CN218345173U - Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system - Google Patents
Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system Download PDFInfo
- Publication number
- CN218345173U CN218345173U CN202120532125.4U CN202120532125U CN218345173U CN 218345173 U CN218345173 U CN 218345173U CN 202120532125 U CN202120532125 U CN 202120532125U CN 218345173 U CN218345173 U CN 218345173U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- pressure
- regeneration
- adsorption
- flushing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model discloses a regeneration pressure swing adsorption purification hydrogen system is washed to low pressure solves prior art normal pressure and washes that the hydrogen rate of recovery is low and the regeneration technology investment is managed to find time high technical problem in the regeneration technology. The utility model discloses an adsorption tower, feed gas conveying pipeline, wash out the pipeline, the pipeline of releasing gas against the contrary, wash into the pipeline, in the same direction as putting pipeline, second voltage-sharing/third voltage-sharing pipeline, fourth voltage-sharing pipeline, first voltage-sharing and finally step up the pipeline, the outer pipeline of product gas and evacuation equipment, wash into the pipeline and in the same direction as putting the intercommunication between the pipeline and have the pipeline, establish on the pipeline in the same direction as putting the governing valve, first voltage-sharing and finally step up and fill the governing valve through ending between pipeline and the outer pipeline of product gas and be linked together. The utility model discloses the evacuation makes when the adsorption tower is in and washes the step and washes regeneration pressure and be less than the ordinary pressure and wash technology regeneration pressure, and washing efficiency is higher, and the adsorbent regeneration is more thorough to improve adsorbent dynamic adsorption capacity, improve the hydrogen rate of recovery.
Description
Technical Field
The utility model belongs to the technical field of pressure swing adsorption purification gas, concretely relates to regeneration pressure swing adsorption purification hydrogen system is washed to low pressure.
Background
The pressure swing adsorption hydrogen purification technology is widely applied to the fields of petroleum, chemical industry, energy and the like, and with the development of industrial technology, a pressure swing adsorption hydrogen purification system becomes a main unit of a large-scale industrial system, and the scale of the pressure swing adsorption hydrogen purification system is gradually increased, and the hydrogen production per hour is dozens of ten thousand cubic meters.
The pressure swing adsorption hydrogen purification technology is to utilize the difference of adsorption capacity of an adsorbent to different gases, the adsorption capacity is increased along with the increase of adsorption pressure, and the adsorption capacity is reduced along with the reduction of the adsorption pressure, the hydrogen is adsorbed under high pressure and desorbed and regenerated under low pressure, and thus, the purification of the hydrogen is realized. One of the two regeneration modes of the common adsorbent is normal pressure flushing regeneration, namely, the adsorbent is flushed and regenerated by utilizing a part of hydrogen under normal pressure, and the regeneration pressure is 0.02-0.05 MPag; the other regeneration mode is evacuation regeneration, namely, a vacuum pump is used for vacuumizing the adsorption tower, the adsorbent is regenerated under the vacuum condition, and the regeneration pressure is-0.08 MPag to-0.095 MPa. Wherein, the quantity of the adsorption towers for the flushing regeneration process is small, the investment is low, but the recovery rate of the hydrogen is relatively low; and the evacuation regeneration process needs more pressure equalizing times, and the evacuation process generally has more than 2 steps of pressure equalizing than the flushing process, so that the number of adsorption towers is more, the investment is higher, and the recovery rate of hydrogen is relatively higher.
