔数量可以为吸附塔总数的 1/3 ~ 2/3 , 能更好地满足各种吸附工艺的要求。本发明的技术方案 The invention provides a pressure swing adsorption gas separation method. According to the method, the number of adsorption towers can be determined to be any number from 2 to 24 based on the characteristics of the adsorbent, and the number of adsorption towers in the adsorption state can be 1 of the total number of adsorption towers. / 3 ~ 2/3, can better meet the requirements of various adsorption processes. Technical solution of the present invention

本发明的变压吸附气体分离方法包括： The pressure swing adsorption gas separation method of the present invention includes:

(1) .设有 N个吸附塔， N大于等于 2 , 其中有些吸附塔能同时处于吸附状态，使吸附塔同时处于吸附状态尽可能的多，以提高吸附剂的利用率； (1) There are N adsorption towers, N is greater than or equal to 2, and some of them can be in the adsorption state at the same time, so that the adsorption towers are in the adsorption state as much as possible at the same time to improve the utilization rate of the adsorbent;

(2) .设有 M个空罐， M大于等于 2，用于在吸附塔降压过程中与吸附塔均压，这种间接均压最多能进行 M次，避免或减少吸附塔间的直接均压，同时，回收吸附塔流出的气体，并由这些空罐供气给吸附塔最终充压前升压或冲洗，使吸附塔在工作时间上的相互制约減少，从而能合理安排流程，并能使均压次数增多，使同时处于吸附状态的吸附塔数目增加，最高可达总塔数的 2/3，脱附时间增长,并能按排吸附、冲洗、置换、抽真空、脱附或升压步骤连续进行； (2) There are M empty tanks, M is greater than or equal to 2, used to equalize the pressure with the adsorption tower during the pressure reduction process of the adsorption tower. This indirect pressure equalization can be performed at most M times to avoid or reduce the direct between the adsorption towers. At the same time, at the same time, the gas flowing out of the adsorption tower is recovered, and these empty tanks supply gas to the adsorption tower to increase the pressure or flush before the final charging, so that the mutual constraints on the working time of the adsorption tower are reduced, so that the process can be reasonably arranged, and It can increase the number of equalizing pressures, increase the number of adsorption towers in the adsorption state at the same time, up to 2/3 of the total number of columns, the desorption time increases, and can be adsorbed, washed, replaced, evacuated, desorbed or desorbed in rows. The step-up step is performed continuously;

(3) .优选的 N为 2-24 ； (3). Preferred N is 2-24;

(4) .最好的同时处于吸附状态的塔数为 N/3-2N/3； (4). The best number of columns in the adsorption state at the same time is N / 3-2N / 3;

(5) .优选的 M为 2-18； (5). Preferred M is 2-18;

(6) .在冲洗、置换搡作时，设置成 1-12小***，使气体组份不同的冲洗、置换气体能分阶段对吸附塔工作； (6) During the flushing and replacement operation, a 1-12 small system is set up so that the different flushing and replacement gas components can work on the adsorption tower in stages;

(7) .在***抽空解吸操作时，分 1-12个相对独立的小***，使其中各个抽空***能连续对吸附塔抽空； (7). When the system is degassed and desorbed, it is divided into 1-12 relatively independent small systems, so that Each of the evacuation systems can continuously evacuate the adsorption tower;

(8) .抽空操作分 1-12个小步骤，处于各小步骤时，吸附塔与不同的抽空***相连，这样能使各抽空***连续、直接对吸附塔抽空，并在不同的抽空***出口获得不同组份的气体； (8) The evacuation operation is divided into 1-12 small steps. At each small step, the adsorption tower is connected to different evacuation systems, so that each evacuation system can continuously and directly evacuate the adsorption tower and exit at different evacuation systems. Obtaining different component gases;

(9) .吸附塔升压过程中，部分或全部空罐中的气体可从吸附塔的出口或其入口流入吸附塔； (9) During the pressurization of the adsorption tower, part or all of the gas in the empty tank can flow into the adsorption tower from the exit of the adsorption tower or its inlet;

(10) .整个工艺流程中的全部装置能连续恒流量地最终升压，省去因最终升压不连续而设计的原料气或吸附流出气緩冲罐。 (10). All devices in the entire process can be continuously boosted at a constant constant flow rate, eliminating the need for a feed gas or adsorption outflow gas buffer tank designed for the discontinuous boost.

本发明所述的变压吸附包括：冲洗变压吸附、真空变压吸附、变温变压吸附、真空变温变压吸附。 The pressure swing adsorption of the present invention includes: flushing pressure swing adsorption, vacuum pressure swing adsorption, temperature swing pressure swing adsorption, vacuum temperature swing pressure adsorption.

