CA2200997A1 - Process for treating a gas mixture by pressure swing adsorption - Google Patents
Process for treating a gas mixture by pressure swing adsorptionInfo
- Publication number
- CA2200997A1 CA2200997A1 CA002200997A CA2200997A CA2200997A1 CA 2200997 A1 CA2200997 A1 CA 2200997A1 CA 002200997 A CA002200997 A CA 002200997A CA 2200997 A CA2200997 A CA 2200997A CA 2200997 A1 CA2200997 A1 CA 2200997A1
- Authority
- CA
- Canada
- Prior art keywords
- adsorber
- gas
- process according
- cycle
- countercurrent
- 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.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000000203 mixture Substances 0.000 title claims description 5
- 238000001179 sorption measurement Methods 0.000 title claims description 4
- 230000006837 decompression Effects 0.000 claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 30
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
- 238000010828 elution Methods 0.000 claims description 6
- 238000010926 purge Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims 1
- 239000003463 adsorbent Substances 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 2
- 230000003584 silencer Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000011067 equilibration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/053—Pressure swing adsorption with storage or buffer vessel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/4006—Less than four
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40077—Direction of flow
- B01D2259/40079—Co-current
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40077—Direction of flow
- B01D2259/40081—Counter-current
Abstract
In this process, for the or each adsorber (1), the duration (T R) of the countercurrent recompression step is much less than that (T D) of the cocurrent decompression step.
Application, in particular, to the production of oxygen from atmospheric air.
Application, in particular, to the production of oxygen from atmospheric air.
Description
The present invention relates to a process for treating a gas mixture by pressure swing adsorption in a plant comprising at least one adsorber of the type wherein, in the or in each adsorber, a cycle is carried out which comprises a production phase and a regeneration phase, the latter including an initial phase, which includes a cocurrent decompression step, and a final phase, which includes a countercurrent recompression step, The invention applies in particular to the production of oxygen by treating atmospheric air.
The pressures in question here are absolute pressures.
Most pressure swing adsorption cycles, intended to separate two or more gases, have, during their sequence of steps, one step at least of cocurrent deccmpression or depressurization, to which there corresponds at least one countercurrent recompression step which uses the gas output from the cocurrent 20~ decompression step.
The aim of these steps is to improve the overall performance of the cycle by partly recovéring the fraction of the least adsorbable gas or gases which, at the end of the production step, is or are in the front region and in the free volumes of the adsorber, and by using this fluid to recompress partially at least one adsorber at the end of the regeneration phase.
In the absence of this pair of steps, the least adsorbable gas would be removed during the countercurrent decompression or purge step which - follows the cocurrent decompression step, at the same time as the most highly adsorbed fraction of the gas or gases. This gas would then participate in the regeneration of the adsorber by lowering the partial pressure of the most easily adsorbed components, but generally much less effectively than according to the process described above.
In known cycles, irrespective of whether they involve adsorbers which are connected directly together (documents EP-A-354,259 or EP-A-654,439), or one or more adsorbers which are associated with a buffer tank in which the gas output from the cocurrent decompression is temporarily stored (document US-A-5,370,728), the duration of the two coupled steps is identical or practically identical.
However, the Applicant Company has surprisingly found that a process of the aforementioned type, wherein, according to the invention, at least during the recompression step of the final regeneration phase, gas output from the cocurrent decompression step is introduced in countercurrent, the duration of the countercurrent recompression step being less than that of the cocurrent decompression step, allowed the performance of the cycle to be improved substantially.
A process of this type may include one or more of the following characteristics:
- the duration of the countercurrent recompression step is less than 0.8 times, typically less than 0.5 times, that of the cocurrent decompression step;
- the gas output from the cocurrent decompression step is stored temporarily in a buffer tank;
25- the process uses a single adsorber;
- the mixture to be treated is atmospheric air with a view to the production of oxygen.
Illustrative embodiments of the invention will now be described with reference to the appended drawings, in which:
Figure 1 schematically represents one embodiment of a single-adsorber plant for implementing a process according to the invention; and Figure 2 is a diagram which illustrates an example of a cycle according to the invention, implemented in the plant in Figure 1.