The purpose of the research of the pressure swing adsorption hydrogen extraction process is to improve the efficiency and the regeneration, and the patent CN210874700U adopts a high-pressure regeneration process to improve the traditional flushing regeneration pressure from 0.02-0.05 MPag to 0.1-0.3 MPag, so that the pressurization energy consumption of desorption gas can be reduced, however, the high-pressure flushing process can reduce the regeneration effect of an adsorbent and reduce the hydrogen recovery rate; in order to improve the regeneration effect of the evacuation process, a plurality of patents disclose that the purge gas is introduced at the later stage of the evacuation step, that is, the evacuation purge process is adopted to enhance the regeneration of the adsorbent at the later stage of the evacuation, for example, patent CN110052114a adopts a process in which evacuation and purge are simultaneously carried out at the middle and later stages of the evacuation step, and simultaneously, the switching between the evacuation process and the purge process can also be realized, and patent technologies such as CN1151957C, CN109276973A, CN109529534A, CN110252083A, CN211635878U introduce the evacuation purge step after the evacuation step, however, the improvement is still based on evacuation regeneration, and more pressure equalizing times, lower regeneration pressure and larger vacuum pump are still needed than the purge process. How to increase the efficiency of the flushing regeneration process remains a problem to be solved.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: provides a system for purifying hydrogen by pressure swing adsorption with low pressure flushing and regeneration, which solves the technical problems of low hydrogen recovery rate and high investment of evacuation regeneration process in the normal pressure flushing and regeneration process in the prior art.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a low-pressure flushing regeneration pressure swing adsorption hydrogen purification system comprises at least three adsorption towers, a raw material gas conveying pipeline, a flushing pipeline and a reverse gas release pipeline which are connected into the adsorption towers, and a flushing inlet pipeline, a forward discharge pipeline, a second pressure equalizing/third pressure equalizing pipeline, a fourth pressure equalizing pipeline, a first pressure equalizing and final boosting pipeline and a product gas output pipeline which are connected from the inside of the adsorption towers; be equipped with evacuation equipment on the washing exit line, wash into the pipeline and put the pipeline in the same direction as between the pipeline intercommunication have the pipeline, be equipped with in the same direction as putting the governing valve on the pipeline, first pressure-equalizing and finally step up and fill the governing valve and be linked together through ending between pipeline and the product gas outward transport pipeline.
Further, a first program control valve 10X is arranged on the raw material gas conveying pipeline.
Further, a second programmable valve 20X is arranged on the flushing outlet line.
Further, a third programmable valve 30X is arranged on the reverse air release pipeline.
Further, a fourth stroke control valve 40X is provided on the flush inlet line.
Further, a fifth sequencing valve 50X is arranged on the sequencing line.
Further, a sixth program control valve 60X is arranged on the fourth pressure equalizing line.
Further, a seventh program control valve 70X is arranged on the second pressure equalizing line/the third pressure equalizing line.
Furthermore, an eighth program control valve 80X is arranged on the first pressure equalizing and final boosting pipeline.
Further, a ninth program control valve 90X is arranged on the product gas outward transmission pipeline.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model has the advantages of simple structure and scientific and reasonable design, convenient to use gives the adsorption tower evacuation when the adsorption tower is in the washing step for wash regenerated pressure and be less than the regeneration pressure that the ordinary pressure washed technology, it is higher to wash efficiency, and the adsorbent regeneration is more thorough, thereby improves the dynamic adsorption capacity of adsorbent, improves the hydrogen rate of recovery, and the hydrogen rate of recovery can improve more than 4 percentage points, and the throughput of unit adsorbent improves more than 30%.
Drawings
FIG. 1 is a flow chart of the system for purifying hydrogen by pressure swing adsorption with low pressure flushing and regeneration (taking 10 towers as an example).
Fig. 2 is the pressure change curve diagram of the low-pressure flushing regeneration adsorption tower of the utility model.
Wherein, the names corresponding to the reference numbers are:
1-raw material gas conveying pipeline, 2-flushing pipeline, 3-reverse gas discharging pipeline, 4-flushing inlet pipeline, 5-forward discharging pipeline, 6-fourth pressure equalizing pipeline, 7-second pressure equalizing/third pressure equalizing pipeline, 8-first pressure equalizing and final pressure boosting pipeline, 9-product gas output pipeline, 10-final filling adjusting valve, 11-forward discharging adjusting valve, 12-vacuumizing equipment, 13-adsorption tower and 14-pipeline.
