CN113491929B - Strengthening process for capturing carbon dioxide in flue gas by membrane separation method - Google Patents
Strengthening process for capturing carbon dioxide in flue gas by membrane separation method Download PDFInfo
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- CN113491929B CN113491929B CN202010269990.4A CN202010269990A CN113491929B CN 113491929 B CN113491929 B CN 113491929B CN 202010269990 A CN202010269990 A CN 202010269990A CN 113491929 B CN113491929 B CN 113491929B
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- 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
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The invention belongs to the technical field of gas separation, and relates to a strengthening process for capturing carbon dioxide in flue gas by a membrane separation method. The method provided by the invention can obviously improve the separation performance of the membrane separator, simultaneously fully utilizes the water separated out in the process of compressing the feed gas, reduces the wastewater discharge of the process, reduces the condensation load of the compressor, and has good application prospect in the field of carbon dioxide capture.
Description
Technical Field
The invention belongs to the technical field of gas separation, and particularly relates to a strengthening process for capturing carbon dioxide in flue gas by a membrane separation method.
Background
Greenhouse gases represented by carbon dioxide cause great damage to the stability of the earth ecosystem, and become a serious environmental problem to be solved urgently. Greenhouse gas emission reduction can be achieved mainly through three ways: firstly, the energy efficiency is improved, and the emission of carbon dioxide is reduced; secondly, changing the energy structure and increasing the proportion of clean energy in the total energy; and thirdly, the discharged carbon dioxide is collected, recycled and sealed (CCUS).
The proportion is low in view of the technical and economic limits existing in the short term of the scale application of the clean energy. The position of fossil fuels is still irreplaceable in the coming decades. Carbon dioxide discharged by fossil combustion accounts for about 80% of total emission, wherein flue gas is a long-term stable centralized emission source of carbon dioxide, and the amount of discharged carbon dioxide accounts for nearly one third of the total emission. Therefore, the capture of carbon dioxide in flue gases has received a great deal of attention.
The carbon dioxide capture technology mainly comprises an absorption separation method, an adsorption separation method, a low-temperature distillation method, chemical cycle combustion, a membrane separation method, hydrates and the like. The membrane separation method is a novel carbon dioxide capture technology, has the advantages of mild operation conditions, easiness in amplification, environmental friendliness, small occupied area and the like, and has become a hotspot of the carbon dioxide capture technology.
Due to the low partial pressure of carbon dioxide in flue gas, it is pressurized first to separate it using membrane separation techniques. However, the conventional membrane material has poor separation performance for carbon dioxide, and cannot meet the requirement of carbon capture in industry. The promotion transfer membrane adds some carriers capable of generating reversible reaction with the separation gas into the original membrane, and the carrier is used for transporting the gas to be separated, so that the permeability of the gas can be obviously improved, and the promotion transfer membrane becomes the latest research direction in the research field of carbon dioxide membrane separation materials in flue gas. Three factors are main obstacles for promoting the transfer membrane to capture the carbon dioxide in the flue gas, which restrict the industrial application of the transfer membrane.
Firstly, because the reversible reaction of carbon dioxide and a carrier needs the participation of water, the technology for capturing carbon dioxide in flue gas by a membrane separation method generally has certain requirements on the humidity of raw material gas, but the water cannot achieve good distribution in a membrane component and gases at two sides of a membrane under the influence of the gradient distribution of the separation concentration of the carbon dioxide, particularly, the technology for capturing carbon dioxide in flue gas by membrane separation usually needs a multi-stage membrane separation process to achieve the purity of carbon dioxide products which is industrially required due to the limitation of single-stage membrane separation performance, and at the moment, the gas at the interception side is often required to be circulated in order to ensure the recovery rate of the process, so that the water distribution in each stage of membrane separation reactors is seriously uneven, and the membrane separation performance is reduced.
Second, as a reversible chemical reaction, temperature has a significant effect on the direction in which the reaction proceeds. However, in the current technology for capturing carbon dioxide in flue gas by using a membrane separation method, only the temperature of raw material gas and the heat preservation of a membrane separation reactor are considered, a temperature gradient favorable for reversible reaction cannot be formed on two sides of a membrane, and even for some membrane separation reactors with poor heat preservation conditions, the distribution of the temperature gradient can hinder the effective separation of carbon dioxide from flue gas.
Thirdly, in the technology of capturing carbon dioxide in flue gas by membrane separation, the carbon dioxide molecules have a large molecular weight and the permeation side pressure is often low, so that the permeated carbon dioxide molecules are easy to gather at the permeation side to form a high-concentration carbon dioxide region, the resistance of carbon dioxide passing through a membrane interface is increased, and the membrane separation effect of carbon dioxide is reduced.
Therefore, the invention develops a strengthening process aiming at the process of capturing the carbon dioxide in the flue gas by the membrane separation method from the perspective of constructing the reasonable humidity, temperature and concentration gradient in the membrane separation process, can improve the performance of the process of capturing the carbon dioxide in the flue gas by the current membrane separation method, and has wide application prospect.
Disclosure of Invention
The invention aims to provide an enhanced process for capturing carbon dioxide in flue gas by a membrane separation method, which is different from the traditional membrane separation process, and reasonable humidity, temperature and concentration gradient distribution is constructed in a membrane separation reactor through organic combination of drainage, flash evaporation and condensation of a compressor.
A strengthening process for capturing carbon dioxide in flue gas by a membrane separation method comprises the following process flows: the compressed raw material flue gas enters a membrane separator, gas containing carbon dioxide with different concentrations is obtained at a permeation side and a interception side respectively, water flash evaporation generated in the flue gas compression process is separated to generate vapor which is sent to the permeation side of the membrane separator and used for maintaining the humidity and temperature distribution of two sides of the membrane, the carbon dioxide concentration of the permeation side is reduced, the flash evaporation vapor is led out of the membrane separator along with the permeation gas and condensed, and condensate is pressurized and then sprayed to the interception side of the membrane separator.
The strengthening process for capturing the carbon dioxide in the smoke by the membrane separation method provided by the invention has the advantages that the used membrane separation process needs to compress the smoke, and the compression pressure is 0.3-1MPa.
The invention provides a strengthening process for capturing carbon dioxide in flue gas by a membrane separation method.
The invention provides a strengthening process for capturing carbon dioxide in smoke by a membrane separation method, wherein the membrane separation process is a multistage membrane separation process with the progression of 2 to 5.
The strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the advantages that the carbon dioxide concentrated gas obtained at the permeation side can be used as raw material gas to be compressed and enter the next-stage membrane separator except the last stage.
The strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the advantages that carbon dioxide degassing gas obtained at the interception side can be emptied or partially returned to the membrane separator before the stage according to the requirement of the recovery rate.
The strengthening process for capturing the carbon dioxide in the smoke by the membrane separation method provided by the invention has the advantage that the flash evaporation pressure of the water precipitated in the smoke compression process is 0-0.3 MPa.
The strengthening process for capturing the carbon dioxide in the smoke by the membrane separation method provided by the invention has the advantage that the flash evaporation temperature of water separated out in the smoke compression process is 40-120 ℃.
The strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the advantage that the condensation temperature of the permeating gas out of the membrane separator is 20-50 ℃.
The strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the advantage that the pressurizing pressure of the condensate of the permeation gas of the membrane separator is 0.3-2MPa.
The strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the advantages that the flashed water vapor and the pressurized permeation gas condensate can be respectively sent to the permeation side and the interception side of the membrane separator of the stage, and can also be sent to the permeation side and the interception side of other stages of membrane separators.
The pressurizing regeneration process for capturing the carbon dioxide in the flue gas by the alcohol amine method is suitable for raw material gases of power plants, chemical plants and iron and steel plants.
The pressurized regeneration process for capturing the carbon dioxide in the flue gas by the alcohol amine method is suitable for 5-50% of the carbon dioxide content in the raw material gas.
Compared with the common process for capturing the carbon dioxide in the flue gas by the membrane separation method, the strengthening process for capturing the carbon dioxide in the flue gas by the membrane separation method provided by the invention has the following advantages:
(1) The temperature, the humidity and the concentration gradient suitable for carbon dioxide separation are established in the membrane separator, so that the membrane separation performance of the carbon dioxide is improved;
(2) The water separated out in the compression process of the raw material gas is fully utilized, and the wastewater discharge of the process is reduced;
(3) The water separated out by the compressor does not need to be cooled, and the load of the condenser of the compressor is reduced.
Drawings
FIG. 1 is a process flow diagram of a certain stage of membrane separation in an embodiment of the present invention.
1-compressor, 2-flash tank, 3-membrane separator, 4-permeation gas heat exchanger, 5-separator and 6-booster pump.
Detailed Description
The invention is further illustrated by the following examples and figures.
Example 1
The method of the embodiment has the following steps:
(1) The device shown in the attached figure 1 is used for carrying out a single-stage separation performance evaluation test of the facilitated transfer membrane, feed gas is compressed by a compressor and then enters a membrane separator, part of components penetrate through the membrane and are taken as permeating gas to be led out of the membrane separator, and the components which do not penetrate through the membrane and are taken as trapped gas to be led out of the membrane separator.
(2) The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is 0.12MPa, the water content is saturated, and the dry basis content is CO 2 10% by v, O 2 10% by v, N 2 80v% was obtained.
(3) Without process strengthening, the compressor discharge pressure is 0.4MPa, and CO in the permeating gas is measured 2 The content was 17%.
(4) Using the strengthening process, discharging water from a compressor, introducing the discharged water into a flash tank, introducing flash steam with the pressure of 0.2MPa and the temperature of 80 ℃ into the permeation side of the membrane separator of the stage, condensing the permeation gas at the temperature of 40 ℃, pressurizing the condensate to 0.45MPa, introducing the condensate into the interception side of the membrane separator of the stage, and measuring the CO in the permeation gas 2 The content is 22%.
Example 2
The method of the embodiment has the following steps:
(1) The device shown in the attached figure 1 is used for carrying out a single-stage separation performance evaluation test of the facilitated transfer membrane, feed gas is compressed by a compressor and then enters a membrane separator, part of components penetrate through the membrane and are taken as permeating gas to be led out of the membrane separator, and the components which do not penetrate through the membrane and are taken as trapped gas to be led out of the membrane separator.
(2) The raw material gas is simulated flue gas, the temperature is 20 ℃, the pressure is 0.15MPa, the water content is saturated, and the dry basis content is CO 2 15% by v, O 2 5% by v, N 2 The concentration was 80v%.
(3) Without process enhancement, the exhaust pressure of the compressor is 0.6MPa, and CO in the permeation gas is measured 2 The content is 23%.
(4) Using the strengthening process, discharging water from a compressor, introducing the discharged water into a flash tank, introducing flash steam with the pressure of 0.11MPa and the temperature of 70 ℃ into the permeation side of the membrane separator of the stage, condensing the permeation gas at the temperature of 30 ℃, pressurizing the condensate to 0.65MPa, introducing the condensate into the interception side of the membrane separator of the stage, and measuring the CO in the permeation gas 2 The content is 36%.
Example 3
The method of the embodiment has the following steps:
(1) The device shown in figure 1 is used for evaluating the performance of promoting the two-stage separation of the transfer membrane, the raw material gas is compressed by a first-stage compressor and then enters a first-stage membrane separator, the first-stage permeating gas is compressed by a second-stage compressor and then enters a second-stage membrane separator, the first-stage trapped gas is directly discharged, the second-stage trapped gas returns to the first-stage membrane separator, and the second-stage permeating gas is used as CO product 2 And (5) leading out.
(2) The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is 0.15MPa, the water content is saturated, and the dry basis content is CO 2 12% by v, O 2 8% by v, N 2 80v% was obtained.
(3) Without process strengthening, the exhaust pressure of the first-stage compressor is 0.4MPa, the exhaust pressure of the second-stage compressor is 0.45MPa, and the CO in the secondary permeation gas is measured 2 The content was 61%.
(4) Using a strengthening process, draining water from a primary compressor, feeding the primary flash steam with the pressure of 0.15MPa and the temperature of 75 ℃ into a permeation side of a primary membrane separator, condensing the primary permeating gas at the temperature of 40 ℃, pressurizing condensate to 0.45MPa, feeding the condensate into a rejection side of the primary membrane separator, discharging water from a secondary compressor, feeding the secondary flash steam with the pressure of 0.2MPa and the temperature of 80 ℃ into a permeation side of a secondary membrane separator, condensing the secondary permeating gas at the temperature of 40 ℃, pressurizing the condensate to 0.48MPa, feeding the condensate into the rejection side of the secondary membrane separator, and measuring CO in the secondary permeating gas 2 The content is 85%.
Example 4
The method of the embodiment has the following steps:
(1) The device shown in figure 1 is used for evaluating the performance of promoting the two-stage separation of the transfer membrane, the raw material gas is compressed by a first-stage compressor and then enters a first-stage membrane separator, the first-stage permeating gas is compressed by a second-stage compressor and then enters a second-stage membrane separator, the first-stage trapped gas is directly discharged, the second-stage trapped gas returns to the first-stage membrane separator, and the second-stage permeating gas is used as CO product 2 And (5) leading out.
(2) The raw material gas is simulated flue gas, the temperature is 60 ℃, the pressure is 0.2MPa, the water content is saturated, and the dry basis content is CO 2 7% by v, O 2 13v% of N 2 80v% was obtained.
(3) Without process reinforcement, the exhaust pressure of the first-stage compressor is 0.5MPa, the exhaust pressure of the second-stage compressor is 0.55MPa, and CO in the second-stage permeation gas is measured 2 The content was 55%.
(4) Using a strengthening process, draining water from a primary compressor, feeding the primary flash steam with the pressure of 0.18MPa and the temperature of 78 ℃ into a permeation side of a primary membrane separator, condensing the primary permeating gas at the temperature of 45 ℃, pressurizing condensate to 0.55MPa, feeding the condensate into a rejection side of the primary membrane separator, discharging water from a secondary compressor, feeding the secondary flash steam with the pressure of 0.15MPa and the temperature of 75 ℃ into a permeation side of a secondary membrane separator, condensing the secondary permeating gas at the temperature of 40 ℃, pressurizing the condensate to 0.58MPa, feeding the condensate into the rejection side of the secondary membrane separator, and measuring CO in the secondary permeating gas 2 The content was 87%.
Example 5
The method of the embodiment has the following steps:
(1) The device shown in figure 1 is used for carrying out the evaluation test of the three-stage separation performance of the promotion transfer membrane, the raw material gas is compressed by a first-stage compressor and then enters a first-stage membrane separator, first-stage permeation gas is compressed by a second-stage compressor and then enters a second-stage membrane separator, first-stage trapped gas is directly discharged, second-stage trapped gas returns to the first-stage membrane separator, second-stage permeation gas is compressed by the third-stage compressor and then enters the third-stage membrane separator, third-stage trapped gas returns to the second-stage membrane separator, and third-stage permeation gas is used as product CO 2 And (5) leading out.
(2) The raw material gas is simulated flue gas, the temperature is 55 ℃, the pressure is 0.14MPa, the water content is saturated, and the dry basis content is CO 2 6% by v, O 2 14v% of N 2 The concentration was 80v%.
(3) Without process reinforcement, the exhaust pressure of the first-stage compressor is 0.35MPa, the exhaust pressure of the second-stage compressor is 0.4MPa, the exhaust pressure of the third-stage compressor is 0.45MPa, and CO in the third-stage permeation gas is measured 2 The content was 82%.
(4) Using the strengthening process, the water discharged by the primary compressor enters a primary flash tank, primary flash steam with the pressure of 0.15MPa and the temperature of 85 ℃ enters the permeation side of the primary membrane separator, and the condensation temperature of the primary permeation steam is 40Pressurizing the condensate to 0.38MPa, allowing the condensate to enter the interception side of a primary membrane separator, allowing the discharged water of a secondary compressor to enter a secondary flash tank, allowing secondary flash steam with the pressure of 0.18MPa and the temperature of 77 ℃ to enter the permeation side of the secondary membrane separator, allowing secondary permeating gas to condense at 45 ℃, pressurizing the condensate to 0.43MPa, allowing the condensate to enter the interception side of the secondary membrane separator, allowing the discharged water of a tertiary compressor to enter a tertiary flash tank, allowing tertiary flash steam with the pressure of 0.2MPa and the temperature of 82 ℃ to enter the permeation side of the tertiary membrane separator, allowing tertiary permeating gas to condense at 40 ℃, allowing the condensate to pressurize to 0.48MPa, allowing the condensate to enter the interception side of the secondary membrane separator, and measuring CO in the tertiary permeating gas 2 The content was 93%.
Example 6
The method of the embodiment has the following steps:
(1) The device shown in figure 1 is used for carrying out the evaluation test of the three-stage separation performance of the promotion transfer membrane, the raw material gas is compressed by a first-stage compressor and then enters a first-stage membrane separator, first-stage permeation gas is compressed by a second-stage compressor and then enters a second-stage membrane separator, first-stage trapped gas is directly discharged, second-stage trapped gas returns to the first-stage membrane separator, second-stage permeation gas is compressed by the third-stage compressor and then enters the third-stage membrane separator, third-stage trapped gas returns to the second-stage membrane separator, and third-stage permeation gas is used as product CO 2 And (5) leading out.
(2) The raw material gas is simulated flue gas, the temperature is 60 ℃, the pressure is 0.16MPa, the moisture is saturated, and the dry basis content is CO 2 15% by v, O 2 5% by v, N 2 80v% was obtained.
(3) Without process reinforcement, the exhaust pressure of the first-stage compressor is 0.4MPa, the exhaust pressure of the second-stage compressor is 0.45MPa, the exhaust pressure of the third-stage compressor is 0.5MPa, and CO in the third-stage permeation gas is measured 2 The content was 84%.
(4) Using the strengthening process, the water discharged by a primary compressor enters a primary flash tank, primary flash steam with the pressure of 0.2MPa and the temperature of 94 ℃ enters the permeation side of a primary membrane separator, the condensation temperature of the primary permeation steam is 40 ℃, condensate is pressurized to 0.43MPa and enters the interception side of the primary membrane separator, the water discharged by a secondary compressor enters a secondary flash tank, secondary flash steam with the pressure of 0.15MPa and the temperature of 84 ℃ enters the permeation side of a secondary membrane separator, and the condensation temperature of the secondary permeation steam is 4Pressurizing the condensate to 0.48MPa at 0 ℃, introducing the condensate into the interception side of a secondary membrane separator, introducing the drain water of a tertiary compressor into a tertiary flash tank, introducing the tertiary flash steam with the pressure of 0.15MPa and the temperature of 87 ℃ into the permeation side of the tertiary membrane separator, and measuring CO in the tertiary permeate gas 2 The content was 97%.
Example 7
The method of the embodiment has the following steps:
(1) The device shown in figure 1 is used for carrying out the evaluation test of the three-stage separation performance of the transfer-promoting membrane, raw gas is compressed by a first-stage compressor and then enters a first-stage membrane separator, first-stage permeation gas is compressed by a second-stage compressor and then enters a second-stage membrane separator, first-stage trapped gas is directly discharged, second-stage trapped gas returns to the first-stage membrane separator, second-stage permeation gas is compressed by the third-stage compressor and then enters a third-stage membrane separator, third-stage trapped gas returns to the first-stage membrane separator, and third-stage permeation gas is taken as a product CO (carbon monoxide) 2 And (5) leading out.
(2) The raw material gas is simulated flue gas, the temperature is 60 ℃, the pressure is 0.16MPa, the moisture is saturated, and the dry basis content is CO 2 10% by v, O 2 10% by v, N 2 80v% was obtained.
(3) Without process enhancement, the exhaust pressure of the first-stage compressor is 0.3MPa, the exhaust pressure of the second-stage compressor is 0.35MPa, the exhaust pressure of the third-stage compressor is 0.4MPa, and CO in the third-stage permeation gas is measured 2 The content is 85%.
(4) Using a strengthening process, draining water from a primary compressor, allowing primary flash steam with the pressure of 0.12MPa and the temperature of 84 ℃ to enter the permeation side of a primary membrane separator, condensing the primary permeating steam at the temperature of 40 ℃, pressurizing condensate to 0.33MPa, allowing the condensate to enter the interception side of the primary membrane separator, draining water from a secondary compressor, allowing secondary flash steam with the pressure of 0.12MPa and the temperature of 88 ℃ to enter the permeation side of a secondary membrane separator, condensing the secondary permeating steam at the temperature of 40 ℃, pressurizing condensate to 0.38MPa, allowing the condensate to enter the interception side of the secondary membrane separator, draining water from a tertiary compressor, allowing tertiary flash steam with the pressure of 0.12MPa and the temperature of 92 ℃ to enter the permeation side of the primary membrane separator, and measuring CO in the tertiary permeating steam 2 The content was 95%.
Claims (5)
1. An enhancement process for capturing carbon dioxide in flue gas by a membrane separation method is characterized in that: in one stage of the multi-stage membrane separator, compressed raw material flue gas enters the membrane separator, gas containing carbon dioxide with different concentrations is obtained on a permeation side and an interception side respectively, water separated out in the flue gas compression process is subjected to flash evaporation to generate water vapor which is sent to the permeation side of the membrane separator and used for maintaining the humidity and temperature distribution on two sides of the membrane on one hand and reducing the carbon dioxide concentration on the permeation side on the other hand, the flash evaporation vapor is led out of the membrane separator along with the permeation gas and is condensed, and condensed fluid is pressurized and then sprayed to the interception side of the membrane separator; the water vapor flashed out and the pressurized permeate gas condensate are respectively sent to the permeation side and the interception side of the membrane separator of the stage, or sent to the permeation side and the interception side of other membrane separators of the stage; wherein the condensation temperature of the permeation gas of the membrane separator is 20-50 ℃, and the pressurization pressure of the permeation gas condensate is 0.3-2 MPa; the pressure of flue gas compression is 0.3-1 MPa, the flash evaporation pressure of water separated out in the flue gas compression process is 0-0.3 MPa, and the flash evaporation temperature is 40-120 ℃; the membrane used is a transfer-promoting membrane, and the separation of carbon dioxide is realized by utilizing the reversible reaction of carbon dioxide and carriers in the membrane.
2. The strengthening process as claimed in claim 1, wherein the number of stages of the multi-stage membrane separator is 2-5.
3. The strengthening process of claim 1, wherein the carbon dioxide enriched gas obtained from the permeation side except the last stage is compressed as a raw material gas to enter the next stage membrane separator.
4. The process of claim 1 wherein the carbon dioxide stripping gas from the reject side is vented or partially returned to the membrane separator prior to this stage as required for recovery.
5. The strengthening process of claim 1, wherein the raw material gas is selected from the group consisting of power plant flue gas, chemical plant flue gas, and steel plant flue gas; the content of carbon dioxide in the applicable feed gas is 5% -50%.
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| JP2017154120A (en) * | 2016-03-04 | 2017-09-07 | 東京瓦斯株式会社 | Carbon dioxide separation system and fuel cell system |
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