CN215610414U

CN215610414U - Wash gas separation purification system that regeneration effect is stable

Info

Publication number: CN215610414U
Application number: CN202121798006.XU
Authority: CN
Inventors: 殷文华; 党凯; 吴巍; 李克兵; 张宏宇; 张崇海; 李凤娇; 高永康; 陶北平; 张海亮; 管宁
Original assignee: Southwest Research and Desigin Institute of Chemical Industry
Current assignee: Southwest Research and Desigin Institute of Chemical Industry
Priority date: 2021-08-03
Filing date: 2021-08-03
Publication date: 2022-01-25
Anticipated expiration: 2031-08-03

Abstract

The utility model belongs to the technical field of industrial gas separation and purification, and particularly relates to a gas separation and purification system with stable flushing regeneration effect. The gas separation and purification system comprises a raw gas pipeline and a product gas pipeline, wherein a plurality of adsorption pipelines are connected between the raw gas pipeline and the product gas pipeline, adsorption towers are arranged on the adsorption pipelines, a forward discharge pipeline is connected between the adsorption pipelines, and a plurality of flushing regeneration adjusting pipelines are connected in parallel on the forward discharge pipeline; the flushing regeneration adjusting pipeline is sequentially provided with a sequential tank and a flushing adjusting valve, a singular number flushing pipeline is connected between a plurality of singular number adsorption pipelines, an even number flushing pipeline is connected between a plurality of even number adsorption pipelines, and the other end of the flushing regeneration adjusting pipeline is respectively connected with the singular number flushing pipeline and the even number flushing pipeline. The utility model provides a gas separation and purification system which has the overall consistent effect of multiple staggered flushing regeneration so as to ensure the overall operation effect of the device and the product yield.

Description

Wash gas separation purification system that regeneration effect is stable

Technical Field

The utility model belongs to the technical field of industrial gas separation and purification, and particularly relates to a gas separation and purification system with stable flushing regeneration effect.

Background

Pressure Swing Adsorption (PSA) gas separation and purification technology utilizes the difference of Adsorption characteristics such as equilibrium Adsorption capacity and Adsorption rate of gas components on an adsorbent and the characteristic that the Adsorption capacity changes with Pressure to realize the alternation of Adsorption and desorption processes through periodic Pressure change, thereby realizing the separation or purification of gas, belonging to the physical process and being capable of realizing the separation or purification at normal temperature. Because the PSA system is formed by combining a plurality of adsorption towers and program control valves which are completely same in configuration, the overall performance of the PSA system also follows the theory of short wooden barrels, and the performance of the whole system is determined by the worst performance of parallel units, so that the consistency of each process in the system is required to be improved as much as possible.

The pressure swing adsorption technology (ZL 200510020305.X) patent with two sequential release tanks adopts two regulating valves arranged behind each sequential release tank to control a flushing regeneration process, see operation step sequence table 1 and figure 7, each step of flushing regeneration respectively controls different series of flushing regeneration processes by the two regulating valves, the flushing regeneration process can have different flushing regeneration effects due to the performance difference of the regulating valves, parameters are respectively required to be set for different control schemes in the front, middle and later stages of each regulating valve, the control program configuration of the regulating valves is very complex, the actual control effect and the theoretical design have larger difference, the flushing regeneration clean degree of an adsorbent is influenced, and finally the flushing regeneration effect deviates from a design value.

Table 1: 10-2-5/P pressure swing adsorption operation process table with two sequential discharge tanks

When the first flushing regeneration process adopts two regulating valves to respectively control the first flushing regeneration processes of different series, and the second flushing regeneration process also adopts two different regulating valves to control the second flushing regeneration processes of different series, each flushing regeneration process can lead to different regeneration effects due to the performance difference of the two regulating valves. The pressure swing adsorption process with two sequential discharge tanks ensures that the product yield of the actual operation of the device is ensured only when the first flushing regeneration effect and the second flushing regeneration effect of the single-double series corresponding to the four flushing processes controlled by the two series of four regulating valves are the same. When the regeneration effect is deviated due to the performance difference of the regulating valves in any one flushing regeneration process, the yield cannot reach the optimal value, and the overall performance of the device is greatly reduced. According to the analysis of the actual operation effect, when the performances of the four regulating valves are inconsistent and have larger difference, the overall recovery rate of the device is reduced by about 0.5% compared with the design in the actual operation state.

SUMMERY OF THE UTILITY MODEL

In order to solve the above problems in the prior art, the present invention aims to provide a gas separation and purification system with uniform regeneration effect by multiple staggered flushes, so as to ensure the overall operation effect and product yield of the device.

The technical scheme adopted by the utility model is as follows:

a gas separation and purification system with stable flushing and regeneration effects comprises a feed gas pipeline and a product gas pipeline, wherein a plurality of adsorption pipelines are connected between the feed gas pipeline and the product gas pipeline, adsorption towers are arranged on the adsorption pipelines, a forward discharging pipeline is connected between the adsorption pipelines, and a plurality of flushing and regeneration adjusting pipelines are connected in parallel on the forward discharging pipeline; the flushing regeneration adjusting pipeline is sequentially provided with a sequential tank and a flushing adjusting valve, a singular number flushing pipeline is connected between a plurality of singular number adsorption pipelines, an even number flushing pipeline is connected between a plurality of even number adsorption pipelines, and the other end of the flushing regeneration adjusting pipeline is respectively connected with the singular number flushing pipeline and the even number flushing pipeline.

And during the flushing step, flushing the adsorbent in the adsorption tower after the reverse pressure releasing step by adopting flushing regeneration gas discharged in the sequential pressure releasing step, and completely regenerating residual impurities from the adsorbent. The speed of the forward air release tank is controlled by a flushing regulating valve on a flushing regeneration regulating pipeline, and then a single flushing pipeline and a double flushing pipeline are switched to carry out a flushing regeneration process on the single-double series adsorption towers which finish the reverse pressure release step. The sequential discharge tanks sequentially wash and regenerate the same adsorption tower. Because the other end that washes regeneration adjusting line respectively with singular flushing line, the doublic number pipeline connection that washes, when using certain jar of putting in the same direction to wash respectively singular adsorption tower and the doublic number adsorption tower, the governing valve that washes that uses is one, then should be in the same direction as the jar to the effect of washing of the adsorption tower of singular and doublic number unanimous, and the effect of the regeneration is whole unanimous in the crisscross washing many times, has guaranteed whole operation effect of device and product yield.