本发明使用空罐贮存吸附塔降压流出气。空罐数量、体积尺寸，主要取决于吸附压力、放空初压、吸附塔体积、被吸附组份解吸性能以及产品气体浓度要求。吸附塔数量的确定，按照吸附剂的性能以及气体处理要求来定。 The present invention uses an empty tank to store the depressurized effluent gas from the adsorption tower. The number of empty tanks and the size of the tank are mainly determined by the adsorption pressure, the initial pressure of venting, the volume of the adsorption tower, the desorption performance of the adsorbed components, and the product gas concentration requirements. The number of adsorption towers is determined according to the performance of the adsorbent and the requirements for gas treatment.

对于变温变压吸附，是在吸附塔降压步骤后，升压步骤前，增加或同时执行升温。降温步骤是在升温结束以后进行 For temperature and pressure swing adsorption, the temperature increase or increase is performed simultaneously after the pressure reduction step of the adsorption tower and before the pressure increase step. The cooling step is performed after the heating is completed

对于真空变温变压吸附，是在吸附塔降压步骤后，升压步骤前，增加或同时执行升温。降温步骤是在真空步骤后增加或同时执行。本发明的效果 For vacuum temperature and pressure swing adsorption, the temperature increase is increased or performed simultaneously after the pressure reduction step of the adsorption tower and before the pressure increase step. The cooling step is performed after or simultaneously with the vacuum step. Effect of the invention

本发明的变压吸附气体分离方法，具有如下的突出优点和效果： The pressure swing adsorption gas separation method of the present invention has the following outstanding advantages and effects:

1. 本发明是对中国专利申请公开 CN1160598A的改进，是一种既能够使装置有足够的均压次数，又能使同时处于吸附状态塔数足够多，还能使吸附剂再生时间充足的设计方法，采用本设计方法，可使吸附剂实际使用效率较现有技术提高很多。 1. The invention is an improvement on the Chinese patent application publication CN1160598A, and is a design that can not only make the device have a sufficient number of pressure equalizations, but also make the number of towers in the adsorption state sufficient at the same time, and also make the adsorbent regeneration time sufficient Method: By adopting the design method, the actual use efficiency of the adsorbent can be greatly improved compared with the prior art.

2. 本发明在变压吸附工艺流程中，设计了能使吸附塔总数中的三分之一至三分之二的吸附塔同时处于吸附状态，使吸附剂利用率提高，使被吸附气体组份在相同时间内的被吸附气体量增多。已有技术由于过多兼顾吸附塔与吸附塔之间的相互均压与直接协调，不可能也未想到，采用本发明的设计方法来实际提高在相同时间、相同吸附剂量的条件下的吸附气体量。同时，如中国专利申请公开 CN1175474 , 虽然采用 N-2个吸附塔同时处于吸附状态，却没有也不可能给吸附剂的解吸留下充足的时间，而且该变压吸附工艺因没有采用本发明的设计方法，因此，在吸附压力较高时，无法有效地回收吸附塔降压过程流出的有用气体。 2. In the pressure swing adsorption process of the present invention, the One-third to two-thirds of the adsorption towers are in the adsorption state at the same time, which improves the utilization rate of the adsorbent, and increases the amount of the adsorbed gas component in the same time. In the prior art, due to too much consideration of mutual equalization pressure and direct coordination between the adsorption tower and the adsorption tower, it is impossible and unexpected to adopt the design method of the present invention to actually improve the adsorption gas at the same time and the same adsorption dose. the amount. At the same time, as in Chinese Patent Application Publication CN1175474, although N-2 adsorption towers are used in the adsorption state at the same time, there is no and it is impossible to leave sufficient time for the desorption of the adsorbent, and the pressure swing adsorption process does not use the invention. The design method, therefore, when the adsorption pressure is high, the useful gas flowing out of the depressurization process of the adsorption tower cannot be effectively recovered.

3. 本发明的分离方法中，设计了 1个或多个空罐回收吸附塔降压过程流出的气体，分阶段地回收不同组份的流出气，并将空罐气体用于吸附塔升压或沖洗，由此协调吸附塔之间的配合。设计多个空罐似乎会使设备总投资增加，但事实恰恰相反，这样设计会使吸附塔流出气中的有用气体回收更多，能量回收也更多，并可減小吸附设备的尺寸、节省其它大型緩冲罐以及价格昂贵的吸附剂，从而使整个变压吸附装置的总投资降低。 3. In the separation method of the present invention, one or more empty tanks are designed to recover the gas flowing out of the depressurization process of the adsorption tower, recover the effluent gas of different components in stages, and use the empty tank gas for the pressure increase of the adsorption tower. Or flush, thereby coordinating the cooperation between the adsorption towers. It seems that designing multiple empty tanks will increase the total equipment investment, but the opposite is true. This design will recover more useful gas and more energy from the effluent gas of the adsorption tower, and reduce the size and savings of the adsorption equipment. Other large buffer tanks and expensive adsorbents reduce the total investment for the entire PSA plant.