The plant in Figure 1 is advantageously intended for producing oxygen, having a purity of the order of 90~ to 93~, from atmospheric air. It ~ .
essentially comprises a single adsorber 1 containing an adsorbent, typically at least one zeolite, a reversible rotary machine 2 forming a compressor and vacuum pump, a filter/silencer 3, a refrigerator 4, a production tank 5 and a buffer tank 6.
The apparatus 2 is connected, on the one hand, via a conduit 7, to the atmosphere through the filter/silencer 3 and, on the other hand, via a conduit 8 which passes through the refrigerator 4, to the inlet of the adsorber 1, which is the lower end thereof. The outlet (upper end) of the adsorber is connected, on the one hand, to the tank 5 via a conduit 9 equipped with a control valve 10 and, on the other hand, to the buffer tank 6 via a conduit 11 equipped with a control valve 12. The production conduit of the plant, which departs from the tank 5, has been indicated at 13.
The plant furthermore includes means, known per se and not shown, for control, regulation and supply of electricity and refrigerant, which are designed to carry out the cycle illustrated in Figure 2.
In Figure 2, where the time t is plotted on the abscissa and the absolute pressure P is plotted on the ordinate, the lines oriented by arrows indicate the movements and destinations of the gas flows, and furthermore the direction of flow in the adsorber: when an arrow is in the increasing-ordinate direction (towards the top of the diagram), the flow is termed cocurrent in the adsorber. If the arrow directed upwards is located below the line indicating the pressure in the adsorber, the flow enters the adsorber through the inlet end of the adsorber; if the arrow, directed upwards, is located above the line indicating ~ the pressure, the flow leaves the adsorber through the outlet end of the adsorber, the inlet and outlet ends being respectively those for the gas to be treated and for the gas drawn off in the isobaric production phase;
when an arrow is in the decreasing-ordinate direction (towards the bottom of the diagram), the flow is termed countercurrent in the adsorber. If the arrow directed g ~ 7 .
downwards is located below the line indicating the pressure of the adsorber, the flow leaves the adsorber through the inlet end of the adsorber; if the arrow directed downwards is located above the line indicating the pressure, the flow enters the adsorber through the outlet end of the adsorber, the inlet and outlet ends still being those for the gas to be treated and the gas drawn off in the isobaric production phase.
The cycle in Figure 2, the period T of which is, for example, 86.5 s, comprises the following successive steps:
(1) From t = 0 to tl = 20 s, final cocurrent recompression using the gas to be treated, from a first intermediate pressure PI1 to the maximum pressure PM of the cycle, which is, for example, about 1.5 x 105 Pa.
The pressures in question here are absolute pressures.
Most pressure swing adsorption cycles, intended to separate two or more gases, have, during their sequence of steps, one step at least of cocurrent deccmpression or depressurization, to which there corresponds at least one countercurrent recompression step which uses the gas output from the cocurrent 20~ decompression step.
The aim of these steps is to improve the overall performance of the cycle by partly recovéring the fraction of the least adsorbable gas or gases which, at the end of the production step, is or are in the front region and in the free volumes of the adsorber, and by using this fluid to recompress partially at least one adsorber at the end of the regeneration phase.
In the absence of this pair of steps, the least adsorbable gas would be removed during the countercurrent decompression or purge step which - follows the cocurrent decompression step, at the same time as the most highly adsorbed fraction of the gas or gases. This gas would then participate in the regeneration of the adsorber by lowering the partial pressure of the most easily adsorbed components, but generally much less effectively than according to the process described above.
In known cycles, irrespective of whether they involve adsorbers which are connected directly together (documents EP-A-354,259 or EP-A-654,439), or one or more adsorbers which are associated with a buffer tank in which the gas output from the cocurrent decompression is temporarily stored (document US-A-5,370,728), the duration of the two coupled steps is identical or practically identical.
However, the Applicant Company has surprisingly found that a process of the aforementioned type, wherein, according to the invention, at least during the recompression step of the final regeneration phase, gas output from the cocurrent decompression step is introduced in countercurrent, the duration of the countercurrent recompression step being less than that of the cocurrent decompression step, allowed the performance of the cycle to be improved substantially.