As a preferable scheme of the utility model, a raw material gas program control valve is arranged at one end of the adsorption pipeline close to the raw material gas pipeline, and a product gas program control valve is arranged at one end of the adsorption pipeline close to the product gas pipeline. In the adsorption step, the raw gas program control valve and the product gas program control valve on the adsorption pipeline are opened, so that the raw gas enters the adsorption tower from the bottom of the adsorption tower, impurity components in the raw gas are adsorbed by the adsorbent in the adsorption tower, and weakly-adsorptive components such as hydrogen are sent out of a boundary region from a product gas pipeline on the upper part of the adsorption tower. And when the impurity components in the product gas meet the requirements, closing the feed gas program control valve and the product gas program control valve.

As a preferable scheme of the utility model, a plurality of pressure equalizing pipelines are connected among a plurality of adsorption pipelines, and a pressure equalizing program control valve is arranged between each pressure equalizing pipeline and each adsorption pipeline. After the adsorption step is completed, opening the pressure-equalizing program control valve, transferring the adsorbent gap in the adsorption tower, the product gas components adsorbed by the adsorbent and the adsorption heat to the adsorption tower with increased pressure, and closing the pressure-equalizing program control valve after the pressures of the adsorption tower with increased pressure and the adsorption tower with decreased pressure are basically equal. The pressure drop is completed for several times according to the conditions of adsorption pressure, adsorption tower number, adsorbent performance, product quality and yield requirements.

As a preferred scheme of the utility model, a forward-discharging special program control valve is connected between the forward-discharging pipeline and the adsorption pipeline, a forward-discharging public program control valve is arranged on the flushing regeneration regulating pipeline, and the forward-discharging special program control valve is positioned on one side of the forward-discharging tank, which is far away from the flushing regulating valve. After the pressure reduction step is finished, a small amount of effective components absorbed by the adsorbent in the adsorbent gaps in the adsorption tower can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction forward releasing step. The materials enter the sequential-discharging tank through the sequential-discharging special program control valve and the sequential-discharging public program control valve to be stored.

As the preferable scheme of the utility model, a single number flushing dedicated program control valve is connected between the single number flushing pipeline and the single number adsorption pipeline, an even number flushing dedicated program control valve is connected between the even number flushing pipeline and the even number adsorption pipeline, a single number flushing common program control valve is arranged at one end of the flushing regeneration adjusting pipeline connected with the single number flushing pipeline, and an even number flushing common program control valve is arranged at one end of the flushing regeneration adjusting pipeline connected with the even number flushing pipeline. In order to regenerate the adsorbent in the adsorption tower more thoroughly, flushing regeneration gas discharged in the forward releasing step is adopted to flush the adsorbent in the adsorption tower which completes the reverse releasing step, and residual impurities are completely regenerated from the adsorbent. The speed of the forward release gas in the forward release tank is controlled by a flushing regulating valve in a flushing regeneration regulating pipeline, and the single-series adsorption tower and the double-series adsorption tower which finish the reverse pressure release step are flushed and regenerated by switching a single flushing public program control valve and a double flushing public program control valve.

As a preferable scheme of the utility model, the adsorption device further comprises a plurality of desorption pipelines, and desorption program control valves are connected between the desorption pipelines and the adsorption pipelines. After the sequential releasing step is finished, impurities and partial effective gas in the adsorption tower are discharged through a desorption program control valve at the bottom of the adsorption tower. During the flushing step, residual impurities in the adsorption tank are completely regenerated from the adsorbent through the desorption line.

As a preferred scheme of the utility model, a final boosting pipeline is connected among a plurality of adsorption pipelines, a special program control valve for final boosting is connected between the final boosting pipeline and the adsorption pipelines, the final boosting pipeline is connected with a product air pipeline, and a product air regulating valve is connected between the final boosting pipeline and the product air pipeline. Because the pressure of the adsorption tower cannot reach the adsorption pressure through multiple pressure rising steps, the pressure of the product gas needs to be raised from the top of the adsorption tower to reach the adsorption operation pressure, the raw material gas can also be used for raising the pressure of the adsorption tower from the bed layer feeding end according to different processes, or the product gas and the raw material gas are adopted for raising the pressure of the adsorption tower at the same time until the adsorption tower reaches the adsorption operation pressure, and finally the adsorption tower enters the next cycle process according to an operation program. When the adsorption tower is finally pressurized, the product gas regulating valve and the corresponding special program control valve for final pressurization on the final pressurization pipeline are opened, so that the product gas enters the adsorption tower to realize the final pressurization.

The gas separation and purification method with stable flushing regeneration effect comprises the following steps:

s1: feeding the raw material gas into an adsorption pipeline for separation and purification, and feeding the product gas out of a boundary region;

s2: transferring the product gas components and adsorption heat adsorbed by the adsorbent gap and the adsorbent in the adsorption tower to the adsorption tower with increased pressure until the pressure of the adsorption tower with decreased pressure and the pressure of the adsorption tower with increased pressure are balanced;

s3: discharging a small amount of effective components in the adsorbent gaps and adsorbed by the adsorbent in the adsorption tower into a sequential release tank for storage;

s4: reversely discharging impurities and part of effective gas in the adsorption tower;

s5: flushing the adsorbent in the adsorption tower having completed the step S4 with the flushing regeneration gas discharged in the step S3; when a single sequential tank flushes a singular adsorption tower and an even adsorption tower, the same flush regulating valve is adopted to regulate the flow;

s6: increasing the pressure of the adsorption column ending the step S5 with the gas of the adsorption column performing the step S2 until the pressures of the adsorption column whose pressure is increased and the adsorption column whose pressure is decreased are equalized;

s7: the product gas is used to eventually increase the pressure from the top of the adsorption column to the adsorption operating pressure.