4. 本发明的分离方法中在吸附塔降压时，首先与空罐均压后，最多保留一次吸附塔与吸附塔之间的直接均压，这样有利于使最终升压气体量在任何时间保持稳定。 4. In the separation method of the present invention, when the adsorption tower is depressurized, first, after equalizing the pressure with the empty tank, the direct equalization pressure between the adsorption tower and the adsorption tower is retained at most once, which is beneficial to the final pressurized gas amount at any time. keep it steady.

5. 本发明的分离方法中设计了 1-12个冲洗、置换***，目的在于，吸附塔可以使用多种组份气体分阶段冲洗、置换，有利于达成连续沖洗、置换，并节省用气量。 5. In the separation method of the present invention, 1 to 12 flushing and replacing systems are designed. The purpose is that the adsorption tower can use multiple component gases to flush and replace in stages, which is beneficial to achieving continuous flushing and replacing, and to save gas consumption.

6. 本发明的分离方法中设计了 1-12 个抽空***，目的在于，吸附塔需要真空抽吸时，可以使真空***直接、连续对塔抽空，不需要设置真空蓄能器。 6. In the separation method of the present invention, 1 to 12 evacuation systems are designed. The purpose is that when the adsorption tower needs vacuum suction, the vacuum system can be evacuated directly and continuously without the need for a vacuum accumulator.

7. 本发明的分离方法中设计了每个吸附塔抽空步骤分作 1-12 个小步骤，吸附塔与不同的抽空***相连，这样可以使各抽空*** 连续对塔抽空，并可在不同的抽空***出口获取不同组分的气体。 8. 本发明的分离方法中设计了将均压流出气含较多易吸附组份的空罐气体从吸附塔进口端均压入的方法，有利于克服均压次数太多，造成的吸附前沿较早突破的弊端，从而保证不会由于增加均压次数而使气体分离纯化效果差。另外，与吸附流出气组份相近或相同的空罐气体则仍由吸附塔出口端均压入，这有利于吸附前沿的回推。 7. In the separation method of the present invention, it is designed that each evacuation step of the adsorption tower is divided into 1-12 small steps, and the adsorption tower is connected to different evacuation systems, so that each evacuation system can continuously evacuate the tower, and can be used in different The evacuation system exits to obtain gases of different components. 8. In the separation method of the present invention, a method for equalizing the pressure of the empty tank gas containing the more easily adsorbable components from the equalized effluent gas from the inlet end of the adsorption tower is designed to overcome the number of equalization pressures, leading to the adsorption front The shortcomings of earlier breakthroughs ensure that the gas separation and purification results will not be poor due to the increase in the number of pressure equalizations. In addition, the empty tank gas that is similar to or the same as the component of the adsorption effluent gas is still uniformly pushed in from the outlet end of the adsorption tower, which is beneficial to the pushback of the adsorption front.

9. 本发明的分离方法中设计了连续最终充压过程的目的，是使原料气或吸附流出气，作为充压气体时，流量不产生波动，由此可省去相应的緩沖罐。 9. The purpose of the continuous final pressurization process in the separation method of the present invention is to make the raw gas or the adsorbed outflow gas, as the pressurized gas, the flow does not fluctuate, thereby eliminating the corresponding buffer tank.

10.采用本发明，对于必需采用多塔变压吸附工艺的大型气体分离，由于吸附剂利用率的提高，可大大降低吸附剂的用量，吸附设备相应减小，虽然使用多个空罐，也不会使占地面积增加。 10. With the present invention, for large-scale gas separation that requires a multi-tower pressure swing adsorption process, the use of the adsorbent can be greatly reduced due to the increased utilization of the adsorbent, and the adsorption equipment is correspondingly reduced. Although multiple empty tanks are used, Does not increase the footprint.

