US 5,248,322 AGrant
Depressurization Effluent Repressurized Adsorption Process
Issue Date:1993-09-28
•8 Claims
•1 Drawing Sheets
Abstract
A pressure swing adsorption process is set forth for the recovery of two gas products at high recovery and high purity using the steps of adsorption, depressurization, evacuation and repressurization. A portion of the depressurization effuent is used to partially accomplish the repressurization step.
Metadata
Assignee
- Air Products and Chemicals, Inc.
Inventor
- Ravi Kumar
Application Information
Application Number:US 9556206
Filing Date:1992-10-01
Priority Date:1992-10-01
Art Unit:135
Classifications
IPC:
B01D 5304
Field of Search:
5525;26;58;62;68;74;75;71;73
Patent Drawings (1 sheets)
Description
Field of the Invention
The present invention is directed to a pressure swing adsorption process which uses a plurality of parallel adsorption beds to separate more readily adsorbed gas component(s) from less readily adsorbed gas component(s) in a gas mixture comprising the steps of adsorption, depressurization, evacuation and repressurization.
Background of the Invention
Pressure swing adsorption (PSA) processes which use a plurality of parallel adsorption beds to separate more readily adsorbed gas component(s) from less readily adsorbed gas component(s) in a gas mixture comprising the steps of adsorption, depressurization, evacuation and repressurization are known in the art. A state of the art example is the process taught in U.S. Pat. No. 5,026,406 which recovers two gas products at high recovery and high purity while using less power than any comparable process.
It is an object of the present invention to recover two products at high recovery and high purity using the steps of adsorption, depressurization, evacuation and repressurization while using less power than any comparable process, including the state of the art process taught in U.S. Pat. No. 5,026,406.
Summary of the Invention
The present invention is an improvement to a pressure swing adsorption process for the recovery of two gas products at high recovery and high purity from a feed gas stream containing said products wherein a first gas product is one or more, less strongly adsorbed components and a second gas product is one or more, more strongly adsorbed components. The process to which the improvement of the present invention pertains comprises:
(a) introducing a feed gas stream at elevated pressure containing said one or more, less strongly adsorbed components and said one or more, more strongly adsorbed components into one of a plurality of parallel adsorptive beds filled with one or more adsorbents selective for said one or more, more strongly adsorbed components, so as to retain said one or more, more strongly adsorbed components on said one or more adsorbents and allow said one or more, less strongly adsorbed components to pass through said bed for recovery as said first gas product at high recovery and high purity;
(b) terminating the introduction of said feed gas stream into said bed before said one or more, more strongly adsorbed components break through the downstream end of said bed and depressurizing said bed to approximately ambient pressure to remove said one or more, less strongly adsorbed components from said bed and recycling a portion of the resulting depressurization effluent to said feed gas stream;
(c) evacuating said bed to a subambient pressure to recover said one or more, more strongly adsorbed components as said second gas product at high recovery and high purity; and
(d) repressurizing said bed with one or more, less strongly adsorbed components to approximately the pressure of the feed gas stream, wherein the steps (a) through (d) are performed on said plurality of beds to result in a continuous process.
The improvement increases the energy efficiency of the process and comprises a depressurization effluent repressurization step wherein said bed is partially repressurized after step (c) and prior to the repressurization step (d) with a last portion of the depressurization effluent from one of said parallel beds presently undergoing step (b).
In one embodiment of the present invention, the process further comprises a low pressure purge step after step (b) and prior to step (c) wherein a low pressure purge gas stream of one or more, more strongly adsorbed components is passed through said bed to remove any residual one or more, less strongly adsorbed components from said bed.
Brief Description of the Drawings
FIG. 1 is a schematic diagram illustrating one embodiment of the present invention.