A process of this type may include one or more of the following characteristics:
- the duration of the countercurrent recompression step is less than 0.8 times, typically less than 0.5 times, that of the cocurrent decompression step;
- the gas output from the cocurrent decompression step is stored temporarily in a buffer tank;
25- the process uses a single adsorber;
- the mixture to be treated is atmospheric air with a view to the production of oxygen.
Illustrative embodiments of the invention will now be described with reference to the appended drawings, in which:
Figure 1 schematically represents one embodiment of a single-adsorber plant for implementing a process according to the invention; and Figure 2 is a diagram which illustrates an example of a cycle according to the invention, implemented in the plant in Figure 1.
The plant in Figure 1 is advantageously intended for producing oxygen, having a purity of the order of 90~ to 93~, from atmospheric air. It ~ .
essentially comprises a single adsorber 1 containing an adsorbent, typically at least one zeolite, a reversible rotary machine 2 forming a compressor and vacuum pump, a filter/silencer 3, a refrigerator 4, a production tank 5 and a buffer tank 6.
The apparatus 2 is connected, on the one hand, via a conduit 7, to the atmosphere through the filter/silencer 3 and, on the other hand, via a conduit 8 which passes through the refrigerator 4, to the inlet of the adsorber 1, which is the lower end thereof. The outlet (upper end) of the adsorber is connected, on the one hand, to the tank 5 via a conduit 9 equipped with a control valve 10 and, on the other hand, to the buffer tank 6 via a conduit 11 equipped with a control valve 12. The production conduit of the plant, which departs from the tank 5, has been indicated at 13.
The plant furthermore includes means, known per se and not shown, for control, regulation and supply of electricity and refrigerant, which are designed to carry out the cycle illustrated in Figure 2.
In Figure 2, where the time t is plotted on the abscissa and the absolute pressure P is plotted on the ordinate, the lines oriented by arrows indicate the movements and destinations of the gas flows, and furthermore the direction of flow in the adsorber: when an arrow is in the increasing-ordinate direction (towards the top of the diagram), the flow is termed cocurrent in the adsorber. If the arrow directed upwards is located below the line indicating the pressure in the adsorber, the flow enters the adsorber through the inlet end of the adsorber; if the arrow, directed upwards, is located above the line indicating ~ the pressure, the flow leaves the adsorber through the outlet end of the adsorber, the inlet and outlet ends being respectively those for the gas to be treated and for the gas drawn off in the isobaric production phase;
when an arrow is in the decreasing-ordinate direction (towards the bottom of the diagram), the flow is termed countercurrent in the adsorber. If the arrow directed g ~ 7 .
downwards is located below the line indicating the pressure of the adsorber, the flow leaves the adsorber through the inlet end of the adsorber; if the arrow directed downwards is located above the line indicating the pressure, the flow enters the adsorber through the outlet end of the adsorber, the inlet and outlet ends still being those for the gas to be treated and the gas drawn off in the isobaric production phase.
The cycle in Figure 2, the period T of which is, for example, 86.5 s, comprises the following successive steps:
(1) From t = 0 to tl = 20 s, final cocurrent recompression using the gas to be treated, from a first intermediate pressure PI1 to the maximum pressure PM of the cycle, which is, for example, about 1.5 x 105 Pa.
(2) From tl to t2 = 30 s, substantially isobaric production at pressure PM The production is sent to the tank 5, from which a smaller flow rate of oxygen is drawn off continuously to a user station, via the conduit 13. In practice, as a variant, the production, sent to the tank 5, starts before time tl, during the final pressurization phase at close to the maximum pressure PM of the cycle.
(3) From tl to t3 = 40.5 s, that is to say for a duration TD = 10 . 5 s, cocurrent decompression to a second intermediate pressure PI2. The gas output from the adsorber during this step is sent to the buffer tank 6. As a variant, during this step (3), it is also possible to carry out simultaneous countercurrent decompression.
(4) From t3 to t4 = 83 s, countercurrent decompression by pumping to the minimum pressure Pm cf the cycle, which is, for example, about 0.5 x 105 Pa, then purge/elution, typically substantially isobaric at pressure Pm by continuing the pumping and, simultaneously, countercurrent introduction of production gas originating from the tank 5.
(5) From t4 to T, that is to say for a duration TR = 3.5 s, first countercurrent recompression to the _ - 5 -first intermediate pressure PI1, using gas originating from the buffer tank 6.