The system of the utility model comprises six or more than six adsorption towers, a PSA system which is composed of at least two sequential-discharging tanks, at least two flushing regeneration adjusting modules, a tail gas system and the like and continuously operates in multiple towers, and each adsorption tower completes the same step sequence, but the operation of the process steps is staggered by one sub-period so as to ensure the continuous operation of the separation process. The adsorption tower after the adsorption step is subjected to pressure reduction for a plurality of times, so that the residual pressure is fully utilized, the adsorption tower which finishes the reverse discharge can gradually increase the pressure, and the adsorption tank after the pressure increase has better adsorption again. After the pressure reduction step is finished, a small amount of effective components in the adsorbent gaps in the adsorption tower and adsorbed by the adsorbent can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction forward releasing step. After the sequential releasing step is finished, impurities and partial effective gas in the adsorption tower are discharged through a desorption program control valve at the bottom of the adsorption tower. In order to regenerate the adsorbent in the adsorption tower more thoroughly, flushing regeneration gas discharged in the forward releasing step is adopted to flush the adsorbent in the adsorption tower which completes the reverse releasing step, and residual impurities are completely regenerated from the adsorbent. Since the adsorption tower pressure cannot be brought to the adsorption pressure by the pressure rising step for many times, the pressure of the product gas is required to be raised from the top of the adsorption tower to be brought to the adsorption operation pressure.

In steps S2 and S5, the final pressure-raising line for the final pressure-raising in step S7 is used for equalizing the pressure of the adsorption column for the first pressure drop and the pressure of the adsorption column for the last pressure rise. And opening the final boosting program control valve at the corresponding position of the final boosting pipeline, and adjusting the final boosting regulating valve to a determined small opening degree, so that the difference between the pressure of the adsorption tower and the pressure of the product gas can be reduced when the pressure of the adsorption tower with the first pressure drop and the pressure of the adsorption tower with the last pressure rise are equalized, and the time for performing final boosting is shortened.

In step S1, the raw material gas enters the adsorption pipeline under 2.0-4.0 MPa and at 20-40 ℃.

The utility model has the beneficial effects that:

the flushing regulating valve on the flushing regeneration regulating pipeline can control the speed of the forward venting gas of the forward venting tank, and then the odd flushing pipeline and the even flushing pipeline are switched to carry out the flushing regeneration process on the single-double series adsorption towers which finish the reverse pressure relief step. Because the other end that washes regeneration adjusting line respectively with singular flushing line, the doublic number pipeline connection that washes, when using certain jar of putting in the same direction to wash respectively singular adsorption tower and the doublic number adsorption tower, the governing valve that washes that uses is one, then should be in the same direction as the jar to the effect of washing of the adsorption tower of singular and doublic number unanimous, and the effect of the regeneration is whole unanimous in the crisscross washing many times, has guaranteed whole operation effect of device and product yield.

Drawings

FIG. 1 is a schematic view of the structure of the present invention in example 1;

FIG. 2 is a schematic structural view of the present invention in example 2;

FIG. 3 is a schematic structural view of the present invention in example 3;

FIG. 4 is a schematic structural view of the present invention in example 4;

FIG. 5 is a schematic structural view of the present invention in example 5;

FIG. 6 is a schematic structural view of the present invention in example 6;

fig. 7 is a schematic structural diagram of a conventional gas separation and purification system.

In the figure, 1-feed gas line; 2-product gas line; 3-an adsorption line; 4-arranging the pipeline in sequence; 5-flushing the regeneration regulating line; 6-singular flush lines; 7-double flush lines; 8-a pressure equalization line; 9-desorption line; 10-final booster line; 31-raw material gas program control valve; 32-product gas programmable valve; 41-sequentially placing a special program control valve; 61-single number flushing special program control valve; 71-programmed valve special for double flushing; 81-pressure equalizing program control valve; 91-desorption program control valve; 101-a special program control valve for final pressure increase; 102-product gas regulating valve; HV-101, HV-102, HV-103-flush regulating valves; KV-1, KV-2 and KV-3-sequentially releasing common program control valves; KV-1A, KV-2A, KV-3A-single flushing public program control valve; KV-1B, KV-2B, KV-3B-double flushing common program control valve.

Detailed Description

Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the utility model and are not to be construed as limiting the utility model.

Example 1: separation and purification process with 3 sequential discharge tanks and 10 adsorption towers

Table 2: 10-2-5/P operation process table

As can be seen from the operational process table 2 in this example, each adsorption tower undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a fifth pressure drop E5D, a forward first PP1, a forward second PP2, a forward third PP3, a reverse D, a flushing third P3, a flushing second P2, a flushing first P1, a fifth pressure rise E5R, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR in sequence within one cycle period, and the other adsorption towers undergo the same process except that the processes are staggered in time by one sub-cycle period.

As shown in FIG. 1, in which the adsorption columns numbered in the singular number T101, T103, T105, T107 and T109 constitute a single series, the adsorption columns numbered in the plural number T102, T104, T106, T108 and T110 constitute a double series.

Three in-line discharging tanks V101, V102 and V103 are arranged, one in-line discharging common program control valve KV-1, KV-2 and KV-3 is respectively arranged on an in-line discharging pipeline 4, and a flushing regeneration adjusting module mainly comprises flushing adjusting valves HV-101, HV-102 and HV-103 which are respectively arranged on an outlet main pipe of the in-line discharging tank. The single and double series of the common program control valve KV-1A, KV-2A, KV-3A for single flushing and the common program control valve KV-1B, KV-2B, KV-3B for double flushing are respectively arranged on the flushing inlet manifold. The forward discharging common program control valve KV-1 is connected with a forward discharging tank V101, and the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B. The sequential discharge common program control valve KV-2 is connected with the sequential discharge tank V102, and the flushing adjusting module B consists of a flushing adjusting valve HV-102 and two common program control valves KV-2A/B. The sequential discharge common program control valve KV-3 is connected with the sequential discharge tank V103, and the flushing adjusting module C consists of a flushing adjusting valve HV-103 and two common program control valves KV-3A/B.

The process comprises the following specific steps:

and (B) adsorption A: the feed gas programmable valve 31 and the product gas programmable valve 32 are opened. The raw material gas enters the adsorption tower from the bottom of the adsorption tower through the raw material gas pipeline 1 and the raw material gas program control valve 31 under the pressure of 2.0-4.0 MPa and at the temperature of 20-40 ℃, impurity components in the raw material gas are adsorbed by an adsorbent in the adsorption tower, weakly-adsorptive components such as hydrogen are sent out of a boundary zone from the upper part of the adsorption tower through a pipeline and the product gas program control valve 32, when the impurity components in the product gas meet requirements, the raw material gas program control valve 31 and the product gas program control valve 32 are closed, and the adsorption step is finished.

Pressure drop EiD step: after the adsorption step A is completed, the pressure equalizing program control valve 81 is opened, the adsorbent gap in the adsorption tower, the product gas components adsorbed by the adsorbent and the adsorption heat are transferred to the adsorption tower with increased pressure, and the pressure equalizing program control valve 81 is closed after the pressure of the adsorption tower with increased pressure is basically equal to the pressure of the adsorption tower with reduced pressure. According to the conditions of adsorption pressure, the number of adsorption towers, adsorbent performance, product quality, yield requirement and the like, the pressure drop is completed for 5 times, and the pressure drop is abbreviated as E1D, E2D and … … E5D in sequence. Specifically, when the pressure equalization is performed between the adsorption column with the first pressure drop and the adsorption column with the last pressure rise, the final boost program control valve at the corresponding position of the final boost pipeline 10 is opened, and the final boost regulating valve is regulated to a certain small opening.

Sequential PP1/2/3 step: after the pressure reduction EiD step is completed, a small amount of effective components in the adsorbent gaps in the adsorption tower and adsorbed by the adsorbent can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction sequential PP1/2/3 step. The forward-placing PP1 enters a V101 forward-placing tank I through a forward-placing special program control valve 41 and a forward-placing public program control valve KV-1 to be stored, the forward-placing second PP2 enters a V102 forward-placing tank II through the forward-placing special program control valve 41 and a forward-placing public program control valve KV-2 to be stored, and the forward-placing third PP3 enters the V103 forward-placing tank II through the forward-placing special program control valve 41 and the forward-placing public program control valve KV-3 to be stored.

And D, reversely releasing pressure: after the step of sequentially releasing PP1/2/3 is finished, the desorption program control valve 91 is opened, impurities and part of effective gas in the adsorption tower are discharged through the desorption program control valve 91 at the bottom of the adsorption tower, and the pressure in the adsorption tower is 0.002-0.45 MPaG after reverse pressure release is finished.

Washing P3/2/1 step: in order to regenerate the adsorbent in the adsorption tower more completely, flushing regeneration gas discharged in the sequential PP1/2/3 step is adopted to flush the adsorbent in the adsorption tower completing the reverse pressure release D step, and residual impurities are completely regenerated from the adsorbent. Firstly, the speed of the downstream air release in the V103 downstream release tank III is controlled by the regulating valve HV103 in the flushing regeneration regulating module C, and the first flushing regeneration P3 process is carried out on the single-double series adsorption towers completing the reverse pressure release step D by switching two flushing common program control valves KV-3A/B. And the speed of the downstream air in the V102 downstream tank II is controlled by an adjusting valve HV102 in a flushing regeneration adjusting module B, and a P2 process of flushing regeneration is carried out on the single-series adsorption tower and the double-series adsorption tower which finish the step of flushing P3 for the first time by switching two flushing common program control valves KV-2A/B. And finally, the speed of the downstream gas in the first V101 downstream tank is controlled by an adjusting valve HV101 in a flushing regeneration adjusting module A, a third flushing regeneration P1 process is carried out on the single-double series adsorption towers completing the second flushing regeneration P2 process by switching two flushing common program control valves KV-1A/B, and the pressure in the flushed adsorption towers is reduced to 0.001-0.40 MPaG in the flushing process.

And a pressure increasing EiR step, which corresponds to the pressure decreasing EiD step, wherein after the P3/2/1 flushing step is completed, the pressure equalizing program control valve 81 is opened, and the gas in the pressure decreasing EiD step is used for gradually increasing the pressure of the adsorption tower finishing the P3/2/1 flushing step, wherein the pressure increasing step can be completed by 5 times, and is sequentially abbreviated as E5R, … … E2R and E1R.

And a final pressure increasing FR step: since the adsorption tower pressure cannot be brought to the adsorption pressure by the pressure raising EiR step for a plurality of times, the pressure of the product gas is raised from the top of the adsorption tower to be brought to the adsorption operation pressure. According to different processes, the raw gas can be used for boosting the pressure of the adsorption tower from the feed end of the bed layer, or the product gas and the raw gas are used for boosting the pressure of the adsorption tower at the same time until the adsorption tower reaches the adsorption operation pressure, and finally the adsorption tower enters the next cycle process according to the operation program.

Each adsorption tower passes through the same step sequence, and only the process steps are staggered with each other by a sub-period in operation so as to ensure that the separation process is continuously carried out.

Example 2: separation and purification process with 2 sequential discharge tanks and 12 adsorption towers

Table 3: 12-2-6/P operation process table

As can be seen from the operational process table 3 in this example, each adsorption tower undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a fifth pressure drop E5D, a sixth pressure drop E6D, a forward-release first PP1, a forward-release second PP2, a reverse-release D, a flushing second P2, a flushing first P1, a sixth pressure rise E6R, a fifth pressure rise E5R, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR in sequence in one cycle, and the other adsorption towers undergo the same process except that the processes are staggered in time by one sub-cycle.

As shown in FIG. 2, in which the adsorption columns numbered in the singular number T101, T103, T105, T107, T109 and T1011 constitute a single series, the adsorption columns numbered in the plural number T102, T104, T106, T108, T110 and T112 constitute a double series.

Two in-line discharging tanks V101 and V102 are arranged, and an in-line discharging public program control valve KV-1 and KV-2 are respectively arranged on an in-line discharging pipeline 4. The flushing regeneration adjusting module mainly comprises adjusting valves HV-101 and HV-102 which are respectively arranged on an outlet header pipe of the sequential discharging tank, a single-double series of single-number flushing public program control valves KV-1A, KV-2A and double-number flushing public program control valves KV-1B, KV-2B which are respectively arranged on a flushing inlet header pipe. The forward discharging common program control valve KV-1 is connected with a forward discharging tank V101, and the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B. The flushing regulating module B consists of a flushing regulating valve HV-102 and two common program control valves KV-2A/B.

The process comprises the following specific steps:

and (B) adsorption A: and opening the feed gas program control valve 31 and the product gas program control valve 32, and enabling the feed gas to enter the adsorption tower from the bottom of the adsorption tower through the feed gas pipeline 1 and the feed gas program control valve 31 at the pressure of 2.0-4.0 MPa and the temperature of 20-40 ℃. And (3) the impurity components in the raw material gas are adsorbed by the adsorbent in the adsorption tower, the weakly-adsorptive components such as hydrogen are sent out of the interface region from the upper part of the adsorption tower through a pipeline and the product gas program control valve 32, when the impurity components in the product gas meet the requirements, the raw material gas program control valve 31 and the product gas program control valve 32 are closed, and the adsorption step is finished.

Pressure drop EiD step: after the adsorption step A is completed, the pressure equalizing program control valve 81 is opened, the adsorbent gap in the adsorption tower, the product gas components adsorbed by the adsorbent and the adsorption heat are transferred to the adsorption tower with increased pressure, and the pressure equalizing program control valve 81 is closed after the pressure of the adsorption tower with increased pressure is basically equal to the pressure of the adsorption tower with reduced pressure. According to the conditions of adsorption pressure, the number of adsorption towers, adsorbent performance, product quality, yield requirement and the like, the pressure drop is completed for 6 times, and the pressure drop is sequentially abbreviated as E1D, E2D and … … E6D. Specifically, when the pressure equalization is performed between the adsorption column with the first pressure drop and the adsorption column with the last pressure rise, the final boost program control valve at the corresponding position of the final boost pipeline 10 is opened, and the final boost regulating valve is regulated to a certain small opening. When the sequential discharging step is not performed in the canister, the sequential discharging line 4 is used as a pressure equalizing line.

Sequential PP1/2 step: after the pressure reduction E5D step is completed, a small amount of effective components absorbed by the adsorbent in the adsorbent gaps in the adsorption tower can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction sequential PP1/2 step. And a forward-discharge PP1 enters the V101 forward-discharge tank through the forward-discharge special program control valve 41 and the forward-discharge public program control valve KV-1 to be stored. The clockwise-releasing second PP2 enters the V102 clockwise-releasing second tank through the clockwise-releasing special program control valve 41 and the clockwise-releasing public program control valve KV-2 to be stored.

And D, reversely releasing pressure: after the step of sequentially releasing PP1/2 is finished, the desorption program control valve 91 is opened, impurities and partial effective gas in the adsorption tower are discharged through the desorption program control valve 91 at the bottom of the adsorption tower, and the pressure in the adsorption tower is 0.002-0.45 MPaG after reverse pressure release is finished.

Washing P2/1 step: in order to regenerate the adsorbent in the adsorption tower more completely, flushing regeneration gas discharged in the sequential PP1/2 step is adopted to flush the adsorbent in the adsorption tower completing the reverse pressure release step D, and residual impurities are completely regenerated from the adsorbent. Firstly, the speed of forward air release in the V102 forward air release tank II is controlled by an adjusting valve HV102 in a flushing regeneration adjusting module B, and a first flushing regeneration P2 process is carried out on a single-double series adsorption tower completing a reverse pressure release step D by switching two program control valves KV-2A/B. And then the speed of the downstream gas in the first V101 downstream tank is controlled by an adjusting valve HV101 in a flushing regeneration adjusting module A, the second flushing regeneration P1 process is carried out on the single-double series adsorption towers completing the first flushing regeneration P2 process by switching two program control valves KV-1A/B, and the pressure in the flushed adsorption towers is reduced to 0.001-0.40 MPaG in the flushing process.

And a pressure increasing EiR step, which corresponds to the pressure decreasing EiD step, wherein after the P2/1 flushing step is completed, the pressure of the adsorption tower ending the P2/1 flushing step is gradually increased by using the gas in the pressure decreasing EiD step, and the step can be completed in 6 times, namely E6R, … … E2R and E1R.

Example 3: separation and purification process with 2 sequential discharge tanks and 14 adsorption towers

Table 4: 14-2-8/P operation process table

As can be seen from the operational process table 4, each adsorption column undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a fifth pressure drop E5D, a sixth pressure drop E6D, a seventh pressure drop E7D, an eighth pressure drop E8D, a forward first PP1, a forward second PP2, a reverse discharge D, a flushing second P2, a flushing first P1, an eighth pressure rise E8R, a seventh pressure rise E7R, a sixth pressure rise E6R, a fifth pressure rise E5R, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR 2 in this order within one cycle period. The remaining adsorption columns also undergo the same process, but are staggered in time by one sub-cycle.

As shown in FIG. 3, in which the adsorption columns numbered in the singular number T101, T103, T105, T107, T109, T111 and T113 constitute a single series, the adsorption columns numbered in the plural number T102, T104, T106, T108, T110, T112 and T114 constitute a double series.

Two in-line discharging tanks V101 and V102 are arranged, one in-line discharging common program control valve KV-1 and one in-line discharging common program control valve KV-2 are respectively arranged on an in-line discharging pipeline 4, a flushing regeneration adjusting module mainly comprises adjusting valves HV-101 and HV-102 respectively arranged on an outlet header pipe of the in-line discharging tanks, a single-double series of single-number flushing common program control valves KV-1A, KV-2A and double-number flushing common program control valves KV-1B, KV-2B respectively arranged on a flushing inlet header pipe. The forward discharging common program control valve KV-1 is connected with a forward discharging tank V101, and the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B. The flushing regulating module B consists of a flushing regulating valve HV-102 and two common program control valves KV-2A/B.

The process comprises the following specific steps:

and (B) adsorption A: and opening the feed gas program control valve 31 and the product gas program control valve 32, enabling the feed gas to enter the adsorption tower from the bottom of the adsorption tower through the feed gas pipeline 1 and the feed gas program control valve 31 at the temperature of 20-40 ℃ under the pressure of 4.0-6.0 MPa, adsorbing impurity components in the feed gas by an adsorbent in the adsorption tower, and delivering weak-adsorbability components such as hydrogen out of a boundary region from the upper part of the adsorption tower through a pipeline and the product gas program control valve 32. And when the impurity components in the product gas meet the requirements, closing the feed gas program control valve 31 and the product gas program control valve 32, and finishing the adsorption step.

Pressure drop EiD step: after the adsorption step A is completed, the pressure equalizing program control valve 81 is opened, the adsorbent gap in the column, the product gas components adsorbed by the adsorbent and the adsorption heat are transferred to the adsorption column with increased pressure, and the pressure equalizing program control valve 81 is closed after the pressure of the adsorption column with increased pressure is basically equal to the pressure of the adsorption column with reduced pressure. According to the conditions of adsorption pressure, the number of adsorption towers, adsorbent performance, product quality, yield requirement and the like, the pressure drop is completed for 8 times, and the pressure drop is sequentially abbreviated as E1D, E2D and … … E8D. Specifically, when the pressure equalization is performed between the adsorption column with the first pressure drop and the adsorption column with the last pressure rise, the final boost program control valve at the corresponding position of the final boost pipeline 10 is opened, and the final boost regulating valve is regulated to a certain small opening. When the sequential discharging step is not performed in the canister, the sequential discharging line 4 is used as a pressure equalizing line.

Sequential PP1/2 step: after the pressure reduction EiD step is completed, a small amount of effective components in the adsorbent gaps in the adsorption tower and adsorbed by the adsorbent can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction sequential PP1/2 step. The clockwise-release first PP1 enters the V101 clockwise-release first tank through the clockwise-release special program control valve 41 and the clockwise-release public program control valve KV-1 to be stored, and the clockwise-release second PP2 enters the V102 clockwise-release second tank through the clockwise-release special program control valve 41 and the clockwise-release public program control valve KV-2 to be stored.

And D, reversely releasing pressure: after the step of sequentially releasing PP1/2 is finished, impurities and part of effective gas in the adsorption tower are discharged through a desorption program control valve 91 at the bottom of the adsorption tower, and the pressure in the adsorption tower is 0.002-0.450 MPaG after reverse pressure release is finished.

Pressure raising EiR step: this step corresponds to the pressure drop EiD step, and after the P2/1 step of purging is completed, the pressure of the adsorption tower ending the P2/1 step of purging is gradually increased by using the gas in the pressure drop EiD step, and the step can be completed in 8 times, which are abbreviated as E8R, … … E2R and E1R in sequence.

Example 4: separation and purification process with 2 sequential discharge tanks and 8 adsorption towers

Table 5: 8-1-4/P operation process table

As can be seen from the operational process table 5, each adsorption tower undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a forward-release PP1, a forward-release PP2, a reverse-release D, a flushing second P2, a flushing first P1, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR in sequence in one cycle period, and the other adsorption towers undergo the same process except that they are staggered in time by one sub-cycle period.

As shown in fig. 4, in which the T101, T103, T105 and T107 adsorption columns numbered in the singular form a single series, and the T102, T104, T106 and T108 adsorption columns numbered in the double form a double series.

Two in-line discharging tanks V101 and V102 are arranged, one in-line discharging common program control valve KV-1 and one in-line discharging common program control valve KV-2 are respectively arranged on an in-line discharging pipeline 4, a flushing regeneration adjusting module mainly comprises adjusting valves HV-101 and HV-102 respectively arranged on an outlet header pipe of the in-line discharging tanks, a single-double series of single-number flushing common program control valves KV-1A, KV-2A and double-number flushing common program control valves KV-1B, KV-2B respectively arranged on a flushing inlet header pipe. The forward discharging common program control valve KV-1 is connected with a forward discharging tank V101, the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B, and the flushing adjusting module B consists of a flushing adjusting valve HV-102 and two common program control valves KV-2A/B.

The process comprises the following specific steps:

and (B) adsorption A: opening the feed gas program control valve 31 and the product gas program control valve 32, enabling the feed gas to enter the adsorption tower from the bottom of the adsorption tower through the feed gas pipeline 1 and the feed gas program control valve 31 at the temperature of 20-40 ℃ under the pressure of 2.0-4.0 MPa, enabling impurity components in the feed gas to be adsorbed by the adsorbent in the adsorption tower, enabling weakly-adsorptive components such as hydrogen to be sent out of a boundary zone from the upper part of the adsorption tower through a pipeline and the product gas program control valve 32, closing the feed gas and the product gas program control valve 32 when the impurity components in the product gas meet requirements, and ending the adsorption step.

Pressure drop EiD step: after the adsorption step A is completed, the pressure equalizing program control valve 81 is opened, the adsorbent gap in the column, the product gas components adsorbed by the adsorbent and the adsorption heat are transferred to the adsorption column with increased pressure, and the pressure equalizing program control valve 81 is closed after the pressure of the adsorption column with increased pressure is basically equal to the pressure of the adsorption column with reduced pressure. According to the conditions of adsorption pressure, the number of adsorption towers, adsorbent performance, product quality, yield requirement and the like, the pressure drop is completed for 4 times, and the pressure drop is sequentially abbreviated as E1D, E2D and … … E4D. Specifically, when the pressure equalization is performed between the adsorption column with the first pressure drop and the adsorption column with the last pressure rise, the final boost program control valve at the corresponding position of the final boost pipeline 10 is opened, and the final boost regulating valve is regulated to a certain small opening. When the sequential discharging step is not performed in the canister, the sequential discharging line 4 is used as a pressure equalizing line.

Sequential PP1/2 step: after the pressure reduction E4D step is completed, a small amount of effective components absorbed by the adsorbent in the adsorbent gaps in the adsorption tower can be further discharged from the bed layer to be used as flushing regeneration gas for utilization through a forward pressure reduction sequential PP1/2 step. The clockwise-release first PP1 enters the V101 clockwise-release first tank through the clockwise-release special program control valve 41 and the clockwise-release public program control valve KV-1 to be stored, and the clockwise-release second PP2 enters the V102 clockwise-release second tank through the clockwise-release special program control valve 41 and the clockwise-release public program control valve KV-2 to be stored.

And D, reversely releasing pressure: after the step of sequentially releasing PP1/2 is finished, impurities and part of effective gas in the adsorption tower are discharged through a desorption program control valve 91 at the bottom of the adsorption tower, and the pressure in the adsorption tower is 0.002-0.45 MPaG after reverse pressure release is finished.

Pressure raising EiR step: this step corresponds to the pressure drop EiD step, and after the P2/1 step of purging is completed, the pressure of the adsorption tower ending the P2/1 step of purging is gradually increased by using the gas in the pressure drop EiD step, and the step can be completed in 4 times, which are abbreviated as E4R, … … E2R and E1R in sequence.

Example 5: separation and purification process with 2 sequential discharge tanks and 10 adsorption towers

Table 6: 10-2-4/P operation process table

As can be seen from the operation process table 6, each adsorption tower undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a forward PP1, a forward PP2, a reverse D, a flushing P2, a flushing P1, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR in sequence in one cycle period, and the other adsorption towers undergo the same process except that they are staggered in time by one sub-cycle period.

As shown in FIG. 5, in which the adsorption columns numbered in the singular number T101, T103, T105, T107 and T109 constitute a single series, the adsorption columns numbered in the plural number T102, T104, T106, T108 and T110 constitute a double series.

Two in-line discharging tanks V101 and V102 are arranged, one in-line discharging common program control valve KV-1 and one in-line discharging common program control valve KV-2 are respectively arranged on an in-line discharging pipeline 4, a flushing regeneration adjusting module mainly comprises adjusting valves HV-101 and HV-102 respectively arranged on an outlet header pipe of the in-line discharging tanks, a single-double series of single-number flushing common program control valves KV-1A, KV-2A and double-number flushing common program control valves KV-1B, KV-2B respectively arranged on a flushing inlet header pipe. The forward discharging common program control valve KV-1 is connected with a forward discharging tank V101, and the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B. The sequential discharge common program control valve KV-2 is connected with the sequential discharge tank V102, and the flushing adjusting module B consists of a flushing adjusting valve HV-102 and two common program control valves KV-2A/B.

The process comprises the following specific steps:

Washing P2/1 step: in order to regenerate the adsorbent in the adsorption tower more completely, flushing regeneration gas discharged in the sequential PP1/2 step is adopted to flush the adsorbent in the adsorption tower completing the reverse pressure release step D, and residual impurities are completely regenerated from the adsorbent. Firstly, the speed of forward air release in the V102 forward air release tank II is controlled by an adjusting valve HV102 in a flushing regeneration adjusting module B, and a second flushing regeneration P2 process is carried out on the single-double series adsorption tower completing the first reverse release D step by switching two program control valves KV-2A/B. And finally, the speed of the downstream gas in the V101 downstream tank I is controlled by an adjusting valve HV101 in a flushing regeneration adjusting module A, a third flushing regeneration P1 process is carried out on the single-double series adsorption towers completing the second flushing regeneration P2 process by switching two program control valves KV-1A/B, and the pressure in the flushed adsorption towers is reduced to 0.001-0.40 MPaG in the flushing process.

Pressure raising EiR step: this step corresponds to the pressure drop EiD step, and after the P2/1 step of flushing is completed, the pressure of the adsorption tower ending the P3/2/1 step of flushing is gradually increased by using the gas in the pressure drop EiD step, and the step can be completed in 4 times, which are abbreviated as E4R, … … E2R and E1R in sequence.

And a final pressure increasing FR step: because the pressure of the adsorption tower cannot reach the adsorption pressure through the step of raising the pressure EiR for multiple times, the product gas is required to be used for raising the pressure from the top of the adsorption tower to reach the adsorption operation pressure, the raw material gas can also be used for raising the pressure of the adsorption tower from the bed layer feeding end according to different processes, or the product gas and the raw material gas are simultaneously used for raising the pressure of the adsorption tower finally until the adsorption tower reaches the adsorption operation pressure, and finally the adsorption tower enters the next cycle process according to an operation program.

Example 6: separation and purification process with 3 sequential discharge tanks and 12 adsorption towers

Table 7: 12-2-7/P operation process table

As can be seen from the operational process table 7, each adsorption column undergoes adsorption a, a first pressure drop E1D, a second pressure drop E2D, a third pressure drop E3D, a fourth pressure drop E4D, a fifth pressure drop E5D, a sixth pressure drop E6D, a seventh pressure drop E7D, a forward first PP1, a forward second PP2, a forward second PP3, a reverse discharge D, a rinse third P3, a rinse second P2, a rinse first P1, a seventh pressure rise E7R, a sixth pressure rise E6R, a fifth pressure rise E5R, a fourth pressure rise E4R, a third pressure rise E3R, a second pressure rise E2R, a first pressure rise E1R, and a final pressure rise FR in this order within one cycle period. The remaining adsorption columns also undergo the same process, but are staggered in time by one sub-cycle.

As shown in FIG. 6, in which the adsorption columns numbered in the singular number T101, T103, T105, T107, T109 and T111 constitute a single series, the adsorption columns numbered in the plural number T102, T104, T106, T108, T110 and T112 constitute a double series.

Three in-line discharging tanks V101, V102 and V103 are arranged, one in-line discharging common program control valve KV-1, KV-2 and KV-3 is respectively arranged on an in-line discharging pipeline 4, and a flushing regeneration adjusting module mainly comprises adjusting valves HV-101, HV-102 and HV-103 which are respectively arranged on an outlet main pipe of the in-line discharging tank. The single and double series of the common single flushing program control valve KV-1A, KV-2A, KV-3A and the common double flushing program control valve KV-1B, KV-2B, KV-3B are respectively arranged on the flushing inlet header pipe, the common sequential discharge program control valve KV-1 is connected with the sequential discharge tank V101, and the flushing adjusting module A consists of a flushing adjusting valve HV-101 and two common program control valves KV-1A/B. The sequential discharge common program control valve KV-2 is connected with the sequential discharge tank V102, and the flushing adjusting module B consists of a flushing adjusting valve HV-102 and two common program control valves KV-2A/B. The sequential discharge common program control valve KV-3 is connected with the sequential discharge tank V103, and the flushing adjusting module C consists of a flushing adjusting valve HV-103 and two common program control valves KV-3A/B.

The process comprises the following specific steps:

and (B) adsorption A: and opening the feed gas program control valve 31 and the product gas program control valve 32, enabling the feed gas to enter the adsorption tower from the bottom of the adsorption tower through the feed gas pipeline 1 and the feed gas program control valve 31 at the temperature of 20-40 ℃ under the pressure of 4.0-6.0 MPa, adsorbing impurity components in the feed gas by an adsorbent in the adsorption tower, and delivering weak-adsorbability components such as hydrogen out of a boundary region from the upper part of the adsorption tower through a pipeline and the product gas program control valve 32. When the impurity component in the product gas meets the requirement, the feed gas and product gas program control valve 32 is closed, and the adsorption step is finished.