11.本发明采用了 M个用作间接均压的空罐，可以将每一个步序的时间，按照吸附剂的特性需要加长或缩短，而不用强迫其他步序时间相应增长或缩短，整个***时序编排变得容易而且合理。均压次数的确定，不再受到吸附塔数量的限制，而是设计人按照吸附剂的吸附与解吸特性来确定，这样一来，可以通过最大限度的设计均压次数，以提高有用气体收率。同时，吸附剂再生时间与吸附时间之比也可大大提高，有利于吸附剂每次吸附容量的提高。再则，可以将吸附剂同时处于吸附状态的比例尽可能提高，更进一步加强了单位时间、单位体积吸附剂的气体处理能力。由此，对于相同的气体处理量，相同的气体回收率， ***投资将大大减少。同理，相同的投资，可以处理更多的气体，而且，气体回收率也将得到提高。 11. The present invention adopts M empty tanks used as indirect equalizing pressure, which can lengthen or shorten the time of each step according to the characteristics of the adsorbent, without forcing other steps to increase or shorten the corresponding time. The entire system Timing is easy and reasonable. The determination of the number of equalization pressures is no longer limited by the number of adsorption towers, but the designer determines according to the adsorption and desorption characteristics of the adsorbent. In this way, the maximum number of pressure equalizations can be designed to improve the useful gas yield . At the same time, the ratio of the regeneration time of the adsorbent to the adsorption time can also be greatly improved, which is conducive to the increase of the adsorption capacity of the adsorbent each time. Furthermore, the proportion of the adsorbent in the adsorption state can be increased as much as possible, which further enhances the gas processing capacity of the adsorbent per unit time and unit volume. Therefore, for the same gas treatment volume and the same gas recovery rate, the system investment will be greatly reduced. By the same token, the same investment can process more gas, and the gas recovery rate will be improved.

原有表 2 ~表 9的技术，吸附塔之间的直接均压必须相互对应，由此导致某些步序的时间长度不能完全按照吸附剂本身的特性来确定，而必须受到其他步序时间的制约；均压次数必须按照吸附塔个数和同时进原料气吸附塔个数来确定，而不能完全按照吸附剂的吸附与解吸特性来确定. 12. 依照本发明的分离方法，对于五塔以上的***，依照本发明的分离方法，编排时序表时，很容易得到连续终充、连续沖洗、连续抽空的效果；也可以很容易地将冲洗、真空再生分为单***、双***、多***等。但在实际设计时是否使用这些特点，应该按照吸附剂的特性来确定。 In the original Tables 2 to 9, the direct equalization pressures between the adsorption towers must correspond to each other. As a result, the length of some steps cannot be completely determined according to the characteristics of the adsorbent itself, but must be affected by other steps. The number of equalizing pressures must be determined according to the number of adsorption towers and the number of simultaneous feed gas adsorption towers, but not completely based on the adsorption and desorption characteristics of the adsorbent. 12. According to the separation method of the present invention, for a system with more than five towers, according to the separation method of the present invention, it is easy to obtain the effects of continuous final charge, continuous flushing, and continuous evacuation when programming the timetable; it can also be easily flushed. The vacuum regeneration is divided into single system, dual system, and multiple systems. However, whether these characteristics are used in actual design should be determined according to the characteristics of the adsorbent.

13. 依照本发明的分离方法，能够容易地使***可以共用的程控阀门更多。 13. According to the separation method of the present invention, it is possible to easily make more program-controlled valves that the system can share.

14. 依照本发明的分离方法，可以容易地使吸附塔均压降流出气体从吸附塔入口端均压流入，而并不更多地需要程控阀门。这对于低压阶段均压流出气体中含有较高吸附相气体浓度的工艺来说，气体分离效果将更好，有用气体回收率将更高。 14. According to the separation method of the present invention, it is possible to easily make the pressure drop of the adsorption tower outflow and the gas to flow in uniformly from the inlet end of the adsorption tower without requiring more program-controlled valves. For a process with a higher concentration of adsorbed phase gas in the equal-pressure effluent gas at the low pressure stage, the gas separation effect will be better and the useful gas recovery rate will be higher.

由上所述，采用本发明的分离方法来确定工艺流程，可以使单位时间、单位体积的吸附剂，气体处理能力较以往的技术提高很多。因此，我们可以减少吸附剂的使用量，相应减少吸附塔重量。如果采用连续终充，对于从非吸附相得到产品的工艺流程，还可以取消非吸附相产品緩冲罐，而且非吸附相产品气体流量可以比已有技术更稳定。 From the above, using the separation method of the present invention to determine the process flow can make the adsorbent per unit time and unit volume, and the gas treatment capacity is greatly improved compared with the prior art. Therefore, we can reduce the amount of adsorbent used and correspondingly reduce the weight of the adsorption tower. If continuous final charging is used, for the process of obtaining products from the non-adsorbed phase, the buffer tank for the non-adsorbed phase product can also be eliminated, and the gas flow of the non-adsorbed phase product can be more stable than the existing technology.

为了更清楚地说明本发明，给出下列实施例，但其对本发明并无任何限制。 In order to explain the present invention more clearly, the following examples are given, but they do not limit the present invention in any way.

实施例 1 Example 1

本发明的一种变压吸附气体分离纯化方法，其流程如表 10所示。吸附塔数 2 , 同时处于吸附状态的塔数是 1，均压次数是 N ( 2 - 1 8 ), 冲洗与最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 10. The number of adsorption towers is 2, the number of columns in the adsorption state at the same time is 1, the number of equalizing pressures is N (2-1 8), and the flushing and the final pressure increase are discontinuous.