As can be seen, according to one aspect of the invention, the duration T~ of the cocurrent decompression step (3) is much greater than the duration TR of the first countercurrent recompression step (5), which uses gas output from step (3).
Surprisingly, it has been observed that the performance of a cycle of this type is substantially improved in comparison with that of a cycle which is similar, but in which each step (3) and (5) has the same duration (10.5 + 3.5)/2 = 7 s. This is clearly demonstrated in the following table, which corresponds to a plant, such as the one described in Figure 1, with PM = 1. 5 x 105 Pa and Pm = 0.45 x 105 Pa.
Cycle No. 1 2 3 4 (Prior (Invention) (Invention) (Counter-art) example) Cycle duration 86.5 86.5 83 83 T(s) Cocurrent 7 10.5 7 3.5 recompression duration TD (S) Countercurrent 7 3.5 3.5 7 recompression duration TR ( S ) Productivity 35.08 37.1 37.3 35.6 (m3(s.t.p.) cf ~2 /m3xh) Yield (~) 57.3 59.5 57.2 54.9 Intrinsic 0.86 0.89 0.86 0.82 productivity (m3(s.t.p.) of c2/m3x cycle) Specific energy 0.30 0.29 0.30 0.31 (kWh/m (s.t.p.) of ~2 ) The productivity is, conventionally, the hourly production of the plant for 1 m3 of adsorbent; the intrinsic productivity is the production per cycle for 1 m3 of adsorbent; the specific energy is the energy required to produce 1 m3 ( s . t.p.) of oxygen; and the yield is the ratio of the quantity of oxygen produced to the quantity of oxygen contained in the air which is treated.
In the above table:
- Cycle No. 1 is a conventional cycle, in which the durations TD and TR are equal.
- Cycle No. 2 corresponds to the cycle according to the invention in Figure 2, with TD = 10 . 5 s and TR = 3 . 5 s. An improvement in all the parameters is observed. In particular, the productivity is increased, while the specific energy is reduced. For its part, the yield is also increased, although this is not, per se, an important parameter in the case of treating atmospheric air, which costs nothing.
- Cycle No. 3 is also a cycle according to the invention, but one which differs from the former cycle in that the duration TD is the same (7 s) as in the conventional cycle No. 1. It is observed that, in comparison with the latter, the specific energy is increased, but that the intrinsic productivity remains unchanged; consequently, since the cycle is shorter, the productivity is greater. A cycle of this type may therefore be beneficial in regions where energy is inexpensive.
In cycle No. 4, by way of counter-example, in contrast to the teachings of the invention, it is the cycle TD which is reduced. A degradation in all the parameters (productivity, yield, specific energy, intrinsic productivity) is observed. In particular, the 3 5 drop in intrinsic productivity is greater than the gain which might be expected from the reduction in the duration of the cycle, so that the productivity is reduced.
-The invention is also applicable to cycles which differ from the one in Figure 2 by the fact of simultaneously carrying out, during step (5), cocurrent introduction, into the adsorber, of the gas mixture to be separated, or countercurrent removal in order to complete the elution, or alternatively by temporarily introducing gas from the tank 6 in countercurrent during the purge/elution step 4, typically at the end of the latter.
By way of example, for implementing a cycle of the type described above, with an adsorbent of zeolite 5A type and a pressure PI2 of 1.1 x 105 Pa, with medium-purity oxygen storage at a pressure differential of about 0.3 x 105 Pa, the volume of the tank 6 is about 3.5 m3/m3 of zeolite.
For implementation with two adsorbers in parallel, the common use of the two tanks 5 and 6 allows, in particular, continuous use of the vacuum pump and two-stage pseudo-equilibration between the two adsorbers.
As can be seen, according to one aspect of the invention, the duration T~ of the cocurrent decompression step (3) is much greater than the duration TR of the first countercurrent recompression step (5), which uses gas output from step (3).
Surprisingly, it has been observed that the performance of a cycle of this type is substantially improved in comparison with that of a cycle which is similar, but in which each step (3) and (5) has the same duration (10.5 + 3.5)/2 = 7 s. This is clearly demonstrated in the following table, which corresponds to a plant, such as the one described in Figure 1, with PM = 1. 5 x 105 Pa and Pm = 0.45 x 105 Pa.