Pressure drop EiD step: after the adsorption step A is completed, the pressure equalizing program control valve 81 is opened, the adsorbent gap in the column, the product gas components adsorbed by the adsorbent and the adsorption heat are transferred to the adsorption column with increased pressure, and the pressure equalizing program control valve 81 is closed after the pressure of the adsorption column with increased pressure is basically equal to the pressure of the adsorption column with reduced pressure. According to the conditions of adsorption pressure, the number of adsorption towers, adsorbent performance, product quality, yield requirement and the like, the pressure drop is completed for 7 times, and the pressure drop is abbreviated as E1D, E2D and … … E7D in sequence. Specifically, when the pressure equalization is performed between the adsorption column with the first pressure drop and the adsorption column with the last pressure rise, the final boost program control valve at the corresponding position of the final boost pipeline 10 is opened, and the final boost regulating valve is regulated to a certain small opening.

And D, reversely releasing pressure: after the step of sequentially releasing PP1/2/3 is finished, impurities and part of effective gas in the adsorption tower are discharged through a desorption program control valve 91 at the bottom of the adsorption tower, and the pressure in the adsorption tower is 0.002-0.450 MPaG after reverse pressure release is finished.

Washing P3/2/1 step: in order to regenerate the adsorbent in the adsorption tower more completely, flushing regeneration gas discharged in the sequential PP1/2/3 step is adopted to flush the adsorbent in the adsorption tower completing the reverse pressure release D step, and residual impurities are completely regenerated from the adsorbent. Firstly, the speed of forward air release in a V103 forward air release tank III is controlled by an adjusting valve HV103 in a flushing regeneration adjusting module C, and a first flushing regeneration P3 process is carried out on a single-double series adsorption tower completing a reverse pressure release step D by switching two program control valves KV-3A/B. And then the speed of the downstream vent gas in the V102 downstream tank II is controlled by a regulating valve HV102 in a flushing regeneration regulating module B, the P2 process of secondary flushing regeneration is carried out on the single-double series adsorption towers completing the step of primary flushing P3 by switching two program control valves KV-2A/B, finally the speed of the downstream vent gas in the V101 downstream tank I is controlled by a regulating valve HV101 in a flushing regeneration regulating module A, the P1 process of tertiary flushing regeneration is carried out on the single-double series adsorption towers completing the P2 process of secondary flushing regeneration by switching two program control valves KV-1A/B, and the pressure in the adsorption towers flushed in the flushing process is reduced to 0.001-0.40 MPaG.

Pressure raising EiR step: this step corresponds to the pressure drop EiD step, and after the purge P3/2/1 step is completed, the pressure of the adsorption column ending the purge P2/1 step is gradually increased by the gas in the pressure drop EiD step, and this step can be completed 7 times, which are abbreviated as E7R, … … E2R and E1R.

The utility model is not limited to the above alternative embodiments, and any other various forms of products can be obtained by anyone in the light of the present invention, but any changes in shape or structure thereof, which fall within the scope of the present invention as defined in the claims, fall within the scope of the present invention.

Claims

1. A gas separation and purification system with stable flushing regeneration effect is characterized by comprising a raw gas pipeline (1) and a product gas pipeline (2), wherein a plurality of adsorption pipelines (3) are connected between the raw gas pipeline (1) and the product gas pipeline (2), adsorption towers are arranged on the adsorption pipelines (3), a forward discharge pipeline (4) is connected between the adsorption pipelines (3), and a plurality of flushing regeneration adjusting pipelines (5) are connected in parallel on the forward discharge pipeline (4); the device is characterized in that the flushing regeneration adjusting pipeline (5) is sequentially provided with a sequential tank and a flushing adjusting valve, a singular flushing pipeline (6) is connected between a plurality of singular adsorption pipelines (3), an even flushing pipeline (7) is connected between a plurality of even adsorption pipelines (3), and the other end of the flushing regeneration adjusting pipeline (5) is respectively connected with the singular flushing pipeline (6) and the even flushing pipeline (7).

2. The gas separation and purification system with stable flushing regeneration effect according to claim 1, wherein the adsorption pipeline (3) is provided with a raw gas program control valve (31) at the end close to the raw gas pipeline (1), and the adsorption pipeline (3) is provided with a product gas program control valve (32) at the end close to the product gas pipeline (2).

3. The gas separation and purification system with stable flushing regeneration effect according to claim 1, wherein a plurality of pressure equalizing pipelines (8) are connected between a plurality of adsorption pipelines (3), and a pressure equalizing program control valve (81) is arranged between the pressure equalizing pipelines (8) and the adsorption pipelines (3).

4. The gas separation and purification system with stable flushing regeneration effect according to claim 1, wherein a forward-discharge dedicated program control valve (41) is connected between the forward-discharge pipeline (4) and the adsorption pipeline (3), a forward-discharge common program control valve is arranged on the flushing regeneration regulation pipeline (5), and the forward-discharge dedicated program control valve (41) is positioned on one side of the forward-discharge tank far away from the flushing regulation valve.

5. The gas separation and purification system with stable flushing regeneration effect as claimed in claim 1, wherein a single flushing dedicated program control valve (61) is connected between the single flushing pipeline (6) and the single adsorption pipeline (3), an even flushing dedicated program control valve (71) is connected between the even flushing pipeline (7) and the even adsorption pipeline (3), a single flushing common program control valve is arranged at one end of the flushing regeneration adjusting pipeline (5) connected with the single flushing pipeline (6), and an even flushing common program control valve is arranged at one end of the flushing regeneration adjusting pipeline (5) connected with the even flushing pipeline (7).

6. The gas separation and purification system with stable flushing regeneration effect according to claim 1, further comprising a plurality of desorption pipelines (9), wherein a desorption program control valve (91) is connected between the desorption pipeline (9) and the plurality of adsorption pipelines (3).

7. The gas separation and purification system with stable flushing and regeneration effects as claimed in claim 1, wherein a final pressure boosting pipeline (10) is further connected between the plurality of adsorption pipelines (3), a final pressure boosting dedicated program control valve (101) is connected between the final pressure boosting pipeline (10) and the adsorption pipelines (3), the final pressure boosting pipeline (10) is connected with the product gas pipeline (2), and a product gas regulating valve (102) is connected between the final pressure boosting pipeline (10) and the product gas pipeline (2).