A first programmable valve 10X, a second programmable valve 20X, a third programmable valve 30X, a fourth programmable valve 40X, a fifth programmable valve 50X, a sixth programmable valve 60X, a seventh programmable valve 70X, an eighth programmable valve 80X, and a ninth programmable valve 90X. Wherein X in 10X, 20X, 30X, 40X, 50X, 60X, 70X, 80X, and 90X is the number of the adsorption tower, and correspondingly, 10X, 20X, 30X, 40X, 50X, 60X, 70X, 80X, and 90X are the numbers of the program control valves, as shown in fig. 1, 10X, 20X, 30X, 40X, 50X, 60X, 70X, 80X, and 90X corresponding to adsorption tower No. T03 are respectively 103, 203, 303, 403, 503, 603, 703, 803, 903, and 10X, 20X, 30X, 40X, 50X, 60X, 70X, 80X, and 90X corresponding to adsorption tower No. T10 are respectively 110, 210, 310, 410, 510, 610, 710, 810, 910, and so on.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings. It is to be understood that the disclosed embodiments are merely exemplary of the invention, and are not intended to limit the invention to the precise embodiments disclosed. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a specific orientation or be constructed and operated in a specific orientation, and thus, it should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; of course, mechanical connection and electrical connection are also possible; alternatively, they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
As shown in fig. 1 and 2, the utility model provides a pressure swing adsorption hydrogen purification system with low-pressure flushing and regeneration, which comprises at least three adsorption towers 13, a raw material gas conveying pipeline 1 connected to the interior of the adsorption tower 13 and provided with a first program control valve 10X, a flushing outlet pipeline 2 provided with a second program control valve 20X, a reverse gas discharging pipeline 3 provided with a third program control valve 30X, a flushing inlet pipeline 4 connected from the interior of the adsorption tower 13 and provided with a fourth program control valve 40X, a forward discharging pipeline 5 provided with a fifth program control valve 50X, a second pressure equalizing/third pressure equalizing pipeline 7 provided with a seventh program control valve 70X, a fourth pressure equalizing pipeline 6 provided with a sixth program control valve 60X, a first pressure equalizing and final pressure increasing pipeline 8 provided with an eighth program control valve 80X, and a product gas output pipeline 9 provided with a ninth program control valve 90X; the flushing pipeline 2 is provided with a vacuumizing device 12, a pipeline 14 is communicated between the flushing pipeline 4 and the clockwise releasing pipeline 5, the pipeline 14 is provided with a clockwise releasing regulating valve 11, and the first pressure equalizing and final boosting pipeline 8 and the product gas output pipeline 9 are communicated through a final filling regulating valve 10.
The utility model has the advantages of simple structure and scientific and reasonable design, convenient to use gives the adsorption tower evacuation when the adsorption tower is in the washing step for wash regenerated pressure and be less than the regeneration pressure that the ordinary pressure washed technology, it is higher to wash efficiency, and the adsorbent regeneration is more thorough, thereby improves the dynamic adsorption capacity of adsorbent, improves the hydrogen rate of recovery, and the hydrogen rate of recovery can improve more than 4 percentage points, and the throughput of unit adsorbent improves more than 30%.