Cycle No. 1 2 3 4 (Prior (Invention) (Invention) (Counter-art) example) Cycle duration 86.5 86.5 83 83 T(s) Cocurrent 7 10.5 7 3.5 recompression duration TD (S) Countercurrent 7 3.5 3.5 7 recompression duration TR ( S ) Productivity 35.08 37.1 37.3 35.6 (m3(s.t.p.) cf ~2 /m3xh) Yield (~) 57.3 59.5 57.2 54.9 Intrinsic 0.86 0.89 0.86 0.82 productivity (m3(s.t.p.) of c2/m3x cycle) Specific energy 0.30 0.29 0.30 0.31 (kWh/m (s.t.p.) of ~2 ) The productivity is, conventionally, the hourly production of the plant for 1 m3 of adsorbent; the intrinsic productivity is the production per cycle for 1 m3 of adsorbent; the specific energy is the energy required to produce 1 m3 ( s . t.p.) of oxygen; and the yield is the ratio of the quantity of oxygen produced to the quantity of oxygen contained in the air which is treated.
In the above table:
- Cycle No. 1 is a conventional cycle, in which the durations TD and TR are equal.
- Cycle No. 2 corresponds to the cycle according to the invention in Figure 2, with TD = 10 . 5 s and TR = 3 . 5 s. An improvement in all the parameters is observed. In particular, the productivity is increased, while the specific energy is reduced. For its part, the yield is also increased, although this is not, per se, an important parameter in the case of treating atmospheric air, which costs nothing.
- Cycle No. 3 is also a cycle according to the invention, but one which differs from the former cycle in that the duration TD is the same (7 s) as in the conventional cycle No. 1. It is observed that, in comparison with the latter, the specific energy is increased, but that the intrinsic productivity remains unchanged; consequently, since the cycle is shorter, the productivity is greater. A cycle of this type may therefore be beneficial in regions where energy is inexpensive.
In cycle No. 4, by way of counter-example, in contrast to the teachings of the invention, it is the cycle TD which is reduced. A degradation in all the parameters (productivity, yield, specific energy, intrinsic productivity) is observed. In particular, the 3 5 drop in intrinsic productivity is greater than the gain which might be expected from the reduction in the duration of the cycle, so that the productivity is reduced.
-The invention is also applicable to cycles which differ from the one in Figure 2 by the fact of simultaneously carrying out, during step (5), cocurrent introduction, into the adsorber, of the gas mixture to be separated, or countercurrent removal in order to complete the elution, or alternatively by temporarily introducing gas from the tank 6 in countercurrent during the purge/elution step 4, typically at the end of the latter.
By way of example, for implementing a cycle of the type described above, with an adsorbent of zeolite 5A type and a pressure PI2 of 1.1 x 105 Pa, with medium-purity oxygen storage at a pressure differential of about 0.3 x 105 Pa, the volume of the tank 6 is about 3.5 m3/m3 of zeolite.
For implementation with two adsorbers in parallel, the common use of the two tanks 5 and 6 allows, in particular, continuous use of the vacuum pump and two-stage pseudo-equilibration between the two adsorbers.
Claims (9)
1. Process for treating a gas mixture by pressure swing adsorption in a plant comprising at least one adsorber (1), wherein, in the or in each adsorber (1), a cycle is carried out which comprises a production phase and a regeneration phase, the latter including an initial phase, which includes a cocurrent decompression step, and a final phase, which includes a countercurrent recompression step, characterized in that, at least during the recompression step (5) of the final regeneration phase, gas output from the cocurrent decompression step (3) is introduced in countercurrent, and in that the duration (TR) of the countercurrent recompression step (5) is less than that (TD) of the cocurrent decompression step (3).
2. Process according to Claim 1, characterized in that the duration (TR) of the countercurrent recompression step is less than 0.8 times that (TD) of the cocurrent decompression step.
3. Process according to Claim 2, characterized in that the duration (TR) of the countercurrent recompression step is less than 0.5 times that (TD) of the cocurrent decompression step.
4. Process according to any one of Claims 1 to 3, characterized in that the gas output from the cocurrent decompression step (3) is stored temporarily in a buffer tank (6).