实施例 2 Example 2

本发明的一种变压吸附气体分离纯化方法，其流程如表 11所示。吸附塔数 3，同时处于吸附状态的塔数是 1 , 均压次数是 N ( 2 - 1 8 ), 塔对塔冲洗与最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 11. The number of adsorption towers is 3, the number of columns in the adsorption state at the same time is 1, and the number of equalizing pressures is N (2-1 8). The column flushing and the final pressure increase are discontinuous.

实施例 3 本发明的一种变压吸附气体分离纯化方法，其流程如表 12所示。吸附塔数 3 , 同时处于吸附状态的塔数是 1 , 均压次数是 N ( 2 ~ 1 8 ) + 1 (一次直接均压），塔对塔冲洗与最终升压不连续。 Example 3 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 12. The number of adsorption towers is 3, the number of columns in the adsorption state at the same time is 1, and the number of equalizing pressures is N (2 ~ 1 8) + 1 (one direct equalizing pressure). The column flushing and the final pressure increase are not continuous.

实施例 4 Example 4

本发明的一种变压吸附气体分离纯化方法，其流程如表 13所示。吸附塔数 3 , 同时处于吸附状态的塔数是 2 , 均压次数是 N ( 2 - 1 8 ), 冲洗与最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 13. The number of adsorption towers is 3, the number of simultaneous adsorption towers is 2, the number of equalizing pressures is N (2-1 8), and the flushing and final pressure increase are discontinuous.

实施例 5 Example 5

本发明的一种变压吸附气体分离纯化方法，其流程如表 14所示。吸附塔数 4，同时处于吸附状态的塔数是 2，均压次数是 N ( 2 - 1 8 ), 塔对塔冲洗不连续，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 14. The number of adsorption towers is 4, the number of columns in the adsorption state at the same time is 2, and the number of equalizing pressures is N (2-1 8).

实施例 6 Example 6

本发明的一种变压吸附气体分离纯化方法，其流程如表 15所示。吸附塔数 4,同时处于吸附状态的塔数是 2，均压次数是 N( 2 - 1 8 ), 冲洗连续，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 15. The number of adsorption towers is 4, the number of columns in the adsorption state at the same time is 2, the number of equalizing pressure is N (2-1 8), the flushing is continuous, and the final pressure increase is discontinuous.

实施例 7 Example 7

本发明的一种变压吸附气体分离纯化方法，其流程如表 16 所示。吸附塔数 5 , 同时处于吸附状态的塔数是 2，均压次数是 N ( 2 - 1 8 ) + 1，塔对塔冲洗连续，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 16. The number of adsorption towers is 5, the number of columns in the adsorption state at the same time is 2, the number of equalizing pressures is N (2-1 8) + 1, the column is flushed to the column continuously, and the final pressure increase is not continuous.

实施例 8 Example 8

本发明的一种变压吸附气体分离纯化方法，其流程如表 17所示。吸附塔数 5 , 同时处于吸附状态的塔数是 2，均压次数是 N ( 2 - 1 8 ), 冲洗连续，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 17. The number of adsorption towers is 5, the number of columns in the adsorption state at the same time is 2, the number of equalizing pressure is N (2-1 8), the washing is continued, and the final pressure increase is continuous.

实施例 9 Example 9

本发明的一种变压吸附气体分离纯化方法，其流程如表 18所示。吸附塔数 6 , 同时处于吸附状态的塔数是 2，均压次数是 N ( 2 - 1 8 ) + 1，塔对塔冲洗不连续，最终升压连续。实施例 1 o A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 18. The number of adsorption towers is 6, the number of columns in the adsorption state at the same time is 2, the number of equalizing pressures is N (2-1 8) + 1, the column-to-column flushing is discontinuous, and the final pressure increase is continuous. Example 1 o

本发明的一种变压吸附气体分离纯化方法，其流程如表 19所示。吸附塔数 6 , 同时处于吸附状态的塔数是 3，均压次数是 N ( 2 - 1 8 ), 双***连续洗，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 19. The number of adsorption towers is 6, the number of columns in the adsorption state is 3 at the same time, and the number of equalizing pressures is N (2-1 8). The two systems are continuously washed, and the final pressure increase is discontinuous.

实施例 1 1 Example 1 1

本发明的一种变压吸附气体分离纯化方法，其流程如表 20所示。吸附塔数 6 , 同时处于吸附状态的塔数是 3，均压次数是 N ( 2 - 1 8 ) + 1，塔对塔不连续沖洗，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 20. The number of adsorption towers is 6, the number of towers in the adsorption state at the same time is 3, and the number of equalizing pressures is N (2-1 8) + 1.