Detailed Description of the Invention
To better understand the present invention, it is important to understand the prior art with respect to PSA processes which use a plurality of parallel adsorption beds to separate more readily adsorbed gas component(s) from less readily adsorbed gas component(s) in a gas mixture. A state of the art example is the following process taught in claim 1 of U.S. Pat. No. 5,026,406 as follows:
"1. A pressure swing adsorption process for recovery of two gas products at high recovery and high purity from a feed gas stream containing said products wherein a first gas product is one or more, less strongly adsorbed components and a second gas product is one or more, more strongly adsorbed components, comprising:
(a) introducing a feed gas stream at elevated pressure containing said one or more, less strongly adsorbed components and said one or more, more strongly adsorbed components into one of a plurality of parallel adsorptive beds filled with one or more adsorbents selective for said one or more, more strongly adsorbed components, so as to retain said one or more, more strongly adsorbed components on said one or more adsorbents and allow said one or more, less strongly adsorbed components to pass through said bed for recovery as said first gas product at high recovery and high purity;
(b) terminating the introduction of said feed gas stream into said bed before said one or more, more strongly adsorbed components break through the downstream end of said bed and depressurizing said bed to approximately ambient pressure to remove said one or more, less strongly adsorbed components from said bed and recycling the resulting depressurization effluent to said feed gas stream;
(c) passing a low pressure purge gas stream of one or more, more strongly adsorbed components through said bed to remove any residual one or more, less strongly adsorbed components from said bed and recycling the resulting effluent from said purged bed to the feed gas stream;
(d) evacuating said bed to a subambient pressure to recover said one or more, more strongly adsorbed components as said second gas product at high recovery and high purity, and
(e) repressurizing said bed with one or more, less strongly adsorbed components to approximately the pressure of the feed gas stream, wherein the steps (a) through (e) are performed on said plurality of beds to result in a continuous process."
The present invention is an improvement to the above process (hereinafter the "prior art process") which increases the energy efficiency of the process. (It should be noted that step (c) of the prior art process is not mandatory for application of the present invention.) The improvement comprises a depressurization effluent repressurization step wherein said bed is partially repressurized after step (d) and prior to the repressurization step (e) with a last portion of the depressurization effluent from one of said parallel beds presently undergoing step (b). In the prior art process, the entire portion of the depressurization effluent is recycled to the feed gas stream. The remaining initial portion of the depressurization effluent from step (b) continues to be recycled to the feed gas stream as in the prior art process. Typically, the first 90%, of the depressurization effluent continues to be recycled to the feed while the last 10%. is used for partial repressurization. Regardless of the split, the effluent is always a last portion of the depressurization effluent.
The depressurization effluent repressurization step increases the energy efficiency of the prior art process because the effluent stream in issue is no longer recycled to the feed as in the prior art process. As a result, this effluent stream no longer has to be compressed to feed pressure as in the prior art process. The skilled practitioner will appreciate that the tradeoff is the efficiency of the adsorption step since the effluent gas being used to partially repressurize the bed consists primarily of the more strongly adsorbed component(s). (Ideally, the repressurization gas should consist only of the less strongly adsorbed component(s)). In particular, the effluent stream from the present invention's adsorption step (i.e. the "first gas product") will contain more of the more strongly adsorbed component(s) than in the prior art process. As a result, the purity of the less strongly adsorbed component(s) in the first gas product and the recovery of the more strongly adsorbed component(s) in the second gas product will both be less than in the prior art process. This negative impact on said purity and recovery is slight however since the volume of gas used in the present invention's partial repressurization step is much smaller than the volume of gas used to complete the repressurization.
A first embodiment of the present invention consists of the following cycle of steps:
1. Adsorption
2. First Depressurization
3. Second Depressurization
4. Evacuation
5. Depressurization Effluent Repressurization
6. Repressurization
A second embodiment of the present invention further includes a low pressure purge step as follows:
1. Adsorption
2. First Depressurization
3. Second Depressurization
4. Low Pressure Purge
5. Evacuation
6. Depressurization Effluent Repressurization
7. Repressurization
The steps in the above embodiments are carried out in two or more adsorbent beds with appropriate gas storage tanks. The process step sequence using five adsorbent beds for each of the above embodiments is listed in Tables 1 and 2, respectively. Other variations can be made to these basic steps. One example of such a variation is the introduction of a blowdown step after the low pressure purge step in case the low pressure purge step is carried out at pressure higher than ambient pressure. Another example is the introduction of one or more pressure equalization steps. Still another example is the introduction of "B" beds in series to the five existing "A" beds for a subsequent purification of the less strongly adsorbed component(s) as taught in U.S. Pat. No. 4,913,709. (The "B" beds are used when ultra-high purity of the less strongly adsorbed component(s) is desired; in such cases, the above described negative impact of the present invention on the purity of the less strongly adsorbed component(s) is non-existant.)
The process cycle for the first embodiment of the present invention will now be described in detail:
1. Adsorption Step, which consists of:
(a) Flowing the feed gas stream at a pressure of approximately 30-500 psia and temperature of approximately 0.degree. -3000 .degree. F. through a bed packed with one or more adsorbents capable of selectively adsorbing the more strongly adsorbed component(s) from the feed gas stream.
(b) Withdrawing an effluent stream of high purity less strongly adsorbed component(s) (the first gas product) from the downstream end of the bed.
(c) Continuing steps l(a) and l(b) for a predetermined cycle time or until the concentration of the more strongly adsorbed component(s) in the effluent stream reaches a preset limit. The bed is now called "spent" because it has exhausted its capacity for adsorbing the more strongly adsorbed component(s) from the feed gas stream.
2. First Depressurization Step, which consists of:
(a) Discontinuing the feed gas stream flow through the "spent" bed and transferring the feed to a parallel bed on step 1(a) of this cycle.
(b) Reducing the pressure in the spent bed to a somewhat lower level (approximately 20-50 psia) by venting the gas in the bed in a direction either opposite to or the same as the feed gas stream flow.
(c) Raising the pressure of all the depressurized gas from step 2(b) to the same level as the feed gas stream pressure in step 1(a) by a compressor.
(d) Mixing the gas from 2(c) with the fresh feed gas stream and feeding the mixed gas to a parallel bed on step l(a) of this cycle.
3. Second Depressurization Step, which consists of:
(a) Further reducing the pressure in the spent bed from the current level (approximately 20-50 psia) to approximately 15 psia by connecting the feed or product end of the bed with the feed or product end of a parallel bed on step 5 of this cycle.
(b) Continuing step 3(a) for a predetermined time or until the pressure in the parallel bed on step 5 of this cycle has reached a predetermined low level (200-760 torr).
4. Evacuation Step, which consists of:
(a) Lowering the pressure of the saturated bed from approximately 15 psia to approximately 40-200 torr by evacuating the gas from the feed end of the bed or by simultaneously evacuating the gas from both the feed and the product ends of the bed.
(b) Storing the evacuated gas which consists of the more strongly adsorbed component(s) at high purity (the second gas product) at ambient pressure.
5. Depressurization Effluent Repressurization Step, which consists of:
(a) Discontinuing the pressure reduction of the bed. The bed is now called "regenerated" because its capacity for adsorbing the more strongly adsorbed gas component(s) has been restored.
(b) Raising the pressure in the regenerated bed from evacuation level (40-200 torr) to a somewhat higher level (200-760 torr) by connecting the product or feed end of this bed with the effluent end of a parallel bed on step 3(a) of this cycle.
(c) Discontinuing this step when the pressure in the regenerated bed has reached a predetermined level or after a predetermined cycle time.
6. Repressurization Step, which consists of:
(a) Further raising the pressure in the regenerated bed from the current level (200-760 torr) to adsorption level (30-500 psia) by connecting the product end of the regenerated bed with the product end of a parallel bed on step 1(b) of this cycle.
(b) Discontinuing the above step when the pressure in the regenerated bed has reached the desired level.
(c) This bed is now ready to undergo a new cycle starting at step 1(a) of this cycle.
The process cycle for the second embodiment of the present invention will now be described in detail:
1. Adsorption Step, which consists of:
(a) Flowing the feed gas stream at a pressure of approximately 30-500 psia and temperature of approximately 0.degree.-300.degree. F. through a bed packed with one or more adsorbents capable of selectively adsorbing the more strongly adsorbed component(s) from the feed gas stream.
(b) Withdrawing an effluent stream of high purity less strongly adsorbed component(s) (the first gas product) from the downstream end of the bed.
(c) Continuing steps 1(a) and 1(b) for a predetermined cycle time or until the concentration of the more strongly adsorbed component(s) in the effluent stream reaches a preset limit. The bed is now called "spent" because it has exhausted its capacity for adsorbing the more strongly adsorbed component(s) from the feed gas stream.
2. First Depressurization Step, which consists of:
(a) Discontinuing the feed gas stream flow through the "spent" bed and transferring the feed to a parallel bed on step 1(a) of this cycle.
(b) Reducing the pressure in the spent bed to a somewhat lower level (approximately 20-50 psia) by venting the gas in the bed in a direction either opposite to or the same as the feed gas stream flow.
(c) Raising the pressure of all the depressurized gas from step 2(b) to the same level as the feed gas stream pressure in step l(a) by a compressor.
(d) Mixing the gas from 2(c) with the fresh feed gas stream and feeding the mixed gas to a parallel bed on step 1(a) of this cycle.
3. Second Depressurization Step, which consists of:
(a) Further reducing the pressure in the spent bed from the current level (approximately 20-50 psia) to approximately 15 psia by connecting the feed or product end of the bed with the feed or product end of a parallel bed on step 6 of this cycle.
(b) Continuing-step 3(a) for a predetermined time or until the pressure in the parallel bed on step 6 of this cycle has reached a predetermined low level (200-760 torr).
4. Low Pressure Purge Step, which consists of:
(a) Flowing a portion of the high purity more strongly adsorbed component(s) obtained from a parallel bed on step 5 of this cycle at approximately 15 psia through the depressurized bed in a direction either countercurrent or cocurrent to the feed gas stream flow.
(b) Continuing step 4(a) for a predetermined cycle time or until the concentration of the more strongly adsorbed component(s) in the effluent stream reaches a preset limit. The bed is now called "saturated."
5. Evacuation Step, which consists of:
(a) Lowering the pressure of the saturated bed from approximately 15 psia to approximately 40-200 torr by evacuating the gas from the feed end of the bed or by simultaneously evacuating the gas from both the feed and the product ends of the bed.
(b) Storing the evacuated gas which is high purity more strongly adsorbed component(s) (the second gas product) at ambient pressure for further use.
(c) Part of this gas stream is used for low pressure purge in step 4(a).
6. Depressurization Effluent Repressurization Step, which consists of:
(a) Discontinuing the pressure reduction of the bed. The bed is now called "regenerated" because its capacity for adsorbing the more strongly adsorbed gas component(s) has been restored.
(b) Raising the pressure in the regenerated bed from evacuation level (40-200 torr) to a somewhat higher level (200-760 torr) by connecting the product or feed end of this bed with the effluent end of a parallel bed on step 3(a) of this cycle.
(c) Discontinuing this step when the pressure in the regenerated bed has reached a predetermined level or after a predetermined cycle time.
7. Repressurization Step, which consists of:
(a) Further raising the pressure in the regenerated bed from the current level (200-760 torr) to adsorption level (30-500 psia) by connecting the product end of the regenerated bed with the product end of a parallel bed on step 1(b) of this cycle.
(b) Discontinuing the above step when the pressure in the regenerated bed has reached the desired level.
(c) This bed is now ready to undergo a new cycle starting at step 1(a) of this cycle.
FIG. 1 is a schematic diagram of the first embodiment of the present invention wherein 5 beds are operated sequentially in parallel with one another according to Table 1's step sequence. Table 3 outlines FIG. 1's valve sequence for a typical cycle time of 20 minutes. Referring now to FIG. 1, a fresh feed gas stream 100 at a pressure and temperature of approximately 100 psia and 700.degree. F. respectively is mixed with the recycle stream 120 at similar pressure and temperature. The mixed gas 140 is fed to one of the PSA beds, let us say bed A1 via open valve 1. This bed has been previously pressurized to the adsorption pressure of approximately 100 psia. The first gas product comprising the less strongly adsorbed component(s) is withdrawn from bed A1 via open valve 26 in line 160. A part of the first gas product from vessel 320 is removed as a product for export in line 340 and the remainder is recycled in line 300 as repressurization gas. The adsorption step is continued until a fixed time or until the effluent concentration of the more strongly adsorbed component(s) from bed Al has reached a predetermined level. At the end of the adsorption step, the feed gas stream is directed to the second bed, let us say bed A2. Bed A1 is now depressurized to approximately 20 psia cocurrently to the feed gas stream flow via open valve 16. The desorbed gas from bed Al is recompressed to the adsorption pressure of approximately 100 psia by the recycle compressor 180 and is mixed with the fresh feed gas stream before entering bed A2, which is on the adsorption step.
At the end of the first depressurization step, valve 16 is closed and the bed is further depressurized to approximately 15 psia by opening valve 21. This depressurization effluent which is rich in the more strongly adsorbed component(s) is introduced into bed A4 via open valve 24. Bed A4 has just finished evacuation and is at a pressure of approximately 100 mmHg.
Following the second depressurization step, bed A1 undergoes pressure reduction by evacuation via open valve 11 through line 220. The pressure in bed A1 is reduced from approximately 15 psia at the end of the second depressurization step to approximately 100 mmhg at the end of the evacuation step by means of vacuum pump 240. The evacuated gas contains the more strongly adsorbed component(s) of the gas mixture and is at a pressure of approximately 1 atmosphere. This gas is removed from vessel 260 as the second gas product in line 280. Bed A1 is then partially repressurized by introducing the second depressurization step effluent from bed A3 via open valves 21 and 23. Finally, Bed A1 is fully repressurized to the adsorption pressure with the first gas product stream via open valves 21 and 31 and line 300. Bed Al is now ready to undergo another cycle starting from the adsorption step.
Example
A feed stream containing hydrogen (67.7%), carbon monoxide (32%), methane (0.2%) and nitrogen (0.1%) at approx 200 psig and 70.degree. C. was used to produce high purity primary product (hydrogen) and secondary product (carbon monoxide) streams when fractionated pursuant to the prior art cycle. Based upon the lab data for the prior art cycle, it is estimated that the second embodiment of the present invention will require 4% less power to produce a similar purity (99%) carbon monoxide stream. Based upon the lab data for the prior art cycle without the low pressure purge step, it is estimated that the first embodiment of the present invention will also require 4% less power to produce a similar purity (95%) carbon monoxide stream.
Any adsorbent which can selectively adsorb the secondary gas product from the first gas product can be used. The key adsorptive properties are (i) high selectivity, (ii) high working capacity, (iii) fast kinetics, and (iv) low heat of adsorption. Typical examples are zeolites, carbons, aluminas, or silica gels. Other desired properties of the adsorbents are (i) high crush strength, (ii) high attrition resistance, (iii) large bulk density, (iv) low interparticle void, (v) high heat capacity, (vi) large thermal conductivity, and (vii) small particle size. Pressure drop through the adsorbent beds during adsorption, purge, and evacuation steps are also important properties for adsorbent selection. Exemplary adsorbents for specific gas separations are 13X zeolite for CH.sub.4 /CO.sub.2 and N.sub.2 /CO.sub.2 separations; an activated carbon for H.sub.2 /CH.sub.4 separations; CaX zeolite for O.sub.2 /N.sub.2 separations; and 13X zeolite for H.sub.2 /CH.sub.4 /CO.sub.2 /N.sub.2 /CO separations wherein H.sub.2 is the first gas product containing an acceptable CH.sub.4 impurity and CO.sub.2 is the second gas product containing an acceptable CH.sub.4 impurity.
The present invention has been described with reference to two specific embodiments thereof. These embodiments should not be viewed as a limitation to the present invention, the scope of which should be ascertained by the following claims.
Claims
What is claimed is:
1. In a pressure swing adsorption process for the recovery of two gas products at high recovery and high purity from a feed gas stream containing said products wherein a first gas product is one or more, less strongly adsorbed components and a second gas product is one or more, more strongly adsorbed components, and wherein said process comprises the steps of: (a) introducing a feed gas stream at elevated pressure containing said one or more, less strongly adsorbed components and said one or more, more strongly adsorbed components into one of a plurality of parallel adsorptive beds filled with one or more adsorbents selective for said one or more, more strongly adsorbed components, so as to retain said one or more, more strongly adsorbed components on said one or more adsorbents and allow said one or more, less strongly adsorbed components to pass through said bed for recovery as said first gas product at high recovery and high purity; (b) terminating the introduction of said feed gas stream into said bed before said one or more, more strongly adsorbed components break through the downstream end of said bed and depressurizing said bed to approximately ambient pressure to remove said one or more, less strongly adsorbed components from said bed and recycling a portion of the resulting depressurization effluent to said feed gas stream; (c) evacuating said bed to a subambient pressure to recover said one or more, more strongly adsorbed components as said second gas product at high recovery and high purity; and (d) repressurizing said bed with one or more, less strongly adsorbed components to approximately the pressure of the feed gas stream, wherein the steps (a) through (d) are performed on said plurality of beds to result in a continuous process; the improvement to increase the energy efficiency of the process comprising a depressurization effluent repressurization step wherein said bed is partially repressurized after step (c) and prior to step (d) with a last portion of the depressurization effluent from one of said parallel beds presently undergoing step (b).
2. The process of claim 1 wherein the process further comprises a low pressure purge step after step (b) and prior to step (c) wherein a low pressure purge gas stream of one or more, more strongly adsorbed components is passed through said bed to remove any residual one or more, less strongly adsorbed components from said bed.
3. The process of claim 1 wherein the elevated pressure of said feed gas stream is in the range of approximately 30 to 500 psia.
4. The process of claim 1 wherein the depressurization is conducted down to a pressure of approximately 15 psia.
5. The process of claim 1 wherein the evacuation is conducted down to a pressure in the range of approximately 40 to 200 torr.
6. The process of claim 1 wherein said less strongly adsorbed components and said more strongly adsorbed components are selected from the group consisting of hydrogen, oxygen, carbon dioxide, nitrogen, carbon monoxide, methane, and other hydrocarbons.
7. The process of claim 1 wherein the adsorbent is selected from the group consisting of zeolites, carbons, aluminas and silica gels.
8. The process of claim 1 wherein the feed gas temperature is in the range of approximately 0.degree. to 3OO.degree. F.
Patent Citations (16)
| Patent | Date | Inventor | Cited By |
|---|---|---|---|
| USRe31014 | 1982-08-01 | Sircar | |
| US3085379 | 1963-04-01 | Kiyonaga et al. | |
| US3788037 | 1974-01-01 | Shell et al. | |
| US4171207 | 1979-10-01 | Sircar | |
| US4566881 | 1986-01-01 | Richter et al. | |
| US4599094 | 1986-07-01 | Werner et al. | |
| US4705541 | 1987-11-01 | Sircar | |
| US4775394 | 1988-10-01 | Yamano et al. | |
| US4790858 | 1988-12-01 | Sircar | |
| US4913709 | 1990-04-01 | Kumar | |
| US4914218 | 1990-04-01 | Kumar et al. | |
| US4915711 | 1990-04-01 | Kumar | |
| US4986835 | 1991-01-01 | Uno et al. | |
| US5026406 | 1991-06-01 | Kumar | |
| US5084075 | 1992-01-01 | Sircar | |
| US5133785 | 1992-07-01 | Kumar et al. |