5. Process according to one of Claims 1 to 4, employed in a plant using a single adsorber (1).
6. Process according to one of Claims 1 to 5, characterized in that the regeneration phase comprises an intermediate purge/elution phase (4).
7. Process according to Claim 6, characterized in that the purge/elution gas is production gas.
8. Process according to Claim 7, characterized in that the purge/elution gas is stored temporarily in a production tank (5).
9. Process according to one of the preceding claims, for the separation of oxygen from air.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR9603809 | 1996-03-27 | ||
| FR9603809A FR2746668B1 (en) | 1996-03-27 | 1996-03-27 | PROCESS FOR TREATING A GAS MIXTURE BY PRESSURE VARIATION ADSORPTION |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2200997A1 true CA2200997A1 (en) | 1997-09-27 |
Family
ID=9490598
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002200997A Abandoned CA2200997A1 (en) | 1996-03-27 | 1997-03-25 | Process for treating a gas mixture by pressure swing adsorption |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US5772737A (en) |
| EP (1) | EP0798028B1 (en) |
| JP (1) | JPH1024208A (en) |
| CN (1) | CN1170624A (en) |
| CA (1) | CA2200997A1 (en) |
| DE (1) | DE69724311T2 (en) |
| ES (1) | ES2205143T3 (en) |
| FR (1) | FR2746668B1 (en) |
Families Citing this family (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2755875B1 (en) * | 1996-11-15 | 1999-01-29 | Air Liquide | PROCESS AND INSTALLATION FOR SEPARATION OF GAS MIXTURES BY ADSORPTION AT VARIATION OF PRESSURE |
| US5882380A (en) * | 1997-05-14 | 1999-03-16 | Air Products And Chemicals, Inc. | Pressure swing adsorption process with a single adsorbent bed |
| FR2764205B1 (en) * | 1997-06-09 | 1999-07-16 | Air Liquide | PSA DEVICE AND METHOD FOR SEPARATING A GASEOUS MIXTURE |
| US5961694A (en) * | 1997-06-09 | 1999-10-05 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus and process for the separation of gas mixtures by pressure swing adsorption |
| FR2765810B1 (en) * | 1997-07-09 | 1999-08-13 | Air Liquide | METHOD FOR SEPARATING A GAS MIXTURE BY PRESSURE VARIATION ADSORPTION |
| US6010555A (en) * | 1997-11-04 | 2000-01-04 | Praxair Technology, Inc. | Vacuum pressure swing adsorption system and method |
| US6048384A (en) * | 1997-12-09 | 2000-04-11 | Smolarek; James | PSA process and system using simultaneous top and bottom evacuation of absorbent bed |
| US5997611A (en) * | 1998-07-24 | 1999-12-07 | The Boc Group, Inc. | Single vessel gas adsorption system and process |
| US6217635B1 (en) * | 1998-11-09 | 2001-04-17 | Fantom Technologies Inc. | Method and apparatus for concentrating a gas using a single stage adsorption chamber |
| US6156100A (en) * | 1999-02-01 | 2000-12-05 | Fantom Technologies, Inc. | Method and apparatus for concentrating a gas using a single stage adsorption zone |
| US6162283A (en) * | 1999-02-01 | 2000-12-19 | Fantom Technologies Inc. | Method and apparatus for concentrating a gas using a single stage adsorption zone |
| US6096115A (en) * | 1998-11-25 | 2000-08-01 | Air Products And Chemicals, Inc. | Pressure swing adsorption process and system utilizing two product storage tanks |
| US6102985A (en) * | 1998-11-25 | 2000-08-15 | Air Products And Chemicals, Inc. | Pressure swing adsorption process and system with dual product storage tanks |
| US6146447A (en) * | 1998-11-25 | 2000-11-14 | Air Products And Chemicals, Inc. | Oxygen generation process and system using single adsorber and single blower |
| US6156101A (en) * | 1999-02-09 | 2000-12-05 | Air Products And Chemicals, Inc. | Single bed pressure swing adsorption process and system |