实施例 1 2 Example 1 2

本发明的一种变压吸附气体分离纯化方法，其流程如表 21所示。吸附塔数 6 , 同时处于吸附状态的塔数是 3，均压次数是 N ( 2 - 1 8 ), 连续冲洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 21. The number of adsorption towers is 6, the number of columns in the adsorption state at the same time is 3, the number of equalizing pressures is N (2-1 8), continuous washing is performed, and the final pressure increase is continuous.

实施例 1 3 Example 1 3

本发明的一种变压吸附气体分离纯化方法，其流程如表 22所示。吸附塔数 7 , 同时处于吸附状态的塔数是 3 , 均压次数是 N ( 2 - 1 8 )，连续冲洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 22. The number of adsorption towers is 7, the number of columns in the adsorption state at the same time is 3, the number of equalizing pressures is N (2-1 8), the continuous washing is performed, and the final pressure increase is continuous.

实施例 1 4 Example 1 4

本发明的一种变压吸附气体分离纯化方法，其流程如表 23所示。吸附塔数 7 , 同时处于吸附状态的塔数是 4，均压次数是 N ( 2 - 1 8 ), 连续沖洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 23. The number of adsorption towers is 7, the number of columns in the adsorption state at the same time is 4, the number of equalizing pressures is N (2-1 8), continuous washing is performed, and the final pressure increase is continuous.

实施例 1 5 Example 1 5

本发明的一种变压吸附气体分离纯化方法，其流程如表 24所示。吸附塔数 8，同时处于吸附状态的塔数是 3 , 均压次数是 N ( 2 - 1 8 ) + 1，连续冲洗，最终升压连续。 A method for separating and purifying a PSA gas according to the present invention is shown in Table 24. The number of adsorption towers is 8, the number of columns in the adsorption state at the same time is 3, the number of equalizing pressures is N (2-1 8) + 1, continuous washing is performed, and the final pressure increase is continuous.

实施例 1 6 Example 1 6

本发明的一种变压吸附气体分离纯化方法，其流程如表 25所示。吸附塔数 8 , 同时处于吸附状态的塔数是 4 , 均压次数是 N ( 2 - 1 8 ), 连续冲洗，最终升压连续。实施例 1 7 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 25. The number of adsorption towers is 8, the number of columns in the adsorption state at the same time is 4, the number of equalizing pressures is N (2-1 8), continuous washing is performed, and the final pressure increase is continuous. Example 1 7

本发明的一种变压吸附气体分离纯化方法，其流程如表 26所示。吸附塔数 8 , 同时处于吸附状态的塔数是 5 , 均压次数是 N ( 2 - 1 8 ), 不连续冲洗，最终升压不连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 26. The number of adsorption towers is 8, the number of columns in the adsorption state at the same time is 5, the number of equalizing pressures is N (2-1 8), the discontinuous washing is performed, and the final pressure increase is discontinuous.

实施例 1 8 Example 1 8

本发明的一种变压吸附气体分离纯化方法，其流程如表 27所示。吸附塔数 9 , 同时处于吸附状态的塔数是 4 , 均压次数是 N ( 2 - 1 8 ), 连续冲洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 27. The number of adsorption towers is 9 and the number of adsorption towers at the same time is 4. The number of equalizing pressures is N (2-1 8).

实施例 1 9 Example 1 9

本发明的一种变压吸附气体分离纯化方法，其流程如表 28所示。吸附塔数 9，同时处于吸附状态的塔数是 5 , 均压次数是 N ( 2 - 1 8 ), 连续沖洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 28. The number of adsorption towers is 9, the number of columns in the adsorption state at the same time is 5, the number of equalizing pressures is N (2-1 8), continuous washing is performed, and the final pressure increase is continuous.

实施例 2 0 Example 2 0

本发明的一种变压吸附气体分离纯化方法，其流程如表 29所示。吸附塔数 8 , 同时处于吸附状态的塔数是 4 , 均压次数是 N ( 2 - 1 8 ), 双***连续抽空，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 29. The number of adsorption towers is 8 and the number of adsorption towers is 4 at the same time. The number of equalizing pressures is N (2-1 8). The dual systems are continuously evacuated, and the final pressure increase is continuous.

实施例 2 1 Example 2 1

本发明的一种变压吸附气体分离纯化方法，其流程如表 30所示。吸附塔数 6，同时处于吸附状态的塔数是 3,均压次数是 N( 2 ~ 1 8 ), 连续抽真空。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 30. The number of adsorption towers is 6, the number of columns in the adsorption state at the same time is 3, and the number of equalizing pressures is N (2 ~ 1 8), and the vacuum is continuously evacuated.