The utility model also provides a low pressure washes regeneration pressure swing adsorption purification hydrogen method of system, adopt at least three adsorption tower to carry out pressure swing adsorption purification hydrogen through the recirculation step respectively, be filled with the molecular sieve adsorbent in the adsorption tower, perhaps one kind in molecular sieve and the active alumina, active carbon, silica gel is to the multiple composite adsorption bed of constituteing, every adsorption tower experiences the recirculation step in proper order for the adsorption step, the cisoid step of stepping down, reverse step of stepping down, regeneration step and reverse step of stepping up are washed to the low pressure. Wherein, the adsorption step is that the raw material gas enters the adsorption tower from the feed end of the adsorption tower under the pressure of 1.0-7.0 MPa, non-hydrogen impurities are adsorbed by the adsorbent, and a hydrogen product flows out from the discharge end of the adsorption tower; the forward depressurization step is that gas in the adsorption tower flows out of the adsorption tower along the gas flow direction during adsorption, the pressure in the adsorption tower is reduced, the forward depressurization step comprises at least two depressurization processes, and the forward depressurization step comprises a pressure equalizing depressurization step and a forward release step of providing flushing regeneration gas for the regeneration adsorption tower; the reverse pressure reduction step is that the gas in the adsorption tower flows out of the adsorption tower against the flow direction of the gas during adsorption, the pressure in the adsorption tower is reduced, and the reverse pressure reduction step comprises at least one pressure reduction process; the low-pressure flushing regeneration step is that the regenerated gas is flushed from the outlet end of the adsorption tower against the gas flow direction during adsorption, the impurities adsorbed in the adsorption tower are desorbed under low pressure and flow out of the adsorption tower along with the flushing gas, and in the process, the vacuumizing equipment vacuumizes the adsorption tower in the flushing regeneration step to ensure that the internal pressure of the adsorption tower is-0.06-0.005 MPa, preferably-0.035-0.005 MPa; the reverse pressure increasing step comprises a pressure equalizing and increasing step and a final pressure increasing step, the pressure equalizing and increasing step is an adsorption tower after regeneration is completed, and the gas in the forward pressure reducing step is used for reversely increasing the pressure of the adsorption tower; and in the final pressure boosting step, the pressure of the adsorption tower is boosted to the adsorption pressure by utilizing product gas or raw gas in the adsorption tower completing the pressure equalizing and boosting step.
By adopting the method, when the adsorption tower is in the flushing step, the adsorption tower is vacuumized, so that the pressure for flushing regeneration is lower than the regeneration pressure of a normal-pressure flushing process, the flushing efficiency is higher, the adsorbent is regenerated more thoroughly, the dynamic adsorption capacity of the adsorbent is improved, the hydrogen recovery rate can be improved by more than 4 percent, and the processing capacity of the unit adsorbent is improved by more than 30 percent. The utility model discloses the preferred vacuum pump of evacuation equipment for.
In order to make the technical solution better understood by those skilled in the art, a 10-tower example will now be described in detail. The following concentration percentages are used as mole percentages, pressure gauge, and absolute pressures unless explicitly indicated.
As shown in fig. 1, utilize the utility model discloses a regeneration pressure swing adsorption purification hydrogen system is washed to low pressure, including ten adsorption towers 13, feed gas pipeline 1, product gas outward transport pipeline 9, contrary gassing pipeline 3, wash exit line 2, first voltage-sharing and finally the pipeline 8 that steps up, second voltage-sharing/third voltage-sharing pipeline 7, fourth voltage-sharing pipeline 6, in the same direction as putting pipeline 5, wash into pipeline 4 and program control valve 101 ~ 910, fill governing valve HV101 eventually, in the same direction as putting governing valve PV101, equipment 12 evacuates to find time.
The 10-tower embodiment adopts a 10-2-4/P flow, the process time sequence and the on-off state of a T01 valve of the adsorption tower are shown in Table 1, namely 10 adsorption towers, 2 adsorption towers are used for simultaneous adsorption, 4 steps of pressure equalization and low-pressure flushing regeneration. The cycle process taking the adsorption column T01 as an example is as follows (for convenience of description, the adsorption column 13 will be described below using specific column numbers, that is, the adsorption column 13 will be described as the adsorption column T01, the adsorption column T02, the adsorption column T03, the adsorption column T04, the adsorption column T05, the adsorption column T06, the adsorption column T07, the adsorption column T08, the adsorption column T09, and the adsorption column T10 according to the adsorption columns specifically referred to):
step 1 adsorption step (a): step 1 to step 4, raw material gas flows into the adsorption tower T01 through the raw material gas conveying pipeline 1 and the first program control valve 101, impurities are adsorbed by an adsorbent in the adsorption tower T01, and hydrogen is sent out of the system through the ninth program control valve 901 and the product gas external conveying pipeline 9, so that product gas is obtained.
Step 2 first pressure equalizing and reducing step (1D): step 5, closing the first program control valve 101 and the ninth program control valve 901, opening the eighth program control valve 801 and the eighth program control valve 804, communicating the adsorption tower T01 and the adsorption tower T04 through the first pressure equalizing and final boosting pipeline 8, and performing first pressure equalizing on the adsorption tower T01 and the adsorption tower T04, namely, the adsorption tower T01 is a first pressure equalizing and reducing step, and the adsorption tower T04 is a first pressure equalizing and boosting step.
Step 3, a second pressure equalizing and reducing step (2D): step 6, the eighth program control valve 801 is closed, the seventh program control valve 701 and the seventh program control valve 705 are opened, the adsorption tower T01 and the adsorption tower T05 are communicated through the second pressure equalizing/third pressure equalizing pipeline 7, the adsorption tower T01 and the adsorption tower T05 are subjected to second pressure equalizing, namely, the adsorption tower T01 is a second pressure equalizing and reducing step, and the adsorption tower T05 is a second pressure equalizing and increasing step.
Step 4, a third pressure equalizing and reducing step (3D): step 7, the seventh programmable valve 705 is closed, the seventh programmable valve 706 is opened, the adsorption tower T01 and the adsorption tower T06 are communicated through the second pressure equalizing/third pressure equalizing pipeline 7, the adsorption tower T01 and the adsorption tower T06 perform third pressure equalizing, namely, the adsorption tower T01 is a third pressure equalizing and reducing step, and the adsorption tower T06 is a third pressure equalizing and increasing step.
Step 5, a fourth pressure equalizing and reducing step (4D): step 8, closing the seventh programmable valve 701 and the seventh programmable valve 706, opening the sixth programmable valve 601 and the sixth programmable valve 607, communicating the adsorption tower T01 and the adsorption tower T07 through the fourth pressure equalizing pipeline 6, and performing fourth pressure equalization on the adsorption tower T01 and the adsorption tower T07, namely, the adsorption tower T01 is a fourth pressure equalizing and reducing step, and the adsorption tower T07 is a fourth pressure equalizing and increasing step.
Step 9 a fourth voltage equalizing and boosting step (4R): step 16, closing the second program control valve 201 and the fourth program control valve 401, opening the sixth program control valve 601 and the sixth program control valve 605, communicating the adsorption tower T01 and the adsorption tower T05 through a fourth pressure equalizing pipeline 6, and performing fourth pressure equalization on the adsorption tower T01 and the adsorption tower T05, namely, the adsorption tower T01 is a fourth pressure equalizing and boosting step, and the adsorption tower T05 is a fourth pressure equalizing and depressurizing step.
Step 12 first pressure equalizing and raising step (1R): step 19, closing the seventh programmable valve 701 and the seventh programmable valve 707, opening the eighth programmable valve 801 and the eighth programmable valve 808, communicating the adsorption tower T01 and the adsorption tower T08 through the first pressure equalizing and final pressure increasing pipeline 8, and performing first pressure equalizing on the adsorption tower T01 and the adsorption tower T08, namely, the adsorption tower T01 is a first pressure equalizing and pressure increasing step, and the adsorption tower T08 is a first pressure equalizing and pressure decreasing step.
TABLE 1 example 1 timing and T01 valve switch watch
Note: a: adsorption step, 1D: a first pressure equalizing and reducing step, 2D: a second pressure equalizing and reducing step, 3D: a third pressure equalizing and reducing step, 4D: a fourth pressure equalizing and reducing step, PP: step D: reverse amplification step, PV: low-pressure flushing step, 4R: a fourth voltage equalizing and boosting step, 3R: a third voltage-equalizing and boosting step, 2R: a second voltage-equalizing and boosting step, 1R: a first voltage equalizing and boosting step, FR: and finally, a pressure rising step.
The experiment verifies that a simulation experiment is carried out in a laboratory, the experimental process is 10 < -2 > -4/P, the flow chart is shown in figure 1, the pressure of the raw material gas is 2.5MPa, and the regeneration pressure is-0.035 MPa-0.005 MPa; the raw material gas composition is as follows: h 2 :N 2 :CO:CH 4 :CO 2 1 =77, the purity of hydrogen gas produced is 99.9% or higher, the purity of CO is 10ppmv or lower, and the purity of CO is 10 2 The adsorption tower is less than or equal to 10ppmv, the adsorbent adopts two adsorbents, namely a molecular sieve and activated carbon, the pressure change curve in the adsorption tower is shown in figure 2 (flushing pressure is-0.03 MPa), the system operation performance under different flushing regeneration pressures is shown in table 2, namely the low-pressure flushing process is compared with normal-pressure (0.02-0.05 MPa) flushing, the system performance is obviously improved, the recovery rate of hydrogen is 4.3 percent higher than that of hydrogen in flushing regeneration at-0.03 MPa, and the treatment capacity of the unit adsorbent is improved by 32 percent.
TABLE 2 Performance of the device at different flushing pressures
| Working conditions | Regeneration pressure/MPa | Hydrogen recovery rate/%) | Raw gas treatment capacity/relative value |
| 1 | 0.03 | 88.3 | 100 |
| 2 | 0 | 90.8 | 116 |
| 3 | -0.03 | 92.6 | 132 |
Finally, it should be noted that: the above embodiments are only preferred embodiments of the present invention to illustrate the technical solution of the present invention, but not to limit the same, and certainly not to limit the scope of the present invention; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; that is, the technical problems solved by the present invention are still consistent with the present invention, and all the modifications or colors made in the spirit and the idea of the main design of the present invention are included in the protection scope of the present invention; in addition, will the technical scheme of the utility model direct or indirect application is in other relevant technical field, all including on the same reason the utility model discloses an in the patent protection scope.
Claims (10)
1. A low-pressure flushing regeneration pressure swing adsorption hydrogen purification system is characterized by comprising at least three adsorption towers (13), a raw material gas conveying pipeline (1), a flushing outlet pipeline (2) and a reverse gas release pipeline (3) which are connected into the adsorption towers (13), and a flushing inlet pipeline (4), a forward discharging pipeline (5), a second pressure equalizing/third pressure equalizing pipeline (7), a fourth pressure equalizing pipeline (6), a first pressure equalizing and final boosting pipeline (8) and a product gas output pipeline (9) which are connected from the adsorption towers (13); the flushing pipeline (2) is provided with a vacuum pumping device (12), a pipeline (14) is communicated between the flushing inlet pipeline (4) and the forward discharging pipeline (5), the pipeline (14) is provided with a forward discharging regulating valve (11), and the first pressure equalizing and final boosting pipeline (8) is communicated with the product gas output pipeline (9) through a final charging regulating valve (10).
2. The system for purifying hydrogen through pressure swing adsorption with low pressure flushing regeneration according to claim 1, characterized in that the feed gas conveying pipeline (1) is provided with a first programmable valve 10X.
3. The system for purifying hydrogen through pressure swing adsorption with low pressure flush regeneration according to claim 1, wherein the second program control valve 20X is provided on the flush outlet line (2).
4. The system for purifying hydrogen through pressure swing adsorption with low pressure flushing regeneration according to claim 1, wherein the reverse vent line (3) is provided with a third program control valve 30X.
5. The system for purifying hydrogen through pressure swing adsorption with low pressure flush regeneration according to claim 1, wherein the flush inlet line (4) is provided with a fourth program control valve 40X.
6. The system for purifying hydrogen through pressure swing adsorption with low pressure flushing regeneration as claimed in claim 1, wherein a fifth programmable valve 50X is arranged on the forward discharging pipeline (5).
7. The system for purifying hydrogen through pressure swing adsorption with low pressure flushing regeneration as claimed in claim 1, wherein a sixth programmable valve 60X is arranged on the fourth pressure equalizing pipeline (6).
8. A system for purifying hydrogen by pressure swing adsorption with low pressure flush regeneration according to claim 1, wherein the second pressure equalizing/third pressure equalizing line (7) is provided with a seventh programmable valve 70X.
9. A low pressure flush regeneration pressure swing adsorption hydrogen purification system as claimed in claim 1 wherein the first equalization and final boost line (8) is provided with an eighth programmable valve 80X.
10. The system for purifying hydrogen through pressure swing adsorption with low pressure flushing regeneration as claimed in claim 1, wherein the product gas output pipeline (9) is provided with a ninth programmable valve 90X.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120532125.4U CN218345173U (en) | 2021-03-15 | 2021-03-15 | Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120532125.4U CN218345173U (en) | 2021-03-15 | 2021-03-15 | Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218345173U true CN218345173U (en) | 2023-01-20 |
Family
ID=84921308
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120532125.4U Active CN218345173U (en) | 2021-03-15 | 2021-03-15 | Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218345173U (en) |
-
2021
- 2021-03-15 CN CN202120532125.4U patent/CN218345173U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104058371A (en) | Pressure swing adsorption gas production system and pressure swing adsorption gas production method | |
| CN113350968A (en) | Hydrogen extraction device and process for recovering tail gas components by using synthetic hydrogen | |
| CN103112823B (en) | Method and device for jointly separating hydrogen through pressure swing adsorption and unpowered membrane separation | |
| CN101700876B (en) | Nitrogen making method by pressure swing adsorption | |
| CN111204712A (en) | Pressure swing adsorption gas hydrogen separation and purification system and separation and purification method thereof | |
| WO2024098997A1 (en) | Pressure swing adsorption gas separation method and device for variable-path step-by-step voltage sharing | |
| CN112919414A (en) | Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system and hydrogen purification method | |
| CN218345173U (en) | Low-pressure flushing regeneration pressure swing adsorption hydrogen purification system | |
| CN113457373A (en) | VPSA oxygen generation process and system for efficiently utilizing adsorbent | |
| CN1302983C (en) | Pressure swing adsorption continuous oxygen generation method | |
| CN208829260U (en) | Pressure swing adsorption hydrogen production system | |
| CN111320136B (en) | Method and system for separating and purifying hydrogen from mixed gas | |
| CN206823468U (en) | A kind of device of pressure-variable adsorption recovery hydrogen | |
| CN113426245B (en) | High-purity gas preparation method based on pressure swing adsorption | |
| CN108821248A (en) | A kind of novel energy-saving high-efficiency type PSA equipment of making nitrogen | |
| CN208049671U (en) | A kind of device improving recycling hydrogen purity | |
| CN212309247U (en) | High-frequency valve back-blowing pipeline for molecular sieve adsorption integrated tower | |
| CN212712741U (en) | PSA pressure swing adsorption oxygen and nitrogen generation integrated system | |
| CN1215627A (en) | Pressure swing adsorption process for separating carbon monooxide from carbon monooxide contg. mixed gas | |
| CN213160114U (en) | Pressure swing adsorption forward and backward discharging system | |
| CN212492394U (en) | Device system for recovering nitrogen in polyethylene device flare gas | |
| CN113041782B (en) | Gas pressure swing adsorption separation and purification system and separation and purification method thereof | |
| CN209306950U (en) | A kind of novel energy-saving high-efficiency type PSA equipment of making nitrogen | |
| CN111232937A (en) | Multi-tower cyclic pressure swing adsorption nitrogen production device and method | |
| CN220609748U (en) | Pressure swing adsorption pressure equalizing recovery system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |