CN116785897A - Gas separation device - Google Patents
Gas separation device Download PDFInfo
- Publication number
- CN116785897A CN116785897A CN202310143289.1A CN202310143289A CN116785897A CN 116785897 A CN116785897 A CN 116785897A CN 202310143289 A CN202310143289 A CN 202310143289A CN 116785897 A CN116785897 A CN 116785897A
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- Prior art keywords
- separation
- gas
- separation module
- recovering
- module
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- 238000000926 separation method Methods 0.000 title claims abstract description 148
- 238000011084 recovery Methods 0.000 claims abstract description 60
- 239000012466 permeate Substances 0.000 claims abstract description 43
- 239000012528 membrane Substances 0.000 claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 118
- 239000001569 carbon dioxide Substances 0.000 claims description 59
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 59
- 239000007789 gas Substances 0.000 description 79
- 238000010586 diagram Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000004205 dimethyl polysiloxane Substances 0.000 description 2
- 229920000435 poly(dimethylsiloxane) Polymers 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- -1 Polydimethylsiloxane Polymers 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000035699 permeability Effects 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
- B01D53/22—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 diffusion
- B01D53/228—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 diffusion characterised by specific membranes
-
- 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
- B01D53/22—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 diffusion
- B01D53/225—Multiple stage diffusion
- B01D53/226—Multiple stage diffusion in serial connexion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides a gas separation device (10), comprising: a first separation module (1 a) and a second separation module (1 b) each having a separation membrane (M) that selectively permeates a specific gas component, the first separation module (1 a) recovering the specific gas component at a first recovery rate, the second separation module (1 b) recovering the specific gas component at a second recovery rate lower than the first recovery rate; a first supply line (L1 a) for supplying a raw material gas containing a specific gas component at a predetermined concentration or higher to the first separation module (1 a); second supply lines (L2 a, L1 b) for recovering the permeate gas having permeated through the separation membrane (M) from the first separation module (1 a) and supplying the permeate gas to the second separation module (1 b); and third supply lines (L3 b, L1 a) for recovering the permeate gas having permeated through the separation membrane (M) from the second separation module (1 b) and supplying the permeate gas to the first separation module (1 a).
Description
Technical Field
The present invention relates to a gas separation device for separating a specific component from a mixed gas.
Background
As such a device, there is knownUsing selective activation of carbon dioxide (CO) in air 2 ) Recovery of high concentration CO through separation membrane 2 Is disclosed (see patent document 1, for example). In the apparatus of patent document 1, a plurality of membrane separation modules are connected in series, and CO is performed in multiple stages 2 Is separated and recovered, thereby recovering CO with high concentration 2 。
However, if the separation and recovery are performed in multiple stages as in the apparatus of patent document 1, CO in the gas is supplied further to the rear stage 2 The lower the partial pressure, the lower the CO becomes the driving force for permeation 2 The lower the partial pressure difference, the more difficult it is to recover high concentration CO with less energy usage 2 。
Prior art literature
Patent literature
Patent document 1: japanese patent laid-open No. 2020-195968 (JP 2020-195968A).
Disclosure of Invention
A gas separation device according to an aspect of the present invention includes: a first separation module and a second separation module, each having a separation membrane selectively permeable to a specific gas component, the first separation module recovering the specific gas component at a first recovery rate, the second separation module recovering the specific gas component at a second recovery rate lower than the first recovery rate; a first supply line for supplying a raw material gas containing a specific gas component at a predetermined concentration or higher to the first separation module; a second supply line for recovering the permeate gas having permeated through the separation membrane from the first separation module and supplying the permeate gas to the second separation module; and a third supply line for recovering the permeate gas having permeated through the separation membrane from the second separation module and supplying the permeate gas to the first separation module.
Drawings
The objects, features and advantages of the present invention are further elucidated by the following description of embodiments in connection with the accompanying drawings.
Fig. 1 is a view for explaining a separation membrane used in a gas separation device according to an embodiment of the present invention.
FIG. 2 is a schematic diagram for explaining each initial CO 2 CO at a concentration of 2 Recovery ofA plot of the relationship between the rate and the separation recovery energy.
Fig. 3 is a block diagram schematically showing an example of the main part configuration of the gas separation device according to the embodiment of the present invention.
Fig. 4 is a block diagram schematically showing another example of the main part configuration of the gas separation device according to the embodiment of the present invention.
Detailed Description
Hereinafter, an embodiment of the present invention will be described with reference to fig. 1 to 4. The gas separation device according to the embodiment of the present invention separates and recovers a specific component from a mixed gas by using a separation membrane that selectively transmits the specific component in the mixed gas. In particular, the separation and recovery of a specific component at a high concentration. Next, the catalyst contains CO at a high concentration (for example, about 1 to 10 vol%) 2 CO is separated and recovered from raw material gases such as the atmosphere or the factory exhaust 2 Examples of (a) are described.
Fig. 1 is a diagram for explaining a separation membrane M used in a gas separation device according to an embodiment of the present invention. As shown in fig. 1, the separation membrane M is formed, for example, as a Polydimethylsiloxane (PDMS) film, and selectively contains nitrogen (N 2 ) Oxygen (O) 2 )、CO 2 CO in air, etc 2 And (3) transmitting. CO 2 Is permeated by CO at the supply side 2 Partial pressure and CO on the permeate side 2 The partial pressure difference of the partial pressure is a driving force until the partial pressure difference disappears.
FIG. 2 is a schematic diagram for explaining each initial CO 2 Concentration (supply side CO) 2 Concentration) of CO 2 And a graph of the relationship between recovery and separation recovery energy. CO 2 Recovery [%]As a CO relative to the feed gas 2 Quantity of ton-CO 2 /day]CO recovery of (c) 2 Quantity of ton-CO 2 /day]And (5) calculating.
As shown in FIG. 2, in the process of starting from the initial CO 2 CO is separated and recovered from raw material gas with relatively high concentration (for example, more than 10 percent) 2 In the case of (2), due to the supply side CO 2 The partial pressure is relatively high, so in order to increase CO 2 Recovery of separation recovery energy [ GJ/ton-CO ] for use in recovery 2 ]Become compared withFew. On the other hand, in the process of starting CO 2 CO is separated and recovered from raw material gas with relatively low concentration (for example, less than 10 percent) 2 In the case of (2), due to the supply side CO 2 The partial pressure is relatively low, so in order to increase CO 2 The recovery rate and the separation recovery energy used become extremely large.
When such separation and recovery are performed in multiple stages, the CO of the entire apparatus can be improved 2 Recovery rate, but the later, supply side CO 2 The lower the concentration, the more CO at the supply side 2 The lower the partial pressure, the greater the energy usage, and thus the greater the energy usage of the overall plant, as the recovery rate of the later stage is increased. Therefore, in the present embodiment, by performing the separation recovery in multiple stages and setting only the forefront stage to a high recovery rate, it is possible to recover CO at a high concentration with a small amount of energy usage 2 The gas separation device was constructed as follows.
Fig. 3 and 4 are block diagrams schematically showing an example of the main part configuration of the gas separation device 10 according to the embodiment of the present invention. As shown in fig. 3 and 4, the gas separation apparatus 10 includes a plurality of separation modules 1 (three separation modules 1a to 1c in the drawing), a supply line L1 (L1 a to L1 c), a recovery line L2 (L2 a to L2 c), and an exhaust line L3 (L3 a to L3 c) connected in series. The plurality of separation modules 1 may be configured by connecting a plurality of separation modules 1 arranged in parallel in series.
The separation module 1 is configured as a hollow membrane-like module, a spiral-type module, or the like using a separation membrane M (fig. 1). The internal space of the separation module 1 is partitioned into a first space on the supply side and a second space on the permeate side by a separation membrane M as a partition wall.
To separate and recycle CO in the exhaust gas 2 The separation module 1a of the foremost stage is constructed as CO with a sufficiently low concentration 2 The recovery rate is equal to or higher than a predetermined recovery rate (for example, 90% or higher). The separation modules 1b and 1c after the second stage are configured as CO in order to sufficiently reduce the energy usage amount of separation and recovery 2 The recovery rate is low (e.g., about 10%). By adjusting the membrane properties (gas permeability, CO) of the separation membrane M used in each separation module 1 2 Selectivity), membrane area, feed-side pressure, permeateThe CO of each separation module 1 can be obtained by the passing side pressure, the supply side flow rate (flow velocity), the permeation side flow rate, or the like 2 The recovery rate was set to an appropriate value.
The supply lines L1a to L1c supply the mixed gas to the first spaces of the separation modules 1a to 1c, respectively. The supply lines L1a to L1c may be provided with a compressor for pressurizing the supply gas, a regulating valve for regulating the supply-side flow rate, and the like.
The recovery lines L2a to L2c recover the permeate gas having permeated the separation membrane M from the second spaces of the separation modules 1a to 1c, respectively. The recovery lines L2a to L2c may be provided with a vacuum pump for depressurizing the second space of each of the separation modules 1a to 1c, an adjustment valve for adjusting the permeate-side flow rate, and the like. The final recovered gas separated and recovered by the gas separation device 10 is obtained from the recovery line L2c of the final stage.
The exhaust lines L3a to L3c separate CO from the first spaces of the separation modules 1a to 1c, respectively 2 And discharging the air after the process. The exhaust lines L3a to L3c may be provided with a vacuum pump, an adjustment valve for adjusting the flow rate of exhaust gas, and the like. The forefront exhaust line L3a is opened to the atmosphere, and CO having a sufficiently low concentration is discharged from the forefront separation module 1a set to a high recovery rate to the atmosphere 2 Is provided.
The supply line L1a constitutes a raw material supply line for supplying a raw material gas to the foremost separation module 1 a. The recovery line L2a and the supply line L1b constitute an intermediate supply line for recovering the permeate gas from the separation module 1a and supplying the permeate gas to the separation module 1b in the subsequent stage. The recovery line L2b and the supply line L1c constitute an intermediate supply line for recovering the permeate gas from the separation module 1b and supplying the permeate gas to the separation module 1c in the subsequent stage.
The exhaust line L3b and the supply line L1a constitute a return line for recovering the permeate gas from the separation module 1b and supplying the permeate gas to the separation module 1a in the preceding stage. In the example of fig. 3, the exhaust line L3c and the supply line L1b constitute a return line for recovering the permeate gas from the separation module 1c and supplying the permeate gas to the separation module 1b in the preceding stage. In the example of fig. 4, the exhaust line L3c and the supply line L1a constitute a return line for recovering the permeate gas from the separation module 1c and supplying the permeate gas to the forefront separation module 1 a.
Thus, by returning the recovered gas in the subsequent stage set to a low recovery rate to the stage preceding the gas recovery gas, the gas separation apparatus 10 as a whole can recover CO at a high concentration with a small amount of energy 2 (FIGS. 3 and 4). In addition, when the recovered gas in the latter stage is returned to the forefront stage, the energy consumption in the forefront stage can be further reduced, and the gas separation device 10 as a whole can recover CO of high concentration with a smaller energy consumption 2 (FIG. 4).
The present embodiment can provide the following effects.
(1) The gas separation device 10 includes: a foremost separation module 1a and a later separation module 1b, which have a function of selectively separating CO 2 A separation membrane M which permeates therethrough, and the separation module 1a recovers CO at a high recovery rate 2 The separation module 1b recovers CO at a low recovery rate 2 The method comprises the steps of carrying out a first treatment on the surface of the A raw material supply line (supply line L1 a) containing CO at a predetermined concentration or higher 2 Is supplied to the foremost separation module 1a; an intermediate supply line (recovery line L2a and supply line L1 b) for recovering the permeate gas from the foremost separation module 1a and supplying the permeate gas to the later separation module 1b; and return lines (an exhaust line L3b and a supply line L1 a) for recovering the permeate gas from the separation module 1b at the rear stage and supplying the permeate gas to the separation module 1a at the forefront stage (fig. 3 and 4). By setting the separation module 1a in the foremost stage to have a high recovery rate and setting the separation module 1b in the latter stage to have a low recovery rate in this way, the recovered gas in the latter stage is returned to the foremost stage having a high recovery rate, and thus the entire gas separation apparatus 10 can recover CO in a high concentration with a small amount of energy 2 。
(2) The gas separation apparatus 10 further includes: a separation module 1c having a separation membrane M for recovering CO at a low recovery rate 2 The method comprises the steps of carrying out a first treatment on the surface of the An intermediate supply line (recovery line L2b and supply line L1 c) for recovering the permeate gas from the separation module 1b in the preceding stage and supplying the permeate gas to the separation module 1c in the subsequent stage; and a return line (exhaust line L3c and supply line L1a or exhaust line L3c and supply line L1 b) for recovering the permeate gas from the downstream separation module 1c and supplying the permeate gas to the forefront separation module 1a or the forefront separation module 1b (fig. 3 and 4).By setting the recovery rate of the separation modules 1b to 1c at the subsequent stage to be low in this way, the recovery gas at the subsequent stage is returned to the stage preceding the recovery gas, and thus the gas separation apparatus 10 as a whole can recover CO at a higher concentration with a smaller amount of energy 2 。
(3) The return lines (exhaust line L3c and supply line L1 a) collect the permeate gas from the separation module 1c in the subsequent stage and supply the permeate gas to the separation module 1a in the forefront stage (fig. 4). By setting the recovery rate of the separation module 1c in the subsequent stage to be low in this way, the recovery gas in the subsequent stage is returned to the forefront stage, and the energy consumption in the forefront stage can be further reduced, so that the gas separation apparatus 10 as a whole can recover CO of high concentration with a smaller energy consumption 2 。
(4) The raw material gas is the atmosphere or the factory exhaust. In the presence of CO at high concentration 2 In the forefront stage using the atmosphere or the factory exhaust gas as the raw material gas, CO can be recovered with high recovery rate even with a small energy consumption 2 (FIG. 2), the gas separation device 10 as a whole is therefore capable of recovering high concentrations of CO with reduced energy usage 2 。
In the above embodiment, the separation of CO is performed using FIG. 1 or the like 2 Although the above-described examples have been described, the specific components to be separated by the gas separation apparatus are not limited thereto. The gas separation device can be preferably applied to separation of CO in plant exhaust gas 2 And the like, in the case of separating a specific component at a high concentration.
One or more of the above embodiments and modifications may be arbitrarily combined, or the modifications may be combined with each other.
The invention can recycle high-concentration CO with less energy consumption 2 。
While the invention has been described in connection with preferred embodiments, it will be understood by those skilled in the art that various modifications and changes can be made without departing from the scope of the disclosure of the following claims.
Claims (6)
1. A gas separation device (10) is characterized by comprising:
a first separation module (1 a) and a second separation module (1 b) each having a separation membrane (M) selectively permeable to a specific gas component, the first separation module (1 a) recovering the specific gas component at a first recovery rate, the second separation module (1 b) recovering the specific gas component at a second recovery rate lower than the first recovery rate;
a first supply line (L1 a) for supplying a raw material gas containing the specific gas component at a predetermined concentration or higher to the first separation module (1 a);
a second supply line (L2 a, L1 b) for recovering the permeate gas having permeated through the separation membrane (M) from the first separation module (1 a) and supplying the permeate gas to the second separation module (1 b); and
and third supply lines (L3 b, L1 a) for recovering the permeate gas having permeated through the separation membrane (M) from the second separation module (1 b) and supplying the permeate gas to the first separation module (1 a).
2. The gas separation device (10) according to claim 1, further comprising:
a third separation module (1 c) having the separation membrane (M) for recovering the specific gas component at a third recovery rate lower than the first recovery rate;
fourth supply lines (L2 b, L1 c) for recovering the permeate gas having permeated through the separation membrane (M) from the second separation module (1 b) and supplying the permeate gas to the third separation module (1 c); and
and a fifth supply line (L3 c, L1a, or L3c, L1 b) for recovering the permeate gas that has permeated through the separation membrane (M) from the third separation module (1 c) and supplying the permeate gas to the first separation module (1 a) or the second separation module (1 b).
3. The gas separation device (10) according to claim 2, wherein,
the fifth supply lines (L3 c, L1 a) collect the permeate gas having permeated through the separation membrane (M) from the third separation module (1 c) and supply the permeate gas to the first separation module (1 a).
4. A gas separation device (10) according to any one of claims 1 to 3, characterized in that,
the specific gas component is carbon dioxide,
the raw material gas is the atmosphere or factory exhaust.
5. The gas separation device (10) according to claim 4, wherein,
the predetermined concentration is about 1 vol%.
6. The gas separation device (10) according to any one of claims 1 to 3, 5, characterized in that,
the first recovery rate is more than 90 percent,
the second recovery rate was 10%.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2022045994A JP2023140120A (en) | 2022-03-22 | 2022-03-22 | Gas separator |
| JP2022-045994 | 2022-03-22 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116785897A true CN116785897A (en) | 2023-09-22 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310143289.1A Pending CN116785897A (en) | 2022-03-22 | 2023-02-20 | Gas separation device |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP2023140120A (en) |
| CN (1) | CN116785897A (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020203994A1 (en) * | 2019-03-29 | 2020-10-08 | 宇部興産株式会社 | Gas separation system |
| US11285434B2 (en) * | 2020-03-30 | 2022-03-29 | Air Products And Chemicals, Inc. | Membrane process and system for high recovery of a nonpermeating gas |
-
2022
- 2022-03-22 JP JP2022045994A patent/JP2023140120A/en active Pending
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2023
- 2023-02-20 CN CN202310143289.1A patent/CN116785897A/en active Pending
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| Publication number | Publication date |
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| JP2023140120A (en) | 2023-10-04 |
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