实施例 2 2 Example 2 2

本发明的一种变压吸附气体分离纯化方法，其流程如表 31 所示。吸附塔数 16, 同时处于吸附状态的塔数是 10, 均压次数是 7，连续沖洗，最终升压连续。 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 31. The number of adsorption towers is 16, while the number of adsorption towers at the same time is 10, the number of equalizing pressures is 7, continuous flushing, and the final pressure increase is continuous.

实施例 23 Example 23

本发明的一种变压吸附气体分离纯化方法，其流程如表 32 所示。吸附塔数 23, 同时处于吸附状态的塔数是 13，均压次数是 7，连续冲洗，最终升压连续。 O 99/21639 实施例 24 A pressure swing adsorption gas separation and purification method of the present invention is shown in Table 32. The number of adsorption towers is 23, the number of towers in the adsorption state at the same time is 13, the number of equalizing pressures is 7, continuous washing, and the final pressure increase is continuous. O 99/21639 Example 24

本发明与已有技术比较例的投资、消耗、气体收率，如表 33 所示。 The investment, consumption, and gas yield of the comparative examples of the present invention and the prior art are shown in Table 33.

表 10 二塔一进 N均工艺

Table 10 Two towers and one N process

表 11 三塔一进 N均工艺

Table 11 Three towers and one N process

表 12 三塔一进 N + 1均工艺 Table 12: Three towers and one N + 1 process

表 13 三塔二进 N均工艺

Table 13 Three tower binary N process

表 14 四塔二进 N均工艺一

Table 14 Four tower binary N process

表 15 四塔二进 N均工艺二

Table 15 Four tower binary N process

表 16 五塔二进 N + 1均工艺一

表 17 五塔二进 N均工艺二

Table 16 Five towers binary N + 1 process 1

Table 17 Five tower binary N process two

表 18 六塔二进 N + 1均工艺

Table 18 Six-bin binary N + 1 process

表 19 六塔三进 N均工艺

表 20 六塔三进 N + 1均工艺二

Table 19 Six towers and three into N process

Table 20 Six towers and three into N + 1

表 21 六塔三进 N均工艺二

Table 21: Six towers, three inlets, and two N processes

表 22 七塔三进 N均工艺

表 ²³ 七塔四进 N均工艺 Table 22 Seven towers and three into N process

Table ²³ Seven towers and four into N

表 24 八塔三进 N均工艺 * Table 24: Eight-tower three-entry N-average process *

*·· 将 NL与 NR之间增加 N + 1L/R史盖可得 N + 1均 ― 表 25 八塔四进 N均工艺 * * ·· Increase N + 1L / R between NL and NR to obtain N + 1 both-Table 25 Eight-Pole Quadruple N-Pipe Process *

表 26八塔五进 N均工艺 *

Table 26: Eight towers, five-entry and N-all processes *

将 NL与 NR之间增加 N + 1LR交盖可得 N + 1均表 27 九塔四进 N均工艺

表 28 九塔五进 N均工艺

Add N + 1LR between NL and NR to get N + 1

Table 28 Nine towers and five-entry N process

表 29 八塔四进 N均真空工艺

Table 29 Eight towers and four into N are vacuum process

表 30 六塔三进 N均真空工艺 * Table 30 Six-column three-entry N-all vacuum process *

*:本表中 P表示用产品气体冲洗， PP表示真空抽吸吸附塔. 表 31 十六塔十进 7均冲洗工艺 *: In this table, P means flushing with product gas, PP means vacuum suction adsorption tower. Table 31 Washing process

表 32 二十三塔十三进 7均冲洗工艺 Table 32 Twenty-three towers, thirteen inlets and seven flushing processes

r- w r- w

表 33 处理气量 7000NM³/H压力 0.8Mpa变换气脱碳装置投资消耗对照 Table 33 Comparison of investment and consumption of processing gas volume 7000NM ³ / H pressure 0.8Mpa shift gas decarburization unit

有效气体回收率分离 1000NM3变换气中 C02 工艺特点 VOL½ 相对投资消耗 Effective gas recovery rate Separation of C02 process characteristics in 1000NM3 conversion gas VOL½ Relative investment consumption

H2 N2 CO 工业冷却水电耗 (%) 已有技术四塔一进二均 96 82 85 0.8吨 12KWH 100 本发明例四塔二进七均 98 90 95 0.65吨 8KWH H2 N2 CO Industrial cooling water Power consumption (%) Existing technology

已有技术六塔二进七均 98 90 95 0.65吨 8K H Existing technology Six towers, two into seven, 98 90 95 0.65 tons 8K H

本发明例六塔三进七均 98 90 95 0.65吨 8KWH Example of the invention Six towers, three entrances and seven entrances 98 90 95 0.65 tons 8KWH

Claims

权利要求 Rights request

1. 一种变压吸附气体分离方法，其特征在于，所述的变压吸附包括：沖洗变压吸附、真空变压吸附、变温变压吸附、真空变温变压吸附；所述的分离方法是：设有 N个吸附塔， N大于等于 2 , 同时设有 M个空罐， M大于等于 2 , 空罐用于在吸附塔降压过程中与吸附塔最多进行 M次间接均压，回收吸附塔流出的气体，并由这些空罐供气给吸附塔最终充压前升压或冲洗，避免或减少吸附塔间直接均压，使各吸附塔操作时间上相互制约减少，使均压次数增加，而且使同时处于吸附状态的吸附塔数目增加，最高可达总塔数的 2/3，脱附时间增长，并能安排吸附、冲洗、置换、抽真空、脱附或升压步骤连续进行。 A method for pressure swing adsorption gas separation, characterized in that the pressure swing adsorption includes: flushing pressure swing adsorption, vacuum pressure swing adsorption, temperature swing pressure swing adsorption, vacuum temperature swing pressure swing adsorption; and the separation method is : There are N adsorption towers, N is greater than or equal to 2, and there are M empty tanks, M is greater than or equal to 2, the empty tanks are used to perform at least M indirect pressure equalization with the adsorption tower during the pressure reduction process of the adsorption tower to recover the adsorption. The gas flowing out of the tower is supplied from these empty tanks to the adsorption tower to increase the pressure or flush before the final charging, to avoid or reduce the direct equalization pressure between the adsorption towers, to reduce the mutual constraints on the operation time of each adsorption tower, and to increase the number of equalization Moreover, the number of adsorption towers in the adsorption state is increased up to 2/3 of the total number of towers, the desorption time is increased, and the adsorption, washing, displacement, vacuum, desorption or boosting steps can be arranged to be performed continuously.

2. 按照权利要求 1所述的分离方法，其特征在于，所述的吸附塔数 N为 2 ~ 24。 2. The separation method according to claim 1, wherein the number N of the adsorption columns is 2 to 24.

3. 按照权利要求 1所述的分离方法，其特征在于，所述的空罐数 M为 2 ~ 18。 3. The separation method according to claim 1, wherein the number M of empty cans is 2-18.

4. 按照权利要求 1所述的分离方法，其特征在于，所述的同时处于吸附状态的吸附塔数为吸附塔总数 N的 1/3 - 2/3。 4. The separation method according to claim 1, characterized in that the number of the adsorption towers simultaneously in the adsorption state is 1/3-2/3 of the total number of adsorption towers N.

5. 按照权利要求 1所述的分离方法，其特征在于，所述的沖洗、置换操作可设置成 L个小***， L为 1 ~ 12 , 使气体组分不同的冲洗、置换气体能分阶段对吸附塔工作。 5. The separation method according to claim 1, wherein the flushing and replacing operations can be set into L small systems, where L is 1 to 12, and the flushing and replacing gases with different gas components can be divided into stages. Work on adsorption tower.

6. 按照权利要求 1所述的分离方法，其特征在于，所述的*** 抽空解吸操作可分作 K个相对独立的小***， K为 1 ~ 12，这样能使各抽空***连续对吸附塔抽空，不需设置真空蓄能设备。 6. The separation method according to claim 1, wherein the system evacuation and desorption operation can be divided into K relatively independent small systems, where K is 1 to 12, so that each evacuation system can continuously contend with the adsorption tower. Evacuation, no need to set up vacuum energy storage equipment.

7. 按照权利要求 1所述的分离方法，其特征在于，所述的抽空操作可以分作 I个小步骤， I为 1 ~ 12 , 处于各小步骤时，吸附塔与不同的抽空***相连，这样能使各抽空***连续、直接对塔抽空，并可在不.同的抽空***出口获取不同组分的气体。 7. The separation method according to claim 1, wherein the evacuation The operation can be divided into I small steps, I is 1 ~ 12, in each small step, the adsorption tower is connected to different evacuation systems, so that each evacuation system can be continuously and directly evacuated to the tower, and can be different. The evacuation system exits to obtain gases of different components.

8. 按照权利要求 1所述的分离方法，其特征在于，所述的吸附塔升压过程中，部分或全部空罐中的气体可从吸附塔出口端流入吸附塔或从进口端流入吸附塔。 8. The separation method according to claim 1, wherein during the pressurization of the adsorption tower, part or all of the gas in the empty tank can flow from the exit end of the adsorption tower into the adsorption tower or from the inlet end into the adsorption tower. .

9. 按照权利要求 1所述的分离方法，其特征在于，可设置全装置连续恒流量最终升压。 9. The separation method according to claim 1, wherein a continuous constant flow rate of the whole device is finally set to finally increase the pressure.