| US6183538B1 (en) | 1999-02-09 | 2001-02-06 | Air Products And Chemicals, Inc. | Pressure swing adsorption gas flow control method and system |
| FR2806321B1 (en) * | 2000-03-16 | 2002-10-11 | Air Liquide | METHOD AND REACTOR FOR TREATING A GAS USING A REGENERABLE ACTIVE TRIM |
| KR100731775B1 (en) * | 2000-10-12 | 2007-06-22 | 엘지전자 주식회사 | control mathod and control device in oxygen generator |
| US6425938B1 (en) * | 2000-11-01 | 2002-07-30 | Air Products And Chemicals, Inc. | Single bed pressure swing adsorption process |
| JPWO2002049959A1 (en) * | 2000-12-19 | 2004-04-22 | 住友精化株式会社 | Recovery method of concentrated oxygen gas |
| FR2833183B1 (en) * | 2001-12-12 | 2004-01-23 | Air Liquide | PROCESS FOR TREATMENT BY ADSORPTION OF A GAS MIXTURE, AND CARBON MONOXIDE PRODUCTION PLANT INCLUDING A TREATMENT UNIT FOR IMPLEMENTATION OF SUCH A PROCESS |
| CN1287886C (en) * | 2004-06-11 | 2006-12-06 | 成都天立化工科技有限公司 | Improved two-stage pressure-varying adsorption method for preparing high-purity oxygen |
| US7954490B2 (en) | 2005-02-09 | 2011-06-07 | Vbox, Incorporated | Method of providing ambulatory oxygen |
| EP2456540A4 (en) | 2009-07-22 | 2013-10-09 | Vbox Inc | Apparatus for separating oxygen from ambient air |
Family Cites Families (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3430418A (en) * | 1967-08-09 | 1969-03-04 | Union Carbide Corp | Selective adsorption process |
| US3564816A (en) * | 1968-12-30 | 1971-02-23 | Union Carbide Corp | Selective adsorption process |
| US3636679A (en) * | 1971-01-04 | 1972-01-25 | Union Carbide Corp | Selective adsorption gas separation process |
| US3788036A (en) * | 1972-07-26 | 1974-01-29 | D Stahl | Pressure equalization and purging system for heatless adsorption systems |
| US4194890A (en) * | 1976-11-26 | 1980-03-25 | Greene & Kellogg, Inc. | Pressure swing adsorption process and system for gas separation |
| US4381189A (en) * | 1981-10-27 | 1983-04-26 | Union Carbide Corporation | Pressure swing adsorption process and system |
| US4468237A (en) * | 1982-10-19 | 1984-08-28 | Union Carbide Corporation | Pressure swing adsorption with direct and indirect pressure equalizations |
| US4643743A (en) * | 1983-02-10 | 1987-02-17 | Union Carbide Corporation | Pressure swing adsorption process for supplying oxygen under variable demand conditions |
| US4561865A (en) * | 1983-11-01 | 1985-12-31 | Greene & Kellogg, Inc. | Single bed pressure swing adsorption gas separation system |
| DE3433058A1 (en) * | 1984-09-08 | 1986-03-20 | Bergwerksverband Gmbh, 4300 Essen | METHOD AND DEVICE FOR PRODUCING NITROGEN |
| US4589888A (en) * | 1984-10-05 | 1986-05-20 | Union Carbide Corporation | Pressure swing adsorption process |
| US4816039A (en) * | 1986-02-24 | 1989-03-28 | The Boc Group, Inc. | PSA multicomponent separation utilizing tank equalization |
| FR2599274B1 (en) * | 1986-06-02 | 1988-08-26 | Air Liquide | PROCESS AND PLANT FOR SEPARATING A GAS MIXTURE BY ADSORPTION. |
| US5223004A (en) * | 1990-03-02 | 1993-06-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for producing oxygen by adsorption separation from air |
| JP2981302B2 (en) * | 1991-05-13 | 1999-11-22 | 東洋エンジニアリング株式会社 | Gas separation method |
| US5248322A (en) * | 1992-10-01 | 1993-09-28 | Air Products And Chemicals, Inc. | Depressurization effluent repressurized adsorption process |
| US5370728A (en) * | 1993-09-07 | 1994-12-06 | Praxair Technology, Inc. | Single bed pressure swing adsorption system and process |
| US5382280A (en) * | 1993-11-16 | 1995-01-17 | Air Products And Chemicals, Inc. | Two stage pressure swing adsorption process for producing the less strongly adsorbed component of a feed gas mixture |
| US5565018A (en) * | 1995-07-12 | 1996-10-15 | Praxair Technology, Inc. | Optimal pressure swing adsorption refluxing |
| US5620501A (en) * | 1995-08-15 | 1997-04-15 | The Boc Group, Inc. | Recovery of trace gases from gas streams |
| US5656065A (en) * | 1995-10-04 | 1997-08-12 | Air Products And Chemicals, Inc. | Multibed pressure swing adsorption apparatus and method for the operation thereof |
| US5658371A (en) * | 1995-11-06 | 1997-08-19 | Praxair Technology, Inc. | Single bed pressure swing adsorption process for recovery of oxygen from air |
-
1996
- 1996-03-27 FR FR9603809A patent/FR2746668B1/en not_active Expired - Fee Related
-
1997
- 1997-03-20 EP EP97400632A patent/EP0798028B1/en not_active Expired - Lifetime
- 1997-03-20 ES ES97400632T patent/ES2205143T3/en not_active Expired - Lifetime
- 1997-03-20 DE DE69724311T patent/DE69724311T2/en not_active Expired - Fee Related
- 1997-03-25 CA CA002200997A patent/CA2200997A1/en not_active Abandoned
- 1997-03-26 US US08/827,055 patent/US5772737A/en not_active Expired - Fee Related
- 1997-03-26 CN CN97109646.5A patent/CN1170624A/en active Pending
- 1997-03-26 JP JP9074128A patent/JPH1024208A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| ES2205143T3 (en) | 2004-05-01 |
| FR2746668A1 (en) | 1997-10-03 |
| EP0798028A1 (en) | 1997-10-01 |
| FR2746668B1 (en) | 1998-04-30 |
| EP0798028B1 (en) | 2003-08-27 |
| DE69724311D1 (en) | 2003-10-02 |
| JPH1024208A (en) | 1998-01-27 |
| US5772737A (en) | 1998-06-30 |
| DE69724311T2 (en) | 2004-06-24 |
| CN1170624A (en) | 1998-01-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5772737A (en) | Process for treating a gas mixture by pressure swing adsorption | |
| US4070164A (en) | Adsorption-desorption pressure swing gas separation | |
| JP3492869B2 (en) | Single bed pressure swing adsorption method for oxygen recovery from air | |
| US4969935A (en) | Process for treating a gaseous mixture by adsorption | |
| US5518526A (en) | Pressure swing adsorption process | |
| KR100254295B1 (en) | Pressure swing adsorption process with a single adsorbent bed | |
| US4406675A (en) | RPSA Process | |
| US6010555A (en) | Vacuum pressure swing adsorption system and method | |
| FI85953B (en) | FOERFARANDE FOER FRAMSTAELLNING AV EN SYREPRODUKT MED EN RENHETSGRAD AV 95% FRAON OMGIVANDE LUFT. | |
| US5702504A (en) | Vacuum pressure swing adsorption process | |
| US5906674A (en) | Process and apparatus for separating gas mixtures | |
| US6524370B2 (en) | Oxygen production | |
| EP1004342B1 (en) | Pressure swing adsorption gas separation process and system using single adsorber and product recycle | |
| EP1018359A2 (en) | Pressure swing adsorption process and system with product storage tank(s) | |
| US5441558A (en) | High purity nitrogen PSA utilizing controlled internal flows | |
| US6045603A (en) | Two phase pressure swing adsorption process | |
| US6048384A (en) | PSA process and system using simultaneous top and bottom evacuation of absorbent bed | |
| JPH04330913A (en) | Absorption process for separating gaseous mixture | |
| JPH07745A (en) | Gas separation | |
| US5997611A (en) | Single vessel gas adsorption system and process | |
| US6090185A (en) | Process for gas separation by adsorption with variable production rate | |
| GB2109266A (en) | Pressure swing process for the separation of gas mixtures by adsorption | |
| US5968233A (en) | Method and plant for the treatment of a gas mixture by pressure-swing adsorption | |
| EP0482863A1 (en) | PSA Employing high purity purging | |
| JPS6027606A (en) | Preparation of nitrogen by pressure swing adsorption method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |